Abstract:
To obtain olefins by the thermal cracking of hydrocarbons, e.g., vacuum gas oil, by hydrogenation and subsequent steam cracking, an intermediate fractionation of the hydrogenate is provided so that the light fraction enriched in branched isomers can be used as fuel and the heavy fraction only is subjected to the steam cracking.
Abstract:
In a process for the production of olefins in two stages wherein, in the first stage, heavy petroleum fractions are hydrogenated in the presence of hydrogen and a hydrogenation catalyst and, in the second stage, the thus-hydrogenated fractions are subjected to thermal cracking in the presence of steam, the improvement which comprises employing as the hydrogenation catalyst a support-free catalyst consisting essentially of elements from Groups VIb, VIIB, and VIII of the periodic table of the elements in the form of the metals, metal oxides, metal sulfides, or organometal complexes, or mixtures thereof.
Abstract:
To obtain olefins by the thermal cracking of hydrocarbons, e.g., vacuum gas oil, by hydrogenation and subsequent steam cracking, an intermediate fractionation of the hydrogenate is provided so that the light fraction enriched in branched isomers can be used as fuel and the heavy fraction only is subjected to the steam cracking.
Abstract:
In a process for the production of olefins in two stages wherein, in the first stage, heavy petroleum fractions are hydrogenated in the presence of hydrogen and a hydrogenation catalyst and, in the second stage, the thus-hydrogenated fractions are subjected to thermal cracking the presence of steam, the improvement which comprises employing as the hydrogenation catalyst a zeolite of the faujasite structure combined with elements from Groups VIB, VIIB and VIII of the periodic table of the elements, wherein the alkali component of the zeolite is exchanged at least partially for ammonium, hydronium, alkaline earth and/or rare earth ions, and the elements are present in a metallic, ionic, oxidic and/or sulfidic form.
Abstract:
A catalyst for decreasing the content of nitrogen oxides in flue gases. The catalyst contains at least one of the metals titanium, zirconium, vanadium, tungsten, molybdenum, or cerium in the form of one or more of their oxides combined with a silicate with a three-layer structure (three-layer silicate) selected from the group consisting of illite and mica. The atomic ratio of the silicon in the three-layer silicate to the metal in the oxide is from 0.2 and 50 and preferably from 0.4 to 25.
Abstract:
A process for the treatment of a hydrocarbon fraction having a boiling point range beginning above 200.degree. C. and obtained in the cracking of hydrocarbons, in which the polymeric component resulting from the cracking pyrolysis is removed and the remaining polymer-free hydrocarbon is subjected to hydrogenation under such reaction conditions that the product is high in monoaromatic components while the polyaromatics are removed therefrom.
Abstract:
A catalyst based on crystalline aluminosilicates of the pentasil type, having an Si/Al atomic ratio of at least 10, has the structure of primary crystallites of a mean diameter of at least 0.1 micron and at most 0.9 micron, which crystallites are partially combined into agglomerates the primary crystallites and/or agglomerates being mutually joined by finely disperse alumina obtainable by hydrolysis of aluminum-organic compounds, the BET surface area of the catalyst being 300 to 600 m.sup.2 /g and its pore volume (determined by mercury porosimetry) being 0.3 to 0.8 cm.sup.3 /g.
Abstract:
A process for decreasing the content of nitrogen oxides in flue gases. The process comprising contacting the flue gases with a catalyst. The catalyst contains at least one of the metals titanium, zirconium, vanadium, tungsten, molybdenum, or cerium in the form of one or more of their oxides combined with a silicate with a layer structure (layer silicate) comprising acid-activated kaolin. The crystalline layer structure of the acid-activated kaolin is essentially retained, while being not yet X-ray amorphous. The acid activation increases the BET surface area at least 15% and preferably at least 50% in terms of the BET surface area of the kaolin before acid activation. The atomic ratio of the silicon in the acid-activated kaolin to the metal in the oxide is from 0.2 and 50 and preferably from 0.4 to 25.
Abstract:
A catalyst for lowering the nitrogen oxide content of flue gases contains as the active component an acid-activated layer silicate, in particular of the smectite type, whose layered structure is to a large extent intact after the acid treatment.
Abstract:
A ferruginous catalyst for decreasing the content of nitrogen oxide in flue gases. The catalyst comprising an active constituent in the form of a combination of a compound of iron and of an acid aluminosilicate that has a layered structure.