Abstract: A petroleum distillate feed is upgraded and a substantial C.sub.3 -C.sub.4 olefin product fraction produced by contacting the feed with ZSM-5 type zeolite at (1) a temperature in the 500.degree.-800.degree. F. range, (2) a pressure below about 13 atmospheres gauge, and (3) an LHSV in the 0.1-15 V/V/Hr range, and fractionating the effluent product stream.

Abstract: A catalytic process for hydrocracking C.sub.5.sup.+ hydrocarbons or mixtures thereof into a C.sub.2 -C.sub.5 mixture paraffin stream in the presence of a palladium/Group IIA, e.g. Be Mg, or IIIB, e.g. Sc, Y, ZSM-20 hydrocracking catalyst, and thermally cracking this mixture to recover ethylene and propylene.

Abstract: A hydrocarbon feedstock derived from crude oil or other sources is subjected continuously to thermal cracking under pressure and in the presence of hydrogen in order to convert the feedstock to products of lower molecular weight containing high proportions of olefinic components. In a first processing step, a catalytic hydrogenating pretreatment is performed at a temperature within the range of 300.degree. C. to 600.degree. C. and under a pressure within the range of 12 to 85 bars. In a second step, a thermal cracking treatment is performed under a pressure within the range of 10 to 70 bars with residence times of less than 0.5 second and at a temperature within the range of 625.degree. C. to 1,000.degree. C., the quantity of hydrogen employed being such that the molar concentration in the effluents is at least equal to 20%.

Abstract: A catalytically hydrogenated naphtha stream containing less than 10 ppm by weight of sulfur is pyrolyzed without added hydrogen to a product including ethylene. Selectivity to ethylene is increased by adding a sulfur compound to increase the sulfur content to above 20 ppm by weight based on hydrogenated naphtha. Addition of the sulfur compound increases the quality of hydrogenated naphtha as a pyrolysis feedstock nearly to that of a C.sub.2 to C.sub.5 paraffin stream.

Abstract: The present process has for object the manufacture of olefinic hydrocarbons with respectively 2 and 3 carbon atoms per molecule. This object is attained by treating a charge selected from such cuts as light or heavy naphthas, kerosenes and light gas oils of distillation point lower than 360.degree. C. The cut is subjected to hydrogenolysis and the resulting C.sub.2 and C.sub.3 hydrocarbons are fed to a steam-cracking plant, while the C.sub.4.sup.+ hydrocarbons are subjected to further hydrogenolysis.

Abstract: A process for thermal cracking of petroleum light gas oil to produce a product including ethylene comprising passing said oil, a diluent gas and entrained hot solids through a cracking zone at a temperature between 1,300.degree. and 2,500.degree. F. at a relatively high cracking severity corresponding to a methane yield of at least 12 weight percent based on hydrocarbon feed oil and with a weight ratio of diluent gas to feed oil of at least 0.3. A naphtha feedstock can be separately cracked at a lower severity using a lower weight ratio of diluent gas to feed oil, with the inert solids from both cracking zones being sent to a common burner whose fuel comprises heavy oil product from both cracking zones.

Abstract: A process for the production of low sulfur, low nitrogen fuels at low hydrogen consumption by splitting a feed into two components, a high boiling component, suitably a 1050.degree. F.+ fraction, and a low boiling component, suitably a 1050.degree. F.- fraction, and processing the two different components over two different types of catalysts, at different severities. Suitably, on the one hand, the high boiling component is treated over a large pore metal hydrogenation catalyst at severity sufficient to convert at least 30 percent, preferably at least 50 percent of the feed, based on the weight of the feed, to a 1050.degree. F.- product. The 1050.degree. F.- product from the conversion over the large pore metal hydrogenation catalyst is then blended with the low boiling component split from the original feed, and the blended low boiling material is then treated at low severity over a small pore metal hydrogenation catalyst to hydrodesulfurize and hydrodenitrogenate said low boiling components.

Abstract: A method for catalytically cracking an isolated reactant feed, 80-100 volume percent of which is a substantially mono-aromatic hydrocarbon fraction boiling in the boiling range of heavy gasoline and the remainder of which is a vaporizable hydrocarbon fraction, under effective cracking conditions of cracking temperature, catalyst composition, catalyst activity, catalyst-to-feed weight ratio, and weight hourly space velocity, to produce an isolated product having increased low molecular weight olefin and low molecular weight mono-aromatic contents and a reduced sulfur content and having a high octane rating.

Abstract: A thermal cracking process comprising thermally cracking a non-deasphalted residual oil in a thermal cracking zone containing a fixed bed of inert solids.

Abstract: A process for the production of ethylene by the non-catalytic riser cracking of hydrodesulfurized residual petroleum oils in the presence of entrained hot, inert solids.

Abstract: A process for producing and upgrading carbonaceous tars including adding the carbonaceous material into a first reaction zone of a reactor having at least two reaction zones; adding hot hydrogen to the stream of carbonaceous material to effect a reaction with same to produce reaction products; quenching the mixture while insuring that the total residence time varies from about 2 milliseconds to about 2 seconds; removing at least a portion of the reaction products from the quenched mixture; introducing the residual carbonaceous material into a subsequent reaction zone and repeating the steps for the subsequent reaction zone; and introducing carbonaceous tars produced directly into a fluid coking zone to obtain gas, upgraded coal tars, and hot coke.

Abstract: Residual hydrocarbons stocks obtained after atmospheric distillation are converted into light distillates by certain sequences of processing steps including catalytic cracking, high and low pressure catalytic hydrotreatment, deasphalting, gasification and thermal cracking or coking.

Abstract: A process for producing a low sulfur content fuel oil in a high yield from a starting oil having a high sulfur content, which comprises (1) treating a residual petroleum oil with hydrogen at a temperature of about 350.degree. to 450.degree. C and a pressure of about 50 to 200 Kg/cm.sup.2 at a liquid hourly space velocity of about 0.2 to 4 l/H.l in the presence of a catalyst, (2) introducing an inert gas or steam at a temperature of about 400.degree. to 900.degree.C and pyrolyzing the treated oil at a temperature of about 350.degree. to 500.degree.C and at a pressure of about atmospheric pressure to 100 Kg/cm.sup.2 with a residence time of about 0.5 to 10 hours, and (3) hydrodesulfurizing the pyrolyzed oil at a temperature of about 300.degree. to 400.degree.C and a pressure of about 30 to 100 Kg/cm.sup.2 at a liquid hourly space velocity of about 0.5 to 4 l/H.l in the presence of a desulfurizing catalyst.

Abstract: A catalytic process for hydrocracking crude oil fractions into a C.sub.2 -C.sub.5 alkane mixture having a normal paraffin to isoparaffin molar ratio greater than about 3:1 and thermally cracking this mixture to recover ethylene and propylene.The hydrocracking catalysts used are made from a Group VIII metal, a Group VI B metal or mixtures thereof, with a halogen supported on a silica-alumina support or a natural or synthetic faujasite. The catalysts must be sulfided prior to or during use.