Exxon Chemical Patents, Inc.

Exxonmobil Chemical Patents Inc.

Shell Oil Comapny

Dane Clark Grenoble

Roy T Halle

Brendan Dermot Murray

Martin Leo Gorbaty

Richard Charles Stell

Stanley Nemec Milam

Robert David Strack

John R Messinger

John Ernest Asplin

Richard M Foley

Bruce H C Winquist

Carl W Bradow

Harold W Helmke

William Douglas Thomson

James C Vartuli

Doron Levin

Shifang Luke Luo

Paul Benjerman Himelfarb

Charles Morris Yarbrough

Brian Scott Vanderwilp

Michael Norris Treybig

Disclosed is a process for the selective hydrogenation of diolefins and sulfur compounds that are contained in a pyrolysis gasoline feedstream. The process includes utilizing a single hydrotreating reaction stage by introducing the pyrolysis gasoline feedstock that includes a diolefin concentration and an organic sulfur concentration into a reactor that is loaded with a high activity hydrotreating catalyst and which is operated under selective hydrogenation conditions. A reactor effluent having a reduced diolefin concentration and a reduced organic sulfur concentration is yielded from the reactor and is separated into a portion that is recycled as a reactor feed. The remaining portion of the reactor effluent is passed downstream for further processing or handling.

Process for the selective hydrogenation and hydrodesulferization of a pyrolysis gasoline feedstock

A method is disclosed for treating gaseous effluent from a hydrocarbon pyrolysis unit to provide steam cracked tar of reduced asphaltene and toluene insolubles content. The method is suitable for preparing reduced viscosity tar useful as a fuel blending stock, or feedstock for producing carbon black, while reducing or eliminating the need for externally sourced lighter aromatics additives to meet viscosity specifications. The method comprises drawing steam cracked tar from a separation vessel, e.g., a primary fractionator or tar knock-out drum, cooling the tar, and returning it to the separation vessel to effect lower overall tar temperatures within the separation vessel, in order to reduce viscosity increasing condensation reactions. An apparatus for carrying out the method is also provided.

Method for processing hydrocarbon pyrolysis effluent

A process for selectively converting a dialkyl ether to the corresponding alkene and alkanol comprises contacting a feed containing at least one dialkyl ether with a catalyst comprising a mixed metal oxide which comprises at least one metal selected from Group 4 of the Periodic Table of Elements and at least one metal selected from Group 3 (including the Lanthanides and Actinides) and Group 6 of the Periodic Table of Elements.

Selective decomposition of ethers

An integrated process for converting a hydrocarbon feedstock having components boiling above about 100&deg; C. into steam cracked products is described. The process first involves passing the feedstock to a hydrotreating zone to effect substantially complete decomposition of organic sulfur and/or nitrogen compounds. The product from the hydrotreating zone is passed to an aromatics saturation zone. The product is then passed to a steam cracking zone. Hydrogen and C,-C,hydrocarbons, steam cracked naphtha, steam cracked gas oils and steam cracked tar are recovered. The amount of steam cracked tar produced is reduced by at least about 30 percent, and the amount of steam cracked tar produced is reduced by at least about 40 percent, basis the starting hydrocarbon feedstock which has not been subject to hydrotreating and aromatics saturation.

Steam cracking of hydrotreated and hydrogenated hydrocarbon feeds

An integrated process for converting a hydrocarbon feedstock having components boiling above about 100&deg; C. into steam cracked products is described. The process first involves passing the feedstock to a hydrotreating zone at a pressure in the range of from about 400 psig to about 1,250 psig to effect substantially complete decomposition of organic sulfur and/or nitrogen compounds. The product from the hydrotreating zone is passed to a steam cracking zone. Hydrogen and C,-C,hydrocarbons, steam cracked naphtha, steam cracked gas oil and steam cracked tar are recovered, where the amount of steam cracked tar produced is reduced by at least about 15 percent, basis the starting hydrocarbon feedstock which has not been subject to hydrotreating.

Integrated hydrotreating steam cracking process for the production of olefins

A safe, effective, and economical method is provided for recovering olefins from cat-cracked gases without accumulating dangerous amounts of nitrogen oxides. A stream of cat-cracked gas first is scrubbed to remove acid gases, including nitrogen dioxide (NO.sub.2), and then is passed through a depropanizer fractionation tower. Hydrocarbons having four or more carbon atoms are recovered in the bottoms of the depropanizer, and the overhead from the depropanizer--which is composed of hydrocarbons having three or fewer carbon atoms--is sent to an absorber demethanizer tower. Hydrocarbons having two or more carbon atoms are recovered in the bottoms from the absorber demethanizer tower, where temperatures are no lower than about -45.56.degree. C. (-50.degree. F.) The overhead from the absorber demethanizer tower--which is composed of methane, hydrogen, and trace amounts of nitrogen oxide, C.sub.2, and absorbent (C.sub.3)--then is chilled to condense and recover trace amounts of C.sub.2 and heavier gases, including trace amounts of the C.sub.3 absorbent, at temperatures of about -101.11.degree. C. (-150.degree. F.) or higher. Thus, recovery of desired hydrocarbons from the cat-cracked gas is conducted at temperatures that are high enough to prevent the oxidation of nitric oxide (NO) to form nitrogen dioxide (NO.sub.2) and high enough to prevent the accumulation of unwanted nitrogen oxides.

Process for recovering olefins from cat-cracked gas without accumulating

A process for the production of gaseous olefins which involves introducing a hydrocarbon feedstock stream into a high temperature thermal cracking zone to produce a high temperature cracked product stream, quenching the cracked product stream to stop the cracking reactions, injecting at least one HDD (hydrogen donor diluent) into the cracked product stream at or downstream of the point at which the reaction is quenched, recovering normally gaseous olefins from the cracked product stream, and recovering a liquid product stream containing a diminished asphaltene content.

Method for upgrading steam cracker tars

A safe, effective, and economical method is provided for recovering olefins from cat-cracked gases without accumulating dangerous amounts of nitrogen oxides. A stream of cat-cracked gas first is scrubbed to remove acid gases, including nitrogen dioxide (NO.sub.2), and then is passed through a depropanizer fractionation tower. Hydrocarbons having four or more carbon atoms are recovered in the bottoms of the depropanizer, and the overhead from the depropanizer--which is composed of hydrocarbons having three or fewer carbon atoms--is sent to an absorber demethanizer tower. Hydrocarbons having two or more carbon atoms are recovered in the bottoms from the absorber demethanizer tower, where temperatures are no lower than about -45.56.degree. C. (-50.degree. F.). The overhead from the absorber demethanizer tower--which is composed of methane, hydrogen, and trace amounts of nitrogen oxide, C.sub.2, and absorbent (C.sub.3)--then is chilled to condense and recover trace amounts of C.sub.2 and heavier gases, including trace amounts of the C.sub.3 absorbent, at temperatures of about -101.11.degree. C. (-150.degree. F.) or higher. Thus, recovery of desired hydrocarbons from the cat-cracked gas is conducted at temperatures that are high enough to prevent the oxidation of nitric oxide (NO) to form nitrogen dioxide (NO.sub.2) and high enough to prevent the accumulation of unwanted nitrogen oxides.

A two-step process for the production of large quantities of heartcut distillate resin precursors from steamed cracked gas oil product which involves hydrogenation of the steam cracked gas oil followed by steam cracking of the hydrogenated product to produce a greater than 15 wt. % yield of heartcut distillate resin precursors. A process for producing heartcut distillate comprising hydrogenating a hydrocarbon oil comprising two-ring aromatic molecules to form a hydrogenated hydrocarbon oil comprising partially saturated naphtheno-aromatic molecules; and subjecting a feedstock comprising hydrogenated hydrocarbon oil to steam cracking under conditions which favor producing a heartcut distillate containing an amount greater than about 4 wt. % yield of heartcut distillate resin precursors. A method for producing heartcut distillate which involves subjecting a hydrogenated hydrocarbon feedstock boiling in the range of about 200.degree. C. to 320.degree. C. to steam cracking under conditions which favor producing a heartcut distillate containing an amount greater than about 4 wt. % yield of heartcut distillate (HCD) resin precursors. A method for producing heartcut distillate which involves subjecting a hydrotreated steam cracked gas oil (SCGO) product to steam cracking under conditions which favor producing a heartcut distillate containing an amount greater than about 4 wt. % yield of heartcut distillate (HCD) resin precursors.

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Houston, TX, United States of America

Dane Clark Grenoble