TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Ratio: The ratio of a mole number of a manganese to a mole number of total of manganese and zirconium is 0.1-0.62, preferably 0.17-0.5. The ratio of a mole number of copper to a mole number of total of copper and zinc is 0.2-0.6, preferably 0.3-0.48.Preferred Process: The mixed oxide is washed and filtered by maintaining the mixed oxide at 70-90 degreesC for 20-60 minutes, repeatedly. The mixed oxide material is obtained by washing and filtering, and is dried at 100-150 degreesC. The mixed oxide is then baked at 200-700 degreesC for 1-3 hours. Hydrogen reduction of the mixed oxide material is performed after baking at 200-400 degreesC. EXAMPLE - A CuOx/ZnO/ZrO2/MnOx precursor was obtained by dissolving predetermined amounts of copper nitrate (Cu(NO3)2.3H2O), zinc nitrate (Zn(NO3)2.6H2O), zirconium nitrate (ZrO(NO3)2.2H2O) and manganese nitrate (Mn(NO3)2.6H2O) in distilled water, and then adding a predetermined amount of sodium carbonate aqueous solution into the formed solution. The precursor solution including the supernatant was heated at 70 degreesC for 30 minutes, washed and filtered repeatedly. The resultant sediment was dried at 120 degreesC for 24 hours or more, and filtered to remove sodium ions through dissolution into water. The dried powder was baked at 350 degreesC for 2 hours, and a methanol reforming catalyst of CuOx/ZnO/ZrO2/MnOx, was obtained. The methanol reforming catalyst was subjected to hydrogen reduction at 200-400 degreesC.    Steam reforming of methanol in a mixture gas maintained at 250 degreesC, and having a ratio of mole number of water to mole number of methanol of 2, and ratio of number of oxygen atoms to number of carbon atoms in methanol of 0.23, was performed, in a liquid hourly space velocity with respect to methanol in conversion to liquid of 2l/h. Durability of the catalyst was determined by maintaining the mixture gas at 350 degreesC before steam reforming of methanol in the mixture gas in the presence of the catalyst. The methanol reforming catalyst exhibited high methanol reforming ratio. The catalyst had excellent durability, since manganese and/or yttrium contained in the catalyst decomposed acetic acid produced as by-product in very small amount in the steam reforming reaction of methanol, at lower steam reforming temperature. Deterioration of catalytic capability of the methanol reforming catalyst by copper acetate formed by reaction of produced acetic acid with copper in the methanol reforming catalyst was prevented. The methanol reforming catalyst obtained after baking was used immediately without being further processed. The methanol reforming catalyst was coated on the surfaces of the monolithic honeycomb such as a honeycomb tube, and monolithic catalyst was formed. The degree of freedom in designing the contact area per unit volume was increased, so that the steam reforming of methanol was efficiently performed. Since methanol reforming catalyst was subjected to hydrogen reduction at 200-400 degreesC, the methanol reforming catalyst does not undergo sintering with sharp temperature rise at the start of the use of catalyst.