Unravelling the Nature of the Active Species as well as the Doping

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Unravelling the Nature of the Active Species as well as the Doping Effect over Cu/Ce Based Catalyst for Carbon Monoxide Preferential Oxidation Jichang Lu, Jing Wang, Zou Qin, Dedong He, Liming Zhang, Zhizhi Xu, Sufang He, and Yongming Luo ACS Catal., Just Accepted Manuscript • Publication Date (Web): 24 Jan 2019 Downloaded from http://pubs.acs.org on January 24, 2019

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ACS Catalysis

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Submitted to ACS Catalysis for publication

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Title:

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Unravelling the Nature of the Active Species as well as the Doping Effect over

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Cu/Ce Based Catalyst for Carbon Monoxide Preferential Oxidation

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Jichang Lu,† Jing Wang,†,‡ Zou Qin,† Dedong He,† Liming Zhang,† Zhizhi Xu,† Sufang

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He,§ and Yongming Luo†,*

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Faculty of Environmental Science and Engineering, Kunming University of Science

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and Technology, Kunming 650500, P. R. China

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Hengyang 421001, P. R. China

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§

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Technology, Kunming 650093, P. R. China

College of Life Science and Environment, Research Hengyang Normal University,

Research Center for Analysis and Measurement, Kunming University of Science and

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ABSTRACT: The active sites of a mixed Cu/Ce material and the doping effect of

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typical element (iron, Fe) on the active species and the catalytic behavior of Cu/Ce for

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CO preferential oxidation in rich H2 (CO-PROX) were investigated by in-situ diffuse

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reflectance infrared fourier transform spectroscopy (DRIFTS), in-situ oxygen storage

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capacity measurement (OSC) combing with designed temperature-programmed

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reduction (TPR), along with Raman, X-ray photoelectron spectroscopy (XPS), X-ray

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diffraction (XRD) and temperature-programmed desorption/reduction of CO

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(CO-TPD/TPR). These results showed that two kinds of surface active center were

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involved in the CuCe and Fe doped CuCe systems, i.e., Cu+ as adsorption sites for the

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chemisorption and the activation of CO molecules, the surface reactive oxygen (the

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highly dispersed oxygen and surface lattice oxygen) that directly participated in the

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whole CO oxidation process. The addition of Fe into CuCe sample resulted in the

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incorporation of Fe into CeO2 lattice forming Fe-O-Ce structure and generated more

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oxygen vacancies, which not only enhanced the interaction between Cu and Ce to

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form more Cu+ absorption sites, but also trapped the gas-phase oxygen and promoted

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the release of subsurface lattice oxygen to supply more reactive oxygen. Thus, the

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turnover frequency (TOF) value was increased from 3.62×10-2 s-1 for CuCe to

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4.50×10-2 s-1 for Fe-doped CuCe. Moreover, with the enhancement of the lattice

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oxygen migration combining with the promotional role of Fe on the water gas shift

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(WGS), the capacity of the resistance to CO2 and H2O was enhanced for Fe-doping

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CuCe, and the corresponding stability time was largely prolonged from 170 h to 400 h,

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in the coexistence of CO2 and H2O. 2 ACS Paragon Plus Environment

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Keywords: CO-PROX, CuO-CeO2, active species, promotional role of Fe, stability.

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1. INTRODUCTION

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In the new energy scenario, with the increasing interest on the development of more

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clean energy with environmentally friendly and high-efficiency ways, proton

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exchange membrane fuel cells (PEMFCs) are considered as a promising source for

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energy in the future due to the advantages of the efficient, combustion-less and

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virtually pollution free.1 Hydrogen suitable to feed PEMFCs is normally generated by

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alcohols or hydrocarbons steam reforming followed by water gas shift reaction

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(WGSR).2 However, the gas stream obtained still contains a substantial level of CO

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(about 1%) which must be further reduced to 10 ppm in order to avoid poisoning of

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the platinum anode catalysts.3-5 The preferential oxidation of CO (CO-PROX) is

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deemed as a promising and potential solution due to its economic, practical and

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efficient characteristics for purifying H2-rich gases.3,6,7

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In general, two kinds of CO-PROX catalysts are mainly involved, i.e., supported

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noble metal materials and CuO-CeO2 based catalysts. Noble metal materials are one

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kind of catalysts with high-performance for CO-PROX, but they suffer from such

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obstacles as the high in price and the limitation in resource as well as low selectively

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at the high temperature.8-10 CuO-CeO2 is the other kind of the most researched

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catalytic system for the elimination of CO, which alternatives to noble metal catalytic

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systems for the best compromise between cost, activity, selectivity and thermally

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stability.6,11-14 The high catalytic activity of Cu/Ce catalysts is mainly assigned to the

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synergistic effect of copper and cerium oxides.15-18 It is known that CeO2 as the

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typical and promising support for various oxidation reactions is due to the following 4 ACS Paragon Plus Environment

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outstanding characteristics, one is the prominent redox ability of Ce4+/Ce3+ that can

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create the oxygen vacancies and induce the changes in the electron properties of

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active Cu species, and the other is the presence of abundant surface oxygen species,

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which usually involved in the oxidation reactions. Meanwhile, Cu species presented

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as Cu2+, Cu+, Cu0 over CeO2 surface possesses the well redox ability, and the

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synergistic interaction between Cu and Ce oxides enables Cuδ+ species to become the

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active adsorption sites for CO-PROX. However, since there are various kind of

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oxidized Cu species presented in the CuCe based sample owing to the

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above-mentioned features, for instance, CuOx clusters, bulk CuO, Cu2+ into CeO2

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lattice, Cu3+ and Cu-[Ox]-Ce structure, the surface redox properties of CuCe sample is

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usually complex. The origin of the catalytic activity and the relevant active center

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over CuCe catalysts for CO-PROX remains an open question in the reported literature.

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Some authors generally considered that the highly dispersed CuOx species is the

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catalytically active center for both CO-PROX and CO oxidation via the specific

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pretreatment (acid/base) for removing highly dispersed CuOx or eliminating the

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Cu-[Ox]-Ce structure.19-22 Strongly bound Cu-[Ox]-Ce layers was proved to promote

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the catalytic activity of CuCe for CO-PROX via providing the supply role.23-25

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Further, the specific Cu ions species was proposed and proved to be the active sites

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for CO-PROX. The researchers found by the DRIFTS spectra with the aid of parallel

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time-resolved X-ray diffraction (XRD) measurements under operando conditions that

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interfacial Cu+ species stabilized via the interaction between Cu and Ce oxides

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exhibited a strong correlation with the CO catalytic performance.26,27 Through the 5 ACS Paragon Plus Environment

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characterization of Fourier transformed extended X-ray absorption fine structure

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(EXAFS) spectra in the anaerobic process, the reduction of Cu2+ species into Cu1+ via

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the elimination of the first oxygen of Cu2+ was also demonstrated to make an

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important contribution to the CO-PROX reaction.28,29 Furthermore, recent research on

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the CO oxidation confirmed through X-ray absorption spectroscopy together with

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Density functional calculations that surface-substituted CuxCe1-xO2-y phase with the

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stabilization of Cu3+ and Cu2+ into host CeO2 lattice was the active phase and Cu3+

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was implicated in the mechanism for CO oxidation over Cu/Ce catalysts.30,31 It is not

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surprising because the heterogeneous catalysis is totally a complex processes, even for

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the relatively simple reactions system, which results in the fact that the catalytic

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activity is not only limited by the difference in the adsorption properties of CO over

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different Cuδ+ species, but also depends on the surface redox chemistry, the active

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oxygen properties, and oxygen vacancies and so on. In view of those, the

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understanding of the roles these Cu ions play in the reaction of CO-PROX (specific

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catalytic active center) over CuO-CeO2 catalysts is still in progress. And more notably,

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little attention has been extensively paid to the significance of the active oxygen

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species on the reaction process of CO-PROX.26,32

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More importantly, any adjustment or modification in nanoscale via the doping of

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different types of additives or the preparation with different methods could evoke the

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unexpected variation in the catalytic behavior.33 As an typical promoter, Fe oxides

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has the high oxygen storage capacity as similar to CeO2. It should be noted that Fe

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itself also possesses high redox ability as well as the lower redox potential of 6 ACS Paragon Plus Environment

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Fe2+/Fe3+ (0.77 V) than that of Ce3+/Ce4+ (1.61 V),34 thus the interaction between

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Fe2+/Fe3+, Cu2+/Cu+, and Ce3+/Ce4+ makes the changes in the structural and electronic

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properties to be more complicated. Thus, Fe species is selected as the model additives

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to investigate the doping effect on the active center over CuCe sample for CO-PROX.

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Although large number of researches focused on the research of the catalytic

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properties over Cu/Ce catalysts, the in-depth insight into the catalytic behavior for the

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modification of Cu/Ce catalysts by iron (Fe) species in the reaction process of

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CO-PROX (especially the tolerance of H2O and CO2 as well as the stability) is

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relatively less. At present, for the selective CO oxidation, some authors found that the

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incorporation of Fe species into Cu/Ce catalysts prepared by wet impregnation and

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single-step citrate method generated better reducibility to improve the interaction

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between Cu and Ce, which leads to the higher dispersion of copper, thus posing the

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positive effect on the CO oxidation activity.35,36 Other researchers deemed that the

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introduction of Fe additives into Cu/Ce catalysts in the certain preparation procedure

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promoted the generation of additional amount of active sites related to CuO due to the

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electron-ion interactions, which improved the CO-PROX activity.37 However, the

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negative CO oxidation activity was reported for using CuO-CeO2 catalysts doped with

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Fe species when the co-precipitated method was applied.38 They deemed that the

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reversible desorption of absorbed CO was not beneficial to the selective CO oxidation

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via the characterization of in situ DRIFTS and XPS techniques. Moreover, in the field

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of soot combustion,39,40

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chemical-looping reforming,41 the water gas shift (WGS) reaction,42 Fe species was

selective catalytic reduction of NH3 with NO,34

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extensively applied to modify the redox property of pure CeO2 catalysts, and they

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found that the electronic inductive effect between Fe3+ and Ce4+ might enhance the

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redox properties for various catalytic activity of above reactions, sometimes involving

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the generation of Fe-O-Ce structure when prepared by surfactant-assisted and

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coprecipitation method.34,40 In a word, the modification of Fe additive into CuCe

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sample prepared by the different methods could largely give rise to the change in the

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catalytic behaviors. Therefore, the investigation of the doping influence of Fe additive

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on the structure, the catalytic active sites and the catalytic behavior (the tolerance of

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H2O and CO2 as well as the stability) of Cu/Ce catalyst system as well as the catalytic

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active species over Fe doping CuCe catalysts for CO-PROX are of great necessity.

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In our previous literature, the different ratio of Fe/Cu and the different Fe

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precursors were selected to be doped on the CuO-Ce0.8Zr0.2O2 materials for

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CO-PROX.43 In this work, simplified CuO-CeO2 and Fe doped CuO-CeO2 materials

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were prepared by the simple and solvent-free route of combustion synthesis. With the

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aid of designed in-situ TPR and the CO pulsing technique as well as in-situ DRIFTS,

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the catalytic active center for CO-PROX over CuCe and CuCe-Fe were illuminated

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from

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composition-structure-activity-stability relationships for the introduction of Fe into

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CuCe sample were well understood. The long-term stability of about 400 h was

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obtained for Fe doped CuCe sample in the presence of H2O and CO2, which was twice

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as stability as CuCe sample. This results can provide insights into understanding the

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active sites over doped CuO-CeO2 based materials for CO-PROX and give guidelines

the

point

of

the

principle

of

heterogeneous

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for the practical applications.

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2. MATERIALS AND METHODS

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2.1. Catalyst Preparation. CuO-CeO2 catalyst was synthesized with a solvent-free

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combustion synthesis (SFCS) method. The method was briefly depicted in the

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following. Firstly, the calculated amount of Copper nitrate hydrate (Cu(NO3)2·3H2O,

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AR), Cerium(III) nitrate hexahydrate (Ce(NO3)3·6H2O, AR) and Carbamide

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(CO(NH2)2, AR) were added into an agate mortar without additional water, and then

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ground completely for 10 min, where a transparent and homogeneous viscous gel was

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obtained. Subsequently, the as-obtained gel was calcined at 700 ºC for 20 min,

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denoted as CuCe, where the corresponding content of CuO was 10 wt. %. Fe-doped

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Cu/Ce sample was also prepared by mixing and grinding the Iron nitrate nonahydrate

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(Fe(NO3)3·9H2O, AR) with above-mentioned chemicals. The Fe/Cu mass ratio was

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0.025, and the subsequent procedures were the same as described by CuCe catalyst,

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denoted as CuCe-Fe.

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2.2. Conventional characterizations. XRD patterns were performed on a Rigaku

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D/max-1200 instrument equipped with Cu Kα radiation at 2θ ranges between 10 and

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90o. Peak identification was conducted by the software of Jade 6. Transmission

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Electron Microscopy (TEM) was performed by using a Tecnai G2 TF30 S-Twin

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microscope operated with an accelerating voltage of 300 kV. Nitrogen sorption

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isotherms were determined on a V-Sorb 2800P instrument at 77 K. Before

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measurement, the samples were degassed at 200 ºC under vacuum for 3 h. X-ray

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photoelectron spectroscopy (XPS) was performed on a PHI 5000 VersaProbe II with 9 ACS Paragon Plus Environment

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non-monochromatic Al Kα radiation (1486.6 eV) as the excitation X-ray source. The

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chemical states and the corresponding surface element compositions of all the samples

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were determined by the Casa XPS software. The charge calibration was applied by

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setting the main C 1s peak at 284.6 eV. Raman spectra were detected by using a Via

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Reflex Confocal Raman Microscope with a laser (514 nm) working at 5 mV power.

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The common experiments of hydrogen temperature programmed reduction (H2-TPR)

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were generally carried out in a catalyst bed with a quartz tube reactor equiped with a

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thermal conductivity detector (TCD). Before each measurement, the prepared samples

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were pretreated in pure O2 at 400 °C for 30 min. 100 mg of the pretreated samples

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were heated in a gas flow (30 cm3/min) of 10% H2 in Ar from 50 to 400 ºC (800 ºC) at

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a ramp rate of 10 ºC/min.

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Oxygen storage capacity (OSC) of samples was determined by the CO pulsing

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technique. The micro-reactor equipped with the six-way gas-sampling valve with a

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measuring ring (50 μmol/L) was used to introduce the quantitative gas sample. Before

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testing, the sample (50 mg, 100-120 mesh) was pretreated at 550 oC for 60 min in the

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flow of 20% (v/v)O2/He with the velocity of 30 mL/min. Then, the samples were

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cooled down to the desired temperature (150 oC and 200 oC, respectively) under the

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flow gas of high-purity helium (He). Afterwards, the pure CO gas sample (99.99%)

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was introduced every 5 min into the micro-reactor until reaching the plateau. The

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detection of CO and CO2 was performed by the on-line detector equipped with a

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high-sensitivity of TCD and a flame ionization detector (FID) together with a

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methanation reactor. To verify the presence of the deposited carbon over samples 10 ACS Paragon Plus Environment

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surface, the CO pulse was introduced at 140 oC over CuCe and CuCe-Fe samples (100

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mg) until the amount of CO reaches the steady state. The samples were denoted as

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pulsed CuCe and pulsed CuCe-Fe, respectively.

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Temperature programmed desorption of CO (CO-TPD) was performed on the same

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apparatus with TCD detector. 100 mg of samples (100-120 mesh) were firstly

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pretreated under the 20% O2/He at 400 oC for 1 h. After that, the temperature was

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cooled down to 30 oC, and the flow gas was switched to 100% CO (30 ml/min).

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Afterwards, the pretreated samples were saturated using pure CO at 30 oC for 30 min,

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then were purged with He (30 mL/min) for 60 min to remove the physisorbed CO.

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The CO-TPD experiment was carried out by elevating temperature up from 30 to 300

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o

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gas of He into pure N2 to detect the product of H2 with TCD detector. 200 mg of

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samples were exposed to 10% CO/N2 at 30 oC for 30 min with a flow rate of 30

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mL/min. Then, the temperature was ramped from 30 to 300 oC at a ramp rate of 1

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o

210

valve.

C with a heating rate of 10 oC/min. CO-TPR was carried out by switching the carrier

C/min, and the gas was analyzed every 5 min assisted with a six-way gas-sampling

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Diffuse Reflectance Infrared Fourier Transform Spectroscopy (DRIFTS) was

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conducted on a Nicolet 6700 spectrophotometer equipped with an mercury cadmium

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telluride (MCT) detector with a resolution of 4 cm-1. A diffuse reflection infrared cell

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was connected to a vacuum apparatus, and was fitted with temperature controlled

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parts and a CaF2 window. Prior to the measurements, the samples were firstly

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pretreated at 300 oC for 30 min under the atmosphere of 10% O2/Ar. Background 11 ACS Paragon Plus Environment

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spectra were subtracted at the target temperature under the high-purity Ar atmosphere

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by averaging 32 scans. For every measurement, DRIFTS spectra were obtained for

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samples under the feed gas of 1% CO/1% O2/50% H2/He and then recorded from 30

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to 210 oC by every 20 oC. To investigate the deactivation reason caused by the

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addition of H2O, small amount of H2O was introduced to system via carried by the

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reaction gas stream through bubbling, in-situ DRIFTS spectra were performed over

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CuCe and FeCuCe catalysts from 90 oC to 210 oC by every 20 oC.

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2.3. Designed characterizations. Four kinds of designed H2-TPR over CuCe and

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CuCe-Fe samples were carried out and classified as follows: 1) the elimination of

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surface oxygen species (β peak-TPR). To effectively eliminate α peak corresponding

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to the highly dispersed CuOx species and avoid the thermal effect, the ramp rate was

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decreased from 10 to 5 ºC/min, the samples (100 mg) were firstly pretreated with 10%

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H2/Ar (v/v, 30mL/min) at 150 oC for 0, 1, 2, 3, 5 min, respectively, denoted as P150-0,

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P150-1, P150-2, P150-3, P150-5. Then, the gas mixtures was switched into the

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atmosphere of high-purity He followed by decreasing the pretreatment temperature

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from 150 oC to the room temperature. These H2-TPR measurement were finally

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conducted with the procedure as same as above-mentioned TPR process. The optimal

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pretreatment conditions were found at 150 oC by 2 min for CuCe (P150-2) and by 1

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min for CuCe-Fe sample (P150-1); 2) the in-situ characterization of the active oxygen

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species of above pretreated sample (pretreatment-OSC). CuCe and CuCe-Fe samples

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were firstly pretreated using 10% H2/Ar at 150 oC for 2 min and for 1 min,

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respectively. Then, the corresponding temperature was decreasing to 30 oC and the 12 ACS Paragon Plus Environment

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flow gas was switched to the flow of He to completely remove the H2/Ar gas.

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Subsequently, the OSC measurement of pretreated samples was performed at the

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temperature of 200 oC. 3) the ex-situ characterization of the oxygen migration

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(Activity-TPR). Firstly, the samples (100 mg) were pretreated by 10% H2/Ar to

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eliminate α peak as did in the Section 1). Then, the normal catalytic activity tests of

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pretreated samples were performed under the feed gas of 1% CO/1% O2/50% H2/He

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(80 mL/min) from 60 to 160 oC (P150-R160) and 60 to 220 oC (P150-R220),

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respectively. Afterwards, after the temperature was declined under the high-purity He,

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the spent CuCe and CuCe-Fe samples were rapidly transferred to conduct the H2-TPR

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measurement,

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P150-1-R220), respectively. 4) the in-situ characterization of the oxygen migration

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(OSC-TPR). Firstly, the samples were pretreated under the flow of 20% O2/He (30

251

mL/min) at 550 oC for 60 min. After switching into the high-purity He and decreasing

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the temperature to 200 oC. The OSC measurement of samples was carried out at 200

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o

254

consume the surface initial active oxygen. Then, the temperature was declined to 50

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o

256

to the 10% H2/Ar, and the in-situ TPR experiments were conducted from 50 to 400 oC

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with a ramping rate of 10 oC/min.

denoted

as

(P150-2-R160,

P150-2-R220) and

(P150-1-R160,

C where only one CO pulse with a measuring ring of 50 μmol/L was introduced to

C under the atmosphere of high-purity He. Subsequently, the flow gas was switched

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2.4. Catalytic activity tests. The selective oxidation of CO in H2-rich gas was

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conducted on a tubular reactor at the temperature between 60-220 ºC with the

260

atmospheric pressure. 300 mg of catalyst (sieve fraction, 40-60 mesh) was placed in a 13 ACS Paragon Plus Environment

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quartz tubular reactor. The synthetic gas (containing 1% CO, 1% O2, 50% H2 in

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volume and He as balance gas) was introduced to fix a total flow velocity of 80

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mL/min. To investigate the influence of CO2 and H2O on the catalytic activity and

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stability, the experiments for the resistance to CO2 and H2O over two samples were

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performed by introducing 15% CO2 and 10% H2O into the feed gas to arrive the total

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flow rate of 80 mL/min. The stability tests were conducted at 160 oC for CuCe and

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155 oC for FeCuCe with the same other conditions. Moreover, the independent WGS

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reaction tests were performed over CuCe and FeCuCe samples at the temperature

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range of 120-260 oC using the mixtures of 1% CO, 10% H2O, and pure N2 as balance

270

(80 mL/min). The WGS reactions over pulsed CuCe and CuCe-Fe samples (100 mg,

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the carbon species was formed) were also conducted using the mixtures of 10% H2O

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and pure N2 as balance with the same flow rate.

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In order to research the essential role of the different surface active oxygen species

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and the oxygen mobility, two kinds of specific activity tests were also designed. For

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the first activity test, 100 mg of fresh CuCe and CuCe-Fe samples were performed

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under the same feed gas composition with the unchanged flow rate. With respect to

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the second activity test, 100 mg of fresh CuCe and CuCe-Fe samples were firstly

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pretreated under the flow gas of 10% H2/Ar at 150 oC for 2 min and 1 min,

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respectively, in order to remove the α peak corresponding to the highly dispersed

280

oxygen in CuOx species. Then, the flow gas was switched into the atmosphere of

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high-purity He, and the temperature was declined to 60 oC. Afterwards, the mixture

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gas (1% CO/1% O2/50% H2/He) was introduced to conduct the other normal activity 14 ACS Paragon Plus Environment

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283

ACS Catalysis

test.

284

Every activity tests were conducted when the steady state was arrived at the

285

corresponding temperature, and were ran at least six times on each temperature and

286

then took the average. The inlet and outlet streams of various reactions were

287

determined by using an on-line gas chromatography (GC), which was equipped with a

288

TCD detector with different carrier gas depending on the detected products. CO

289

conversion (%) and CO2 selectivity (%) were calculated according to CO and O2

290

consumption, as described below:

291

CO conversion%  [CO]in - [CO]out 100 [CO]in

292

CO 2 selectivit y %   0.5  [CO] in - [CO] out   100 [O 2 ]in - [O 2 ]out 

(1) (2)

293

To calculate the the turnover frequency (TOF) of samples, the internal/external

294

diffusion effects could be excluded by making a Weisz-Prater analysis and a Mears

295

analysis. On the basis of the assumption of hemispheric model over CuCe based

296

catalysts, TOF values of catalysts for CO-PROX were calculated according to the

297

following equations:44,45

298

TOF (s -1 )  FCO  xCO  mcat /( DCuO  nCuO )

299

where mcat is the weight of catalyst (g), FCO is the flow velocity of feed gas (mol s-1),

300

χCO is the CO conversion, which was kept below 10% at 80 oC by increasing the flow

301

rate assisted by decreasing the amount of catalysts, nCuO is the total molar amount of

302

CuO (mol), DCuO is the dispersion of CuO, which was calculated based on the ratio of

303

Cu/Ce from XPS results.

304

3. RESULTS AND DISCUSSION

1

(3)

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305

3.1. Catalytic activities of CuCe based materials. Fig. 1 displays the conversion

306

of CO and the selectivity of CO2 during the process of CO-PROX over the CuCe and

307

CuCe-Fe samples. From Fig. 1A, CuCe-Fe catalyst exhibits the higher catalytic

308

performance than that of CuCe. The reaction temperatures T50 and T100

309

(corresponding to 50% and 100% of CO conversion) are introduced as the important

310

criterion to evaluate the CO oxidation activity. It can be seen that the reaction

311

temperature for T50 is 69, 77 ºC, and the corresponding temperature for T100 is 99, 120

312

ºC over CuCe-Fe, CuCe, respectively. The corresponding temperature window widens

313

from 40 ºC (120-160 ºC) for CuCe to 60 ºC (100-160 ºC) for CuCe-Fe. Those results

314

indicates that the doping of Fe into CuCe catalyst promotes the CO oxidation activity,

315

especially for the low temperature activity. The turnover frequency (TOF) and the

316

reaction rate are calculated to estimate the CO oxidation activity, and the results of

317

CuCe-Fe and CuCe samples are complied in Table 1. It is found that the incorporation

318

of Fe increases the corresponding TOF value (and the reaction rate) from 3.62×10-2 s-1

319

(1.13×10-6 mol·g-1·s-1) to 4.50×10-2 s-1 (1.60×10-6 mol·g-1·s-1), testifying the

320

promotional role of Fe species on the catalytic activity of CuCe catalyst for

321

CO-PROX. With further rising the temperature from 160 to 220 oC, the conversion of

322

CO for all the catalysts declines to the different degree due to the rapid oxygen

323

consumption rate at the high temperature as well as the occurrence of hydrogen

324

oxidation. The selectivities of CO2 for two catalysts are shown in Fig. 1B. As seen,

325

with increasing the reaction temperature, the selectivity of CO2 for the catalysts

326

gradually decreases, probably owing to the possible competing reaction for converting 16 ACS Paragon Plus Environment

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327

H2 and O2 to H2O. It can be concluded that the addition of Fe have evidential

328

promotional effect on the catalytic activity of CuCe for CO-PROX. Therefore, the

329

following characterizations are used to investigate the promotional effect of Fe

330

additive on the structural, textural, and electronic properties of CuCe catalyst for

331

CO-PROX.

332

3.2. Structural, textural and electronic properties of CuCe and CuCeFe

333

materials. The structural property of catalyst is studied by X-ray diffraction (XRD).

334

The corresponding patterns of CuCe and CuCe-Fe samples are shown in Fig. 2A. The

335

main crystallite size and the lattice parameter of CeO2 particles over two catalysts are

336

calculated and listed in Table 1. The small and weak diffraction peaks at 35.2 and

337

38.5o attributed to copper oxides (CuOx) are visible for CuCe sample, indicating that

338

large number of CuOx species is aggregated on the surface to be detected by XRD and

339

a small portion of CuOx is incorporated into CeO2 lattice (the lower unit cell

340

parameter for CuCe (0.54126 nm) than that for pure CeO2 (0.54131 nm)). However,

341

the characteristic peaks of CuOx are not discovered in the XRD pattern of CuCe-Fe

342

catalyst. Two reasons could be probably considered to interpret this phenomenon, one

343

can expect that the doping of Fe species might result in the incorporation of more

344

CuOx species into CeO2 lattice forming the solid solution. The other can expect that

345

the incorporation of Fe species into CeO2 lattice by replacing Cu species is presented,

346

which facilitates the highly redispersion of more CuOx species over the CeO2 surface,

347

forming the stronger interacting of Cu with Ce.46,47 Compared with the diffraction

348

diagram of CuCe, the (111) peak shifts to a higher location for the CuCe-Fe (Fig.2, 17 ACS Paragon Plus Environment

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349

inset). Meanwhile, the unit cell parameters calculated were 0.54126 for CuCe and

350

0.54016 nm for CuCe-Fe sample, respectively. This lattice shrinkage and the shift of

351

the position of the (111) peak demonstrate the consequence of the incorporation of

352

iron or more copper species into the CeO2 lattice, due to the smaller Fe (II 0.075 nm;

353

III 0.064 nm) and Cu(II 0.073 nm) ionic radius compared to that of Ce(IV 0.097

354

nm).22 This incorporation effect might result in the formation of the distortion in the

355

cubic fluorite structure of CeO2, thus generating more defective sites.48 The ratio of

356

Cu/Ce evaluated by the measurement of XPS (Fig.2) is used to characterize the

357

distribution state of Cu species over CeO2. The corresponding result is summarized in

358

Table 1. The Cu/Ce atomic ratios are calculated to be 0.293 and 0.336 for CuCe and

359

CuCe-Fe, respectively. The higher value for CuCe-Fe indicates the generation of more

360

amount of surface dispersed Cu oxide species, demonstrating that the addition of Fe

361

species gives rise to the incorporation of Fe into CeO2 lattice, which leads to the

362

migration and redistribution of partial Cu oxide species from CeO2 bulk lattice to

363

surface and interface (as evidenced by the higher intensity of α and β TPR peaks).

364

Moreover, the main reflections (2θ=28.5, 33.1, 47.5, 56.3, 59.1, 69.4, 76.7 and

365

79.1o) corresponding to the fluorite-type cubic structure of CeO2 with diffractions of

366

(111), (200), (220), (311), (222), (400), (331) and (420) planes (ICDD 34-0394) are

367

observed for both CuCe and CuCe-Fe samples.49-51 It is seen Fig. 2A (insert) that the

368

characteristic peaks of CeO2 over CuCe-Fe are much broader and have a lower

369

intensity than those of CuCe, suggesting the formation of smaller-sized CeO2

370

crystallites. As seen from Table 1, the corresponding crystallite size is calculated to be 18 ACS Paragon Plus Environment

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371

9.6 nm for CuCe-Fe, smaller than that of CuCe (11.0 nm), suggesting the addition of

372

Fe has a certain influence on the crystallite size of CeO2, due to the fact that the

373

distortion of CeO2 fluorite-type cubic phase caused by Fe additive inhibits the

374

excessive growth of particles clusters. The textural properties of the CuCe and

375

CuCe-Fe catalysts were listed in Table 1. The specific surface area (SBET) of CuCe-Fe

376

sample is higher than that of CuCe, suggesting that the modification of Fe causes an

377

increase in the surface area of the resultant catalyst (CuCe-Fe), which is due to the

378

smaller crystallite size of CuCe-Fe. TEM characterization is used to analyse the

379

morphological feature of CuCe and CuCe-Fe, as shown in Fig. S1-A and Fig. S1-B,

380

and the particles size distribution is shown in the corresponding inserts. TEM images

381

display the existence of near-spherical, agglomerated particles in two samples. The

382

average sizes are calculated to be 9.7 nm for CuCe-Fe and 10.7 nm for CuCe sample,

383

respectively, consistent with the XRD result. Furthermore, CuCe-Fe sample possesses

384

the relative narrow and uniform particles size distribution compared to that CuCe

385

sample, demonstrating that the addition of Fe improves the dispersion of CuCe

386

sample.

387

The XPS spectrum is employed to acquire further information about the surface

388

composition and the oxidation/valence state of Ce, Fe and CuOx species. Fig. 2B, 2C

389

and 2D display the Ce 3d, Fe 2p and Cu 2p signal of CuCe and CuCe-Fe samples,

390

respectively. As shown in Fig. 2B, the Ce 3d XPS spectra of CuCe and CuCe-Fe

391

samples are complex and contain four spin-orbit doublets. Three doublets marked as v

392

(ca. 882.2 eV) - u (ca. 900.7 eV), vˊˊ (ca. 888.6 eV) - uˊˊ (ca. 907.6 eV) and vˊˊˊ (ca. 19 ACS Paragon Plus Environment

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393

898.3 eV) - uˊˊˊ (ca. 916.5 eV) are attributed to the presence of Ce4+ species. Letters v

394

and u refer to the 3d5/2 and 3d3/2 spin-orbit components, respectively. Meanwhile, for a

395

practical simplification, two components of vˊ (ca. 884.5 eV) and uˊ (ca. 903.0 eV)

396

are ascribed to the existence of Ce3+ species.52 Those results indicates Ce3+ and Ce4+

397

species are simultaneously presented in the CuCe and CuCe-Fe samples. For Fe

398

species, as shown in the Fig. 2C, the broaden and asymmetric peaks suggests that both

399

Fe2+ and Fe3+ co-exist in the CuCe-Fe sample. The binding energy at 710.0 eV for Fe

400

2p3/2 sates followed with a satellite around 716.3 eV is attributed to the presence of

401

Fe2+ species, another peak around 713.4 eV with a corresponding statellite at 719.4 eV

402

is assigned to the Fe3+ species.53,54 This Fe3+ species is found to be shifted to high

403

value compared to that reported for Fe3+ around 712-713 eV in the literature,53,54

404

suggesting the change in the electron environment around Fe species. This is possibly

405

due to the fact that the incorporation of Fe species into CeO2 lattice enhances the

406

interaction between Fe and Ce leading to the formation of Fe-O-Ce structure.34,39

407

Furthermore, the intensity ratios of the satellite to main peak of Fe 2p3/2 are calculated

408

to be 1.70 for Fe2+ and 4.18 for Fe3+ species, respectively, which is higher than that

409

reported in literature (blew 1).55 As inferred from the literature,55,56 according to

410

Harrison’s relation, the intensity of the satellite peak of iron oxides is proportional to

411

the value of 1-1/R7.0, where R is the interatomic distance of Fe-O bond (Section 2 of

412

supporting information (SI)). Since the incorporation of Fe species into CeO2 lattice

413

leads to the increment in the length of Fe-O bond due to the difference of ionic radius

414

between Fe2+ (0.075 nm), Fe3+ (0.064 nm) and Ce3+ (0.097 nm), the satellite intensities 20 ACS Paragon Plus Environment

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ACS Catalysis

415

thus significantly increase, which, in turn, proves the formation of Fe-O-Ce structure.

416

From Fig. 2D, a main and asymmetric Cu 2p3/2 peak at around 930-936 eV is found

417

for CuCe sample, which can be decomposed in two contributions centered at 932.2 eV

418

and 933.4 eV, generally associated with the Cu+ and Cu2+ species, respectively.57-59

419

This suggests that the coexistence of both Cu2+ and reduced Cu+ species in the CuCe

420

sample where CuOx species is mainly presented in the form of reduced Cu+ species.

421

The almost inexistence of satellite peaks that is located at 938-946 eV for Cu2+ seems

422

to confirm the existence of main Cu+ species. The intensity ratio of the shake-up peak

423

to the principal peak (Isat/Ipp) is used to characterize the valence state of Cu species. It

424

is generally accepted that the value below 0.57 is corresponding to Cu+ species and

425

the higher value is assigned to Cu2+ species.22,28 The corresponding values are

426

compiled in Table 1. CuCe and CuCe-Fe samples display the ratios of 0.19 and 0.32,

427

proving the existence of Cu+ species. Cu LMM Auger spectra was performed to

428

confirm the presence of reduced Cu oxide species, as shown in the inset of Fig. 2(D).

429

It is seen that the binding energy at 569.7 eV is attributed typically to the existence of

430

Cu+ species, followed by two other peaks representing different Auger transitions

431

involving Cu+, and no distinct signal assigned to Cu0 species at about 568 eV is

432

observed, demonstrating the presence of the main valence state of reduced Cu species

433

as Cu+.60,61 The reduced copper species on the sample may be originated from the

434

strong interaction between CeO2 and the active Cu components,62 because of the

435

existence of the redox balance (Ce3+ + Cu2+ ↔ Ce4+ + Cu1+),32 as confirmed by redox

436

Ce4+/Ce3+ in the Ce 3p XPS. After the addition of Fe species, the redox properties of 21 ACS Paragon Plus Environment

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437

CuCe species has changed largely. It can be seen that the Cu 2p3/2 peak are broadened

438

and more Cu2+ ion are formed, possibly due to the additional redox equilibrium (Fe3+

439

+ Cu+ ↔ Fe2+ + Cu2+). The structural and electronic impact of Fe additive on the

440

CuCe sample are further demonstrated by Raman and O 1s XPS analysis.

441

Raman spectroscopy is a useful tool to characterize the vibration of metal-oxygen

442

bond, the defects of nanophase as well as their surrounding chemical environment. It

443

has proven that the doping phenomenon caused by electrons was associated with the

444

change in the position of Raman band.63,64 Therefore, the doping effect of Fe species

445

on the CuCe sample is characterized by Raman analysis, and the corresponding

446

spectra of CuCe and CuCe-Fe catalysts are shown in Fig. 3A. The CuCe sample

447

displays an intense band at about 463 cm-1, attributed to the Raman active F2g

448

vibrational mode for oxygen atoms around the cerium ions, which is an evidence for

449

the typical cubic fluorite structure CeO2.64,65 The broad peak around 599 cm-1 can be

450

linked to the oxygen vacancies/defects within the lattice of CeO2.66,67 When the Fe

451

species is added, the intense band is observed to be shifted slightly toward the low

452

frequency at 459 cm-1. This phenomenon is attributed to the fact that the generation of

453

Fe-O-Ce structure gives rise to the change in the metal-oxygen bond lengths owing to

454

the difference in the atomic radius between Fe3+ and Ce4+/Ce3+, forming the lattice

455

distortions.34,64 The increase of lattice distortions indicates the formation of more

456

oxygen vacancies. The oxygen vacancies concentration is calculated with the nature

457

of a major peak at 459 cm-1 by the spatial correlation model,64,68,69 as shown in

458

Section 3 of SI. The defect concentration of CuCe and CuCe-Fe is calculated to be 22 ACS Paragon Plus Environment

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ACS Catalysis

459

3.84 × 1021 cm-3 and 4.43 × 1021 cm-3, respectively (listed in Table 1), suggesting that

460

the addition of Fe species increases the amount of oxygen vacancies, which also

461

proves the Fe doping into CeO2 lattice to generate Fe-O-Ce structure. Moreover, the

462

absence of any Raman band for Fe species at the low Raman band (217, 296, 398 cm-1)

463

also confirms this point.70 The further evidence for Fe doping into CeO2 lattice to

464

form Fe-O-Ce coordination could be achieved by looking at the binding energy of O

465

1s. Fig. 3B presents a comparison of O 1s signal of CuCe and CuCe-Fe samples. The

466

main binding energy peak centered at 528.9 eV and a shoulder peak around 531.3 eV

467

are observed for CuCe sample. The main peak is ascribed to the lattice oxygen (OI),

468

and the shoulder peak reflects chemisorbed oxygen (OII) in carbonates and hydroxyl

469

groups.71,72 Upon Fe doping, it can be seen that the main peak shifts to a higher value

470

at 529.3 eV, which could be associated with the transformation of O chemical

471

environment from original Ce-O-Ce to Fe-O-Ce coordination (Fe containing

472

CeO2-like solid solution).66,73 In a word, the structural model of CuCe as well as the

473

promotional effect of Fe additives on the structural property of CuCe are well

474

illuminated in Scheme 1.

475

3.3. Fe promotional effect on the oxygen mobility. The structure-activity

476

relationship over CuCe materials has been previously reported and discussed

477

extensively by large amount of researchers.19-31 Although the presence of various

478

viewpoints on the cognition of the active species over CuCe catalysts, all these

479

researches provide insight into the possible critical factors affecting the final catalytic

480

performances from different views via different methods and techniques. Thus, we 23 ACS Paragon Plus Environment

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481

would take the active sites of CuCe based catalysts into account from the view of the

482

principle of heterogeneous catalysis. In general, the catalytic reaction process

483

commonly involved, firstly, the adsorption and the activation of reactant molecules,

484

then the reaction between reactants over the active sites, as well as the desorption of

485

products. As for CO-PROX (including CO oxidation and H2 oxidation) and CO

486

oxidation, it was generally accepted that CO oxidation started with the chemisorption

487

and the activation of CO molecules over Cu ions active sites, then the reaction

488

between Cu ions-CO species and surface active oxygen species over Cu-Ce oxides

489

formed CO2 and leaved an oxygen vacancy, finally the formed oxygen vacancies were

490

replenished by gas-phase oxygen, which was known to be a Mars-van Krevelen

491

mechanism.27,74-77 Therefore, the catalytic activity of CuCe based materials toward

492

CO oxidation in H2-rich is speculated to be largely affected by two significant factors,

493

one is the surface active oxygen species, and the other is the Cu ions active sites.

494

Liable/reducible oxygen species is usually involved in the oxidation reactions over

495

oxide catalysts.74,75 In general, when an reactant is oxidized at the active surface, the

496

oxidant is usually a surface lattice oxygen atom instead of gas-phase oxygen, then

497

creating a surface oxygen vacancy.78,79 The production of oxygen vacancies plays an

498

important role in the formation of mobile oxygen species. As is known that the

499

amount of oxygen vacancies can be estimated by several parameters, such as the ratio

500

of Ce3+/(Ce3++Ce4+) from Ce 3d XPS,80 the value of A599/A600 for Raman,81 and the

501

ratio of OII/(OI+OII) from O 1s XPS.82 According to the preceding result, these values

502

are calculated to be 27.56, 0.67, 51.65 for CuCe-Fe sample, which is totally larger 24 ACS Paragon Plus Environment

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ACS Catalysis

503

than that of 22.0, 0.60, 36.33, respectively, for CuCe sample. This would demonstrate

504

that the addition of Fe into CuCe sample leads to the generation of more amount of

505

oxygen vacancies. The presence of oxygen vacancies possibly enhances the activity of

506

oxygen (which can be evaluated by the oxygen mobility ability). The oxygen mobility

507

promoted by Fe additive is further demonstrated by designed H2-TPR and OSC

508

characterizations.

509

Temperature-programmed reduction by hydrogen (H2-TPR) is actually used to

510

characterize the presence of reducible/active oxygen species due to the consumption

511

of oxygen by H2 to produce water in the TPR process. The common H2-TPR profiles

512

of the CuCe and CuCe-Fe catalysts are shown in Figure 4A. For CuCe sample,

513

H2-TPR profile show three peaks at 161 ºC (α), around 233 ºC (β), and 250 ºC (γ). It

514

is generally accepted that the small α peak could be assigned to the consumption of

515

reducible oxygen from the highly dispersed CuOx species, large β peak can be

516

ascribed to the reduction of active oxygen in the strong interaction of Cu-[Ox]-Ce (or

517

Fe-O-Ce) species, and small γ peak is attributed to the oxygen species presented in

518

bulk CuO.19,23,83 Compared to the oxygen consumption of pure CuO characterized by

519

one peak at 280-350 oC (Section 4 of SI) and between 300-400 oC in the literature,20,84

520

the decreased reduction temperature for CuCe sample indicates that the oxygen

521

species linked to Cu is activated by the interaction with CeO2. Upon the doping Fe

522

into CuCe sample, the α and β peak slightly shift to a lower temperature and the

523

corresponding H2 consumption increases from 792.6 μmol/g for CuCe to 937.9

524

μmol/g for FeCuCe, indicating that Fe additive activates the surface lattice oxygen in 25 ACS Paragon Plus Environment

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525

CeO2, promoting the oxygen migration. In other words, as before proved that Fe

526

doping into CeO2 lattice results in the creation of more oxygen vacancies, the

527

presented oxygen vacancies possibly promote the migration ability of oxygen from

528

CeO2 subsurface to surface Cu-[Ox]-Ce and from surface to the highly dispersed CuOx,

529

and thus the generation of more highly reducible oxygen species,85,86 as shown in

530

Scheme 1. The TPR peak in the higher temperature region in Fig.4A(a) supports the

531

conclusion. It is seen that after the incorporation of Fe additive, the H2 consumption

532

peak at around 400 oC corresponding to the subsurface lattice oxygen over CuO-CeO2

533

(surface lattice oxygen of CeO2) disappears, and the higher intensity of peak centered

534

around 780 oC characterized by the bulk lattice oxygen of CeO2 over Fe-CuCe (464.4

535

μmol/g) compared to CuCe sample (390.5 μmol/g) is observed, indicating that Fe

536

doping facilitates the migration of subsurface lattice oxygen as well as the release of

537

bulk lattice oxygen over CuO-CeO2.

538

It is deduced that the enhanced performance for the CO catalytic oxidation using

539

CuO-CeO2 as the catalyst depends on the ability to provide the reactive oxygen to the

540

reaction process. Thus, the roles the oxygen mobility plays in the reaction process

541

becomes even more significant. The oxygen release behavior and the oxygen mobility

542

are further characterized by the CO pulsing technique at 150 oC and 200 oC, with

543

which oxygen storage capacity (OSC) and oxygen storage complete capacity (OSCC)

544

are determined and evaluated by the production of CO2 (shown in Fig. 4B) and the

545

consumption of CO (shown in Fig. 4C). For Fig. 4B, at 150 oC, the CuCe sample

546

exhibits the low OSC vlaue of 46.4 μmol CO2/g at the first pulse with arriving the 26 ACS Paragon Plus Environment

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ACS Catalysis

547

maximum value at the fifth pulse, indicating the low oxygen mobility. While after the

548

addition of Fe the corresponding value is 94.8 μmol CO2/g at the first pulse with

549

arriving the maximum value forward to the third pulse, which provides the direct

550

evidence to indicate that Fe doping into CeO2 lattice largely facilitates the migration

551

rate between the highly dispersed oxygen, the surface lattice oxygen and the

552

subsurface lattice oxygen via oxygen vacancies.87,88 With the temperature elevating to

553

200 oC, the oxygen consumption rate obviously enhances, and the oxygen storage

554

capacity is observed to be improved by the incorporation of Fe. These results

555

demonstrate that Fe doping into CuCe sample largely enhances the ability of oxygen

556

migration without the presence of O2, as shown in scheme 1(b). The change in the CO

557

consumption shown in Fig. 4C is consistent with the production of CO2, which also

558

supports the conclusion. Moreover, an interesting phenomenon is observed for the

559

generation of CO2 with the pulsing time proceeding. It is generally speaking that the

560

production of CO2 during the pulsing process goes through one stage, i.e., the amount

561

of CO2 would generate largely at the first pulsing and keeps at a maximum value, and

562

then decrease gradually to zero. However, in our Fig. 4B, the production of CO2 goes

563

through two stages, i.e., the amount of generated CO2 keeps firstly at a low value, and

564

then arrives to a maximum value, afterwards the value reduces to zero. These volcanic

565

and inverted-volcanic curves observed in the production of CO2 and the consumption

566

of CO during the pulsing process indicates the existence of two different types of

567

reactive oxygen species over CuCe and CuCe-Fe samples. One is very highly

568

reactivity to CO and another has relative reactive activity. Combining with the TPR 27 ACS Paragon Plus Environment

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569

results, it is initially inferred that the first active oxygen is attributed to the oxygen

570

bound to the highly dispersed CuOx, and the second active oxygen is assigned to the

571

surface lattice oxygen bound to Cu-[Ox]-Ce species.

572

To prove the above assumption and further investigate the role of the different

573

types of reactive oxygen species on the activity of CO-PROX, a specific pretreatment

574

by 10 % (v/v) H2/Ar at 150 oC (for 2 min over CuCe, P150-2, and for 1 min over

575

CuCe-Fe, P150-1, respectively) is used to eliminate the oxygen bound to the highly

576

dispersed CuOx, and the corresponding TPR, OSC, and the CO oxidation activity over

577

CuCe and CuCe-Fe samples are in-situ characterized without contacting any air. And

578

the corresponding results are shown in Fig. 5A and 5B, Fig. 5C and 5D, Fig. 5E and

579

5F, respectively. In the TPR profiles (Fig. 5A and 5B), it is found that when the CuCe

580

and CuCe-Fe samples are exposed to the 10 %(v/v) H2/Ar at 150 oC for 2 min and 1

581

min, respectively, all the α peaks corresponding to the oxygen bound to the highly

582

dispersed CuOx are completely consumed, and the β peaks characterized by the

583

surface lattice oxygen bound to Cu-[Ox]-Ce species are almost unaffected. These

584

pretreated samples are then in-situ characterized by the CO pulsing processing. It is

585

seen from Fig. 5C and 5D that the volcanic and inverted-volcanic curves of CuCe and

586

CuCe-Fe samples disappear, and the amount of CO2 generates at the first pulsing with

587

a maximum value, and then decrease gradually to zero. This result provides a proof to

588

prove that the oxygen consumed at the first three CO pulsing in the Fig. 4B and 4C

589

should be related to the highly dispersed CuOx, and the oxygen consumed after the

590

three CO pulsing should be associated with Cu-[Ox]-Ce species. It seems to deduce 28 ACS Paragon Plus Environment

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ACS Catalysis

591

that the very high reactive oxygen is connected to the highly dispersed CuOx, which is

592

thought to be preferentially consumed in the CO-PROX process especially at the low

593

temperature. The catalytic activities for CO-PROX over CuCe and CuCe-Fe samples

594

evaluated in-situ after the H2 pretreatment are shown in Fig. 5E and 5F, respectively.

595

The CO oxidation activity is expected to reduce at the low temperature region over

596

CuCe catalyst, which proves that the oxygen bound to highly dispersed CuOx is

597

beneficial to improve the low-temperature CO oxidation activity. Although the CO

598

oxidation activity decreases to some extent, the dominant activity for CO-PROX is

599

not loss, which is an indicative of the importance of the surface lattice oxygen bound

600

to the Cu-[Ox]-Ce species that participate in the CO oxidation process, especially at

601

the relative high temperature region. However, when Fe species is incorporated into

602

CuCe sample, it is strange that there is no decrease in the CO oxidation activity. This

603

result seems to arrive a opposite result that the oxygen bound to highly dispersed

604

CuOx has no influence on the CO oxidation activity. To illuminate clearly this

605

phenomenon, the structural properties change induced by the incorporation of Fe

606

should be considered. As evidenced by XRD, XPS, Raman and H2-TPR that the

607

incorporation of Fe into CeO2 lattice leads to the formation of more oxygen vacancies,

608

which promotes the lattice oxygen migration rate. Thus, we assume that the identical

609

CO oxidation activity before and after the H2 pretreatment is not only due to the

610

migration of the subsurface lattice oxygen to surface lattice oxygen at the relative high

611

temperature (≥100 oC) and but also owing to the migration of gas-phase oxygen to the

612

highly dispersed oxygen during the reaction process at the relative low temperature 29 ACS Paragon Plus Environment

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613

( 300 oC).102,103 CuCe catalysts was reported to have good

788

activity for WGS at the temperature above 200 oC, while only about 5% CO 37 ACS Paragon Plus Environment

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789

conversion was obtained at the temperature blew 200 oC.104-106 If the addition of Fe

790

species into CuCe catalysts could facilitate the occurrence of WGS reaction at blew

791

200 oC, further improving the tolerance of H2O and CO2 as well as the stability of

792

catalysts, is not clear.

793

In general, WGS reaction over CuCe catalyst includes the reaction of CO with

794

surface original -OH groups of catalyst surface as well as the H2O-assisted CO

795

oxidation by the formation of surface -OH groups. Firstly, the reaction of CO with

796

surface original -OH groups of catalyst surface via the WGS type reaction (CO + -OH

797

→ CO2 + 1/2H2) is considered. Since hydrogen (H2) is a probe molecule for the

798

occurrence of WGS-type reaction, thus, CO-TPR was used to detect the presence of

799

H2, and in-situ DRIFTS is conducted to detect the formation of intermediate species.

800

The CO-TPR profiles and in-situ DRIFTS spectra on CuCe and FeCuCe samples are

801

displayed in Fig. 9(A), 9(B), 9(C). As for Fig. 9(A), it is found that the initial

802

temperature for producing H2 is 170 oC for CuCe sample, while the corresponding

803

temperature decreased to 140 oC over FeCuCe sample, suggesting the possible

804

occurrence of WGS-type reaction between surface original -OH and CO at 140 and

805

160 oC due to the promotion role of Fe additive. To investigate the effect of adsorbed

806

water on the WGS-type reaction, fresh FeCuCe was pretreated at 700 oC for 1 h in the

807

atmosphere of pure N2. After the removal of adsorbed water and partial OH groups,

808

the observed temperature increases to 190 oC over FeCuCe sample, indicating that the

809

WGS-type reaction is either facilitated by the adsorbed water or inhibited by the

810

decreased amount of -OH groups. As known, formate species is generally regarded as 38 ACS Paragon Plus Environment

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ACS Catalysis

811

an intermediate species in WGS-type reaction, which would decompose into CO2 and

812

H2 with the temperature raising.81,104,107 In Fig. 9(B) and 9(C), the absorbed formate

813

species characterized by the vibrational frequencies at 2842, 2852, 2932, and 2965

814

cm-1 are distinctly observed for CuCe and FeCuCe samples.81,107,108 It is also seen that

815

larger amount of this intermediate species is formed on FeCuCe at the lower

816

temperature, when compared with the sample of CuCe. Meanwhile, the starting

817

temperature for the decrease in peaks intensity of intermediate species over CuCe is

818

150 oC, while the corresponding temperature for FeCuCe is 170 oC. These results

819

demonstrate the promotional effect of Fe additive on the formation of absorbed

820

formates and on the decomposition of intermediate into CO2 and H2, i.e., WGS-type

821

reaction, which is in well accordance with the CO-TPR results.

822

Secondly, 10% H2O is introduced into the reaction system to consider the

823

H2O-assisted CO oxidation by the formation of surface -OH groups. The independent

824

WGS reactions were performed over CuCe and FeCuCe samples by using 1% CO and

825

10% H2O as reaction gas. CO conversion and products concentration of WGS reaction

826

over two samples are shown in Fig. 10(A) and 10(B), respectively. It is seen from Fig.

827

10(A) that CO conversions of CuCe and FeCuCe samples are close to 0% at 120 oC,

828

and, at higher temperature, the conversion is higher for FeCuCe (10.5% at 140 oC and

829

20.7% at 160 oC, respectively) than that for CuCe (1.2% at 140 oC and 4.9% at 160 oC,

830

respectively), suggesting that WGS reaction occurs at a temperature above 120 oC,

831

and the addition of Fe largely facilitates the WGS reaction. The concentration of

832

products (CO2 and H2) during the course of WGS reaction is further analyzed to 39 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

833

confirm the promotional effect of Fe additive as well as the reaction mechanism. As

834

shown in Fig. 10(B), it is found that, CO with the concentration of 1046 ppm is

835

consumed at 140 oC (in fact, the difference in the tolerance of H2O and CO2 of the

836

catalysts is significant at this temperature), 488 ppm of CO2 accompanied with 13

837

ppm of H2 is generated over FeCuCe. This result demonstrates that the reaction

838

between CO and surface formed -OH groups is not the main factor promoting the

839

tolerance of H2O and CO2 of the catalysts at 140 oC, since the amount of produced H2

840

is small at this time. Meanwhile, nearly half amount of the generated CO2 compared to

841

the consumed CO confirms that the high tolerance of CO2 and H2O of FeCuCe

842

catalyst at 140 oC (Fig. 8(A) and Fig. 8(B)) is resulted from the possible occurrence of

843

the disproportionation reaction (2CO → CO2 + C). With the temperature increasing to

844

160 oC (the stability tests are performed), when 2071 ppm of CO is consumed, 1268

845

ppm of CO2 accompanied with 379 ppm of H2 is formed over FeCuCe, suggesting

846

that 758 ppm of CO is used for the reaction between CO and surface formed -OH

847

groups, and 1020 ppm of CO is used for the disproportionation reaction. These results

848

evidence that, although the reaction between CO and surface formed -OH groups

849

becomes important, the disproportionation reaction has the slight greater impact on

850

the stability than the latter (1.34 vs 1.0). Thus, the longer-term stability of FeCuCe

851

than CuCe sample at about 160 oC is attributed to the synergistic roles of the

852

disproportionation reaction with the reaction between CO and surface formed -OH

853

groups. With the temperature increasing from 160 oC to the higher one, the reaction

854

between CO and surface formed -OH groups is gradually predominant. 40 ACS Paragon Plus Environment

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ACS Catalysis

855

To further prove the occurrence of the disproportionation of CO as well as the

856

subsequent reaction (C + H2O = CO + H2), which is deemed as another pathway for

857

WGS reaction, the determination of the presence of carbon-containing species over

858

the catalyst surface is an important evidence. Therefore, the CO pulsing technique

859

was introduced to proceed the disproportionation of CO where enough CO pulse was

860

consumed at 140 oC. The pulsed FeCuCe sample was further reacted with 10% H2O at

861

140 oC for 3 h to verify the subsequent reaction (C + H2O = CO + H2). The pulsed

862

CuCe and FeCuCe samples as well as reacted FeCuCe after CO pulsing were

863

characterized by Raman technique so as to determine the presence and the variation of

864

carbon species. The Raman spectroscopy of them are shown in Fig. 10(C), and H2

865

concentration produced during the reaction of pulsed FeCuCe with H2O is also

866

displayed in Fig. 10(D). It is found that no Raman bands corresponding to carbon

867

species are found for pulsed CuCe sample, whereas pulsed FeCuCe sample exhibits

868

distinct Raman peaks at 1360-1400 cm-1, and 1480-1520 cm-1 as well as

869

1580-1640cm-1, attributed typically to the different type of unorganized carbonaceous

870

species,72,109-111 which evidences the occurrence of the disproportionation of CO.

871

After the reaction between the pulsed FeCuCe sample with deposited carbonaceous

872

species and H2O, the amount of deposited carbonaceous species obviously decreases

873

(Fig. 10C-(c)), and meanwhile, a small number of H2 is generated (Fig. 10(D)),

874

demonstrating unambiguously the consumption of carbonaceous species by the

875

presence of H2O (C + H2O = CO + H2). These carbonaceous species are generally

876

under development, and thus can be reacted with H2O to generate CO and H2 under 41 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

877

the current reaction condition. However, large amount of H2 cannot be produced

878

possibly because that the reaction of carbonaceous species with H2O is a

879

rate-determining step, which is favorable in the long-term stability test instead. This

880

slow reaction rate of deposited carbonaceous species with H2O and the fast reaction

881

rate of the disproportionation reaction could lead to the generation of small amount of

882

H2 as well as large amount of CO2, which can also explain the situation that the

883

selectivity of H2 decreases at 140 oC in Fig. 8(B) (CO2 selectively increases) as well

884

as the selectivity of H2 increases at about 160 oC in Fig. 8(C) (CO2 selectively

885

decreases).

886

In summary, considering that the conversions of CO in WGS reaction are

887

approximately 10 % at 140 oC and 20% at 160 oC over FeCuCe, the primary causes of

888

the high tolerance of H2O and CO2 towards FeCuCe catalyst at 140 oC and the

889

long-term stability of FeCuCe around 160 oC is due to the promotional effect of Fe

890

additive on the lattice oxygen mobility, the second one is the important role of the

891

WGS reaction, which is driven by the addition of Fe. Two reaction pathways

892

(mechanism) are considered to be occurred during the course of WGS reaction. The

893

disproportionation of CO is responsible for the high tolerance of H2O and CO2 of

894

FeCuCe catalyst at 140 oC, and WGS reaction by the disproportionation pathway as

895

well as the H2O-assisted CO oxidation by the formation of surface -OH groups are

896

beneficial to the long-term stability of FeCuCe. However, the decomposition of

897

surface carbonate by H2O is not regarded as the main reason contributing to the high

898

tolerance of H2O and CO2 and the excellent stability of the catalyst, as confirmed 42 ACS Paragon Plus Environment

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ACS Catalysis

899

(Section 5 of SI).

900

4. CONCLUSIONS

901

In summary, CuCe and Fe doped CuCe catalysts were prepared via a solvent-free

902

combustion synthesis (SFCS) method to investigate the active species and the Fe

903

doping effect. The active Cu1+ species was demonstrated by in-situ DRIFTS technique

904

and XPS as well as CO-TPD to be adsorption sites for the adsorption and the

905

activation of CO molecules. The modification of Fe additive resulted in the

906

incorporation of CeO2 lattice so as to induce the redox chemistry between Fe3+/Fe2+

907

and Cu1+/Cu2+, which appropriately enhanced the adsorption ability of CO over Cu1+

908

adsorption sites. Our combined in-situ OSC and designed TPR characterizations

909

showed that the surface highly dispersed oxygen species related to CuOx species was

910

confirmed as one of active species and to be involved in the CO oxidation at low

911

temperature. The surface lattice oxygen species assisted with Cu-[Ox]-Ce (Fe-O-Ce)

912

was also proved to participate into the reaction process. Due to the charge

913

compensation and the difference in the ionic radius between Fe and Ce ions, the

914

incorporation of Fe into CeO2 lattice generated plentiful oxygen vacancies, which was

915

not only in favor of trapping gas-phase oxygen to form the surface highly dispersed

916

oxygen, but also promoted the migration of subsurface lattice oxygen to surface active

917

oxygen. The former promoted the CO catalytic activity (TOF value increased from

918

3.62×10-2 s-1 for CuCe to 4.50×10-2 s-1 for CuCe-Fe), and the latter in combination

919

with the high resistance to H2O using Fe doped as favourable WGS catalyst made an

920

important contribution to the long stability in the presence of CO2 and H2O (increased 43 ACS Paragon Plus Environment

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921

the lifetime from 170 to 400 h).

922

● Supporting Information

923

The Supporting Information is available free of charge on the ACS Publications

924

website.

925

Additional Transmission electron microscope (TEM). H2-TPR profile of CuO.

926

In-situ DRIFTS of CuCe and FeCuCe samples in the gas stream with the addition of a

927

certain amount of H2O. The method of calculating the concentration of oxygen

928

vacancies, and the explanation of satellite peak of Fe 2p XPS spectra.

929



930

Corresponding Authors

931

* E-mail: [email protected]

932

Notes

933

The authors declare no competing financial interest.

934



935

We gratefully acknowledge the financial supports of National Natural Science

936

Foundation of China (Grant No. 21267011, 21367015, 21666013, 51704137 and

937

U1402233).

AUTHOR INFORMATION

ACKNOWLEDGMENTS

938

44 ACS Paragon Plus Environment

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939

ACS Catalysis

Table 1 Textural parameters and structural properties of CuCe and CuCe-Fe catalysts.

Samples

TOF×

r(CO)×10-6

lattice parameter

crystallite

10 (s )

(mol g s )

CuCe-Fe

4.50

1.60

0.54016

9.6

CuCe

3.62

1.13

0.54126

11.0

-2

-1 a

-1 -1

size (nm)

Cu/Ce

Vp

d

(m g )

(cm g )

0.336

19.7

0.042

0.293

12.6

0.044

c

(nm) b

SBET

Concentration of

2

-1

3

Isat/Imp

d

oxygen vacancies

Ce3+/(Ce3++C e

e ) (3d5/2) 4+

-1

(%)

0.32

4.43

27.56

51.65

0.19

3.84

22.00

36.33

a

TOF value was calculated based on the CO conversion at 80 oC,

941

b

Lattice parameters were obtained by using MDI Jade 5.0 software according the data of XRD,

942

c

Crystallite size determined from XRD by the Scherrer’s equation with the half width of the diffraction peak of the (111) plane,

943

d

Values were estimated from XPS peak fitting data,

944

e

The concentration of oxygen vacancies (N) was calculated by using Raman spectroscopy.

ACS Paragon Plus Environment

OII) d (%)

(×1021 cm-3)

940

45

OII/(OI +

d

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

945



REFERENCES

[1] Ercolino, G.; Ashraf, M. A.; Specchia, V.; Specchia, S. Performance evaluation and comparison of fuel processors integrated with PEM fuel cell based on steam or autothermal reforming and on CO preferential oxidation or selective methanation. Appl. Energy 2015, 143, 138-153. [2] Lu, J. C.; Li, X. F.; He, S. F.; Han, C.Y.; Wan, G. P.; Lei, Y. Q.; Chen, R.; Liu, P.; Chen, K. Z.; Zhang, L.; Luo, Y. M. Hydrogen production via methanol steam reforming over Ni-based catalysts: Influences of Lanthanum (La) addition and supports. Int. J. Hydrogen Energ. 2017, 42, 3647-3657. [3] Njagi, E. C.; Genuino, H. C.; Kingondu, C. K.; Chen, C. H.; Horvath, D.; Suib, S. L. Preferential oxidation of CO in H2-rich feeds over mesoporous copper manganese oxides synthesized by a redox method. Int. J. Hydrogen Energ. 2011, 36, 6768-6779. [4] Zhang, L.; Kim, J.; Zhang, J.; Nan, F.; Gauquelin, N.; Botton, G. A.; He, P.; Bashyam, R.; Knights, S. Ti4O7 supported Ru@Pt core-shell catalyst for COtolerance in PEM fuel cell hydrogen oxidation reaction. Appl. Energy 2013, 103, 507-513. [5] Ayastuy, J.; Gutiérrez, O. M.; González-Marcos, J.; Aranzabal, A.; González, V. J. Kinetics of the Low-Temperature WGS Reaction over a CuO/ZnO/Al2O3 Catalyst. Ind. Eng. Chem. Res. 2005, 44, 41-50. [6] Reyes, C. A.; Arango, D. A.; Moretti, E.; Talon, A.; Storaro, L.; Lenarda, M.; López, A. J.; Castellón, E. R. CuO/CeO2 supported on Zr doped SBA-15 as catalysts for preferential CO oxidation (CO-PROX). J. Power Sources 2011, 196, 4382-4387. [7] Song, C. Fuel processing for low-temperature and high-temperature fuel cells Challenges, and opportunities for sustainable development in the 21st century. Catal. Today 2002, 77, 17-49. 46 ACS Paragon Plus Environment

Page 46 of 74

Page 47 of 74 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

[8] Zhang, Y.; Liang, H.; Gao, X. Y.; Liu, Y. Three-dimensionally ordered macro-porous CuO-CeO2 used for preferential oxidation of carbon monoxide in hydrogen-rich gases. Catal. Comm. 2009, 10, 1432-1436. [9] Trimm, D. L. Minimisation of carbon monoxide in a hydrogen stream for fuel cell application. Appl. Catal., A Gen. 2005, 296, 1-11. [10] Morse, J. D. Micro-fuel cell power sources. Int. J. Energy Res. 2007, 31, 576-602. [11] Moretti, E.; Lenarda, M.; Storaro, L.; Talon, A.; Frattini, R.; Polizzi, S.; Rodríguez, C. E.; Jiménez, L. A. Catalytic purification of hydrogen streams by PROX on Cu supported on an organized mesoporous ceria-modified alumina. Appl. Catal. B Environ. 2007, 72, 149-156. [12] Liu, Z. G.; Zhou, R. X.; Zheng, X. M. Influence of preparation methods on CuO-CeO2 catalysts in the preferential oxidation of CO in excess hydrogen. J. Nat. Gas Chem. 2008, 17, 125-129. [13] Avgouropoulos, G.; Ioannides, T.; Papadopoulou, C.; Batista, J.; Hocevar, S.; Matralis, H. K. A comparative study of Pt/γ-Al2O3, Au/α-Fe2O3 and CuO-CeO2 catalysts for the selective oxidation of carbon monoxide in excess hydrogen. Catal. Today 2002, 75, 157-167. [14] Gamarra, D.; Munuera, G.; Hungria, A. B.; Fernandez, G. M.; Conesa, J. C.; Midgley, P. A.; Wang, X. Q.; Hanson, J. C.; Rodriguez, J. A.; Martinez, A. A. Structure-activity relationship in nanostructured copper-ceria-based preferential CO oxidation catalysts. J. Phys. Chem. C 2007, 111, 11026-11038. [15] Gamarra, D.; Hornés, A.; Koppàny, Z.; Schay, Z.; Munuera, G.; Soria, J.; Martínez, A. A. Catalytic processes during preferential oxidation of CO in H2-rich streams over catalysts based on copper-ceria. J. Power Sources 2007, 169, 110-116. 47 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

[16] Ilichev, A. N.; Firsova, A. A.; Korchak, V. N. Mechanism of CO oxidation in excess H2 over CuO/CeO2 catalysts: ESR and TPD studies. Kinet. Catal. 2006, 47, 585-592. [17] Skårman, B.; Grandjean, D.; Benfield, R. E.; Hinz, A.; Andersson, A.; Wallenberg, L. R. Carbon monoxide oxidation on nanostructured CuOx/CeO2 composite particles characterized by HREM, XPS, XAS, and High-energy diffraction. J. Catal. 2002, 211, 119-133. [18] Gamarra, D.; Cámara, A. L.; Monte, M.; Rasmussen, S. B.; Chinchilla, L. E.; Hungría, A. B.; Munuera, G.; Gyorffy, N.; Schay, Z.; Corberán, V. C.; Conesa, J. C.; Martínez, A. A. Preferential oxidation of CO in excess H2 over CuO/CeO2 catalysts: Characterization and performance as a function of the exposed face present in the CeO2 support. Appl. Catal. B Environ. 2013, 130-131, 224-238. [19] Wang, W. W.; Du, P. P.; Zou, S. H.; He, H. Y.; Wang, R. X.; Jin, Z.; Shi, S.; Huang, Y. Y.; Si, R.; Song, Q. S.; Jia, C. J.; Yan, C. H. Highly Dispersed Copper Oxide Clusters as Active Species in Copper-Ceria Catalyst for Preferential Oxidation of Carbon Monoxide. ACS Catal. 2015, 5, 2088-2099. [20] Luo, M. F.; Ma, J. M.; Lu, J. Q.; Song, Y. P.; Wang, Y. J. High-surface area CuO-CeO2 catalysts prepared by a surfactant-templated method for low-temperature CO oxidation. J. Catal. 2007, 246, 52-59. [21] Zeng, S. H.; Zhang, W. L.; Guo, S. L.; Su, H. Q. Inverse rod-like CeO2 supported on CuO prepared by hydrothermal method for preferential oxidation of carbon monoxide. Catal. Commun. 2012, 23, 62-66. [22] Wang, J.; Deng, L.; He, D. D.; Lu, J. C.; He, S. F.; He, S. Y.; Luo, Y. M. A facile and rapid route to synthesize CuOx/Ce0.8Zr0.2O2 catalysts with high performance for CO preferential oxidation (CO-PROX). Int. J. Hydrogen Energ. 2015, 40, 48 ACS Paragon Plus Environment

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12478-12488. [23] Guo, X. L.; Zhou, R. X. Identification of the nano/micro structure of CeO2(rod) and the essential role of interfacial copper-ceria interaction in CuCe(rod) for selective oxidation of CO in H2-rich streams. J. Power Sources 2017, 361, 39-53. [24] Guo, X. L.; Mao, J. X.; Zhou, R. X. Influence of the copper coverage on the dispersion of copper oxide and the catalytic performance of CuO/CeO2(rod) catalysts in preferential oxidation of CO in excess hydrogen. J. Power Sources 2017, 371, 119-128. [25] Du, P. P.; Wang, W. W.; Jia, C. J.; Song, Q. S.; Huang, Y. Y.; Si, R. Effect of strongly bound copper species in copper-ceria catalyst for preferential oxidation of carbon monoxide. Appl. Catal., A: Gen. 2016, 518, 87-101. [26] Gamarra, D.; Belver, C.; Fernandez-Garcıa, M.; Martınez-Arias, A., Selective CO Oxidation in Excess H2 over Copper-Ceria Catalysts: Identification of Active Entities/Species. J. Am. Chem. Soc. 2007, 129, 12064. [27] Yao, S. Y.; Mudiyanselage, K.; Xu, W. Q.; Johnston-Peck, A. C.; Jonathan, C. H.; Wu, T. P.; Dario, S.; José, A. R.; Zhao, H. Y.; Kevin, A. B.; Karena, W. C.; Peter, J. C.; Arturo, M. A.; Si, R.; Trudy, B. B.; Liu, We. J.; Sanjaya, D. S. Unraveling the Dynamic Nature of a CuO/CeO2 Catalyst for CO Oxidation in Operando: A Combined Study of XANES (Fluorescence) and DRIFTS. ACS Catal. 2014, 4, 1650-1661. [28] Zeng, S. H.; Wang, Y.; Ding, S. P.; Jesper, J. H.; Sattler, B.; Borodina, E.; Zhang, L.; Bert, M. W.; Su, H. Q. Active sites over CuO/CeO2 and inverse CeO2/CuO catalysts for preferential CO oxidation. J. Power Sources 2014, 256, 301-311. [29] Zhang, R.; Jeffery, T. M.; Chelsey, D. B. Identifying the active redox oxygen sites in a mixed Cu and Ce oxide catalyst by in situ X-ray absorption spectroscopy and anaerobic reactions with CO in concentrated H2. J. Catal. 2012, 294, 69-78. 49 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

[30] Joseph, S. E.; Marcel, R.; Livia, G. D.; Azzam, N. M.; Yang, S. H. Structure, Bonding, and Catalytic Activity of Monodisperse, Transition-Metal-Substituted CeO2 Nanoparticles. J. Am. Chem. Soc. 2014, 136, 17193-17200. [31] Joseph, S. E.; Nongnuch, A.; Matthieu, B.; Livia, G.; Gianluigi, A. B.; Alexie, M. K.; Yang, S. H. Elucidating the Nature of the Active Phase in Copper/Ceria Catalysts for CO Oxidation. ACS Catal. 2016, 6, 1675-1679. [32] Christopher, S. P.; Hari, N.; Chelsey, D. B. Study of active sites and mechanism responsible for highly selective CO oxidation in H2 rich atmospheres on a mixed Cu and Ce oxide catalyst. J. Catal. 2009, 266, 308-319. [33] Liu, L. Q.; Zhou, F.; Wang, L. G.; Qi, X. J.; Shi, F.; Deng, Y. Q. Low-temperature CO oxidation over supported Pt, Pd catalysts: Particular role of FeOx support for oxygen supply during reactions. J. Catal. 2010, 274, 1-10. [34] Wang, H.; Qu, Z. P.; Xie, H. B.; Maeda, N.; Miao, L.; Wang, Z. Insight into the mesoporous FexCe1-xO2-δ catalysts for selective catalytic reduction of NO with NH3: Regulable structure and activity. J. Catal. 2016, 338, 56-67. [35] Bielun, Z. L.; Bettahar, M. M.; Monteverdi, S. Fe-promoted CuO/CeO2 catalyst Structural characterization and CO oxidation activity. Catal. Comm. 2010, 11, 1137-1142. [36] Khampol, S.; Apanee, L.; Sangobtip, P. Selective oxidation of CO to CO2 over Cu-Ce-Fe-O composite-oxide catalyst in hydrogen feed stream. Int. J. Hydrogen Energ. 2007, 32, 915-926. [37] Firsova, A. A.; Ilichev, A. N.; Khomenko, T. I.; Gorobinskii, L. V.; Maksimov, Y. V.; Suzdalev, I. P.; Korchak, V. N. Selective Oxidation of CO in the Presence of Hydrogen on CuO/CeO2 Catalysts Modified with Fe and Ni Oxides. Kinet. Catal. 2007, 48, 282-291. 50 ACS Paragon Plus Environment

Page 50 of 74

Page 51 of 74 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

[38] Zou, H. B.; Chen, S.; Liu, Z.; Lin, W. Selective CO oxidation over CuO-CeO2 catalysts doped with transition metal oxides. Powder Technol. 2011, 207, 238-244. [39] Sahoo, T. R.; Armandi, M.; Arletti, R.; Piumetti, M.; Bensaid, S.; Manzoli, M.; Panda, S. R.; Bonelli, B. Pure and Fe-doped CeO2 nanoparticles obtained by microwave assisted combustion synthesis: Physico-chemical properties ruling their catalytic activity towards CO oxidation and soot combustion. Appl. Catal. B: Environ. 2017, 211, 31-45. [40] Zhang, Z. L.; Han, D.; Wei, S.; Zhang, Y. Determination of active site densities and mechanisms for soot combustion with O2 on Fe-doped CeO2 mixed oxides. J. Catal. 2010, 276, 16-23. [41] He, F.; Wei, Y.; Li, H.; Wang, H. Synthesis Gas Generation by Chemical-Looping Reforming Using Ce-Based Oxygen Carriers Modified with Fe, Cu, and Mn Oxides. Energy & Fuels 2009, 23, 2095-2102. [42] Reddy, G. K.; Boolchand, P.; Smirniotis, P. G. Sulfur tolerant metal doped Fe/Ce catalysts for high temperature WGS reaction at low steam to CO ratios-XPS and Mössbauer spectroscopic study. J. Catal. 2011, 282, 258-269. [43] Wang, J.; Han, C.; Gao, X.; Lu, J.; Wan, G.; He, D.; Chen, R.; Chen, K.; He, S.; Luo, Y. Rapid synthesis of Fe-doped CuO-Ce0.8Zr0.2O2 catalysts for CO preferential oxidation in H2-rich streams: Effect of iron source and the ratio of Fe/Cu. J. Power Sources 2017, 343, 437-445. [44] Zhang, X.; Tian, P.; Tu, W.; Zhang, Z.; Xu, J.; Han, Y. F. Tuning the Dynamic Interfacial Structure of Copper-Ceria Catalysts by Indium Oxide during CO Oxidation. ACS Catal. 2018, 8, 5261-5275. [45] Jia, A. P.; Jiang, S. Y.; Lu, J. Q.; Luo, M. F. Study of Catalytic Activity at the CuO-CeO2 Interface for CO Oxidation. J. Phys. Chem. C 2010, 114, 21605-21610. 51 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 52 of 74

[46] Zhao, Z. K.; Bao, T.; Zeng, Y.; Wang, G.; Muhammad, T. Efficient cobaltmanganese oxide catalyst deposited on modified AC with unprecedented catalytic performance in CO preferential oxidation. Catal. Commun. 2013, 32, 47-51. [47] Cao, J. L.; Wang, Y.; Zhang, T. Y.; Wu, S. H.; Yuan, Z. Y. Preparation, characterization

and

catalytic

behavior

of

nanostructured

mesoporous

CuO/Ce0.8Zr0.2O2 catalysts for low-temperature CO oxidation. Appl. Catal. B Environ. 2008, 78, 120-128. [48] Vlaic, G.; Fornasiero, P.; Geremia, S.; Kaspar, J.; Graziani, M. Relationship between the zirconia-promoted reduction in the Rh-loaded Ce0.5Zr0.5O2 mixed oxide and the Zr-O local structure. J. Catal. 1997, 168, 386-392. [49] Liu, Z.; Wu, Z.; Peng, X.; Binder, A.; Chai, S.; Dai, S. Origin of active oxygen in a ternary CuOx/Co3O4-CeO2 catalyst for CO oxidation. J. Phys. Chem. C 2014, 118, 27870-27877. [50] Maciel, C. G.; Silva, T. F.; Profeti, L.; Assaf, E. M.; Assaf, J. M. Study of CuO/CeO2 catalyst with for preferential CO oxidation reaction in hydrogen-rich feed (PROX-CO). Appl. Catal., A Gen. 2012, 431-432, 25-32. [51] Jung, C. R.; Kundu, A.; Nam, S. W.; Lee, H. Doping effect of precious metal on the activity of CuO-CeO2 catalyst for selective oxidation of CO. Appl. Catal., A Gen. 2007, 331, 112-20. [52] Fan, J.; Wu, X.; Wu, X.; Liang, Q.; Ran, R.; Weng, D. Thermal ageing of Pt on low-surface-area CeO2-ZrO2-La2O3 mixed oxides: effect on the OSC performance. Appl. Catal. B Environ. 2008, 81, 38-48. [53] Reddy, G. K.; Boolchand, P.; Smirniotis, P. G. Sulfur tolerant metal doped Fe/Ce catalysts for high temperature WGS reaction at low steam to CO ratios-XPS and Mössbauer spectroscopic study. J. Catal. 2011, 282, 258-269. 52 ACS Paragon Plus Environment

Page 53 of 74 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

[54] Pereira, A. L. C.; Berrocal, G. J. P.; Marchetti, S. G.; Albornoz, A.; Souza, A. O.; Rangel, M. C. A comparison between the precipitation and impregnation methods for water gas shift catalysts. Mol. Catal. 2008, 281, 66-72. [55] Fujii, T.; Groot, F.; Sawatzky. G. In situ XPS analysis of various iron oxide films grown by NO2-assisted molecular-beam epitaxy. Phys. Rev. B. 1999, 59, 3195-3202. [56] Harrison, W. A. Electronic Structure and the Properties of Solids (Freeman, San Francisco, 1980) [57] Moretti, E.; Storaro, L.; Talon, A.; Lenarda, M.; Riello, P.; Frattini, R.; Yuso, M.; Jiménez, L. A.; Rodríguez, C. E.; Ternero, F.; Caballero, A.; Holgado, J. P. Effect of thermal treatments on the catalytic behaviour in the CO preferential oxidation of a CuO-CeO2-ZrO2 catalyst with a flower-like morphology. Appl. Catal. B Environ. 2011, 102, 627-37. [58] Kundakovic, L.; Stephanopoulos, M. F. Reduction characteristics of copper oxide in cerium and zirconium oxide systems. Appl. Catal., A Gen. 1998, 171, 13-29. [59] Liu, W.; Stephanopoulos, M. F. Total oxidation of carbon-monoxide and methane over transition metal fluorite oxide composite catalysts II. catalyst characterization and reaction-kinetics. J. Catal. 1995, 153, 317-32. [60] Peng, Y., Shang, L., Cao, Y., Waterhouse, G. I., Zhou, C., Bian, T., Wu, L. Z.; Tung C. H.; Zhang, T. Copper (I) cysteine complexes: Efficient earth-abundant oxidation co-catalysts for visible light-driven photocatalytic H2 production. Chem Comm. 2015, 51, 12556-12559. [61] Liu, P.; Hensen, E. J. Highly efficient and robust Au/MgCuCr2O4 catalyst for gas-phase oxidation of ethanol to acetaldehyde. J. Am. Chem. Soc. 2013, 135, 14032-14035. [62] Avgouropoulos, G.; Ioannides, T.; Matralis, H. Influence of the preparation 53 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

method on the performance of CuO-CeO2 catalysts for the selective oxidation of CO. Appl. Catal. B Environ. 2005, 56, 87-93. [63] Pimenta, M. A.; Corro, E.; Carvalho, B. R.; Fantini, C.; Malard, L. M. Comparative Study of Raman Spectroscopy in Graphene and MoS2-type Transition Metal Dichalcogenides. Acc. Chem. Res. 2015, 48, 41−47. [64] Pal, P.; Singha, R. K.; Saha, A.; Bal, R.; Panda, A. B. Defect-Induced Efficient Partial Oxidation of Methane over Nonstoichiometric Ni/CeO2 Nanocrystals. J. Phys. Chem. C 2015, 119, 13610-13618. [65] Li, X.; Quek, X. Y.; Ligthart, D. M.; Guo, M.; Zhang, Y.; Li, C.; Yang, Q.; Hensen, E. M. CO-PROX reactions on copper cerium oxide catalysts prepared by melt infiltration. Appl. Catal. B Environ. 2012, 123-124, 424-32. [66] Pu, Z. Y.; Liu, X. S.; Jia, A. P.; Xie, Y. L.; Lu, J. Q.; Luo, M. F. Enhanced activity for CO oxidation over Pr- and Cu-Doped CeO2 catalysts: Effect of oxygen vacancies. J. Phys. Chem. C 2008, 112, 15045-51. [67] McBride, J. R.; Hass, K. C.; Poindexter, B. D.; Weber, W. H. Raman and x-ray studies of Ce1-xRExO2-y, where RE=La, Pr, Nd, Eu, Gd, and Tb. J. Appl. Phys. 1994, 76, 2435-41. [68] Trogadas, P.; Parrondo, J.; Ramani, V. CeO2 surface oxygen vacancy concentration governs in situ free radical scavenging efficacy in polymer electrolytes. ACS Appl. Mater. Interfaces 2012, 4, 5098-5102. [69] Kosacki, I.; Suzuki, T.; Anderson, H. U.; Colomban, P. Raman scattering and lattice defects in nanocrystalline CeO2 thin films. Solid State Ionics 2002, 149, 99-105. [70] Laguna, O. H.; Centeno, M. A.; Boutonnet, M.; Odriozola, J. A. Fe-doped ceria solids synthesized by the microemulsion method for CO oxidation reactions. Appl. 54 ACS Paragon Plus Environment

Page 54 of 74

Page 55 of 74 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

Catal. B Environ. 2011, 106, 621-629. [71] Chen, D.; He, D.; Lu, J.; Zhong, L.; Liu, F.; Liu, J.; Yu, J.; Wan, G.; He, S.; Luo, Y. Investigation of the role of surface lattice oxygen and bulk lattice oxygen migration of cerium-based oxygen carriers: XPS and designed H2-TPR characterization. Appl.Catal. B: Environ. 2017, 218, 249-259. [72] Lu, J.; Hao, H.; Zhang, L.; Xu, Z.; Zhong, L.; Zhao, Y.; He, D.; Liu, J.; Chen, D.; Pu, H.; He, S.; Luo, Y. The investigation of the role of basic lanthanum (La) species on the improvement of catalytic activity and stability of HZSM-5 material for eliminating methanethiol-(CH3SH). Appl. Catal. B: Environ. 2018, 237 , 185-197. [73] Dou, X.; Sabba, D.; Mathews, N.; Wong, L. H.; Lam, Y. M.; Mhaisalkar, S. Hydrothermal Synthesis of High Electron Mobility Zn-doped SnO2 Nanoflowers as Photoanode Material for Efficient Dye-Sensitized Solar Cells. Chem. Mater. 2011, 23, 3938-3945. [74] Sedmak, G.; Hocevar, S.; Levec, J. Kinetics of selective CO oxidation in excess of H2 over the nanostructured Cu0.1Ce0.9O2−y catalyst. J. Catal. 2003, 213, 135-150. [75] Li, J.; Han, Y.; Zhu, Y.; Zhou, R. Purification of hydrogen from carbon monoxide for fuel cell application over modified mesoporous CuO-CeO2 catalysts. Appl. Catal., B: Environ. 2011, 108-109, 72-80. [76] Polster, C. S.; Nair, H.; Baertsch, C. D. Study of active sites and mechanism responsible for highly selective CO oxidation in H2 rich atmospheres on a mixed Cu and Ce oxide catalyst. J. Catal. 2009, 266, 308-319. [77] Lykaki, M.; Pachatouridou, E.; Carabineiro, S. A.C.; Iliopoulou, E.; Andriopoulou, C.; Kallithrakas, K. N.; Boghosian, S. Michalis Konsolakis, Ceria nanoparticles shape effects on the structural defects and surface chemistry: Implications in CO oxidation by Cu/CeO2 catalysts. Appl. Catal. B: Environ. 2018, 55 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

230, 18-28. [78] Campbell, C. T.; Peden, C. H. F. Oxygen Vacancies and Catalysis on Ceria Surfaces. Science 2005, 5735, 309, 713-714. [79] Campbell, C. T. Waltzing with O2. Science 2003, 5605, 299, 357. [80] Liotta, L.F.; Carlo, D.G.; Pantaleo, G.; Venezia, A. M.; Deganello, G. Co3O4/CeO2 composite oxides for methane emissions abatement: Relationship between Co3O4-CeO2 interaction and catalytic activity. Appl. Catal. B Environ. 2006, 66, 217-227. [81] Zheng, Y.; Li, K.; Wang, H.; Wang, Y.; Tian, D.; Wei, Y.; Zhu, X.; Zeng, C.; Luo, Y. Structure dependence and reaction mechanism of CO oxidation: A model study on macroporous CeO2 and CeO2-ZrO2 catalysts. J. Catal. 2016, 344, 365-377. [82] Wang, J.; Han, C.; Gao, X.; Lu, J.; Wan, G.; He, D.; Chen, R.; Chen, He, K. S.; Luo, Y. Rapid synthesis of Fe-doped CuO-Ce0.8Zr0.2O2 catalysts for CO preferential oxidation in H2-rich streams: Effect of iron source and the ratio of Fe/Cu. J. Power Sources 2017, 343, 437-445. [83] Wang, W. W.; Yu, W. Z.; Du, P. P.; Xu, H.; Jin, Z.; Si, R.; Ma, C.; Shi, S.; Jia, C. J.; Yan, C. H. Crystal Plane Effect of Ceria on Supported Copper Oxide Cluster Catalyst for CO Oxidation: Importance of Metal-Support Interaction. ACS Catal. 2017, 7, 1313-1329. [84] Tang, C.; Sun, J.; Yao, X.; Cao, Y.; Liu, L.; Ge, C.; Gao, F.; Dong, L. Efficient fabrication of active CuO-CeO2/SBA-15 catalysts for preferential oxidation of CO by solid state impregnation. Appl. Catal. B: Environ. 2014, 146, 201-212. [85] Du, P. P.; Wang, W. W.; Jia, C. J.; Song, Q. S.; Huang, Y. Y.; Si, R. Effect of strongly bound copper species in copper-ceria catalyst for preferential oxidation of carbon monoxide. Appl. Catal., A: Gen. 2016, 518, 87-101. 56 ACS Paragon Plus Environment

Page 56 of 74

Page 57 of 74 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

[86] Li, K.; Wang, H.; Wei, Y.; Yan, D. Direct conversion of methane to synthesis gas using lattice oxygen of CeO2-Fe2O3 complex oxides. Chem. Eng. J. 2010, 156, 512-518. [87] Bin, F.; Wei, X.; Li, B.; Hui, K. S. Self-sustained combustion of carbon monoxide promoted by the Cu-Ce/ZSM-5 catalyst in CO/O2/N2 atmosphere. Appl. Catal. B: Environ. 2015, 162, 282-288. [88] Arandiyan, H.; Dai, H.; Deng, J.; Liu, Y.; Bai, B.; Wang, Y.; Li, X.; Xie, S.; Li, J. Three-dimensionally ordered macroporous La0.6Sr0.4MnO3 with high surface areas: Active catalysts for the combustion of methane. J. Catal. 2013, 307, 327-339. [89] Luo, M. F.; Zhong, Y. J.; Yuan, X. X.; Zheng, X. M. TPR and TPD studies of CuO/CeO2 catalysts for low temperature CO oxidation. Appl. Catal., A Gen. 1997, 162, 121-131. [90] Hadjiivanov, K. I.; Vayssilov, G. N. Characterization of oxide surfaces and zeolites by carbon monoxide as an IR probe molecule. Adv. Catal. 2002, 47, 307-511. [91] Padley, M. B.; Rochester, C. H.; Hutchings, G. J.; King, F. FTIR Spectroscopic Study of Thiophene, SO2, and CO Adsorption on Cu/Al2O3 Catalysts. J. Catal. 1994, 148, 438-452. [92] Manzoli, M.; Monte, R. D.; Boccuzzi, F.; Coluccia, S.; Kaspar, J. CO oxidation over CuOx-CeO2-ZrO2 catalysts: Transient behaviour and role of copper clusters in contact with ceria. Appl. Catal., B 2005, 61, 192-205. [93] Hollins P. The influence of surface defects on the infrared spectra of adsorbed species. Surf. Sci. Rep. 1992, 16, 51-94. [94] Elias, J. S.; Stoerzinger, K. A.; Hong, W. T.; Risch, M.; Giordano, L.; Mansour, A. N.; Horn, Y. S. In Situ Spectroscopy and Mechanistic Insights into CO Oxidation on Transition-Metal-Substituted Ceria Nanoparticles. ACS Catal. 2017, 7, 6843-6857. 57 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

[95] Park, J. W.; Jeong, J. H.; Yoon, W. L.; Rhee, Y. W. Selective oxidation of carbon monoxide in hydrogen-rich stream over Cu-Ce/γ-Al2O3 catalysts promoted with cobalt in a fuel processor for proton exchange membrane fuel cells. J. Power Sources 2004, 132, 18-28. [96] Mariño, F.; Descorme, C.; Duprez, D. Supported base metal catalysts for the preferential oxidation of carbon monoxide in the presence of excess hydrogen (PROX). Appl. Catal. B 2005, 58, 175. [97] Inui, T.; Fujimoto, K.; Uchijima, T.; Masai, M. New aspects of Spillover Effect in Catalysis. Elsevier, Amsterdam 1993, 27. [98] Gulari, E.; Guldur, C.; Srivannavit, S.; Osuwan, S. Co oxidation by silver cobalt composite oxide. Appl. Catal., A:Gen. 1999, 182, 147. [99] Gamarra, D.; Martínez, A. A. Preferential oxidation of CO in rich H2 over CuO/CeO2: Operando-DRIFTS analysis of deactivating effect of CO2 and H2O. J. Catal. 2009, 263, 189-195. [100] Park, J. W.; Jeong, J. H.; Yoon, W. L.; Rhee, Y. W. Selective oxidation of carbon monoxide in hydrogen-rich stream over Cu-Ce/γ-Al2O3 catalysts promoted with cobalt in a fuel processor for proton exchange membrane fuel cells. J. Power Sources. 2004, 132, 18. [101] Snytnikow, P.V.; Sobyanin, V. A.; Belyaev, V. D.; Tsyrulnikov, P. G.; Shitova, N. B.; Shlyapin, D. A. Selective oxidation of carbon monoxide in excess hydrogen over Pt-, Ru- and Pd-supported catalysts. Appl. Catal. A: Gen. 2003, 239, 149. [102] LeValley, T. L.; Richard, A. R.; Fan, M. The progress in water gas shift and steam reforming hydrogen production technologies-A review. Inter. J. Hydrogen Energ. 2014, 39, 16983-17000. [103] Reddy, G. K.; Kim, S. J.; Dong, J.; Smirniotis, P. G.; Jasinski, J. B. Long-term 58 ACS Paragon Plus Environment

Page 58 of 74

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ACS Catalysis

WGS stability of Fe/Ce and Fe/Ce/Cr catalysts at high and low steam to CO Ratios-XPS and Mössbauer spectroscopic study. Appl. Catal., A: Gen. 2012, 415-416, 101-110. [104] Wang, X.; Rodriguez, J. A.; Hanson, J. C.; Gamarra, D.; Martınez-Arias, A.; Fernandez-Garcıa, M. In Situ Studies of the Active Sites for the Water Gas Shift Reaction over Cu-CeO2 Catalysts: Complex Interaction between Metallic Copper and Oxygen Vacancies of Ceria. J. Phys. Chem. B 2006, 110, 428-434. [105] Jeong, D. W.; Jang, W. J.; Shim, J. O.; Han, W. B.; Roh, H. S.; Jung, U. H.; Yoon, W. L. Low-temperature wateregas shift reaction over supported Cu Catalysts. Renew. Energy 2014, 65, 102-107. [106] Si, R.; Raitano, J.; Yi, N.; Zhang, L.; Chan, S. W.; Flytzani-Stephanopoulos, M. Structure sensitivity of the low-temperature water-gas shift reaction on Cu-CeO2 catalysts. Catal. Today 2012, 180, 68-80. [107] Wu, Z.; Li, M.; Overbury, S. H. On the structure dependence of CO oxidation over CeO2 nanocrystals with well-defined surface planes. J. Catal. 2012, 285, 61-73. [108] Pozdnyakova, O.; Teschner, D.; Wootsch, A.; Kröhnert, J.; Steinhauer, B.; Sauer, H.; Toth, L.; Jentoft, F. C.; Knop-Gericke, A.; Paál, Z.; Schlögl, R. Preferential CO oxidation in hydrogen (PROX) on ceria-supported catalysts, part I: Oxidation state and surface species on Pt/CeO2 under reaction conditions. J. Catal. 2006, 237, 1-16. [109] Nemanich, R. J.; Glass, J. T.; Lucovsky, G.; Shroder, R. E. Raman scattering characterization of carbon bonding in diamond and diamondlike thin films. J. Vac. Sci. & Technol. A 1988, 6, 1783. [110] Ferrari, A. C.; Robertson, J. Raman spectroscopy of amorphous, nanostructured, diamond-like carbon, and nanodiamond. Phil. Trans. R. Soc. Lond. A 2004, 362, 2477-2512. 59 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

[111] Botas, J. A.; Serrano, D. P.; García, A.; Vicente, J.; Ramos, R. Catalytic conversion of rapeseed oil into raw chemicals and fuels over Ni- and Mo-modified nanocrystalline ZSM-5 zeolite. Catal. Today 2012, 195, 59-70.

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Figure captions Fig. 1 (a) CO conversion and (b) CO2 selectivity of CuCe and CuCe-Fe. Reaction conditions: mcat=300 mg, feed gas: 1% CO, 1% O2, 50% H2 and balance He, flow rate=80 mL/min. Fig. 2 (A) XRD patterns of CuCe and CuCe-Fe. X-ray photoelectron spectra of CuCe and CuCe-Fe in the Ce 3d region (B), Fe 2p region (C) and Cu 2p region (D). Fig. 3 (A) Raman spectroscopy and (B) O 1s XPS spectra of CuCe and CuCe-Fe. Scheme 1. Structural model for CuCe (a) and CuCe-Fe (b) samples as well as the corresponding reaction mechanism for special CO oxidation as main reaction in CO-PROX. Fig. 4 (A) H2-TPR profiles of CuCe and CuCe-Fe. Comparison of oxygen storage capacity (OSC) in the form of CO2 (B) and CO (C) under mild conditions of T=150 and 200 oC for CuCe and CuCe-Fe. Fig. 5 Designed TPR characterization of CuCe (A) and CuCe-Fe (B) samples, P150-0: the fresh samples, P150-1 and P150-2: after pretreatment at 150 oC for 1 min, P150-1-R160 and P150-2-R160: the pretreated samples were reacted from 60 to 160 C every 20 oC, and P150-1-R220 and P150-2-R220: the pretreated samples were

o

reacted from 60 to 220 oC every 20 oC. OSC measurements of the pretreated CuCe and CuCe-Fe samples calculated in the form of CO2 (C) and CO (D). Comparison of the catalytic activity of CuCe (E) and CuCe-Fe (F) before (black line) and after (red line) pretreatment without contacting any oxygen gas. Reaction conditions: mcat=100 mg, feed gas: 1% CO, 1% O2, 50% H2 and balance He, flow rate=80 mL/min. 61 ACS Paragon Plus Environment

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Fig. 6 Designed in-situ TPR characterization of CuCe (A) and CuCe-Fe (B) samples before (gray line) and after (red line) one CO pulse was introduced without contacting any oxygen gas. Fig. 7 (A) CO-TPD of CuCe and CuCe-Fe. In-situ DRIFTS spectra of CuCe (B) and CuCe-Fe (C) recorded under the reaction stream of 1% CO/1% O2/50% H2/He at the elevated temperature. Fig. 8 (A) CO conversion and (B) CO2 selectivity of CuCe and CuCe-Fe with the coexistence of H2O and CO2. (C) The stability test with time on stream for CuCe at 160 oC and CuCe-Fe at 155 oC, respectively. mcat=300 mg, feed gas composition: 1% CO, 1% O2, 50% H2, 15% CO2, 10% H2O and He as balance gas, flow rate=80 mL/min. Fig. 9 (A) CO-TPR profiles of fresh CuCe and FeCuCe samples as well as the pretreated FeCuCe sample (calcined in-situ in the atmosphere of pure N2 at 700 oC for 1 h). In-situ DRIFTS spectra of CuCe (B) and CuCe-Fe (C) recorded at the range of 2500-3200 cm-1 under the reaction stream of 1% CO/1% O2/50% H2/He. Fig. 10 (A) CO conversion and (B) products concentration of WGS reaction over CuCe and CuCe-Fe samples. Reaction conditions: mcat=300 mg, feed gas: 1% CO, 10 % H2O, and balance N2, flow rate=80 mL/min. (C) Raman spectroscopy of (a) pulsed CuCe (all the oxygen was consumed by CO pulsing), (b) pulsed FeCuCe, (c) pulsed FeCuCe after the reaction with 10% H2O at 140 oC for 3 h (balance with pure N2 to keep the flow rate of 80 mL/min). (D) H2 concentration of pulsed FeCuCe sample after the reaction with 10% H2O at 140 oC for 3 h. 62 ACS Paragon Plus Environment

Page 62 of 74

Page 63 of 74

CO Conversion (%)

100

(A)

80

CuCe CuCe-Fe

60 40 20 80

120

160 o

Temperature ( C)

100

CO2 Selectivity (%)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

200

(B)

80 60

CuCe CuCe-Fe

40 20 80

120

160 o

200

Temperature ( C)

Fig. 1 Lu et al

63 ACS Paragon Plus Environment

ACS Catalysis

(A)

CuO

CuCe-Fe

CeO2

CuCe







27

29



30

30

40





50

60

70

2-Theta (degree)

80

890

900

Fe 2p1/2

Fe

3+

713.4

Fe

2+

710.0

3+

Fe (sat) 719.4

910

Binding Energy (eV)

(D) Fe 2p3/2

u''

u'

v' v''

880

u'''

v''' u

CuCe v

(C)

Fe 2p

740

31

CuCe

 

20

28

CuCe-Fe

Intensity (a.u.)

Intensity (a.u.)



(B)

CuCe-Fe

Intensity (a.u.)



Intensity (a.u.)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 64 of 74

Cu LMM

+

Cu (569.7) Fe-CuCe

Cu 2p

CuCe

1+

Cu 2+ 932.2 Cu 933.4

2+

Fe (sat)

920

580

952.6

570

952.6

560

FeCuCe CuCe

shake-up

716.3

730

720

Binding Energy (eV)

710

930

940

950

Binding Energy (eV)

960

Fig.2 Lu et al

64 ACS Paragon Plus Environment

0.75

(A)

A599/A459

CuCeFe

300

0.60

463 459

0.45 0.30

CuCe CuCe-Fe

0.15 0.00

CuCe CuCe-Fe

599

CuCe

400

500

600

-1

700

800

Raman shift (cm ) 529.3 (B)

Intensity (a.u.)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

Normalized intensity (a.u.)

Page 65 of 74

CuCe-Fe

+0.4

528.9 OII

OI 526

O 1s

528

530

532

Binding Energy (eV)

CuCe 534

536

Fig. 3 Lu et al

65 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 66 of 74

Scheme 1 Lu et al 66 ACS Paragon Plus Environment

Page 67 of 74

(a)

H2 Consumption (a.u.)

H2 Consumption (a.u.)

CuCe CuCe-Fe

(A)

β

α

100

 200

300

400 500 600 700 o Temperature ( C)

800

300 400 o Temperature ( C)

500

700

(B)

OSC (umol CO2/g)

600 500

CuCe-150 FeCuCe-150 CuCe-200 FeCuCe-200

400 300 200 100 0

0

2

4

6

8

10

Pulse number

12

14

16

18

1000

OSC (umol CO/g)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

800

CuCe-150 FeCuCe-150 CuCe-200 FeCuCe-200

600 400 200 0

(C) 0

2

4

6

8

10

Pulse number

12

14

16

18

Fig. 4 Lu et al

67 ACS Paragon Plus Environment

200 300 o Temperature ( C)

600 500 400 300 200 100 0

CuCe-P150-2min FeCuCe-P150-1min

0 2 4 6 8 10 12 14 16 18 Pulse number

1000 P150-1-R220 P150-1-R160 P150-1 P150-0

200 300 o Temperature ( C)

(a) CuCe

40

(b) CuCe-150-2min

20 0

60

80 100 120 140 160 o Temperature ( C)

(C)

600 400

CuCe-P150-2min FeCuCe-P150-1min

200 0

400

80 60

800

(E)

100

(D) Conversion of CO (%)

700

400 100

(B)

OSC (umol CO/g)

P150-2-R220 P150-2-R160 P150-2 P150-0

CuCe-Fe

Page 68 of 74

0 2 4 6 8 10 12 14 16 18 Pulse number (F)

100

Conversion of CO (%)

(A) H2 Consumption (a.u.)

CuCe

100

OSC (umol CO2/g)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

H2 Consumption (a.u.)

ACS Catalysis

80

(a) FeCuCe

60 40

(b) FeCuCe-150-1min

20 0

60

80 100 120 140 160 o Temperature ( C)

Fig.5 Lu et al

68 ACS Paragon Plus Environment

Page 69 of 74

H2 Consumption (a.u.)

(A)

CuCe CuCe-one pulse

100

200

300 o

400

Temperature ( C)

(B)

H2 Consumption (a.u.)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

CuCeFe CuCeFe-one pulse 100

200

300 o

400

Temperature ( C)

Fig.6 Lu et al 69 ACS Paragon Plus Environment

ACS Catalysis

Intensity (a.u.)

(A) (b) CuCe-Fe

(a) CuCe 50

100

150

200

Temperature ( C)

(B)

1579

Absorbance (a.u.)

1294

o

o

210 C o 190 C o 170 C o 150 C o 130 C o 110 C

250

300

CuCe

2105

o

90 C o

70 C o

50 C o

30 C

1200

1600

2000

2400

-1

Wavenumber (cm )

(C) 1294

Absorbance (a.u.)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 70 of 74

1579

o

210 C o 190 C o 170 C o 150 C o 130 C

2100

CuCe-Fe

o

110 C o

90 C o

70 C o

50 C o

30 C

1200

1600

2000 -1

2400

Wavenumber (cm )

Fig.7 Lu et al

70 ACS Paragon Plus Environment

Page 71 of 74

(A) 100

CO Conversion (%)

80 60

CuCe with H2O and CO2

CuCe-Fe with H2O and CO2

40 20 100

(B)

120

140

160

o

Temperature ( C)

80

CO2 Selectivity (%)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

60 40

CuCe with H2O and CO2 CuCe-Fe with H2O and CO2

20 100

(C)

120

140

160

o

Temperature ( C)

100

CO Conversion

80 CO2 Selectivity

60

CuCe-Fe CuCe

40 20

0

100

200

Time (h)

300

400

Fig. 8 Lu et al

71 ACS Paragon Plus Environment

ACS Catalysis

(A) H2 signal (a.u.)

CuCe FeCuCe FeCuCe o (700 C 1h)

80

120

160

200

240

o

280

Temperature ( C)

(B)

2852 2965 2842 2932

Intensity (a.u.)

CuCe

2600

(C)

FeCuCe

2800

3000 -1

Wavenumber (cm )

2856 2967 2843 2935

Intensity (a.u.)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

Page 72 of 74

210 190 170 150 130 110 90 70 50 30 3200

210 190 170 150 130 110 90 70 50 30

2600

2800

3000 -1

3200

Wavenumber (cm )

Fig. 9 Lu et al

72 ACS Paragon Plus Environment

CO Conversion (%)

100

(A)

CuCe FeCuCe

80 60 40 20 0 120

140

160

180

200

o

220

240

5000

CuCe-CO2

(C)

4000

CuCe-H2

3000

FeCuCe-H2

2000 1000

260

0 120

140

160

H2 concentration (ppm)

(c)

1360-1400

o

(a) Pulsed CuCe at 140 C o

(b) Pulsed FeCuCe at 140 C (c) Reacted FeCuCe

1000

1200

1400

1600 1800 -1 Raman Shift (cm )

200

o

10

(b)

1480-1520

180

220

240

260

Temperature ( C)

(a) 1580-1640

(B)

FeCuCe-CO2

Temperature ( C)

Intensity (a.u.)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

ACS Catalysis

Products Concentration (ppm)

Page 73 of 74

2000

(D)

8

FeCuCe sample after the CO pulsing

6 4 2 0

0

40

80

120

Time (min)

160

200

Fig. 10 Lu et al

73 ACS Paragon Plus Environment

ACS Catalysis 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60

297x112mm (300 x 300 DPI)

ACS Paragon Plus Environment

Page 74 of 74