Abstract: In the delayed coking of a coking feedstock wherein the feedstock is continuously heated in a coking heater and introduced into a coke drum, the heater is operated to provide a coke drum temperature of from 415.degree. to 455.degree. C., and, after filling of the drum to the desired level, feedstock introduction is discontinued and the coke drum contents are heated at a temperature of 450.degree. C. to 500.degree. C., and which heating temperature is at least 10.degree. C. greater than the coking temperature, by passing a non-coking vapor through the contents of the drum to reduce the volatile combustible matter content to a value of 4% to 10% by weight and thereby reduce the CTE of the formed coke. The process is applicable to the production of needle coke from various kinds of feedstocks, in particular from a petroleum feedstock wherein the feedstock is initially treated by thermal soaking in the presence of sulfur, followed by thermal cracking to increase the aromaticity.

Abstract: Arsenic is removed from a hydrocarbon containing arsenic as an impurity; e.g., shale oil, by contact with hydrogen in the presence of a contact material, such as coke, to deposit the arsenic on the contact material. The arsenic deposited on the contact material is subsequently reacted with an iron compound to produce an iron-arsenic compound suitable for disposal.

Abstract: In a hydrogenation operation employing an ebullated catalytic bed, recycle is recovered from the hydrogenated product with at least 25%, by volume, of the recycle boiling above 950.degree. F. The recycle is cooled to a temperature of from 350.degree. to 600.degree. F. to separate coke precursors, prior to recycle to the hydrogenation. Higher conversion levels can be achieved by effecting recycle in such manner.

Abstract: A portion of a steam pyrolysis tubular coil, preferably the outlet portion, is provided with an insert to provide a radiation absorption surface within the tube. The insert is dimensioned to increase heat flux without adversely increasing pressure drop. A preferred insert has a central body and outwardly extending vanes in contact with the interior of the coil.

Abstract: A compound is chlorinated with chlorine to produce chlorinated product and hydrogen chloride byproduct. Recovered hydrogen chloride byproduct is contacted with oxygen and a molten salt mixture containing the higher and lower valent chlorides of a multivalent metal, such as cuprous and cupric chloride, to effect recovery of the hydrogen chloride by enriching the molten salt content of the higher valent chloride. The molten salt, enriched in higher valent chloride, is then dechlorinated by use of a stripping gas, preferably hydrogen chloride, to produce a gaseous effluent containing stripped chlorine and the stripping gas, which is then recycled to the chlorination step. The presence of stripping gas, as a diluent, improves the chlorination operation.

Abstract: In the liquefaction of a sub-bituminous and/or lignitic coal, an ash containing coal liquid is heated to a temperature of from 410.degree. C. to 450.degree. C., and delayed coked adiabatically at a pressure of from 15 psig to 120 psig to produce an ash containing soft coke, having a volatile matter content of above 16% and generally no greater than 30%, all by weight, which is particularly suitable as a blending stock for the production of metallurgical coke.

Abstract: Coal is catalytically hydroliquefied by passing coal dispersed in a liquefaction solvent and hydrogen upwardly through an expanded catalyst bed in a stream having a cross-sectional flow area of no greater than 255 inches square, with the stream through the catalyst bed having a length and a liquid and gas superficial velocity to maintain an expanded catalyst bed and provide a Peclet Number of at least 3. If recycle is employed, the ratio of recycle to total feed (coal and liquefaction solvent) is no greater than 2:1 based on volume. Such conditions provide for improved selectivity to liquid product to thereby reduce hydrogen consumption.

Abstract: Coal is catalytically hydroliquefied by passing coal dispersed in a liquefaction solvent and hydrogen upwardly through a plurality of parallel expanded catalyst beds, in a single reactor, in separate streams, each having a cross-sectional flow area of no greater than 255 inches square, with each of the streams through each of the catalyst beds having a length and a liquid and gas superficial velocity to maintain an expanded catalyst bed and provide a Peclet Number of at least 3. If recycle is employed, the ratio of recycle to total feed (coal and liquefaction solvent) is no greater than 2:1, based on volume. Such conditions provide for improved selectivity to liquid product to thereby reduce hydrogen consumption. The plurality of beds are formed by partitions in the reactor.

Abstract: Vanadia supported on a silica-alumina or gamma-alumina support in an amount to provide a vanadia to support weight ratio ranging from about 0.3:1 to about 3:1 substantially entirely within the pores of the support, the vanadia having been placed in molten form substantially within the pores of a support having a surface area greater than about 50 m.sup.2 gram, a porosity greater than about 0.4 cc/gram which further includes an alkali metal, with the vanadium metal to alkali metal mole ratio being from 2:1 to 30:1. At least a portion of the alkali metal is preferably in the form of alkali metal vanadate. The catalyst is used for the production of nitriles from a compound containing at least one alkyl group.

Abstract: A metal containing hydrocarbon feedstock, such as a heavy residue, is contacted with hydrogen and a material characterized by low porosity, less than 0.3 cc/gram; low surface area, less than 5 m.sup.2 /g; high average pore diameter, greater than 1,000 Angstroms; and a high distribution of large pores, at least 40%, and preferably 50 to 80% of pores greater than 10,000 Angstroms. A preferred material is coke.

Abstract: Acid gases are removed from a coal gasification gas, followed by contacting the gas with a reduced iron catalyst at conditions selected to primarily produce methane, and some olefins together with carbon dioxide as byproduct. After separation of carbon dioxide byproduct, the gas is contacted with a nickel catalyst under methanation conditions to produce additional methane and convert olefins to alkanes to thereby produce a pipeline gas having an increased heating value.

Abstract: Methane is oxychlorinated to one or more chlorinated methanes, without net production of carbon tetrachloride, by contacting methane and chlorine and/or hydrogen chloride with a molten mixture of cuprous chloride, cupric chloride, and copper oxychloride, in the presence of an amount of carbon tetrachloride which inhibits net production thereof.

Abstract: A pyrolysis fuel oil is treated by soaking in the presence of sulfur for a period of time sufficient to react the highly unsaturated compounds present in the oil, followed by heating the soaked fuel oil at a temperature of from 850.degree. F. to 1100.degree. F. and an outlet pressure of from 300 to 600 psig to provide a treated feed having an API gravity of -3.degree. or less. The feed may be employed for the production of needle coke and/or carbon black and/or electrode binder pitch.

Abstract: A pyrolysis feedstock, such as a gas oil feed, is hydrotreated in the presence of a bimetallic catalyst which has been promoted by the addition of chlorine and/or fluorine, preferably chlorine, followed by thermal cracking to increase the yields of light olefins and BTX.

Abstract: In the hydroliquefaction of a sub-bituminous and/or lignitic coal, the inlet temperature to the hydroliquefaction zone is maintained at a temperature higher than those previously employed by providing recycle of hot liquid from the outlet portion of the hydroliquefaction zone. In this manner, the hydroliquefaction is operated at higher average temperatures, and total reaction volume is reduced, thereby reducing overall costs.

Abstract: A nitrile, such as terephthalonitrile is catalytically reacted with water, in the vapor phase, to produce a gaseous effluent containing the corresponding carboxylic acid, as well as unreacted nitrile, ammonia and water. The acid product is separated from the gas by sublimation, preferably at a temperature above the dew point of the other components of the mixture.

Abstract: A carbonaceous feedstock, obtained from either a petroleum or coal source, is hydrodenitrified by the use of a supported sulfided catalyst containing nickel, molybdenum and iron, with the molybdenum being present in an amount of from about 10% to about 20%, by weight, calculated as MoO.sub.3, based on total weight of catalyst, the iron to molybdenum atomic ratio being from about 0.05 to about 0.5, and the nickel to molybdenum atomic ratio being from about 0.2 to about 0.6.The process effectively denitrifies high nitrogen content feeds.

Abstract: A high crystalline coke can be prepared by heat-soaking a petroleum feedstock in the presence of added dissolved sulfur, heating to effect controlled thermal cracking thereof, separating non-crystalline substances as pitch, recovering a heavy cokable residue from the pitch free feed, and subjecting the residue to delayed coking.

Abstract: Methane is oxychlorinated to one or more chlorinated methanes, without net production of carbon tetrachloride, by contacting methane and chlorine and/or hydrogen chloride with a molten mixture of cuprous chloride, cupric chloride, and copper oxychloride, in the presence of an amount of carbon tetrachloride which inhibits net production thereof.

Abstract: .[.In a hydrogenation operation employing an ebullated catalytic bed, recycle is recovered from the hydrogenated product with at least 25%, by volume, of the recycle boiling above 950.degree. F. The recycle is cooled to a temperature of from 350.degree. to 600.degree. F. to separate coke precursors, prior to recycle to the hydrogenation. Higher conversion levels can be achieved by effecting recycle in such manner..]..Iadd.Disclosed is a hydrogenation process using at least one fluidized catalytic stage and a recycle material of heavy hydrogenated effluent. The heavy effluent material is cooled to a temperature within 350.degree.-600.degree. F. to separate toluene and heptane insoluble coke precursors prior to recycle. This separation may be enhanced by the use of centrifugation, filtration or a bed of particulate material (e.g. calcined coke). .Iaddend.