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Article

In Situ Regeneration and Deactivation of Co-Zn/H-Beta Catalysts in Catalytic Reduction of NOx with Propane

by
Hua Pan
1,
Dongmei Xu
1,
Chi He
2,* and
Chao Shen
1,*
1
College of Biology and Environment Engineering, Zhejiang Shuren University, Hangzhou 310015, China
2
School of Energy and Power Engineering, Xi’an Jiaotong University, Xi’an 710049, China
*
Authors to whom correspondence should be addressed.
Catalysts 2019, 9(1), 23; https://doi.org/10.3390/catal9010023
Submission received: 23 October 2018 / Revised: 22 December 2018 / Accepted: 24 December 2018 / Published: 30 December 2018
(This article belongs to the Special Issue Catalysts Deactivation, Poisoning and Regeneration)
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Abstract

:
Regeneration and deactivation behaviors of Co-Zn/H-Beta catalysts were investigated in NOx reduction with C3H8. Co-Zn/H-Beta exhibited a good water resistance in the presence of 10 vol.% H2O. However, there was a significant drop off in N2 yield in the presence of SO2. The formation of surface sulfate and coke decreased the surface area, blocked the pore structure, and reduced the availability of active sites of Co-Zn/H-Beta during the reaction of NO reduction by C3H8. The activity of catalyst regenerated by air oxidation followed by H2 reduction was higher than that of catalyst regenerated by H2 reduction followed by air oxidation. Among the catalysts regenerated by air oxidation followed by H2 reduction with different regeneration temperatures, the optimal regeneration temperature was 550 °C. The textural properties of poisoned catalysts could be restored to the levels of fresh catalysts by the optimized regeneration process. The regeneration process of air oxidation followed by H2 reduction could recover the active sites of cobalt and zinc species from sulfate species, as well as eliminate coke deposition on poisoned catalysts. The regeneration pathway of air oxidation followed by H2 reduction is summarized as initial removal of coke by air oxidation and final reduction of the sulfate species by H2.

1. Introduction

Selective catalytic reduction of NOx by hydrocarbons (HC-SCR) was considered a promising technology for NOx removal [1]. Among the HC-SCR catalysts, Co/Beta has attracted much attention due to its excellent activity and N2 selectivity [2,3,4,5,6,7]. The long-term stability [3], nature of active sites [4], influences of Co loading and precursor [5], preparation method [6], and mechanism of HC-SCR [7] have been widely investigated on Co/Beta, especially for C3H8-SCR [2,3,4,5,6]. To improve the stability and activity of Co/zeolites in HC-SCR, many studies also focused on the modification of Co/zeolites by adding promoters, such as Co-Pd/HBeta [8], Co-In/ferrierite [9], and Co-Zn/HZSM-5 [10].
Sulfur tolerance is a great challenge for deNOx catalysts. Unfortunately, Co-based zeolites exhibited unsatisfactory activity in the presence of SO2 [11,12]. On the other hand, coke formation, originating from hydrocarbons, also resulted in the deactivation of deNOx catalysts for HC-SCR [13]. H2 reduction is widely used for the regeneration treatment of catalysts deactivated by SO2, such as NOx storage-reduction (NSR) catalysts [14,15,16,17,18], and catalytic reduction of NO by NH3 (NH3-SCR) catalysts [19,20]. In the case of catalysts deactivated by coke deposition, air calcination was considered as an efficient regeneration method [21,22,23,24,25]. Hence, a regeneration process that combines H2 reduction with air oxidation may be a potential technology for in situ regeneration of deNOx catalysts in HC-SCR. To our knowledge, no reports focused on the regeneration of HC-SCR catalysts deactivated by dual impacts of SO2 and coke deposition.
In the present paper, Co-Zn/H-Beta was chosen as a deNOx catalyst for C3H8-SCR, because it showed good catalytic activity [26]. The regeneration of Co-Zn/H-Beta catalysts deactivated by SO2 and coke deposition was performed in a combined in situ process of air oxidation and H2 reduction. The effects of the regeneration sequence and regeneration temperature on the regeneration efficiency were investigated.

2. Results and Discussion

2.1. Stability of Catalyst

Figure 1 illustrates the influences of SO2 and H2O on the activity of Co-Zn/H-Beta at 450 °C for 80 h. Co-Zn/H-Beta had excellent catalytic activity, with 95% N2 yield obtained for C3H8-SCR at 450 °C without addition of SO2 and H2O. The catalytic activity decreased slightly in the presence of 10 vol.% H2O. Upon removing H2O from the feeding gas, N2 yield almost returned to its original level. This demonstrates that Co-Zn/H-Beta displays a good water resistance. However, N2 yield declined significantly during 50–200 ppm SO2 co-feeding for 15 h. Only 64% N2 yield was achieved when 200 ppm SO2 was added into the feeding gas. Upon switching off the SO2, N2 yield increased from 64% to 71.5%, which was far away from the initial activity of 95%. When both 10 vol.% H2O and 200 ppm SO2 were added simultaneously for 7 h, N2 yield further dropped from 71.5% to 62%. Upon switching off the SO2 and H2O, a partial recovery of catalytic activity was observed. However, N2 yield decreased gradually after aging for 40 h without adding SO2 and H2O. After the stability experiment, the color of the catalyst turned from light gray to black. This demonstrates that carbon deposition occurs on Co-Zn/H-Beta catalysts during the reaction of NO reduction by C3H8.

2.2. Regeneration Performance

Figure 2 presents the influence of regeneration sequence on the activity of the poisoned catalyst at a fixed regeneration temperature of 450 °C. Compared with the poisoned Co-Zn/H-Beta-D catalysts, the regenerated catalysts exhibited higher activity. The activity of regenerated catalysts decreased in the order of: Co-Zn/H-Beta-R (O2 + H2, 450 °C) > Co-Zn/H-Beta-R (H2 + O2, 450 °C) > Co-Zn/H-Beta-R (H2, 450 °C) > Co-Zn/H-Beta-R (O2, 450 °C). Interestingly, Co-Zn/H-Beta-R (O2 + H2, 450 °C) displayed higher activity than Co-Zn/H-Beta-R (H2 + O2, 450 °C). This suggests that combined regeneration is better than single regeneration, and air oxidation followed by H2 reduction is an optimal regeneration sequence for the deactivated Co-Zn/H-Beta catalyst in C3H8-SCR.
Figure 3 exhibits the effect of regeneration temperatures on the activity of the catalysts regenerated by the combined regeneration process. The catalytic activity of both Co-Zn/H-Beta-R (O2 + H2) and Co-Zn/H-Beta-R (H2 + O2) catalysts increased with the regeneration temperature from 450 to 550 °C. The regenerated Co-Zn/H-Beta-R (O2 + H2, 550 °C) displayed similar activity to the fresh catalyst. This indicates that the optimal regeneration temperature was 550 °C. Compared to off-site treatment of solution washing [27] and in situ regeneration by H2 reduction for deactivated deNOx catalysts [28], the in situ regeneration process of air oxidation followed by H2 reduction showed more convenient operation and higher regeneration efficiency, respectively. Thus, although this comparison may be taken with caution because different reaction conditions were employed, the in situ regeneration process of air oxidation followed by H2 reduction is a promising technology for the regeneration of deactivated Co-Zn/H-Beta catalyst.

2.3. Structural and Textural Properties of Catalysts

Table 1 illustrates the textural properties of the samples. Compared with the Co-Zn/H-Beta-F sample, a significant decrease in surface area, microporous area, and pore volume was detected for the Co-Zn/H-Beta-D catalysts. This implies that sulfate species and coke were deposited both on the surface and in the micropores of the deactivated catalysts. For the regenerated catalysts, surface area, microporous area, and pore volume greatly increased after both the combined regeneration process and single regeneration process. Co-Zn/H-Beta-R (O2 + H2, 550 °C) even showed similar values of textural properties to the fresh sample. This implies that air oxidation followed by H2 reduction at 550 °C could eliminate the sulfates and coke deposited over the deactivated Co-Zn/H-Beta.
The X-ray diffraction patterns (XRD) of Co-Zn/H-Beta catalysts are shown in Figure 4. The position of the main diffraction peak around 2θ = 22.4° is generally taken as evidence of lattice contraction/expansion of the Beta structure [29,30]. The peaks at 21.8°, 25.1°, 28.4°, 29.3°, and 43.6° were assigned to Beta-type zeolite. The deactivated and regenerated catalysts preserved the typical Beta crystal structure. The diffraction peaks of Co3O4 (PDF#73-1701), CoO (PDF#71-1178), and Zn(OH)2 (PDF#74-0094 and PDF#71-2115) were detected for all samples. However, the diffraction peak intensity of Zn(OH)2 in the deactivated catalyst was weaker than in the fresh and regenerated samples. No new peak related to sulfate species was observed on any sample. This implies that sulfate species might exist as amorphous bulk species, which could not be detected by XRD.
To identify the state of surface species on various catalysts, the samples were measured by XPS. In Figure 5, the significant movement of the binding energy value of Co 2p3/2 was observed for both deactivated and regenerated samples, compared to the fresh sample. The binding energy of Co 2p3/2 shifted toward a lower value (778.6 eV) in the deactivated catalyst. However, the Co 2p3/2 peaks of regenerated catalysts were shifted to a higher binding energy (781.4–782.7 eV). In Co 2p spectra, shake-up peaks were observed for all samples. This means that metallic cobalt was absent in all samples, because the spectrum of metallic cobalt does not contain shake-up satellite structure at all [31]. Table 1 illustrates the results of Co 2p in the fresh, deactivated, and regenerated catalysts. According to the position of the Co 2p3/2 peak and interval between Co 2p3/2 and Co 2p1/2, CoO, Co3O4, Co(OH)2, and ZnCo2O4 were present in the fresh sample [32,33]. For the deactivated catalyst, the lowest binding energy of Co 2p3/2 (778.6 eV) and highest interval between Co 2p3/2 and Co 2p1/2 (17.2 eV) were observed, which was quite different from other catalysts in Table 1. This implies that sulfate species were generated on the surface of the deactivated catalyst. For Co-Zn/H-Beta-R (H2 + O2, 450 °C), the highest binding energy of Co 2p3/2 (782.7 eV) and lowest interval between Co 2p3/2 and Co 2p1/2 (14.6 eV) were detected among all catalysts. Cobalt species mainly exist as a CoAl2O4 state on Co-Zn/H-Beta-R (H2 + O2, 450 °C) [33]. CoAl2O4 was recognized to be inactive for NO-SCR [34,35]. Thus, the catalytic activity of Co-Zn/H-Beta-R (H2 + O2, 450 °C) was lower than that of Co-Zn/H-Beta-R (O2 + H2) catalysts (Figure 2). In the case of Co-Zn/H-Beta-R (O2 + H2) catalysts, the binding energy value of Co 2p3/2 was from 781.4 to 782.5 eV, and the interval between Co 2p3/2 and Co 2p1/2 was about 15.1 eV. This indicates that CoO, Co3O4, Co(OH)2, and ZnCo2O4 were present in Co-Zn/H-Beta-R (O2 + H2) catalysts [32,33]. Therefore, the regeneration process of air oxidation followed by H2 reduction could promote the recovery of the deactivated cobalt species.
Figure 6 presents XPS spectra of the Zn 2p regions for the fresh, deactivated, and regenerated catalysts. For all samples, binding energy of Zn 2p3/2 and interval between Zn 2p3/2 and Zn 2p1/2 were 1022–1023 eV and 23 eV, respectively, which could be attributed to Zn(OH)+ [36] or ZnO [37]. Compared to the fresh sample, a lower binding energy of Zn 2p3/2 was observed for the deactivated sample, which was similar with the variation trend of Co 2p3/2 lines. The binding energy of Zn 2p3/2 shifting to a lower value may be due to the formation of sulfate species on the surface of the deactivated catalysts. For Co-Zn/H-Beta-R (O2 + H2) catalysts, the position of the binding energy of Zn 2p3/2 and Zn 2p1/2 was the same as the fresh sample. However, a lower binding energy of Zn 2p3/2 and Zn 2p1/2 was also observed for Co-Zn/H-Beta-R (H2 + O2, 450 °C), which was similar with the deactivated sample. Thus, regeneration sequence was important to the regeneration of poisoned catalysts. The peak intensity of both Co 2p3/2 and Zn 2p3/2 was enhanced with the increase of regeneration temperature from 450 to 550 °C, meaning that a regeneration temperature of 550 °C is optimal.
Figure 7 presents the H2-temperature programmed reduction (H2-TPR) of Co-Zn/H-Beta catalysts. The TPR peak centered at around 345 °C is ascribed to the reduction of Co3O4 [38]. The peaks centered at 423 °C and 512 °C could correspond to the reduction of CoOx on the catalyst surface and in the catalyst pore, respectively [38]. The broad peaks centered at 550 °C and 565 °C could be ascribed to the reduction of sulfate and CoAl2O4, respectively. The high temperature reduction peaks of 620 °C and 800 °C may be assigned to the reduction peaks of Zn(OH)+ and ZnO, respectively. The reduction peak of sulfate (550 °C) is clearly detected for Co-Zn/H-Beta-D and Co-Zn/H-Beta-R (O2, 450 °C) catalysts. Thus, air oxidation could not remove sulfate on deactivated catalysts. The reduction peak of CoAl2O4 was observed for Co-Zn/H-Beta-R (H2 + O2, 450 °C), but not for Co-Zn/H-Beta-R (O2 + H2, 450 °C), Co-Zn/H-Beta-R (O2 + H2, 550 °C), and Co-Zn/H-Beta-R (H2, 450 °C). This may be due to the diffusion of Co species on the surface into the pore of zeolite, and interaction with extra-framework Al3+ cations at high temperature during the SCR reaction and regeneration process, resulting in the formation of CoAl2O4 [39]. This means that air oxidation can promote the formation of CoAl2O4, while H2 reduction could inhibit CoAl2O4 formation. CoAl2O4 was recognized to be inactive for HC-SCR [34,35]. Therefore, air oxidation followed by H2 reduction is an optimal regeneration sequence for the deactivated Co-Zn/H-Beta catalysts in C3H8-SCR.
Figure 8 shows thermo gravimetric analysis (TGA) curves of various catalysts. The weight loss of all samples in the temperature range of 50–200 °C can be attributed to the desorption of H2O. However, the deactivated catalyst displayed another stage of weight losses at temperatures above 650 °C, which corresponded to the combustion of coke and sulfate deposited on the catalyst. The regenerated (Co-Zn/H-Beta-R (H2 + O2, 450 °C)) sample showed slighter weight losses than the deactivated sample did at temperatures above 650 °C. Interestingly, no significant weight losses were observed for the regenerated (Co-Zn/H-Beta-R (O2 + H2, 550 °C)) sample. This further indicates that a combined in situ regeneration process of air oxidation followed by H2 reduction at 550 °C is efficient for regeneration of Co-Zn/H-Beta in C3H8-SCR. In summary, the regeneration pathway is illustrated in Scheme 1. Coke on the deactivated catalyst was initially removed by air oxidation at 550 °C. Finally, the sulfate species were reduced to the active cobalt and zinc species by H2 at 550 °C.

3. Materials and Methods

3.1. Catalyst Preparation

Beta zeolite with an atomic ratio Si/Al = 25 was purchased commercially in H-form from Nankai University (Tianjin, China). Co-Zn/H-Beta catalysts were synthesized according to the method described elsewhere [40], using Co(NO3)2 and Zn(NO3)2 as precursors. All the chemicals were purchased from Macklin Inc. (Shanghai, China). The cobalt and zinc content of Co-Zn/H-Beta was 2 wt.%. The fresh samples were noted as Co-Zn/H-Beta-F.

3.2. Deactivation and Regeneration of Catalysts

In the deactivation process, the samples were exposed to a mixture of 50–200 ppm SO2, 600 ppm NO, 25 ppm NO2, 600 ppm C3H8, 6 vol.% O2, 10 vol.% H2O, and balance of N2 at 450 °C for 45 h. The deactivated catalysts were denoted as Co-Zn/H-Beta-D. All the gases were purchased from Hangzhou Jingong Special Gas Co., Ltd. (Hangzhou, China).
The deactivated catalysts were regenerated by 60 mL min−1 air and 400 mL min−1 5 vol.% H2/Ar at regeneration temperatures from 450 to 550 °C for 60 min. The regenerated catalysts were denoted as Co-Zn/H-Beta-R (O2, H2, O2 + H2, and H2 + O2, T), where O2 means that the deactivated catalysts were regenerated by air oxidation, and H2 means that the deactivated catalysts were regenerated by H2 reduction. O2 + H2 means that the deactivated catalysts were regenerated by air oxidation followed by H2 reduction. H2 + O2 means that the deactivated catalysts were regenerated by H2 reduction followed by air oxidation. T is the regeneration temperature.

3.3. Catalytic Activity Measurement

Catalytic activity tests were performed in a self-made packed-bed flow micro-reactor (1 cm i.d.), operating at atmospheric pressure. A 1.5 mL (0.73 g) volume of catalyst powder was held on a quartz frit at the center of the reactor. A typical feeding gas composition was 600 ppm NO, 25 ppm NO2, 600 ppm C3H8, and 6 vol.% O2, with N2 as the balance gas. Each feeding gas flow rate was controlled independently by a mass flow controller (D07, Beijing Sevenstar Electronics Co.,Ltd., Beijing, China). The overall flow rate was 460 mL min−1, which was equal to a space velocity of 18,400 h−1.
NO and NO2 concentrations were continuously monitored by an infrared gas analyzer (Xi’an Juneng Corporation, Xi’an, China). The products were analyzed using a gas chromatograph (Linghua GC9890, Shanghai Ling-Hua Instrument Co., Ltd, Shanghai, China) equipped with a thermal conductivity detector (TCD). A porapak Q column (Shanghai Ling-Hua Instrument Co., Ltd., Shanghai, China) was used for separation of CO2, N2O and NO. The data was collected in the steady state reaction. In this work, N2 selectivity is over 95%, because N2O concentration is below 10 ppm. Thus, the catalytic activity was assessed in terms of the following equation:
N 2   yield   ( % ) = ( NO in + NO 2 , in ) − ( NO out + NO 2 , out + 2 N 2 O out ) ( NO in + NO 2 , in ) × 100 %

3.4. Catalyst Characterizations

N2 adsorption isotherms (ASAP2460, Micromeritics Instrument (Shanghai) Ltd., Shanghai, China) and XRD (Rigaku, Tokyo, Japan) and XPS (PHI-5000C ESCA system, Perkin–Elmer, Waltham, MA, USA) measurements were carried out according to the method described in our previous work [41]. TGA was conducted on an HCR-3 analyzer (Beijing Henven Scientific Instrument Co., Ltd., Beijing, China) from 30 to 800 °C under air, with a heating rate of 5 °C/min.

4. Conclusions

Co-Zn/H-Beta catalysts exhibited a poor stability in the presence of SO2 and H2O for C3H8-SCR, due to SO2 poisoning and carbon deposition. The formation of surface sulfate and coke reduced the availability of surface active sites and textural properties of the catalysts. Coke deposition and surface sulfate could be reduced by the combined processes of air oxidation followed by H2 reduction in situ. The combined process of air oxidation followed by H2 reduction is an available technology for the regeneration of Co-Zn/H-Beta catalysts in C3H8-SCR, for removing NOx from lean-burn and diesel exhausts.

Author Contributions

Conceptualization, H.P. and C.H.; Investigation, H.P. and D.X.; Supervision, C.S.; Writing-original draft, H.P.

Funding

This work was financially supported by the National Natural Science Foundation of China (21677114), Natural Science Foundation of Zhejiang Province of China (LY19E080023), and Young and middle-aged academic team project of Zhejiang Shuren University. We also acknowledge the support of Key Laboratory of Microbial Technology for Industrial Pollution Control of Zhejiang Province.

Conflicts of Interest

The authors declare no conflict of interest.

References

  1. Mendes, A.N.; Ribeiro, M.F.; Henriques, C.; Da Costa, P. On the Effect of Preparation Methods of PdCe-MOR Catalysts as NOx CH4-SCR System for Natural Gas Vehicles Application. Catalysts 2015, 5, 1815–1830. [Google Scholar] [CrossRef]
  2. Tabata, T.; Ohtsuka, H.; Sabatino, L.M.F.; Bellussi, G. Selective catalytic reduction of NOx by propane on Co-loaded zeolites. Microporous Mesoporous Mater. 1998, 21, 517–524. [Google Scholar] [CrossRef]
  3. Tabata, T.; Kokitsu, M.; Ohtsuka, H.; Okada, O.; Sabatino, L.M.F.; Bellussi, G. Study on catalysts of selective reduction of NOx using hydrocarbons for natural gas engines. Catal. Today 1996, 27, 91–98. [Google Scholar] [CrossRef]
  4. Ohtsuka, H.; Tabata, T.; Okada, O.; Sabatino, L.M.F.; Bellussi, G. A study on selective reduction of NOx by propane on Co-Beta. Catal. Lett. 1997, 44, 265–270. [Google Scholar] [CrossRef]
  5. Chen, H.H.; Shen, S.C.; Chen, X.Y.; Kawi, S. Selective catalytic reduction of NO over Co/beta-zeolite: Effects of synthesis condition of beta-zeolites, Co precursor, Co loading method and reductant. Appl. Catal. B Environ. 2004, 50, 37–47. [Google Scholar] [CrossRef]
  6. Čapek, L.; Dědeček, J.; Sazama, P.; Wichterlová, B. The decisive role of the distribution of Al in the framework of beta zeolites on the structure and activity of Co ion species in propane-SCR–NOx in the presence of water vapour. J. Catal. 2010, 272, 44–54. [Google Scholar] [CrossRef]
  7. Pietrzyk, P.; Dujardin, C.; Gora-Marek, K.; Granger, P.; Sojka, Z. Spectroscopic IR, EPR, and operando DRIFT insights into surface reaction pathways of selective reduction of NO by propene over the Co–BEA zeolite. Phys. Chem. Chem. Phys. 2012, 14, 2203–2215. [Google Scholar] [CrossRef]
  8. Ferreira, A.P.; Henriques, C.; Ribeiro, M.F.; Ribeiro, F.R. SCR of NO with methane over Co-HBEA and PdCo-HBEA catalysts: The promoting effect of steaming over bimetallic catalyst. Catal. Today 2005, 107–108, 181–191. [Google Scholar] [CrossRef]
  9. Kubacka, A.; Janas, J.; Sulikowski, B. In/Co-ferrierite: A highly active catalyst for the CH4-SCR NO process under presence of steam. Appl. Catal. B Environ. 2006, 69, 43–48. [Google Scholar] [CrossRef]
  10. Ren, L.L.; Zhang, T.; Liang, D.B.; Xu, C.H.; Tang, J.W.; Lin, L.W. Effect of addition of Zn on the catalytic activity of a Co/HZSM-5 catalyst for the SCR of NOx with CH4. Appl. Catal. B Environ. 2002, 35, 317–321. [Google Scholar] [CrossRef]
  11. Zhang, J.Q.; Liu, Y.Y.; Fan, W.B.; He, Y.; Li, R.F. Effect of SO2 on Catalytic Performance of CoH-FBZ for Selective Catalytic Reduction of NO by CH4 in The Presence of O2. Environ. Eng. Sci. 2007, 24, 292–300. [Google Scholar] [CrossRef]
  12. Chen, S.W.; Yan, X.L.; Wang, Y.; Chen, J.Q.; Pan, D.H.; Ma, J.H.; Li, R.F. Effect of SO2 on Co sites for NO-SCR by CH4 over Co-Beta. Catal. Today 2011, 175, 12–17. [Google Scholar] [CrossRef]
  13. Krishna, K.; Makkee, M. Coke formation over zeolites and CeO2-zeolites and its influence on selective catalytic reduction of NOx. Appl. Catal. B Environ. 2005, 59, 35–44. [Google Scholar] [CrossRef]
  14. Corbos, E.C.; Courtois, X.; Bion, N.; Marecot, P.; Duprez, D. Impact of the support oxide and Ba loading on the sulfur resistance and regeneration of Pt/Ba/support catalysts. Appl. Catal. B Environ. 2008, 80, 62–71. [Google Scholar] [CrossRef]
  15. Wang, Q.; Zhu, J.H.; Wei, S.Y.; Chung, J.S.; Guo, Z.H. Sulfur Poisoning and Regeneration of NOx Storage-Reduction Cu/K2Ti2O5 Catalyst. Ind. Eng. Chem. Res. 2010, 49, 7330–7335. [Google Scholar] [CrossRef]
  16. Liu, Z.Q.; Anderson, J.A. Influence of reductant on the regeneration of SO2-poisoned Pt/Ba/Al2O3 NOx storage and reduction catalyst. J. Catal. 2004, 228, 243–253. [Google Scholar] [CrossRef]
  17. Tanaka, T.; Amano, K.; Dohmae, K.; Takahashi, N.; Shinjoh, H. Studies on the regeneration of sulfur-poisoned NOx storage and reduction catalysts, including a Ba composite oxide. Appl. Catal. A Gen. 2013, 455, 16–24. [Google Scholar] [CrossRef]
  18. Le Phuc, N.; Corbos, E.C.; Courtois, X.; Can, F.; Marecot, P.; Duprez, D. NOx storage and reduction properties of Pt/CexZr1−xO2 mixed oxides: Sulfur resistance and regeneration, and ammonia formation. Appl. Catal. B Environ. 2009, 93, 12–21. [Google Scholar] [CrossRef]
  19. Doronkin, D.E.; Khan, T.S.; Bligaard, T.; Fogel, S.; Gabrielsson, P.; Dahl, S. Sulfur poisoning and regeneration of the Ag/γ-Al2O3 catalyst for H2-assisted SCR of NOx by ammonia. Appl. Catal. B Environ. 2012, 117, 49–58. [Google Scholar] [CrossRef]
  20. Chang, H.Z.; Li, J.H.; Yuan, J.; Chen, L.; Dai, Y.; Arandiyan, H.; Xu, J.Y.; Hao, J.M. Ge, Mn-doped CeO2–WO3 catalysts for NH3–SCR of NOx: Effects of SO2 and H2 regeneration. Catal. Today 2013, 201, 139–144. [Google Scholar] [CrossRef]
  21. Serrano, D.P.; Aguado, J.; Rodríguez, J.M.; Peral, A. Catalytic cracking of polyethylene over nanocrystalline HZSM-5: Catalyst deactivation and regeneration study. J. Anal. Appl. Pyrol. 2007, 79, 456–464. [Google Scholar] [CrossRef]
  22. Aguado, J.; Serrano, D.P.; Escola, J.M.; Briones, L. Deactivation and regeneration of a Ni supported hierarchical Beta zeolite catalyst used in the hydroreforming of the oil produced by LDPE thermal cracking. Fuel 2013, 109, 679–686. [Google Scholar] [CrossRef]
  23. Madaan, N.; Gatla, S.; Kalevaru, V.N.; Radnik, J.; Lücke, B.; Brückner, A.; Martin, A. Deactivation and regeneration studies of a PdSb/TiO2 catalyst used in the gas-phase acetoxylation of toluene. J. Catal. 2011, 282, 103–111. [Google Scholar] [CrossRef]
  24. Villegas, J.I.; Kumar, N.; Heikkilä, T.; Lehto, V.P.; Salmi, T.; Murzin, D.Y. Isomerization of n-butane to isobutane over Pt-modified Beta and ZSM-5 zeolite catalysts: Catalyst deactivation and regeneration. Chem. Eng. J. 2006, 120, 83–89. [Google Scholar] [CrossRef]
  25. Mazzieri, V.A.; Pieck, C.L.; Vera, C.R.; Yori, J.C.; Grau, J.M. Analysis of coke deposition and study of the variables of regeneration and rejuvenation of naphtha reforming trimetallic catalysts. Catal. Today 2018, 133–135, 870–878. [Google Scholar] [CrossRef]
  26. Zhang, Y.T.; Pan, H.; Li, W.; Shi, Y. SCR of NOx with C3H8 over Co/H-beta Modified by Zn at High GHSV. J. Chem. Eng. Chin. Univ. 2009, 23, 236–239. [Google Scholar]
  27. Khodayari, R. Regeneration of commercial TiO2-V2O5-WO3 SCR catalysts used in bio fuel plants. Appl. Catal. B Environ. 2001, 30, 87–99. [Google Scholar] [CrossRef]
  28. Pan, H.; Jian, Y.F.; Yu, Y.K.; He, C.; Shen, Z.X.; Liu, H.X. Regeneration and sulfur poisoning behavior of In/H-BEA catalyst for NOx reduction by CH4. Appl. Surf. Sci. 2017, 401, 120–126. [Google Scholar] [CrossRef]
  29. Dzwigaj, S.; Janas, J.; Machej, T.; Che, M. Selective catalytic reduction of NO by alcohols on Co- and Fe-Siβ catalysts. Catal. Today 2007, 119, 133–136. [Google Scholar] [CrossRef]
  30. Reddy, J.S.; Sayari, A. A simple method for the preparation of active Ti beta zeolite catalysts. Stud. Surf. Sci. Catal. 1995, 94, 309–316. [Google Scholar]
  31. Chung, K.S.; Massoth, F.E. Studies on molybdena-alumina catalysts: VII. Effect of cobalt on catalyst states and reducibility. J. Catal. 1980, 64, 320–331. [Google Scholar] [CrossRef]
  32. Stranick, M.S.; Houalla, M.; Hercules, D.M. Spectroscopic characterization of TiO2Al2O3 and CoAl2O3TiO2 catalysts. J. Catal. 1987, 106, 362–368. [Google Scholar] [CrossRef]
  33. Zsoldos, Z.; Guczi, L. Structure and Catalytic Activity of Alumina Supported Platinum Cobalt Bimetallic Catalysts. 3. Effect of Treatment on the Interface Layer. J. Phys. Chem. 1992, 96, 9393–9400. [Google Scholar] [CrossRef]
  34. Gomez-Garcia, M.A.; Pitchon, V.; Kiennemann, A. Pollution by nitrogen oxides: An approach to NOx abatement by using sorbing catalytic materials. Environ. Int. 2005, 31, 445–467. [Google Scholar] [CrossRef] [PubMed]
  35. Yan, J.; Kung, M.C.; Sachtler, W.M.H.; Kung, H.H. Co/Al2O3 Lean NOx Reduction Catalyst. J. Catal. 1997, 172, 178–186. [Google Scholar] [CrossRef]
  36. Gong, T.; Qin, L.J.; Lu, J.; Feng, H. ZnO modified ZSM-5 and Y zeolites fabricated by atomic layer deposition for propane conversion. Phys. Chem. Chem. Phys. 2016, 18, 601–614. [Google Scholar] [CrossRef] [PubMed]
  37. Kicir, N.; Tuken, T.; Erken, O.; Gumus, C.; Ufuktepe, Y. Nanostructured ZnO films in forms of rod, plate and flower: Electrodeposition mechanisms and characterization. Appl. Surf. Sci. 2016, 377, 191–199. [Google Scholar] [CrossRef]
  38. Wang, X.; Chen, H.Y.; Sachtler, W.M.H. Catalytic reduction of NOx by hydrocarbons over Co/ZSM-5 catalysts prepared with different methods. Appl. Catal. B Environ. 2000, 26, L227–L239. [Google Scholar] [CrossRef]
  39. Zhang, Q.; Wang, X.D. Charaterization of the phase and valency state of Co on Co/HZSM-5 catalysts. Chem. J. Chin. Univ. 2002, 23, 129–131. [Google Scholar]
  40. Shi, Y.; Su, Q.F.; Chen, J.; Wei, J.W.; Yang, J.T.; Pan, H. Combination non-thermal plasma and low temperature-C3H8-SCR over Co-In/H-beta catalyst for NOx abatement. Environ. Eng. Sci. 2009, 26, 1107–1113. [Google Scholar] [CrossRef]
  41. Pan, H.; Guo, Y.H.; Bi, H.T. NOx adsorption and reduction with C3H6 over Fe/zeolite catalysts: Effect of catalyst support. Chem. Eng. J. 2015, 280, 66–73. [Google Scholar] [CrossRef]
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Figure 1. The stability of Co-Zn/H-Beta in C3H8-SCR under the dual effects of SO2 and H2O.
Figure 1. The stability of Co-Zn/H-Beta in C3H8-SCR under the dual effects of SO2 and H2O.
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Figure 2. Optimization of regeneration sequence.
Figure 2. Optimization of regeneration sequence.
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Figure 3. Optimization of regeneration temperature for (a) H2 reduction followed by air oxidation and (b) air oxidation followed by H2 reduction.
Figure 3. Optimization of regeneration temperature for (a) H2 reduction followed by air oxidation and (b) air oxidation followed by H2 reduction.
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Figure 4. XRD patterns of Co-Zn/H-Beta catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (d) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (e) Co-Zn/H-Beta-R (O2 + H2, 500 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
Figure 4. XRD patterns of Co-Zn/H-Beta catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (d) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (e) Co-Zn/H-Beta-R (O2 + H2, 500 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
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Figure 5. XPS spectra of the Co 2p regions for fresh, deactivated, and regenerated catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (d) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (e) Co-Zn/H-Beta-R (O2 + H2, 500 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
Figure 5. XPS spectra of the Co 2p regions for fresh, deactivated, and regenerated catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (d) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (e) Co-Zn/H-Beta-R (O2 + H2, 500 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
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Figure 6. XPS spectra of the Zn 2p regions for fresh, deactivated, and regenerated catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (d) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (e) Co-Zn/H-Beta-R (O2 + H2, 500 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
Figure 6. XPS spectra of the Zn 2p regions for fresh, deactivated, and regenerated catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (d) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (e) Co-Zn/H-Beta-R (O2 + H2, 500 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
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Figure 7. H2-TPR of fresh, deactivated, and regenerated catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (O2, 550 °C), (d) Co-Zn/H-Beta-R (H2, 550 °C), (e) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (g) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
Figure 7. H2-TPR of fresh, deactivated, and regenerated catalysts. (a) Co-Zn/H-Beta-F, (b) Co-Zn/H-Beta-D, (c) Co-Zn/H-Beta-R (O2, 550 °C), (d) Co-Zn/H-Beta-R (H2, 550 °C), (e) Co-Zn/H-Beta-R (H2 + O2, 450 °C), (f) Co-Zn/H-Beta-R (O2 + H2, 450 °C), (g) Co-Zn/H-Beta-R (O2 + H2, 550 °C).
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Figure 8. TGA curves of fresh, deactivated, and regenerated catalysts.
Figure 8. TGA curves of fresh, deactivated, and regenerated catalysts.
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Scheme 1. Regeneration pathway for the combined polluted Co-Zn/H-Beta catalyst.
Scheme 1. Regeneration pathway for the combined polluted Co-Zn/H-Beta catalyst.
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Table
Table 1. Textural properties and X-ray photoelectron spectroscopy (XPS) results of samples.
Table 1. Textural properties and X-ray photoelectron spectroscopy (XPS) results of samples.
SampleSBETa (m2 g−1)Smicrob (m2 g−1)Vtotala (cm3 g−1)Binding Energy of Co2p3/2 (eV)Interval between Co2p3/2 and Co2p1/2 (eV)
Co-Zn/H-Beta-F428.42338.880.17780.515.8
Co-Zn/H-Beta-D333.65264.140.13778.617.2
Co-Zn/H-Beta-R (O2, 550 °C)384.56298.220.15//
Co-Zn/H-Beta-R (H2, 550 °C)360.12282.360.14//
Co-Zn/H-Beta-R (H2 + O2, 450 °C)388.50305.970.15782.714.6
Co-Zn/H-Beta-R (O2 + H2, 450 °C)418.49323.970.16781.515.2
Co-Zn/H-Beta-R (O2 + H2, 500 °C)419.91336.470.17781.415.1
Co-Zn/H-Beta-R (O2 + H2, 550 °C)426.54337.370.17782.515.1
a BET method. b t-Plot method.

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MDPI and ACS Style

Pan, H.; Xu, D.; He, C.; Shen, C. In Situ Regeneration and Deactivation of Co-Zn/H-Beta Catalysts in Catalytic Reduction of NOx with Propane. Catalysts 2019, 9, 23. https://doi.org/10.3390/catal9010023

AMA Style

Pan H, Xu D, He C, Shen C. In Situ Regeneration and Deactivation of Co-Zn/H-Beta Catalysts in Catalytic Reduction of NOx with Propane. Catalysts. 2019; 9(1):23. https://doi.org/10.3390/catal9010023

Chicago/Turabian Style

Pan, Hua, Dongmei Xu, Chi He, and Chao Shen. 2019. "In Situ Regeneration and Deactivation of Co-Zn/H-Beta Catalysts in Catalytic Reduction of NOx with Propane" Catalysts 9, no. 1: 23. https://doi.org/10.3390/catal9010023

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