Abstract: This disclosure relates to devices, e.g., baffle plate and combination dipleg valve/baffle devices, for use in achieving rapid disengagement of entrained hydrocarbons vapors, especially in high flux spent catalyst flow exiting from a cyclone separator dipleg in a fluidized catalytic cracking (FCC) unit. The baffle plate is preferably located near and typically below the catalyst dipleg of a fluid catalytic cracking reactor or separation zone and comprises a baffle plate body member having a surface, and in preferred embodiments also includes one or more apertures located on at least a portion of the surface. The valve/baffle is located at the outlet of the catalyst dipleg and comprises a combination valve and catalyst baffle in which the valve/baffle is designed to allow the top surface of the valve/baffle to seat against the dipleg outlet until the weight of the catalyst above the valve/baffle forces it to open.

Abstract: 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.

Abstract: The atomization of a fluid injected into an atomization zone is enhanced by providing the fluid with an effective amount of an additive capable of reducing the static and dynamic interfacial tension of the fluid components.

Abstract: 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 60–300° F. naphtha crackate as the feed.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: A process for producing polymers from olefins selectively produced by a two stage process for selectively producing C2 to C4 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° C. and a hydrocarbon partial pressure from about 10 to 40 psia.

Abstract: 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.

Abstract: A two stage process for reforming a naphtha feed at low severities with tin modified platinum-iridium catalysts. In particular, both high selectivity, and high activity are manifested by such catalysts in reforming a naphtha feed at low severities in a first fixed-bed reforming stage which is comprised of a series of reforming zones, or reactors; i.e., within the dehydrogenation and ring isomerization zones of a reforming unit. The first stage zones are charged with a tin-containing platinum-iridium catalyst, and the naphtha feed reformed to produce an intermediate RON clear C.sub.5 + liquid reformate. The intermediate octane product of the first reforming stage is passed to a second stage which is comprised of one or more moving-bed reforming zones, or reactors, which are operated in a continuous catalyst regeneration mode with platinum containing catalyst.

Abstract: A two stage process for catalytically reforming a gasoline boiling range hydrocarbonaceous feedstock. The reforming is conducted in two stages wherein the first stage is operated in a fixed-bed mode, and the second stage is operated in a moving-bed continual catalyst regeneration mode. A gaseous stream comprised of hydrogen and predominantly C.sub.4.sup.-- hydrocarbon gases are separated between stages. A portion of the hydrogen-rich gaseous stream is recycled and the remaining portion along with the C.sub.5.sup.+ stream are sent to second stage reforming.

Abstract: Catalytic reforming wherein the lead reactor contains a catalyst comprised of platinum and a relatively low level of Re on an inorganic oxide support. The tail reactor contains a tin modified platinum-iridium catalyst wherein the metals are substantially uniformly dispersed throughout the inorganic oxide support.

Abstract: A process for reforming a naphtha feed at low severities with tin modified platinum-iridium catalysts. In particular, both high selectivity, and high activity are manifested by such catalysts in reforming a naphtha feed at low severities in the lead reactor, or reactors, of a series of reactors; i.e., within the dehydrogenation and ring isomerization zone, or zones, of a reforming unit. The lead reactors of the series are charged with a tin-containing platinum-iridium catalyst, and the naphtha feed reformed to produce a low RON clear C.sub.5 + liquid reformate. The low octane product of the lead reactors may be transferred to a mogas pool, into blending components, or all or some part of the product further reformed. Preferably, the product is further reformed in a tail reactor, and preferably the tail reactor is charged with a non-tin containing platinum, or platinum-iridium catalyst.

Abstract: Tin modified platinum-iridium catalysts provide high yields of C.sub.5 +liquid reformate in catalytic reforming, concurrent with high activity. In particular, the tin modified platinum-iridium catalysts are of unusually high selectivity, as contrasted with known iridium promoted platinum catalysts. The high selectivity is manifested in reforming a naphtha feed in a reactor charged to capacity with the catalyst, but particularly when used in the dehydrocyclization zone, or tail reactor of a series of reactors, while the lead reactors of the series contain a non tin-containing platinum catalyst, especially a platinum-iridium, or a platinum-rhenium catalyst. The tin modified platinum-iridium catalysts are also highly active, with only moderate loss in the high activity for which iridium stabilized platinum catalysts are known.

Abstract: A two stage process for catalytically reforming a gasoline boiling range hydrocarbonaceous feedstock. The reforming is conducted in two stages wherein the first stage is operated in a fixed bed mode, and the second stage is operated in a moving bed continual catalyst regeneration mode. A gaseous stream comprised of hydrogen and predominantly C.sub.4.sup.- and a C.sub.5.sup.+ liquid stream are produced between stages. A portion of the hydrogen-rich stream is recycled and the and the remaining portion and an aromatics-lean stream, which is obtained during aromatics separation between stages, is sent to second stage reforming.

Abstract: Disclosed is a process for catalytically reforming a gasoline boiling range hydrocarbonaceous feedstock. The reforming is conducted in multiple stages with heavy aromatics removal between the first and second stages.

Abstract: A two stage catalytic reforming process. The first stage is comprised of two separate fixed-bed reforming units each comprised of one or more serially connected fixed-bed reforming zones. The second stage is comprised of one or more moving-bed reforming zones with continual catalyst regeneration. A hydrogen-rich gaseous stream is separated after each fixed-bed unit and a portion is recycled to the respective fixed-bed reforming zones.