Phillips Petroleum Company

Cecil O Carter

Dwight D Boesiger

Thomas Hutson, Jr

Daniel M Coombs

Donald M Haskell

A high temperature absorption process for bulk recovery of CO.sub.2 comprises contacting a gaseous mixture containing CO.sub.2, H.sub.2 S, and natural gas with C.sub.3 and heavier components and having a high and variable CO.sub.2 loading, with an amine absorbent solution at a temperature above 220.degree. F. The amine absorbent solution is continuously regenerated in a multiple section flashing so as to reduce the energy requirements for regeneration and thereby making the process more suitable for bulk recovery of CO.sub.2 from gas streams associated with enhanced oil recovery projects employing CO.sub.2 for miscible flood of oil reservoirs.

Bulk CO.sub.2 recovery process

A mixture of normally liquid organic compounds, particularly a light cycle oil obtained by the catalytic cracking of petroleum oils, is separated by contacting the mixture with an essentially anhydrous organic sulfoxide, particularly dimethylsulfoxide, to dissolve an organic extract in said sulfoxide and form an extract phase, comprising sulfoxide and the organic extract, and a raffinate phase, comprising the organic raffinate; diluting the extract phase with about 4.0 to 10.0 wt. % of water; separating the diluted extract phase into an aqueous phase, comprising the water containing the sulfoxide dissolved therein, and an organic phase, comprising the organic extract with minor amounts of the sulfoxide and water; fractionating the organic phase to separate the water and sulfoxide from the organic extract, which is suitable for use as a flotation agent; recycling the thus separated water and sulfoxide to the dilution step; drying the aqueous phase to remove the water and produce an essentially anhydrous sulfoxide; and recycling the sulfoxide to the solvent extraction step.

Method for separating normally liquid organic compounds

A gas stream containing CO.sub.2 and H.sub.2 S is contacted with an alkanolamine in a contacting zone. The rich solution is then selectively stripped in a stripping zone to produce a gas stream containing a higher CO.sub.2 :H.sub.2 S mole ratio than the initial stream. This stream can be recycled to the alkanolamine contacting zone. The partially stripped solution can be introduced into another stripping zone to provide a third gas stream which is rich in H.sub.2 S and lean in CO.sub.2 suitable as feed for a Claus Unit and a lean alkanolamine solution which can be recycled to the contacting zone.

Process and apparatus for removing H.sub.2 S from gas streams

A method of pre-conditioning the walls of an olefin dimerization reactor and starting a dimerization process comprises sequential steps of introducing a first soluble homogeneous catalyst component comprising, e.g. a complex of a divalent metal selected from the group consisting of nickel, cobalt and iron, and a second soluble homogeneous catalyst component comprising, e.g. an organoaluminum compound, at rates such that the molar catalyst feed ratio of said aluminum to said divalent metal is maintained at a first value during the pre-conditioning and startup period and at a second, higher, value during the operating period.

Surface conditioning in olefin dimerization reactors

A solvent system composed essentially of sulfolane and a ketone, e.g., sulfolane and methyl ethyl ketone is employed in a liquid-liquid extraction operation to separate a low boiling olefin, e.g., pentene-2, hexene-1, octene-1, etc., from a corresponding close boiling paraffin, e.g., n-pentane, n-hexane, and n-octane, respectively, and wherein solvent is recovered by employing a portion thereof in a drying or stripping column.

Liquid-liquid extraction of low boiling olefin contained in

Olefins are dimerized in a loop reactor with flashing of the reactor effluent in a flashing zone within the loop. A subsequent flash in a second flashing zone can also be used for the removal of product as flash vapor. In another embodiment, separated product dimers or product heavies are used as absorbents for unreacted ethylene. The use of a vapor-liquid contacting device incorporated in the loop reactor is especially helpful in the dimerization of an olefin when the olefin is available in low-concentration gas streams. A thermosiphon loop reactor can also be used for low-concentration olefin streams to minimize the power requirements as the energy of the feed gas is used to induce the reactor circulation.

Olefin dimerization

A method for separating olefins from paraffins in which a mixture of olefin and paraffin is contacted with a dimethyl sulfoxide (DMSO) extractant stream in the liquid phase thereby dissolving olefins in the DMSO and permitting separation of a paraffin stream. The DMSO containing dissolved olefin is then contacted with water and a phase separation is effected between olefin and a mixture of DMSO and water. At least a portion of the DMSO and water mixture can be fractionated to produce a dried DMSO product which can be recycled as a portion of the extractant into contact with the mixture of olefin and paraffin.

Separating olefins from paraffins with dimethyl sulfoxide extractant

Preparation of a hydrocarbon-soluble nickel complex substantially free of moisture comprising reacting a nickel compound with an organic complexing agent in a hydrocarbon solvent to form a complex, allowing the complex to settle and separate into a water phase and a hydrocarbon solution of the complex, then drying the hydrocarbon solution of complex by azeotropic distillation. The substantially anhydrous nickel complex obtained can be mixed with an alkylaluminum halide to form a catalyst system useful for the dimerization of olefins.

Catalyst preparation

A C.sub.4 -hydrocarbon feedstream containing butenes, butadiene, and vinylacetylene is subjected to a first extractive distillation with a selective solvent to remove butenes and a first portion of vinylacetylene as the extract; by the extraction with a minor quantity of methylethyl ketone in the selective solvent in this step, it has been found that a major portion of the vinylacetylene can be rejected, together with the butenes in the rich extract and that simultaneously the quantity of butadiene extracted could be considerably reduced; in a second extractive distillation the butadiene-rich raffinate of the first extractive distillation is further purified by extractive distillation using a mixture of sulfolane and methylethyl ketone as the solvent; after solvent stripping, the butadiene stream is finally purified in a fractionation step, wherein further vinylacetylene is removed.

Butadiene purification with simultaneous prefractionation and

In the production of ethylfluoride by reacting ethylene with hydrofluoric acid, the addition of a very minor amount of a heavier olefin such as a C.sub.3 and/or C.sub.4 olefin greatly improves conversion and selectivity of the reaction. The product ethylfluoride can be recovered by liquid-liquid extraction.

Ethylfluoride production

The overhead stream of a deisobutanizer in an HF-alkylation plant is extracted with HF to produce a stream containing isobutane, HF and ethyl fluoride, which in turn is fractionated under a pressure of about 150 to 300 psig. The bottoms stream of this fractionation, then, is fractionated under a pressure of 50 to 145 psig to produce a relatively pure ethyl fluoride overhead stream and a relatively pure HF bottoms stream.

Process to separate ethyl fluoride and HF

A process and apparatus for HF alkylation wherein the vapor from the fractionation zone in which the effluent of the reaction zone is fractionated is contacted with water, the mixture formed is reacted with an olefin to form an alkyl fluoride, the alkyl fluoride is recovered and reintroduced into the alkylation reaction zone.

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Wann, OK, United States of America

Cecil O Carter