Exxonmobil Chemical Patents Inc.

Exxonmobil Research and Engineering Company

Exxon Research and Engineering Company

Exxonmobile Chemical Patents Inc.

Brian Erik Henry

Gordon Frederick Stuntz

Philip Andrew Ruziska

Tan Jen Chen

Paul F Keusenkothen

Stephen M Davis

William A Wachter

Paul K Ladwig

Karl Gottlieb Strohmaier

Shun Chong Fung

Tan-Jen Chen

Avelino Corma Canos

David E W Vaughan

Antonio Chica Lara

John E Asplin

John Ernest Asplin

Joaquin Perez Pariente

Javier Agundez Rodriguez

James D Dearth

John Scott Buchanan

David Lawrence Stern

Daniel Paul Leta

George A Swan, Iii

Miroslav Petro

Ronald G Searle

Kirk C Nadler

Todd R Steffens

Stephen M Cundy

Edward W Corcoran

Thomas Harding McWaid

Li Song

Michael Walter Bedell

Jay F Carpency

Jacob Johannes Thiart

Nicole J Lai

Yan Ying Chan

This invention relates to a process for producing a product stream with improved reduction of Conradson Carbon Residue ('CCR') and a reduced average boiling point from a heavy hydrocarbon feedstream utilizing a high-pressure, low-energy separation process. The invention may be utilized to reduce the CCR content and reduce the average boiling point in heavy hydrocarbon feedstreams, such as whole crudes, topped crudes, synthetic crude blends, shale oils, bitumen, oil from tar sands, atmospheric resids, vacuum resids, or other heavy hydrocarbon streams. This invention also results in a process with an improved CCR separation efficiency while maintaining permeate flux rates.

Reduction of conradson carbon residue and average boiling points utilizing high pressure ultrafiltration

The present invention relates to a process for selectively producing Colefins from a catalytically cracked or thermally cracked naphtha stream. The process is practiced by recycling a Crich fraction of the catalytic naphtha product to the riser upstream the feed injection point, to a parallel riser, to the spent catalyst stripper, and/or to the reactor dilute phase immediately above the stripper.

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A process for selectively producing Colefins from a catalytically cracked or thermally cracked naphtha stream is disclosed herein. The naphtha stream is introduced into a process unit comprised of a reaction zone, a stripping zone containing a dense phase, 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 about 50 wt. % of a crystalline zeolite having an average pore diameter less than about 0.7 nanometers at reaction conditions. 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, and are then recycled to the reaction zone. Overhead products from the reaction zone are passed to a fractionation zone where a stream of Cproducts is recovered and a stream rich in Colefins is recycled to a dilute phase reaction zone in the stripping zone separate from the dense phase of the stripping zone. The olefins can be further processed and polymerized to form a variety of polymer materials.

A multi component catalyst and catalytic cracking process for selectively producing Colefins. The catalyst comprises a first molecular sieve having an intermediate pore size, a second molecular sieve and, optionally a third molecular sieve having a large pore size. At least one of the channels of the second molecular sieve has a pore size index that is less than the pore size index of at least one channel of the first molecular sieve. The process is carried out by contacting a feedstock containing hydrocarbons having at least 5 carbon atoms is contacted, under catalytic cracking conditions, with the multi component catalyst. The catalyst finds application in the cracking of naphtha and heavy hydrocarbon feedstocks.

Multi component catalyst and its use in catalytic cracking

A process for selectively producing Cto Colefins from feedstock such as a gas oil or resid. The feedstock is reacted in a first stage comprising a fluid catalytic cracking unit wherein it is converted in the presence of a mixture of conventional large pore zeolitic catalyst and a medium pore zeolitic catalyst to reaction products, including a naphtha boiling range stream. The naphtha boiling range stream is introduced into a second stage where it is contacted with a catalyst containing from about 10 to about 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 about 650&#xb0; C. and a hydrocarbon partial pressure from about 10 to about 40 psia (about 70 to about 280 kPa).

The present invention relates to a process for selectively producing Colefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain at least a Crich fraction and feeding the Crich fraction into a reaction stage at a point wherein the residence time of the Crich fraction is minimized.

The present invention relates to a process for selectively producing Colefins from a catalytically cracked or thermally cracked naphtha stream by fractionating the naphtha feed to obtain a Cfraction and feeding the Cfraction either in the riser downstream of the injection point for the reminder of the naphtha feed, in the stripper, and/or in the dilute phase immediately downstream or above the stripper of a process unit.

A process for producing polypropylene from olefins selectively produced from a catalytically cracked or thermally cracked naphtha stream is disclosed herein. The naphtha stream is contacted 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 from about 500&deg; C. to 650&deg; C. and a hydrocarbon partial pressure from about 10 to 40 psia. The catalyst may be pre-coked with a carbonaceous feed. Alternatively, the carbonaceous feed used to coke the catalyst may be co-fed with the naphtha feed.

Process for selectively producing propylene in a fluid catalytic cracking process

Disclosed are silicoaluminophosphates (SAPOs) having unique silicon distributions and high catalytic cracking activity a method for their preparation and their use as FCC catalysts. More particularly, the new SAPOs have a high silica:alumina ratio and favorable Si atom distribution. The new SAPOs may have a small crystal size and may be synthesized from a single-phase synthesis solution.

Silicoaluminophosphates having an AEL structure and their use as FCC catalysts

A process for producing propylene from a catalytically cracked or thermally cracked naphtha stream is disclosed herein. The naphtha stream is contacted 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 from about 500&deg; C. to 650&deg; C. and a hydrocarbon partial pressure from about 10 to 40 psia. A separate stream containing aromatics may be co-fed with the naphtha stream.

Process for selectively producing C3 olefins in a fluid catalytic cracking process

Disclosed are silicoaluminophosphates (SAPOs) having unique silicon distributions, a method for their preparation and their use as catalysts for the catalytic cracking of hydrocarbon feedstocks. More particularly, the new SAPOs have a high silica: alumina ratio, and are prepared from microemulsions containing surfactants.

Catalytic silicoaluminophosphates having an AEL structure, and their use in catalytic craking

Disclosed are silicoaluminates (SAPOs) having unique silicon distributions, a method for their preparation and their use as naphtha cracking catalysts. More particularly, the new SAPOs have a high silica:alumina ratio and favorable Si atom distribution.

Method for the use of new silicoaluminophosphas having an AEL structure to convert naptha to C2 to C4 olefins

Disclosed are silicoaluminophosphates (SAPOs) having unique silicon distributions, a method for their preparation and their use as catalysts for the catalytic cracking of hydrocarbon feedstocks. More particularly, the new SAPOs have a high silica:alumina ratio, and are prepared from microemulsions containing surfactants.

Naphtha cracking utilizing new catalytic silicoaluminophosphates having an AEL structure

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.

A process for selectively producing C.sub.2 -C.sub.4 olefins from a catalytically cracked or thermally cracked naphtha stream. The naphtha stream is contacted 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 from about 500 to 650.degree. C. and a hydrocarbon partial pressure from about 10 to 40 psia.

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Baton Rouge, LA, United States of America

Brian Erik Henry