1111results 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 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.

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.

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.

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 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 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.

The invention refers to the method for producing gasolines or aromatic compound concentrates, where three streams are used as feedstock, one of which includes hydrocarbon fraction, the second stream includes oxygenate, the third stream includes olefin-containing fraction with one or more olefins selected from the group consisting of ethylene, propylene, normal butylenes, isobutylene, in total from 10 to 50 wt %, and where three reaction zones filled with zeolite catalyst are used, with distribution of hydrocarbon fraction and oxygenate to the first reaction zone, and with olefin-containing fraction distributed over the three reaction zones, with the third stream mass fraction distributed to the final reaction zone higher than the mass fraction of the third stream distributed to each of the previous reaction zones. This method allows to increase the yield of C5+ hydrocarbons, enhance n-hexane and n-heptane conversion, reduce benzene content in the product, avoid recycling of gaseous products and decrease consumption of oxygenates. 1 independent claim and 35 dependent claims in the formula, 12 examples, 7 tables.

The utility model discloses a closed sampler for catalyst sampling, which belongs to the technical field of catalyst sampling and comprises a first pipe group, a sampling tank and a second pipe group. The first pipe set comprises a first pipeline, a second pipeline, a third pipeline and a fourth pipeline. The first pipeline is connected with the catalyst pipeline and is provided with a first valve and a second valve; and the second pipeline, the third pipeline and the fourth pipeline are connected with the first pipeline and are respectively provided with a third valve, a fourth valve and a fifth valve. The sampling tank is connected with a fourth pipeline, is connected with a pressure gauge through a fifth pipeline, is connected with a filter through a sixth pipeline, and is respectively provided with a sixth valve and a seventh valve. And the second pipe group comprises a seventh pipeline and an eighth pipeline. And the seventh pipeline is connected with the sampling tank and is provided with an eighth valve. And the eighth pipeline is connected with the seventh pipeline and is provided with a ninth valve and a one-way valve. According to the utility model, the problem that the catalyst is unsmooth to convey and discharge when the existing closed sampler is used for sampling is solved.

The present technology provides compositions that include at least about 98 weight percent ("wt%") n-paraffins which, among other surprising features, may be suitable for use as a diesel fuel, an aviation fuel, a jet fuel blendstock, a blendstock to reduce the cloud point of a diesel fuel, a fuel for portable heaters, and / or as a charcoal lighter fluid. The composition includes at least about 98 wt% C7-C12 n-paraffins, where at least about 10 wt% of composition includes n-decane, at least about 20 wt% of the composition includes n-dodecane, and at least about 75 wt% of the composition includes even carbon number paraffins. The composition also includes less about 0.1 wt% oxygenates and less than about 0.1 wt % aromatics. The composition may be produced by a process that includes hydrotreating a biorenewable feedstock comprising at least one of palm kernel oil, coconut oil, babassu oil, microbial oil, or algal oil.

Provided is a continuous process for converting waste plastic into recycle for polypropylene polymerization. The process comprises selecting waste plastics containing polyethylene and / or polypropylene and preparing a stable blend of petroleum and the selected plastic. The amount of plastic in the blend comprises no more than 20 wt. % of the blend. The blend is passed to a refinery hydrocracking unit. A liquid petroleum gas C3 olefin / paraffin mixture is recovered from the hydrocracking unit. The C3 paraffins and C3 olefins are separated into different fractions with the C3 olefin fraction passed to a propylene polymerization reactor, and the C3 paraffin fraction passed optionally to a dehydrogenation unit to produce additional propylene. A heavy fraction can also be recovered from the hydrocracking unit and passed to an isomerization dewaxing unit to prepare base oil.

The invention relates to a method for producing atmospheric distillates from oil derived from the solvolysis of used elastomers, comprising the following steps: 1) a step of solvolysis of elastomers under highly specific conditions in order to obtain a first gaseous effluent and a first liquid effluent comprising carbon black; 2) steps of liquid / solid separation and fractionation of the first liquid effluent in order to recover the carbon black and various liquid fractions including a heavy hydrocarbon cut with an initial boiling temperature of between 340°C and 440°C; 3) a step of catalytic cracking of the heavy hydrocarbon cut obtained in a fluidised bed reactor in the presence of a solid catalyst at a temperature of between 500°C and 700°C and a pressure of between 0.1 and 0.6 MPa in order to obtain an atmospheric distillate comprising at least a gasoline cut and a diesel cut.

A catalytic cracking catalyst containing a large particle sol and a method for producing the same. The catalytic cracking catalyst contains, based on its total weight, 15-50 wt% of β zeolite, 10-75 wt% of clay, and 10-50 wt% of a large particle sol. The pore distribution is measured by a low-temperature nitrogen adsorption method, and the total pore volume is 0.200 mL / g or more. The pore volume of mesopores having a parameter of 4-50 nm accounts for 60% or more of the total pore volume. The large particle sol contains 10-40 wt% Al 2 O 3 , 50 to 85% by weight P 2 O 5 , and 0.2 to 10 wt.% SiO 2 Including P 2 O 5 :Al 2 O 3 The mass ratio of SiO is (1.5~5.0):1. 2 :Al 2 O 3 The mass ratio of is (0.01-0.3):1, and the average particle size distribution of the sol is concentrated at 20-50 nm. The preparation method includes the following steps: mix an aluminum source with deionized water to obtain a first slurry, mix the first slurry with a phosphorus source to obtain a second slurry, add silica sol to the second slurry to obtain a third slurry, and age the third slurry to obtain a large particle size sol. The large particle size sol is uniformly mixed with clay and β zeolite to obtain a fourth slurry, and the fourth slurry is dried and calcined. This catalyst is applied in the catalytic cracking process, which can significantly improve the yield and selectivity of C4 olefins.

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.

A catalyst composition and method for treating a feed including oxygen is provided. The catalyst composition includes a zeolite and a coprocessing material including an oxide of at least one of magnesium (Mg), vanadium (V), and cerium (Ce).

The application discloses a catalytic cracking catalyst with mesopore and macropore structures and a preparation method thereof. The catalytic cracking catalyst contains 15-60 wt% of molecular sieve, 5-40 wt% of first binder of large-grained pseudo-boehmite calculated based on alumina, 0-15 wt% of second binder and 20-80 wt% of clay based on dry weight. The large-grained pseudo-boehmite has a grain size of 6-10 nm. The total pore volume of the catalytic cracking catalyst is 0.4-0.5 mL / g. The preparation method comprises the following steps: preparing the first binder of large-grained pseudo-boehmite by a carbonization method, adding hydrochloric acid to gelatinize the large-grained pseudo-boehmite, adding the clay, the molecular sieve and the second binder, spray-drying and molding, calcining, washing and drying. The large-grained pseudo-boehmite is prepared by the following steps: neutralizing sodium metaaluminate solution with carbon dioxide to form a gel, aging the slurry by gradually increasing the temperature in stages after the gel is formed, filtering the slurry, continuously washing and drying after the aging. The catalytic cracking catalyst has good abrasion performance while retaining the mesopore and macropore structures. When applied to a catalytic cracking process, the catalytic cracking catalyst can significantly improve heavy oil conversion rate, reduce coke formation and optimize product distribution.