Uop Lcc

Upo LLC

Matthew Lippmann

Joseph A Kocal

Paul T Barger

Maureen L Bricker

Kurt M Vanden Bussche

Stanley Joseph Frey

Peter K Coughlin

Vasant P Thakkar

John Qianjun Chen

James A Johnson

Mark Paul Lapinski

Gregory A Funk

David James Shecterle

Paolo Palmas

Lev Davydov

Michael S Sandacz

Zhihao Fei

Lakshmi P Mokka

David A Wegerer

Keith Allen Couch

Clayton Colin Sadler

Douglas A Nafis

Mary Jo Wier

David S Lafyatis

Eric Leeton

Gregory J Schrad

David Lowry

Alex A Rio

A counter-current catalyst regenerator with at least two stages of counter-current contact along with a regenerator riser is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst. The regenerator riser may provide a passage to transport the catalyst and may serve as a secondary stage for coke combustion to provide the regenerated catalyst.

FCC counter-current regenerator with a regenerator riser

A process for treating an ionic liquid containing waste stream is described. If there is a liquid waste stream, the liquid waste stream is introduced into a liquid treatment zone. The ionic liquid in the liquid waste stream is neutralized. The concentration of the ionic liquid in the liquid waste stream is determined, and the allowed concentration of the ionic liquid in the liquid waste stream is determined. The concentration of the ionic liquid in the neutralized liquid waste stream is reduced to the allowed concentration, and the liquid waste stream having the allowed concentration is released. If there is a vapor waste stream, the vapor waste stream is introduced into a vapor treatment zone. The vapor waste stream is treated to form a treated vapor waste stream, and the treated vapor waste stream is released to a plant vapor treatment zone.

Ionic liquid waste handling system

A process for catalytic cracking includes the steps of: (a) contacting a hydrocarbon feed with a catalyst at catalytic cracking conditions; (b) adsorbing hydrogen on the catalyst during cracking; and (c) producing a cracked product, preferably propylene, wherein the catalyst comprises (i) a matrix, (ii) a catalytically active material, and (iii) a hydrogen adsorption material. Another process for catalytic cracking includes the steps of: (a) contacting a hydrocarbon feed with a catalyst at catalytic cracking conditions; (b) contacting the hydrocarbon feed with a hydrogen adsorption material; (c) adsorbing hydrogen on the hydrogen adsorption material during cracking; and (d) producing a cracked product, wherein the catalyst comprises (i) a matrix and (ii) a catalytically active material.

Fluid catalytic cracking process including adsorption of hydrogen and a catalyst for the process

Hydrocarbon processing apparatuses and processes for producing n-pentane and isobutane are provided herein. In an embodiment, a process for producing n-pentane and isobutane includes providing a hydrocarbon feed stream that includes C4 and C5 hydrocarbons. A recycle stream that includes C4+ hydrocarbons and the hydrocarbon feed stream is combined to produce a combined feed stream. The combined feed stream is separated to produce an iC4 product stream, an nC5+ product stream, and an iC5/nC4 feed stream. The iC5/nC4 feed stream is simultaneously disproportionated and isomerized in an isomerization zone to produce an intermediate stream that includes C3-C6 hydrocarbons. The C3-C6 hydrocarbons in the intermediate stream are separated to produce a C3&#x2212; stream and the recycle stream that includes C4+ hydrocarbons.

Hydrocarbon processing apparatuses and processes for producing N-pentane and isobutane

Process for adsorbing a species from a feed gas stream. Feed gas stream is introduced to an adsorption zone having a sorbent. Species from the feed gas stream is adsorbed onto the sorbent at an adsorbing temperature to enrich the sorbent with the species and deplete the species from the feed gas stream. Species-lean product gas stream is output. Species-rich sorbent from the adsorption zone is passed to a regeneration zone. Regenerant gas at a regenerating temperature greater than the adsorbing temperature is introduced into the regeneration zone to strip the species from the species-rich sorbent. Regenerated sorbent from the regeneration zone passes to a cooling zone disposed below the regeneration zone. Regenerated sorbent is cooled at a cooling temperature below the regenerating temperature. Cooled sorbent is transferred to the adsorbent zone.

Moving bed temperature swing adsorption process

A process for controlling a yield of an isomerization zone. Prior to entering the isomerization zone, Ccyclic hydrocarbons are removed from a feed stream. Disproportionation reaction selectivity is observed which produces valuable Chydrocarbons and Chydrocarbons. Also, a higher ring opening conversion of Ccyclic hydrocarbons is observed. The disproportionation reactions and the ring opening reactions may be selectively controlled by adjusting an amount of Ccyclic hydrocarbons passed into the isomerization zone.

Process for controlling the yield of an isomerization zone

A process for increasing a yield of an isomerization zone by removing at least a portion of the Ccyclic hydrocarbons from a stream having iChydrocarbons, iChydrocarbons, and iChydrocarbons prior to the stream being passed into the same isomerization zone. Suppression of the iChydrocarbons does not occur, allowing the iChydrocarbons to be isomerized in the same isomerization zone as the iChydrocarbons and iChydrocarbons.

Process for increasing the yield of an isomerization zone

A process for increasing a yield of an isomerization zone by removing at least a portion of the Ccyclic hydrocarbons from a stream prior to it being passed into the isomerization zone. Additionally, disproportionation reactions occur producing valuable Chydrocarbons and Chydrocarbons. Also, a higher ring opening conversion of Ccyclic hydrocarbons is observed.

Process for increasing the yield of an isomerization zone fractionation

A process for producing a feed for a stream cracker. At least a portion of the Ccyclic hydrocarbons are removed from a stream prior to it being passed into an isomerization zone. Disproportionation reaction selectivity is increased, producing valuable Chydrocarbons and Chydrocarbons. Also, a higher ring opening conversion of Ccyclic hydrocarbons is observed. The yield may be adjusted by controlling an amount of Ccyclic hydrocarbons passed to the isomerization zone. The catalyst in the isomerization zone is free of chloride, and the streams including effluent from the isomerization zone may be passed to a steam cracker without requiring chloride removal.

Process for producing a feed stream for a steam cracker

A process for transalkylating a coal tar stream is described. A coal tar stream is provided, and is fractionated to provide at least one hydrocarbon stream having polycyclic aromatics. The hydrocarbon stream is hydrotreated in a hydrotreating zone, and then hydrocracked in a hydrocracking zone. A light aromatics stream is added to the hydrocracking zone. The light aromatics stream comprises one or more light aromatics having a ratio of methyl/aromatic available position that is lower than a ratio of methyl/aromatic available position for the hydrotreated stream. The hydrocracked stream is transalkylated in the hydrocracking zone.

Hydrocracking process for a hydrocarbon stream

A process for providing aromatics from a coal tar stream. A coal tar stream is provided, and the coal tar stream is fractionated into at least a naphtha range stream. The naphtha range stream is hydrotreated, and the hydrotreated naphtha range stream is separated to provide at least a naphthene rich stream. The naphthene rich stream is reformed or dehydrogenated to convert the naphthene. The dehydrogenated naphthene rich stream may be combined with a portion of a reformed crude oil hydrocarbon stream.

Process for providing aromatics from coal tar

A process for selectively dealkylating aromatic compounds includes providing a coal tar stream comprising aromatic compounds and hydrotreating the coal tar stream to reduce a concentration of one or more of organic sulfur, nitrogen, and oxygen in the coal tar stream, and to hydrogenate at least a portion of the aromatic compounds in the coal tar stream. The process further includes hydrocracking the hydrotreated coal tar stream to further hydrogenate the aromatic compounds and to crack at least one ring of multi-ring aromatic compounds to form single-ring aromatic compounds. The single-ring aromatic compounds present in the hydrocracked stream are then dealkylated to remove alkyl groups containing two or more carbon atoms.

Process for selectively dealkylating aromatic compounds

A process for pyrolyzing a coal feed is described. A coal feed is pyrolyzed into a coal tar stream and a coke stream in a pyrolysis zone. The coal tar stream is separated into at least a pitch stream comprising aromatic hydrocarbons. The pitch stream is reacted in a reaction zone to add at least one functional group to an aromatic ring of the aromatic hydrocarbons in the pitch stream. The functionalized pitch stream is recycled to the pyrolysis zone.

Process for pyrolysis of a coal feed

A process for producing alkylated aromatic compounds includes pyrolyzing a coal feed to produce a coke stream and a coal tar stream. The coal tar stream is hydrotreated and the resulting hydrotreated coal tar stream is cracked. A portion of the cracked coal tar stream is separated to obtain a fraction having an initial boiling point in the range of about 60&#xb0; C. to about 180&#xb0; C., and an aromatics-rich hydrocarbon stream is extracted by contacting the fraction with one or more solvents. The aromatics-rich hydrocarbon stream is contacted with an alkylating agent to produce an alkylated aromatic stream, or the aromatics-rich hydrocarbon stream is reacted with an aliphatic compound or methanol in the presence of a catalyst to produce a methylated aromatic stream. The alkylated aromatic stream, the methylated aromatic stream, or both are separated into at least a benzene stream, a toluene stream, and a xylenes stream.

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Chicago, IL, United States of America

Matthew Lippmann