Exxon Research and Engineering Company

Robert B Long

Fred A Caruso

Martin Leo Gorbaty

David G Walker

Richard J DeFeo

Richard Henry Schlosberg

Lawrence L Murrell

Lonnie W Vernon

Dane C Grenoble

Kenneth A Gould

Jack Griffel

A major portion, preferably a substantial portion, of the coke precursors may be removed from atmospheric and vacuum resids having a Conradson carbon residue of at least about 10 wt. % by selectively removing the components of said feedstock which have an overall Hildebrand solubility parameter greater than 9.0 and a complexing solubility parameter greater than 1.3, such that there results a coke precursor rich fraction containing components having the requisite solubility parameters and a coke precursor depleted fraction. Each fraction may then be processed separately. Segregation of coke precursors by removing the components having the requisite solubility parameters also results in an enhanced yield of useable liquid hydrocarbons relative to that obtained using conventional separation processes.

Selective removal of coke precursors from hydrocarbon feedstock

A hydrocarbon feedstock may be selectively separated into its various fractions by contact with a mixture of specified polar and nonpolar solvents at a temperature so as to form a two-phase system, separating the first extract and raffinate phases so obtained, cooling the raffinate (nonpolar) phase so that three phases form, and separating the three phases. The three phases obtained consist of the polar solvent containing low molecular weight polars, the nonpolar solvent containing the saturates and aromatics, and an asphaltene-containing phase. The asphaltene-containing phase may be further washed to yield an asphalt with a higher microcarbon residue than the non-washed asphalt.

Selective separation of heavy oil using a mixture of polar and nonpolar

Basic asphaltenes are selectively removed from asphaltene-containing hydrocarbon feeds by contacting the feed with a transition metal oxide solid acid catalyst which selectively adsorbs the basic asphaltenes. The catalyst will comprise a catalytic metal component selected from the group consisting essentially of oxides of (a) tungsten, niobium, and mixtures thereof and (b) mixtures of (a) with tantalum, hafnium, chromium, titanium, zirconium and mixtures thereof, supported on an inorganic refractory oxide support such as alumina. Asphalt-laden catalyst is separated from the feed, the asphaltenes adsorbed thereon are cracked off in the presence of steam and the catalyst is regenerated and recycled back to the adsorption zone.

Separating basic asphaltenes using transition metal oxide acid catalysts

Basic asphaltenes are selectively removed from asphaltene-containing hydrocarbon feeds by contacting the feed with a solid acid, such as a solid acid cracking catalyst, which selectively adsorbs the basic asphaltenes present in the feed. The adsorption is carried out at a temperature below about 575.degree. F. to avoid cracking the asphaltenes in the adsorption zone. The basic asphaltene-containing catalyst is then separated from the feed, the basic asphaltenes are cracked off the catalyst, the catalyst is regenerated by suitable techniques such as air burning and then recycled back to the adsorption zone. The basic asphaltene-reduced feed is sent to further processing.

Adsorption of basic asphaltenes on solid acid catalysts

Properties of phenol-containing hydrocarbonaceous streams are improved by first treating the stream with a C.sub.1 to C.sub.10 alcohol and an acid. If enough alcohol and acid are employed, two liquid phases are formed, an alcohol/acid phase and a hydrocarbonaceous phase. The alcohol/acid phase, which now contains phenols, can be separated and contacted with a C.sub.1 to C.sub.16 olefin or the olefin can be added in situ. In any case, oxygen-alkylation of the phenolic groups occurs.

Separation and oxygen-alkylation of phenols from phenol-containing

Particulate coal is contacted with a hydrogen donor solvent, preferably a vapor phase hydrogen donor solvent, to swell the coal particles and, thereafter, the swollen coal particles are subjected to coal liquefaction conditions in the absence of liquid phase solvent.

Coal liquefaction process

An integrated coal pretreatment, liquefaction and gasification process is provided in which particulate coal is contacted with a vapor phase hydrogen donor solvent to swell the coal particles. The swollen coal particles are subjected to coal liquefaction conditions at relatively low temperatures. The solid residue of the coal liquefaction stage is subjected to pyrolysis conditions at relatively high temperatures to produce an additional amount of hydrocarbonaceous oil. The solid residue of the pyrolysis stage is gasified by treatment with steam and a molecular oxygen-containing gas to produce a hydrogen-containing gas.

Particulate coal is contacted with a vapor phase hydrogen donor solvent to swell the coal particles and, thereafter, the swollen coal particles are subjected to coal liquefaction conditions in the presence of a liquid phase solvent.

Bimetallic salts, having the generic formula MM'X.sub.n wherein M is a Group IB metal, M' is a Group IIIA metal, X is a halide and n is equal to the sum of the valences of M and M', are prepared by reacting the halogen salts of the individual metals, M and M', in a suitable solvent. The bimetallic salt formed thereby is a discrete monomeric species and can be utilized in the separation and recovery of various ligands, by preferential complexation. Complexation can be conducted with the bimetallic salt in the solid state, in solution, or as a slurry, and with the complexible ligand in the gaseous or liquid state. The ligand is recovered by decomplexation of the bimetallic salt-ligand complex or by displacement of the complexed ligand with another ligand.

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Atlantic Highlands, NJ, United States of America

Robert B Long