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Article

Preparation of K Modified Three-Dimensionally Ordered Macroporous MnCeOx/Ti0.7Si0.3O2 Catalysts and Their Catalytic Performance for Soot Combustion

by
Chunlei Zhang
1,
Di Yu
1,
Chao Peng
1,
Lanyi Wang
2,
Xiaoqiang Fan
1,
Xuehua Yu
1,* and
Zhen Zhao
1,2,*
1
Institute of Catalysis for Energy and Environment, College of Chemistry and Chemical Engineering, Shenyang Normal University, Shenyang 110034, China
2
State Key Laboratory of Heavy Oil Processing, China University of Petroleum, 18# Fuxue Road, Changping, Beijing 102249, China
*
Authors to whom correspondence should be addressed.
Processes 2021, 9(7), 1149; https://doi.org/10.3390/pr9071149
Submission received: 10 June 2021 / Revised: 27 June 2021 / Accepted: 28 June 2021 / Published: 30 June 2021
(This article belongs to the Special Issue Environmental Catalysis and Air Pollution Control)
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Abstract

:
Soot particles in diesel engine exhaust is one of the main reasons for hazy weather and elimination of them is urgent for environmental protection. At present, it is still a challenge to develop new catalysts with high efficiency and low cost. In this paper, a kind of K modified three-dimensionally ordered macroporous (3DOM) MnCeOx/Ti0.7Si0.3O2 catalysts are designed and synthesized by a sample method. Due to the macroporous structure and synergistic effect of K, Mn, and Ce, the KnMnCeOx/Ti0.7Si0.3O2 (KnMnCeOx/M-TSO) catalysts exhibit good catalytic performance for soot combustion. The catalytic activity of K0.5MnCeOx/M-TSO was the best, and the T10, T50, and T90 are 287, 336, and 367 °C, respectively. After the prepared catalyst was doped with K, the physicochemical properties and catalytic performance changed significantly. In addition, the K0.5MnCeOx/M-TSO catalyst also somewhat exhibits sulfur tolerance owing to it containing Ti. Because of its simple synthesis, high activity, and low cost, the prepared KnMnCeOx/M-TSO catalysts are regarded as a promising candidate for application.

1. Introduction

Diesel engines have been widely used in automobile, ship, light truck, heavy machinery, and other fields because of its excellent thermal efficiency and durability [1,2]. However, diesel engines are also considered to be one of the major sources of soot particles emission and a cause of hazy weather [3,4]. With increasing awareness of environmental protection, the standards on exhaust emission of diesel engines have become increasingly stringent. Therefore, it is urgent to eliminate soot particles to meet emission standards. Nowadays, post-treatment technology is considered to be one of the effective ways to eliminate soot particles. However, since the spontaneous combustion temperature of soot particles (550–650 °C) is higher than the exhaust temperature of the diesel engine (150–450 °C), the development of new catalysts with low cost and excellent catalytic performance is one of the main challenges in the application of post-treatment technology [5,6].
At present, owing to three-phase gas(O2)-solid(soot)-solid(catalyst) reaction for soot combustion, various catalysts were prepared to improve the contact efficiency between soot and catalyst [7,8]. Different morphologies of catalysts with nanotube array, nanobelt, nanofiber, nanowire, disordered macropore, and 3DOM structures are studied to enhance effective contact [9,10,11,12,13,14]. Among the above morphologies, due to the interconnected macroporous structure with large pore diameter (>50 nm) and low diffusion resistance, the 3DOM catalyst has enough migration space for soot particles in its internal pores, which are expected to show excellent catalytic ability [15,16,17]. Many previous studies have shown that the catalytic performance of 3DOM oxide-based catalysts for soot combustion is superior to that of corresponding nanoparticle catalysts due to their structural effects [18,19,20]. To improve the intrinsic activity, a series of 3DOM oxides-supported Au and Pt catalysts have also been prepared in our research group, and the prepared 3DOM oxides-supported noble metal catalysts exhibit excellent catalytic ability in soot combustion reaction [21,22,23]. However, it is unsatisfactory that the application of noble metals is restricted by their high cost.
In recent years, considering the economy of catalyst cost, a number of rare earth oxides and transition metals have been studied for soot combustion [20,24,25,26]. MnOx-CeO2 mixed oxides with Mn and Ce synergistic effects have become one of the low cost and high performance catalysts [27,28,29,30]. In addition, alkali metals, especially potassium (K), exhibit excellent catalytic ability in soot combustion reaction. However, because of the low melting point of K, K-contained catalysts have weak thermostability in repeated cycles. To improve the stability of K-based catalysts, the incorporation of K into other stable structures is considered to be a promising way to resolve the problem of thermostability, and many kinds of K-doped catalysts have been reported by previous literature [31,32,33]. However, how to effectively combine the good contact efficiency of 3DOM structure and high catalytic activities of K, Mn, and Ce in one system of catalysts is also a research hotspot in the design and preparation of catalysts [34,35].
In this paper, a series of K-modified 3DOM MnCeOx/Ti0.7Si0.3O2 catalysts were synthesized by a simple preparation method. The catalysts have 3DOM structure and three active components of K, Mn, and Ce. The physicochemical properties of the as-prepared catalysts were characterized by X-ray diffraction (XRD), scanning electron microscopy (SEM), temperature-programmed reduction with H2 (H2-TPR), temperature-programmed desorption with O2 (O2-TPD), temperature-programmed oxidation with NO (NO-TPO), etc. The effect of macropore structure combined with the synergistic effect of K, Mn, and Ce is expected to improve the catalytic ability of the synthesized catalyst in soot combustion reaction.

2. Experimental Section

2.1. Catalysts Preparation

2.1.1. Synthesis of Highly Well-Defined PMMA Microspheres

Monodispersed polymethyl methacrylate (PMMA) microspheres were synthesized by the emulsifier-free emulsion polymerization method with potassium persulfate (KPS) as the initiator and methyl methacrylate (MMA) as the raw material. Ordered macroporous templates were prepared by centrifugal precipitation self-assembly method. The preparation method was reported in our previous work [36].

2.1.2. Synthesis of 3DOM Ti0.7Si0.3O2

3DOM Ti0.7Si0.3O2 was prepared by the colloidal template method. Tetrabutyl titanate, tetraethyl orthosilicate (TEOS), HCl, H2O, and ethanol were weighed according to a certain stoichiometric ratio and magnetically stirred for 3 h to obtain a homogeneous and clarified solution. The PMMA crystal template was immersed in the precursor solution for 1 h. After suction filtration and drying, the PMMA colloidal template was removed by calcination with air in a tubular furnace. The heating rate was 1 °C/ min, it was calcined at 310 °C for 3 h, and then heated to 600 °C and subsequently calcined for 4 h.

2.1.3. Synthesis of K Modified 3DOM MnCeOx/Ti0.7Si0.3O2

The 3DOM MnCeOx/Ti0.7Si0.3O2 catalysts were synthesized by the incipient wet impregnation method. The raw materials and amount of catalyst preparation are listed in Table 1. Ce(NO3)3⋅6H2O, 50% Mn(NO3)2, and KNO3 solution were dissolved in water, and the total volume was about 2 mL. The impregnated 3DOM Ti0.7Si0.3O2 was treated by ultrasonic for 15 min and dried at 80 °C for 12 h. The dried solid was calcined at 550 °C for 4 h to obtain 3DOM KnMnCeOx/Ti0.7Si0.3O2. To easily express the prepared catalysts, the 3DOM Ti0.7Si0.3O2 is abbreviated by M-TSO.

2.2. Physical and Chemical Characterization

XRD spectrum was obtained using the Rigaku Ultima IV X-ray diffractometer with Cu Kα radiation. The scanning range was 10–90° and the scanning speed was 10°/min. The phase identification of the catalyst was performed by comparing with the reference data of JCPDS.
The surface morphology and pore structure of the catalyst were observed by the Hitachi SU8010N scanning electron microscope under 1 V–5 kV accelerating voltage. To improve the quality of SEM photos, the samples were treated by spraying gold.
The specific surface area, pore size, and pore volume of the catalyst were determined by BET technique using the Micromeritics TriStar II: 3020 specific surface analyzer. The samples were analyzed after degassing at 300 °C for 3 h.
H2-TPR measurements were performed by the Micromeritics AutoChem II 2920 Chemical Adsorption Instrument. The sample was first purged with argon at 300 °C for 1 h, and then dropped to room temperature. After switching the gas flow to a hydrogen argon mixture, the instrument rose to 850 °C (heating rate was 10 °C/min) and the thermal conductivity detector (TCD) was used to monitor H2 consumption signals.
O2-TPD was determined by the TP-5076 adsorption instrument. The 100 mg sample was pretreated in O2 atmosphere at 300 °C for 1 h, and then dropped to room temperature. The flow rate was switched to He flow (60 mL/min), and the temperature was raised to 900 °C at a heating rate of 10 °C/min. TCD was used to monitor desorption oxygen.
NO-TPO measurements were performed by the NOx Analyzer nCLD 62. After pretreatment of 0.1 g catalyst in argon atmosphere at 200 °C for half an hour, the reaction gas was changed. The total flow rate was 50 mL/min, containing 1000 ppm NO, 10% O2, and the rest was argon. The temperature program was set to rise from 50 °C to 600 °C at a heating rate of 2 °C/min. The instrument can monitor the content of nitrogen oxides in the outlet gas in real time.

2.3. Catalytic Activity Measurements

The catalytic activity of catalysts for soot combustion was evaluated by temperature programmed oxidation (TPO) in a fixed bed tubular quartz reactor (Φ = 8 mm). The model soot was Printx-U particulates (25 nm diameter, purchased from Degussa, Frankfurt, Germany). The elemental composition of Printx-U particles was 94.2% C, 3.1% O, 0.8% H, 0.4% S, 0.2% N, and 4.7% others [37]. Measures of 0.01 g of soot and 0.1 g of catalyst were weighed and mixed uniformly at a mass ratio of 1:10 to simulate loose contact conditions, and then they were loaded into the quartz reactor. The reaction gas (50 mL/min) included 10% O2, 2000 ppm NO, and the rest was argon. We set the heating program from 100 °C to 650 °C, with a heating rate of 2 °C/min. The main components of the outlet gas were N2, NOx, CO2, and CO. The outlet gas compositions were analyzed by an online gas chromatograph (GC, Agilent 7890B) equipped with a flame ionization detector (FID). Complete conversion of CO and CO2 to CH4 over nickel catalyst was maintained at 380 °C before entering FID. The temperature T10, T50, and T90 of 10%, 50%, and 90% conversion of soot particles can be used to evaluate the catalytic activity. The selectivity of CO2 is another essential standard for evaluating the catalytic combustion of soot. Equation (1) was the calculation method applied.
S m C O 2 = [ C O 2 ] o u t m a x [ C O 2 ] o u t m a x + [ C O ] o u t m a x × 100 %
[ C O 2 ] o u t m a x and [ C O ] o u t m a x are, respectively, expressed as the concentration of CO2 and CO in the reaction product when the reaction temperature is the peak temperature, and S m C O 2 is the selectivity of CO2 when the soot combustion rate is the fastest.
Other reaction conditions remain constant; the sulfur resistance of the catalyst to soot combustion was tested by changing the gas composition of the reaction gas. The total gas flow rate was 50 mL/min, containing 100 ppm or 300 ppm SO2, 10% O2, 2000 ppm NO, and the rest was argon.

3. Result and Discussion

3.1. Structural Features of the Synthesized Catalysts

3.1.1. XRD Patterns of the Prepared Catalysts

The XRD patterns of KnMnCeOx/M-TSO catalysts with different K doping amounts, M-TSO support, and K0.5MnCeOx/M-SiO2 are shown in Figure 1. For M-TSO support, the pattern peak for 2θ of 25.4°(101) belongs to anatase TiO2 (marked by “◆” in Figure 1a; JCPDS Card No. 21-1272) [38,39,40]. As shown in Figure 1b, MnCeOx/M-TSO catalyst exhibits four feature peaks, which are located at 2θ of 28.8°(111), 33.5°(200), 47.6°(220), and 56.8°(311) (marked by “▲” in Figure 1b), and these correspond to diffraction peaks of CeO2. However, the peak of anatase TiO2 disappeared, which is related to coverage of M-TSO surface by MnCeOx oxides. It can be seen from Figure 1c–h that the XRD patterns of KnMnCeOx/M-TSO catalysts also belonged to the CeO2 crystal structure when the K was doped into MnCeOx/M-TSO. However, compared with reported crystal structure of pure CeO2 (JCPDS Card No. 43-1002), a slight shifting towards a higher diffraction angle of 2θ was observed on KnMnCeOx/M-TSO catalysts, in which the 2θ was shifted from 28.5 to 28.8° for the crystal face of (111) [41,42]. In addition, Figure 1c–h also exhibits that no feature peaks of KNO3, KOx, or MnOx can be observed. The above phenomena indicate that due to the large lattice spacing of CeO2, K and Mn have been doped into the lattice of CeO2. It can be seen from Figure 1i that the XRD pattern of the K0.5MnCeOx/M-SiO2 catalyst also belongs to the CeO2 crystal structure.

3.1.2. SEM Images of the Catalysts

Figure 2 is the SEM images of prepared catalysts. Figure 2a indicates that macroporous structures can be well observed in the M-TSO support. The diameters of the macropores are about 290–330 nm and the wall thicknesses of macropores are about 30–50 nm. Meanwhile, three small pores with diameter of 80–120 nm, which formed in the contact area of two PMMA spheres, can be also obtained in a macropore, and they are interconnected with other adjacent macropores [43]. When the MnCeOx and KnMnCeOx are loaded on the M-TSO support, the pore structure of MnCeOx/M-TSO and KnMnCeOx/M-TSO are well maintained (Figure 2b–e). The SEM results indicate that the loading processes of MnCeOx and KnMnCeOx do not destroy the pore structure of M-TSO support, and also demonstrate that the 3DOM structure of the M-TSO support is stable and strong. As shown in the SEM image of Figure 2, the prepared catalyst has uniform pore sizes, which are arranged highly periodically and connected through small windows [44]. The ordered pore structures are beneficial to improving catalyst-soot contact efficiency.

3.1.3. N2 Adsorption–Desorption Isotherms of the Prepared Catalysts

The N2 adsorption-desorption isotherm and the pore size distribution of the prepared catalyst can be seen in Figure 3. Based on the IUPAC, the prepared catalysts have typical type II adsorption-desorption isotherm [45]. However, the hysteresis loops of prepared catalysts are different with each other when MnCeOx and KnMnCeOx are loaded on the M-TSO support. As shown in Figure 3A(a–c), the M-TSO support exhibits weak intensity of the hysteresis loop, while MnCeOx/M-TSO and K0.1MnCeOx/M-TSO catalysts exhibit obvious hysteresis loops at high relative pressure. However, with increasing the doping dosage of K, the hysteresis loops of the KnMnCeOx/M-TSO catalysts are changed to indistinct (Figure 3A(d–h)). The pore size distributions in Figure 3B also indicate that MnCeOx/M-TSO and K0.1MnCeOx/M-TSO catalysts have obvious mesoporous structures at the range of 2–40 nm, while the other samples do not exhibit mesopores. Textural properties of prepared catalysts are listed in Table 2. Compared with M-TSO support, MnCeOx/M-TSO and K0.1MnCeOx/M-TSO catalysts exhibit higher surface area and total pore volume, which are well agreed with the results of N2 adsorption-desorption isotherms and pore size distributions. With the increase of K doping, the surface area decreases, and the value reduces to 30.1 m2/g. The above phenomena are possibly related to the accumulation pores of MnCeOx and K0.1MnCeOx active components on the surface of M-TSO, while the morphologies of KnMnCeOx may be changed at high doping dosage of K. With the increase of K doping, the total pore volume of KnMnCeOx/M-TSO decreased first, and then kept stable, while the pore size decreased first, and then increased. This phenomenon may be related to the deposition of KnMnCeOx active components on the surface of M-TSO. When the doping of K is increased, a mass of K or KMnCeOx species are filled into the surface gaps of M-TSO and reduce the amounts of small pores. Therefore, the pore size increases with the increasing of K doping. Figure 3A(i), Figure 3B(i), and Table 2 show that K0.5MnCeOx/M-SiO2 also has a lower specific area and a larger pore size than that of K0.5MnCeOx/M-TSO.

3.1.4. H2-TPR Profiles of the Prepared Catalysts

The inherent redox property of the catalyst is the key to enhance the catalytic activity and deep oxidation of soot. In this work, to clearly investigate the influence of different K doping amounts and different active components, five representative catalysts, i.e., M-TSO, MnCeOx/M-TSO, K0.1MnCeOx/M-TSO, K0.5MnCeOx/M-TSO, and K1MnCeOx/M-TSO, were determined by H2-TPR. Since no obvious reduction peak is observed in Figure 4a at a low temperature (<500 °C), it indicates that the redox ability of M-TSO was very weak. The weak reduction peak observed at 650 °C is related to the reduction reaction of Tin+ in M-TSO [46]. When MnCeOx and KnMnCeOx are loaded on the M-TSO support, the reduction peak positions and types of prepared catalysts have distinct differences with that of M-TSO support. As shown in the Figure 4b–e, the reduction peaks can be divided into four ranges of 178–250 °C, 280–350 °C, 350–450 °C, and >650 °C. Due to the large negative reduction potential, MnO was not reduced to Mn0, even above 950 °C. Therefore, MnO was considered to be the final state for the preparation of catalyst reduction [47,48]. According to the reduction process of Mn-based oxides, the first peak at 178–250 °C may be attributed to MnO2 reduction to Mn2O3, the second peak at 280–350 °C could be related to Mn2O3 reduction to Mn3O4, and the third peak at 350–450 °C could belong to the Mn3O4 reduction to MnO [16,49]. The fourth peak at >650 °C is assigned to the reduction of CeO2 to Ce2O3. Compared with MnCeOx/M-TSO catalyst, the doping of K into MnCeOx will lead to the lower reduction temperature (Figure 4c). However, with increasing the K doping amounts, the reduction temperature is increased. The H2-TPR results indicate that the doping of K in MnCeOx/M-TSO catalyst can modify the reduction properties of KnMnCeOx/M-TSO catalysts and is beneficial for regulating catalyst activities.

3.1.5. O2-TPD Results of the Prepared Catalysts

The active oxygen species are essential for improving catalytic activity for deep oxidation of soot combustion. To conformably compare with the H2-TPR results, the same samples as those of H2-TPR that were determined were studied by O2-TPD, and the results are shown in Figure 5. The oxygen desorption peaks of prepared catalysts can be divided into three peaks, and the temperature regions are located at T ≤ 250 °C, 250 °C ≤ T ≤ 500 °C, and T ≥ 500 °C, respectively. However, the M-TSO support exhibits only two obvious oxygen desorption peaks, which are located at 100 and 380 °C. The first oxygen desorption peak (named as α in the Figure 5) at T ≤ 250 °C belongs to the surface-active oxygen species (Osurf) or physically adsorbed oxygen [50]. The second peak, which is located at 250 °C ≤ T ≤ 500 °C and named as β, can be assigned to chemically adsorbed oxygen on the oxygen vacancies (O2−/O−) [51]. The third peak, named γ, belongs to the desorption of lattice oxygen (O2−) in the MnCeOx and KnMnCeOx [52]. Compared with M-TSO support, it can be discovered that the third peaks are newly appeared. In addition, the shapes of the third peaks are also different with various K doping amounts. The reasons for the above phenomena are possibly related to the interaction of K and MnCeOx.

3.1.6. NO-TPO Results of the Prepared Catalysts

Because of the relationship of “trade off” between soot and NOx, NOx is an inevitable gas in the emission of diesel engines [53]. In addition, NOx, especially NO2, is an important factor to improve the catalytic performance. Based on the above reasons, the NO-TPO of the M-TSO support, MnCeOx/M-TSO, and K0.5MnCeOx/M-TSO catalysts were studied, and the results of the test are shown in Figure 6. Owing to strong oxidization ability, soot particles can be directly oxidized by NO2. Therefore, NO2 participates in the reaction and changes the reaction path of soot combustion. The soot combustion reaction will change from gas(O2)-solid(catalyst)-solid(soot) to gas(O2)-gas(NO2)-solid(soot), which is beneficial to enhance the catalytic activity. As shown in the Figure 6A, M-TSO support exhibits low NO2 concentration at the temperature range of 100–400 °C. When the temperature is higher than 400 °C, there is a little enhancement of NO2 concentration, and the NO concentration decreases correspondingly. This result indicates that M-TSO support may exhibit low catalytic activity during soot combustion. The low NO2 concentration also agrees well with the H2-TPR result of M-TSO support. Figure 6B,C exhibit the NOx, NO, and NO2 concentration of the MnCeOx/M-TSO and K0.5MnCeOx/M-TSO catalyst. Compared with Figure 6A, the NO2 concentration for the MnCeOx/M-TSO and K0.5MnCeOx/M-TSO catalyst has obvious enhancement at the temperatures of 200–500 °C. The generated NO2 is expected to improve the catalytic activity of the MnCeOx/M-TSO and K0.5MnCeOx/M-TSO catalyst for soot combustion. As shown in Figure 6B, the temperature for the most concentration of NO2 is about 300 °C, while it can be seen from Table 3 that the T50 of K0.5MnCeOx/M-TSO catalyst for soot combustion is 354 °C. At a high temperature, part of NO2 has been decomposed and cannot react with soot particles. From Figure 6C, the temperature for the most concentration of NO2 for the K0.5MnCeOx/M-TSO catalyst is about 330 °C. This temperature is concordant with the T50 of the K0.5MnCeOx/M-TSO catalyst. Therefore, most of the NO2 can directly react with soot particles, which is beneficial to improve the catalytic activity.

3.2. Catalytic Performance in Soot Combustion

3.2.1. Catalytic Activities of the Prepared Catalysts

The catalytic activity of the prepared catalyst in soot combustion was evaluated by TPO test, and to better evaluate the catalytic activity of active components, the combustion performance of soot on M-TSO under the same conditions was compared. As shown in Table 3, the combustion temperatures T10, T50, and T90 of pure soot are 457, 552, and 594 °C, respectively. The combustion temperature of soot on M-TSO was slightly lower than that of pure soot. The catalytic activity of M-TSO was very weak, and the T10, T50, and T90 were 376, 517, and 565 °C, respectively. However, when MnCeOx is loaded on the M-TSO support, the catalytic ability of the MnCeOx/M-TSO catalyst in soot combustion reaction is obviously improved. When the K are doped into the MnCeOx/M-TSO, the catalytic activities of KnMnCeOx/M-TSO catalysts are further improved. With the increase of K doping amounts, the catalytic activity of the catalyst increased continuously until the molar ratio of K to Mn reached 0.5; after that, with the further increase of the K doping amount, the catalytic activity decreased continuously. Among the prepared catalysts, the catalytic activity of the K0.5MnCeOx/M-TSO catalyst was the best, and the T10, T50, and T90 were 287, 336, and 367 °C, respectively. In addition, the CO2 selectivity of the MnCeOx/M-TSO and KnMnCeOx/M-TSO catalysts are more than 96%, which is much higher than that of the M-TSO support.

3.2.2. Sulfur Resistances of Prepared Catalysts

Due to the methods of the formation of fossil fuels, sulfur compounds are unavoidable in the diesel engine exhausts. Many previous studies have proved that Ti has high sulfur resistance in the catalytic reaction. To demonstrate the sulfur resistance of prepared catalysts, the catalytic performances of the K0.5MnCeOx/M-TSO and K0.5MnCeOx/M-SiO2 catalysts under 100 ppm SO2 were estimated. It can be seen from Figure 7 that there are significant differences between the two catalysts at T10 temperature, which indicates that K0.5MnCeOx/M-TSO has somewhat sulfur resistance. However, the temperatures of T50 and T90 for the tested catalysts are similar. In addition, compared with the results of Table 3 and Figure 7, the catalytic activity of K0.5MnCeOx/M-TSO has certainly declined with increasing of SO2 concentration. The reason for the above phenomena may be related to the sulfuration of K0.5MnCeOx at high temperatures. In order to better explore the sulfur resistance, the reacted K0.5MnCeOx/M-TSO catalyst under 300 ppm SO2 was calcined at 550 °C for 4 h again to regenerate. After regeneration, the activity test was carried out again under 300 ppm SO2. The result indicates that the activity of the regenerated K0.5MnCeOx/M-TSO catalyst is also certainly decreased (Figure 7).

4. Conclusions

In summary, a K-modified 3DOM MnCeOx/Ti0.7Si0.3O2 catalyst was prepared by a simple method, in which the catalyst had 3DOM structure and three active components of K, Mn, and Ce. The KnMnCeOx/M-TSO catalysts exhibit excellent catalytic performance for soot combustion because of the macroporous structure and synergistic effect of K, Mn, and Ce. The K0.5MnCeOx/M-TSO catalyst has the best catalytic performance among the prepared catalysts, and the T10, T50, and T90 are 287, 336, and 367 °C, respectively. The characterization results indicate that the physicochemical properties of catalysts are changed when the K is doped into the MnCeOx/M-TSO catalyst, and different doping amounts of K have obvious influence on the catalytic performance. In addition, compared with the K0.5MnCeOx/M-SiO2 catalyst, the K0.5MnCeOx/M-TSO catalyst also exhibits somewhat sulfur tolerance owing to it containing Ti. Meantime, the research results show that the prepared KnMnCeOx/M-TSO catalyst has the advantages of simple synthesis method, low cost, and high activity, and this has a certain application prospect.

Author Contributions

Conceptualization, C.Z. and X.Y.; methodology, C.Z.; software, C.P.; validation, D.Y., L.W. and C.P.; formal analysis, X.F.; investigation, C.Z. and D.Y.; resources, X.Y.; data curation, C.Z.; writing—original draft preparation, C.Z.; writing—review and editing, X.Y.; visualization, Z.Z.; supervision, X.Y.; project administration, Z.Z.; funding acquisition, X.F. All authors have read and agreed to the published version of the manuscript.

Funding

This research was funded by National Natural Science Foundation of China (22072095, U1908204, 21761162016); Key Research and Development Program of MOST (2017YFE0131200) for collaboration between China and Poland; General Projects of Liaoning Province Natural Fund (2019-MS-284); National Engineering Laboratory for Mobile Source Emission Control Technology (NELMS2018A04); University level innovation team of Shenyang Normal University; Major Incubation Program of Shenyang Normal University (ZD201901).

Institutional Review Board Statement

Not applicable.

Informed Consent Statement

Not applicable.

Data Availability Statement

All the data during the study appeared in the submitted article.

Acknowledgments

The instruments and equipment used in this work are supported by Major Platform for Science and Technology of the Universities in Liaoning Province: The Engineering Technology Research Center of Catalysis for Energy and Environment and The Belt and Road International Joint Research Center of Catalysis for Energy and Environment.

Conflicts of Interest

The authors declare no conflict of interest.

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Figure 1. XRD patterns of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.3MnCeOx/M-TSO; e: K0.5MnCeOx/M-TSO; f: K0.7MnCeOx/M-TSO; g: K0.9MnCeOx/M-TSO; h: K1MnCeOx/M-TSO; i: K0.5MnCeOx/M-SiO2).
Figure 1. XRD patterns of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.3MnCeOx/M-TSO; e: K0.5MnCeOx/M-TSO; f: K0.7MnCeOx/M-TSO; g: K0.9MnCeOx/M-TSO; h: K1MnCeOx/M-TSO; i: K0.5MnCeOx/M-SiO2).
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Figure 2. SEM images of the catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.5MnCeOx/M-TSO; e: K1MnCeOx/M-TSO).
Figure 2. SEM images of the catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.5MnCeOx/M-TSO; e: K1MnCeOx/M-TSO).
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Figure 3. Nitrogen adsorption-desorption isotherms (A) and pore size distributions (B) of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.3MnCeOx/M-TSO; e: K0.5MnCeOx/M-TSO; f: K0.7MnCeOx/M-TSO; g: K0.9MnCeOx/M-TSO; h: K1MnCeOx/M-TSO; i: K0.5MnCeOx/M-SiO2).
Figure 3. Nitrogen adsorption-desorption isotherms (A) and pore size distributions (B) of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.3MnCeOx/M-TSO; e: K0.5MnCeOx/M-TSO; f: K0.7MnCeOx/M-TSO; g: K0.9MnCeOx/M-TSO; h: K1MnCeOx/M-TSO; i: K0.5MnCeOx/M-SiO2).
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Figure 4. H2-TPR curves of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.5MnCeOx/M-TSO; e: K1MnCeOx/M-TSO).
Figure 4. H2-TPR curves of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.5MnCeOx/M-TSO; e: K1MnCeOx/M-TSO).
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Figure 5. O2-TPD of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.5MnCeOx/M-TSO; e: K1MnCeOx/M-TSO).
Figure 5. O2-TPD of prepared catalysts (a: M-TSO; b: MnCeOx/M-TSO; c: K0.1MnCeOx/M-TSO; d: K0.5MnCeOx/M-TSO; e: K1MnCeOx/M-TSO).
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Figure 6. NOx, NO, and NO2 concentration over M-TSO support (A), MnCeOx/M-TSO catalyst (B), and K0.5MnCeOx/M-TSO catalyst (C).
Figure 6. NOx, NO, and NO2 concentration over M-TSO support (A), MnCeOx/M-TSO catalyst (B), and K0.5MnCeOx/M-TSO catalyst (C).
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Figure 7. Catalytic performance of catalysts under 100 ppm or 300 ppm SO2.
Figure 7. Catalytic performance of catalysts under 100 ppm or 300 ppm SO2.
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Table
Table 1. Expression of catalyst and amount of raw materials.
Table 1. Expression of catalyst and amount of raw materials.
CatalystsKNO3/gMn(NO3)2/gCe(NO3)3/g3DOM TiSiO/g3DOM SiO2/g
MnCeOx/M-TSO00.8230.9980.5—
K0.1MnCeOx/M-TSO0.0230.8230.9980.5—
K0.3MnCeOx/M-TSO0.0700.8230.9980.5—
K0.5MnCeOx/M-TSO0.1160.8230.9980.5—
K0.7MnCeOx/M-TSO0.1630.8230.9980.5—
K0.9MnCeOx/M-TSO0.2090.8230.9980.5—
K1MnCeOx/M-TSO0.2320.8230.9980.5—
K0.5MnCeOx/M-SiO20.0460.3290.399—0.2
Table
Table 2. Textural properties of prepared catalysts.
Table 2. Textural properties of prepared catalysts.
CatalystsSurface Area (m2/g) aTotal Pore Volume (m2/g) bPore Size (nm) c
M-TSO51.30.1239.9
MnCeOx/M-TSO81.10.2189.4
K0.1MnCeOx/M-TSO69.70.21811.2
K0.3MnCeOx/M-TSO45.00.12110.1
K0.5MnCeOx/M-TSO44.20.1058.9
K0.7MnCeOx/M-TSO36.70.10110.5
K0.9MnCeOx/M-TSO31.80.10913.8
K1MnCeOx/M-TSO30.10.10114.1
K0.5MnCeOx/M-SiO231.20.10013.1
a Calculated by BET method; b Calculated by BJH desorption cumulative volume of pores between 1.7 nm and 300 nm diameter; c Calculated by BJH desorption average pore diameter.
Table
Table 3. Catalytic performance of prepared catalysts for soot combustion.
Table 3. Catalytic performance of prepared catalysts for soot combustion.
CatalystsT10/℃T50/℃T90/℃Sco2m/%
Soot45755259441%
M-TSO37651756550.5%
MnCeOx/M-TSO28435439399.3%
K0.1MnCeOx/M-TSO28634638099.4%
K0.3MnCeOx/M-TSO28533837998.3%
K0.5MnCeOx/M-TSO28733636798.9%
K0.7MnCeOx/M-TSO29334137997.7%
K0.9MnCeOx/M-TSO29534537997.3%
K1MnCeOx/M-TSO30034938496.7%
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Zhang, C.; Yu, D.; Peng, C.; Wang, L.; Fan, X.; Yu, X.; Zhao, Z. Preparation of K Modified Three-Dimensionally Ordered Macroporous MnCeOx/Ti0.7Si0.3O2 Catalysts and Their Catalytic Performance for Soot Combustion. Processes 2021, 9, 1149. https://doi.org/10.3390/pr9071149

AMA Style

Zhang C, Yu D, Peng C, Wang L, Fan X, Yu X, Zhao Z. Preparation of K Modified Three-Dimensionally Ordered Macroporous MnCeOx/Ti0.7Si0.3O2 Catalysts and Their Catalytic Performance for Soot Combustion. Processes. 2021; 9(7):1149. https://doi.org/10.3390/pr9071149

Chicago/Turabian Style

Zhang, Chunlei, Di Yu, Chao Peng, Lanyi Wang, Xiaoqiang Fan, Xuehua Yu, and Zhen Zhao. 2021. "Preparation of K Modified Three-Dimensionally Ordered Macroporous MnCeOx/Ti0.7Si0.3O2 Catalysts and Their Catalytic Performance for Soot Combustion" Processes 9, no. 7: 1149. https://doi.org/10.3390/pr9071149

APA Style

Zhang, C., Yu, D., Peng, C., Wang, L., Fan, X., Yu, X., & Zhao, Z. (2021). Preparation of K Modified Three-Dimensionally Ordered Macroporous MnCeOx/Ti0.7Si0.3O2 Catalysts and Their Catalytic Performance for Soot Combustion. Processes, 9(7), 1149. https://doi.org/10.3390/pr9071149

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