Deactivation E ﬀ ect of CaO on Mn-Ce / AC Catalyst for SCR of NO with NH 3 at Low Temperature

: In this study, the poisoning e ﬀ ect of CaO on activated carbon (AC)-based Mn-Ce catalysts was discussed. Loading CaO inhibited the catalytic activity of the catalyst and the NO conversion of the catalyst decreased from 69.5% to 38.2% at 75 ◦ C. The amount of MnO 2 in AC surface decreased in the process of loading CaO, which was detrimental to the Selective Catalytic Reduction (SCR) performance of the catalyst. The change of manganese oxide form inhibited generation rate for the chemisorption oxygen and NO 2 , which was the most critical reason for the decrease of catalytic activity. Besides, loaded CaO entered into the pores of the catalyst, which led to the blockage of the pores and further resulted in the decrease of the Brunauer-Emmett-Teller (BET) surface area and total pore volume. It also destroyed the oxygen-containing functional groups and acid site on the surface of AC. All of these caused the deactivation of Mn-Ce / AC catalyst after loading CaO.


Introduction
Nitrogen oxides (NO x ) emissions from the steel plant, especially the sintering process, have contributed to local air pollution and the global environmental problems [1][2][3]. Many scholars believed that Selective Catalytic Reduction (SCR) of NO x with NH 3 was the most feasible technique to solve the problem of NO x emission in steel plant [4,5]. The operating temperature window of commercial SCR catalyst V 2 O 5 -WO 3 /TiO 2 was about 300-400 • C [3], so it would have a sharp drop in the SCR activity when working in the sintering flue gas (120-180 • C). Therefore, the exploitation of SCR catalysts that could work well at low temperature was the primary task to solve NO x emissions in steel plants. An attractive alternative for lower temperatures, and thus for tail-end configuration without or with much lower flue gas heating, is the application of activated carbons (ACs) [6][7][8]. In our previous study [1,[9][10][11][12], MnO 2 and CeO 2 supported on AC catalyst showed outstanding SCR activity at the lower temperature. Therefore, it is expected to work successfully in the NO removal of sintered flue gas.
The SCR activity of the SCR catalyst was affected not only by the type of active component, but also by the damaging metal elements (K, Pb, Ca, As and Na, etc.) in the sintering flue gas. Although the Mn-Ce/AC catalyst exhibited outstanding NO conversion under ideal experimental conditions, complex flue gas conditions must be considered when the catalyst is used in the industry. Therefore, the poisoning effects of different metal elements on the catalyst should be studied systematically. In our earlier work [1], K + occupied the oxygen vacancy of the catalyst, and KCl interacted with functional groups on the surface of AC, resulting in reduced adsorption of NH 3 and NO. Loaded As 2 O 3 was converted to As 2 O 5 preferentially by the chemisorption oxygen, which led to the decrease of the chemisorption oxygen participating in the SCR reaction [1]. The PbO poisoning over Mn-Ce/AC catalyst was also studied by the authors [13], the result indicated that the "fast SCR" reaction was inhibited for the catalyst and caused the decrease of SCR performance.
The presence of Ca in the form of CaO, CaCl 2 or CaOH would affect the activity of commercial catalysts and TiO 2 -based catalysts in flue gas, and the poisoning effect of calcium has been studied by some scholars [14][15][16][17]. Li found that the SCR performance of Ca-poisoning V 2 O 5 -WO 3 /TiO 2 catalyst decreased seriously [14]. The poisoning effect of Ca(OH) 2 on Mn-Ce/TiO 2 catalyst was more serious compared with that of CaCl 2 [15]. The study of Liu [16] suggested that NH 3 adsorption and NO oxidation for Ce/TiO 2 were inhibited after loading CaO. Nevertheless, the behavior and effect of CaO over Mn-Ce/AC catalyst has not been researched. Therefore, the Mn-Ce/AC and CaO poisoning catalyst were prepared by in this study, aiming to investigate the deactivation reason of Mn-Ce/AC catalyst after loading CaO by a series of characterization methods. Figure 1a compares the deNO x activity of Mn-Ce/AC and CaO poisoning catalyst. Mn-Ce/AC catalyst achieved a high NO conversion of 69.4% at 75 • C, which may be mainly attributed to the NO adsorption capacity of AC. Mn-Ce/AC catalyst showed excellent SCR activity with the highest NO conversion of 96.5% at 225 • C. However, the SCR performance of the catalyst took place a noticeable change after doping CaO. The NO conversion of CaO poisoning catalyst decreased to 84.4% at 225 • C, which indicated that CaO on the AC surface inhibited the catalytic action of the Active components on AC. Noteworthily, the NO conversion was significantly decreased due to the load of CaO in the low temperature range of 75-125 • C. With the increase of temperature, the deactivation degree of CaO poisoning catalyst decreased. N 2 selectivity and N 2 O concentration of the two catalysts are also displayed in Figure 1b. From Figure 1b, The N 2 selectivity of all catalyst samples decreased as the temperature increased. CaO poisoning catalyst had the smaller N 2 selectivity compared with Mn-Ce/AC catalyst. Therefore, loading CaO was unfavorable for keeping high N 2 selectivity of the catalyst. Besides, More N 2 O was produced on the Mn-Ce/AC catalyst after loading CaO, which was a key factor in the decrease of N 2 selectivity for CaO poisoning catalyst.

Catalyst Performance
Catalysts 2020, 10, x FOR PEER REVIEW 2 of 11 Ce/AC catalyst was also studied by the authors [13], the result indicated that the "fast SCR" reaction was inhibited for the catalyst and caused the decrease of SCR performance. The presence of Ca in the form of CaO, CaCl2 or CaOH would affect the activity of commercial catalysts and TiO2-based catalysts in flue gas, and the poisoning effect of calcium has been studied by some scholars [14][15][16][17]. Li found that the SCR performance of Ca-poisoning V2O5-WO3/TiO2 catalyst decreased seriously [14]. The poisoning effect of Ca(OH)2 on Mn-Ce/TiO2 catalyst was more serious compared with that of CaCl2 [15]. The study of Liu [16] suggested that NH3 adsorption and NO oxidation for Ce/TiO2 were inhibited after loading CaO. Nevertheless, the behavior and effect of CaO over Mn-Ce/AC catalyst has not been researched. Therefore, the Mn-Ce/AC and CaO poisoning catalyst were prepared by in this study, aiming to investigate the deactivation reason of Mn-Ce/AC catalyst after loading CaO by a series of characterization methods. Figure 1a compares the deNOx activity of Mn-Ce/AC and CaO poisoning catalyst. Mn-Ce/AC catalyst achieved a high NO conversion of 69.4% at 75 °C, which may be mainly attributed to the NO adsorption capacity of AC. Mn-Ce/AC catalyst showed excellent SCR activity with the highest NO conversion of 96.5% at 225 °C. However, the SCR performance of the catalyst took place a noticeable change after doping CaO. The NO conversion of CaO poisoning catalyst decreased to 84.4% at 225 °C, which indicated that CaO on the AC surface inhibited the catalytic action of the Active components on AC. Noteworthily, the NO conversion was significantly decreased due to the load of CaO in the low temperature range of 75-125 °C. With the increase of temperature, the deactivation degree of CaO poisoning catalyst decreased. N2 selectivity and N2O concentration of the two catalysts are also displayed in Figure 1b. From Figure 1b, The N2 selectivity of all catalyst samples decreased as the temperature increased. CaO poisoning catalyst had the smaller N2 selectivity compared with Mn-Ce/AC catalyst. Therefore, loading CaO was unfavorable for keeping high N2 selectivity of the catalyst. Besides, More N2O was produced on the Mn-Ce/AC catalyst after loading CaO, which was a key factor in the decrease of N2 selectivity for CaO poisoning catalyst.

Pore Properties Analysis
The pore properties of the Mn-Ce/AC and CaO poisoning catalyst are given in Table 1. It could be found from Figure 2 that the nitrogen adsorption-desorption isotherms of all catalysts were of typical type IV, with a hysteresis loop of type H4. It was a typical mesoporous material and the loading of CaO did not change the pore structure of the catalyst. Brunauer-Emmett-Teller (BET) results showed that Mn-Ce/AC catalyst had a relatively large BET surface area. The specific surface area of Mn-Ce/AC catalyst was 825 m 2 /g, while that of CaO poisoning catalyst was 724 m 2 /g. In

Pore Properties Analysis
The pore properties of the Mn-Ce/AC and CaO poisoning catalyst are given in Table 1. It could be found from Figure 2 that the nitrogen adsorption-desorption isotherms of all catalysts were of typical type IV, with a hysteresis loop of type H4. It was a typical mesoporous material and the loading of CaO did not change the pore structure of the catalyst. Brunauer-Emmett-Teller (BET) results showed that Mn-Ce/AC catalyst had a relatively large BET surface area. The specific surface area of Mn-Ce/AC catalyst was 825 m 2 /g, while that of CaO poisoning catalyst was 724 m 2 /g. In addition, the total pore volume decreased significantly to 0.16 cm 3 /g after loading CaO. However, the average pore diameter of CaO poisoning catalyst had little change. These changes may be caused by the blockage of some micropores on AC surface. Loaded CaO entered into the pores of the catalyst, which resulted in the blockage of the pores and further led to the reduction of the BET surface area and total pore volume of the catalyst. addition, the total pore volume decreased significantly to 0.16 cm 3 /g after loading CaO. However, the average pore diameter of CaO poisoning catalyst had little change. These changes may be caused by the blockage of some micropores on AC surface. Loaded CaO entered into the pores of the catalyst, which resulted in the blockage of the pores and further led to the reduction of the BET surface area and total pore volume of the catalyst.

SEM Analysis
To verify the conclusion of BET, the SEM characterization was performed and the surface morphology of the two catalysts is shown in Figure 3. Figure 3a is the scanning electron microscope morphology of the Mn-Ce/AC catalyst. Mn-Ce/AC catalyst had developed pores, large pore size and fine particles on the AC surface, which was consistent with the BET experimental results ( Table 1). The surface of the catalyst became compacted and the total pore diameter and the number of microspores became smaller after loading CaO, Because the loaded CaO entered into the pores of the catalyst, which led to the blockage of the pores and further lead to the destruction of carbon pore morphology of AC, and the surface of the catalyst became rough. Poor surface morphology would hinder the adsorption behavior of reacted gas.

SEM Analysis
To verify the conclusion of BET, the SEM characterization was performed and the surface morphology of the two catalysts is shown in Figure 3. Figure 3a is the scanning electron microscope morphology of the Mn-Ce/AC catalyst. Mn-Ce/AC catalyst had developed pores, large pore size and fine particles on the AC surface, which was consistent with the BET experimental results ( Table 1). The surface of the catalyst became compacted and the total pore diameter and the number of microspores became smaller after loading CaO, Because the loaded CaO entered into the pores of the catalyst, which led to the blockage of the pores and further lead to the destruction of carbon pore morphology of AC, and the surface of the catalyst became rough. Poor surface morphology would hinder the adsorption behavior of reacted gas.
Catalysts 2020, 10, x FOR PEER REVIEW 3 of 11 addition, the total pore volume decreased significantly to 0.16 cm 3 /g after loading CaO. However, the average pore diameter of CaO poisoning catalyst had little change. These changes may be caused by the blockage of some micropores on AC surface. Loaded CaO entered into the pores of the catalyst, which resulted in the blockage of the pores and further led to the reduction of the BET surface area and total pore volume of the catalyst.

SEM Analysis
To verify the conclusion of BET, the SEM characterization was performed and the surface morphology of the two catalysts is shown in Figure 3. Figure 3a is the scanning electron microscope morphology of the Mn-Ce/AC catalyst. Mn-Ce/AC catalyst had developed pores, large pore size and fine particles on the AC surface, which was consistent with the BET experimental results ( Table 1). The surface of the catalyst became compacted and the total pore diameter and the number of microspores became smaller after loading CaO, Because the loaded CaO entered into the pores of the catalyst, which led to the blockage of the pores and further lead to the destruction of carbon pore morphology of AC, and the surface of the catalyst became rough. Poor surface morphology would hinder the adsorption behavior of reacted gas.   Figure 4, both catalysts appeared the broad diffraction peaks of graphite crystallite with layer structure (002) at 22-31 • and turbostratic graphite-like structure (100) at 41-47 • [18,19]. In the XRD curves of Mn-Ce/AC, the characteristic peaks of SiO 2 at 26.65 • and the weak diffraction peak of CeO 2 (JCPDS 42-1348) at 35.5 • were detected [13,20] [21,22]. The decrease of MnO 2 would definitely cause the reduction of the SCR performance for the catalyst.   Figure 4 displays the XRD patterns of Mn-Ce/AC and CaO poisoning catalyst. From Figure 4, both catalysts appeared the broad diffraction peaks of graphite crystallite with layer structure (002) at 22-31° and turbostratic graphite-like structure (100) at 41-47° [18,19]. In the XRD curves of Mn-Ce/AC, the characteristic peaks of SiO2 at 26.65° and the weak diffraction peak of CeO2(JCPDS 42-1348) at 35.5° were detected [13,20]. However, there were three new characteristic peaks of 2θ = 36.79°, 50.34° and 68.22° appearing on the CaO poisoning catalyst surface, in which the peaks at 2θ = 36.79° and 68.22° (JCPDS 06-0540) corresponded to Mn2O3 and the peak at 2θ = 50.34° belonged to MnO2 (JCPDS 42-1348). Moreover, the intensity of CeO2 peak on CaO poisoning catalyst became stronger compared with Mn-Ce/AC. These results demonstrated that the crystallization and agglomeration phenomenon of the active components, especially manganese oxide, happened on the catalyst surface after doping CaO. More importantly, the peak of Mn2O3 could be detected on CaO poisoning catalyst surface, indicating that part of MnO2 in AC surface was converted to Mn2O3. MnO2 participated in a main catalytic role and promoted the conversion rate of NO to NO2 [21,22]. The decrease of MnO2 would definitely cause the reduction of the SCR performance for the catalyst.

XPS Analysis
The change of surface atomic on AC surface had an important influence on SCR reaction. Therefore, it was of great significance to discuss the change of the surface atomic structure of the catalyst.
The XPS spectra of Mn 2p for Mn-Ce/AC and CaO poisoning catalyst is displayed in Figure 5a. According to the reference [23,24], peaks of Mn 2p3/2 was divided into three peaks of 640.24, 642.15 and 646.60 eV, corresponding to Mn 2+ , Mn 3+ and Mn 4+ , respectively. As shown in Figure 5a, the Mn 4+ peak area of CaO poisoning catalyst decreased significantly. The valence ratios of Mn 2+ , Mn 3+ and Mn 4+ over Mn-Ce/AC were 30.99%, 34.29% and 34.72%, respectively. However, for CaO poisoning catalyst, the corresponding ratios were 29.52%, 44.05% and 26.43%. It was found that the content of Mn 2+ did not change after loading CaO. Therefore, most of the reduced Mn 4+ in AC surface was converted to Mn 3+ after loading CaO. A similar conclusion was also obtained from XRD result ( Figure  4). Mn 4+ had the higher NO removal efficiency and redox ability compared with Mn 3+ in the form of Mn2O3 [25,26]. Manganese dioxide also promoted the conversion of NO to NO2 and the generation of active intermediate [22,27], which is beneficial to SCR reaction. So, loading CaO changed the manganese phase on AC surface and decreased the Mn 4+ concentration.
XPS spectra of Ce 3d of the two catalysts are displayed Figure 5b. In these eight peaks, the peaks of u1 and v1 belonged to Ce 3+ and the others were attributed to Ce 4+ [16,28]. The reports [29,30] had

XPS Analysis
The change of surface atomic on AC surface had an important influence on SCR reaction. Therefore, it was of great significance to discuss the change of the surface atomic structure of the catalyst.
The XPS spectra of Mn 2p for Mn-Ce/AC and CaO poisoning catalyst is displayed in Figure 5a. According to the reference [23,24], peaks of Mn 2p 3/2 was divided into three peaks of 640.24, 642.15 and 646.60 eV, corresponding to Mn 2+ , Mn 3+ and Mn 4+ , respectively. As shown in Figure 5a, the Mn 4+ peak area of CaO poisoning catalyst decreased significantly. The valence ratios of Mn 2+ , Mn 3+ and Mn 4+ over Mn-Ce/AC were 30.99%, 34.29% and 34.72%, respectively. However, for CaO poisoning catalyst, the corresponding ratios were 29.52%, 44.05% and 26.43%. It was found that the content of Mn 2+ did not change after loading CaO. Therefore, most of the reduced Mn 4+ in AC surface was converted to Mn 3+ after loading CaO. A similar conclusion was also obtained from XRD result ( Figure 4). Mn 4+ had the higher NO removal efficiency and redox ability compared with Mn 3+ in the form of Mn 2 O 3 [25,26]. Manganese dioxide also promoted the conversion of NO to NO 2 and the generation of active intermediate [22,27], which is beneficial to SCR reaction. So, loading CaO changed the manganese phase on AC surface and decreased the Mn 4+ concentration.
The XPS of O 1s was consisted of two peaks at 532.4 eV and 530.2 eV, belonging to the chemisorption oxygen (Oα) and lattice oxygen (Oβ), respectively [11,31]. From Figure 5c, the content of Oα for Mn-Ce/AC catalyst was 76.92%, while that for CaO poisoning catalyst decreased to 74.63%. Similar to the XPS result of Ce, the ratio of Oα also had a little decrease after doping CaO. The amount of the chemisorption oxygen (Oα) was closely related to the valence of Ce [29], so loading CaO had almost no effect on the state of oxygen.  XPS spectra of Ce 3d of the two catalysts are displayed Figure 5b. In these eight peaks, the peaks of u1 and v1 belonged to Ce 3+ and the others were attributed to Ce 4+ [16,28]. The reports [29,30] had suggested that Ce 3+ was more conducive to the generation of oxygen vacancies and unsaturated chemical bonds. Therefore, the Ce 3+ was favorable for SCR reaction. The Ce 3+ and Ce 4+ content of Mn-Ce/AC and CaO poisoning catalyst could be obtained from XPS spectra, and the ratio of Ce 3+ for Mn-Ce/AC and CaO poisoning catalyst were 37.21% and 35.57%, respectively. Therefore, the content of Ce 3+ only had a little change after loading CaO. So the valence of Ce was basically not affected by loading CaO.
The XPS of O 1s was consisted of two peaks at 532.4 eV and 530.2 eV, belonging to the chemisorption oxygen (O α ) and lattice oxygen (O β ), respectively [11,31]. From Figure 5c, the content of O α for Catalysts 2020, 10, 873 6 of 11 Mn-Ce/AC catalyst was 76.92%, while that for CaO poisoning catalyst decreased to 74.63%. Similar to the XPS result of Ce, the ratio of O α also had a little decrease after doping CaO. The amount of the chemisorption oxygen (O α ) was closely related to the valence of Ce [29], so loading CaO had almost no effect on the state of oxygen.

FT-IR Analysis
The FT-IR characterization was performed and the results are displayed in Figure 6. The FT-IR curves of both catalysts contained four bands at 1634, 3454, 1384 and 1080 cm −1 , which was corresponded to the stretching of C=O, the stretching vibrations of -OH groups, aliphatic C-H groups and C-O-C groups, respectively [32][33][34][35]. Studies have shown that -OH and C=O groups could provide adsorption sites for NH 3 and promote the transformation of ammonia gas (NH 3 (g)) to adsorbed ammonia (NH 3 (ads)) [10,36,37]. Besides, NH 3 and NO were more easily adsorbed when functional groups existed on the AC surface [33,37]. From Figure 6, the intensity of the bands at 1384 and 1080 cm −1 became weak. Moreover, the intensity of the bands at 3454 and 1634 cm −1 decreased obviously. This indicated that all oxygen-containing functional groups were reduced to some extent after doping CaO. Therefore, the presence of CaO destroyed the oxygen-containing functional groups and inhibited the SCR performance of the catalyst.

FT-IR Analysis
The FT-IR characterization was performed and the results are displayed in Figure 6. The FT-IR curves of both catalysts contained four bands at 1634, 3454, 1384 and 1080 cm −1 , which was corresponded to the stretching of C=O, the stretching vibrations of -OH groups, aliphatic C-H groups and C-O-C groups, respectively [32][33][34][35]. Studies have shown that -OH and C=O groups could provide adsorption sites for NH3 and promote the transformation of ammonia gas (NH3(g)) to adsorbed ammonia (NH3(ads)) [10,36,37]. Besides, NH3 and NO were more easily adsorbed when functional groups existed on the AC surface [33,37]. From Figure 6, the intensity of the bands at 1384 and 1080 cm −1 became weak. Moreover, the intensity of the bands at 3454 and 1634 cm −1 decreased obviously. This indicated that all oxygen-containing functional groups were reduced to some extent after doping CaO. Therefore, the presence of CaO destroyed the oxygen-containing functional groups and inhibited the SCR performance of the catalyst.  Figure 7 showed NH3-TPD profiles of Mn-Ce/AC and CaO-Mn-Ce/AC catalysts. In NH3-TPD profiles, the acid amount and strength were decided by the area and position of the desorption peak [11]. From Figure 7, the peak of weak acid site on Mn-Ce/AC and CaO poisoning catalysts could be observed at about 130-170 °C, which indicated that loading CaO did not change the position of the weak acid site. However, the peak intensity of weak acid site decreased after loading CaO. The peak of strong acid site on Mn-Ce/AC and CaO-Mn-Ce/AC catalysts could be observed at 614 °C and 819 °C and the peak of strong acid site on Mn-Ce/AC catalyst moved towards the higher temperature zone. Moreover, the peak area of strong acid site on Mn-Ce/AC catalyst became smaller after doping CaO. All the acid sites played an important role during the NO removal process and the higher the number of acid sites, the more NH3 would be adsorbed on the surface of the catalyst [38]. Therefore, the decrease of weak and strong acid site was one of the factors for different SCR performance between Mn-Ce/AC and CaO poisoning catalysts.  Figure 7 showed NH 3 -TPD profiles of Mn-Ce/AC and CaO-Mn-Ce/AC catalysts. In NH 3 -TPD profiles, the acid amount and strength were decided by the area and position of the desorption peak [11]. From Figure 7, the peak of weak acid site on Mn-Ce/AC and CaO poisoning catalysts could be observed at about 130-170 • C, which indicated that loading CaO did not change the position of the weak acid site. However, the peak intensity of weak acid site decreased after loading CaO. The peak of strong acid site on Mn-Ce/AC and CaO-Mn-Ce/AC catalysts could be observed at 614 • C and 819 • C and the peak of strong acid site on Mn-Ce/AC catalyst moved towards the higher temperature zone. Moreover, the peak area of strong acid site on Mn-Ce/AC catalyst became smaller after doping CaO. All the acid sites played an important role during the NO removal process and the higher the number of acid sites, the more NH 3 would be adsorbed on the surface of the catalyst [38]. Therefore, the decrease of weak and strong acid site was one of the factors for different SCR performance between Mn-Ce/AC and CaO poisoning catalysts.

Discussion
In our previous study [10], the Mn-Ce carbon-based catalyst has been studied and the NO removal reaction occurred on catalyst followed the Eley-Rideal (E-R) mechanism. The specific reaction steps are as follows: Simultaneously, the "fast SCR" reaction would also occur on the Mn-Ce carbon-based catalyst [9]: In the E-R mechanism, MnO2 was reduced to Mn2O3 and provided the chemisorption oxygen (Oα) (Equation (2)) and it was a crucial step for the SCR reaction process. Besides, MnO2 promoted the conversion rate of NO to NO2 (Equation (7)) in the "fast SCR" reaction [9,22].
However, XRD and XPS results proved that part of MnO2 in AC surface was converted to Mn2O3 in the process of loading CaO. Mn 3+ in the form of Mn2O3 had the lower redox ability compared with MnO2. Therefore, the decrease of MnO2 resulted in a decline of generation rate for the chemisorption oxygen and inhibited the formation of intermediate product -NH2 (Shown in Figure 8). Furthermore, the decrease of MnO2 also caused the reduction of reaction rate for the "fast SCR" reaction ( Figure 8) because of less NO2 production (Equation (7)). Therefore, the change of manganese oxide form inhibited generation rate for the chemisorption oxygen and NO2, which was the most critical reason for the decrease of catalytic activity for Mn-Ce/AC catalyst.

Discussion
In our previous study [10], the Mn-Ce carbon-based catalyst has been studied and the NO removal reaction occurred on catalyst followed the Eley-Rideal (E-R) mechanism. The specific reaction steps are as follows: −NH 2 (a) + NO(g) → NH 2 NO(a) → N 2 (g) + H 2 O Simultaneously, the "fast SCR" reaction would also occur on the Mn-Ce carbon-based catalyst [9]: In the E-R mechanism, MnO 2 was reduced to Mn 2 O 3 and provided the chemisorption oxygen (O α ) (Equation (2)) and it was a crucial step for the SCR reaction process. Besides, MnO 2 promoted the conversion rate of NO to NO 2 (Equation (7)) in the "fast SCR" reaction [9,22].
However, XRD and XPS results proved that part of MnO 2 in AC surface was converted to Mn 2 O 3 in the process of loading CaO. Mn 3+ in the form of Mn 2 O 3 had the lower redox ability compared with MnO 2 . Therefore, the decrease of MnO 2 resulted in a decline of generation rate for the chemisorption oxygen and inhibited the formation of intermediate product -NH 2 (Shown in Figure 8). Furthermore, the decrease of MnO 2 also caused the reduction of reaction rate for the "fast SCR" reaction ( Figure 8) because of less NO 2 production (Equation (7)). Therefore, the change of manganese oxide form inhibited generation rate for the chemisorption oxygen and NO 2 , which was the most critical reason for the decrease of catalytic activity for Mn-Ce/AC catalyst.
The intensity of all bands for functional groups decreased after loading CaO (from FT-IR result), indicating the oxygen-containing functional groups of CaO poisoning catalyst were destroyed (From Figure 6). The decrease of oxygen-containing functional groups, especially -OH and C=O groups, resulted in the less gas being absorbed onto the AC surface (Shown in Figure 8). This was the limiting factor for increasing the reaction rate of the NO removal process. The decrease of weak and strong acid site also hindered the adsorption of NH 3 . In addition, CaO also caused the reduction of the BET surface area and total pore volume of the catalyst (from Figure 3). The large BET surface area could provide more contact opportunities for adsorbed gas (NH 3 and NO) and active components. So the oxygen-containing functional groups and the reduction of BET surface area was also one of the reasons for the deactivation of Mn-Ce/AC catalyst. The intensity of all bands for functional groups decreased after loading CaO (from FT-IR result), indicating the oxygen-containing functional groups of CaO poisoning catalyst were destroyed (From Figure 6). The decrease of oxygen-containing functional groups, especially -OH and C=O groups, resulted in the less gas being absorbed onto the AC surface (Shown in Figure 8). This was the limiting factor for increasing the reaction rate of the NO removal process. The decrease of weak and strong acid site also hindered the adsorption of NH3. In addition, CaO also caused the reduction of the BET surface area and total pore volume of the catalyst (from Figure 3). The large BET surface area could provide more contact opportunities for adsorbed gas (NH3 and NO) and active components. So the oxygen-containing functional groups and the reduction of BET surface area was also one of the reasons for the deactivation of Mn-Ce/AC catalyst.

Catalyst Preparation
The AC carrier was provided by Shanxi Xin-Hua Activated Carbon Factory and the particle size of AC used in this experiment was 16-20 mesh. First, it was pretreated with 65 wt% HNO3 solution at 80 °C for 8 h. Finally, the pretreated AC was dried at 120 °C for 10 h.
The precursors used in the experiment were 50 wt% Mn(NO3)2, Ce(NO3)3.6H2O and Ca(NO3)2. Active components Mn and Ce were supported onto the surface of the AC by impregnation method. The total weight percentage of CeO2 and MnO2 loading was 10% (Mn/Ce (molar ratio) = 7:3). First, AC was immersed in the prepared precursors, followed by ultrasonic Oscillation for 30 min., then placing in the water bath at 65 °C for 12 h. Finally, the mixture was calcined at 400 °C for 4 h. The obtained catalyst was marked as Mn-Ce/AC. The CaO poisoning catalysts were prepared by impregnating Ca(NO3)2 onto fresh catalyst, and molar ratios of Ca/Mn were 0.5. The samples obtained were marked as CaO-Mn-Ce/AC.

Catalytic Activity Measurements
The mass of the catalyst sample using in the experiments was 1 g. The flow rate was 500 mL/min with 500 ppm NO and NH3, 5% O2, and N2 as the balance gas. The temperature range was from 75 to 250 °C and a flue gas analyzer was used to monitored continuously the outlet gas concentrations of

Catalyst Preparation
The AC carrier was provided by Shanxi Xin-Hua Activated Carbon Factory and the particle size of AC used in this experiment was 16-20 mesh. First, it was pretreated with 65 wt% HNO 3 solution at 80 • C for 8 h. Finally, the pretreated AC was dried at 120 • C for 10 h.
The precursors used in the experiment were 50 wt% Mn(NO 3 ) 2 , Ce(NO 3 ) 3 ·6H 2 O and Ca(NO 3 ) 2 . Active components Mn and Ce were supported onto the surface of the AC by impregnation method. The total weight percentage of CeO 2 and MnO 2 loading was 10% (Mn/Ce (molar ratio) = 7:3). First, AC was immersed in the prepared precursors, followed by ultrasonic Oscillation for 30 min, then placing in the water bath at 65 • C for 12 h. Finally, the mixture was calcined at 400 • C for 4 h. The obtained catalyst was marked as Mn-Ce/AC. The CaO poisoning catalysts were prepared by impregnating Ca(NO 3 ) 2 onto fresh catalyst, and molar ratios of Ca/Mn were 0.5. The samples obtained were marked as CaO-Mn-Ce/AC.

Catalytic Activity Measurements
The mass of the catalyst sample using in the experiments was 1 g. The flow rate was 500 mL/min with 500 ppm NO and NH 3 , 5% O 2 , and N 2 as the balance gas. The temperature range was from 75 to 250 • C and a flue gas analyzer was used to monitored continuously the outlet gas concentrations of NO. The catalytic activity was calculated by the formulas:

Catalyst Characterization
Nitrogen adsorption isotherm was measured with Micromeritics ASAP 2010 instrument at 77 K. The BET and the t-plot method were used to calculate the BET specific surface, the total pore volume and average pore size. The microstructures of the experimental samples were studied by Scanning Electron Micrograph (SEM, JEOL S-4800). XRD was operated by Rigaku D/max-2500/PC diffractometer with the scanning range of 10 to 90 • . X-ray photoelectron spectra (XPS) were obtained with Al Kα X-ray (hv = 1486.6 eV) radiation at 150 W from Thermo Scientific ESCALAB 250. Nicolet 5DXC spectrometer was used to record Fourier Transform Infrared Spectroscopy (FT-IR) and investigate the surface functional groups of catalysts in the range of 4000-400 cm −1 .

Conclusions
Mn-Ce/AC and CaO poisoning catalysts were prepared by the impregnation method and the poisoning effect of CaO on the catalyst was discussed in this study. The activity test experiment showed that loading CaO inhibited the catalytic activity of Mn-Ce/AC catalyst and the NO conversion of the catalyst decreased from 69.5% to the 38.2% at 75 • C. CaO poisoning catalyst had the smaller N 2 selectivity compared with Mn-Ce/AC catalyst. MnO 2 played a main catalytic role on SCR reaction and promoted the conversion rate of NO to NO 2 . However, the amount of MnO 2 in AC surface decreased in the process of loading CaO, which was detrimental to the SCR performance of the catalyst. The change of manganese oxide form inhibited generation rate for the chemisorption oxygen and NO 2 , which was the most critical reason for the decrease of catalytic activity for Mn-Ce/AC. In addition, loaded CaO entered into the pores of the catalyst, which led to the blockage of the pores and further led to the decrease of the BET surface area and total pore volume. It also destroyed the oxygen-containing functional groups of CaO poisoning catalyst. All of these caused the decrease of SCR activity for Mn-Ce/AC catalyst after loading CaO.

Conflicts of Interest:
The authors declare no conflict of interest.