Received Date: March 05, 2017; Accepted Date: May 09, 2017; Published Date: June 15, 2017
Citation: Pardo-Tarifa F, Cabrera S, Sanchez-Dominguez M, et al. Synthesis and Characterization of Novel Zr-Al2O3 Nanoparticles Prepared by Microemulsion Method and Its Use as Cobalt Catalyst Support for the CO Hydrogenation Reaction. Synth Catal. 2017, 2:2.
For the first time binary Zr-Al oxide nanoparticles were synthetized by coprecipitation in water-in-oil microemulsion. For comparison, a similar material was prepared by Zr impregnation on commercial alumina. After calcination, these materials and unpromoted alumina were used as cobalt catalyst supports to study and compare their structural characteristics and catalytic behavior in CO hydrogenation reaction. The supports and final cobalt catalysts were characterized by X-ray diffraction (XRD), N2 physisorption, scanning and transmission electron microscopy (SEM and TEM), temperature programmed reduction (TPR) and H2 chemisorption. The material synthetized by microemulsion (Zr-Al2O3 (ME)) presented homogeneous nanoparticles with highly dispersed zirconium, textural porosity with narrow pore size distribution and high surface area. On the other hand, the material prepared by Zr impregnation on Al2O3 (Zr-Al2O3 (IM)) produced a nonhomogeneous material with low Zr distribution and structural porosity. The cobalt deposition on these supports seems to be affected by the presence of zirconium. In the presence of highly dispersed Zr on alumina, the cobalt interaction with the support is higher. On the other side, the presence of ZrO2 islands on alumina avoids the cobalt-support interaction favoring the cobalt reduction degree, which makes a more active catalyst in the tested reaction. The final catalysts were tested in CO hydrogenation, and a higher CO conversion was obtained with increased Co° availability on the catalyst surface. Furthermore, the selectivity was affected by the CO conversion and the physico-chemical properties of the catalyst. This study gives highlights on the synthesis of highly uniform bimetallic nanoparticles used as support for cobalt catalysts and their application.
Zr-promoter; Zr-Al2O3; Water-in-oil; Microemulsion method; Cobalt catalyst; Co3O4 reducibility; CO hydrogenation
In the search for highly active and selective catalysts for the CO hydrogenation reaction, all elements in metallic form from group VIII are able to chemisorb and dissociate CO and H2. However, only Ru, Co, Fe, and Ni are considered for use in commercial applications . Fischer-Tropsch synthesis (FTS) is an exothermic reaction between H2 and CO producing water and a wide variety of hydrocarbons in gas, liquid, and solid state used as fuels and chemicals [2,3]. Supported cobalt based catalysts have been used for FTS due to their higher activity, high selectivity to linear hydrocarbons, and low activity for water-gas shift (WGS) reaction [4,5]. The activity and selectivity of cobalt catalysts are dependent on metal dispersion and reduction degree, support and promoter. The interaction of cobalt and alumina is high and promoters have been incorporated in order to avoid metal-support interactions [6,7].
Zirconium seems to increase the performance of Co/Al2O3 catalysts [7-14]. Some authors attribute its promotion effect to the increase of active intermediates (-CH2-) which causes an enhancement of the catalyst activity and the selectivity to long-chain hydrocarbons . Other authors found that Zr enhances the cobalt reducibility and consequently the catalyst activity [13,16,17]. On the other hand, as important as the choice of the promoter is the choice of the synthesis method. Considering the relevance of the synthesis procedure for obtaining promoted alumina supports, the microemulsion preparation method is a promising strategy. It allows the synthesis of highly homogeneous materials with controlled structural properties and particle sizes . This methodology has been employed for preparation of metal nanoparticles, metal oxides and mixed metal oxides for catalytic and electrochemical processes [19,20]. The synthesis of inorganic nanoparticles in water-in-oil microemulsions is driven by microscopic micelles that act as nanoreactors where the nanoparticle synthesis occurs. A water-in-oil (W/O) microemulsion is a transparent or translucent solution which is optically isotropic and thermodynamically stable. It is made up of droplets of water surrounded by a continuous oil phase, where the interfacial tension between oil and water is overcome by the use of surfactants [18,21].
The synthesis of a variety of binary metal oxides has been studied as catalysts supports for several catalytic reactions and has shown good results due to a high homogeneity and intimate binary metal interaction. In addition, small size particles maximize the surface area exposed to the reactant, allowing more reactions to occur [22,23]
Based on the presented literature, the presence of Zr in alumina increases the CO hydrogenation reaction; however, the method of Zr incorporation into Al2O3 has not been fully investigated. In addition, binary oxide nanoparticles used as supports have given good results in different application . To the best of our knowledge, no Zr-Al nanoparticles co-precipitated by microemulsion method have previously been prepared and studied. Therefore the synthesis of Zr-Al oxide nanoparticles is an adequate candidate for preparing cobalt catalyst supports. The aim of this work is to synthetize as well as to study the characteristics of co-precipitated Zr-Al nanoparticles. At the same time understand how affect this material compared with similar ones on the cobalt deposition and further application as catalyst for CO hydrogenation reaction.
The co-precipitation of Zr-Al nanoparticles was accomplished by mixing two water-in-oil microemulsion solutions (microemulsion 1 (ME1) and microemulsion 2 (ME2)) (Table 1). ME1 contained Zr and Al precursors while ME2 contained the precipitating agent NH4OH. ME2 was added to ME1 dropwise under continuous stirring at 30°C until pH 9 was reached. The solution was kept at constant conditions for 12 h to complete the reaction. The final solution was destabilized with acetone and the solid product was separated by centrifugation and washed with acetone and water. The product was freeze-dried in order to avoid particle agglomeration. Afterwards, the product was calcined in air for 6 h at 550°C (heating rate 10°C/min). The obtained material was labeled as Zr-Al2O3 (ME).
|ME||Phase||Compound (s)||Composition (wt%)|
|Aqueous Solution||1 M (AlCl3·6H2O-ZrO (NO3)||7.9|
|molar ratio of Zr:Al=1:8)|
|Aqueous solution||NH4OH 38 wt%||7.9|
Table 1: Selected composition of the microemulsion systems.
For comparison, Al2O3 and Zr/Al2O3 were also prepared. A commercial pseudo-boehmite Al2O3 (Versal 250) was dried at 120°C for 5 h and calcined at 550°C for 6 h. Afterwards, an aqueous solution of ZrO(NO3)2 was prepared and added to the treated alumina by incipient wetness impregnation (molar ratio Al:Zr=8). The material was thermally treated in the same way as Zr-Al2O3(ME). The obtained material was labeled as Zr-Al2O3(IM).
The carriers (Zr-Al2O3 (ME), Zr-Al2O3(IM) and Al2O3) were dried at 120°C for 5 h prior to the 12 wt% of cobalt deposition. An aqueous solution of Co(NO3)2·6H2O with volume equivalent to the pore volume of each support was added to the supports dropwise. The carrier pore volume was determined by N2-adsorption technique. After metal impregnation, the materials were dried for 6 h at 120°C and calcined in air at 350°C for 10 h (heating rate: 1°C/ min). The final catalysts were labeled as Co/Zr-Al2O3(ME), Co/Zr- Al2O3(IM) and Co/Al2O3.
X-ray diffraction (XRD) of the fresh samples was performed on a Siemens D5000 X-ray diffractometer with Cu Kα radiation (40 kV, 30 mA). The measurements were recorded from 10° to 90° in the 2θ range using a step size of 0.020° and a step time of 12s for all the samples. The phases were identified by the Eva software (version 126.96.36.199, 2007). Crystallite sizes of Co3O4 were calculated using the Scherrer equation and assuming spherical particles . The Co° crystallite size was estimated from Co3O4 using the formula d(Co°)=0.75·d(Co3O4) [26,27]. The analyses were performed in a pressure interval between 20 and 510 mmHg. Chemisorption isotherms were extrapolated at zero pressure in order to determine the adsorption of hydrogen . The stoichiometry assumption was that two cobalt atom per molecule of hydrogen. The average particle size of Co°, was estimated according to d(Co°)H=96 D · DOR, assuming spherical shape [29,30].
Brunauer–Emmet–Teller (BET) surface area and porosity data was collected with a Micromeritics ASAP 2000/2020 unit. 0.2 g of the samples was outgassed at 250°C overnight prior to analysis. The data was recorded by N2 adsorption at liquid nitrogen temperature at relative pressures between 0.06 and 0.2.
The reducibility of the catalysts was investigated by hydrogen temperature-programmed reduction (H2-TPR) . The calcined catalysts (0.15 g) were studied in a Micromeritics Autochem 2910 at a flow of 5 vol% H2 in Ar in a range of temperatures from 30°C to 930°C (heating rate: 10°C/min). The H2 consumption was monitored during the study by the difference in thermal conductivity between the inlet and outlet gases. The degree of reduction (DOR, %) was calculated using H2-TPR of the in situ reduced catalysts. 0.15 g of the fresh catalyst was reduced at 350°C (1°C/min) for 16 h in flowing H2, then flushed with helium gas for 30 min. Afterwards, the helium was changed to 5 vol % H2 in Ar and the temperature was increased from 350 to 930°C (10°C/min) and the H2 consumption was monitored. The TCD was calibrated with Ag2O as standard. The DOR was calculated assuming that unreduced cobalt after the reduction pre-treatment was in the form of Co2+ according to:
where ATCD is the integration of the TCD signal, normalized per mass catalyst; AWCo is the atomic weight of Co (58.9 g/mol), f is a calibration factor correlating the area of the TCD signal and the H2 consumed; XCo is the cobalt loading (12% Co).
The cobalt dispersion (D, %) and the cobalt crystallite size (d(Co°), nm), was calculated by hydrogen static chemisorption on the reduced catalysts. The measurements were performed on a Micromeritics ASAP 202°C unit at 35°C, after reducing about 0.15 g of the fresh catalysts under the same conditions as in TPR analysis (H2 flow at 350°C for 16 h (heating rate: 1°C/min)).
The morphology of the supports and final catalysts was studied by high resolution-scanning electron microscopy (HR-SEM) using an XHR-SEM Magellan 400 instrument supplied by the FEI Company. The samples were investigated using a low accelerating voltage and no conductive coating.
Transmission electron microscopy (TEM) analysis was performed using a Philips CM300UT-FEG electron microscope with a point resolution of 0.17 nm, information limit of 0.1 nm, which was operated at 200 kV, in which images were acquired with a TVIPS CCD camera. The samples were prepared by immersing a Quantifoil R copper micro grid in a fresh catalyst dispersed in ethanol.
CO hydrogenation was tested at operating conditions similar to Fischer-Tropsch synthesis. Experiments were performed in a stainless-steel fixed-bed reactor (i.d. 9 mm) at process conditions: 210°C, 20 bar, molar H2/CO ratio=2.1. A mixture of 1 g of catalyst with a pellet size between 53–90 μm was diluted and mixed with 5 g of SiC (for an even temperature profile) and thereafter placed in the reactor [28,32]. Prior to the reaction the catalyst was activated by reducing it in situ with hydrogen at 350°C for 16 h at atmospheric pressure. After activation, the reactor was cooled down to 180°C and then flushed with He before increasing the pressure to 20 bar. The catalysts were tested during two periods, first at a syngas flow of 100 cm3/min (NTP) and in the second period the gas flow was adjusted in order to obtain a CO conversion of 30% [7,32-34]. The heavy hydrocarbons and most of the water were condensed in two traps kept at 120°C and room-temperature, respectively. The product gases leaving the traps were depressurized and analyzed on-line with a gas chromatograph (GC) Agilent 6890 equipped with a thermal conductivity detector (TCD) and a flame ionization detector (FID). H2, N2, CO, CH4, and CO2 were separated by a Carbosieve II packed column and analyzed on the TCD. The percentage of CO conversion was calculated by:
C1–C6 products were separated by an alumina-plot column and quantified on the FID detector, from which it was possible to determine the C5+ selectivity (SC5+). The CO2-free SC5+ (i.e., SC5+ if excluding CO2 from the C-atom balance) is defined as follows [28,32]:
Zr-Al co-precipitated in water-in-oil microemulsion: Several microemulsions were prepared in order to define the composition and temperature of the water/surfactant/oil (W/S/O) system at which the microemulsion was formed and stable. The selected weight ratio in percentages was 7.9/26.4/65.7 (Table 1). The Zr- Al2O3 precursor was formed by collision and coalescence of water droplets between microemulsions 1 and 2 (ME1 and ME2). Oxo-hydroxo complexes of zirconium and aluminum were produced when the base came in contact with the metal initiating the nucleation and formation of the first particles inside the water droplets [18,35]. The simultaneous co-precipitation of the precursors inside the water droplets favored in this way a good dispersion of Zr in alumina, and uniform growth of the particles. In addition, the EDX spectra of the material showed Al/Zr/Co atomic ratios (Table 2) similar to the added metals. These results show that both Zr and Al precipitated during the synthesis and no loss of metal was detected.
|Material||Al/Zr Atomic ratio||Al/Co Atomic ratio|
Table 2: Representative EDX elemental analysis of the supports and the catalysts.
Wetness impregnation: The commercial alumina used as support has a pseudo ϒ-Al2O3 porous structure. This framework allows the deposition of zirconium first and after cobalt oxides inside the pores and on the surface of the alumina. During the calcination step, decomposition of the precursors and reactions between the Zr, Co and ϒ-Al2O3 might occur.
Characterization of the materials
X-Ray diffractograms: The X-ray diffractograms of the carriers and Co-catalysts are illustrated in Figure 1. The Zr‑Al2O3(ME) support presents a low crystalline of ϒ-Al2O3 phase. In addition, no Zr species were detected which might be attributed to the applied synthesis method. One explanation could be that Zr is encapsulated in the alumina matrix and consequently Zr oxide species crystal formation was inhibited [36,37]. In contrast, the Zr- Al2O3(IM) material presents characteristic peaks for ϒ-Al2O3 and a band at 2θ=32° assigned to a metastable ZrO2 with orthorhombic structure (Figure 1).
After Co deposition, the XRD patterns (Figure 1 right) showed that highly crystalline Co3O4 species were formed in all the catalysts with similar crystallite sizes of approximately 11 nm (Figure 1 and Table 3). Thus, it can be concluded that the presence of Zr does not affect the Co3O4 particle size.
|BET Surface area (m2/g)||Total Pore volumea (cm3/g)||Average Pore diameter (nm)b||Particle size Co3O4 (nm)c||Particle size Co° (nm)d||Particle size Co° (nm)e||Metal Dispersion %Df||DORi|
Table 3: Physicochemical characterization of the supports and catalysts (aDetermined from a single point of adsorption at P/P0=0.998; bEstimated by BJH formalism (adsorption branch); cAverage crystallite size of Co3O4 estimated from Scherrer equation; dAccording with: d(CoO)= 0.75·d(Co3O4); eAccording to: d(CoO)H= 96·DOR; fMetal dispersion, after reduction at 350°C for 16 h in H2; iDegree of reduction (DOR) from TPR of reduced catalysts).
N2 physisorption: The catalyst porosity is presented in Figure 2. The isotherms correspond to type IV . The hysteresis loop for Co/Zr-Al2O3(ME), corresponds to type H2(b) , associated with complex pore networks consisting of pores with ill-defined shapes in the mesopore range. Materials with textural porosity formed by voids between particles can be associate with type H2(b). In addition, this material showed narrow pore size distribution. Co/ Zr-Al2O3(IM) and Al2O3 supports showed type H3 hysteresis loop , correspondent to materials with non-rigid aggregates and wide pore size distribution like amorphous alumina. The carrier isotherms were similar and therefore not included in Figure 2.
The surface area for all materials was between 190 and 248 m2/g (Table 3). Incorporation of Co and/or Zr phases on alumina leads to a decrease in BET surface area and pore volume (Table 3), due to partial pore blockage of the deposited oxides inside the pores [39,40]. The Co3O4 particle size was smaller than the Al2O3 and Zr-Al2O3(IM) pore sizes, therefore Co3O4 deposition is favored inside the pores. On the other hand, Zr-Al2O3(ME) had smaller pore diameter size than the Co3O4 particles (Table 3), which leads to the conclusion that some of the Co3O4 was deposited on the carrier surface.
Scanning and transmission electron microscopy: The Zr- Al2O3(ME) and Co/Zr-Al2O3(ME) morphology (Figure 3) showed non-agglomerated uniform particle size distribution. However, Co/Al2O3, Zr-Al2O3(IM) and Co/Zr-Al2O3(IM) showed heterogeneous spherical agglomerations of smaller particles of 120, 80 and 80 μm respectively. These agglomerations are attributed to Zr and/ or Co deposition. Zr-Al2O3(ME) does not agglomerate after cobalt deposition (Figure 3). Based on these findings, it is considered that Zr prevents particle agglomeration, especially when Zr is highly dispersed.
For a better understanding of the species and morphology in the promoted-catalysts, TEM pictures were taken (Figure 4). Co/Zr-Al2O3(ME) shows a homogeneous material formed by agglomerated nanoparticles. Co/Zr-Al2O3(ME) shows carrier particle sizes between 4-7 nm and Co3O4 cubic crystals (Figure 4a). STEM-EDX mapping results show a homogeneous distribution of Zr on Co/Zr-Al2O3(ME) (Figure 4a). This picture demonstrates how the ME technique can be applied for the synthesis of highly disperse oxide promoter on a carrier. The Zr dispersion on alumina in Co/Zr-Al2O3(IM) (Figure 4b) was lower, forming Zr-rich islands on the Al2O3 surface. Furthermore, the cobalt deposition seems to be better in the ME material than in the Zr-impregnated material.
H2-Temperature programmed reduction: A typical TPR profile for all the catalysts is shown in Figure 5. In general, the first two peaks correspond to the reduction of Co3O4 + H2 → 3CoO + H2O  and 3CoO + 3H2 → 3Co0 + 3H2O . The peak around 700°C is attributed to Co3AlO6 (Co3O4-AlO2) and/or CoO-Al2O3, and the peak at 900°C corresponds to CoAl2O4 [43-45].
Co3O4 in Co/Zr-Al2O3(ME) was harder to reduce, as a consequence the reduction temperature was shifted towards higher temperatures compared to the other catalysts. The lack of crystallinity in the ME carrier favored the cobalt-aluminate formation and also its reduction temperature.
The TPR for Co/Zr-Al2O3(IM) presents similar peaks as for Co/Al2O3 with the difference that the reduction temperature was lower by about 50°C. In addition an extra H2 uptake is seen at 608°C which can correspond to the partial reduction of Zr. The amount of cobalt aluminate species was decreased compared with Co/Al2O3, attributed to the presence of Zr. CoAl2O4 (spinel) was not detected by the XRD technique since its diffractogram peaks overlaps with the Co3O4 peaks.
Additionally, TPR experiments (Figure 5 right) were performed after the catalyst activation in order to identify the unreduced cobalt amount and consequently the degree of reduction (DOR) (i.e., from 350 to 930°C in H2). Co3O4 in Co/Zr-Al2O3(IM) is completely reduced after catalyst activation with a DOR of 70%, while the DOR for Co/Al2O3 and for Zr-Al2O3(ME) is 30 % and 11%, respectively (Table 3 and Figure 5). Thereafter, it can be concluded that the presence of Zr in islands as is the case of Co/ Zr-Al2O3(IM) decrease the cobalt-alumina interactions, favoring in this way a more metallic formation which is required for a CO hydrogenation reaction.
Interesting to note in all the catalysts (Figure 5 right) is that the unreduced cobalt species (peaks around 700 and 900°C) shifted the reduction temperature to higher temperatures compared with the first TPR analysis (Figure 5 left). The explanation given is that during catalysts activation, the remaining unreduced-cobalt in the form of Co° interacts with water (produced by the metal reduction) to form Co-aluminate which is reduced at a higher temperature .
Table 3 presents the dispersion of metallic cobalt Co° calculated by H2 chemisorption (see experimental part). The results show that Co° dispersion is quiet similar in Co/Zr-Al2O3(IM) and Co/Zr- Al2O3(ME). This results compared with Co/Al2O3 are higher, so it is concluded that Zr favors the dispersion of cobalt in alumina support. In addition, the measured Co° particle size by this technique and by TEM is higher than the calculated from the Scherrer equation, from which it can be concluded that during catalyst activation the metallic particles are sintered. This effect is higher in Co/Zr-Al2O3(ME) and one of the explanations might be due to the textural porosity and the lack of structural porosity which makes the cobalt-sintering easier.
Comparing CO conversions for all the catalysts after 25 h of syngas stream (H2:CO=2.1) (Table 3), the catalyst activity decreases in the following order: Co/Zr-Al2O3(IM)>Co/Al2O3>Co/Zr-Al2O3(ME). The results are related to: the higher the DOR (degree of reduction of Co) the higher the CO conversion in period one (Table 3).
In all the cases, the selectivity is affected by the CO conversion; the higher the CO conversion, the higher the C5+ selectivity (SC5+) and as a consequence the selectivity to CH4 and C2-C4 are decreased. The selectivities to CH4 and C2-C4 were higher for the ME catalyst during both periods; this might be attributed to two facts: low Co0 formation in the Co/Zr-Al2O3 (ME) catalyst and the small pore size of the carrier, around 4 nm, leading to internal mass transfer limitations favoring the faster H2 diffusion due to its smaller size compared to the CO molecule which diffuses more slowly. This led to higher H2/CO ratios within the catalyst particles than at the pellet surface.
For the first time, Zr-Al oxides nanoparticles were synthetized by the water-in-oil microemulsion method. The material presented a high Zr dispersion in alumina and it was highly homogeneous with uniform particle sizes, narrow pore size distribution and high surface area. This material was used as cobalt support and compared with similar material prepared by Zr impregnated on commercial alumina. The presence of ZrO2-islands on alumina favored the dispersion and degree of reduction of cobalt, while the high Zr dispersion in the Zr-Al2O3 (ME) material hindered ZrO2 crystallization. This produced producing a more amorphous material, leading to a higher degree of CoAl2O4 formation and therefore increased selectivity to methane and short-chain hydrocarbons C2-C4. The catalytic activity and SC5+ is favored by the Co/Zr-Al2O3 (IM) catalyst. These results are attributed to the catalyst porosity and higher Co0 availability on the surface. However, even if the cobalt on Zr-Al2O3 nanoparticles catalysts (prepared by water-in-oil microemulsion) are not the best for use in CO hydrogenation reaction where a high C5+ selectivity is desired; the material has very good properties to be considered for other applications: such as base material in three-way-catalysts; or as catalyst support for other catalytic reaction like hydrodesulphurization, or to stabilize alumina phases when it is used at high temperatures.
Swedish International Development Cooperation Agency (SIDA), Nanoandes network and European project COST Action: CM1101 for financial support. Special thanks to Dr. Emanuela Negro (Deft University of Technology), Edgar Cardenas (Luleå University) and Cesar Leyva Porras (CIMAV, S.C.) for measurements of TEM, SEM and HRTEM/STEM.
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