1913results 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.

Integrated processes and facilities for providing recycled content hydrocarbon products (r-products) from mixed waste plastic are provided. Carbon dioxide capture and energy recovery from one or more process streams described herein increase energy efficiency and help reduce overall environmental impact while producing valuable final products from chemically recycled waste plastic.

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 present application relates to a phosphorus-aluminum sol, a preparation method therefor, and a use thereof as a binder in a hydrocarbon oil conversion catalyst. The present application also relates to a hydrocarbon oil conversion catalyst, a preparation method therefor, and a hydrocarbon oil catalytic conversion method using the catalyst. The phosphorus-aluminum sol provided by the present application has an appropriate colloidal particle size, a high degree of polymerization, high stability, and good adhesion, when used in a catalyst containing a molecular sieve, such as an FCC catalyst, the phosphorus-aluminum sol can reduce the blockage of molecular sieve pores, and when synergizing with other matrix materials in the catalyst, the phosphorus-aluminum sol can improve hydrothermal stability, catalytic performance and mechanical strength of the catalyst.

The invention discloses a high-temperature radiation furnace tube for enhancing heat transfer as well as a preparation method and application of the high-temperature radiation furnace tube. The heat-transfer-enhanced high-temperature radiation furnace tube comprises a high-temperature radiation furnace tube, namely a thick tube, of which the inner surface is subjected to roughness treatment and / or a high-temperature radiation furnace tube, namely a streaming terminal, of which the inner surface is sequentially subjected to roughness treatment and streaming structure surfacing treatment, and the roughness parameter Ra of the inner surface of the thick tube is 3.2-40.5 m; and the streaming structure is in one or more forms of a sphere, a raindrop shape and a strip shape. According to the invention, the heat conduction effect and the temperature and airflow uniformity of the furnace tube can be obviously improved through combination of slight increase of the inner surface area and a micron-scale inner surface streaming structure within a certain range, meanwhile, the filling volume of a catalyst in the furnace tube is not influenced, and obvious pressure drop at the outlet end of the furnace tube is avoided.

The present invention provides a method for preparing a multi-level porous composite molecular sieve, comprising the following steps: S1) mixing a binder, a carrier, a mesoporous directing agent and water, and spraying to obtain microspheres; S2) mixing the microspheres with a silicon source, an aluminum source and a mesoporous directing agent after calcination, and calcining and activating again; S3) mixing the microspheres obtained in step S2) with a template agent and water for synthesizing a ZSM-5 molecular sieve, and calcining the solid product obtained after crystallization to obtain a multi-level porous composite molecular sieve. The present application also provides a multi-level porous composite molecular sieve and its application. The composite molecular sieve provided in the present application can be applied to fields such as heavy oil catalytic cracking, effectively improving the diffusion of catalyst acid sites and substrate molecules and product molecules in the reaction, improving the reaction conversion rate and inhibiting coke formation.

The invention provides a high-stability in-situ crystallization catalyst as well as a preparation method and application thereof, and belongs to the technical field of oil refining catalysts. The preparation method comprises the following steps: firstly preparing kaolin microspheres, then roasting the kaolin microspheres into high soil balls and partial soil balls, and mixing the high soil balls and partial soil balls with a silicon source, sodium hydroxide, a seed crystal and a silicon-aluminum activator for in-situ crystallization, so that not only is the activation degree of silicon dioxide in kaolin promoted, but also the timely insertion of active silicon species into a NaY zeolite skeleton in the crystallization process is accelerated, and the activity of the NaY zeolite is improved. The high-stability in-situ crystallization catalyst is prepared by carrying out ammonium salt and rare earth exchange, roasting and phosphorus or boron modification treatment on the crystallized microspheres, and has the characteristics of strong heavy oil conversion and metal pollution resistance and high total liquid yield when being used for catalyzing heavy oil cracking.

The invention discloses an additive for improving the octane number of propylene and gasoline as well as a preparation method and application thereof, and belongs to the technical field of catalyst preparation and application. The additive for improving the octane number of propylene and gasoline comprises 20-65% of a regular ZSM-5 molecular sieve, 0-25% of other molecular sieves, 3-30% of P2O5, 3-18% of a binder and the balance of clay, wherein the total percentage is 100%. The specific surface area of the regular ZSM-5 molecular sieve is 300-510 m < 2 > / g, the micropore volume is 0.20-0.42 mL / g, the mesopore volume is 0.10-0.27 mL / g, the grain size is 30-300 nm, and the silica-alumina ratio is 20-180. The regular ZSM-5 molecular sieve prepared without the template agent is high in yield, high in crystallinity, excellent in acid property and open in pore structure. The additive for improving the octane number of the propylene and the gasoline contains a regular ZSM-5 molecular sieve and is subjected to phosphorus compound modification, so that the catalytic activity and the shape-selective cracking capability are synchronously improved, the cracking capability of low-octane number alkane components is improved, the propylene yield and the octane number of the gasoline are greatly improved, and the manufacturing cost is effectively reduced.

The invention relates to a method and a system for producing low-carbon olefin and light aromatic hydrocarbon through catalytic cracking. The method comprises the following steps: (1) carrying out contact reaction on raw oil and a catalytic cracking catalyst in a constant linear velocity fluidized bed reactor to obtain an oil agent mixture; (2) separating the oil agent mixture to obtain reaction oil gas and a spent catalyst; and (3) separating the reaction oil gas to obtain a low-carbon olefin component, a gasoline component and an oil slurry component. In a constant-linear-speed fluidized bed reactor, light petroleum hydrocarbons such as diesel oil are contacted with a catalytic cracking catalyst with a high silica-alumina ratio, and self-heat balance is maintained through regeneration flue gas circulation to produce low-carbon olefins, light aromatic hydrocarbons and the like. According to the method disclosed by the invention, heavy oil such as naphtha, wax oil and residual oil can be processed while light hydrocarbon such as diesel oil is processed, the conversion rate of the diesel oil is high, self-heating balance can be realized, the problem of excessive diesel oil production capacity of a refinery plant is solved, and the processing benefit of crude oil is also improved.

This disclosure relates to methods of thermal carbonization, including heating a petroleum feedstock and a carbonization catalyst to form a sulfur-doped carbon product.

A rotary bladed apparatus (100) for processing feedstocks in a process fluid is provided, said apparatus comprises means for adjusting position of a working blade cascade of the rotor (3) relative to stator components (2, 4) in a longitudinal direction of a rotor shaft (1). Adjustment is performed through axial displacement of the rotor (3) or, alternatively, through axial displacement of the reactor housing (22 A, 32A). A method for improving process efficiency and for regulating flow losses during processing of feedstocks in a process fluid, in particular, in off-design conditions in the bladed apparatus (100) is further provided. In embodiments, processing of feedstocks includes thermal- or thermochemical cracking of hydrocarbon-containing feedstock.

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 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.

Methods and systems for mixing dissimilar hydrocarbon feedstock materials to form hydrocarbon feedstock blends for subsequent processing. The dissimilar hydrocarbon feedstock materials can differ by chemical composition, polarity, solubility, and / or physical state and include one or more of biomass-derived materials, non-petroleum-derived oils or fats, polymers, fabrics or textiles, paper or cardboard, rubber, waste products, pyrolysis products of the foregoing, or petroleum-derived materials. Efficient and thorough mixing of the dissimilar hydrocarbon feedstock materials is performed by static inline mixing to form an intermediate blend, which is further mixed by high shear mixing to form the hydrocarbon feedstock blend. The methods and systems may involve other processing equipment e.g., strainers, filters, pumps, furnaces, heat exchangers, reactors, separators, tanks, and / or distillation columns. The hydrocarbon feedstock blend may be further processed by hydrocracking or hydroconversion e.g., by ebullated bed, fixed bed, or slurry bed reactor), solvent deasphalting, coking, fluid catalytic cracking, hydroprocessing, or hydrotreating.

The invention relates to a method and a system for producing chemical materials including ethylene based on a constant linear velocity fluidized bed reactor, and the method comprises the following steps: (1) carrying out contact reaction on raw oil and a shape-selective molecular sieve catalyst in the constant linear velocity fluidized bed reactor to obtain an oil agent mixture; (2) separating the oil agent mixture to obtain reaction oil gas and a spent catalyst; and (3) separating the reaction oil gas in an oil-gas separation system to obtain chemical materials including ethylene, C4 olefin and the like. In a constant-linear-speed fluidized bed reactor, light petroleum hydrocarbons such as diesel oil are contacted with a shape-selective molecular sieve catalyst, and self-heat balance is maintained through regeneration flue gas circulation to produce ethylene, propylene and the like. According to the method disclosed by the invention, heavy oil such as naphtha, wax oil and residual oil can be processed while light hydrocarbon such as diesel oil is processed, the yield of ethylene and propylene is high, self-heating balance can be realized, the problem of excessive diesel oil production capacity of a refinery plant is solved, and the defects of chemical materials are made up.

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

The invention relates to the technical field of catalysis, and discloses a catalytic cracking device and method. The device comprises a multi-stage reaction unit and a cracking reaction unit, the multi-stage reaction unit comprises a variable-diameter riser and a multi-stage reaction settler, and the cracking reaction unit comprises a cracking riser and a cracking settler; the variable-diameter lifting pipe comprises a first reaction zone, a second reaction zone and a third reaction zone which are sequentially connected in series in the length direction, the inner diameter of the second reaction zone is larger than that of the first reaction zone and that of the third reaction zone, and an inner conveying pipe extending into the second reaction zone is arranged at the joint of the third reaction zone and the second reaction zone; the cracking settler comprises a cracking steam stripping section, a turbulence reaction section and a cracking settling section which are sequentially arranged along the length direction of the cracking settler, an outlet of the cracking riser is positioned in the turbulence reaction section, and the cracking steam stripping section is provided with a cracking catalyst outlet communicated with the second reaction area. The device can improve the reaction efficiency of catalytic cracking of heavy oil and light hydrocarbon, and realizes tight coupling of heavy oil and light hydrocarbon.

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.

The invention discloses a composite aperture molecular sieve catalytic cracking catalyst and a preparation method thereof, and belongs to the technical field of catalytic cracking, the composite aperture molecular sieve catalytic cracking catalyst comprises 20-30% of a macroporous material, 40-60% of a mesoporous-microporous molecular sieve and 20-30% of a binder; the macroporous material is a macroporous alumina / kaolin compound, and the macroporous alumina / kaolin compound takes macroporous alumina as a core and macroporous kaolin as a shell; the mesoporous-microporous molecular sieve is a ZMQ-1 molecular sieve. According to the mode, the macroporous material is prepared from the macroporous aluminum oxide / kaolin compound, the ZMQ-1 molecular sieve and the binder, and the macroporous material takes macroporous aluminum oxide as a core and macroporous kaolin as a shell in the macroporous aluminum oxide / kaolin compound. The catalyst for catalytic cracking of heavy oil has the advantages of high yields of dry gas, liquefied gas, gasoline and diesel oil, low yields of coke and heavy oil and the like. The secondary cracking reaction of gasoline or diesel oil can be effectively prevented, so that the yield of gasoline and diesel oil is improved.

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.

A continuous process for transporting one or more waste plastic feedstocks to a refinery processing unit, includes receiving, in a blending unit, one or more waste plastic feedstocks, one or more waste plastic-immiscible bio feedstocks and a recycled inert carrier fluid received from a refinery processing unit, generating, in the blending unit, a homogeneous solution comprising the one or more waste plastic feedstocks, the one or more waste plastic-immiscible bio feedstocks and the recycled inert carrier fluid, and processing the homogeneous solution in the presence of a catalyst under catalytic cracking conditions in the refinery processing unit.

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.

A process includes flowing a catalyst composition comprising catalyst particles into a radial flow moving bed reactor, wherein the catalyst particles move by gravity through the radial flow moving bed reactor to an exit point of the radial flow moving bed reactor, wherein the catalyst particles form a moving catalyst bed in the radial flow moving bed reactor, flowing a light hydrocarbon feed stream comprising C1 to C3 alkanes into the radial flow moving bed reactor in a manner so that the light hydrocarbon feed stream flows radially inward or radially outward through the moving catalyst bed and thereby contacts the catalyst particles under reaction conditions to produce a product effluent stream comprising a C2 to C10 hydrocarbon product and hydrogen, and flowing the product effluent stream from the radial flow moving bed reactor.

Disclosed is a process for preparing a high silica Y-zeolite by utilizing a waste silica source. The method comprises the following steps: preparing a dilute nucleating agent, and preparing a thick nucleating agent by mixing sodium silicate, sodium aluminate, deionized water and sodium hydroxide. Furthermore, an aluminosilicate gel is prepared by mixing the dilute nucleating agent with sodium silicate, aluminum sulfate, deionized water and the thick nucleating agent, and then the aluminosilicate gel is crystallized, filtered and washed to obtain a Y-zeolite filter cake. The Y-zeolite is ammonium exchanged, dried and calcined to obtain a high silica Y-zeolite.

The invention discloses a device and a method for direct catalytic cracking of electric heating crude oil. A plurality of nozzles are arranged in the circumferential direction of the side wall of the fluidized bed and are close to the bottom of the fluidized bed; a slag discharge port and a first gas inlet are formed in the bottom of the fluidized bed; a plurality of output ends of the raw material and catalyst mixer are respectively connected to the plurality of corresponding nozzles; the second heating assembly extends into the fluidized bed; the annular heating area is located above the nozzle, and the first air inlet corresponds to the annular heating area; one end of the reaction tube is connected to the top of the fluidized bed, and the other end is connected to the input end of the cyclone separator; the first heating assembly is arranged on the outer wall of the vertical part of the reaction tube; the first output end of the cyclone separator is connected to the fine coke particle storage area, and the second output end of the cyclone separator is connected to the input end of the cooling separator. An electric heating heat supply mode is adopted, a cheap catalyst does not need to be burnt and regenerated, a regenerator-free device is adopted, carbon emission is low, the structure is simple, and operation is convenient.