Cerium Modified Pillared Montmorillonite Supported Cobalt Catalysts for Fischer Tropsch Synthesis.
Fischer-Tropsch (FT) synthesis was accomplished over Al-pillared Montmorillonite supported 20 wt% Co modified with different weight% of cerium catalysts. These catalysts were prepared by impregnation method while structural characterizations of the prepared samples were performed by XRD, TPR, NH3TPD, TGA, BET, XRF and SEM techniques. The Fischer Tropsch reaction was studied in fixed bed micro catalytic reactor at temperature range of 220, 260 and 275 oC and at different pressure (1, 5, and 10 bars). From the activity results, it was found that by pillaring NaMMT with Al higher catalytic activity and lower methane selectivity of NaMMT was achieved. Furthermore, the results of FT synthesis reaction revealed that cerium incorporation increased the dispersion of Co3O4 on the surface and consequently resulted in enhanced catalytic activity. Additionally, the C5-C12 hydrocarbons and methane selectivity increased while C22+ hydrocarbons selectivity was decreased over cerium modified catalysts.
Higher reaction temperature (greater than 220 oC) resulted in significant enhancement in CO conversion and methane selectivity. Though, increase in pressure from 1 to 10 bars eventually resulted in increase in C5+ hydrocarbons and decrease in methane and C2-C5 hydrocarbons selectivity.
Key Words: FT synthesis; Syngas; Cobalt; Cerium; Hydrocarbons; Montmorillonite
Fischer-Tropsch (FT) synthesis is an industrially well-known important process which deals with the conversion of syngas (H2/CO) into value added products. For this purpose, a variety of supported transition metal catalysts containing cobalt, iron and ruthenium have been extensively studied due to higher catalytic activity . Among them, cobalt have been preferred due the lower methane and higher C5+ hydrocarbons selectivity at high pressure and lower temperature .
The use of Co-based catalysts has attained considerable attention due to lower temperature FT synthesis  but the major drawback is the formation of higher molecular weight hydrocarbons (waxes) which result in blocking active sites of the catalyst and hence lowering of catalytic activity. The FT synthesis products over Co-based catalysts consist of multi component mixture of linear and branched hydrocarbons and oxygenated compounds. The hydrocarbons in the range of C22+ are called FT waxes, having higher boiling point and remain solid at lower temperature. Considerable progresses have been made towards the cracking of these higher hydrocarbon fractions to lower ones, in order to increase the overall conversion and selectivity of liquid hydrocarbons in FT synthesis. It was found that the active metals along with supports play an important role in FT synthesis that effect the activity and products selectivity of a catalysts dramatically [4, 5].
Recent studies showed that silica, alumina, titania and zeolite are the most extensively used supports in FT synthesis [4, 6]. However, considerable attention has been paid towards the use of bifunctional catalysts for the hydrocracking of long chain alkanes. Transition metals such as Co, Ni, Pt, Pd and bimetallic Ni/Co alloy systems have been extensively used over acidic supports such as ZSM-5, ZSM-22, mordenite, SAPO-31, SAPO-11, SAPO-41 for the hydrocracking of higher molecular weight hydrocarbon waxes. In active metal support systems, the role of acidic support is hydrocracking and hydroisomerization while transition metal provides a site of hydrogenation and dehydrogenation [7, 8].
It has been reported that Montmorillonite (MMT) clay has been widely used for hydrocracking catalysts in the petroleum industries as a support due its similar properties to those of zeolite [9, 10]. But the major drawback associated with MMT is its lower thermal stability and lower porosity which can be improved by modification or pillaring of MMT . Various methods has been employed for fabrication of Pillared montmorillonite (PILC) and one of them includes the exchange of cations of MMT with larger cations through the hydrolysis of metal salts or oxides. The hydrolysis process results into the formation of larger sized cations which can replace or exchange the cations already present in the interlayer of MMT .
Previously, the effect of MMT as a support for the iron FT catalyst have been explored but the main problem associated with this system is the production of unwanted products (methane and carbon dioxide etc) due to the complexity of metal oxide reduction to metallic state by MMT . So, there is an essential need to develop a catalyst with minimum production of methane and CO2. For this purpose, it is scrutinized that the use of MMT supported Co catalyst could result in increase of C2-C12 hydrocarbons selectivity and decrease in selectivity of C21+ hydrocarbons due to the cracking ability of MMT.
Furthermore, use of certain promoters with MMT supported catalyst can notably decrease the higher selectivity of CO2 and methane. Various metal promoters like Re, Pt and Ru and oxides promoters including ZrO2, CeO2 and La2O3 have been explored to increase catalytic activity and C5+ products selectivity of cobalt based FT catalysts [14-21]. Previously, CeO-Co/C has been reported as an efficient catalyst resulting in the lower methane, higher olefins and heavy hydrocarbons selectivity in the FT synthesis [20, 22]. The partial reduction of CeO2 results in the CO adsorption sites which are responsible for enhanced CO dissociation . Until now, little literature is available on the MMT supported cobalt catalysts for enhanced gasoline selectivity including hydrocarbons via hydrocracking of FT waxes. In current study the FT activity of MMT supported cobalt catalyst have been investigated thoroughly.
Furthermore, effect of different cerium incorporations on the activity and product selectivity has been explored during FT synthesis.
Sodium Montmorillonite (NaMMT), Aluminium chloride (AlCl3 .6H2O) and cobalt nitrate (Co(NO3)2.6H2O) from Sigma Aldrich while Cerium nitrate (Ce(No3)3.6H2O) from Merck were of analytical grade and were used without any further purification. NaMMT was selected as a starting material to prepare Al-PILC.
Preparation of Al-PILC and 20 wt% Co/Al-PILC
The Al-PILC and 20 wt% Co/Al-PILC were synthesized by our already reported method [4, 9].
Preparation of 20 wt% Co/Al-PILC with different Ce- loadings
Ce-Co/Al-PILC with 20 wt% Co containing 0.5, 1.0, 1.6 wt% Ce-loadings was prepared by wet impregnation method. The required amount of calcined pillared clay was dispersed into 0.1M solution of Co(NO3)2.6H2O and Ce(NO3)3.6H2O with constant stirring. The resultant suspension was evaporated at 40 oC through rotary evaporator, washed with distilled water, dried and calcined at 400 oC for 5h.
Characterization of Prepared Catalysts
The structural parameters of the prepared samples have been evaluated by X-ray diffraction (XRD) using Scintag XDS 2000 diffractometer. Textural parameters including BET surface area and pore volume have been acquired by Coulter SA 3100 analyzer using liquid nitrogen at a temperature of (78 K). H2-TPR and NH3-TPD profile was recorded on a TPDRO/1100 Series. Thermo gravimetric analyses (TGA) of all catalysts were carried out on Thermo Electron Corporation, Italy. Mettler TGA/SDTA 851e in the temperature range of 0-100 oC. Chemical composition and catalysts surface morphology was studied by SEM JEOL JSM 6490-A equipped with Energy Dispersive X-ray Spectrometer (EDX). JEOL Model JSX-3202M X-ray fluorescence was used for chemical composition determination.
The catalytic activity was conducted in a fixed bed micro reactor. The detailed procedure and setup for catalytic activity evaluation is described in our previously reported work [4, 9, 11].
Results and Discussion
Chemical Composition Analysis
The chemical composition of the naturally occurring clay NaMMT and our prepared samples i.e., Al-PILC and Ce-Co /Al-PILC was determined through XRF and given in Table-1.
Table-1: Chemical composition (wt%) of the prepared catalysts determined by XRF analysis.
###Samples###SiO2 Al2O3###Na2O Fe2O3 MgO Co2O3 CeO2
###NaMMT###55.6 30.3###4.41 2.3 5.3 -###-
###Al-PILC###53.1 40.4###less than 0.001 0.9 5.1 -###-
0.5 Ce -Co/Al-PILC###39.9 34.0###less than 0.001 0.8 5.1 19.3 0.8
1.0 Ce -Co/Al-PILC###39.3 33.9###less than 0.001 0.8 5.1 19.6 1.0
1.6 Ce-Co/Al-PILC 39.0###34.2###less than 0.001###0.8###5.1###18.5###1.7
It is obvious from the Table-1 that there is an increase in Al2O3 content of the clay from 30.1 to 40.4 which can be attributed to the complete substitution of Na cation present in MMT interlayer by Al2O3. However, Mg and SiO2 contents are almost same for all the Co-loaded MMT samples depicting no obvious change in the clay sheets composition.
The XRD pattern of NaMMT and AlPILC is already described in our previous work . Fig. 1 shows the XRD pattern of Ce-Co/Al-PILC. After pillaring of MMT with Al which replace the smaller cation in the interlayer of two dimensional MMT structure causes change in the gallery height and d001 basal plane . As can be seen in Fig. 1, there is an intense peak at 2 = 8 with basal reflection of 001, basal spacing of 12.06 A and a host layer thickness of 9.3 A . Gallery height of 3.3 A was calculated by subtracting the host layer thickness from the obtained basal spacing of the NaMMT which is similar to the previously reported value . The XRD spectra of Al-PILC gives diffraction planes at 8, 19.7, 35 and 61.8 which are characteristic of two dimensional layers structure of clay . The Al-PILC gives the 001 basal reflection at lower 2 value with increased d-spacing values i.e., from 12.06 to 18.7 A and increased gallery height i.e., from 3.3 to 9.4 A .
This effect may be due to the expansion of MMT layer structure as a consequence of pillaring which was similar to the reported value . However, the decrease in intensity of 001 peak of Al-PILC can be attributed to the intercalation of Al into the MMT clay interlayers. Moreover, no other structural changes or shifting of peak positions were observed in the XRD spectra of both the samples.
The presence of 001 diffraction peak, a basal reflection of Al-PILC is evident from the XRD pattern of Ce-Co/Al-PILC catalysts as shown in Fig. 1. While the small decrease in the 001 diffraction peak intensity was observed corresponding to the slight decrease in layered structure of MMT. XRD pattern of Ce-Co/ Al-PILC (Fig. 1) shows cobalt oxides (Co3O4) diffraction peaks at 19.5, 31.4, 36.9, 44.9 and 59.6 (JCPDS 65-3103) in all samples indicating a uniform dispersion of pure Co3O4 on pillared MMT . While no reflection peaks were observed for cerium in all samples thus confirming the high dispersion and lower content of cerium on Al-PILC surface .
The average crystallite size of the Co3O4 was determined by employing the Scherer equation and was found in the range of 30-40 nm. Furthermore, no reflection planes of cobalt aluminates or silicate in the XRD pattern were found, showing the presence of highly dispersed Co3O4. This also confirms that no interaction of Co with MMT components exists [25-28].
Textural Properties of Ce-Co/Al-PILC
The textural data including BET surface area pore volume and pore diameter are summarized in Table-2. The higher surface area of Al-PILC as compared to NaMMT indicates that Al has successfully replaced Na present in the silicate layer of MMT. The larger surface area is due to the higher N2 adsorption as a result of increased pore volume caused by Al-pillaring . While the addition of cerium and Co on Al-PILC resulted in decrease in BET surface area and pore volume which can be attributed to the presence of metal particles at pore openings and on the surface of the pores. Since, the average pore diameter and pore size remained constant for all samples, therefore the pore blocking of Co can be neglected . The pore volume depicts the micro porous and non-porous nature of Ce-Co/Al- PILC and NaMMT, respectively.
Table-2: Textural properties of the prepared catalysts
###BET###Pore diameter###Pore volume
NH3-TPD study was carried out for the evaluation of acidic properties of the prepared sample. It is obvious from NH3-TPD profile as shown in Fig. 2, that Al-PILC possess both Bronsted and Lewis acidic sites . The lower temperature desorption peak at 150 oC and higher temperature desorption peak at 600 oC can be attributed to weaker Bronsted acidic and stronger Lewis acidic site respectively. The lower temperature desorption peak (at 150 oC, Bronsted site) of Al-PILC is due to the presence of hydroxyl groups in the layered structure of MMT . However, the high temperature desorption (600 oC) for strong Lewis acidic site can be attributed to the alumina pillars [30-32]. The peak intensity of low temperature desorption peak for Bronsted acidic sites slightly increased with cerium loadings depicting the slight increase in Bronsted acidity, while the intensity of Lewis acidic peak showed very minor changes with increasing cerium loading.
The cerium cobalt loaded samples showed minor decrease in acidic property due to the presence of these on the pore opening resulting in the decreased Lewis acidic sites density .
The reduction behavior of samples was studied by H2-TPR and the obtained TPR profiles are presented in Fig. 3. Normally, the reduction of cobalt oxide occurs in two steps. First step involves the reduction of Co3O4 to CoO while in second step CoO undergoes reduction to metallic cobalt (Coo) .
It can be seen from Fig. 3 that the 0.5 wt% cerium modified Co/Al-PILC shows three reduction peaks at 208 oC, 278 oC and 379 oC. The first peak at 208 oC can be attributed to the decomposition of Co(No3)2 . While peaks at 278 oC and 379 oC may be due to the two step reduction of Co3O4 to CoO and CoO to Coo, respectively. A distinct change in the TPR profile is observed for higher cerium loaded Co/Al- PILC, whereas the two steps reduction occurs at 284 oC, 381 oC and at 291 oC, 391 oC for 1 wt% and 1.6 wt% cerium doped catalysts respectively. The shift in reduction peak towards higher temperature confirms the hindrance in Co3O4 reduction with cerium addition.
Similar trends of TPR profile for cerium promoted Co/SiO2 was reported by B Ernst et al .
Thermo Gravimetric Analysis (TGA)
TGA of 20 wt% Co/Al-PILC with different cerium loadings has been carried out (Fig. 4). This is clearly seen from TGA data that all samples exhibit continuous weight lost behavior till 800 oC. The weight lost upto 160 oC can be attributed to the removal of surface adsorbed water while the weight lost between 150 oC to 500 oC is attributed to the interlayer water and due to the dehydroxylation of cerium species. Interestingly, as the wt% of cerium increased, the weight loss around 300 oC also increased. The continuous weight lost from 600 oC till 800 oC was attributable to the removal of hydroxide groups as a result of dehydroxylation of pillar and clay structure, causing collapse in MMT layer structure [10-12, 28, 29, 33-36]. These results also show an agreement with previously reported results for thermal behavior of vanadia-loaded pillared clays .
Fig. 5, presents the typical SEM micrographs of prepared samples. NaMMT and cerium promoted Co/Al-PILC exhibits flake like morphology. It is interesting to note from micrographs that cerium addition and calcination temperature has no marked effect on the layered structure of MMT. No apparent morphology and distribution of cobalt and cerium particles was observed due to densified nature of clay as well as lower magnification of the instruments. In addition, high dispersion and lower concentration of cobalt and cerium hinders the study of surface morphology for these metal particles on MMT clay surface.
Effect of Ce Doping on FT Activity of Co Supported
The effect of Al-pillaring on the FT activity of Co-supported MMT catalysts was reported in our previous findings [4, 9]. In this work, we present the effect of Ce promoter on the FT activity of Al-PILC supported cobalt catalyst. The incorporation of Ce to the Co-supported Al-PILC has pronounced effect on the catalytic activity and product selectivity (Table- 3). The CO conversion boosts up to 33.5% resulting in higher selectivity of C5+ hydrocarbons over cerium modified Co/Al-PILC. This may be due to the increased dispersion of Co3O4 on the surface of support and presence of larger active sites as a result of cerium addition.
Moreover, addition of 1.6 wt% Ce to 20 wt% Co/Al-PILC resulted in the increased selectivity of gasoline range hydrocarbons (C5-C12) and methane from 18.23% to 31.7% and 27.7 to 30.8%, respectively, while selectivity of C21+ were decreased to 23.1%. This behavior can be attributed to the ability of cerium to promote the hydrocracking ability of cobalt supported Al-pillared clay and is in accordance to the results reported for cerium promoted Co/SiO2 catalysts . The lower catalytic activity was expected due to the increase in reduction temperature of Co3O4 after the cerium incorporation. The unexpected increase in initial activity and C5+ products selectivity were seen after the reaction which can be attributed to the more active sites as a result of CeO2 to CeO2-x partial reduction [18-21] on the surface of Co/Al-PILC after cerium doping [17, 19].
In FT synthesis (CHx)ad species are formed as a result of hydrogenation of adsorbed CO on the surface of catalysts which are mainly responsible for the production of methane via hydrogenation or higher hydrocarbons via polymerization. Furthermore, the hydrogenation of (CHx)ad suppressed with the incorporation of cerium due to enhanced formation of Co-C intermediates, resulting in decreased (CHx)ad hydrogenation. The improved FT catalytic activity may also be attributed to the modified electronic properties of Co-atoms as a result of CeO2 to CeO2-x partial reduction. This behavior is similar to the results reported earlier for cerium promoted Co/SiO2 catalysts .
Table-3: Results of different catalysts for FT synthesis.
###Catalysts###CO conversion###CO2 selectivity###C1 (Wt%)###C5-C12 (Wt%)###C13-C20 (Wt%)###C21+ (Wt%)
###1.0 Ce-Co/ Al-PILC###33.0###2.3###28.9###26.0###11.3###31.4
###1.6 Ce-Co/ Al-PILC###33.5###2.4###30.8###31.7###12.0###23.1
The catalyst stability of Co/Al-PILC was studied for reaction time of 30h, initially. The CO conversion was achieved up to 28% for 20 wt% Co/Al-PILC (Fig. 6) which decreased with TOS and reached at minimum level of 11% after 30h of TOS, calculated by a normalization equation . However, the cerium modified catalysts showed higher TOS stability. 0.5 and 1% cerium addition showed little decrease in CO conversion after 8h which remained constant for 30h of TOS while 1.6% cerium catalyst showed higher stability and constant catalytic activity for 30h of TOS. It is obvious from our results that cerium addition to the Co/Al-PILC catalyst increases the catalyst stability and higher cerium loading (1.6 wt%) showed greater TOS stability and is in agreement with previously reported results for Co/SiO2 system . The catalytic activity of different catalysts were in order of 1.6 wt% Ce- 20wt% Co/Al-PILC greater than 1wt% Ce-20wt% Co/Al-PILC greater than 0.5wt% Ce-20 wt%Co/Al-PILC greater than 20wt% Co/Al- PILC.
These results prove that, as the cerium loading increases, the degree of dispersion of Co3O4 also increases on the surface of Al-PILC and hence catalytic activity increases. This enhanced catalytic activity with the increased cerium modified sample is mainly due to high dispersion ability of cerium over the support.
Effect of Reaction Temperature and Pressure on Catalytic Activity of Catalysts
The effect of reaction temperature and reaction pressure on catalytic activity of 1.6 wt% Ce 20 wt% Co/Al-PILC was also investigated and presented in Fig. 7.a and Fig. 7.b respectively.
The reaction carried out at a temperature of 220 oC gives almost 33.5% CO conversion resulting in the hydrocarbons selectivity of 30.8, 31.7, 12 and 23.1% for methane, C5-C12, C13-C20, C21+ respectively (Fig. 7.a). When the reaction temperature is increased to 260 oC, the CO conversion and methane selectivity also increased to 35.4 and 32.7, respectively, and decrease in C5+ hydrocarbons selectivity to 28.6%. Furthermore, as the temperature is increased to 275 oC, the CO conversion was increased to 36.3% and selectivity of methane to 34% while the C5+ hydrocarbons decreased to 28%. However, no significant change in the selectivity of C13-C20 and C21+ hydrocarbons was observed with increase in reaction temperature. This effect of the catalysts can be attributed to the higher hydrogenation activity of the catalysts at high temperature similar to the performance of standard cobalt-thorium catalysts .
Increase in reaction temperature from 220 to 275 oC results in higher production of methane which is not beneficial in Co-based FT synthesis as reported earlier . Reaction pressure also imparts crucial role on the activity and selectivity of FT catalysts. The FT reaction carried out at a pressure of 1, 5 and 10 bar is shown in Fig. 7.b. At a pressure of 1 bar, the CO conversion was 33.5%, while selectivity of methane and C5C12 hydrocarbons was 30.8% and 31.7%, respectively, over 1.6 wt% Ce-20 wt% Co/Al-PILC. As the pressure is increased from 5 to 10 bar, the CO conversion was increased from 35 to 36.5%, while the methane selectivity was decreased to 28.3 and 27%, respectively. At this increased pressure, the percent selectivity of C5C12 hydrocarbons was also improved from 33.5 to 34.4% (Fig. 7.b). A little change in the selectivity of C13-C20 and C21+ hydrocarbons was observed with increasing reaction pressure.
It can be concluded that higher pressure favors the production o f high molecular weight hydrocarbons as a result of chain growth probability . The increase in CO conversion can be ascribed to the increase in partial pressure of hydrogen because the reaction rate is proportional to the hydrogen partial pressure and the increased selectivity of the C5+ hydrocarbons is due to the increased CO partial pressure .
The enhanced catalytic activity and lower methane selectivity was achieved over Al-pillared MMT supported Co catalyst. The Na+ in MMT interlayer responsible for higher methane production was completely replaced by Al after pillaring along with enhanced CoO reduction. The incorporation of small amount of cerium to the Co/Al-PILC results in increase in reduction temperature. Instead of increase in reduction temperature cerium incorporation results in high dispersion of cobalt particles and formation of new active sites which are responsible for higher catalytic activity and higher hydrocarbons (C5-C12) selectivity. The increased selectivity towards methane and C5-C12 hydrocarbons were obtained over cerium modified Co/Al-PILC as a result of cracking of C22+ hydrocarbons.
The addition of cerium to the Co/Al-PILC increases C2-C4 hydrocarbons of FT products due to decreased availability of adsorbed hydrogen. Higher reaction temperature (greater than 220 oC) increases CO conversion and methane selectivity and decreases C5+ hydrocarbons selectivity. Increase in reaction pressure from 1 to 10 bar favors an increase in C5+ hydrocarbons selectivity and decrease in the methane fraction.
The enhanced catalytic activity and lower methane selectivity was achieved over Al-pillared MMT supported Co catalyst. The Na+ in MMT interlayer responsible for higher methane production was completely replaced by Al after pillaring along with enhanced CoO reduction. The incorporation of small amount of cerium to the Co/Al-PILC results in increase in reduction temperature. Instead of increase in reduction temperature cerium incorporation results in high dispersion of cobalt particles and formation of new active sites which are responsible for higher catalytic activity and higher hydrocarbons (C5-C12) selectivity. The increased selectivity towards methane and C5-C12 hydrocarbons were obtained over cerium modified Co/Al-PILC as a result of cracking of C22+ hydrocarbons. The addition of cerium to the Co/Al-PILC increases C2-C4 hydrocarbons of FT products due to decreased availability of adsorbed hydrogen.
Higher reaction temperature (greater than 220oC) increases CO conversion and methane selectivity and decreases C5+ hydrocarbons selectivity. Increase in reaction pressure from 1 to 10 bar favors an increase in C5+ hydrocarbons selectivity and decrease in the methane fraction.
Authors would like to thank Higher Education Commission (HEC) of Pakistan for financial support of this work.
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|Publication:||Journal of the Chemical Society of Pakistan|
|Date:||Aug 31, 2015|
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