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Journal of the Chilean Chemical Society

On-line version ISSN 0717-9707

J. Chil. Chem. Soc. vol.57 no.1 Concepción Mar. 2012 

J. Chil. Chem. Soc, 57, No 1 (2012); págs.: 1048-1053





1 Department of Chemistry, Nanchang University, Nanchang, 330031, P. R. China . *e-mail:
2Department of Chemistry, Jiangxi Agricultural University, Nanchang, 330045, P. R. China


The CeO2-MnOx mixed oxides were prepared by deposition-precipitation (DP) and surfactant-templated (CB) methods, and then used as the support of CuO/ CeO2-MnOx catalysts. The samples were characterized by means of XRD, BET, H2-TPR, CO-TPD and XPS. Results show that preparation methods of CeO2-MnOx support have a direct effect on the physicochemical properties and catalytic activities of CuO/CeO2-MnOx catalysts for the CO preferential oxidation in H2-rich gases(CO PROX). CuO/CeO2-MnOx (CB) catalyst exhibits higher CO conversion and stability in H2-rich gases than CuO/CeO2-MnOx (DP), with 100% conversion of CO at 140 °C after a temperature cycle, which indicates that CeO2-MnOx (CB) as support of CuO based catalyst is more useful for CO PROX reaction than CeO2-MnOx (DP). Compared with CuO/CeO2-MnOx (DP), there are richer oxygen vacancies and more Mn4+ species on the surface of CuO/CeO2-MnOx (CB), and stronger interaction between CeO2 and MnOx in it. More amounts of active copper species and complicated transfer of electrons density on CuO/CeO2-MnOx (CB) also favour the activity of the catalyst.

Keywords: CuO/CeO2-MnOx catalyst, Preparation method of CeO2-MnOx, CO oxidation, In H2-rich gases.


In recent years, polymer electrolyte membrane fuel cell (PEMFC) which utilizes hydrogen as a fuel has been attracting much attention in the applications to electric vehicles or residential power-generations due to its low operation temperature, excellent energy efficiency and zero-emission of air pollutants. Hydrogen for PEMFC is generally generated from steam reforming or partial oxidation of hydrocarbons or methanol followed by the water-gas shift reaction. However, typical hydrogen mixtures from such a process usually contain 0.5-2% CO which can poison the Pt electrode in the PEMFC. Thus, carbon monoxide needs be decreased to a trace-level (below 10 ppm) to avoid poisoning of the Pt electrode. Among the current available methods to remove CO in the H2-rich gases, preferential oxidation of CO in H2-rich gases (PROX) was proved to be the most straightforward and economic one 1-4. So far, extensive studies have focused on improving the activity of the catalysts for CO-PROX reaction. However, developing efficient catalysts for PROX system is still a challenge.

Catalysts for CO PROX are mainly the precious metals catalysts (such as Pt, Ru and Rh), gold-based catalysts and CuO-based catalysts 1,5. Ofthese catalysts, catalysts based on combinations between copper and cerium oxides have also shown promising properties for CO PROX and constitute a more interesting alternative from an economical point of view. Extensive investigations have been carried out about the preparation methods, characterization, mechanism and testing of CuO/CeO2 catalysts 3-8. Some researchers reported the performance of CuO/CeO2 catalysts was superior to that of Pt-based catalysts because of strong interactions between the copper species and the CeO2 support 6,7. However, most CuO/CeO2 catalysts showed the narrow temperature window with high CO conversions and its catalytic activity strongly depended on the preparation methods 1. Generally, the mechanism for CO PROX on CuO/CeO2 can be regarded as a redox reaction process involving lattice oxygen and lattice vacancy, and thus metals modification is important to improve the activity of CuO/CeO2 catalysts.

Previous investigations in CuO/(CeO, M) catalysts field have revealed that changing the chemical composition of support with ceria-related mixed oxides (Ce-M) instead of pure CeO2 could greatly improve the catalyst activity, which has mainly been attributed to the enhanced oxygen mobility of CeO2-MOx and the synergetic effect through the interaction between the mixed oxides 8. CeO2-MnOx mixed oxides, as the two-way support, could exhibit much better redox properties than ceria alone due to multi-valence state and strong interaction between ceria and manganese. However, reports on CO-PROX over CeO2-MnOx oxides support are still less.

It is well known that catalytic activity strongly depended on not only chemical composition of catalyst, but also the preparation methods. However, to our knowledge, the effect of CeO2-MnOx support prepared with different methods on the activity of the CuO-based catalysts for CO-PROX has not been studied. In this work, two CeO2-MnOx supports were prepared by deposition-precipitation and surfactant-templated methods, respectively, and the effect of preparation methods on the performance was studied. Characterizations of the CeO2-MnOx or CuO/CeO2-MnOx were performed with N2 adsorption, X-ray diffraction (XRD), H2 temperature- programmed reduction (TPR), CO temperature-programmed desorption (TPD), X-ray photoelectron spectra (XPS). The results of this physicochemical characterization were discussed in relation to the exhibited catalytic performance of the CuO/CeO2-MnOx catalysts.


2.1.    Catalysts preparation

2.1.1.   Preparation of CeO2, MnOx and CeO2-MnOx supports

Pure CeO2 and MnOx were prepared by precipitation method. The appropriate quantities of ammonia solution (5%) were added dropwise into the ammonium cerium(IV) nitrate solution (0.1 mol/L) and manganese(II) nitrate solution (0.1 mol/L), respectively, with vigorous stirring until pH of solution remained approximately at 10.0. The mixture was stirred for 4 h, filtered and washed with deionized water. The obtained sample was dried at 100 °C overnight and then calcined at 500 °C for 4 h under air.

CeO2-MnOx (DP) was prepared by deposition-precipitation method. A certain amount of ceria powder was added into the solution of 50% Mn(NO3)2 (Mn/(Mn + Ce) = 0.3, molar ratio) under vigorous stirring. Then 5% ammonia solution was added dropwise into the suspension until pH of the suspension solution was maintained at 10.0. The other steps were similar to those for the preparation of CeO2.

CeO2-MnOx (CB) was prepared by surfactant-templated method. A certain amount of cetyltrimethyl ammonium bromide (CTAB, 1 mmol) as template was dissolved in 500 mL of distilled water, followed by the addition of (NH4)2Ce(NO3)6 and 50% Mn(NO3)2 solution (Mn/(Mn + Ce) = 0.3, molar ratio) with vigorous stirring. The other steps were similar to those for the preparation of CeO2.

2.1.2.    Preparation of CuO-based catalyst

The CuO-based catalysts were prepared by impregnation method. The as-synthesized supports were impregnated with an ethanol solution of copper nitrate for 24 h, followed by drying (100 °C; 12 h) and calcining (400 °C; 4 h). The CuO loading for CuO-based catalysts was 8.0 wt %.

2.2.     Catalytic activity measurements

The CO oxidation reaction in H2-rich gas was carried out in a continuous micro-reactor. The catalyst (0.1 g) was used. The composition of the mixture gas was 1.9 vol. % CO, 3.3 vol.% O2, 50 vol.% H2 and 44.8 vol.% N2, and the space velocity was 60,000 ml/h-g. The gas composition was analyzed before and after the reaction by on-line gas chromatographs with thermal conductor detector (TCD) and carbon molecular sieve (TDX-01) column. The catalytic activity is expressed as conversion of CO. After the first measurement from 60 °C to 200 °C, the catalysts were kept at 200 °C for 10 h and decreased to room temperature, and then the second measurement was carried out from 60 °C to 200 °C to test the stabilities of the catalysts.

2.3.    Characterization of the catalysts

The BET surface area and porous texture were evaluated by N2 adsorption isotherms obtained at -196 °C using ASAP 2020 (Micrometrics) equipment. Before each measurement, the samples were degassed at 350 °C in vacuum (0.13 Pa) for 5 h. The surface area and average pore size of the samples were calculated with the BET equation and BJH formula, respectively.

The crystalline structure of the solids was studied by X-ray diffraction (XRD) using German Bruker-AXS Corporation D8 Advnce diffractometer equipped with a rotating anode, Cu Ka radiation combined with the nickel filter. Operating voltage was 40 kV and current 30 mA, with a scanning rate of 1o/min from 2θ = 20° to 80°.

H2 temperature-programmed reduction (H2-TPR) measurements were carried out on a Chemisorb 2750 instrument (Micrometrics). A 0.01 g sample was heated from room temperature to 600 °C under a He flow (50 ml/min) at a rate of 10 °C/min in order to remove possible impurities. After cooling to room temperature in He, a gas mixture consisting of H2 and N2 (10:90 v/v) was introduced into the system, heated to 600 °C at a rate of 10 °C /min for recording the TPR spectra.

CO temperature-programmed desorption (TPD) measurement was carried out on the same instrument with the H2-TPR measurement. A 0.01 g sample was heated from room temperature to 400 °C under a He flow (50 ml/min) at a rate of 10 °C/min. After being cooled to room temperature, CO was injected into the reactor until adsorption was saturated. Then the sample was heated to 400 °C at a rate of 10 °C/min in He flow (50 ml/min) for recording the CO-TPD spectra.

X-ray photoelectron spectra (XPS) were determined using a KROTAS AXIS Ultra DLD spectrometer with Al Ka radiation (hv = 1486.6 ev). The spectra of O 1s and Mn 2P2/3 levels were recorded. Charging effects were corrected by adjusting the binding energy of C 1s peak to 284.6 ev.


3.1.      The structural studies of CeO2-MnOx supports

The N2-physisorption isotherms and pore size distributions of CeO2 and CeO2-MnOx supports are shown in Fig. 1. Pure CeO2 exhibits a typical type-IV isotherm with a pronounced hysteresis loop characteristics which always is connected with pore structure, and CeO2-MnOx (DP) exhibits a similar isotherm indicating that the pore structure is maintained. The isotherm of CeO2-MnOx (CB) shows a obvious difference as compared with them. The change in the shape of isotherms is probably because the Mnx+ ions enter ceria bulk lattice resulting in the destruction of pores. The effect of preparation method of CeO2-MnOx supports on the surface area (SBET), pore volume (Vp), the mean pore diameter (rp), crystallite size and cell parameter of CeO2-MnOx are shown in Table 1. The BET surface area of CeO2-MnOx (DP) is lower than that of CeO2, probably resulting from a part ceria being covered with MnOx during the precipitation processes. Comparing with CeO2, CeO2-MnOx (CB) has larger BET surface area and smaller crystallite size, which might be due to that the CTAB template can effectively inhibit the crystal growth of CeO2 during precipitation and calcination processes. High surface area and small crystallite size are favorable for the redox properties of the mixed oxides 9.

XRD patterns of the CeO2, MnOx and CeO2-MnOx mixed oxides are shown in Fig. 1. The peaks observed at 2θ = 28.5°, 33.0°, 47.4° and 56.4° were assigned to the diffraction patterns of CeO2 (111), (200), (220) and (311) planes, respectively. For pure MnOx, the intensive and sharp diffractions peaks could be primarily attributed to Mn3O4 (PDF#24-0734). Weak diffraction peaks of MnOx (2θ = 37.1°) is found in CeO2-MnOx (DP), indicating the presence of separated MnOx, but no diffraction of MnOx is observed in CeO2-MnOx (CB). Compared with pure CeO2, the diffraction peaks of CeO2 in CeO2-MnOx (CB) slightly shift to higher values of the Bragg angles and the cell parameter of that decrease obviously, which indicates the formation of solid solution of CeO2 and MnOx 10. It leads to the increase of surface oxygen vacancies, as confirmed by O2-TPD 11. And the defect surface of solid solution can enhance the chemisorption of oxygen and accelerate the mobility of surface oxygen species 10, 12.

3.2      The reduction performance of supports and catalysts

H2-TPR can provide information concerning the reducibility of different chemical species presented in the catalyst as well as the degree of interaction between metal-support. The H2-TPR profiles of CeO2, MnOx, CuO/CeO2, CeO2 MnOx and CuO/CeO2 MnOx are shown in Fig. 3 and Table 2 lists the reduction temperature and hydrogen consumption of all peaks. Pure CeO2 exhibits two reduction peaks at 380 and 780 °C, which are ascribed to the reduction of surface and bulk oxygen of CeO2, respectively 13. The amount of H2 consumption is 342 µmol· g-1 at temperature less than 400 °C, and is about 12% of the total amount for the complete reduction of ceria from CeO2 to Ce2O3 The H2-TPR profile of pure MnOx shows a main reduction peaks at 323 °C with a slight overlapped shoulder peak at 273 °C, indicating a two-step reduction (MnOx Mn3O4 and Mn3O4 MnO)14. The total H2 consumption is calculated to be 5103 μmol· g-1, from which the predominant manganese species is estimated to be Mn3O4 as well as some higher valence manganese oxides. It is consistent with the result of XRD. For CeO2-MnOx mixed oxides, the H2-TPR profiles also show two reduction peaks (denoted as β and γ, respectively). According to the reduction characteristics of pure CeO2 and MnOx associated to the disappearance of the ceria low-temperature peak of CeO2-MnOx (CB), peak β is assigned to the reduction of MnOx2 Mn3O4, and peak γ represents the combined reductions of Mn3O42 MnO and the surface Ce4+ . Compared with the reduction temperature of pure MnOx and CeO2, the reduction temperatures of CeO22 MnOx (CB) at 180 and 208 °C greatly shift to lower regions, indicating the presence of interaction between manganese and cerium oxides. Although that of CeO22 MnOx (DP) also shift to lower temperature, the magnitude of shift is little. Thus, it can be inferred that the interaction between manganese and cerium oxides in CeO2-MnOx (DP) is weaker than that in CeO22 MnOx (CB). It is worthy noting that the H2 consumptions of peak β is more than that of peak γ, which imply that some manganese oxide species turn to higher oxidation states in CeO2-MnOx (CB). All these are possibly related to the formation of CeO2- MnOx (CB) solid solution.

The H2-TPR profile of CuO/CeO2 shows two overlapped reduction peaks at 166 °C and 176 °C which should be due to the complete reductions of copper species and the surface Ce4+ according to the H2 consumptions. For CuO/ CeO2-MnOx catalysts, three reduction peaks can be observed: α, β and γ. The appearance of peak a should obviously be due to the reduction of copper oxides compared with the reduction characteristics of CeO2-MnOx. The reduction temperature of peak a in CuO/CeO2-MnOx (CB) at 131 °C demonstrates a significant decrease compared with that in CuO/CeO2 and CuO/CeO2-MnOx (DP). Generally, there are three kinds of copper species in CuO-CeO2 and their reducibility follows this order 15-18: highly dispersed CuxO in contact with ceria particle > isolated copper ions interacting with the support > large clusters and bulk CuO phase that do not contribute to the activity. According to literatures 17, 18, large clusters and bulk CuO phase are reduced at temperature higher than 200 °C; isolated copper ions interacting with the support begin to be reduced at about 160 °C; highly dispersed Cu O in contact with ceria is easy to be reduced at 127-160 °C. Thus, from the reduction characteristics of copper species associated to the H2 consumption of peak a, it can be deduced that highly dispersed CuxO interacted with supports and isolated copper ions are the main copper species for CuO/CeO2- MnOx, and the amounts of highly dispersed CuxO in CuO/CeO2-MnOx (CB) are more than that in CuO/CeO2-MnOx (DP). In addition, the formation of CeO2-MnOx (CB) solid solution can facilitates the mobility of oxygen species on the surface 14, and then oxygen species can easily transfer to copper species from CeO2-MnOx (CB) during the reduction process. This also promote the reduction of copper species in CuO/CeO2-MnOx (CB) catalyst.

3.3     Study of XPS spectra of the catalysts

XPS characterization was performed to obtain information of the chemical state of the surface elements. Fig.4 (a) shows the XPS spectra of Mn 2p. It can be seen that the binding energy (BE) peaks of Mn 2p3/2 for CuO/CeO2-MnOx (DP) and CuO/MnOx are both centered at 641.8 eV, indicting the similar state of manganese species in the two samples, and that for CuO/CeO2-MnOx (CB) shifts to higher binding energy centered at 642.0 eV. According to the literature 19, the BE of Mn2p3/2 in pure manganese oxides was found to be at 641.2 eV (Mn2+), 641.8 eV (Mn3+) and 642.1 eV (Mn4+), respectively. Then, from deconvolution of the Mn 2p3/2 peaks, it can be estimated that the relative ratio of Mn3+ is about 83% for CuO/CeO2-MnOx (DP) and that of Mn4+ is about 62% for CuO/CeO2-MnOx (CB). Therefore, the Mn3+ is the dominant species in CuO/CeO2-MnOx (DP), while Mn4+ ions exist in CuO/CeO2-MnOx (CB) as main manganese species. Six B.E peaks at 882.3, 888.8, 898.4, 900*8, 907.2 and 916.7 eV are observed in the Ce 3d XPS spectra shown in Fig.4 (b). These components should be assigned to Ce4+ species by comparison with the data of literatures 20. CuO/CeO2-MnOx (CB) catalyst shows an inconspicuous peak at 885.0 eV along with the decrease of BE peak at 898.4 eV(arrowed in figure), which indicates the existence of Ce3+ species in addition to Ce4+. The generation of more Mn4+ species with existence of partial Ce3+ species should be arised from the strong interaction between CeO2 and MnOx in CuO/CeO2-MnOx (CB). As is well known, high valence state of manganese oxides is easily reduced, so the presence of Mn4+ may enhance the redox property of the catalyst.

Fig.4 (c) shows the XPS spectra of Cu 2p3/2 in CuO-based catalysts. It can be observed that these spectra consist of the main peak of Cu 2p3/2 centered at 932.6-933.8 eV and a shake-up peak around 942.5 eV. The B.E peak of Cu 2p3/2 for CuO/CeO2 is found at 933.8 eV with a clear shake-up peak, which is the characteristic of CuO according to the literature 21, 22. Lower B.E at 932.2-933.1 eV and the absence of the shake-up peak are characteristic of Cu2O 22, 23. The Cu 2p3/2 peaks shift to lower B.E for CuO/CeO2 -MnOx(CB), CuO/CeO2-MnOx(DP) and CuO/MnOx compared with CuO/CeO2, and CuO/CeO2-MnOx(CB) exhibits the lowest BE. The shift indicates some modifications of electronic properties of copper species, suggesting the occurrence of electrons transfer between copper species and manganese species. The valence state of copper species on CuO/CeO2- MnOx(CB) are also effected by oxygen vacancy on CeO2-MnO (CB) solid solution according to U.R. Pillai's reports 24. Simultaneously, the shift is accompanied with a obvious decrease of the intensity of the shake-up peak. Thus, their XPS spectra of Cu 2p3/2 demonstrate that Cu+ species exist in these three catalysts, and the number of Cu+ species on CuO/CeO2-MnOx (CB) seems to be more than that on CuO/CeO2 -MnOx (DP). Cu+ species is far likely to be the active site for CO adsorption during the CO PROX reaction 7.

Fig. 5 displays the XPS spectra of O1s used to investigate the oxygen species on the surface of CuO/CeO2-MnOx catalysts. The O1s spectra of CuO/ CeO2-MnOx catalysts contain a main peak at 528.9-529.5 eV could be ascribed to the lattice oxygen (denoted as O ), along with a shoulder at 531.3-532.3 eV assigned to the defect oxides or a mixture of hydroxyl groups on the surface of the catalysts (denoted as Oβ) 25. The defect oxides are favorable produce of oxygen vacancy. The comparison of the XPS spectra of O 15 between CuO/CeO2-MnOx (DP) and CuO/CeO2- MnOx (CB) indicates that the main peak intensity of the two catalysts is similar, indicating their lattice oxygen amount is almost the same. The relative concentrations of Oβ listed in table 3 are 23.6 and 41.7 % for CuO/CeO2-MnOx (DP) and CuO/CeO2-MnOx (CB), respectively. According to the following mechanism of preferential oxidation of CO (PROX) 26: (1) CO + M (adsorption site) CO-M; (2) CO-M + O*(lattice oxygen) CO2-M + Od (oxygen vacancy); (3) CO2-M — CO2 + M; (4) O2 + 2Od 2O*, the high concentrations of Oβ may be favorable for reaction (4). Oxygen molecular in reaction gases can transfer to lattice oxygen via oxygen vacancy. Compared with CuO/CeO2- MnOx (DP), Oβ peak intensity of CuO/CeO2-MnOx (CB) is stronger, which are favorable for the mobility of oxygen species and the generation of lattice oxygen.

3.4.      CO adsorption property of the catalysts

CO-TPD curves of CuO/CeO2-MnOx catalysts are given in Fig. 5. CuO/CeO2-MnOx catalysts show two CO desorption peaks: α and β. CO desorption peaks temperature of CuO/CeO2-MnOx (DP) and CuO/CeO2-MnOx (CB) is 110, 175 °C and 105, 180 °C, respectively. As reported 27, 28, the CO desorption peaks are around 250 and 110 □ for pure MnOx and CuO/CeO2, respectively. This indicates that the peak α and β should be due to CO adsorbed on the copper species and manganese species in CuO/CeO2-MnOx catalysts, respectively. The a peak areas of CuO/CeO2-MnOx (CB) catalyst is much larger, implying that more copper active sites as CO adsorption sites exist in CuO/CeO2-MnOx (CB). CuO/CeO2-MnOx (DP) shows stronger peak β, indicating more manganese species as CO adsorption sites on its surface. The more copper species active sites and adsorption amount of CO, the more available the reactions were.

3.5.      Performance of CuO/CeO2-MnOx catalysts

The catalytic activity of CeO2-MnOx mixed oxides and CuO-based catalysts for CO PROX system is shown in Fig. 7. CeO2-MnOx mixed oxides show relative low CO conversion in the temperature range investigated. It can be found that catalytic activity is not only dependent upon active constituents, but also has relations with supports of the catalysts. Obviously, the catalytic activity values of CuO-based catalysts with CeO2-MnOx mixed oxides as two-way support are higher than that with single support, especially at low temperature. From Fig.7, the catalytic activity of catalysts can be ranked as: CuO/CeO2-MnOx (CB)>CuO/CeO2-MnOx (DP)>CuO/CeO2 >CuO/MnOx. The activity of CuO/CeO2-MnOx (CB) catalyst is higher than that of CuO/ CeO2-MnOx (DP). A complete conversion of CO over CuO/CeO2-MnOx (CB) achieves at 140 °C, whereas that over CuO/CeO2-MnOx (DP) catalyst is at 180 °C. This result indicates that the preparation methods of CeO2-MnOx support have a significant influence on the catalytic performance of CuO/CeO2-MnOx catalysts. After the first measurement, CuO/CeO2-MnOx catalysts are successively under reaction atmosphere at 200 °C for 10 h and cool down to room temperature, and then start the second activity test. The results after the temperature cycle are shown in Fig. 8. It can be observed that the conversion of CO remains almost unchanged, in addition to a slight decrease at 60 °C and 80 °C. The values of CuO/CeO2-MnOx (CB) and CuO/CeO2-MnOx (DP) decrease by 6% and 10% at 80 °C, respectively. This indicates that CuO/CeO2-MnOx(CB) catalyst is more stable for CO oxidation in H2-rich gases than CuO/CeO2-MnOx (DP).


In this work, CeO2-MnOx was prepared by deposition-precipitation (DP) and surfactant- templated (CB) methods, and then used as support of CuO/ CeO2-MnOx catalysts. The structure analysis indicates that CeO2-MnOx (CB) support prepared by surfactant-templated mothd possesses a larger BET surface area and smaller particle size, compared with CeO2-MnOx (DP). Meanwhile, the formation of stable solid solution results in the strong interaction between CeO2 and MnOx in CeO2-MnOx (CB). The experimental results confirm that there are richer surface oxygen vacancies and more Mn4+ species on the surface of CuO/CeO2-MnOx (CB) than that of CuO/CeO2-MnOx (DP). Surface oxygen vacancies facilitate the transference of oxygen species from CeO2-MnOx (CB) to active copper species and Mn4+ species improve the reduction of catalyst. And there are complicated electrons transfer occurred in CuO/CeO2-MnOx (CB) catalyst. All these must be benefit to CuO/CeO2-MnOx (CB) catalyst on CO PROX reaction. In addition, the more amounts of active copper species and CO adsorption sites distributed on CeO2-MnOx (CB) should be responsible for the superior performance of CuO/CeO2-MnOx (CB) catalyst. As a result, CuO/CeO2-MnOx (CB) catalyst shows higher catalytic activity (CO conversion reach 100% at 14¾ °C) and stability than CuO/CeO2-MnOx (DP).


We gratefully acknowledge the financial support from the National Natural Science Foundation of China (No. 21062013).

(Received: August 5, 2011 - Accepted: October 3, 2011)



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