Abstract: Systems and methods are provided for co-processing of pyrolysis tar with pre-pyrolysis flash bottoms. In some aspects, the co-processing can correspond to solvent-assisted hydroprocessing. By combining pyrolysis tar and flash bottoms with a solvent, various difficulties associated with hydroprocessing of the fractions can be reduced or minimized, such as difficulties associated with hydroprocessing of high viscosity feeds and/or high sulfur feeds. Optionally, separate solvents and/or fluxes can be used for the pyrolysis tar and the flash bottoms. The resulting upgraded products can be suitable, for example, for inclusion in low sulfur fuel oils (LSFO).

Abstract: Processes for improving hydrocarbon feedstock compatibility are provided. More specifically, a process for preparing a liquid hydrocarbon product includes heat soaking a tar stream to produce a reduced reactivity tar and blending the reduced reactivity tar with a utility fluid comprising recycle solvent to produce a lower viscosity, reduced reactivity tar. The process also includes hydroprocessing the lower viscosity, reduced reactivity tar at a temperature of greater than 350° C. to produce a total liquids product containing the liquid hydrocarbon product and the recycle solvent. The process further includes separating the recycle solvent from the total liquids product, where the recycle solvent has the SBN of greater than 110, and flowing the recycle solvent to the reduced reactivity tar for blending to produce the lower viscosity, reduced reactivity tar.

Abstract: The invention described herein relates to a novel process to create carbon black feed stocks derived from coal by utilizing direct coal liquefaction resulting in an economic process for producing carbon black feedstock. Moreover, relative to the current state of the art (use of FCC slurry oil), the invention process will be significantly more profitable when oil prices increase.

Abstract: The invention described herein relates to a novel process to create carbon black feed stocks derived from coal by utilizing direct coal liquefaction resulting in an economic process for producing carbon black feedstock. Moreover, relative to the current state of the art (use of FCC slurry oil), the invention process will be significantly more profitable when oil prices increase.

Abstract: A hydrocarbon conversion process comprises providing a hydrocarbon feedstock comprising an effluent fraction from a pyrolysis process, wherein the effluent fraction has an initial boiling point at atmospheric pressure of at least 177° C. and a final boiling point at atmospheric pressure of no more than 343° C. and comprises at least 0.5 wt. % of olefinic hydrogen atoms based on the total weight of hydrogen atoms in the effluent fraction. The hydrocarbon feedstock is hydroprocessed in at least one hydroprocessing zone in the presence of treatment gas comprising molecular hydrogen under catalytic hydroprocessing conditions to produce a hydroprocessed product comprising less than 0.5 wt. % of olefinic hydrogen atoms based on the total weight of hydrogen atoms in the hydroprocessed product. The hydroprocessing conditions comprise a temperature from 150 to 350° C. and a pressure from 500 to 1500 psig (3550 to 10445 kPa-a).

Abstract: According to an embodiment disclosed, a feedstock hydrocarbon may be processed by a method which may include separating the feedstock hydrocarbon into a lesser boiling point hydrocarbon fraction and a greater boiling point hydrocarbon fraction, cracking the greater boiling point hydrocarbon fraction in a high-severity fluid catalytic cracking reactor unit to form a catalytically cracked effluent, cracking the lesser boiling point hydrocarbon fraction in a steam cracker unit to form a steam cracked effluent, and separating one or both of the catalytically cracked effluent or the steam cracked effluent to form two or more petrochemical products. In one or more embodiments, the feedstock hydrocarbon may include crude oil and one of the petrochemical products may include light olefins.

Abstract: The invention relates to pyrolysis tar upgrading processes, and in particular for decreasing reactor pressure drop when the upgrading includes converting pyrolysis tar in a reactor. The invention also relates to upgraded pyrolysis tar, and the use of upgraded pyrolysis tar, e.g., as a fuel oil blending component.

Abstract: A fluid catalytic cracking catalyst for increased production of propylene and gasoline from heavy hydrocarbon feedstock, the catalyst comprising between 10 and 20% by weight of an ultra-stable Y-type zeolite, between 10 and 20% by weight of a phosphorous modified sub-micron ZSM-5, between 20 and 30% by weight of a pseudoboehmite alumina, and between 30 and 40% by weight kaolin.

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: A process for producing light olefins and aromatics, which comprises reacting a feedstock with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone. The spent catalyst is separated, from the reaction product vapor, regenerated, and then returned to the reactor. The reaction product vapor is separated to obtain the desired products, light olefins and aromatics. This process efficiently produces light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

Abstract: The invention relates to processes for upgrading products obtained from hydrocarbon pyrolysis, equipment useful for such processes, and the use of upgraded pyrolysis products.

Abstract: The invention relates to upgraded pyrolysis products, hydroconversion processes for upgrading products obtained from hydrocarbon pyrolysis, equipment useful for such processes. In particular the invention provides methods for reducing coke fouling in such equipment.

Abstract: A hydrocarbon feed is passed to a first zone of a vaporization unit to separate a first vapor stream and a first liquid stream. The first liquid stream is passed to a second zone of the vaporization unit and contacted with a counter-current steam to produce a second vapor stream and a second liquid stream. The first vapor stream and the second vapor stream are cracked in the radiant section of the steam cracker to produce a cracked effluent. The second liquid stream is catalytically cracked to produce a cracked product. The cracked product is distilled to produce an overhead stream, a light cycle oil, and a heavy cycle oil. The light cycle oil is reacted with hydrogen in the presence of a catalyst to produce a hydrotreated light cycle oil. The hydrotreated light cycle oil and the overhead stream are fed to the vaporization unit.

Abstract: Methods and apparatuses for upgrading a pyrolysis oil stream and a hydrocarbon stream are provided herein. In an embodiment, a method for upgrading a pyrolysis oil stream and a hydrocarbon stream includes separately introducing the pyrolysis oil stream and the hydrocarbon stream into a reaction zone to form a mixture of the pyrolysis oil stream and the hydrocarbon stream in the reaction zone. The mixture of the pyrolysis oil stream and the hydrocarbon stream is catalytically cracked in the presence of a particulate cracking catalyst in the reaction zone. The pyrolysis oil stream is maintained at a temperature of less than or equal to about 100° C. substantially up to introduction into the reaction zone.

Abstract: Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) is processed to produce useful products, such as fuels. For example, systems can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy materials, to produce ethanol and/or butanol, e.g., by fermentation.

Abstract: An integrated hydrotreating, steam pyrolysis and catalytic cracking process for the production of olefins and aromatic petrochemicals from a crude oil feedstock is provided. Crude oil and hydrogen are charged to a hydroprocessing zone under conditions effective to produce a hydroprocessed effluent, which is thermally cracked in the presence of steam in a steam pyrolysis zone to produce a mixed product stream. Heavy components are catalytically cracked, which are derived from one or more of the hydroprocessed effluent, a heated stream within the steam pyrolysis zone, or the mixed product stream catalytically cracking. Catalytically cracked products are produced, which are combined with the mixed product stream and the combined stream is separated, and olefins and aromatics are recovered as product streams.

Abstract: This invention provides a fluidized catalytic cracking apparatus and process for converting a hydrocarbon feedstock containing higher concentrations of Conradson Carbon Residue (CCR), metal impurities, etc into lighter products by employing two riser reactors in which the feed impurities are removed using an adsorbent in a first riser reactor and cracking a portion of first riser reactor liquid product in a second riser reactor to lighter products using the active catalyst thus eliminating the catalyst deactivation due to metal, impurities and FCC catalyst activity dilution effect to achieve a better conversion and higher catalyst longevity.

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: The present invention is directed to the upgrading of heavy petroleum oils of high viscosity and low API gravity that are typically not suitable for pipelining without the use of diluents. The method comprises introducing a particulate heat carrier into an up-flow reactor, introducing the feedstock at a location above the entry of the particulate heat carrier, allowing the heavy hydrocarbon feedstock to interact with the heat carrier for a short time, separating the vapors of the product stream from the particulate heat carrier and liquid and byproduct solid matter, collecting a gaseous and liquid product mixture comprising a mixture of a light fraction and a heavy fraction from the product stream, and using a vacuum tower to separate the light fraction as a substantially bottomless product and the heavy fraction from the product 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: An apparatus for catalytic cracking of feedstock includes a first channel in which a feedstock is treated with an adsorbent to obtain a treated intermediate. The apparatus further comprises a separator-reactor vessel. The separator-reactor vessel includes an adsorbent separating region to remove the adsorbent from the treated intermediate. The separator-reactor vessel further includes a second channel connected to the adsorbent separating region. The treated intermediate is contacted with a catalyst in the second channel to produce a cracking yield. The second channel terminates in a catalyst separating region of the separator-reactor vessel. The catalyst is removed from the cracking yield in the catalyst separating region. The separator-reactor vessel further includes a physical partition disposed between the adsorbent separating region and the catalyst separating region to separate the two regions.

Abstract: Novel catalytic compositions for cracking of crude oil fractions are disclosed. The catalytic compositions comprise a basic material. When used in a cracking process, preferably a FCC process, the resulting LCO and HCO fractions have desirably low aromatics levels. Further disclosed is a one-stage FCC process using the catalytic composition of the invention. Also disclosed is a two-stage FCC process for maximizing the LCO yield.

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: This invention relates to a process for the selective conversion of vacuum gas oil. The vacuum gas oil is treated in a two step process. The first is thermal conversion and the second is catalytic cracking of the products of thermal conversion. The product slate can be varied by changing the conditions in the thermal and catalytic cracking steps as well as by changing the catalyst in the cracking step. The combined products from thermal and catalytic cracking are separated in a divided wall fractionator.

Abstract: The present invention relates to a process for the selective conversion of hydrocarbon feed having a Conradson Carbon Residue content of 0 to 6 wt %, based on the hydrocarbon feed. The hydrocarbon feed is treated in a two-step process. The first is thermal conversion and the second is catalytic cracking of the products of the thermal conversion. The present invention results in a process for increasing the distillate production from a hydrocarbon feedstream for a fluid catalytic cracking unit. The resulting product slate from the present invention can be further varied by changing the conditions in the thermal and catalytic cracking steps as well as by changing the catalyst in the cracking step.

Abstract: A process 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: 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: The invention is to provide a catalyst excellent in product producibility and selectivity, and in coking degradation resistance and regeneration degradation resistance, which is for production of ethylene and propylene through catalytic conversion from a hydrocarbon material. The invention relates to a method for producing ethylene and propylene through catalytic conversion from an olefin, by contacting a hydrocarbon material with a zeolite-containing shaped catalyst satisfying the following requirements (1) to (6), in a reactor: (1) the zeolite is an intermediate pore-size zeolite having a pore size of from 5 to 6.5 angstroms, (2) the zeolite does not substantially contain a proton, (3) the zeolite contains at least one metal selected from the group consisting of metals belonging to the Group IB of the Periodic Table, (4) the zeolite-containing shaped catalyst comprises silica as a binder, (5) the zeolite-containing shaped catalyst has a side-crush strength of at least 2.

Abstract: The invention is to provide a catalyst for long-term, high-yield and stable production of ethylene and propylene in an efficient and simple method of catalytic conversion from a hydrocarbon material. The invention relates to a method for producing ethylene and propylene by contacting a hydrocarbon material that contains an olefin having from 4 to 12 carbon atoms in an amount of at least 20% by weight, with a zeolite-containing shaped catalyst satisfying the following requirements (1) to (4), in a reactor for catalytic conversion of that olefin: (1) the zeolite is an intermediate pore-size zeolite having a pore size of from 5 to 6.5 angstroms, (2) the zeolite does not substantially contain a proton, (3) the zeolite contains at least one metal selected from the group consisting of metals belonging to the Group IB of the Periodic Table, (4) the zeolite has a silica/alumina molar ratio (SiO2/Al2O3 molar ratio) of from 800 to 2,000.

Abstract: A process for increasing ethylene yield in a cracked hydrocarbon is provided. A hydrocarbon feed stream comprising at least 90% by weight of one or more C4-C10 hydrocarbons can be heated to provide an effluent stream comprising at least 10% by weight propylene. The effluent stream can be selectively separated to provide a first stream comprising heavy naphtha, light cycle oil, slurry oil, or any combination thereof and a second stream comprising one or more C4-C10 hydrocarbons. The second stream can be treated to remove oxygenates, acid gases, water, or any combination thereof to provide a third stream comprising the one or more C4-C10 hydrocarbons. The third stream can be selectively separated to provide a product stream comprising at least 30% by weight propylene. At least a portion of the product stream can be recycled to the hydrocarbon feed stream to increase ethylene yield in the effluent stream.

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 efficiently and stably producing ethylene and propylene which comprises bringing a hydrocarbon feedstock comprising at least one C4-12 olefin into contact with a zeolite-containing catalyst to obtain a reaction mixture containing ethylene and propylene, separating the reaction mixture into a fraction comprising ingredients ranging from hydrogen to C3 hydrocarbons and a fraction comprising C4 and higher hydrocarbons, and recycling the C4 and higher hydrocarbons as they are to a reactor.

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: A process for the conversion of a hydrocarbon feedstock to produce olefins, aromatic compounds and ultra low sulfur diesel wherein the hydrocarbon feedstock is reacted in a fluid catalytic cracking (FCC) zone to produce olefins and light cycle oil. The effluent from the FCC is preferably separated to produce a stream comprising ethylene and propylene, a stream comprising higher boiling olefins and light cycle oil (LCO). The stream containing the higher boiling olefins is cracked to provide additional ethylene and propylene. The LCO is selectively hydrocracked to produce aromatic compounds and ultra low sulfur diesel.

Abstract: The present invention is directed to the upgrading of heavy petroleum oils of high viscosity and low API gravity that are typically not suitable for pipelining without the use of diluents. It utilizes a short residence-time pyrolytic reactor operating under conditions that result in a rapid pyrolytic distillation with coke formation. Both physical and chemical changes taking place lead to an overall molecular weight reduction in the liquid product and rejection of certain components with the byproduct coke. The liquid product is upgraded primarily because of its substantially reduced viscosity, increased API gravity, and the content of middle and light distillate fractions. While maximizing the overall liquid yield, the improvements in viscosity and API gravity can render the liquid product suitable for pipelining without the use of diluents.

Abstract: The present invention is directed to the upgrading of heavy petroleum oils of high viscosity and low API gravity that are typically not suitable for pipelining without the use of diluents. It utilizes a short residence-time pyrolytic reactor operating under conditions that result in a rapid pyrolytic distillation with coke formation. Both physical and chemical changes taking place lead to an overall molecular weight reduction in the liquid product and rejection of certain components with the byproduct coke. The liquid product is upgraded primarily because of its substantially reduced viscosity, increased API gravity, and the content of middle and light distillate fractions. While maximizing the overall liquid yield, the improvements in viscosity and API gravity can render the liquid product suitable for pipelining without the use of diluents.

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 dual riser FCC process is disclosed wherein first and second hydrocarbon feeds (5, 6) are supplied to the respective first and second risers (2, 4) to make an effluent rich in ethylene, propylene and/or aromatics. Where the hydrocarbon feeds are different, the respective risers can have different conditions to favor conversion to ethylene and/or propylene. A minor amount of a coke precursor (80, 82) can be added to one or both of the hydrocarbon feeds (5, 6) to reduce or eliminate the amount of supplemental fuel needed to heat balance the system. The different feeds, including the coke precursor and any recycle streams (36, 44) can be segregated by type to improve olefin yields, including an embodiment where the paraffinic feeds are supplied to one riser and the olefinic feeds to the other.

Abstract: The method allows to remove mercaptans contained in a gaseous feed comprising hydrocarbons by carrying out the following stages: a) contacting, in a reactor R1, gaseous feed 1 with a liquid stream 13 comprising olefins, in the presence of a first acid catalyst so that the mercaptans react with the olefins so as to form sulfides, b) discharging an effluent 3 from reactor R1 and separating the effluent into a gas phase and a liquid phase so as to obtain a mercaptan-depleted treated gas 4 and a sulfide-laden liquid, c) separating the sulfide-laden liquid into a first fraction 6 and a second fraction 5, the volume flow rate of first fraction 6 being at least three times higher than the volume flow rate of second fraction 5, d) recycling first fraction 6 to stage a) as a first portion of said liquid stream to be fed into said reactor R1, e) regenerating second fraction 5 by cracking so as to obtain a sulfide-depleted second fraction 2 that is recycled to stage a) as a second portion of said liquid stream.

Abstract: A distillate fuel steam reformer system in which a fuel feed stream is first separated into two process streams: an aliphatics-rich, sulfur-depleted gas stream, and an aromatics- and sulfur-rich liquid residue stream. The aliphatics-rich gas stream is desulfurized, mixed with steam, and converted in a reforming reactor to a hydrogen-rich product stream. The aromatics-rich residue stream is mixed with air and combusted to provide heat necessary for endothermic process operations. Reducing the amounts of sulfur and aromatic hydrocarbons directed to desulfurzation and reforming operations minimizes the size and weight of the overall apparatus. The process of the invention is well suited to the use of microchannel apparatuses for heat exchangers, reactors, and other system components, which may be assembled in slab configuration, further reducing system size and weight.

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: 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: The present invention provides a catalytic cracking reactor system and process in which a riser reactor is configured to have two sections of different radii in order to produced improved selectivity to propene and butenes as products.

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: 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 naphtha and cycle oils produced in catalytic cracking reactions into light olefins. More particularly, the invention relates to a process for hydroprocessing a catalytically cracked light cycle oil, and then re-cracking it along with naphtha 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 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 present invention is a fluidized catalytic cracking process that incorporates a zoned riser reactor. The process provides an in-situ method for feed upgrading in a riser reactor. The process assists in the removal of undesirable contaminants, such as nitrogen, from FCC feedstocks.

Abstract: The present invention is a fluidized catalytic cracking process that incorporates a zoned riser reactor. The process provides an in-situ method for feed upgrading in a riser reactor. The process assists in the removal of undesirable contaminants, such as nitrogen, from FCC feedstocks.