Exxon Research and Engineering Company

Exxonmobil Research and Engineering Company

Other

George A Swan, Iii

William C Baird, Jr

Gordon Frederick Stuntz

Stuart S Goldstein

Joseph P Boyle

Gerrit S Swart

Paul W Kamienski

Michael Walter Bedell

William A Wachter

David W Staubs

Eduardo Mon

Michel A Daage

Kenneth Ray Clem

Kenneth L Riley

Teh Chung Ho

Michele Sue Touvelle

Paul K Ladwig

Darryl Patrick Klein

Leonard Schoenman

Dean C Draemel

Jackson I Ito

B Erik Henry

William R Adamson

William E Winter

William E Winter, Jr

Rustom Merwan Billimoria

Brian Erik Henry

Todd R Steffens

Rathna P Davuluri

Christopher Gordon Smalley

John E Asplin

James P Glass, Jr

Louis S Dauber

John Ernest Asplin

Steven S Lowenthal

James P Bailor

George W Bailey

David G Brignac

Soni O Oyekan

Stephen D Challis

Staubs, David W

John F Dolan

Robert G Corry

This invention relates to an apparatus and process for injecting a petroleum feed. More particularly, a liquid petroleum feed is atomized with a nozzle assembly apparatus in which the apparatus has injection nozzles that produce a generally flat spray pattern of finely dispersed feed. The injection nozzles are each designed such that the overall effect of the different spray patterns from the individual nozzles provides a more uniform feed coverage across the catalyst stream.

FCC feed injection system

The propylene production of a fluid catalytic cracking unit employing a large pore zeolite cracking catalyst, produces more propylene by adding a naphtha cracking riser and a medium pore zeolite catalytic component to the unit, and recycling at least a portion of the naphtha crackate to the naphtha riser. The large pore size zeolite preferably comprises a USY zeolite and the medium pore size is preferably ZSM-5. Propylene production per unit of naphtha feed to the naphtha riser is maximized, by using the 60&#x2013;300&#xb0; F. naphtha crackate as the feed.

Fluid cat cracking with high olefins production

A process and apparatus for atomizing a fluid is disclosed herein. The fluid is mixed with an atomizing fluid in a plurality of locations and passed through a nozzle.

Apparatus and process for enhanced feed atomization

The invention relates to a process for converting cycle oils produced in catalytic cracking reactions into olefin and naphtha. More particularly, the invention relates to a process for hydroprocessing a catalytically cracked light cycle oil, and then re-cracking it in an upstream zone of the primary FCC riser reactor.

Cycle oil conversion process

The invention relates to a process for converting cycle oils produced in catalytic cracking reactions into light olefin and naphtha. More particularly, the invention relates to a process for hydroprocessing a catalytically cracked light cycle oil in order to form a hydroprocessed cycle oil containing a significant amount of tetralins. The hydroprocessed cycle oil is then re-cracked in an upstream zone of the primary FCC riser reactor.

The invention relates to a process for converting cycle oils produced in catalytic cracking reactions into olefinic naphthas. More particularly, the invention relates to a process for hydroprocessing a catalytically cracked light cycle oil, and then re-cracking in an out-board FCC reactor it in order to form a naphthenic blend-stock.

A process and apparatus for atomizing a fluid is disclosed. The processes and apparatuses are useful for atomizing a feed oil for a fluid cat cracking (FCC) or other suitable process.

Fluid atomization process

An atomizing gas, such as steam, and a hot fluid comprising a hot liquid to be atomized, are passed under pressure, through separate fluid conduits in a heat exchange means, in which the hot liquid heats the steam to a superheat temperature, by indirect heat exchange. The superheated steam is then injected into the hot fluid, which comprises a two-phase fluid comprising steam and the hot liquid, subsequent to the superheated steam injection. The two-phase fluid is passed through an atomizing means, such as an orifice, into a lower pressure atomizing zone, which causes the steam to expand and atomize the liquid into a spray of liquid droplets. The two-phase fluid is formed before or as a consequence of the superheated steam injection and is preferably steam-continuous when passed through the atomizing means. This process is useful for atomizing a hot feed oil for a fluid cat cracking (FCC) process.

Superheating atomizing steam with hot FCC feed oil

A process for producing polymers from olefins selectively produced by a two stage process for selectively producing C,to C,olefins from a gas oil or resid is disclosed herein. The gas oil or resid is reacted in a first stage comprising a fluid catalytic cracking unit wherein it is converted in the presence of conventional large pore zeolitic catalyst to reaction products, including a naphtha boiling range stream. The naphtha boiling range stream is introduced into a second stage comprising a process unit containing a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone. The naphtha feed is contacted in the reaction zone with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500 to 650&deg; C. and a hydrocarbon partial pressure from about 10 to 40 psia. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, which is then recycled to the reaction zone.

Process for producing polypropylene from C3 olefins selectively produced by a two stage fluid catalytic cracking process

C.sub.2 to C.sub.4 olefins are selectively produced from a gas oil or resid in a two stage process. The gas oil or resid is reacted in a first stage comprised of a fluid catalytic cracking unit wherein it is converted in the presence of conventional large pore zeolitic catalyst to reaction products, including a naphtha boiling range stream. The naphtha boiling range stream is introduced into a second stage comprised of a process unit containing a reaction zone, a stripping zone, a catalyst regeneration zone, and a fractionation zone. The naphtha feedstream is contacted in the reaction zone with a catalyst containing from about 10 to 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions which include temperatures ranging from about 500 to 650.degree. C. and a hydrocarbon partial pressure from about 10 to 40 psia. Vapor products are collected overhead and the catalyst particles are passed through the stripping zone on the way to the catalyst regeneration zone. Volatiles are stripped with steam in the stripping zone and the catalyst particles are sent to the catalyst regeneration zone where coke is burned from the catalyst, which is then recycled to the reaction zone.

Two stage fluid catalytic cracking process for selectively producing     b.

Atomization of a high boiling point, hot liquid, such as a hydrocarbon feed oil for a fluid cat cracker, is enhanced by injecting subcooled water into the hot liquid, to form a two-phase fluid of the liquid and steam, upstream of the atomization. The hot liquid is at conditions of temperature and pressure effective for the injected, subcooled water to vaporize into steam, when the water contacts it. Typically this means that the hot liquid is hotter and at a lower pressure than the water. In an FCC process, the subcooled water is sparged into the flowing hot oil in a conduit in a riser feed injector. This produces a spray of hot oil in the riser reaction zone in which the oil drops are smaller and more uniformly distributed in the spray.

FCC feed injection using subcooled water sparging for enhanced feed

A FCC process in which spent catalyst is stripped of hydrocarbon in a stripping zone prior to entering the regenerator. In order to maximize the amount of strippable hydrocarbon removed in the stripping zone with minimal use of stripping gas, a sample of spent catalyst is removed prior to entering the regenerator. The spent catalyst is analyzed for strippable hydrocarbon by conducting the sample to a heated catalyst collection vessel, evacuating the catalyst, collecting the gases from the collection vessel and analyzing the gases for amount of strippable hydrocarbon on the spent catalyst.

Analyzer system for strippable hydrocarbon on FCC catalyst

A process for increasing the yield of C.sub.3 and C.sub.4 olefins by injecting light cat naphtha together with steam into an upstream reaction zone of a FCC riser reactor. The products of the upstream reaction zone are conducted to a downstream reaction zone and combined with fresh feed in the downstream reaction zone.

Recracking of cat naphtha for maximizing light olefins yields

A process for reforming a gasoline boiling range naphtha stream using a reforming process unit comprised of two independent process units, each of which are operated in two stages. The first stage is operated in a fixed-bed mode and is comprised of a plurality of serially connected fixed bed reactors, and the second stage is operated in a moving bed continuous catalyst regeneration mode. A hydrogen-rich stream is recycled through both stages for each process unit and the moving-bed reforming zones share a common regeneration zone.

Reforming with two fixed-bed units, each having a moving-bed tail

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Baton Rouge, LA, United States of America

George A Swan, Iii