TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The supports used are preferably powder charcoal, aluminum silicate, alumina, clays, zeolites, and molecular sieves.    TECHNOLOGY FOCUS - METALLURGY - Preferred Components: The transition metals supported on the catalyst belong to group VIII-B of the periodic table of the elements (preferably palladium, ruthenium, nickel or rhodium). The metal is present in the catalyst formulation of 0.1 -10 (preferably 1 -5) wt.% by weight in the metal catalyst.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: In step a) pre-treatment of the catalyst is carried out preferably at 250-550 degrees C. In step b) the reaction temperature is preferably at 225-350 degrees C. In step c) the pressure is preferably 0.9-980 KPa (0.01-10 kgf/cm2). In step d) the molar ratio glycerine/H2 is preferably of 1:30-1:240. In step e) the space speed is more specifically comprised of 2-20 h-1. The process uses glycerine obtained by processes of transesterification of soybean, castor, Barbados nut, palm, African palm oil, rape, cottonseed, sunflower, canola, babassu, coconut oils, or from the transesterification of vegetable oils used for frying, animal fat and from domestic or industrial sewage, the glycerine is previously neutralized before hydrogenation/hydrogenolysis. The glycerine is converted into oxygenated compounds and hydrocarbons containing 1-3 carbon atoms (preferably propene, propane, propyleneglycol, ethyleneglycol, acetol ( alpha -hydroxy-acetone), acetone, acetaldehyde, ethanol, ethane and methane. The compounds are obtained at a conversion percentage of 10-100%. The hydrogenation reaction takes place in a system where the catalyst is a fixed bed system within the reactor. Preferred Components: The glycerine feedstock is in the form of an aqueous solution in concentration of 30-100 wt.% of glycerine. EXAMPLE - A portion of the catalyst containing 5% palladium supported on alumina was charged into the fixed bed catalytic reactor, and was pre-treated at 550 degrees C for 30 minutes at a heating rate of 10 degrees C/minute under a continuous flow of H2 (40 ml/minute), for reduction of metal sites to take place. The hydrogenation/hydrogenolysis reaction was carried out under a continuous flow of a glycerine feedstock under hydrogen (H2). Glycerine was introduced into the hydrogen gas stream and onto the catalytic bed by an injection bomb. The products were analyzed by a gas chromatograph equipped with a 50 m capillary column of methyl-silicone and a flame ionization detector (DIC), coupled in-line with the catalytic test unit. The conversion and selectivity parameters of the catalyst containing 5% palladium supported on alumina were evaluated according to catalytic tests at 300 degrees C, with varying feedstock space speed in order to maximize propene production. The influence of the space speed (WHSV) on the resulting products was verified by applying values 4.8-6.4 h-1. Under the best reaction conditions used, glycerine conversion was 100%. The products detected were methane, ethane, propane and propene.