The Lummus Company

Maruzen Petrochemical Company, Limited

Lummus Crest, Inc.

Morgan C Sze

Harvey D Schindler

Herbert D Riegel

George J Snell

Abraham P Gelbein

Andre A Simone

Thomas M Bennett

Harold Unger

John E Paustian

Vincent A Strangio

Mikio Nakaniwa

Maurice E Brooks

Ruey H Wang

Nobuyuki Kobayashi

George D Suciu

Anthony J Fanelli

Joon T Kwon

Roger P Van Driesen

William V Bauer

Kiyoshige Hayashi

Kenji Furukawa

Harold B Kohn

Raymond H Long

Dennis F Ogren

Yoshihiko Hase

Daniel H Gold

Richard T Whitehead

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. Noncrystalline substances may be removed prior to coking to further improve the process.

Coke production

Low energy process for the production of gasoline-ethanol blends, comprising dehydrating the aqueous ethanolic product from a conventional fermentation process, preferably containing about 6 wt. % ethanol, so as to generate an aqueous ethanolic effluent containing about 90 wt. % ethanol; mixing the effluent with gasoline feedstock; chilling the resultant gasoline-aqueous ethanol mixture to a temperature of about -10.degree. F., without forming ice, thereby to form (1) a gasohol blend containing about 10 wt. % ethanol and (2) an aqueous stream comprising some ethanol and traces of gasoline; extracting the gasoline-containing aqueous stream with a minor stream of the fermentation ethanol product in order to recover the gasoline it contains; and recovering said blend to produce a gasohol product under-saturated with water at all operating temperatures above -10.degree. F.

Process for the production of gasohol

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.

Removal of arsenic impurity from hydrocarbons

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.

Hydrogenation of high boiling hydrocarbons

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.

Steam pyrolysis of hydrocarbons

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.

Production of chlorinated compounds by use of molten salts

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.

Coke production from liquid derived from sub-bituminous and/or lignitic

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.

Hydroliquefaction of coal

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.

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.

Supported vanadia catalyst and use thereof for nitrile production

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.

Demetallization of hydrocarbon feedstock

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.

Production of pipeline gas from coal

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.

Oxychlorination of methane

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.

Feedstock treatment

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.

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Upper Montclair, NJ, United States of America

Morgan C Sze