1423results about "Catalytic cracking" patented technology

A process for upgrading plastic derived oil includes contacting the plastic derived oil with a mixed catalyst in a first reactor, where the mixed catalyst includes a decontamination catalyst and a cracking catalyst different from the decontamination catalyst. The first reactor reduces concentrations of halogen-containing compounds in the plastic derived oil. The process includes passing the first reactor effluent to a second reactor and contacting the first reactor effluent with the cracking catalyst to produce a second effluent comprising light olefins and naphtha range hydrocarbons. The process includes separating used mixed catalyst from the first reactor to produce a used decontamination catalyst and a second used cracking catalyst, and regenerating the decontamination catalyst and cracking catalyst in separate regenerators to reduce exposure of the cracking catalyst to halogen-containing compounds produced during regeneration of the used decontamination catalyst.

A process for upgrading a plastic derived oil includes providing the plastic derived oil comprising hydrocarbons and greater than or equal to 100 ppmw halogen-containing compounds and contacting the plastic derived oil with an MMO catalyst in a first reactor at reaction conditions to remove halogens from the plastic derived oil to produce a first reactor effluent with less than 100 ppmw halogen-containing compounds. The process includes contacting the first reactor effluent with an adsorbent to produce a treated first reactor effluent, passing the treated first reactor effluent to a second reactor, and contacting the treated first reactor effluent with a cracking catalyst in the second reactor. Contacting with the cracking catalyst may cause hydrocarbons in the treated first reactor effluent to undergo catalytic cracking to produce a second reactor effluent comprising light olefins, naphtha range hydrocarbons, or combinations thereof.

A process for upgrading plastic derived oil includes contacting a plastic derived oil stream with a decontamination catalyst in a first reactor, separating a first reactor effluent from a used decontamination catalyst, passing the first reactor effluent to a second reactor downstream of the first reactor, contacting the first reactor effluent with a cracking catalyst in the second reactor, and separating a second reactor effluent from a used cracking catalyst. The cracking catalyst is different from the decontamination catalyst. The process further includes regenerating the used decontamination catalyst in a decontamination catalyst regenerator to produce regenerated decontamination catalyst, and regenerating the used cracking catalyst in a cracking catalyst regenerator separate from the decontamination catalyst regenerator to produce regenerated cracking catalyst. Regenerating the used cracking catalyst separately reduces deactivation of the cracking catalyst by halogen-containing compounds produced during regeneration of the decontamination catalyst.

A geothermally powered petrochemical refining system includes a geothermal system with a wellbore extending from a surface into an underground magma reservoir. A geothermally powered fractional distillation system receives crude oil and produces distillates which are separated by molecular weight. The distillates may be provided to a geothermally powered cracking system that is heated by a heat transfer fluid heated by the geothermal system to crack heavy hydrocarbons into lighter ones. The distillates may be provided to a geothermally powered reforming system that is heated by a heat transfer fluid heated by the geothermal system to reform hydrocarbons into different structures.

The disclosure relates to the purification and treatment of oil produced from the liquefaction of waste polymer like for instance the pyrolysis of waste plastics via the polymerization of dienes prior to further treatments.

The invention relates to the field of catalytic cracking, in particular to a modified catalytic cracking catalyst and a preparation method and application thereof. The modified catalytic cracking catalyst is of a core-shell structure and comprises an inner core and an outer shell, the inner core contains catalytic cracking catalyst finished product particles and alkaline earth metal elements, and the outer shell contains the alkaline earth metal elements and rare earth metal elements. Compared with other catalysts of the same type, the modified catalytic cracking catalyst has more excellent nickel resistance on the basis of not influencing the catalytic cracking performance, and also has lower dehydrogenation activity.

The invention relates to the field of reforming catalyst preparation, and discloses a supported reforming catalyst, preparation and application thereof, and a catalytic reforming method. The invention relates to a supported reforming catalyst. The catalyst comprises an alumina carrier containing rare earth metal and IVA group metal, and an active component supported on the alumina carrier, the active component comprises a platinum group metal; wherein in the alumina carrier, pores with the pore diameter of 6-10 nm account for 10-22% of the total pore volume, pores with the pore diameter of 10-20 nm account for 50-75% of the total pore volume, and pores with the pore diameter of 20-50 nm account for 10-25% of the total pore volume. The supported reforming catalyst provided by the invention has excellent catalytic performance, is applied to the field of hydrocarbon catalytic reforming, and has relatively high reaction activity and product selectivity.

Systems and processes for cracking hydrocarbons to produce light olefins include an FCC reactor utilizing counter-current flow that includes a reaction zone comprising an elongated reaction tube that has a feed inlet, a product outlet, and a catalyst inlet. In embodiments, the FCC reactor further includes a freeboard zone. The freeboard zone is configured to reduce a superficial velocity of the cracked hydrocarbon fluids in the reaction zone, causing catalyst entrained in the cracked hydrocarbon fluids to at least partially separate from the cracked hydrocarbon fluids. In embodiments, the FCC reactor includes a dense fluidized bed unit. The dense fluidized bed unit is configured to inject a fluidizing gas such that bubbles are formed within the solid particles of the dense fluidized bed of solid particles, which causes the catalyst to overflow from the dense fluidized bed of solid particles into the reaction zone.

Integrated processes for upgrading a hydrocarbon condensate stream to enhanced value streams including splitting a desalted feed stream into a light cut, a middle cut, and a heavy cut. The light cut is provided to a steam cracker unit to generate a steam cracked gas stream, a C4+ hydrocarbon stream, and a C9+ hydrocarbon stream, the middle cut is provided to a first catalytic cracker unit to generate a first cracked product stream, and the heavy cut is provided to a second catalytic cracker unit to generate a second cracked product stream. The steam cracked gas stream is provided to an olefins separation unit to generate at least one light olefin stream. Other effluents from the olefins separation unit and the steam cracker unit are provided to a hydrogenation unit, an aromatic extraction unit, or recycled within the system.

Hybrid catalysts for simultaneous dehalogenation and cracking of plastic derived oil include composite particles, where each of the composite particles includes red mud particles and Mordenite zeolite particles. A process includes contacting a plastic derived oil stream with the hybrid catalyst in an FCC reactor to produce an FCC effluent and a used hybrid catalyst. The plastic derived oil stream comprises halogen-containing compounds, and contacting the plastic derived oil stream with the hybrid catalyst causes halogen-containing compounds to react to form hydrocarbons and hydrogen halides, where the hydrogen halides are adsorbed onto surfaces of the red mud particles. The FCC effluent has a concentration of the halogen-containing compounds less than the plastic derived oil stream. Contacting the plastic derived oil stream with the hybrid catalyst causes hydrocarbons in the plastic derived oil stream to undergo cracking reactions over the Mordenite zeolite particles to produce the FCC effluent.

Processes for decontaminating a plastic derived oil include contacting a plastic derived oil stream containing halogen-containing compounds with a decontamination catalyst at a reaction temperature of 350-450° C. to produce a decontaminated plastic derived oil and a used decontamination catalyst. The decontamination catalyst includes from 5-40 wt. % red mud particles, from 20-60 wt. % matrix material, and from 10-30 wt. % binder, per unit weight of the decontamination catalyst. Contacting the plastic derived oil stream with the decontamination catalyst at the reaction conditions causes halogen-containing compounds to react to form hydrocarbons and hydrogen halides, which further react with the red mud particles to produce metal halides on surfaces of the red mud particles. The decontaminated plastic derived oil has a concentration of the halogen-containing compounds less than a concentration of the halogen-containing compounds in the plastic derived oil stream.

Some examples herein provide a method of processing a feedstock. The feedstock may be flowed into a reactor. A catalyst may be flowed into the reactor. Within the reactor, the feedstock may be converted over the catalyst, at an average reaction temperature, to a product stream. The product stream may be withdrawn from the reactor. A stream of the catalyst may be withdrawn from the reactor. Said stream of the catalyst may be heated to a temperature above the average reaction temperature without exposing the catalyst to any air or other oxidants. The heated stream of catalyst may be returned to the reactor at a temperature higher than the reaction temperature, to obtain the average reaction temperature within the reactor.

A hybrid catalyst for simultaneous dehalogenation and cracking of plastic derived oil includes a plurality of composite particles, wherein each of the composite particles includes red mud particles and beta zeolite particles. A process for upgrading plastic derived oil includes contacting the plastic derived oil with the hybrid catalyst. A system for upgrading plastic derived oil includes an FCC reactor containing the hybrid catalyst.

The present invention belongs to the technical field of catalytic materials and relates to a silicon-aluminum material, its preparation and a low-coking, high-activity heavy oil conversion catalytic cracking catalyst. The silicon-aluminum material has an anhydrous weight chemical formula of (0-1)Na2O·(15-50)Al2O3·(85-50)SiO2, a most probable pore diameter of 10-100 nm, and a specific surface area of ​​150-600 m 2 / g, a pore volume of 0.5-1.5 ml / g, and a pore volume of pores with a pore diameter greater than 10 nm accounting for 70%-98% of the total pore volume. Its preparation method comprises the steps of adding an alkaline silicon source to an acidic aluminum source, contacting with a base, and washing. The low-coking, high-activity heavy oil conversion catalytic cracking catalyst contains the aforementioned silicon-aluminum material and an in-situ crystallized Y-type molecular sieve. The catalytic cracking catalyst has good coke selectivity.

A process for regenerating catalyst from a fluidized catalytic process is disclosed. The process comprises passing a CO2 oxidation stream to a regenerator in which coke is combusted from catalyst to provide a CO2 rich flue gas stream. The CO2 rich flue gas stream is separated into an underflow stream comprising catalyst fines and a CO2 rich flue gas overflow stream. The overflow stream is separated into a recycle stream and a power recovery stream. The recycle stream of the overflow stream is recycled to the regenerator.

The invention discloses a spiral-flow type riser reactor with an annular space structure. The reactor sequentially comprises a feeding section, a reaction section and a reaction stopping section from bottom to top, and the three sections respectively adopt a concentric cylindrical barrel, a concentric conical barrel and a hollow straight barrel. Raw material and catalyst feeding pipes are both positioned at the feeding section and are tangent to the outer cylinder body according to the same rotating direction, and rotational flow is generated in an annular gap between the inner cylinder and the outer cylinder. The catalytic cracking device is mainly used for preparing low-carbon olefin by taking heavy oil, wax oil, low-carbon alkane gas and the like as raw materials. According to the spiral-flow type riser reactor disclosed by the invention, raw materials and a catalyst can be uniformly mixed, and backmixing is basically eliminated; and a relatively large catalyst-oil ratio and strict reaction time can be adopted, so that the process conditions required for producing low-carbon olefins by catalytic cracking can be met, and compared with the conventional hollow cyclone reactor, the hollow cyclone reactor has obvious advantages.

A process for upgrading a hydrocarbon feed comprises contacting the hydrocarbon feed with steam in the presence of a cracking catalyst composition at reaction conditions sufficient to cause at least a portion of hydrocarbons in the hydrocarbon feed to undergo one or more cracking reactions to produce a steam catalytic cracking effluent comprising light olefins, light aromatic compounds, or both, where the cracking catalyst composition comprises a cracking additive comprising metal species impregnated on a ZSM-5 zeolite, where the metal species comprises a metal selected from the group consisting of chromium, vanadium, iron, platinum, molybdenum, cerium, and nickel.

Catalysts that include a first zeolite selected from ZSM-5 and Y zeolite impregnated with P2O5 and a second zeolite different from the first zeolite selected from ZSM-5 and Y zeolite impregnated with La2O3. The catalysts can also include alumina, clay, and silica. The catalysts can be used to crack vacuum gas oil (VGO) into gasoline and butylenes. The catalysts can crack VGO with relatively good selectivity for butylenes over butanes.

Disclosed herein are hydrocarbon based compositions derived from pyrolysis of a feedstock comprising post-consumer and / or post-industrial plastics and methods of making and use thereof.

A nano-sized mesoporous zeolite beta composition and processes for the synthesis and use of the nano-sized mesoporous zeolite beta. The nano-sized mesoporous zeolite beta is synthesized using a hydrothermal treatment without drying and calcination of the zeolite prior to or after hydrothermal treatment. A process for hydrocracking a hydrocarbon feedstock using the nano-sized mesoporous zeolite beta is also provided.

A process for upgrading plastic derived oil includes contacting the plastic derived oil with a mixed catalyst in a first reactor, where the mixed catalyst includes a decontamination catalyst and a cracking catalyst different from the decontamination catalyst. The first reactor reduces concentrations of halogen-containing compounds in the plastic derived oil. The process includes passing the first reactor effluent to a second reactor and contacting the first reactor effluent with the cracking catalyst to produce a second effluent comprising light olefins and naphtha range hydrocarbons. The process includes separating used mixed catalyst from the first reactor to produce a used decontamination catalyst and a second used cracking catalyst, and regenerating the decontamination catalyst and cracking catalyst in separate regenerators to reduce exposure of the cracking catalyst to halogen-containing compounds produced during regeneration of the used decontamination catalyst.

Processes and facilities for producing a recycled content organic chemical compound directly or indirectly from waste plastic. Processing schemes are described herein for converting waste plastic (or hydrocarbon having recycled content derived from waste plastic) into useful intermediate chemicals and final products. The waste plastic can be liquified before being introduced to downstream processing. In some aspects, recycled content aromatics (r-aromatics) can be processed to provide recycled content paraxylene (r-paraxylene), which can then be used to provide recycled content terephthalic acid (r-TPA) and / or recycled content polyethylene terephthalate (r-PET).

A method for processing a plastic-derived oil may comprise contacting the plastic-derived oil with a catalyst to crack the plastic-derived oil to form a hydrocarbon product. The catalyst may comprise a metal oxide-loaded ZSM-5 zeolite comprising: ZSM-5 particles having a size of less than 100 nm, and one or more metal oxides chosen from iron oxide, lanthanum oxide, and cerium oxide. The one or more metal oxides may be disposed on the ZSM-5 particles.

A process includes contacting one or more bio feedstocks and one or more waste plastic feedstocks with a deactivated cracking catalyst comprising a phosphorus-containing ZSM-5 catalyst at catalytic cracking conditions to obtain a product stream containing hydrocarbons, and separating at least one hydrocarbon fraction from the product stream, wherein the deactivated cracking catalyst contains at least one metal contaminant.

A hybrid catalyst for simultaneous dehalogenation and cracking of plastic derived oil includes a plurality of composite particles, where each of the composite particles includes red mud particles and USY zeolite particles. A process for upgrading plastic derived oil includes contacting the plastic derived oil with the hybrid catalyst in an FCC reactor to produce an FCC effluent and a used hybrid catalyst. The plastic derived oil comprises halogen-containing compounds, and the contacting at reaction conditions causes halogen-containing compounds to react to form hydrocarbons and hydrogen halides, which are adsorbed onto surfaces of the red mud particles. The contacting at reaction conditions also causes hydrocarbons in the plastic derived oil to undergo cracking reactions to produce the FCC effluent. The FCC effluent may have a reduced concentration of the halogen-containing compounds. A system that includes the hybrid catalyst is also disclosed.

Provided is a fluid catalytic cracking catalyst including faujasite-type zeolite, boehmite, a binder, and clay minerals, and satisfying the following formulas (1) and (2) in powder X-ray diffraction analysis:A / B≤1.2(1)A / C≥0.8(2)in the formulas (1) and (2), A is an integrated intensity of a diffraction peak attributed to (020) plane of the boehmite, B is an integrated intensity of a diffraction peak attributed to (120) plane of the boehmite, and C is an integrated intensity of a diffraction peak attributed to (331) plane of the faujasite-type zeolite.

To provide a process for producing renewable linear alkylbenzenes from vegetable, animal, nut and / or seed oils, which are biorenewable resources.SOLUTION: The process includes: a linear selective cracking process to crack C14+ chains into C9 to C14 chains which are useful for producing linear alkylbenzene for use in detergents; and a hydroisomerization step to produce paraffins with monomethyl branching which can be reacted with benzene to form monomethyl alkyl benzenes.SELECTED DRAWING: None

A catalyst for fluid catalytic cracking is provided which contains faujasite-type zeolite, boehmite, a binder and clay minerals and which satisfies the following formulas (1) and (2) in powder X-ray diffraction analysis: A / B ≤ 1 .2 A / C ≤ 0.8 where in formulas (1) and (2), A is the integrated intensity of a diffraction peak assigned to the (020) plane of boehmite, B is the integrated intensity of a diffraction peak assigned to the (120) plane of boehmite, and C is the integrated intensity of a diffraction peak assigned to the (33 1) plane of the faujasite-type zeolite.

A method of inputting thermal energy into a fluid medium in a high temperature material production process by at least one rotating device is provided, the rotating device comprising a casing with at least one inlet and at least one outlet, a rotor including at least one rotor blade row arranged around a rotor hub mounted on a rotor shaft, and a stator formed as a fixed vane assembly arranged at least upstream of the at least one rotor blade row, wherein an amount of thermal energy is imparted to a fluid medium flow guided along a flow path formed inside the casing between the inlet and the outlet by a series of energy transformations occurring as the fluid medium flow passes through the fixed vanes and the at least one rotor blade row, respectively. The method further comprises incorporating the at least one rotating device into a high temperature material production facility configured to perform high temperature material production, such as production of glass, glass wool, carbon fiber, carbon nanotubes, and clay-based materials, at a temperature essentially equal to or greater than about 500°C, and directing an amount of input energy into the at least one rotating device incorporated into a heat consuming process facility, the input energy comprising electrical energy. A rotating device and related uses are further provided.

A riser reactor separation system for separating catalyst particles from hydrocarbon vapors may include a separation chamber, a hydrocarbon vapor collecting chamber, a hydrocarbon vapor outlet, and a dipleg extending downwardly towards a catalyst receiving volume. In some implementations the system may include a baffle spaced apart from and extending along a dipleg outer wall, at least partially separating the dipleg into an outer channel and an inner channel. In some implementations the separation chamber may have side walls that extend substantially parallel relative to one another. Riser reactor separation systems and related methods described herein may provide for greater separation efficiency of catalyst particles from hydrocarbon vapors.