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Article

Performance of an Auto-Reduced Nickel Catalyst for Auto-Thermal Reforming of Dodecane

by
Seong Bin Jo
1,†,
Dong Geon Ju
2,3,†,
Suk Yong Jung
4,
Dong Su Ha
5,
Ho Jin Chae
2,
Soo Chool Lee
1,* and
Jae Chang Kim
2,*
1
Research Institute of Advanced Energy Technology, Kyungpook National University, Daegu 41566, Korea
2
Department of Chemical Engineering, Kyungpook National University, Daegu 41566, Korea
3
Korea Evaluation Institute of Industrial Technology (KEIT), Daegu 41069, Korea
4
Wonik Materials Co., Cheongju 28125, Korea
5
Korea Institute of Energy Research, Daejeon 34129, Korea
*
Authors to whom correspondence should be addressed.
†
Seong Bin Jo and Dong Geon Ju contributed equally to this work.
Catalysts 2018, 8(9), 371; https://doi.org/10.3390/catal8090371
Submission received: 17 July 2018 / Revised: 20 August 2018 / Accepted: 20 August 2018 / Published: 3 September 2018
(This article belongs to the Section Catalytic Materials)
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Abstract

:
To investigate the catalytic performance of diesel reforming catalysts for production of hydrogen gas, Ni-Al catalyst was prepared by the polymer-modified incipient method (NA10-PM). NA10-PM showed excellent catalytic performance and economic feasibility in the auto-thermal reforming reaction, compared to other commercially available catalysts. In particular, auto-reduced NA10-PM showed higher dodecane conversion and similar selectivity at 750 °C compared to H2-reduced NA10-PM. X-ray diffraction (XRD) studies showed that the fresh state of NA10-PM initially automatically reduced by product gases through thermal decomposition of dodecane, and then NiAl2O4 was completely reduced to metallic nickel by the CO and H2 gases produced during the reaction. Additionally, catalytic performance of auto-reduced NA10-PM were investigated at varying steam/carbon molar ratio (S/C) and oxygen/carbon molar ratio (O2/C) in order to determine the optimum conditions of the auto-thermal reforming reaction. The conversion of dodecane over auto-reduced NA10-PM catalyst was remarkable (93%) and increased during the reaction, under conditions of S/C = 1.23, O2/C = 0.25, and gas hourly space velocity of 12,000 h−1 at 750 °C. The results of this study demonstrated that the auto-reduced NA10-PM catalyst was applied successfully for auto-thermal reforming of dodecane.

Graphical Abstract

1. Introduction

Fuel cells show higher energy efficiencies than internal combustion engines. The feed gas generally used in fuel cells is H2, which restricts the applications of fuel cells. Although the use of hydrogen is an interesting alternative to increase fuel economy, it is difficult to store hydrogen in vehicle storage tanks because of the absence of suitable infrastructure for hydrogen storage. Fuel cell-based auxiliary power units (APU) take advantage of the fact that liquid hydrocarbons such as gasoline, kerosene, and diesel may be converted into hydrogen. APU systems also offer other advantages such as slightly higher efficiencies and reduced emission of contaminants. Moreover, it is easy to store and transport liquid fossil fuels such as diesel, gasoline, and liquid hydrocarbons compared to hydrogen and methane. In particular, diesel oil is widely used in the industry and is transported via boilers, trucks, and ships. However, fuel reforming technology is needed to enable the use of diesel in fuel cells [1,2,3]. The commonly used technologies for converting diesel oil into H2 and CO in fuel cell-based APUs are steam reforming (SR), partial oxidation reforming (POx), and auto-thermal reforming (ATR). The corresponding reactions are as follows:
  • Steam reforming (SR): CnHm + nH2O ↔ nCO + (n + m/2)H2
  • Partial oxidation (POx): CnHm + (n/2)O2 ↔ nCO + (m/2)H2
  • Auto thermal reforming (ATR): CnHm + (n/4)O2 + (n/2)H2O ↔ nCO + (n + m)/2H2
Exothermic POx requires less energy than endothermic SR in the production of hydrogen from liquid hydrocarbons. ATR, in which the highly endothermic SR is combined with the exothermic POx, is the preferred technology because of optimum reforming and energy efficiencies, and short start-up time. Moreover, ATR of liquid hydrocarbons is thermally more stable than SR. The exothermic water gas shift (WGS, CO + H2O = CO2 + H2) reaction can occur in the presence of CO and H2O [4,5,6,7]. Many researchers have made an effort to synthesize compatible catalysts for use in diesel reforming [8,9]. Ethanol reforming for hydrogen production was conducted over several catalysts (Ni/CeO2-SiO2, Pt/CeO2-SiO2, Pt-Ni/CeO2-SiO2, and Ni/CeO2) [10,11]. Precious metal-based (Pt, Pd, Rh, and Ru) catalysts exhibit better resistance to carbon deposition and sulfur poisoning than Ni-based catalysts. Perovskite-type oxides (ABO3) have also been considered as reforming catalysts in solid oxide fuel cells (SOFC), where A is lanthanum and B is a first-row transition metal (Ni, Co, Fe, Mn, or Cr) [12]. Ni-based catalysts have been studied extensively using various methods and under different conditions in the production of hydrogen. Mesoporous nickel-alumina catalysts have been used in hydrogen production by the SR of liquefied natural gas (LNG) [13]. The performances of Ni-based monolith reforming catalysts for the SR, POx, and ATR of n-dodecane have also been evaluated [14,15,16]. In particular, the catalytic properties and carbon-decomposition resistance of nickel–alumina catalysts have been studied in the SR reactions of various hydrocarbon fuels [17,18,19,20,21]. Nickel–alumina-based catalysts are usually prepared by impregnation or co-precipitation, with the former method being simpler than the latter. However, the efficiencies of the catalysts prepared by impregnation were found to be lower than those of the catalysts prepared by co-precipitation. To complement the shortcomings of the preparation method, polymer-modified incipient method (PM method) was proposed [22,23].
Previous reports showed that the PM method is simple and the thus-synthesized catalysts exhibit high efficiency. However, this catalyst was not studied in detail under different ATR conditions. In this study, the catalytic performances of auto-reduced catalysts were compared with those of the catalyst reduced by hydrogen gas. Conventionally, oxidized catalysts are reduced by H2 gas and then used for reactions. The auto-reduction process is proposed to integrate both catalyst reduction and reaction [24,25,26,27]. The catalytic performances of the catalysts were tested after they were auto-reduced by product gas obtained from thermal decomposition of n-dodecane at the reaction temperature. Furthermore, the ATR performances of the auto-reduced catalysts were investigated as a function of various reaction parameters such as steam/carbon molar ratio (S/C), and oxygen/carbon molar ratio (O2/C). The catalysts were characterized using H2 and CO temperature-programed reduction (TPR), Brunauer-Emmett-Teller (BET) surface area analysis, and X-ray diffraction (XRD) analysis.

2. Results and Discussion

2.1. Catalytic Performance Comparison of NA10-PM with Various Catalysts

Dodecane conversion and selectivity of Ni-Al catalyst prepared by polymer-modified incipient method (NA10-PM) were tested and compared with those of other metal impregnated catalysts on alumina support such as Ni (NA10-IM), Ru (RuA5-IM), and Rh (RhA5-IM). All the catalysts were typically reduced by 10% H2 at 750 °C for 2 h. Figure 1 shows the dodecane conversions and initial selectivity under S/C ratio = 1.23, O2/C ratio = 0.25, and gas hourly space velocity (GHSV) = 12,000 h−1 at 700 °C. The dodecane conversions with NA10-IM, NA10-PM, and RhA5-IM were 72.5%, 85.0%, and 85.8%, respectively, over a period of 300 min. In contrast, dodecane conversion with RuA5-IM was 58.5% initially and then gradually decreased to 45% as the reaction progressed. The product selectivity using NA10-PM was about 67.2% H2, 19.6% CO, 11.6% CO2, and 1.48% CH4. For the NA10-IM catalyst, that was about 68.12% H2, 18.9% CO, 11.8% CO2, and 1.14% CH4. Although the product selectivity showed similar values, the dodecane conversion using the NA10-PM catalyst was higher than that obtained with NA10-IM, in agreement with a previous report [22,23]. In addition, NA10-PM exhibited a similar dodecane conversion (85.8%) as RhA5-IM. These results are excellent from an industrial point of view because the price of nickel is much less than that of rhodium, and there are more nickel reserves.

2.2. Characterization

Conventionally, oxidized catalysts are reduced by H2 gas and then used for reactions. In the auto-reduction process, the oxidized catalysts are initially reduced by heat, photochemical radiation, and a reductant obtained from the thermal decomposition of feedstock [24,25,26,27]. In this study, the oxidized catalysts were reduced by the reductant generated from the thermal decomposition of n-dodecane. Dodecane was thermally decomposed to H2, CO, CO2, and CH4, under S/C = 1.23 and O2/C = 0.25 at 750 °C (Supplementary Materials Figure S1). Temperature-programmed reduction (TPR) was used to investigate the reducibility of the Ni species on the NA10-PM catalyst under the conditions of H2 reduction and auto-reduction (simulated CO and H2 gases). Figure 2 shows the TPR profiles obtained under the conditions of (a) H2 reduction and (b) auto-reduction of the NA10-PM catalyst. Both TPR profiles showed two groups of peaks. The low-temperature peaks were attributed to the reduction of NiO, indicating minimal or no interaction with the alumina supports (NiO and NiO-Al2O3), whereas the high-temperature peaks may be attributed to the strong interaction of NiO and the alumina support (NiAl2O4). It was found that the reduction of NiO and NiAl2O4 occurred at lower temperatures under the auto-reduction conditions (220 and 750 °C, respectively), compared to the H2–reduction conditions (250 and 810 °C, respectively). Thus, it was concluded that the presence of CO with H2 (auto-reduction condition) improved the reducibility of NiO and NiAl2O4, in agreement with a previous report [28].
To elucidate the effect of auto-reduction on the reducibility of NA10-PM, nitrogen adsorption-desorption isotherms and XRD patterns of the fresh and reduced catalysts were investigated. The nitrogen adsorption-desorption isotherms and the textural properties of fresh and reduced NA10-PM catalyst are shown in Figure 3a and listed in Table 1, respectively. Under the typical H2 reduction conditions, NA10-PM was analyzed after reduction using 10% H2 at 750 °C for 2 h. Under the auto-reduction conditions, the catalyst was analyzed after reduction by product gases obtained from the thermal decomposition of n-dodecane, under feed gas conditions of S/C = 1.23 and O2/C = 0.25 at 750 °C for 2 h. As shown in Figure 3a, the fresh, H2-reduced, and auto-reduced NA10-PM catalysts exhibited type IV (a) isotherms, which indicates some steep mesopore condensation at P/P0 = 0.7–0.8 and an almost flat region at P/P0 > 0.8. The auto-reduced catalysts also showed type IV (a) nitrogen adsorption-desorption isotherms; the volume of adsorbed nitrogen gas increased with increasing temperature. Additionally, the volume of adsorbed nitrogen for auto-reduced catalysts at 750 °C is higher than that for typical H2-reduced catalysts. As listed in Table 1, for the fresh catalysts, textural properties such as BET surface area, pore volume, and average pore size of the NA10-PM catalyst were 28.1 m2/g, 0.04 cm3/g, and 3.8 nm, respectively. For H2-reduction, textural properties such as BET surface area, pore volume, and average pore size were 78.1 m2/g, 0.06 cm3/g, and 3.8 nm, respectively. On the other hand, auto-reduced catalysts showed that textural properties such as BET surface area, pore volume, and average pore size were 96.6 m2/g, 0.12 cm3/g, and 4.1 nm, respectively. Based on these results, it is expected that the NA10-PM catalyst was more reduced under auto-reduction condition. Figure 3b showed the XRD patterns of fresh and pre-treated NA10-PM activated by typical H2 reduction and auto-reduction. As shown in Figure 3b, fresh NA10-PM exhibited three main peaks, which overlapped with the two main peaks of –Al2O3 and NiAl2O4 alloy structures, but no diffraction peaks corresponding to bulk NiO. It was revealed that diffraction peak of –Al2O3 at 66.84° shifted to a lower diffraction angle, representing lattice expansion of –Al2O3 caused by the incorporation of Ni2+ ions into –Al2O3 (NiAl2O4) [29,30,31,32]. Therefore, the peak at 66.18° indicated that the Ni components were alloyed with –Al2O3 during preparation. The NiAl2O4 phase was inactive for reforming reaction, but was used as precursor materials, leading to catalysts with desired properties (smaller particle size and higher dispersion of Ni species). After typical H2-reduction and auto-reduction for 2 h, diffraction peak for metallic nickel was observed, and the diffraction peak for NiAl2O4 was shifted to the peak for –Al2O3 after reduction, indicating a portion of NiAl2O4 was reduced to metallic nickel. After auto-reduction for 2 h, more distinctive peak for metallic nickel was observed, compared to the catalyst after H2-reduction. Moreover, it was found that the intensity of metallic nickel increased with the increasing temperature, and the two angle for NiAl2O4 shifted farther to the peak for –Al2O3 (Supplementary Materials Figure S2b). It was found that metallic nickel is more activated by auto-reduction with increasing temperature, under feed gas conditions. These results are in good agreement with the TPR profiles, and nitrogen adsorption-desorption isotherms. Therefore, it can be concluded that nickel species in NA10-PM catalyst was more reduced by an auto-reduction condition, compared to typical H2-reduction.

2.3. Catalytic Performance of Auto-Reduced NA10-PM Catalyst

Figure 4 shows the dodecane conversions and initial selectivity of NA10-PM catalyst reduced by typical H2 reduction and auto-reduction under S/C = 1.23, O2/C = 0.25, and GHSV = 12,000 h–1 at 750 °C. As shown in Figure 4a, the initial dodecane conversions using H2-reduced NA10-PM at 650, 700, and 750 °C were approximately 82%, 85%, and 83%, respectively. While the dodecane conversions at 650 °C decreased as reaction progressed, those at 700 and 750 °C were maintained for 5 h. As shown in Figure 4b, the concentration of H2 gas showed a similar value of approximately 67% regardless of the reaction temperature. On the other hand, the concentration of CO increased, and that of CO2 and CH4 decreased with the rise of reaction temperature. The reason for this concentration change is that the exothermic WGS and methanation reaction decreased with the rise in reaction temperature. As shown in Figure 5a, the initial dodecane conversions of the auto-reduced catalysts at 650, 700, and 750 °C were approximately 75%, 90%, and 93%, respectively. However, the dodecane conversions decreased at 650 and 700 °C as the reaction progressed. It was found that the dodecane conversion of NA10-PM increased with the reaction temperature. This is because the nickel species were not fully reduced by auto-reduction at relatively lower temperatures, and therefore, lower dodecane conversions and catalytic deactivation were observed. As shown in Figure 5b, the initial selectivity of H2 increased, and that of CO, CO2, and CH4 decreased with increasing reaction temperature. In particular, auto-reduced NA10-PM at 750 °C showed a higher dodecane conversion and similar product gas distribution than that of H2-reduced NA10-PM at 750 °C.
To investigate the effect of S/C ratio on catalytic performance, the auto-reduced NA10-PM catalyst was tested at S/C = 0.5, 1.23, 2.0, and 2.75, O2/C = 0.25, and GHSV = 12,000 h–1 at 750 °C. As shown in Figure 6, at S/C = 0.5, the dodecane conversion was approximately 80% during the initial reaction period, and then gradually decreased. However, above S/C = 2.0, the dodecane conversion was maintained at above 95% for 5 h. In addition, the concentration of CO gas at S/C = 0.5 was the highest compared to that at other S/C ratios, and it decreased with the increasing S/C ratios. The initial selectivity of H2 and CO2 showed an opposite trend to that of CO. These results are attributed to the fact that an increase in steam ratio was because of the WGS reaction, leading to an increase in the selectivity of H2 and CO2. The composition of dry product gases at increased S/C ratios resembled the conventional thermodynamic equilibrium performance as reported previously [33]. Figure 7 shows the XRD patterns of the auto-reduced NA10-PM at different S/C ratios (0.5, 1.23, and 2.75), O2/C = 0.25, and GHSV = 12,000 h–1 at 750 °C. Metallic nickel increased with the increase in S/C ratios. With S/C = 2.75, NiAl2O4 was completely transformed to metallic nickel and the two angle of NiAl2O4 was completely shifted to –Al2O3. Considering the amount of steam in the feed, the dodecane conversion, and the selectivity of H2 and CO gases, S/C = 1.23 was selected as the optimal condition.
Figure 8 shows the dodecane conversions and selectivity attained with the auto-reduced NA10-PM catalyst under various O2/C ratios (0.05, 0.15, 0.25, and 0.35), S/C = 1.23, and GHSV = 12,000 h−1 at 750 °C, conducted in order to elucidate the effect of the O2/C ratio on catalytic performance. Under all conditions, the dodecane conversion was above 85% during the initial reaction period. However, the conversions decreased with increasing reaction times, except for O2/C = 0.25. The selectivity of CO, H2, and CH4 among the dry gases decreased slightly with the increase in O2/C ratio, while the concentration of CO2 increased. In particular, the dodecane conversion was only maintained at O2/C = 0.25. To investigate this phenomenon, the XRD patterns are depicted in Figure 9. It was found that the peak intensity of the two angle assigned to metallic nickel after the reaction at O2/C = 0.05 and 0.35 was lower than that at O2/C = 0.25. With a low O2 concentration, the amount of heat emitted by partial oxidation decreased, which caused the dodecane conversion to gradually decrease because of insufficient heat produced in the steam reforming of dodecane. Moreover, this phenomenon could be further accelerated because the catalyst was not sufficiently reduced, as shown by XRD. On the contrary, under high O2 concentrations, although the dodecane conversion was relatively higher during the initial reaction period, the auto-reduced NA10-PM catalyst was suddenly deactivated. It could only be inferred that the oxidation reaction of reduced metallic nickel after the initial reaction by unreacted oxygen during reforming was more dominant than the reduction of NiAl2O4 by product gases (CO and H2). The O2 amount in the feed was more important in maintaining the dodecane conversion of the auto-reduced NA10-PM catalyst at the S/C ratio of 1.23, rather than the amount of steam. The optimum conditions to maintain the maximum catalytic performance on the auto-reduced NA10-PM catalyst were S/C = 1.23 and O2/C = 0.25 at 750 °C.
To evaluate catalytic stability, dodecane conversion obtained using auto-reduced NA10-PM catalyst was compared with those obtained using H2-reduced NA10-IM and NA10-PM catalysts under conditions of S/C = 1.23, O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C (Figure 10). The dodecane conversion by H2-reduced NA10-IM catalyst was initially increased slightly up to 75% and was maintained at that value, followed by a slow decrease. On the other hand, dodecane conversion by H2-reduced NA10-PM was maintained at 83% for 5 h and subsequently decreased slightly to 76%. On the other hand, the dodecane conversion by auto-reduced NA10-PM was initially 93%, which increased up to 97% at 17 h. In order to elucidate this phenomenon, the nitrogen adsorption-desorption isotherms and XRD patterns of the auto-reduced NA10-PM catalyst after reaction were analyzed. As shown in Figure 11a, the catalyst showed type V nitrogen adsorption-desorption isotherms after reaction, unlike those of the fresh and reduced catalysts. As shown in Figure 11b, the XRD patterns of the catalyst showed more obvious metallic Ni peak after reaction, compared to that of the auto-reduced catalyst. Based on these results, it was anticipated that the NA10-PM catalyst was auto-reduced by product gases obtained from thermal decomposition of dodecane, and the thus-activated catalyst produced CO and H2 via the ATR reaction. Moreover, the activated catalyst was further reduced by CO and H2 during the reaction.

3. Materials and Methods

3.1. Preparation of Catalysts

The nickel-alumina catalyst was prepared by the PM method devised for the homogenous distribution of Ni on the catalyst. Nickel (II) nitrate (Ni(NO3)2·6H2O) and aluminum nitrate (Al(NO3)3·9H2O) were dissolved in 15 mL of ethylene glycol (EG) by stirring in a beaker at room temperature. Then, 15 mL of methanol and 1.5 g of poly(methyl methacrylate) (PMMA) colloidal crystals (MW = 500,000–1,000,000) were added to the EG solution, and the solution was stirred on a hot plate at 100 °C until the solution was solidified. The obtained powder sample was dried at 250 °C and calcined at 750 °C for 4 h under air; in this procedure, all the solvents and PMMA were removed. The amount of nickel oxide in the catalyst was 10 wt%; thus, this sample was named NA10-PM [22,23]. To compare the catalytic properties of NA10-PM, nickel-alumina (NA10-IM), ruthenium-alumina (RuA5-IM), and rhodium-alumina (RhA5-IM) catalysts were also prepared by the conventional impregnation method (IM). Three separate solutions were prepared by dissolving Ni(NO3)2·6H2O, ruthenium (III) chloride (RuCl3·xH2O), and rhodium chloride (RhCl3·xH2O) in water. Then, –Al2O3 was added to each solution and the mixtures were stirred at room temperature for 1 h. Each suspension was subsequently evaporated via vacuum evaporation. The resulting powders were dried at 250 °C and calcined at 750 °C for 4 h under air. The amount of nickel in the catalyst was 10 wt%, while those of ruthenium and rhodium were 5 wt% each.

3.2. Characterization

The reduction profiles for the NA10-PM (0.2 g) catalyst were obtained by heating the samples from 120 to 800 °C at 10 °C/min in a fixed-bed reactor under flowing H2 or CO and H2. The outlet gases from the reactor were analyzed using a thermal conductivity detector (TCD; Donam Systems Inc., Seongnam, Korea). The textural properties such as BET surface area, pore volume, and average pore size were determined using the Micrometrics ASAP 2020 apparatus (Norcross, GA, USA). The crystal structures of the catalysts were analyzed using a Cu Ka radiation source in a Phillips XPERT X-ray diffraction (XRD) unit at the Korea Basic Science Institute in Daegu. In order to compare the effect of auto-reduction temperature on the reducibility of the catalyst by thermal decomposition of dodecane, the textural properties and XRD patterns of fresh and reduced NA10-PM were investigated. The NA10-PM catalyst was reduced by conventional H2 reduction and auto-reduction. For conventional H2 reduction, NA10-PM was analyzed after reduction under 10% H2 at 750 °C for 2 h. For auto-reduction, the catalyst was analyzed after auto-reduction by thermal decomposition of n-dodecane, with feed gas condition of S/C = 1.23 and O2/C = 0.25 at various reaction temperatures (650, 700, and 750 °C) for 2 h.

3.3. Catalytic Reforming Measurement

The prepared catalyst (0.5 g) with a particle size of 150–250 µm was packed in the middle of a quartz reactor. The quartz reactor was heated using an electronic furnace and a constant temperature was maintained. The flow rates of gases such as N2 and air were controlled by a mass flow controller. n-Dodecane from Sigma-Aldrich (Yongin, Korea) was selected as a surrogate for diesel fuel because it is regarded to have similar properties. First, n-dodecane and water were injected into the vaporizer using a syringe pump and vaporized at 350 °C. The vapors were carried by N2 into the entrance of the reactor. Condensable liquids were removed before entering the gas chromatograph (GC). The catalytic performances were investigated under various conditions such as varying S/C and O2/C molar ratios.
The n-dodecane conversion and the selectivity of product gases such as H2, CO, CO2, and CH4 were calculated according to Equations (1) and (2), respectively.
Dodecane   conversion   ( % ) = ( F C O ⋅ O u t + F C O 2 ⋅ O u t + F C H 4 ⋅ O u t F C 12 H 26 ⋅ I n × 12 ) × 100
Selectivity   of   product   gas   ( % ) = ( F p r o d u c t ⋅ O u t   F H 2 ⋅ O u t + F C O ⋅ O u t + F C O 2 ⋅ O u t + F C H 4 ⋅ O u t ) × 100

4. Conclusions

To enhance the efficiency of the nickel-alumina catalyst in the ATR of Solid Oxide Fuel Cell, polymer-modified incipient (PM) method was used to prepare the NA10-PM catalyst, which showed excellent performance and economic feasibility compared to other catalysts prepared by the impregnation method (IM), such as NA10-IM, RuA5-IM, RhA5-IM. The NA10-PM catalyst was initially auto-reduced by product gases obtained from thermal decomposition of dodecane. Notably, the crystal structure of the auto-reduced NA10-PM catalyst was completely changed to metallic nickel from NiAl2O4 of the fresh state. Moreover, the effects of various reaction parameters such as steam/carbon (S/C) and oxygen/carbon (O2/C) molar ratios were investigated to determine the optimum reaction conditions. The catalytic performance was more affected by the concentration of oxygen than by steam in the feed. The auto-reduced NA10-PM catalysts showed excellent conversion of dodecane and excellent catalytic stability compared to those of the H2-reduced NA10-IM and NA10-PM catalysts. Interestingly, the highest catalytic performance of auto-reduced NA10-PM was achieved for the reaction under the conditions of S/C = 1.23, O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C. Based on the BET and XRD results, it was proposed that the activated catalyst was more reduced by CO and H2 produced from the thermal decomposition of dodecane during the ATR reaction. Therefore, the auto-reduced NA10-PM catalyst was applied successfully for the auto-thermal reforming of dodecane.

Supplementary Materials

The following are available online at https://www.mdpi.com/2073-4344/8/9/371/s1, Figure S1: Thermal decomposition of n-dodecane with under S/C = 1.23 and O2/C = 0.25 at 750 °C. Figure S2: (a) Nitrogen adsorption-desorption isotherms and (b) XRD patterns of fresh and auto-reduced NA10-PM at various temperature (650, 700, and 750 °C) for 2 h.

Author Contributions

S.Y.J. and D.G.J. designed the experiments, S.C.L. and J.C.K. supervised the entire study; S.B.J. and D.G.J. performed the experiments and wrote the manuscript, D.S.H. and H.J.C. contributed to scientific discussions.

Acknowledgments

This work was supported by Priority Research Centers Program through the National Research Foundation of Korea (NRF) funded by the Ministry of Education, Science, and Technology (2009-0093819). This research was supported by Basic Science Research Program through the National Research Foundation of Korea (NRF) funded by the Ministry of Science, ICT & Future Planning (No. 2017R1A2B4008275).

Conflicts of Interest

The authors declare no conflict of interest.

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Figure 1. (a) Dodecane conversion and (b) initial selectivity of various auto-thermal catalysts under S/C = 1.23 and O2/C = 0.25 at 700 °C.
Figure 1. (a) Dodecane conversion and (b) initial selectivity of various auto-thermal catalysts under S/C = 1.23 and O2/C = 0.25 at 700 °C.
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Catalysts 08 00371 g002 550
Figure 2. Temperature-programed reduction (TPR) profiles of the NA10-PM catalyst under (a) H2-reduction and (b) auto-reduction condition.
Figure 2. Temperature-programed reduction (TPR) profiles of the NA10-PM catalyst under (a) H2-reduction and (b) auto-reduction condition.
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Catalysts 08 00371 g003 550
Figure 3. (a) Nitrogen adsorption-desorption isotherms and (b) XRD patterns of the fresh and reduced NA10-PM, activated by conventional H2 reduction and by auto-reduction at 750 °C for 2 h.
Figure 3. (a) Nitrogen adsorption-desorption isotherms and (b) XRD patterns of the fresh and reduced NA10-PM, activated by conventional H2 reduction and by auto-reduction at 750 °C for 2 h.
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Figure 4. (a) Dodecane conversion and (b) initial selectivity of H2-reduced and NA10-PM at various temperatures (650, 700, and 750 °C) under S/C =1.23 and O2/C = 0.25.
Figure 4. (a) Dodecane conversion and (b) initial selectivity of H2-reduced and NA10-PM at various temperatures (650, 700, and 750 °C) under S/C =1.23 and O2/C = 0.25.
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Figure 5. (a) Dodecane conversion and (b) initial selectivity of auto-reduced and NA10-PM at various temperatures (650, 700, and 750 °C) under S/C =1.23 and O2/C = 0.25.
Figure 5. (a) Dodecane conversion and (b) initial selectivity of auto-reduced and NA10-PM at various temperatures (650, 700, and 750 °C) under S/C =1.23 and O2/C = 0.25.
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Catalysts 08 00371 g006 550
Figure 6. Effect of S/C ratio on catalytic performance: (a) Dodecane conversion and (b) initial selectivity of auto-reduced NA10-PM catalyst under O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C.
Figure 6. Effect of S/C ratio on catalytic performance: (a) Dodecane conversion and (b) initial selectivity of auto-reduced NA10-PM catalyst under O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C.
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Figure 7. XRD patterns of auto-reduced NA10-PM catalyst after reaction at various S/C ratios for 5 h under O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C.
Figure 7. XRD patterns of auto-reduced NA10-PM catalyst after reaction at various S/C ratios for 5 h under O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C.
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Figure 8. Effect of O2/C ratio on catalytic performance: (a) Dodecane conversion and (b) initial selectivity of auto-reduced NA10-PM catalyst under S/C = 1.23, and GHSV = 12,000 h−1 at 750 °C.
Figure 8. Effect of O2/C ratio on catalytic performance: (a) Dodecane conversion and (b) initial selectivity of auto-reduced NA10-PM catalyst under S/C = 1.23, and GHSV = 12,000 h−1 at 750 °C.
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Figure 9. XRD patterns of auto-reduced NA10-PM catalyst after reaction at various O2/C ratios for 5 h under S/C = 1.23, and GHSV = 12,000 h−1 at 750 °C.
Figure 9. XRD patterns of auto-reduced NA10-PM catalyst after reaction at various O2/C ratios for 5 h under S/C = 1.23, and GHSV = 12,000 h−1 at 750 °C.
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Figure 10. Stability comparison of the auto-reduced NA10-PM catalyst with the H2-reduced NA10-IM and NA10-PM catalysts under conditions of S/C = 1.23, O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C.
Figure 10. Stability comparison of the auto-reduced NA10-PM catalyst with the H2-reduced NA10-IM and NA10-PM catalysts under conditions of S/C = 1.23, O2/C = 0.25, and GHSV = 12,000 h−1 at 750 °C.
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Figure 11. (a) Nitrogen adsorption-desorption isotherms and (b) XRD patterns of NA10-PM catalyst.
Figure 11. (a) Nitrogen adsorption-desorption isotherms and (b) XRD patterns of NA10-PM catalyst.
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Table
Table 1. Textural properties of fresh and reduced NA10-PM catalyst activated by conventional H2-reduction and by auto-reduction at 750 °C for 2 h.
Table 1. Textural properties of fresh and reduced NA10-PM catalyst activated by conventional H2-reduction and by auto-reduction at 750 °C for 2 h.
BET Surface Area (m2/g)Pore Volume (cm3/g)Average Pore Size (nm)
Fresh28.10.043.8
H2-reduction78.10.063.8
Auto-reduction96.60.124.1

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MDPI and ACS Style

Jo, S.B.; Ju, D.G.; Jung, S.Y.; Ha, D.S.; Chae, H.J.; Lee, S.C.; Kim, J.C. Performance of an Auto-Reduced Nickel Catalyst for Auto-Thermal Reforming of Dodecane. Catalysts 2018, 8, 371. https://doi.org/10.3390/catal8090371

AMA Style

Jo SB, Ju DG, Jung SY, Ha DS, Chae HJ, Lee SC, Kim JC. Performance of an Auto-Reduced Nickel Catalyst for Auto-Thermal Reforming of Dodecane. Catalysts. 2018; 8(9):371. https://doi.org/10.3390/catal8090371

Chicago/Turabian Style

Jo, Seong Bin, Dong Geon Ju, Suk Yong Jung, Dong Su Ha, Ho Jin Chae, Soo Chool Lee, and Jae Chang Kim. 2018. "Performance of an Auto-Reduced Nickel Catalyst for Auto-Thermal Reforming of Dodecane" Catalysts 8, no. 9: 371. https://doi.org/10.3390/catal8090371

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