Exxon Research and Engineering Company

Exxonmobil Chemical Patents Inc.

Exxonmobil Research and Engineering Company

Exxon Chemical Patents, Inc.

Tan Jen Chen

Philip Andrew Ruziska

Brian Erik Henry

Gordon Frederick Stuntz

Stephen M Davis

Paul F Keusenkothen

Charles P Darnell

Karl Gottlieb Strohmaier

Gary David Mohr

Kenneth Ray Clem

Johannes Petrus Verduijn

Avelino Corma Canos

David E W Vaughan

Antonio Chica Lara

Joaquin Perez Pariente

Javier Agundez Rodriguez

W S Ho

Joseph L Feimer

Russell J Koveal

Jannetje Maatje Van Den Berge

Mechilium Johannes Janssen

Mechilium Johannes Gerardus Janssen

Enrique F Juarez

James Sweet Sweet

Phillip Andrew Ruziska

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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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.

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

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

There is provided a process for converting hydrocarbons which utilizes a zeolite bound zeolite catalyst that has enhanced performance when utilized in hydrocarbon conversion processes, e.g., catalytic cracking, alkylation, disproportionation of toluene, isomerization, and transalkylation reactions. The catalyst comprises a first zeolite having particles of greater than about 0.1 micron average particle size and a binder comprising second zeolite particles having an average particle size less than said first particles.

Toluene disproportionation process using a zeolite bound zeolite catalyst

Hydrocarbon conversion process using a zeolite bound zeolite catalyst

Distillate or hydrotreated distillate effluent is separated into an aromatics rich permeate and an aromatics lean retentate by use of a permselective membrane with the aromatic rich permeate being sent to a hydrotreater, thereby increasing the quantity of reduced aromatics content product.

Membrane process for enhanced distillate or hydrotreated distillate

The pervaporative treatment of hydrocarbon feeds which have been exposed to air or oxygen and which contain mixtures of aromatic and non-aromatic hydrocarbons to selectively separate the feed into an aromatics rich stream and a non-aromatics rich stream is improved by the step of pretreating the hydrocarbon feed over an adsorbent such as attapulgite clay.

Feed pretreatment for pervaporation process

The selectivity of a membrane pervaporation aromatics/non-aromatics separation process is unexpectedly improved by the recycle of permeate to the separation process for co-processing with fresh feed. The selectivity obtained is greater than that achieved by processing either the feed or a recycle permeate stream by itself.

Pervaporation process employing permeate recycle

The present invention is a process for the recovery of normal alcohols, especially C.sub.1 -C.sub.20 n-alcohols, preferably n-C.sub.4 -C.sub.14 alcohols, most preferably n-C.sub.6 -C.sub.11 alcohols from n-paraffins by means of pervaporation through a membrane. The alcohols/paraffin feed mixture may be that produced in the Fischer-Tropsch synthesis process wherein mixtures of CO and H.sub.2 are reacted to produce paraffin waxes and a minor but still valuable amount of alcohols.

Recovery of alcohols from n-paraffins by pervaporation

The separation of aromatic hydrocarbons from mixtures of aromatic and non-aromatic hydrocarbon feeds under pervaporation conditions, is improved by the control of the amount of oxygen present in the feed. The amount of oxygen in the feed, such as heavy cat naphtha or other cracked feed, should be less than 30 wppm, preferably less than 10 wppm. The oxygen level in the feed can be controlled by the addition of small amount of oxygen scavenger into the feed. Hindered phenols are representative of useful oxygen scavengers.

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Kingwood, TX, United States of America

Tan Jen Chen