Influence of Basic/Acidic Treatment on *BEA Zeolite and WO₃ Impregnation in Alcohol Dehydration Reactions

Abstract

This study investigated the hierarchical structuring of *BEA zeolite using 0.2 M sodium hydroxide followed by 0.5 M hydrochloric acid (T-NaOH-HCl). Tungsten trioxide (WO₃) was then impregnated at different loadings (5, 10, 15, and 20 wt.%) onto the hierarchized materials (BEA-T). The modified zeolites were subsequently used as catalysts for the dehydration of ethanol (230 and 250 °C) and 1-propanol (230 °C). The hierarchization treatment increased the Si/Al ratio (from 13 to 39), decreased relative crystallinity by 15%, and reduced the average crystal-domain size (from 18 to 10 nm). After the NaOH–HCl treatment (BEA-T), the mesopore area increased by 7%, the mesopore volume by 19%, and the total pore volume by 12%. Conversely, the BET specific surface area and micropore volume decreased, indicating effective hierarchization of the *BEA zeolite. XRD, FT-IR and Raman confirmed the presence of monoclinic WO₃ on the BEA-T surface. MAS NMR analyses of ²⁷Al and ²⁹Si indicated that the T-NaOH-HCl treatment slightly increased the population of tetrahedral Al environments. The high conversion and selectivity from the dehydration of ethanol and 1-propanol can be attributed to a moderate reduction in the acidity of *BEA zeolite and tunned mesoporosity. Based on TON, catalysts with 10% and 20% WO₃ stood out in dehydration tests.

1. Introduction

The year 2023 was marked by record levels of production and consumption following the COVID-19 pandemic. Crude oil consumption, for example, surpassed 100 million barrels per day for the first time in history, and the use of gasoline, diesel, and jet fuel also returned to 2019 levels and has continued to grow [1]. Due to the current high demand, refineries have sought to maximize chemical yields while minimizing energy consumption. Zeolites such as USY and ZSM-5 are widely used in catalytic cracking processes, which makes studies focused on enhancing the performance and selectivity of these materials of great industrial interest [2]. The *BEA zeolite, first synthesized in 1967 by the Mobil Oil Corporation, possesses wide pores, a high silica content, and acts as an adsorbent with high catalytic activity [3]. It has a three-dimensional framework composed of intersecting channels and large micropores (0.55 × 0.55 nm along the [001] plane and 0.66 × 0.67 nm along the [100] plane), formed by 12-membered rings and typically exhibiting a Si/Al ratio between 12 and 30 [4]. This zeolite may display intergrowth of several distinct but closely related polymorphs, including the chiral polymorph A and the achiral polymorphs B and C [5].

One of the current challenges in zeolite research involves the development of materials with hierarchical pore structures, which can combine the intrinsic catalytic properties of microporous zeolites with improved molecular access and transport through secondary meso- and macropores [6,7,8]. Post-synthesis routes used to prepare hierarchical zeolites often involve demetallation or delamination through acid, alkaline, or fluoride leaching, offering high versatility, low cost, good pore connectivity, and potential scalability [9]. Chemical leaching can induce dealumination or desilication by selectively removing framework aluminum or silicon atoms from the zeolite structure, thereby generating secondary intracrystalline mesopores and amorphous regions within the crystalline framework [10]. The use of base and acid leaching as a post-synthetic modification can preserve crystallinity, allowing better access to micropores. Groen et al. [11] showed that successive steam and alkaline treatment on ZSM-5 resulted in a limited mesoporosity development (80 m² g⁻¹) and a limited Si extraction. An alkaline treatment (0.2 M NaOH aqueous solution) of HBEA [6] resulted on extensive silicon extraction at mild treatment conditions, reducing microporous on half and acid properties at 338 K, while the alkaline treatment at 298 K hardly induced any new mesoporosity. On the other hand, when *BEA zeolite was submitted to an acid leaching procedure (HCl and HNO₃) [12], all kinds of extra-framework impurities from aluminum clusters to silica-alumina debris were removed or passivated [10].

Additionally, the introduction of new catalytically active species, such as metal oxides, into zeolites has been used to reduce coke accumulation on active sites [10]. Among metal oxides, tungsten trioxide (WO₃) can act as a photocatalyst [13], facilitating reactions such as the degradation of organic pollutants in water and the oxidation of hydrocarbons. It can also be employed as a catalyst support material, where its morphology, structure, and acidity play crucial roles [14]. WO₃-impregnated materials exhibit strong performance in surface reactions involving acid sites (Brønsted and Lewis) and demonstrate significant adsorption properties due to the presence of oxygen vacancies [15]. Said et al. studied WO₃ supported on HZSM-5 and HY, showing that these composites are effective catalysts for the non-oxidative dehydrogenation of ethanol to acetaldehyde [16].

Among catalytic applications, biomass conversion plays a crucial role, as it is the only renewable carbon source for producing valuable chemicals such as 5-hydroxymethylfurfural (HMF) from sugars like fructose or glucose through dehydration reactions [17,18]. The dehydration of C₂₊ alcohols to olefins is essential for manufacturing basic chemicals, synthetic resins, fibers, and rubbers, and serves as a precursor process for ethylene production, which underpins industries such as pharmaceuticals, dyes, agrochemicals, and plastics [19,20,21]. This route also represents an important pathway for utilizing non-petroleum feedstocks, including biomass-derived alcohols and coal-based chemical by-products.

Several articles in the literature separately report post-synthesis treatments using either bases (usually NaOH) or acids (HCl, HNO₃, etc.) [6,11,12]. In this contribution, we present a combined approach (NaOH followed by HCl) to tailor the porous and acidic properties of BEA zeolite and its WO₃-impregnated form. The objective of the present study was to prepare *BEA zeolite with a hierarchical pore structure using a post-synthesis treatment with sodium hydroxide followed by hydrochloric acid (T-NaOH-HCl). The hierarchical BEA zeolite was then impregnated with tungsten trioxide (WO₃) to introduce catalytically active acid sites for its application in the dehydration of ethanol (at 230 °C and 250 °C) and 1-propanol (at 230 °C). To evaluate the structure of the modified materials, elemental analysis, X-ray diffraction (XRD), Raman and Fourier transform infrared spectroscopy (FT-IR), pore and specific surface area analysis, solid-state nuclear magnetic resonance with magic-angle spinning (²⁷Al and ²⁹Si MAS NMR), scanning electron microscopy (SEM), and pyridine adsorption followed by FT-IR spectroscopy were employed.

2. Results and Discussion

2.1. Elemental and XRD Analyses

Elemental analysis of Si, Al, and W revealed the composition of the catalysts and is shown in

Table 1. Total Si/Al ratio, WO₃ quantity and relative crystallinity (C) of the catalysts.

Catalyst	Si/Al Ratio	WO3 (%)	C (%)
HB	13	0	100
BEA-T	39	0	85
5W-BEA-T	41	4.9	83
10W-BEA-T	42	10.2	80
15W-BEA-T	42	14.6	74
20W-BEA-T	43	19.4	70

. It can be observed that after the treatment of the BEA zeolite, the Si/Al ratio increased, which confirms the dealumination of the parent zeolite. Additionally, the impregnation of WO₃ was efficient, and the theoretical and actual loadings were very close. Thus, the samples will be referred to from here on by their theoretical values for greater clarity.

The XRD pattern of the BEA zeolite, characterized by both broad and narrow peaks, reflects structural disorder caused by stacking faults resulting from the intergrowth of two polymorphs (44% chiral and 56% achiral). Characteristic diffraction peaks were observed at 7.80° (101) and 22.50° (116) (Figure 1) [17]. The random stacking fault of polymorphs leads to a structure that is not well defined in the XRD pattern. The loss of crystallinity from HB to BEA-T (15%) is relatively small (Table 1, column 4) and comparable to the loss of microporous area (15%) and volume (17%) (

Table 2. Textural parameters for the catalysts.

Catalyst	SBET a (m2/g)	SMicro b (m2/g)	SMeso c (m2/g)	Vp d (cm3/g)	VMicro e (cm3/g)	VMeso f (cm3/g)
HB	661	410	251	0.90	0.17	0.75
BEA-T	616	347	269	1.01	0.14	0.89
WO3	12.4	0	12.4	0.03	0.002	0.028
5W-BEA-T	373	191	182	0.96	0.08	0.88
10W-BEA-T	346	125	221	0.56	0.06	0.50
15W-BEA-T	277	80	197	0.54	0.02	0.52
20W-BEA-T	240	107	134	0.55	0.04	0.51

^a Specific surface area obtained by BET method. The standard error (3σ) was ±5 m² g⁻¹. ^b Microporous area obtained by t-plot method. ^c Mesoporous area (S_Meso) = S_BET − S_Micro. ^d Total pore volume obtained by the amount of gas adsorbed at p/p₀ = 0.99. ^e Microporous volume obtained by t-plot method. ^f Mesoporous volume (V_Meso) = Vp − V_Micro.

). Relative crystallinity, calculated based on the total area of all characteristic peaks, showed a 15% reduction after treatment with T-NaOH-HCl, and WO₃ impregnation led to an additional 20–30% decrease compared to HB. Incorporating more than 10 wt.% of another metal can help prevent significant collapse of the zeolitic structure by occupying silanol nests [22,23].

The calcined material (550 °C) after WO₃ impregnation exhibited a greenish-yellow color, corresponding to the monoclinic phase of WO₃ (JCPDS 43-1035) as the only crystalline phase of this oxide. This phase revealed distinct diffraction peaks at 2θ = 23.2°, 23.5°, 24.0°, 26,7°, 28.7°, 33.6°, 34,3°, and 41,9° in the XRD pattern of WO₃-loaded catalysts, suggesting that a WO₃ crystalline species was successfully supported. These peaks were attributed to the (002), (020), (200), (120), (112), (022), (220) and (140) lattice planes, respectively [16], indicating limited dispersion of WO₃ species, and they became more intense with increasing WO₃ loading on the BEA zeolite [13,16]. A reduction in the average crystalline domain size (D) of HB from 18 nm to 10 nm was observed after hierarchization (BEA-T). After WO₃ impregnation, D of HB increased to approximately 15 nm. Additionally, the WO₃ crystallites domain deposited on BEA ranged from 15 nm (5W-BEA-T) to 50 nm (20W-BEA-T). In contrast to pure WO₃ crystallites (with domains of ~70 nm), the supported materials consisted of smaller nanocrystals deposited on the surface of the agglomerated hierarchical BEA zeolite [16], as observed by SEM (vide Section 2.6).

2.2. FT-IR and Raman Spectroscopies

Infrared (FT-IR) results (Figure 2A,B) showed bands corresponding to *BEA zeolite samples at the following wavenumbers: 573 cm⁻¹ and a small band at 515 cm⁻¹ (vibrational modes of five- and six-membered rings), 779 cm⁻¹ (external symmetric stretching vibration of oxygen in T-O-T bonds), 956 cm⁻¹ (vibration of Si-O bonds), 1088 cm⁻¹ (internal Si-O-T stretching vibration of the zeolite framework where T is a tetrahedral atom like Al or Si), 1235 cm⁻¹ (external vibration of the framework structure or vibrations of guest molecules adsorbed within the zeolite pores), 1647 cm⁻¹ (angular bending vibration of adsorbed or occluded water molecules (H-O-H) and 3440 cm⁻¹ (stretching vibrations of hydroxyl groups of physically adsorbed water molecules) [17,24]. It should be noted that the small bands at approximately 3000, 1838, and 1400 cm⁻¹ are likely due to organic impurities introduced during pellet preparation.

The spectrum of pure WO₃ shows typical absorptions at 853 and 794 cm⁻¹ corresponding to stretching vibrations of the W-O-W (tungsten-oxygen-tungsten) bridging oxygen bonds [16]. WO₃ impregnation on BEA-T clearly reveals the presence of this species on the BEA-T surface through increased vibrational intensities at 838 and 779 cm⁻¹. The shift of these bands to lower wavenumbers indicates a significant interaction between WO₃ and the BEA-T surface, as evidenced by the 15 cm⁻¹ shift to lower wavenumbers, which weakens the W-O-W bond. The band at 1235 cm⁻¹ is sensitive to the overall structure and the presence of extra-framework species or cations. This band is generally assigned to the external asymmetric stretching vibration of the T-O-T (Si-O-Si or Si-O-Al) and when WO₃ is introduced via impregnation, the tungsten species (e.g., tungstate ions, W=O groups) interact chemically and physically with the zeolite surface and internal channels. This interaction can involve the formation of new Si-O-W or Al-O-W bonds or the coordination of W species near existing Si-O-Al sites which alter the local electron density and bond angles of the adjacent framework linkages.

The Raman spectrum of HB (Figure 3) shows the vibrational modes of oxygen in the TO₄ tetrahedra that make up the zeolitic structure. The band at 346 cm⁻¹ corresponds to interlayer vibrations of five-membered rings; the band at 398 cm⁻¹ corresponds to interlayer vibrations of six-membered rings; and the bands at 476 and 500 cm⁻¹ are attributed to interlayer vibrations of four-membered rings, indicating the distinct spectral features of the HB structure [25]. The band at approximately 800 cm⁻¹ is related to the symmetric stretching vibration of Si–O–Si linkages in the zeolitic framework, while the band at 970 cm⁻¹ is associated with Si–O stretching vibrations that are sensitive to the Si/Al ratio. The Raman spectrum of BEA-T is similar to that of the HB sample, except for an increase in the relative intensity of the 970 cm⁻¹ band, which was also observed in the FT-IR spectrum and is consistent with the increase in Si/Al ratio obtained by elemental analysis, as shown in Table 1.

On the other hand, the Raman spectrum of 10W-BEA-T shows four main bands: 330 and 273 cm⁻¹, assigned to bending vibrations, and 808 and 716 cm⁻¹, attributed to stretching modes of W–O–W bonds present in WO₃ nanocrystals. The band at 716 cm⁻¹ is also associated with the formation of crystalline WO₃ [16,26]. The zeolite bands in the Raman spectrum almost disappeared when WO₃ was impregnated on the BEA-T, primarily due to strong electronic and structural interactions between the WO₃ species and the zeolite framework, and potentially self-absorption effects [16,26]. Also, scattering from crystalline metal oxides is very intense and probably contributes to quenching (or lowering) any signals from different supports (amorphous or crystalline). The impregnating solution (ammonium tungstate) interacts with the hydroxyl groups and Brønsted acid sites within the BEA-T and on its external surface. The tungsten species anchor onto these sites, often replacing protons in the Si-OH⁺-Al sites. The formation of W-O-Si or W-O-Al bonds and the subsequent calcination process (which decomposes the precursor to WO₃) lead to a significant change in the local crystal structure of the zeolite framework. Zeolite Raman bands are primarily associated with the bending and stretching vibrations of the T-O-T linkages (T = Si, Al) within the characteristic 5-membered ring that form the BEA zeolite framework. These structural alterations, caused by the incorporation of the large WO₃ species, interfere with these specific vibrational modes, leading to a significant decrease in intensity or the complete disappearance of the characteristic peaks. Increasing WO₃ loading, followed by calcination process might perturb the long-range crystalline order of the BEA-T framework, causing a certain degree of amorphization. Amorphous materials produce broad Raman signals compared to the sharp, intense peaks of a highly crystalline material. The new, potentially intense, Raman bands of the formed WO₃ species (at ~800 cm⁻¹ and 700 cm⁻¹) can mask the underlying, often weaker, zeolite framework bands. Changes in the surface morphology and particle size of the material after impregnation and calcination can also affect the scattering properties and, consequently, the observed Raman intensity.

2.3. Main Textural Properties Determined by N₂ Adsorption/Desorption Isotherms

Textural properties were analyzed using N₂ adsorption/desorption isotherms obtained at −196 °C and t-plot curves (Figures S1 and S2). All samples exhibited a combination of predominantly type I(a) (microporous solid) and type IV(a) isotherms, with a hysteresis loop appearing at higher relative pressures (P/P₀ > 0.7; Figure S1), indicating the presence of a secondary mesoporous structure (Table 2). Assuming that the total area obtained by the BET method includes the microporous, mesoporous, and external surface areas, and that the created mesoporosity can be both intra- and intercrystalline, the mesoporous area was calculated as the external surface area, as previously reported for BEA catalysts [6]. After the NaOH–HCl treatment (BEA-T), the mesopore area increased by 7%, the mesopore volume by 19%, and the total pore volume by 12%. Conversely, the specific surface area (S_BET) and micropore volume (V_Micro) decreased by 15 and 17%, respectively, indicating effective hierarchization of the *BEA zeolite. This trend was also observed for Nb-BEA catalysts [17]. On the other hand, WO₃ nanoparticles exhibited a type II isotherm with an H3 hysteresis loop, according to the IUPAC classification, which are characteristic of nonporous solids composed of non-rigid aggregates of plate-like particles and possessing low surface area [27,28]. The presence of hysteresis also indicates the existence of mesopores or macropores.

The isotherms of the WO₃ catalysts show similar characteristics of *BEA zeolite, i.e., a combination of types I(a) and IV(a). The incorporation of WO₃ clusters into zeolite led generally to a reduction in all measured textural parameters of the HB and BEA-T support, suggesting that tungsten species adhered to the zeolite surface and partially filled the pores. This suggests that impregnating the HB zeolite after hierarchization results in the formation of extra-framework WO₃ species, with surface layer thickness dependent on tungsten loading, as previously reported [16]. The decreasing microporous area and volume of the WO₃ catalysts is also indicative that an overlayer of WO₃ is formed on the BEA-T surface and partially blocks microporous accessibility.

The scenario that can be envisioned for the supported WO₃ suggests that WO₃ species, including the monoclinic nanocrystalline phase, partially cover the surface of the BEA-T zeolite. This partial coverage is evidenced by several analytical methods, such as XRD, FT-IR, Raman, and N₂ adsorption/desorption. If there were a complete, homogeneous coverage of the zeolite surface, all textural properties would be similar to those of pure WO₃, which was not observed. From the point of view of WO₃, its dispersion within the zeolite includes the formation of agglomerates; however, these agglomerates still lead to an increase in accessibility to the newly created acidic sites, as discussed in the acidity section (see Section 2.5).

Furthermore, diffusional limitations were mitigated through the combination of intrinsic microporosity and auxiliary mesoporosity generated by inter- and intra-crystalline structuring, likely driven by silicon and aluminum dissolution mechanisms. This is an important issue, since the catalytic behavior of WO₃–BEA-T composites could achieve optimal performance, which depends on both the mesoporosity and acidity, as will be discussed later.

2.4. Solid State (MAS) ²⁷Al and ²⁹Si NMR Spectroscopy

The MAS NMR spectra of ²⁷Al (Figure 4) exhibit signals corresponding to tetrahedral aluminum (Al-T_d, 40–80 ppm), extra-framework pentacoordinate aluminum species, and octahedral aluminum environments (Al-O_h, −22 to 22 ppm), corroborating the XRD and FT-IR results, which indicate the preservation of the *BEA zeolite structure. This detailed spectral analysis confirms the integrity of the BEA-T zeolite while also revealing the specific nature of any extra-framework species formed during treatment. The intense signal at 1.4 ppm observed for BEA-T and 5W-BEA-T is attributed to octahedrally coordinated Al species with fewer associated water molecules, whereas the signal broadening in this region for the 10W-BEA-T to 20W-BEA-T samples suggests a higher degree of hydration in the catalyst structure [29,30]. The ²⁷Al NMR data corroborate the presence of the 970 cm⁻¹ Raman band on BEA-T, indicating the structural defects (silanol groups) that form when aluminum is removed from the framework. This removed aluminum often relocates to extra-framework positions, where in the presence of water, it adopts a six-coordinate (octahedral) configuration, giving rise to the signal at approximately 0 ppm in the spectrum. Therefore, both signals arise from the same process of dealumination and the subsequent formation of hydrated, extra-framework aluminum species.

Table 3. Relative distribution (%) of tetrahedral (Al-T_d) and octahedral (Al-O_h) aluminum species, and silicon environments Q³ and Q⁴, according to ²⁷Al and ²⁹Si MAS NMR spectra.

Catalyst	Al-Td	Al-Oh	Si-Q4	Si-Q3
HB	62	38	80	20
BEA-T	76	24	74	26
5W-BEA-T	76	24	76	24
10W-BEA-T	71	29	71	29
15W-BEA-T	70	30	72	28
20W-BEA-T	71	29	73	27

presents the relative distribution of Q⁴ [Si(0Al)] and Q³ [Si(1Al)] silicon environments, based on the deconvolution of ²⁹Si MAS NMR spectra, as well as the tetrahedral and octahedral aluminum environments determined from ²⁷Al MAS NMR spectral deconvolution [29]. Hydrolytic cleavage of Si–O–Al bonds results in the formation of Si–O⁻ defects, leading to a reduction in Q⁴ signals (−111, −115 ppm) and an increase in Q³ signals (−102 ppm) observed in the ²⁹Si MAS NMR spectra (Figure 5).

On the other hand, the tetrahedral aluminum species increased after the alkaline–acid treatment, followed by impregnation with a small amount of WO₃ (5W-BEA-T). This was accompanied by a reduction in octahedral aluminum species, likely due to the HCl washing step, which removed deposited EFAL species (Figure 4) [17,29].

The ²⁹Si MAS NMR spectra (Figure 5) of BEA-T showed that the Q³ signal at −102 ppm remained virtually unchanged compared to the HB sample. Likewise, the Q⁴ environments at −111 ppm and −115 ppm were not affected, even after the addition of tungsten.

2.5. Acidity of the Catalysts Determined by Pyridine Adsorption

Dealumination followed by WO₃ impregnation affected both the quantity (

Table 4. Total quantity of adsorbed pyridine (N_Py) on the catalysts obtained by Py-TPD (TG/DTG) analysis. The error is ±0.02 mmol/g.

Catalyst	NPy (mmol/g)
HB	0.62
BEA-T	0.55
5W-BEA-T	0.52
10W-BEA-T	0.49
15W-BEA-T	0.50
20W-BEA-T	0.48

) and strength of the acid sites, increasing the population of weak acid sites (WAS) (Figure 6) and thus enabling the design of an efficient catalyst for the low-temperature dehydration of ethanol to ethylene. After post-synthesis treatment, the total quantity of adsorbed pyridine (N_Py, mmol/g) on the catalysts obtained by pyridine-TPD (TG/DTG) analysis decreased because pyridine molecules preferentially interact with stronger Brønsted acid sites, as these interactions have a more negative associated free energy (Table 4). Infrared spectra of the samples collected after gaseous pyridine adsorption showed that the HB zeolite displayed higher band intensity in the region between 1580 and 1420 cm⁻¹ (Figure 6). These bands correspond to the interaction of pyridine with Brønsted acid sites (1544 cm⁻¹), Lewis acid sites (1445 cm⁻¹), and a combined interaction band at 1490 cm⁻¹, attributed to both acid site types [10,17]. The BEA-T sample showed an intense Lewis band, consistent with the signal around 0 ppm of the ²⁷Al MAS NMR spectrum. Lewis acid sites may also originate from aluminum-based species such as Al³⁺, Al(OH)²⁺, Al(OH)₂⁺, AlOOH, Al(OH)₃ and Al₂O₃ which feature coordinatively unsaturated surface sites. Extra-framework aluminum species can significantly enhance the stability and catalytic performance of zeolites. Zhao et al. [30] demonstrated the reversible transformation between octahedrally and tetrahedrally coordinated framework aluminum in the BEA zeolite, highlighting the dynamic nature of aluminum speciation in these materials. In addition, Choi et al. [31] reported that mesoporous WO₃ predominantly exposes Lewis acid sites, which are associated with isolated and coordinatively unsaturated W(VI) centers. In contrast, Brønsted acid sites are primarily dependent on the presence of polytungstate polymeric species.

The WO₃ impregnated on BEA-T interacts with the surface of the zeolite, particularly at Lewis sites. Lewis acid sites are EFAL species or aluminum atoms with a lower coordination number (defects) on the surface or within the structural framework. The samples with 5 and 10% WO₃/BEA-T showed a partial suppression of the Lewis acid band (1445 cm⁻¹), which can be ascribed to the likely interaction of WO₃ species with these EFAL species on the surface of BEA-T. WO₃ itself has Lewis and Brønsted acid sites, and it tends to increase the quantity of these sites with increasing loading (15 and 20% WO₃). Thus, pyridine interacts mainly with the W(VI) Lewis sites of WO₃, which increase with higher WO₃ loading, reflecting the increase in the Lewis bands in the FT-IR spectra. Certainly, pyridine also interacts with Brønsted sites that are also present, originating from either WO₃ or the zeolite.

2.6. Analyses by SEM Micrographs

The morphologies of HB, BEA-T, and 10W-BEA-T (the sample that exhibited the best catalytic performance in dehydration reactions, vide next section) were analyzed using scanning electron microscopy (SEM), and the qualitative results are shown in Figure 7. The SEM micrographs revealed that HB consists of highly aggregate particles with a rough surface morphology and with uniform crystalline structures resembling rounded grains, as reported in the literature [23].

Treatment with NaOH and HCl was employed to modify the zeolite material. The use of NaOH primarily acts on the superficial Si–O bonds, resulting in minor structural deformation of the zeolite. This step introduces limited changes to the overall morphology by breaking select silicon-oxygen linkages on the external surface. Subsequently, HCl treatment selectively removes extra-framework aluminum species from the structure. Importantly, this process does not cause severe damage to the microporous framework of the zeolite. As a result, the material maintains morphological characteristics similar to the parent zeolite, with the combined chemical treatments facilitating controlled modification while preserving the essential microporous architecture [32]. It was observed that there was a shrinking in the particle size and the creation of intercrystalline mesoporosity in BEA-T in agreement to textural parameters (Table 2). This enhanced accessibility of the new acid sites and faster diffusion of products improved the catalyst’s performance.

The SEM images of WO₃ showed loosely aggregated plate-like nanoparticles, consistent with the literature [27]. The 10W-BEA-T catalyst exhibited a rough morphology with granular crystals, and particle size remained largely unchanged after modification when compared to the parent zeolites. Energy-dispersive X-ray spectroscopy (EDS) analysis confirmed the presence of tungsten (W) (Figure S3).

2.7. Ethanol and 1-Propanol Catalytic Dehydrations

Catalysis has become a highly relevant technology in achieving the goals of sustainable chemistry [33], and zeolites, especially *BEA-type structures, have been widely used as catalysts in various research areas focused on sustainability. To enhance these catalytic processes, it is anticipated that zeolite hierarchization will facilitate the diffusion of reactants, promote the release of products, and improve access to catalytic sites. Previous studies from our group involving the hierarchization of *BEA zeolite using ammonium hexafluorosilicate under solid-state conditions have shown the generation of secondary mesopores and enhanced ethanol diffusion to catalytically active sites, resulting in the conversion of ethanol into two main products: ethylene and diethyl ether [10]. Accordingly, the ethanol dehydration reaction was carried out at 230 °C and 250 °C, and the conversion and selectivity results are presented in Figure 8 and Figure 9. The results are described from the viewpoint of three parameters: ethanol conversion, ethylene selectivity, and TON (turnover number) for ethylene formation (Table S1). Compared to HBEA, at 230 °C, the BEA-T catalyst showed a significant improvement in all three parameters, while at 250 °C the selectivity and TON for ethylene underwent a decrease. This is consistent with both the decrease in total acid sites and the creation of additional mesopores in BEA-T, since the diffusion of reactants and products might have compensated for the loss of acidity in the acid-catalyzed reaction. The higher temperature likely led to the loss in selectivity because it promoted side reactions in the BEA-T zeolite, which has more Lewis acid sites.

The impregnation of WO₃ onto hierarchized BEA generated materials with a lower total number of accessible sites, as determined by Py-TPD, and likely weaker acid sites (WAS), as also observed for Nb₂O₅–BEA-T catalysts [17] and α-Fe₂O₃-BEA catalysts [34]. The results for both reaction temperatures, 230 and 250 °C, clearly showed an enhancement trend in all three parameters, with a maximum activity for 10W-BEA-T (at 230 °C: 91% ethanol conversion, 97% selectivity to ethylene, TON = 0.95; at 250 °C: 94% ethanol conversion, 95% selectivity to ethylene, TON = 1.64). The BEA-T zeolite exhibited an increased Si/Al ratio after treatment and WO₃ impregnation, indicating that dealumination took place. The surface of BEA-T anchored WO₃ species that contributed to both Brønsted and Lewis acid sites. Therefore, the observed high selectivity toward ethylene during the catalytic dehydration of ethanol can be attributed to two key factors. First, a moderate reduction in the acidity of the zeolite material, which created a more controlled catalytic environment, minimizing excessive side reactions. Second, controlled tuning of the mesoporous area appears to play an important role by enhancing the spatial environment needed to facilitate more efficient diffusion of ethylene molecules. These combined effects allowed for improved access to active sites and promoted the effective release of ethylene from the catalyst structure, resulting in the notable selectivity observed in the reaction. The correlation between ethylene selectivity and either mesoporous area or the number of acid sites supports this idea, showing maximum activity for the catalyst with 10 wt.% WO₃ loading (Figure 10). In addition, a performance test using the 10W-BEA-T catalyst with 50 ethanol pulses at 230 °C showed a decrease to 85% ethanol conversion and 79% ethylene selectivity. The ethylene selectivity was about 17% lower than after a single pulse, likely due to coke buildup on the catalyst surface. CHN analysis confirmed around 1% carbon residue on the catalyst after 50 pulses, supporting this explanation for deactivation.

The catalytic dehydration of 1-propanol has been extensively studied due to its importance in producing valuable chemicals such as olefins and ethers [35]. A substantial body of research has examined the mechanistic pathways involved in this reaction, with particular attention to how catalyst composition influences product distribution [36]. It is widely accepted that a combination of active site accessibility and acidity plays a decisive role in directing the reaction pathway. Among these, Brønsted acid sites typically play a critical role in enabling the transformation of 1-propanol into either olefins or ethers.

The dehydration process generally begins with the adsorption of 1-propanol onto the catalyst surface, forming an alkoxy intermediate. This is followed by the elimination of water through an E1 (unimolecular elimination) mechanism, leading to the formation and subsequent desorption of propene. A key step in this mechanism involves the stabilization of a carbocation-like transition state, which is considered the primary factor influencing the rate of unimolecular dehydration. Improved stabilization of this intermediate generally results in higher selectivity toward olefin (propene) formation [37,38,39]. Alternative reaction pathways may involve the formation of dimers or trimers of adsorbed 1-propanol, which are favored under certain pressure conditions.

For the 1-propanol dehydration reaction at 230 °C, BEA-T exhibited the highest performance, achieving 99% conversion and 89% selectivity to propene (Figure 11), which confirms the importance of increased mesopore formation as a key factor in enhancing propene selectivity. Given that 1-propanol is a larger molecule than ethanol, the superior performance of the BEA-T catalyst can likely be attributed to its higher total pore volume, which may enhance the stabilization and accommodation of multimeric intermediates within the zeolitic framework during the reaction. However, when taking the TON into consideration (Table S2), an increase in WO₃ loading on BEA-T resulted in the best activities, with the 20% loading being the most active. Again, the correlation between propene selectivity and either mesoporous area or the number of acid sites (Figure 12) supports this behavior, showing maximum activity for 20W-BEA-T, which demonstrates that these factors are critical in contributing to the improved performance of the WO₃-supported catalysts.

3. Materials and Methods

3.1. Hierarchization of *BEA Zeolite and Impregnation of WO₃

Ammonium-form BEA zeolite NH₄BEA, obtained from Zeolyst International (CP814E, Kansas City, KS, USA), with a mole ratio of SiO₂/Al₂O₃ = 25, was calcined at 550 °C for 8 h, resulting in the formation of a proton-form sample (HB). The hierarchization procedure treated HB with a 0.2 M sodium hydroxide solution (97%, Aldrich, St. Louis, MO, USA), under magnetic stirring at 75 °C for 4 h. Subsequently, the mixture was washed with deionized water (75 °C for 1 h) and the resulting material was treated with a 0.5 M hydrochloric acid solution (37%, Aldrich, St. Louis, MO, USA) under the same conditions as the basic treatment. The material was washed again, and the resulting zeolite was dried (120 °C for 12 h) and calcined (550 °C for 8 h). The impregnation of tungsten oxide into the hierarchical *BEA zeolite was obtained by aqueous impregnation. The sample was dried (200 °C for 4 h) under vacuum to remove adsorbed water molecules and based on the mass of the dry materials, the amount of ammonium tungstate (NH₄)₁₀H₂(W₂O₇)₆ (99.99%, Aldrich, St. Louis, MO, USA) to be used (5, 10, 15, and 20 wt.%) was determined. The solutions containing tungsten and zeolite were placed under magnetic stirring at 90 °C until complete evaporation of the solvent. Finally, the resulting materials were kept dry in an oven (120 °C for 12 h), followed by calcination (550 °C for 8 h).

Table 5. Nomenclature used for studying *BEA zeolite.

Code	Description
HB	Protonic *BEA zeolite
BEA-T	HB treated with NaOH and HCl
5W-BEA-T	HB treated with NaOH and HCl and impregnated with 5 wt.% of WO3
10W-BEA-T	HB treated with NaOH and HCl and impregnated with 10 wt.% of WO3
15W-BEA-T	HB treated with NaOH and HCl and impregnated with 15 wt.% of WO3
20W-BEA-T	HB treated with NaOH and HCl and impregnated with 20 wt.% of WO3

presents the nomenclature used to identify the different samples.

3.2. Experimental Methods of Characterization

3.2.1. Powder X-Ray Diffraction (XRD)

X-ray diffraction (XRD) data were collected using a PANalytical Empyrean diffractometer (Malvern, UK) equipped with a copper anode (Cu Kα radiation, λ = 1.5406 Å), operating at 40 kV and 45 mA. Scans were performed over the 2θ range of 2° to 60°, with a scan rate of 2° min⁻¹ and a step size of 0.02°.

The relative crystallinity (%C) of the samples was determined by comparing their diffraction patterns to that of a standard HB zeolite. This involved integrating the area under the characteristic peaks between 5° and 60° (2θ), following Equation (1).

$$\mathrm{\%}\mathrm{ }\mathrm{C}\mathrm{ }=\mathrm{ }{\displaystyle \frac{\sum \mathrm{d}\mathrm{e}\mathrm{a}\mathrm{l}\mathrm{u}\mathrm{m}\mathrm{i}\mathrm{n}\mathrm{a}\mathrm{t}\mathrm{e}\mathrm{d}\mathrm{ }\mathrm{z}\mathrm{e}\mathrm{o}\mathrm{l}\mathrm{i}\mathrm{t}\mathrm{e}\mathrm{ }\mathrm{p}\mathrm{e}\mathrm{a}\mathrm{k}\mathrm{s}}{\sum \mathrm{H}\mathrm{B}\mathrm{ }\mathrm{p}\mathrm{e}\mathrm{a}\mathrm{k}\mathrm{s}}}\times 100$$

(1)

3.2.2. Elemental Analysis

Elemental analysis of silicon, aluminum, and tungsten was performed using a Shimadzu EDX-720 energy-dispersive X-ray fluorescence (EDXRF) spectrometer (Tokyo, Japan). Samples were prepared using polypropylene film and analyzed under vacuum conditions using a rhodium (Rh) X-ray target, with an operating voltage range of 15–50 kV, to determine the total Si/Al molar ratio.

3.2.3. Fourier-Transform Infrared Spectroscopy (FT-IR)

Infrared spectra were collected using a Thermo Scientific Nicolet 6700 FT-IR spectrometer (Madison, WI, USA), with 512 scans at 4 cm⁻¹ resolution, analyzing the 4000–430 cm⁻¹ range. Samples typically involved 0.6 wt.% of the catalyst mixed into dried, high-purity (>99%) Merck (Rahway, NJ, USA) KBr pellets. Samples typically consisted of pellets with 0.6 wt.% of the catalyst mixed with dried, high-purity KBr (>99%, Merck, São Paulo, Brazil).

3.2.4. Raman Spectroscopy

Raman spectra were acquired using a LabRAM HR Evolution spectrometer (Horiba, Palaiseau, France) under ambient conditions (25 °C). A 795 nm excitation laser was employed at a power setting of 9 mW. Each spectrum was recorded over 64 accumulations, with a spectral resolution of 2 cm⁻¹.

3.2.5. Textural Properties

Textural data were obtained by gaseous physisorption of N₂ at low temperature (−196 °C) in a Micromeritics analyzer (ASAP 2020C, Norcross, GA, USA). Prior to analysis, samples were degassed with evacuation (target pressure of 50 μm Hg) at 300 °C for 4 h.

The main parameters obtained from the analysis of the isotherms were: specific surface area (S_BET), Brunauer–Emmett–Teller (BET), in the range of 0.01 < P/P₀ < 0.1; micropore area (S_Micro) and micropore volume (V_Micro), calculated using the t-plot method of Harkins and Jura; total pore volume (V_p), determined from desorption at P/P₀ = 0.99, according to the Gurvitch Rule; mesoporous area (S_Meso = S_BET − S_Micro) and mesoporous volume (V_Meso = V_p − V_Micro).

3.2.6. Microscopy Analysis

SEM imaging was conducted on a JEOL JSM instrument (Peabody, MA, USA) under high vacuum at 15 kV, using a secondary electron detector (LED, Low Energy Detector) to capture images at magnifications from 100× to 10,000×. The SEM microscope was equipped with energy dispersive X-ray spectroscopy (EDX) from Thermo Scientific NSS Spectral.

3.2.7. Solid-State ²⁷Al and ²⁹Si Magic Angle Spinning Nuclear Magnetic Resonance

Solid-state NMR spectra were acquired for the catalysts using a Bruker Avance III HD Ascend spectrometer (14.1 T, 600 MHz for ¹H, Billerica, MA, USA), equipped with 2 mm or 4 mm CP/MAS probes, employing magic angle spinning (MAS) technique. Catalysts were packed into 4 mm zirconia rotors, and specific acquisition parameters were applied for each nucleus: (i) ²⁷Al MAS NMR (156.4 MHz) was recorded at a spinning rate of 10 kHz, using a 0.4 µs pulse duration (π/20) and a 1 s recycle delay, over 2000 scans. Spectra were referenced to hexa(aqua)aluminum(III) trichloride, [Al(H₂O)₆]Cl₃ (δ = 0 ppm); (ii) ²⁹Si MAS NMR (119.3 MHz) was recorded at a spinning rate of 10 kHz, with a 4.25 µs pulse duration (π/2) and a 20 s recycle delay, over 3072 scans, referenced to tetramethylsilane (TMS), Si(CH₃)₄ (δ = 0 ppm).

The relative distribution of aluminum atoms in the zeolite framework was determined from the ²⁷Al MAS NMR spectra, distinguishing between octahedral (Al_Oh) and tetrahedral (Al_Td) coordination environments, using Equation (2). The framework Si/Al molar ratio was calculated based on the deconvolution of ²⁹Si MAS NMR spectra, using Equation (3).

The ²⁹Si spectra, which identify silicon environments such as Q⁴, Q³, Q², and Q¹, were deconvoluted using a Gaussian–Lorentzian fitting function implemented in Python (Version: 3.9.7 (default, 16 September 2021, 16:59:28), Wilmington, DE, USA), with a line broadening (LB) of 10.

$$\mathrm{\%}\mathrm{A}\mathrm{l}\mathrm{ }\left({\mathrm{O}}_{\mathrm{h}}\mathrm{ }\mathrm{o}\mathrm{r}\mathrm{ }{\mathrm{T}}_{\mathrm{d}}\right)\mathrm{ }=\mathrm{ }{\displaystyle \frac{\mathrm{S}\mathrm{i}\mathrm{g}\mathrm{n}\mathrm{a}\mathrm{l}\mathrm{ }\mathrm{a}\mathrm{r}\mathrm{e}\mathrm{a}\mathrm{ }\mathrm{o}\mathrm{f}\mathrm{ }\mathrm{i}\mathrm{n}\mathrm{t}\mathrm{e}\mathrm{r}\mathrm{e}\mathrm{s}\mathrm{t}}{\sum \mathrm{S}\mathrm{p}\mathrm{e}\mathrm{c}\mathrm{t}\mathrm{r}\mathrm{u}\mathrm{m}\mathrm{ }\mathrm{a}\mathrm{r}\mathrm{e}\mathrm{a}\mathrm{s}}}$$

(2)

$${\left({\displaystyle \frac{Si}{Al}}\right)}_{lattice}={\sum }_{n=0}^4{\displaystyle \frac{n}{4}} I_{Si\left(nAl\right)}$$

(3)

The intensity I_Si(Al) represents the NMR signal corresponding to silicon atoms bonded to n aluminum atoms, with the intensity being proportional to the population of such silicon environments. The total number of silicon atoms (numerator in the Si/Al ratio) is calculated as the sum of all Si(nAl) species observed. According to Löwenstein’s rule, which prohibits the formation of Al–O–Al linkages in zeolite frameworks, each aluminum atom is tetrahedrally coordinated by four silicon atoms. Consequently, each Si(nAl) environment corresponds to one-fourth of an aluminum atom, and the total number of aluminum atoms (denominator) is calculated as ¼ × Σ[n × ISi_(nAl)]. This relationship is used to estimate the framework Si/Al ratio based on the relative intensities obtained from the deconvoluted ²⁹Si MAS NMR spectra.

3.2.8. Acidity of the Catalysts

To evaluate acidity via pyridine adsorption, approximately 20 mg of catalyst was loaded into an aluminum crucible placed inside a borosilicate glass tube. The sample was dehydrated under a nitrogen (N₂) flow at 300 °C for 1 h using a tubular furnace (Thermolyne, model F21100, Waltham, MA, USA). After cooling to 150 °C, gaseous pyridine (>99.8%, Sigma-Aldrich, St. Louis, MO, USA) was passed over the sample for 1 h, followed by an additional 1-h purge at 150 °C in N₂ (5.0 grade, White Martins, São Paulo, Brazil) to remove physiosorbed pyridine. Subsequently, the sample was cooled and immediately prepared as an approximately 6 wt.% catalyst/KBr mixture for FT-IR analysis. The total quantity of acid sites was calculated by Py-TPD (via TG/DTG), which has been described elsewhere [18].

3.2.9. Catalytic Dehydration Reactions

Ethanol (99.5%, Neon, Suzano, São Paulo, Brazil) or 1-propanol PA (99.5%, Aldrich, St. Louis, MO, USA) dehydration reactions were evaluated by three injections of alcohol under 10 mg of catalyst in a pulse microreactor coupled to a gas chromatograph with flame ionization detector (Shimadzu GC-FID, model 2010, Kyoto, Japan), equipped with a Shimadzu CBP1 PONA column (M50-042, 50 m × 0.15 m × 0.33 μm). The reactions were carried out at 250 °C under the following conditions: alcohol injection volume: 0.5 μL; pressure: 95.6 kPa; total flow: 6 mL/min; column flow: 0.1 mL/min; linear velocity: 6.4 cm/s; purge flow: 1 mL/min; split ratio: 49; column temperature: 35 °C; flame temperature: 250 °C. The performance of the catalysts in the ethanol reaction was evaluated after a sequence of 50 pulses of 0.5 μL each, followed by the analysis of conversion and selectivity.

The calculations for reactant conversion and product selectivity (ethylene (EE), dimethyl ether (DME), and propene (PP)) were determined using Equations (4)–(7), where n represents the molar quantity of the reactant. The reported values are the average of the three pulses.

$$\mathrm{C}\mathrm{o}\mathrm{n}\mathrm{v}\mathrm{e}\mathrm{r}\mathrm{s}\mathrm{i}\mathrm{o}\mathrm{n}\mathrm{ }(\mathrm{\%})\mathrm{ }=\mathrm{ }{\displaystyle \frac{{{\mathrm{n}}_{\mathrm{e}\mathrm{t}\mathrm{h}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{i}\mathrm{n}\mathrm{i}\mathrm{t}\mathrm{i}\mathrm{a}\mathrm{l}}-{{\mathrm{n}}_{\mathrm{e}\mathrm{t}\mathrm{h}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{f}\mathrm{i}\mathrm{n}\mathrm{a}\mathrm{l}}}{{{\mathrm{n}}_{\mathrm{e}\mathrm{t}\mathrm{h}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{i}\mathrm{n}\mathrm{i}\mathrm{t}\mathrm{i}\mathrm{a}\mathrm{l}}}}\times \mathrm{ }100$$

(4)

$$\mathrm{S}\mathrm{e}\mathrm{l}\mathrm{e}\mathrm{c}\mathrm{t}\mathrm{i}\mathrm{v}\mathrm{i}\mathrm{t}\mathrm{y}\mathrm{ }(\mathrm{\%})\mathrm{ }=\mathrm{ }{\displaystyle \frac{n_{EE \mathrm{or} } n_{DME}}{{{\mathrm{n}}_{\mathrm{e}\mathrm{t}\mathrm{h}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{i}\mathrm{n}\mathrm{i}\mathrm{t}\mathrm{i}\mathrm{a}\mathrm{l}}-\mathrm{ }{{\mathrm{n}}_{\mathrm{e}\mathrm{t}\mathrm{h}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{f}\mathrm{i}\mathrm{n}\mathrm{a}\mathrm{l}}}}\mathrm{ }\times \mathrm{ }100$$

(5)

$$\mathrm{C}\mathrm{o}\mathrm{n}\mathrm{v}\mathrm{e}\mathrm{r}\mathrm{s}\mathrm{i}\mathrm{o}\mathrm{n}\mathrm{ }(\mathrm{\%})\mathrm{ }=\mathrm{ }{\displaystyle \frac{{{\mathrm{n}}_{\mathrm{p}\mathrm{r}\mathrm{o}\mathrm{p}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{i}\mathrm{n}\mathrm{i}\mathrm{t}\mathrm{i}\mathrm{a}\mathrm{l}}-{{\mathrm{n}}_{\mathrm{p}\mathrm{r}\mathrm{o}\mathrm{p}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{f}\mathrm{i}\mathrm{n}\mathrm{a}\mathrm{l}}}{{{\mathrm{n}}_{\mathrm{p}\mathrm{r}\mathrm{o}\mathrm{p}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{i}\mathrm{n}\mathrm{i}\mathrm{t}\mathrm{i}\mathrm{a}\mathrm{l}}}}\mathrm{ }\times \mathrm{ }100$$

(6)

$$\mathrm{S}\mathrm{e}\mathrm{l}\mathrm{e}\mathrm{c}\mathrm{t}\mathrm{i}\mathrm{v}\mathrm{i}\mathrm{t}\mathrm{y}\mathrm{ }(\mathrm{\%})\mathrm{ }=\mathrm{ }{\displaystyle \frac{n_{PP } }{{{\mathrm{n}}_{\mathrm{p}\mathrm{r}\mathrm{o}\mathrm{p}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{i}\mathrm{n}\mathrm{i}\mathrm{t}\mathrm{i}\mathrm{a}\mathrm{l}}-\mathrm{ }{{\mathrm{n}}_{\mathrm{p}\mathrm{r}\mathrm{o}\mathrm{p}\mathrm{a}\mathrm{n}\mathrm{o}\mathrm{l}}}_{\mathrm{f}\mathrm{i}\mathrm{n}\mathrm{a}\mathrm{l}}}}\mathrm{ }\times \mathrm{ }100$$

(7)

4. Conclusions

This study investigated the hierarchization of *BEA zeolite followed by surface modification with tungsten trioxide (WO₃) and its effects on catalytic performance in the dehydration of ethanol and 1-propanol. The hierarchical structure was achieved via sequential post-synthetic treatments using 0.2 M sodium hydroxide and 0.5 M hydrochloric acid (referred to as T-NaOH-HCl) forming BEA-T. After this treatment, WO₃ was impregnated onto the BEA-T zeolite at loadings of 5, 10, 15, and 20 wt.%. Hierarchization induced several notable structural and textural changes. The SiO₂/Al₂O₃ molar ratio increased from 25 to 39, indicating silica enrichment. Relative crystallinity decreased by 15%, and the average crystalline domain size was reduced from 18 nm to 10 nm. The mesoporous surface area increased from 251 to 269 m²/g, and the total pore volume increased from 0.90 to 1.01 cm³/g. A slight increase in tetrahedrally coordinated aluminum was also observed by ²⁷Al and ²⁹Si MAS NMR. WO₃ crystallites on BEA-T ranged from 11 nm (5W-BEA-T) to 50 nm (20W-BEA-T), in contrast to bulk WO₃ (70 nm), suggesting nanocrystal dispersion on the zeolite surface (a conclusion further supported by SEM analysis).

Catalytic testing for ethanol dehydration at 230 °C and 250 °C revealed that the catalyst impregnated with 10 wt.% WO₃ exhibited the highest performance, achieving 94% conversion and 95% selectivity to ethylene at 250 °C. At 230 °C, the same material achieved 91% conversion and 97% selectivity to ethylene. In contrast, for 1-propanol dehydration at 230 °C, the BEA-T sample (without WO₃) outperformed all others, reaching 99% conversion and 89% selectivity to propene. However, based on TON calculations, 20 wt.% WO₃/BEA-T was the best catalyst, highlighting the importance of the relative active sites in these reactions. The high conversion and selectivity observed in the dehydration of both ethanol and 1-propanol can be attributed to a moderate reduction in the acidity of the BEA zeolite and tuned mesoporosity. Thus, these results highlight the complementary roles of hierarchical structuring and WO₃ functionalization in tuning acidity and improving catalytic performance for alcohol dehydration.