초록 ▼

The process combines hydroconversion and catalytic cracking starting from a feed containing triglycerides, at concentrations of fatty acids above 85%, which maximizes the yields of light olefins, chiefly ethylene and propylene, while reducing the yield of gasoline, with conversion greater than 80 wt

The process combines hydroconversion and catalytic cracking starting from a feed containing triglycerides, at concentrations of fatty acids above 85%, which maximizes the yields of light olefins, chiefly ethylene and propylene, while reducing the yield of gasoline, with conversion greater than 80 wt. %.

대표청구항 ▼

1. Process for production of light olefins from a feed containing triglycerides, characterized in that it maximizes the production of ethylene and propylene comprising the following steps: a) hydroconversion of a feed containing triglycerides with fatty acids of C9-C18 carbon chain, in contact with

1. Process for production of light olefins from a feed containing triglycerides, characterized in that it maximizes the production of ethylene and propylene comprising the following steps: a) hydroconversion of a feed containing triglycerides with fatty acids of C9-C18 carbon chain, in contact with a hydrogen-rich gas stream, on a catalyst of metal oxides to produce: a fraction of fuel gas and water vapour; a gaseous fraction constituted principally of propane; and a liquid fraction of saturated hydrocarbons and dissolved gases;b) separation of the liquid fraction of saturated hydrocarbons comprising predominantly C9-C18 linear carbon chains; andc) fluid catalytic cracking of the separated liquid fraction, in petrochemical conditions, with a catalyst bed constituted predominantly of zeolites, in proportions between 30 and 70 wt. %, temperature at reactor outlet between 450° C. and 620° C., residence time between 1 and 10 seconds inside the reactor and with injection of steam between 5 and 50 wt. % relative to the feed entering the reactor. 2. Process according to claim 1, characterized in that the feed contains triglycerides with fatty acids of (C9-C18) carbon chain obtained from vegetable and/or animal biomass. 3. Process according to claim 1, characterized in that the feed contains triglycerides with concentrations of fatty acids above 65 wt. %. 4. Process according to claim 1, characterized in that the feed is selected from soya oil (Glycine max), castor oil (Ricinus communis), cottonseed oil (Gossypium hirsutum or G. barbadenseis), oil of Brazilian oil palm (Elaies guinensis), pine oil (tall oil), sunflower oil (Helianthus annuus), oil of Barbados nut or Physic nut (Jatropha curcas), seaweed oil, tallow and other oils of animal or vegetable origin. 5. Process according to claim 1, characterized in that the feed comprises a single oil or a mixture of two or more oils, in any proportions. 6. Process according to claim 1, characterized in that the triglycerides are fully hydrogenated in the hydroconversion step, in conditions of temperature between 280° C. and 370° C., hydrogen partial pressure between 1 MPa and 10 MPa and space velocity LHSV between 0.5 and 2.5 h−1, defined in accordance with the molecular structure of the triglycerides in the feed, on a catalyst bed of sulphided metal oxides supported on gamma alumina, MgO or silica/alumina. 7. Process according to claim 2, characterized in that the metal oxides are selected from the pairs Ni and Mo, Co and Mo, or Ni and W. 8. Process according to claim 1, characterized in that the liquid fraction of saturated hydrocarbons is produced in the hydroconversion step at yield above 80%. 9. Process according to claim 1, characterized in that the liquid fraction is constituted predominantly of saturated linear (C9-C18) hydrocarbons. 10. Process according to claim 1, characterized in that the catalyst contains zeolite that is selective for light olefins with silica-alumina ratio equal to 10 or more. 11. Process according to claim 10, characterized in that the element phosphorus is incorporated in the catalyst by treatment of the zeolites. 12. Process according to claim 10, characterized in that the catalyst contains zeolite that is selective for light olefins in proportions between 1 and 55 wt. % relative to the total zeolites in the catalyst. 13. Process according to claim 1, characterized in that the LCO produced in the catalytic cracking step is recycled to the reactor to increase the production of light olefins. 14. Process according to claim 1, characterized in that the propane fraction generated in the hydroconversion step is incorporated in the stream of propane produced in the process. 15. The process according to claim 10, characterized in that the catalyst contains zeolite that is ZSM-8, ZSM-11 or ZSM-12. 16. The process according to claim 10, characterized in that the catalyst contains zeolite that is ZSM-5 (MFI). 17. The process according to claim 1, characterized in that the production of light olefins has a degree of conversion greater than 80 wt. %. 18. The process according to claim 17, characterized in that the production of light olefins has a degree of conversion greater than 90 wt.%.