TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Catalyst: The catalyst comprises (wt.%): the active component (0.1-5); the first additive (2-4); and the second additive (30-60; 40-60 mole% of the total amount in moles of the second additive). The first additive is at least partly dispersed on the surface of the second additive, or partly enters the second additive to form a composite material. The second additive is a complete two-member or three-member composite formed by CeO2 and oxide(s) of other metal(s); or a microcrystalline mixture of CeO2 and oxide(s) of other metal(s) (preferably a single-phase solid solution of CeO2 and oxide(s) of other metal(s)). The catalyst is free of components other than the active component, the first additive and the second additive; where the second additive acts as a physical support of the active component. The catalyst further comprises an inert support material that acts as a physical support for the active component, the first additive and the second additive; and is present in a pellet form. The catalyst is in a monolithic form, and the inert support material is selected from a ceramic honeycomb, a metal honeycomb, or a metal foam. The catalyst precursor (A1), and the catalyst and reduced catalyst are present in a powder form. Preferred Components: The active component is selected from Pt, Pd, Ru, Rh, and/or Ir, or their combination (preferably Rh, or combination or mixture of Rh-Pd, Rh-Ir, or Rh-Pt). The first additive is selected from Na2O, K2O, MgO, CaO, SrO, and/or BaO, or their combination (preferably K2O, MgO and/or CaO, or their combination). The second additive is a two- or three-member composite material of CeO2, and an oxide of a metal selected from La, Pr, Nd, Sm, Eu, Gd, Y, Zr or their combination (preferably two-member composite oxide selected from Ce-Zr, or Ce-Sm; or a three-member composite oxide of Ce-Zr-Y). The inert support material is selected from alpha -Al2O3, MgAl2O4, or CaTiO3. Preferred Process: The step (a) involves: (i) preparing an aqueous solution comprising urea, a salt of Ce, a salt of another lanthanide and/or another transition metal, (ii) heating the solution obtained in the step (i) until urea decomposes, and the solution undergoes a homogeneous-phase precipitation, to obtain a precursor of a CeO2-based composite oxide, and (iii) drying and calcining the precursor obtained in the step (ii) to obtain the catalyst precursor (A1); (ia) preparing an aqueous emulsion comprising a salt of Ce, a salt of another lanthanide and/or another transition metal, a surfactant, a co-surfactant, and an oil-phase solvent, (iia) preparing an aqueous emulsion comprising an ammonia, a surfactant, a co-surfactant, and an oil-phase solvent, (iiia) mixing the emulsions obtained in the steps (ia) and (iia), (iva) separating the precursor of CeO2-based composite oxide material formed in the mixed emulsion obtained in the step (iiia), and (va) drying and calcining the precursor of CeO2-based composite oxide material obtained in the step (iva) to obtain the catalyst precursor (A1) in powder form; or (ib) preparing an aqueous solution comprising a salt of Ce, a salt of another lanthanide and/or another transition metal, (iib) adding ammonia into the solution of the mixed salts obtained in the step (ib) until a precipitate of a precursor of a CeO2-based composite oxide is obtained, and (iiib) drying and calcining the precursor of the CeO2-based composite oxide obtained in step (iib) to obtain the catalyst precursor (A1) in powder form. The step (a) further involves loading the CeO2-based composite oxide material onto the catalyst support, followed by drying and calcination, to obtain a catalyst precursor (A2); and involves (a') providing alpha -Al2O3, MgAl2O4, CaTiO3, or another refractory material as the catalyst support; (b') loading a sol or an aqueous slurry comprising cerium, another lanthanide and/or another transition metal onto a monolithic catalyst support; (c') preparing an aqueous solution comprising a salt of Ce, a salt of another lanthanide and/or another transition metal, adding ammonia into the obtained solution of the mixed salts until a gel is obtained, and adding nitric acid (HNO3) into the obtained gel; (d') loading an aqueous slurry comprising powdered CeO2-based composite oxide material, CeO2-based composite oxide sol, and nitric acid, onto the catalyst support; or (e') homogeneous precipitation, co-precipitation, or microemulsion for the preparation of CeO2-based composite oxide material in the aqueous slurry (preferably the step (c')). EXAMPLE - A Rh/MgO/Ce0.5Zr0.5O2/cordierite ceramic honeycomb catalyst, was prepared as follows. A precut cordierite ceramic honeycomb support (pore density 400 pores/square inch, 400 cpsi) was pre-treated using a 3% nitric acid solution, washed clean using deionized water, then dried at 120 degrees C for 2 hours, and calcined at 900 degrees C for 2 hours. A Ce-Zr composite oxide Powder A (12 g), Ce-Zr colloidal sol with a 1/1 Ce/Zr mole ratio (17 ml), and HNO3 solution (pH = 1.2, 5 ml) were mixed with deionized water (10 ml), and ball milled using a wet ball miller for 12 hours, to obtain an aqueous slurry containing the Ce-Zr composite oxide. The pH of the slurry prepared was adjusted to 3.5-4 using an amount of deionized water and HNO3 solution (pH = 1.2), to obtain the Ce-Zr aqueous slurry (50 ml) for impregnating the honeycomb support. The powder A was prepared as follows. (NH4)2Ce(NO3)6 (54.823 g), Zr(NO3)4-5H2O (42.914 g), and urea (180 g) were dissolved in deionzed water (1500 ml) to form an aqueous mixture solution. The solution was then heated with stirring until urea decomposed. After a precipitate was formed, it was then stirred and boiled (100 degrees C) for 2 hours, then heating was stopped and stirring continued for 2 hours. The precipitate prepared was suctioned and filtered. The filter cake was thoroughly washed in stirred boiling water (750 ml) twice. After each washing, deionized water (500 ml) was added for filtering again. After washing and filtering twice using deionized water, isopropanol (150 ml) was directly poured over the filter cake, and then completely filtered off. The precipitate obtained was dried in a vacuum dryer at 60 degrees C for over 20 hours, then heated in a muffle furnace at a temperature elevation rate of 2.5 degrees C/minute until reaching 500 degrees C, where it was calcined over 2 hours, to obtain a Ce-Zr composite oxide powder A (29.321 g; having specific surface area of 120.4 m2/g, and a particle size of 6-7 nm, and including ZrO2 completely entered in the crystal lattice of CeO2, such that the CeO2 and ZrO2 formed a single-phase solid solution). A ceramic honeycomb support (0.7448 g) was immersed in the Ce-Zr slurry, with stirring the slurry; 3 minutes after the immersion, the honeycomb was taken out, the excess slurry in the channels of the ceramic honeycomb was purged using compressed air, and then the coated honeycomb support was rapidly microwave-dried for 3 minutes. The honeycomb was then calcined at 750 degrees C in a muffle furnace for 2 hours and to obtain a catalyst intermediate with Ce0.5Zr0.5O2 load (0.085 g). The process was repeated 8 times and a catalyst intermediate with Ce0.55Zr0.5O2 load (0.602 g) was obtained. The catalyst intermediate obtained was then immersed in 2.7 M Mg(NO3)2 solution (50 ml), and loaded with MgO (0.035 g) similarly. Then, similarly the MgO-loaded catalyst intermediate was loaded with Rh2O3; by using an impregnation solution (50 ml) of RhCl3 containing Rh (23 mg/ml). After microwave-drying and calcination at 750 degrees C for 2 hours, a ceramic honeycomb catalyst with the precious metal in oxidized state was obtained. The catalyst was then reduced at 700 degrees C for 2 hours using a 10% H2-90% N2 gas mixture, to obtain a catalyst comprising elemental precious metal with having a composition of 0.33% Rh/2.52% MgO/43.42% Ce0.5Zr0.5O2/53.70% cordierite. The catalyst obtained was used as an amplified autothermal reforming (ATR) catalyst; and used in the methane ATR hydrogen system for a fuel-cell system, under the working conditions of methane gas hourly space velocity (GHSV) of 4300 hour-1, O2/C in the feedstock gas of 0.44, H2/C in the feedstock gas of 2.2, temperature at the center of reaction bed of 800 degrees C, and atmospheric reaction pressure. The process resulted in the reformate gas having a dry composition of H2 (45.46%), CO (8.19%), CO2 (9.6%), and CH4 (0.56%), N2 (balance).