Abstract: A respirator includes a head unit configured to be received on a human head and a purifying unit configured to provide purified air to the head unit. The purifying unit includes a first housing portion having an interior side defining a blower cavity, an exterior side defining a partial filter chamber with a filter sealing surface, and an inlet hole circumscribed by the sealing surface and extending between the interior and exterior sides. A second housing portion has an interior side defining a blower cavity. The first and second housings are attached to each other to form a housing such that the blower cavities are opposite each other to define a blower chamber within the housing. A blower is disposed in the blower chamber. A filter covers over the inlet hole and is disposed against the sealing surface such that air entering the hole passes through the filter.

Abstract: Systems and processes are disclosed for producing petrochemical products, such as ethylene, propene and other olefins from crude oil in high severity fluid catalytic cracking (HSFCC) units. Processes include separating a crude oil into a light fraction and a heavy fraction, cracking the light fraction and heavy fraction in separation separate cracking reaction zones, and regenerating the cracking catalysts in a two-zone having a first regeneration zone for the first catalyst (heavy fraction) and a second regeneration zone for the second catalyst (light fraction) separate from the first regeneration zone. Flue gas from the first catalyst regeneration zone is passed to the second regeneration zone to provide additional heat to raise the temperature of the second catalyst of the light fraction side. The disclosed systems and processes enable different catalysts and operating conditions to be utilized for the light fraction and the heavy fraction of a crude oil feed.

Abstract: Disclosed is a method for producing low carbon olefins and/or aromatics from feedstock comprising naphtha. The method can include the following steps: a) feeding feedstock comprising naphtha into a fast fluidized bed reactor; b) contacting the feedstock with a catalyst under conditions to produce a gas product and spent catalyst; c) separating the gas product to produce a stream comprising primarily one or more low carbon olefins and/or one or more aromatics; d) transporting the spent catalyst to a regenerator; e) regenerating the spent catalyst in the regenerator to form regenerated catalyst; and f) returning the regenerated catalyst to the fast fluidized bed reactor.

Abstract: A process for producing propylene and a low-sulfur fuel oil component, comprising the steps of contacting a heavy feedstock oil with a solvent for extraction separation to obtain a deasphalted oil and a deoiled asphalt; contacting the deasphalted oil and optionally a light feedstock oil with a catalytic conversion catalyst for reaction to obtain a reaction product comprising propylene; separating the reaction product to obtain a catalytic cracking distillate oil, and subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low-sulfur hydrogenated distillate oil, wherein the low-sulfur hydrogenated distillate oil and/or the deoiled asphalt is suitable for use as a fuel oil component. The process allows the conversion of saturated hydrocarbons in the heavy feedstock into propylene, eliminates the use of saturated hydrocarbons in the fuel oil component, and thus has better economic and social benefits.

Abstract: A system comprising a riser reactor comprising a gas oil feedstock and a first catalyst under catalytic cracking conditions to yield a riser reactor product comprising a cracked gas oil product and a first used catalyst; a intermediate reactor comprising at least a portion of the cracked gas oil product and a second catalyst under high severity conditions to yield a cracked intermediate reactor product and a second used catalyst; wherein the intermediate reactor feedstock comprises at least one of a fatty acid and a fatty acid ester.

Abstract: Heavy gas oil components, coking process recycle, and heavier hydrocarbons in the delayed coking process are cracked in the coking vessel by injecting a catalytic additive into the vapors above the gas/liquid-solid interface in the coke drum during the coking cycle. The additive comprises cracking catalyst(s) and quenching agent(s), alone or in combination with seeding agent(s), excess reactant(s), carrier fluid(s), or any combination thereof to modify reaction kinetics to preferentially crack these components. The quenching effect of the additive can be effectively used to condense the highest boiling point compounds of the traditional recycle onto the catalyst(s), thereby focusing the catalyst exposure to these target reactants. Exemplary embodiments of the present invention can also provide methods to (1) reduce coke production, (2) reduce fuel gas production, and (3) increase liquids production.

Abstract: The present invention describes a process for the production of gasoline in a fluid catalytic cracking unit having at least one principal reactor operating using feeds with a low Conradson Carbon and a high hydrogen content, said process comprising recycling a coking cut either to a side chamber branching off the stripper or within the stripper itself by means of a tubular vessel within said stripper.

Abstract: One exemplary embodiment can be a fluid catalytic cracking unit. The fluid catalytic cracking unit can include a first riser, a second riser, and a disengagement zone. The first riser can be adapted to receive a first feed terminating at a first reaction vessel having a first volume. The second riser may be adapted to receive a second feed terminating at a second reaction vessel having a second volume. Generally, the first volume is greater than the second volume. What is more, the disengagement zone can be for receiving a first mixture including at least one catalyst and one or more products from the first reaction vessel, and a second mixture including at least one catalyst and one or more products from the second reaction vessel. Typically, the first mixture is isolated from the second mixture.

Abstract: Undesirable gas oil components are selectively cracked or coked in a coking vessel by injecting an additive into the vapors of traditional coking processes in the coking vessel prior to fractionation. The additive contains catalyst(s), seeding agent(s), excess reactant(s), quenching agent(s), carrier(s), or any combination thereof to modify reaction kinetics to preferentially crack or coke these undesirable components that typically have a high propensity to coke. Exemplary embodiments of the present invention also provide methods to control the (1) coke crystalline structure and (2) the quantity and quality of volatile combustible materials (VCMs) in the resulting coke. That is, by varying the quantity and quality of the catalyst, seeding agent, and/or excess reactant the process may affect the quality and quantity of the coke produced, particularly with respect to the crystalline structure (or morphology) of the coke and the quantity & quality of the VCMs in the coke.

Abstract: A reactor process added to a coking process to modify the quantity or yield of a coking process product and/or modify certain characteristics or properties of coking process products.

Abstract: Process for the preparation of C3 and C4 olefins and gasoline by: (a) contacting in a fluidised bed reactor a light hydrocarbon feedstock with a first catalyst inventory comprising a medium pore size zeolite catalyst, wherein the first catalyst inventory is a fresh catalyst inventory; (b) combining at least part of the catalyst inventory as used in step (a) with one or more catalyst streams to form a second catalyst inventory comprising a medium pore size zeolite catalyst and a large pore size zeolite catalyst; (c) contacting a hydrocarbon feedstock with the second catalyst inventory in a reactor riser to form cracked products.

Abstract: A process is disclosed for converting distillate to gasoline-range hydrocarbons using a two-stage catalyst system including a first catalyst containing platinum, palladium, or platinum and palladium, and an acidic support, and a second catalyst containing iridium and an inorganic oxide support, and optionally nickel.

Abstract: A process for the fluid catalytic cracking of mixed hydrocarbon feeds from different sources is described, such as feeds A and B of different crackability, the process being especially directed to obtaining light fractions such as LPG and comprising injecting feed A in the base of the riser reactive section and feed B, of lower crackability, at a height between 10% and 80% of the riser, with feed B comprising between 5% and 50% of the total processed feed. The process requires that the feeds present differences in the contaminant content, improved dispersion of feeds A and B and feed B injection temperature same or higher than that of feed A.

Abstract: Disclosed is a process for making middle distillate and lower olefins. The process includes catalytically cracking a gas oil feedstock within a riser reactor zone by contacting under suitable catalytic cracking conditions within the riser reactor zone the gas oil feedstock with a middle distillate selective cracking catalyst that comprises amorphous silica alumina and a zeolite to yield a cracked gas oil product and a spent cracking catalyst. The spent cracking catalyst is regenerated to yield a regenerated cracking catalyst. Within an intermediate cracking reactor such as a dense bed reactor zone and under suitable high severity cracking conditions a gasoline feedstock is contacted with the regenerated cracking catalyst to yield a cracked gasoline product and a used regenerated cracking catalyst. The used regenerated cracking catalyst is utilized as the middle distillate selective catalyst.

Abstract: A device for the fluidized bed cracking of a hydrocarbon charge using two reaction chambers linked together by a cooling particles transferrer, a fractionating column and conduits to supply the hydrocarbonated effluents from each of the two chambers to the fractionating column. The fractionating column has, internally, at least two different areas: a first partitioned fractionating area in the form of two compartments, each of which communicates with a second common fractionating area. The conduits for the supply of effluents from the first and the second reaction chamber terminate, respectively, in the first and second compartment of the partitioned fractionating area. A recycler and an injector are provided for recycling and injecting into one of the reaction chambers of at least one cut drawn off from the partitioned fractionating compartment of the effluents of the other reaction chamber.

Abstract: The present invention relates to a process for the conversion of hydrocarbon streams with 95% true boiling point less than 400° C. to very high yield of liquefied petroleum gas in the range of 45-65 wt % of feed and high octane gasoline, the said process comprises catalytic cracking of the hydrocarbons using a solid fluidizable catalyst comprising a medium pore crystalline alumino-silicates with or without Y-zeolite, non crystalline acidic materials or combinations thereof in a fluidized dense bed reactor operating at a temperature range of 400 to 550° C., pressure range of 2 to 20 kg/cm2 (g) and weight hourly space velocity in range of 0.1 to 20 hour?1, wherein the said dense bed reactor is in flow communication to a catalyst stripper and a regenerator for continuous regeneration of the coked catalyst in presence of air and or oxygen containing gases, the catalyst being continuously circulated between the reactor-regenerator system.

Abstract: A process for selectively producing C2 to C4 olefins 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° C. and a hydrocarbon partial pressure from about 10 to about 40 psia (about 70 to about 280 kPa).

Abstract: The present invention relates to a catalytic cracking process and a device used in the process in particular, the present invention provides a catalytic cracking process, which comprises which comprises: 1) catalytic cracking a feedstock in the first riser for less than about 1.5 second and sending the resultant stream into the first separating device,; 2) catalytic cracking the recycle oil obtained from the first separating device in the second riser for less than about 1.

Abstract: Supercritical conversion of hydrocarbons boiling above 538° C. (1000° F.) with a solvating hydrocarbon at a weight ratio of solvating hydrocarbon to high-boiling hydrocarbons of at least 2:1 and at conditions above the critical temperature and pressure of the high-boiling hydrocarbons-solvent mixture, in the presence of hot fluidized solids. The hydrocarbons are supplied to a reaction zone at a temperature below that of the hot solids supplied thereto, whereby the resulting hydrocarbons-solids suspension has a thermal equilibrium temperature corresponding to the reaction temperature. The conversion has high rates of sulfur, nitrogen and metals removal, nearly complete conversion to lower molecular weight products, high naphtha and distillate selectivity, and low coke formation.

Abstract: According to this invention, there is provided a process and apparatus for catalytic cracking of various petroleum based heavy feed stocks in the presence of solid zeolite catalyst and high pore size acidic components for selective bottom cracking and mixtures thereof, in multiple riser type continuously circulating fluidized bed reactors operated at different severities to produce high yield of middle distillates, in the range of 50–65 wt % of fresh feed.

Abstract: A process and apparatus are disclosed contacting hydrocarbon feed with catalyst in a reactor vessel under conditions more vigorous than bubbling bed conditions and preferably fast fluidized flow conditions. The vigorous conditions assure thorough mixing of catalyst and feed to suppress formation of dry gas and the promotion of hydrogen transfer reactions.

Abstract: A process and apparatus is disclosed for contacting feed with mixed catalyst in a secondary reactor that is incorporated into an FCC reactor. The mixed catalyst used in the secondary reactor is regenerated catalyst from a regenerator that regenerates spent catalyst from an FCC reactor that is mixed with spent catalyst from either the FCC reactor or the secondary reactor. The mixing of spent and regenerated catalyst reduces the catalyst temperature and tempers catalyst activity to inhibit both thermal and catalytic cracking reactions.

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 present invention relates to a catalytic cracking process and a device used in the process in particular, the present invention provides a catalytic cracking process, which comprises which comprises:

Abstract: A process for cracking, in a fluidized bed, a hydrocarbon charge wherein the cooling particles, which may optionally also be catalytic particles, circulate in two successive reaction chambers (1; 16), in each of which they are brought into contact with at least one cut of hydrocarbons, and the reaction effluents from each of the chambers are directed towards one and the same fractionating unit. The effluents from each of the reaction chambers (1; 16) are fractionated in part separately in one and the same partially partitioned fractionating unit, and at least one cut (12) obtained by separately fractionating the effluents from one of the two reaction chambers (1; 16) is, as a whole or in part, reinjected into the other chamber.

Abstract: The invention relates to a process for converting cycle oils produced in catalytic cracking reactions into light olefin, preferably propylene. More particularly, the invention relates to a process for hydroprocessing a catalytically cracked light cycle oil, and then re-cracking in a second FCC 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: The invention relates to a two-stage catalytic cracking process for converting cycle oils to more valuable products. More particularly, the invention relates to a process that includes interstage hydroprocessing and a tailored catalyst mixture in a second catalytic cracking stage where the hydroprocessed cycle oil is re-cracked.

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 two-stage process for converting petroleum residua and other low value oils to high valued gasoline blendstocks and light olefins. The first stage is comprised of a thermal process unit containing a reaction zone comprised of a horizontal moving bed of fluidized hot particles operated at temperatures from about 500 to 600° C. and having a short vapor residence time, and the second stage is comprised of a catalytic conversion zone operated at a temperature of about 525° C. to about 650° C., and also having a short vapor residence time, preferably shorter than that of the first stage reaction zone.

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 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: Disclosed is a catalytic cracking process that includes more than one catalytic cracking reaction step. The process integrates catalytic cracking steps with hydroprocessing in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, one hydroprocessing step is included between the cat cracking reaction steps, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step.

Abstract: 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.

Abstract: The invention provides a process for improving the conversion of a hydrocarbon feedstock to light olefins comprising the steps of first contacting the hydrocarbon feedstock with a light olefin producing cracking catalyst and subsequently thermally cracking the unseparated stream to produce additional ethylene. Preferably the zeolite catalyst is selected from the group consisting of ferrierite, heulandite, phillipsite, faujasite, chabazite, erionite, mordenite, offretite, gmelinite, analcite, ZSM-5, ZSM-11, ZSM-25, gallium silicate zeolite, zeolite Beta, zeolite rho, ZK5, titanosilicate, zeolites having a silica to alumina molar ratio within the range of about 2.0:1 to 2000:1 ferrosilicate; zeolites such as those described in U.S. Pat. No. 4,238,318; borosilicate zeolites such as those described in Belgian Pat. No. 859656; zeolites designated by the Linde Division of Union Carbide by the letters of X, Y, A, L; zeolites such as those described in U.S. Pat. No.

Abstract: A two-stage process for obtaining a substantial amount of olefinic product from a residua feedstock. The first stage is comprised of a thermal process unit containing a reaction zone comprised of a horizontal moving bed of fluidized hot particles operated at temperatures from about 500.degree. to 600.degree. C. and having a short vapor residence time, and the second stage thermal conversion zone operated at a temperature of about 700.degree. C. to about 1100.degree. C., and also having a short vapor residence time.

Abstract: A two-stage process for obtaining a substantial amount of olefinic product from a residua feedstock. The first stage is comprised of a thermal process unit containing a reaction zone comprised of a horizontal moving bed of fluidized hot particles operated at temperatures from about 500.degree. to 600.degree. C. and having a short vapor residence time, and the second stage thermal conversion zone operated at a temperature of about 700.degree. C. to about 1100.degree. C., and also having a short vapor residence time.

Abstract: Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing process step between the catalytic cracking reaction steps in order to maximize olefins production, mid-distillate quality and naphtha octane level in the cracked products. Preferably, a first cracked hydrocarbon product is obtained from a first cracking stage and separated into a mid-distillate and gas oil containing fraction having an initial boiling point of at least 300.degree. F., the distillate and gas oil containing fraction is hydroprocessed, and a naphtha fraction and a gas oil containing bottoms fraction of the hydroprocessed material are cracked in a second cracking stage.

Abstract: Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing step between the catalytic cracking reaction steps in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, the hydroprocessing step is included between the reaction stages, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step.

Abstract: Disclosed is a catalytic cracking process which includes more than one catalytic cracking reaction step. The process integrates a hydroprocessing step between the catalytic cracking reaction steps in order to maximize olefins production, distillate quality and octane level of the overall cracked product. Preferably, the hydroprocessing step is included between the reaction stages, and a portion of the hydroprocessed products, i.e., a naphtha and mid distillate fraction, is combined with cracked product for further separation and hydroprocessing. It is also preferred that the first catalytic cracking reaction step be a short contact time reaction step.

Abstract: The invention relates to a process for catalytic cracking and the associated apparatus in which the cracking reaction takes place in two substantially vertical and successive reaction zones, the loads being introduced into the first zone where it circulates from the top downwards, then at least a part of the product obtained is introduced into a second reaction zone in which it circulates in an ascending fashion. A supplementary hydrocarbonated phase is advantageously introduced into the product entering the second zone. The invention applies particularly to heavy loads, with a U-shaped apparatus.

Abstract: Methods for the fluidized catalytic cracking of plural hydrocarbon feedstocks in a riser reactor are disclosed. The processes generally comprises contacting a relatively light hydrocarbon feedstock in a first reaction zone with a first catalyst stream comprising spent catalyst, contacting a relatively heavy hydrocarbon feedstock in a second reaction zone with a second catalyst stream comprising freshly regenerated catalyst, and introducing at least a portion of the effluent from the first reaction zone into the second reaction zone. The first reaction zone and the second reaction zone preferably comprise first and second riser reaction zones, respectively.

Abstract: A fluid catalytic cracking (FCC) process and apparatus which employs relatively more elutriatable catalyst particles comprising intermediate pore zeolite, particularly ZSM-5, and relatively less elutriatable catalyst particles comprising large pore zeolite, preferably zeolite Y. The process and apparatus employ a first stripping vessel which also separates a more elutriatable first portion of catalyst from a less elutriatable second portion of catalyst. The more elutriatable first portion passes to a second stripping vessel, and subsequently recycles to a fluid catalytic cracking reactor riser. The second portion of less elutriatable catalyst passes from the first stripping vessel to a fluid catalytic cracking regenerator vessel and, after being regenerated, recycles to the reactor riser. The more elutriatable first portion contains a higher ratio of intermediate pore catalyst particles to large pore catalyst particles than does the second portion.

Abstract: A process for the conversion of residual asphaltene-containing hydrocarbonaceous charge stock to selectively produce large quantities of high quality middle distillate while minimizing hydrogen consumption.

Abstract: A process and system for the production of olefins from heavy hydrocarbon feedstocks. A heavy hydrocarbon feed is first pretreated at high pressure and moderate temperatures to preferentially remove coke precursors in a liquid product. The pretreated hydrocarbon is then separated into lighter and heavier fractions; the lighter fraction being further thermally cracked to produce olefins.

Abstract: Hydrocarbon feedstocks, especially those high in Ramsbottom carbon, are vaporized by contact with a relatively inactive coked cracking catalyst, separating the resulting intermediate into a high and low boiling fraction, and cracking the high boiling fraction in a fluid catalytic cracker containing active cracking catalyst.

Abstract: A high pore volume solid sorbent material of low cracking activity and comprising a select group of metal additives to immobilize accumulated vanadium compounds deposited on the sorbent material in a heavy oil feed visbreaking zone is described and the conditions employed to effect demetallization and decarbonization of the heavy oil feed to produce vaporous products boiling up to about 1000.degree. F. Deposition of metal contaminants within the pores of the high pore volume material is encouraged by restricting the volume of the sorbent pores filled with oil feed to within the range of 1/4 to 2/3.

Abstract: A two-stage cascade flow fluid catalytic cracking process capable of converting high molecular weight hydrocarbons containing catalyst poisons into products of lower molecular weight with high activity cracking catalyst susceptible to catalyst poisons, the cascade flow process resulting in higher yields of desired motor fuel fractions than those obtainable with conventional riser flow fluid catalytic cracking processes. Catalyst poisons, e.g.

Abstract: A process for the production of highly aromatic petroleum fractions from various petroleum feedstocks suitable for catalytic cracking in a fluidized catalytic cracking unit wherein heavy gas oil from a first fluidized catalytic cracking unit is subjected to further catalytic cracking in a separate fluid catalytic cracking unit at temperatures in the range of 565.degree. to 650.degree. C. producing light olefins and a heavy gas oil consisting of essentially aromatic components suitable for the production of needle coke, and the method of producing needle coke from various hydrocarbon cracking stocks.