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Article

Co-Fe-Si Aerogel Catalytic Honeycombs for Low Temperature Ethanol Steam Reforming

by
Montserrat Domínguez
1,2,
Elena Taboada
1,
Elies Molins
3 and
Jordi Llorca
1,2,*
1
Institute of Energy Technologies, Universitat Politècnica de Catalunya, Diagonal 647, Ed. ETSEIB, 08028 Barcelona, Spain
2
Centre for Research in Nanoengineering, Universitat Politècnica de Catalunya, Pasqual i Vila 15, 08028 Barcelona, Spain
3
Institut de Ciència de Materials de Barcelona, Consejo Superior de Investigaciones Científicas, Campus de la UAB, 08193 Bellaterra, Spain
*
Author to whom correspondence should be addressed.
Catalysts 2012, 2(3), 386-399; https://doi.org/10.3390/catal2030386
Submission received: 1 August 2012 / Revised: 6 September 2012 / Accepted: 7 September 2012 / Published: 19 September 2012
(This article belongs to the Special Issue Aerogel Catalyst)
Browse Figures
Versions Notes

Abstract

:
Cobalt talc doped with iron (Fe/Co~0.1) and dispersed in SiO2 aerogel was prepared from silica alcogel impregnated with metal nitrates by supercritical drying. Catalytic honeycombs were prepared following the same procedure, with the alcogel synthesized directly over cordierite honeycomb pieces. The composite aerogel catalyst was characterized by X-ray diffraction, scanning electron microscopy, focus ion beam, specific surface area and X-ray photoelectron spectroscopy. The catalytic layer is about 8 µm thick and adheres well to the cordierite support. It is constituted of talc layers of about 1.5 µm × 300 nm × 50 nm which are well dispersed and anchored in a SiO2aerogel matrix with excellent mass-transfer properties. The catalyst was tested in the ethanol steam reforming reaction, aimed at producing hydrogen for on-board, on-demand applications at moderate temperature (573–673 K) and pressure (1–7 bar). Compared to non-promoted cobalt talc, the catalyst doped with iron produces less methane as byproduct, which can only be reformed at high temperature, thereby resulting in higher hydrogen yields. At 673 K and 2 bar, 1.04 NLH2·mLEtOH(l)−1·min−1 are obtained at S/C = 3 and W/F = 390 g·min·molEtOH−1.

1. Introduction

The development of proton exchange membrane fuel cells (PEMFC) for the market of power sources for portable and mobile applications has moved researchers to investigate the development of small scale catalytic fuel reformers for on-site hydrogen generation from various liquid fuels as an alternative to direct hydrogen storage [1,2]. Among liquid fuels that are currently considered, ethanol is particularly appealing since it is a renewable source when obtained from biomass; it is easy to handle and distribute and it is readily available [3]. One of the most important drawbacks of current catalytic reformers is the lack of fast start up and rapid response to varying loads. In this context, aerogel-based catalysts may play a significant role since their mass transfer characteristics are excellent and offer new possibilities for conducting reforming reactions.
Many studies have been focused on ethanol steam reforming (ESR) using supported nickel, cobalt and noble metal catalysts aimed at generation of hydrogen [4,5,6] (Equation 1).
Catalysts 02 00386 i001
An efficient catalyst for hydrogen production from ethanol has to dissociate the C-C bond, maintain a low CO concentration and be stable under catalytic operation. A survey of the literature reveals that noble metal-based catalysts perform well for ESR [7,8,9]. They are stable and exhibit high activity, but only at high temperature (>800 K). The reason is that the reaction mechanism involves the decomposition of ethanol at moderate temperature into a mixture of hydrogen, carbon monoxide and methane (Equation 2), followed by the water gas shift reaction (WGS, Equation 3) and, finally, the steam reforming of methane at high temperature (Equation 4). The reaction mechanism over nickel-based catalysts follows the same steps as over noble metal-based catalysts; however, the particles of nickel species tend to sinter under ESR reaction conditions.
Catalysts 02 00386 i002
Catalysts 02 00386 i003
Catalysts 02 00386 i004
In contrast, cobalt-based catalysts can operate at a much lower temperature, typically at 673–823 K, since they do not yield methane as an intermediate species in the reaction mechanism, which can only be reformed at high temperature [10,11,12,13,14,15,16,17,18,19,20,21,22,23,24,25,26,27,28,29,30,31,32,33,34,35,36,37,38]. Over cobalt-based catalysts, ethanol is first dehydrogenated at low temperature into a mixture of hydrogen and acetaldehyde (Equation 5), and then acetaldehyde reacts with steam to yield mainly hydrogen and carbon oxides (Equation 6), which participate in the WGS (Equation 3), or decompose into carbon monoxide and methane (Equation 7):
Catalysts 02 00386 i005
Catalysts 02 00386 i006
Catalysts 02 00386 i007
Recently, we reported that cobalt talc (Co3[Si2O5]2(OH)2) in a SiO2 aerogel host is an active and selective catalyst to carry out ESR even at a lower temperature [39,40]. At 623 K, a reformate composition of 68.7% H2, 23.2% CO2, 1.0% CO and 7.1% CH4 is found at a steam-to-carbon ratio of S/C = 1.5 (stoichiometric ethanol-water mixture, Equation 1) and full ethanol conversion [39]. In addition, the catalyst exhibits fast start-up (few seconds) and a stable reformate composition is obtained, even after shut-down and exposure to air up to 613 K. High resolution transmission electron microscopy, X-ray diffraction, magnetic measurements and in situ X-ray photoelectron spectroscopy experiments [41] have revealed that cobalt talc undergoes delamination into individual nanolayers under reaction conditions that remain fixed in the aerogel host. Simultaneously, metal cobalt ensembles segregate at the surface of the nanolayers facilitating the redox pair Co0↔Co2+, thus offering a composite material with high surface area and reactivity, accounting for the outstanding catalytic behavior observed. This catalyst has been also tested in a catalytic membrane reactor for ESR with even faster response to varying loads [42].
On the other hand, it has been demonstrated that alloying cobalt with more electronegative elements such as Ni or Cu results in worse catalytic performance in terms of hydrogen yield, whereas alloying cobalt with the less electronegative elements Fe [22,43,44] and Mn [35,37] promotes the redox pair Co0↔Co2+, both in terms of a lower cobalt reduction temperature as well as a fast re-oxidation, which in turn results in a better catalytic stability. An important advantage of conducting the ESR at low temperature is that the WGS equilibrium favors the formation of hydrogen and CO2 at the expense of CO and water (Equation 3), thus maximizing the production of H2 and avoiding the requirement of additional WGS units at the reactor outlet. This condition considerably simplifies the fuel processor design, both in terms of number of catalytic stages required as well as heat transfer management. Also, the addition of Fe and Mn promoters hinders acetaldehyde decomposition (Equation 7) and less methane is formed as byproduct. In this work, we have extended our work on cobalt talc (Co3[Si2O5]2(OH)2) in SiO2 aerogel host by studying the effect of Fe addition on the catalytic performance for ESR under practical conditions. To that end, we have tested honeycomb structures loaded with the aerogel catalyst under different operational conditions.

2. Results and Discussion

2.1. Catalysts Characterization

The surface area measured for both powdered catalysts is about 330 m2·g−1, and the average Barrett-Joyner-Halenda (BJH) pore size is 9.2 nm. These values are characteristic of aerogel structures [41].The XRD profile of the powdered aer-CoFeSi catalyst is shown in Figure 1, along with that of aer-CoSi [41] for comparison. Both profiles are similar and show diffraction peaks characteristic of the talc structure [45]. The talc structure corresponds to a layered metal silicate hydroxide, (Co,Fe)3[Si2O5]2(OH)2, which is synthesized under supercritical drying between SiO2 and the metal precursors [41]. The peak measured at low angles corresponds to the basal plane (001) of the layered structure. This peak exhibits a very low intensity, which means that the number of layers in the talc crystallites is low, consistent with a good dispersion of the catalyst particles in the aerogel host. The atomic ratio Co:Fe:Si measured by X-ray fluorescence (XRF) is 0.31:0.04:1. The amount of metal added is similar to that observed in the sample without iron, Co:Si = 0.37:1 [39]. Taking into account the stoichiometry of the talc structure and the chemical analysis, the resulting catalyst is a composite material constituted of layered metal silicate hydroxide particles dispersed in an aerogel matrix. The amount of catalyst particles with respect to the aerogel is about 20% w/w.
Catalysts 02 00386 g001 1024
Figure 1. X-ray diffraction (XRD) profiles of catalysts aer-CoFeSi (a) and aer-CoSi (b).
Figure 1. X-ray diffraction (XRD) profiles of catalysts aer-CoFeSi (a) and aer-CoSi (b).
Catalysts 02 00386 g001
The characterization of the catalyst coatings onto the honeycomb structures was carried out by electron microscopy and X-ray photoelectron spectroscopy. Figure 2 shows a picture of the cordierite honeycomb before and after deposition of the aer-CoFeSi catalyst. Figure 3 shows scanning electron microscopy (SEM) images recorded over individual channels of aer-CoFeSi and aer-CoSi catalytic honeycombs as well as of a cordierite channel before deposition. An excellent deposition of the catalysts is achieved, covering all the surface of the channels, including the interior of the wall pores. At high magnification, the particles of the talc structure are clearly observed which, according to the XRD results, exhibit a well-defined layered morphology. For both samples the morphology of the talc layers is similar and measures about 1.5 μm × 300 nm × 50 nm. The catalytic particles are strongly anchored over the aerogel host. No weight loss is observed when the catalytic honeycombs are exposed to mechanical vibration stress tests up to 15 G and 100 Hz for 30 min (NTP conditions).
Figure 4 shows a SEM image corresponding to the aer-CoFeSi catalytic honeycomb recorded after a FIB cut perpendicular to the channel direction. In this way the thickness of the catalyst layer can be directly measured, which is about 8 μm. Interestingly, several pores of the honeycomb structure are also visible and are coated with catalyst as well. The layered structure of the cobalt talc structure doped with iron is clearly visible within the catalytic layer along with the classical cluster-of-grape morphology of SiO2 aerogel. The X-ray maps corresponding to the area enclosed within the square for Co, Fe, Si and Al (Kα signals) are depicted also in Figure 4. Clearly, Co and Fe signals are located within the catalyst layer, both at the channel’s surface and at the interior of honeycomb pores, where the Co signal is more intense, as expected from the catalyst formulation. Contrarily, the Al signal is restricted to the cordierite substrate and the Si signal exhibits contribution both from the cordierite support (more intense) and the catalyst. The Fe/Co atomic ratio of the catalyst layer obtained by energy dispersive X-ray analysis (EDX) is about 0.12, very close to the bulk value determined by XRF.
Catalysts 02 00386 g002 1024
Figure 2. Images of the honeycomb structures (400 cpsi) used in this work (a) and loaded with the aer-CoFeSi catalyst (b).
Figure 2. Images of the honeycomb structures (400 cpsi) used in this work (a) and loaded with the aer-CoFeSi catalyst (b).
Catalysts 02 00386 g002
Catalysts 02 00386 g003 1024
Figure 3. SEM images taken at several magnifications of the interior of a monolith channel (a,b) and loaded with aer-CoFeSi (c,d) and aer-CoSi (e,f) catalysts.
Figure 3. SEM images taken at several magnifications of the interior of a monolith channel (a,b) and loaded with aer-CoFeSi (c,d) and aer-CoSi (e,f) catalysts.
Catalysts 02 00386 g003
Catalysts 02 00386 g004 1024
Figure 4. SEM image corresponding to the interior of a monolith channel loaded with aer-CoFeSi catalysts after a perpendicular focus ion beam (FIB) cut and X-ray maps recorded over the same area for Co, Fe, Si and Al (Kα lines).
Figure 4. SEM image corresponding to the interior of a monolith channel loaded with aer-CoFeSi catalysts after a perpendicular focus ion beam (FIB) cut and X-ray maps recorded over the same area for Co, Fe, Si and Al (Kα lines).
Catalysts 02 00386 g004
Several channels were examined by X-ray photoelectron spectroscopy (XPS) to study the chemical homogeneity of the catalytic surface. Figure 5 shows a representative relative atomic concentration line scan along one channel of the aer-CoFeSi honeycomb. XPS line scan analyses reveal that (Co,Fe)3[Si2O5]2(OH)2 is distributed along all the channel, as expected. However, the distribution is not completely homogeneous, as a higher amount of Co and Fe is found at the edges, while a higher content of Si and Al from silica aerogel and cordierite (Mg2Al4Si5O18) is observed at the center of the channels. This phenomenon could be generated during the free impregnation of the silica alcogel with the metal precursor salts and/or during supercritical drying. Interestingly, the atomic ratio Fe/Co is maintained at an approximately constant value. A surface segregation of Fe is observed (Fe/Co~0.6–0.7) with respect to the bulk value of Fe/Co = 0.13. In all cases, the Co 2p3/2 and Fe 2p3/2 binding energy values recorded (780.6 and 711 eV, respectively) correspond to both oxidized Co and Fe surface species.
Catalysts 02 00386 g005 1024
Figure 5. Atomic concentration line scan along one channel of an aer-CoFeSi honeycomb determined by XPS.
Figure 5. Atomic concentration line scan along one channel of an aer-CoFeSi honeycomb determined by XPS.
Catalysts 02 00386 g005

2.2. Catalytic Behavior

Ethanol conversion and selectivity values obtained over aer-CoFeSi and aer-CoSi catalytic honeycombs under low load of ethanol (diluted conditions) are reported in Table 1 at different temperatures. The aer-CoSi catalyst is more active for the ethanol steam reforming reaction than the aer-CoFeSi catalyst. Accordingly, the amount of acetaldehyde, which is an intermediate of the reaction (Equation 5), is higher in the case of the aer-CoFeSi sample compared to aer-CoSi. Also, the amount of dimethyl ketone is higher for aer-CoFeSi because it is formed by condensation of acetaldehyde [12]. For both catalytic honeycombs, as the temperature increases so does the amount of the reforming products, H2 and CO2, according to the endothermic character of the reaction. At 673 K ethanol conversion is total and there are no traces of acetaldehyde or dimethyl ketone among the reaction products for both catalysts. Under these conditions, the amount of hydrogen obtained is higher with the aer-CoFeSi sample, 72.8% vs. 70.7% for aer-CoSi, with the theoretical maximum value at 75% (Equation 1). This is due to a better WGS activity (Equation 3) and, more interestingly, to a lower selectivity towards CH4. The promoting effect of Fe for the WGS reaction during the ethanol steam reforming has been shown to occur over Co/ZnO and Rh/Ca-Al2O3 catalysts doped with Fe [37,46]. Methane can only be reformed at high temperature, so for an ethanol steam reforming process operating at moderate temperature it is important to avoid it, since methane formation sharply decreases the hydrogen yield. It can be concluded that doping cobalt talc with Fe results in a certain loss of activity for ESR but, conversely, to an important enhancement of hydrogen selectivity due to methane suppression. No signs of deactivation were observed after 80 h on stream for both samples.
Table
Table 1. Ethanol conversion and product distribution (dry basis) over aer-CoFeSi and aer-CoSi catalytic honeycombs under ethanol steam reforming (ESR) conditions at different temperature. S/C = 3, W/F = 104 g·min·molEtOH−1, VHSV = 680 h−1.
Table 1. Ethanol conversion and product distribution (dry basis) over aer-CoFeSi and aer-CoSi catalytic honeycombs under ethanol steam reforming (ESR) conditions at different temperature. S/C = 3, W/F = 104 g·min·molEtOH−1, VHSV = 680 h−1.
CatalystT/KEtOH conv./%Selectivity/%
H2CO2COCH4CH3CHO(CH3)2CO
aer-CoFeSi5738649.73.13.43.240.6-
5989357.86.52.03.928.61.2
6239969.814.51.15.87.11.7
67310072.823.00.93.3--
aer-CoSi5739266.716.65.27.04.10.4
5989968.723.00.97.10.20.1
62310068.723.21.07.1--
67310070.722.71.94.7--
The catalytic performance of the aer-CoFeSi catalytic honeycomb was studied in detail under high load of ethanol (undiluted conditions) at several temperature and pressure conditions. Operation under moderate pressure is advantageous for practical application since it allows for compact fuel processors [1]. However, from the thermodynamics point of view, an increase of reactor pressure is always unfavorable for steam reforming reactions [42]. Therefore, the study of the catalytic performance under various pressure values is important. Figure 6a shows the yields for the different products attained at 673 K over the aer-CoFeSi catalytic honeycomb by varying the pressure between 1 and 7 bar using a pure ethanol-water mixture with no diluents (S/C = 3) taking into account both the ethanol conversion and product selectivity. As the pressure is increased above 4 bar, the ethanol conversion decreases progressively, as expected, from about 85–87% down to 74%. Interestingly, the amount of acetaldehyde decreases when the pressure is increased (from 4.4% of selectivity on a dry basis at 1 bar down to 1.0% at 7 bar), suggesting that pressure affects less negatively the reforming of acetaldehyde (Equation 6) with respect to the dehydrogenation of ethanol into acetaldehyde (Equation 5), which is the first step of the reforming process over Co-based catalysts. Dimethyl ketone is kept constant at a selectivity value of ca. 0.3% for all pressure values. The decrease of ethanol transformation is accompanied by a significant decrease of hydrogen selectivity, whereas the amount of methane among the reaction products increases strongly with pressure, from 8% at 1 bar up to 18.4% at 7 bar. Methane formation is directly correlated with pressure, since reaction between carbon oxides and hydrogen to yield methane is progressively favored as pressure increases [42]. The effect of pressure is also observed for the WGS equilibrium; the higher the pressure the more carbon dioxide is obtained at the expense of CO. All these processes results in a different net amount of hydrogen generated; up to 3 bar the amount of hydrogen generated is kept approximately constant at about 1.6 NLH2·s−1, whereas at pressures higher than 3 bar the production of hydrogen decreases progressively down to 1.0 NLH2·s−1 at 7 bar. Figure 6b shows the product yield obtained at 7 bar by varying the temperature from 598 to 673 K. The reaction temperature has a strong effect on ethanol conversion at high pressure and, consequently, on hydrogen yield. At 7 bar, ethanol conversion drops from 74% at 673 K to 20% at 598 K, whereas the amount of acetaldehyde increases. The maximum hydrogen yield is obtained at 648–673 K. At 648 K the ethanol conversion is lower than at 673 K (66 vs. 74%), but the selectivity is better because an increase of reaction temperature results in a higher selectivity towards methane.
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Figure 6. Ethanol conversion and product distribution (dry basis) over aer-CoFeSi catalytic honeycomb under ethanol steam reforming (ESR) conditions at 673 K and different pressure (a); and at 7 bar and different temperature (b). S/C = 3, W/F = 390 g·min·molEtOH−1, volume hourly space velocity (VHSV) = 1800 h−1. Catalysts 02 00386 i010 H2, Catalysts 02 00386 i011 CO2, Catalysts 02 00386 i012 CO, Catalysts 02 00386 i013 CH4, Catalysts 02 00386 i014 CH3CHO.
Figure 6. Ethanol conversion and product distribution (dry basis) over aer-CoFeSi catalytic honeycomb under ethanol steam reforming (ESR) conditions at 673 K and different pressure (a); and at 7 bar and different temperature (b). S/C = 3, W/F = 390 g·min·molEtOH−1, volume hourly space velocity (VHSV) = 1800 h−1. Catalysts 02 00386 i010 H2, Catalysts 02 00386 i011 CO2, Catalysts 02 00386 i012 CO, Catalysts 02 00386 i013 CH4, Catalysts 02 00386 i014 CH3CHO.
Catalysts 02 00386 g006

3. Experimental Section

3.1. Preparation of Catalysts

Cordierite monoliths (Corning, 400 cpsi) were used as a catalyst support. They were cut with a diamond saw with a cylindrical shape (18 mm diameter, 20 mm length, 156 cells). Co3[Si2O5]2(OH)2 (cobalt talc) doped with Fe (Fe/Co = 0.1 molar ratio) in SiO2 aerogel was grown over the cordierite honeycombs by a sol-gel method followed by supercritical drying [39]. First, the cordierite pieces were coated with a thin layer of silica alcogel through the hydrolysis and condensation of tetraethoxysilane (TEOS, Si(OCH2CH3)4, 98% Sigma Aldrich) dissolved in ethanol. Gelation was catalyzed by addition of an aqueous solution of HNO3 and HF (TEOS:EtOH:H2O:HNO3:HF = 1.0:6.0:15.9:0.03:0.12 molar ratio). Next, the alcogel was impregnated with an ethanolic solution containing both cobalt nitrate hexahydrate (Co(NO3)2·6H2O, 99% Scharlau) and iron nitrate hexahydrate (Fe(NO3)3·6H2O, 99% Scharlau) over 72 h. Finally, the solvent was extracted under supercritical conditions at 6.28 × 106 Pa and 516 K, which resulted in the formation of a thin layer of silica aerogel with cobalt talc doped with Fe over the cordierite surface. This is referred to in this work as aer-CoFeSi. Following exactly the same procedure, catalytic monoliths with cobalt talc were prepared in the absence of iron for comparative purposes, which are referred to as aer-CoSi. Powdered catalysts were obtained in the same reactor batches and used for characterization.

3.2. Characterization Techniques

Elemental composition of the powdered catalysts was determined by X-ray fluorescence (XRF) with a Phillips PW2400 apparatus. X-ray diffraction (XRD) measurements were performed with a Siemens D5000X diffractometer equipped with a Cu Kα X-ray source. XRD analyses were performed in the 2θ range of 3 to 75° at a stepsize of 0.02°. A Micromeritics ASAP 2000 apparatus was used to study the Brunauer-Emmet-Teller (BET) surface area and Barret-Joyner-Halenda (BJH) pore size of the powdered catalysts. A Zeiss Neon 40 focused ion beam electron microscope with cross beam (FIB-SEM) and energy-dispersive X-ray detector (EDX) was used in order to study directly the microstructure and element distribution of the catalytic layers in the honeycomb structures. X-ray photoelectron spectroscopy (XPS) was performed using a Kratos AXIS Ultra DLD spectrometer and a monochromatic X-ray source (Al Kα). An automatic charge neutralizer system was used. Binding energy values were calibrated at 285.0 eV corresponding to the adventitious C1s reference.

3.3. Reaction Tests

The catalytic honeycombs were tested in a tubular stainless steel reactor. Prior to catalytic tests the samples were heated up to 473 K in air for 20 min. The effect of reaction temperature was first studied at atmospheric pressure under diluted conditions with a mixture of EtOH:H2O:N2 = 1:3:96 molar (S/C = 1.5), W/F = 104 g·min·molEtOH−1, VHSV = 680 h−1. The catalysts were exposed to the reaction mixture at 573, 598, 623, and 673 K over 80 h to check for deactivation. The same samples were then studied under high loads of ethanol and water at S/C = 3 with no carrier gas in order to simulate real conditions. The liquid mixture of reactants was supplied directly into the reactor with a Knauer Smartline HPLC pump (0.075 mL·min−1). The performance of the catalytic honeycombs was studied between 598 and 673 K and between 1 and 7 bar under W/F = 390 g·min·molEtOH−1, VHSV = 1800 h−1. The reactor effluent was analyzed on line by gas chromatography using an Agilent 3000A apparatus equipped with MS 5Å, PlotU and Stabilwax columns. Conversion and selectivity values are defined as follows (Equations 8 and 9):
Catalysts 02 00386 i008
Catalysts 02 00386 i009
where nEtOH conv represents the moles of ethanol converted, measured as the sum of moles of CO2, CO, CH4, CH3CHO and (CH3)2CO at the reactor outlet and nEtOH in represents the moles of ethanol at the reactor inlet.

4. Conclusions

Honeycomb structures have been loaded with catalysts containing cobalt talc (Co3[Si2O5]2(OH)2) doped with Fe (Fe/Co~0.1) in a SiO2 aerogel host. The catalytic composite has been prepared directly over cordierite honeycomb pieces from silica alcogel impregnated with metal nitrates by supercritical drying. In addition, to favor mass transfer characteristics, the silica aerogel host allows an excellent dispersion of catalyst particles, which remain well adhered during reaction. The honeycomb catalyst has been tested in the ethanol steam reforming reaction aimed at producing hydrogen for on-board, on-demand applications at moderate temperature (573–673 K) and pressure (1–7 bar). Compared to non-promoted cobalt talc, the catalyst doped with iron is less active but produces less methane as byproduct, resulting in higher hydrogen yields. At 673 K and up to 3 bar, the amount of hydrogen generated is kept approximately constant at about 1.6 NLH2·s−1 under S/C = 3 and W/F = 390 g·min·molEtOH−1.

Acknowledgments

This work was funded through MICINN grant CTQ2009-12520. M.D. acknowledges an FI grant from Generalitat de Catalunya and European Social Fund. E.T. acknowledges a postdoctoral grant from UPC. J.L. is grateful to ICREA Academia program.

Conflict of Interest

The authors declare no conflict of interest.

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MDPI and ACS Style

Domínguez, M.; Taboada, E.; Molins, E.; Llorca, J. Co-Fe-Si Aerogel Catalytic Honeycombs for Low Temperature Ethanol Steam Reforming. Catalysts 2012, 2, 386-399. https://doi.org/10.3390/catal2030386

AMA Style

Domínguez M, Taboada E, Molins E, Llorca J. Co-Fe-Si Aerogel Catalytic Honeycombs for Low Temperature Ethanol Steam Reforming. Catalysts. 2012; 2(3):386-399. https://doi.org/10.3390/catal2030386

Chicago/Turabian Style

Domínguez, Montserrat, Elena Taboada, Elies Molins, and Jordi Llorca. 2012. "Co-Fe-Si Aerogel Catalytic Honeycombs for Low Temperature Ethanol Steam Reforming" Catalysts 2, no. 3: 386-399. https://doi.org/10.3390/catal2030386

APA Style

Domínguez, M., Taboada, E., Molins, E., & Llorca, J. (2012). Co-Fe-Si Aerogel Catalytic Honeycombs for Low Temperature Ethanol Steam Reforming. Catalysts, 2(3), 386-399. https://doi.org/10.3390/catal2030386

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