The Effect of Co-feeding Methyl Acetate on the H-ZSM5 Catalysed Methanol-to-Hydrocarbons Reaction

The reactivity of methanol and methyl acetate mixtures over a HZSM-5 catalyst is studied over a period of 6 h at 350 °C, with small molecular weight olefins and aromatic compounds observed as reaction products. Post-reaction analysis of the catalyst shows the coke content to increase with methyl acetate content. Vibrational spectra (DRIFTS and inelastic neutron scattering, INS) indicate the major hydrocarbon species present in the coked catalysts to be methylated aromatic molecules, with INS spectra indicating a greater degree of methylation in the catalysts used with higher methyl acetate content. The greater extent of deactivation at higher methyl acetate concentrations is tentatively attributed to a diminishment of water in the zeolite cavity, which would otherwise facilitate re-generation of the active sites.


Introduction
The methanol-to-hydrocarbons reaction (MTH) provides a catalytic route where methanol, a relatively cheap feedstock, can be turned into more valuable and industrially relevant products. The MTH reaction uses an acidic zeolite catalyst, commonly ZSM-5, which can produce light olefins and a range of methylated aromatics [1]. The catalyst at steadystate is thought to operate via a 'hydrocarbon pool' (HCP) mechanism. The HCP mechanism is an autocatalytic cycle that describes how the catalyst functions after the first hydrocarbons have formed [2,3]. However, the mechanism of formation of the first carbon-carbon bonds is still elusive, with many different proposals in the literature [4].
Understanding how the first C-C bonds are created may help optimisation of catalyst composition in order to both maximise efficiency but also tune selectivity. One recent proposal independently reported by the groups of Lercher [5] and Weckhuysen [6] is that carbon-carbon bonds are created via methyl acetate (MeOAc) as the first intermediate. [5,6]. Formation of MeOAc from methanol or dimethylether (DME) requires the feedstock to undergo a carbonylation reaction, which forms surface acetate groups. The carbonylation reaction also requires a source of CO, which Lercher et al. suggest may result from dehydrogenation of methanol [5]. Methanol and DME carbonylation to form MeOAc has been reported mainly with a mordenite acid zeolite catalyst, although good selectivity towards MeOAc at relatively lower temperatures has also been observed with HZSM-5 [7,8]. CO has also been observed as part of the initial stages of the MTH reaction, both on ZSM-5 and on SAPO-34 [9,10]. In studies where the carbonylation reaction was the main focus, it has been reported that water causes the carbonylation rate to decrease due to competitive adsorption with the CO, since methanol is dehydrated to form DME and water, the carbonylation step is expected to be the rate limiting step of the MTH reaction [7,11].
In this study we have explored the reactivity of methanol-MeOAc mixtures over an HZSM-5 catalyst at temperatures representative of that employed in MTH chemistry. We particularly focus on the effects of MeOAc on the catalyst lifetime, employing inelastic neutron scattering spectroscopy (INS) to characterise the used catalysts. INS has considerable potential for investigating zeolite catalysts as it provides access to the vibrational spectra of used catalysts over a wide frequency range without obstruction from zeolite lattice modes [12]. We have recently reported the use of INS to study HZSM-5 catalysts used in the MTH reaction [13,14] and the role of DME in the MTH reaction chemistry [15].
In the present work we examine the MTH reaction for a period of 6 h at 350 °C in the presence of different amounts of MeOAc. The reaction was monitored by in-line mass spectrometry whilst, additionally, liquid products were collected in a catch-pot and analysed by GC-MS. Post-reaction, the catalyst samples were analysed by INS, N 2 sorption experiments and temperature programmed oxidation (TPO).

Experimental
The HZSM-5 (Si:Al ratio = 30) zeolite used is a commercially available catalyst provided in powder form by Johnson Matthey plc. Catalyst characterisation has been reported elsewhere [13]. Residual HZSM-5 template (tetrapropyl ammonium bromide) was removed by heating the zeolite in air at 500 °C for 12 h prior to use.

Reaction Testing
The reactions were conducted using a reaction test facility located in the ISIS Neutron and Muon Source that is described in detail by Warringham et al. [16]. The fixed bed reactor is made of stainless steel with an internal diameter of 35 mm and length of 60 cm. 12 g of calcined HZSM-5 were loaded on the reactor and dried under a constant flow of He (150 ml min −1 , CK gas, > 99%) at 350 °C for 3 h. After the drying process, the reactor is kept at temperature and the reactant feed was introduced into the reactor at a rate of 1 g reactant g catalyst −1 h −1 . The reactant feed was a liquid mixture of methanol and methyl acetate (with molar percentages of 0% MeOAc, 10% MeOAc, 30% MeOAc, 60% MeOAc and 100% MeOAc) and all reactions were stopped after 6 h. The reactor was then flushed for 15 min with helium to remove any excess reactant feed present before being isolated and allowed to cool to ambient temperature.

Product Analysis
Gaseous products were analysed by in-line mass spectrometry (Hiden Analytical, HPR-20) connected to the exit line of the reactor via a differentially-pumped heated quartz capillary. A catch-pot placed downstream of the reactor was used to collect liquid products. They were analysed by off-line GC-MS (Agilent 7890A GC, 5975 MSD, DB-1MS capillary l: 60 m, ID 0.25 mm, t 0.25 μm). Initial oven temperature 40 °C held for 2 min, increased at a ramp rate of 10 °C min −1 to 150 °C and held for 3 min.

Post-reaction Catalyst Analysis
For the INS measurements all sample handling was conducted in an argon filled glove box (MBraun UniLab MB-20-G, [H 2 O] < 1 ppm, [O 2 ] < 1 ppm). The reacted catalyst was removed from the reactor and transferred into aluminium INS flat cells sealed with indium wire. INS spectra were collected with the TOSCA instrument. TOSCA is an indirect geometry instrument with a spectral range of 25 to 4000 cm −1 but is optimal below 2000 cm −1 . Some of the reacted catalyst was kept for further analysis using diffuse reflectance infrared Fourier transform spectroscopy (DRIFTS), nitrogen adsorption and temperature programmed oxidation (TPO).
TPO experiments were conducted on the post-reacted ZSM-5 samples using a Hiden CatLab Microreactor integrated with a mass spectrometer and the coke weight percent was verified by thermogravimetric analysis (TGA) using the same procedure (TGA Q50, TA instruments). Approximately, 0.05 g of reacted catalyst was placed in a quartz reactor and dried at 300 °C until no water was detected in the mass spectrometer. The TPO was carried out under 20% O 2 /He with increasing temperature from 40 to 800 °C at a heating rate of 10 °C min −1 . TGA was completed in the same way, however, air was used instead of the O 2 /He mixture.
Surface area analysis was completed using a Quantachrome Quadrasorb EVO/Si gas adsorption instrument. 0.15 g of sample was placed in a 9 mm quartz sample tube and was degassed at < 20 mTorr at 200 °C for 20 h. The weight of the sample was recorded before being mounted on the Quadrasorb instrument. The Brunauer-Emmett-Teller (BET) equation was used to calculate the surface area in the pressure range P/P 0 of 0.02-0.04. The micropore volume was calculated from the t-plot curve using the thickness range between 5 and 6.9 Å. Adsorption isotherm analysis was completed using the QuadraWin software. DRIFTS spectra were collected using an Agilent Carey 680 FTIR spectrometer equipped with a Harrick Praying Mantis accessory. Catalyst samples were loaded under argon into the Harrick Praying Mantis high temperature in situ cell fitted with ZnSe windows. It was then heated in flowing nitrogen (50 mL min −1 ) at a ramp rate of 10 °C min −1 to 350 °C and held at 350 °C for 30 min. Spectra were collected with 64 scans at 4 cm −1 resolution using a liquid nitrogen cooled MCT detector. Figure 1 shows the product profiles versus time on stream for (a) methanol alone, (b) methanol:MeOAc 7:3, (c) methanol:MeOAc 4:6 and (d) MeOAc alone. The mass spectrometric analysis is complicated by the contributions from fragmentation of other species but, nonetheless, a number of trends can be identified. For methanol alone, the formation of ethene, propene and aromatic products remains effectively constant over the 6 h run time.

Reaction Monitoring
Although there is some increase in the amount of unreacted methanol and DME over this time period, the overall conversion of methanol remains high (> 90%). Figure 2 plots the methanol and MeOAc conversions versus time for the different reactant compositions tested (conversions were calculated from comparison with mass spectral peak intensities measured at time = 0 on bypassing the reactor). Figure 1b shows the addition of 30% MeOAc leads to a proportionally greater degree of aromatic products, whilst Fig. 2 shows both MeOH and MeOAc conversions to remain high. Over the range 0-30% MeOAc content, Fig. 2a shows methanol conversion to be slightly improved in increasing MeOAc; for example at 5 h T-o-S 10% and 30% MeOAc return X MeOH values of 99.0% and 99.9% respectively, compared to a value of 98.0% for a pure methanol feed. These small shifts in methanol conversion may reflect changes in the formation of the hydrocarbon pool on increasing presence of the ester.
At 60% MeOAc Fig. 2 shows a noticeable deactivation to occur. The methanol conversion falls steadily throughout the run and, although aromatic production continues (Fig. 1c), the apparent continued production of ethene and propene is largely due to the contributions to m/z = 42 and 27 from fragmentation of unreacted MeOAc. For a pure MeOAc feedstream, Fig. 1d shows the aromatic signal to steadily There is also a significant increase in the methanol signal, suggesting that hydrolysis of MeOAc may be occurring. Figure 3 shows GC-MS analysis of the liquid products retained in the reactor catchpot (total product after 6 h on stream). For pure MeOAc as the reactant, acetic acid is the major liquid product. In all of the reactions, the hydrocarbon products comprise a mixture of xylenes, tri-methylbenzenes, tetra-methylbenzenes and substituted naphthalenes. These products are still present but at much lower levels when pure MeOAc was the reactant.
The conversion of MeOAc over SAPO-34 catalysts is reported to give an initial product distribution similar to that formed from methanol, although the production of alkenes falls after only 10 min on stream at 400 °C [17]. We are not aware of any comparable study of MeOAc conversion over  HZSM-5, although we note that coupling of CO and methanol over HZSM-5 is reported to form aromatic products, presumably via MeOAc [18]. The results presented above suggest that the major role of MeOAc is to promote catalyst deactivation. Accordingly, we examined the used catalysts from the above reactions in more detail.

Post-reaction Catalyst Characterisation
Consistent with the suggested role of MeOAc in promoting catalyst deactivation, the coke content of the used catalysts increased with increasing MeOAc content of the reaction feed, as shown in Table 1. It is noted that this systematic trend contrasts with the small and somewhat anomalous methanol conversion trends observed in Fig. 2a. There is also a corresponding loss of surface area, principally micropore volume, which correlates with the increasing coke content. These data are consistent with earlier reports that initial coke formation in methanol conversion over HZSM-5 occurs within the micropores of the zeolites [19]. Temperatureprogrammed oxidation measurements reveal that addition of MeOAc to the reaction feed causes some change in the nature of the coke species. (Fig. 4).
There is a significant shift to higher temperature in the peak maximum in the TPO profile of the used catalysts when MeOAc is added to the feed, from ~ 520 to 580 °C. The shift being observed even when 10% MeOAc is added to the methanol feed. This suggests that in the presence of MeOAc the coke deposits have a lower H:C ratio than that formed from methanol alone, although there is no evidence for the presence of "hard" or graphitic coke [20] even with a pure MeOAc feed at 350 °C. The peak shift is consistent with an increased presence of aromatics when methyl acetate is added to the methanol feed. Figure 5 shows DRIFTS spectra of the used catalysts in the 4000-2200 cm −1 region, in all cases recorded at 350 °C in flowing helium. The blank zeolite dehydrated at 350 °C shows two characteristic ν(OH) bands at 3735 and 3596 cm −1 assigned respectively to SiOH groups on the external surface or in defects and to Si(OH)Al Brønsted acid sites [21,22]. An additional weak shoulder at 3650 cm −1 is due to extra-framework AlOH groups [23,24]. The used catalysts all show attenuation of the Brønsted acid band, which becomes more attenuated as the MeOAc content of the feed increases. At higher MeOAc concentrations the silanol and extra-framework AlOH bands are also attenuated. The attenuation of the Brønsted acid sites was seen previously in catalysts used for methanol conversion at 350 °C for 3 days [13], consistent with coke formation at the acid sites. Attenuation of the silanol and extra-framework AlOH sites is associated specifically with the presence of MeOAc.
In the ν(CH) region the four bands appearing at 3121, 2971, 2926 and 2869 cm −1 closely resemble those reported by Suwardiyanto et al. [13] and assigned to methylated aromatic hydrocarbon species trapped in the zeolite pores. The intensities of these bands increase with MeOAc content of the feed, as does the coke content, but from this region of the infrared spectrum we cannot identify any differences in the nature of the coke species formed from methanol versus MeOAc. Accordingly, we turned to INS spectroscopy to observe the lower frequency vibrational spectra. Figure 6 shows INS spectra of the blank zeolite, the zeolite containing MeOAc adsorbed at room temperature, and a sample of pure MeOAc. The spectra are normalised with respect to the weight of the sample. The dosed MeOAc on ZSM-5 shows that the MeOAc remains intact on the ZSM-5 with all the major peaks distinguishable. The peaks become broadened and less intense which could be attributed to the confinement effects of the MeOAc inside the zeolite structure. The blank ZSM-5 spectrum is shown as a reference, showing that the zeolite contribution to the spectra is   Figure 7 shows spectra recorded over the same frequency range for the used catalyst samples. As with the infrared spectra in Fig. 5, the intensities of the bands due to hydrocarbon coke species increase with increasing MeOAc content in the feed. This trend additionally reflects that observed for retained coke content (Table 1). No evidence of features attributable to surface bound methyl acetate entities is apparent in either the IR or INS spectra.

Inelastic Neutron Scattering
Interestingly, the spectra measured from catalysts exposed to 30% or more MeOAc resemble those previously reported for HZSM-5 zeolite catalysts reacted with dimethylether at 350 °C [15] and importantly have no correspondence to the spectrum of adsorbed MeOAc (Fig. 6). For example, the doublet at 1370 and 1456 cm −1 in Fig. 7 is respectively assigned to CH 3 symmetric and asymmetric bending modes of methyl groups attached to aromatic rings and both features are present in all of the spectra except that of the 0% MeOAc catalyst. A band at 1186 cm −1 is present  Fig. 6 INS spectra of the blank zeolite (black), methyl acetate (orange) and methyl acetate exposed to ZSM-5 at ambient temperature (grey) 1 3 in all spectra, and appears to grow together with the 1370, 1456 cm −1 doublet, suggesting it is associated with the same species. Likewise, the lower frequency bands are similar to those seen with dimethylether as the reactant [15]. Some differences in relative intensity are noted: bands between 800 and 1000 cm −1 are assigned to aromatic CH out-of-plane bending modes which are less intense in Fig. 7 relative to the 1033 cm −1 band due to CH 3 rocking modes compared with the spectra of the dimethylether catalysts [15]. We attribute these differences to a greater degree of methylation of the aromatic rings in the presence of MeOAc. Highly methylated aromatics have been linked with ZSM-5 deactivation [19,25], which could explain why the increase in MeOAc has also nudged the catalyst in to a deactivation stage earlier than is seen with either methanol or DME. This enhanced extent of methylation in the adsorbed aromatic hydrocarbons appears to be the only significant difference in the INS spectra between the coke deposits formed in the presence and absence of MeOAc.

Discussion
Methyl acetate has been included in the methanol feedstream and its role in MTH chemistry over HZSM-5 considered. Methyl acetate additions over the range 10-100% are seen to modify the product distribution of low molecular weight olefins plus aromatic compounds and perturb methanol conversion. The ester appears to accelerate catalyst deactivation by enhancing the formation of methylated aromatic coke compounds that block active sites within the zeolite. Müller et al. [26] have suggested that initial coke formation in ZSM-5 is enhanced by the presence of oxygenated compounds, but the vibrational spectroscopic data show no evidence for the presence of anything other than methylated aromatics in the used catalysts studied here, and the TPO data show no sign of the Type I coke observed in reference [26]. One possible origin for the deactivation trends observed could be that the presence of methyl acetate in the feedstream leads to a constrained supply of water molecules in the reaction zone (formed as a product in the dimerization of methanol to produce dimethyl ether), which would otherwise facilitate re-generation of the active sites (Brønsted acid sites) [15].