Energy supply, its conversion and storage in a way that essentially protects the environment are of the great challenges for human being in the 21st century. For many years, the vast mankind consumption of fossil fuels (crude oil, coal and natural gas) as primary energy basis owing to their high energy density values and easy accessibility. However, this global pattern of energy source is unbalanced. In addition to the limited fossil-fuel supplies, the global warming issue demands a radical change in finding the renewable energy sources .
Dimethoxymethane (DMM), also recognized as methylal, with chemical formula of C3H8O2 is a commercial chemical compound which has various applications in chemical industries. This compound can be achieved from methanol which produced itself from biomass. The methanol mainstream is presently gained from natural gas-based and coal-based synthesis gas (syngas) [2-6]. DMM and POMM are deliberated as substitute fuels for low-temperature fuel cells which are much safer than methanol, due to, e.g. seldom toxicity of DMM and POMM lower volatility [7,8]. Furthermore, concentrated formaldehyde solutions can be gained through the selective oxidation of DMM into formaldehyde compared to the conventional method (methanol to formaldehyde conversion) . As a significant usage, DMM has been applied as an oxygenated additive to diesel fuel, especially reducing particle emissions, which is a serious danger for the human health [10,11].
DMM is conventionally fabricated by acetalization of formaldehyde and methanol over acidic catalysts. Nevertheless, mentioned method includes sophisticated procedures, severe corrosion of equipment, and high reaction temperature [12,13]. In addition, one step selective oxidation of methanol to DMM owing to the economic and environmental advantages of the process has attracted much attention . In this context, improvement of the selective catalysts for the one step methanol to DMM partial oxidation is an exciting issue, and has gained great concern in the recent years [6,14]. Selective methanol oxidation to DMM characteristically includes two steps: methanol oxidation to formaldehyde on redox sites and formaldehyde condensation with another methanol molecule to form DMM on acidic sites of catalyst [13,15]. To achieve high DMM yield, a suitable bifunctional catalyst with balanced redox ability and acidic sites is demanded. Excessive redox property and insufficient acidic sites can lead to the abundant amount of methyl formate (MF) and oxycarbide, while extreme acidic sites would output a great amount of dimethyl ether (DME) [12,16]. A variety of catalysts such as iron molybdate mixed oxides , molybdenum-based catalysts , ruthenium oxides , rhenium oxides [19,20], heteropolyacids (HPAs) , and vanadium-based catalysts [22,23] have been employed for one step methanol oxidation to DMM.
Newly, Mickael Capron et al. have established one-step gas phase selective methanol conversion to DMM using a mixed iron molybdate oxides as a catalyst with low surface area, about 10 m2g−1, synthesized by the coprecipitation method. This catalyst in a fixed-bed reactor under unusual reaction conditions showed the highest productivity ever observed in the direct conversion of methanol to DMM (4.6 kg DMMh−1 kgcat−1 at 553 K) .
Metal-organic frameworks (MOFs) are innovative class of highly porous hybrid materials assembled with inorganic cation or clusters coordinated [24,25]. MOFs with tridimensional framework have ultimate characteristics such as porous structures with high surface area, tunable pore size, crystalline open structure and suitable thermal stability [26,27]. One of the main applications of MOFs is their catalytic activity. There are numerous investigations based on theusage of MOFs as catalysts or catalyst support systems [28, 29]. Also MOFs have been used as precursors for preparation of nano-sized materials such as porous carbon [30,31] and metal oxides [32,33]. Finding the nano-sized materials with desired morphologies will become possible by selecting suitable MOF precursors with distinct morphologies under suitable operational situations .
In addition to the aforementioned benefits of the one step oxidation of methanol to DMM, the goal of this work is to advance the performance of Fe-Mo catalyst by using metal organic frameworks as precursors to synthesize catalysts with high surface area with different morphologies. For this purpose, MIL-100(Fe) and MOF-235 was synthesized as precursors for Fe(III) while (NH4)6Mo7O24·٤H2O was employed as a Mo(VI) precursor. The fabricated catalysts were characterized to use for one step production of DMM from methanol.
Materials and apparatus
All chemicals used in this project were of analytical reagent grade and purchased from Merck Company without any purification. Fe(III) and Mo(VI) contents were determined by inductively coupled plasma optical emission spectroscopy (ICP-OES) (Shimadzu ICPS-7000, Japan). For all X-ray diffraction (XRD) patterns reported in this study, XRD was performed under atmospheric conditions with a Philips X-Pert. FTIR spectra were documented by a Bruker IFS-66 FT-IR Spectrophotometer (Karlsruhe, Germany). Brunauer-Emmett-Teller (BET) surface area measurements and pore volumes were performed by Belsorp mini II Bel (Japan). Scanning electron microscopy (SEM) was performed by gently distributing the sample powder on the stainless steel stubs, using an SEM (KYKY-3200, Zhongguancun Beijing, China) instrument. Transmission electron microscopy (TEM) analysis was performed by LEO 912AB electron microscope. The elemental analysis of samples was achieved by energy-dispersive X-ray spectroscopy (EDX) (30XL, Philips Company, Holland). Catalyst process evaluation was performed in a catalyst testing system with a fixed bed reactor which was used in earlier work . Dynamic light scattering (DLS) technique was widely employed for sizing NPs in liquid phase using a BI-200 SM Goniometer Version 2 (Brookhaven Instrument Corp., Holtsville, NY, USA). The light scattered by the NPs was distinguished at 173◦, in dynamic laser scattering. For electrophoretic mobility quantification, which is a correlation between the NPs velocity and the electric applied field, size distribution and mean size were considered. Also, zeta potential was restrained by DLS method and was used to investigate the stability of nanoparticles against aggregation.
Synthesis of MOF-235
MOF-235 was prepared under autogenous pressure according to the previous reported method . 0.21 g terephthalic acid (1.23 mmol) was dissolved in 60 ml DMF by stirring for 10 min. Afterward, 0.20 g FeCl3·٦H2O (0.74 mmol) was added to the mixture and stirred for 5 min. At that moment, 30 ml of reaction mixture with 30 ml ethanol were moved to a Teflon-lined autoclave, sealed and placed in a preheated electric oven (353 K) for 12 h. Finally, an orange powder (MOF-235) was attained which was recovered by centrifugation and washed with a DMF-ethanol mixture at least three times. Afterwards, it was dried overnight at 423 K to eliminate DMF.
Synthesis of MIL-100 (Fe)
MIL-100(Fe) was produced at low temperature synthetic method (3, trimesic acid, metallic iron, and H2O were employed as reagents, then, a solution of Fe:trimesic acid:HF:HNO3:H2O with composition of 1.0:1.0:2.0:0.5:100 was transferred into a PTFE flask while refluxed at 368 K for 12 h under vigorous stirring. After crystallization, the achieved powder was adequately purified by hot deionized water followed by drying at vacuum .
Synthesis of Fe-Mo catalysts
Iron molybdate catalysts with Mo:Fe mol ratio of 3:1 was produced with the aid of coprecipitation method. An aqueous solution containing 1.0 mol (NH4)6Mo7O24·٤H2O (AHM) and 2.3 mol FeCl3·٦H2O was prepared according to the previous procedure . Initially, the (NH4)6Mo7O24·٤H2O solution (pH ∼ 5) was acidiﬁed with HCl to pH ~ 1. Afterwards, FeCl3·٦H2O solution was added drop wise for 30 min to the AHM solution at a temperature kept in the range of 323-333 K under vigorous stirring. The yellowish precipitate was agitated for 60 min in its mother liquor. Afterwards, the precipitate was recovered by decantation for several times to remove of chloride ions. As a final point, the precipitate was ﬁltered and dried at 383 K for 4 h. The dried precipitate was calcined at 723 K for 2 h to produce Fe-MoI catalyst. The other catalysts were synthesized with MOF-235 and MIL-100(Fe) precursors and named as Fe-MoII and Fe-MoIII, respectively. An aqueous solution containing 1.7 mol AHM and 1.0 mol MOF-235 were employed for synthesis of Fe-MoII catalyst. On the other hand, 1.3 mol AHM and 1.0 mol MIL-100 (Fe) were used for the synthesis of Fe-MoIII catalyst. The resultant precipitates were maintained under vigorous stirring for 2 h to achieve homogenous solutions, and then, the mixtures evaporated at 303 K to dry. The attained precipitates were calcined at 723 K for 3 h. All catalysts’ colors were light green, and the yields of products were 72 %, 58% and 63% for Fe-MoI, Fe-MoII and Fe-MoIII catalysts, correspondingly.
RESULT AND DISCUSSION
Characterization of the catalysts
FT-IR spectra of MIL-100(Fe), MOF-235, FeMoI, FeMoII and FeMoIII were recorded by KBr pellet method. The peaks were attributed to C=O stretching vibration at 1713 and 1684 cm−1 in MIL-100(Fe) and MOF-235 indicating the presence of carboxylate linkers in their frameworks. The absorption bands due to C=C (1447, 1575 cm-1) and C-H aromatic (3065 cm-1) established the MIL-100(Fe) compound synthesis . Furthermore, the FT-IR spectrum of MOF-235 comprises of the main vibrational bands at 554 cm-1 (Fe-O), 1110 and 776 cm-1 (C-H vibration of aromatic ring), 1286 cm-1 (C-O-C), and 1421 and 1568 cm-1 (C=C aromatic) which are in agreement with earlier reported values for MOF-235 . The main characteristic bands at 853-894 cm-1 (Fe-O) and 612-635 cm-1 (Mo-O) in the FT-IR spectrum of catalysts were illustrated. This showed that the synthesis of all catalysts was performed properly.
SEM, EDX, TEM and DLS
The surface characterization results of Fe-MoI, Fe-MoII and Fe-MoIII morphology were achieved by SEM and TEM techniques accomplished by EDX analysis (Fig. 1 and Fig. 2a,b). EDX is an important non-destructive analytical tool typically useful for the chemical composition; it is one of the electron microscopy procedures used for semi-quantitative analysis (bulk chemical elemental analysis) using the backscattered electron mode. The bulk sediments were analyzed by EDX at low magnification by averaging the results of several spots. SEM-EDX analysis is frequently employed to afford qualitative chemical analyses of elements present in the samples. As shown in Fig. 1 and Figs. 2a, and b, when metal organic frameworks are employed as precursors, the particle size of catalysts are reduced compared to Fe-MoI particles synthesized from (NH4)6Mo7O24·٤H2O (AHM) and FeCl3·٦H2O directly. The SEM micrograph of Fe-MoI showed a non-uniform and disordered structure, while Fe-MOII and Fe-MOIII have nanorod and nanoparticle morphologies, respectively. The Fe-MoII and Fe-MoIII have more porosity compared with Fe-MoI structure (proved by BET and TEM microscopy), so more catalytic activity is expected. Size distribution histogram of the catalysts displays a relatively uniform distribution for Fe-MoII and Fe-MoIII nano catalysts while Fe-MoI catalyst shows non-uniform distribution of particles. Particle size can be measured by determining the random variations in the light intensity scattered from solution. This technique is generally identified as dynamic light scattering (DLS) but is also named photon correlation spectroscopy (PCS) and quasi-elastic light scattering (QELS). The size of nanoparticles was explored by DLS as can be seen in Fig. 2c (for Fe-MoII catalyst as the best catalyst). In general, the nanoparticle size spans the range between 70 and 86 nm. In addition, zeta potential was restrained by DLS technique and was used to consider the stability of nanoparticles against aggregation. NPs with a zeta potential ~ +/-30 mV have been exposed to be steady in suspension, as the surface charge inhibits aggregation of the particles (Fig. 2d).
X-ray diffraction patterns
The crystalline structure of MOFs and prepared catalysts were investigated by XRD technique (Fig. 3). The MOF-235 XRD pattern (Fig. 3b) exhibited high crystallinity with reflection patterns in the range of 5-40˚ (2θ). The main characteristic peaks at 2θ = 9.8, 10.6, 12.8, 17, 19 and 23 were similar to MOF-235 standard data confirming the synthesis of MOF-235 . As depicted in Fig. 3a, the MIL-100(Fe) diffraction patterns are observed in a small angle domain similar to published XRD patterns indicating the formation of MOF . For Fe-Mo catalysts, three phases are expected; Fe2(MoO4)3, MoO3, and β-FeMoO4 components. The presence of three phases was approved by XRD analysis which is in accordance with the published literature  (Fig. 3c).
ICP-OES was regularly performed for the elemental analysis in a wide range of sample matrices for many years due to its relative ease of use, flexibility, low detection limits and low cost. Furthermore, it needs shorter analysis time when equipped with a simultaneous-CCD detector (charge coupled device) as the one available in our laboratory. The ICP-MS measurements of fabricated catalysts were done in order to determine Mo:Fe ratios. The obtained Mo:Fe ratios were 2.9, 2.8, 2.8 for Fe-MoI, Fe-MoII, and Fe-MoIII, respectively, which are in a good agreement with the theoretical ratio of 3:1 (see Table 1).
BET surface area, Mo:Fe ratio, measured from ICP-MS and total pore volume of all catalysts are displayed in Table 1. The surface area of MOF-235 and MIL-100(Fe) were 981 and 1678 m2g-1, respectively, according to previous reports [36,37]. These values decreased to 175 m2g-1 (total pore volume=0.38 cm3g-1) and 213 m2g-1 (total pore volume=0.46 cm3g-1) for Fe-MoII and Fe-MoIII that are derived from MOF-235 and MIL-100(Fe), correspondingly. The BET surface area of Fe-MoI was 8.9 m2g-1 (total pore volume=0.09 cm3g-1) meaningfully lower than Fe-MoII and Fe-MoIII. Fig. 4 demonstrates the nitrogen adsorption-desorption isotherms of Fe-MoI, Fe-MoII and Fe-MoIII catalysts. According to IUPAC classification , the isotherm of Fe-MoI corresponds to nonporous and non-wetting solids (type III) with weak interaction between adsorbent and adsorbate. For Fe-MoII and Fe-MoIII, these isotherms correspond to type IV with an H3 hysteresis loop, characteristic of mesoporous structures with slit-shaped and non-rigid pores. The achieved data were established more porosity in the structure of Fe-MoII and Fe-MoIII compared with Fe-MoI. On the other hand, the catalytic activity of Fe-MoII was higher than that of Fe-MoIII which can be due to its nanorod structure. In fact, morphology of particles and shape of pores with different accessible active sites can be operative in activity of catalysts rather than the specific surface area only.
NH3–TPD technique affords information on the strength and amount of acid sites by using NH3 as a basic probe molecule. The peaks in the NH3–TPD profiles are classified to three types of acid sites with different acid strengths. The desorption peaks in Fig. 4d at ca. ~450 K is related to the weak acid sites.
Catalytic performance tests
Methanol conversion, DMM selectivity and DMM yield
In order to investigate the synthesized catalysts, at each experiment, 1.0 g of the catalyst was loaded into the reactor with stainless steel grid at both ends. For simulation of methanol:air condition, a ratio of CH3OH:O2:N2 with 40/13/47 mol % was chosen. The gas hourly space velocity (GHSV) was adjusted to 16 NLh−1gcat−1 (liquid methanol and air flow rates were controlled at 11 ml h-1 and 160 ml min-1, respectively). The experiments were done at 503, 523, 543 and 563 K and the liquid products were guided to GC analyzer (Teif-Gostar co, Iran). All experiments were completed at atmospheric pressure. The reaction products were analyzed every 30 min until stabilization. On the basis of the results, the catalyst was stabilized after about 5 h. The main byproduct of reaction was formaldehyde (F), therefor the other byproducts were discarded. Methanol conversion, DMM selectivity and DMM yield were calculated according to the utilized formulas.
Yield (%) =
(Methanol conversion × DMM selectivity) × 100 (3)
Fig. 5a represents the catalytic performances of the catalysts at 543 K, which was the optimal temperature for DMM production based on Mickael Capron et al.’s report . The methanol conversion gradually enhanced when reaction time increased. Fe-MoII and Fe-MoIII revealed the similar methanol conversion (ca 42 %), whereas Fe-MoI gave a 30 % conversion. The activity of Fe-MoII and Fe-MoIII catalysts were significantly higher than Fe-MoI, owing to their extra specific surface area with higher porosity compared to Fe-MoI.
The same trend was detected in the case of DMM selectivity evolution, which gradually increased with the reaction time up to 6 h (Fig. 5b). The highest DMM selectivity was perceived over Fe-MoII (92 %). Similarly, a high selectivity (87%) to DMM was achieved with Fe-MoIII. A significantly high DMM selectivity (85 %) was observed for Fe-MoI. The higher selectivity of Fe-MoII and Fe-MoIII can be explained by their higher surface area and active sites in comparison to Fe-MoI. DMM yield as a catalytic performance indicator also was investigated. As shown in Fig. 5c, when the reaction time increased from 1 to 7 h, the DMM yield was improved. Fe-MoII and Fe-MoIII offered higher DMM yield (39.56 and 34.4%) compared with Fe-MoI (24.65 %). Under this condition, DMM yield of Fe-MoII and Fe-MoIII was 39.56 and 34.4, respectively, which are much higher than that of Fe-MoI (24.65 %). All the prepared catalysts have the same Mo:Fe ratio (2.8-2.9), so higher performance of Fe-MoII and Fe-MoIII can be related to the more accessible active sites of these catalysts compared to Fe-MoI. A comparison between previous studies and the current study on methanol conversion, DMM selectivity and DMM yield is presented in Table 2.
Effect of the reaction temperature
Fig. 6 describes the reaction temperature effect on the methanol conversion over Fe-MoI, Fe-MoII, and Fe-MoIII catalysts. The main methanol oxidation products are DMM, formaldehyde, formic acid, methyl formate, and carbon oxides (CO and CO2) [39,40]. However, for the Fe-Mo catalyst, main products were DMM and formaldehyde. The temperature affects the products distribution significantly. The methanol conversion enhanced by increasing temperature from 503 to 563 K. All catalysts are similar in the variance tendency of the methanol conversion with the temperature. Nevertheless, Fe-MoII and Fe-MoIII give a better methanol conversion than Fe-MoI. Porous structures with higher surface areas of Fe-MoII and Fe-MoIII catalysts lead to surface acidity with enhanced quantity and suitable strengths, which can promote the condensation reaction and hence give a positive effect on the methanol oxidation to produce DMM.
Effect of gas hourly space velocity (GHSV)
GHSV effect was explored in the range of 20-30 NLh−1gcat−1. As shown in Fig. 7, methanol conversion decreased gradually with GHSV increasing from 20 to 30 NLh−1gcat−1. The same behavior was distinguished for the studied catalysts while the highest methanol conversion was achieved for Fe-MoII. Using metal-organic frameworks, as appropriate precursors, is an excellent approach to arrange catalysts with high surface areas and more accessible active sites.
In this study, as a novel strategy, two metal-organic frameworks namely MOF-235 and MIL-100(Fe) were employed as precursors to fabricate porous iron molybdate mixed oxide catalysts for the gas phase selective conversion of methanol to DMM using a mixture of methanol and air as reactants. Three different catalysts were synthesized by the coprecipitation of MOF-235, MIL-100(Fe) and FeCl3 with (NH4)6Mo7O24·٤H2O before being calcinated at 723 K in atmospheric pressure. MOF frameworks, as proper precursors, lead to formation of catalysts with higher specific surface areas, subsequently higher selectivity, and productivity. Excellent catalytic performance can be ascribed to the synergetic redox and acid properties presented in the Fe-Mo-O catalyst, and porous structures of the catalysts with high accessible acid sites (related to the consecutive partial oxidation and condensation reactions).
Author acknowledges the support rendered by the Iranian Research Organization for Science and Technology (IROST) and Iran Nanotechnology Initiative Council (INIC) for this study.
CONFLICT OF INTEREST
The authors declare that there is no conflict of interests regarding the publication of this paper.
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