668results about "Catalytic cracking" patented technology

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 The product stream may be withdrawn from the reactor. A stream of the catalyst may be withdrawn from the reactor.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.

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.

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.

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.

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.

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 invention relates to a method and device for preparing low-carbon olefins, and the method comprises the following steps: S1, contacting raw oil with a catalytic conversion catalyst in a catalytic conversion reactor for catalytic conversion reaction to obtain a catalytic conversion reaction product; s2, separating the catalytic conversion reaction product to obtain ethylene and propylene as well as a first circulating olefin flow containing butene and / or a second circulating olefin flow containing C5 + olefin; s3, enabling the olefin material to enter an etherification unit, and contacting the olefin material with an alcohol raw material under an etherification condition to obtain a circulating ether material and etherified olefin; and S4, enabling at least one part of etherified olefin to enter an isomerization unit, and carrying out isomerization reaction in the presence of an isomerization catalyst to obtain isomerized olefin. According to the method disclosed by the invention, the conversion of ethers into low-carbon olefins can be realized, the yield and selectivity of ethylene and propylene are improved, the yield of methane is reduced, the content of methanol in the product is reduced to the greatest extent, and the conversion of low-cost methanol into low-carbon olefins is realized.

Provided is a process of manufacturing light olefins, which is a fluidized bed catalytic naphtha cracking process having improved economic feasibility and decreased greenhouse gas emissions. The process of manufacturing light olefins according to the present invention has a decreased hot spot occurring when supplying an additional fuel oil and decreased tendency of catalyst deactivation by water, thereby improving economic feasibility of the process and reducing greenhouse gas emissions to allow construction of an environmentally friendly process.

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.

A fluidized bed device for coupling naphtha and methanol to prepare aromatics and co-produce olefins and its application method are provided. By using the device, under the action of a catalyst, naphtha reacts with methanol to generate product gas containing aromatics and light olefins as main components. The method can efficiently and selectively convert linear and branched aliphatic hydrocarbons into aromatics, while also increasing p-xylene production through aromatic methylation reactions, with the p-xylene content in the xylene mixture exceeding 75 wt %. The fluidized bed reactor achieves increased p-xylene production by controlling the progression of cascade reactions (naphtha→benzene / toluene→p-xylene). Additionally, it utilizes the methylation reaction of benzene / toluene with methanol to provide in-situ heat for the coupled naphtha-methanol aromatization process, thereby achieving autothermal balance.

This invention relates to the field of catalytic cracking catalyst technology, and discloses a ZMQ-1 molecular sieve catalytic cracking catalyst with low carbon deposition and long lifespan. The catalyst is composed of the following components: ZMQ-1 molecular sieve, metal ion modifier, composite mesoporous molecular sieve material, and carbon deposition inhibitor. The ZMQ-1 molecular sieve is synthesized via a hydrothermal method and possesses excellent pore structure. The metal ion modifier is loaded onto the surface of the ZMQ-1 molecular sieve via impregnation to enhance catalytic activity. The composite mesoporous molecular sieve material is composited with the ZMQ-1 molecular sieve via a sol-gel method to improve the pore structure and enhance catalyst stability. The carbon deposition inhibitor effectively reduces carbon deposition. The catalyst of this invention exhibits excellent catalytic performance during catalytic cracking, significantly improving cracking conversion, reducing carbon deposition, and extending catalyst lifespan. It can be widely applied in catalytic cracking reactions in the petrochemical and energy sectors.

An olefinic material production system may include a metal component comprising an outer surface, an anti-coking coating positioned over the metal component, and a refractory material layer positioned over the anti-coking coating, such that the anti-coking coating is positioned between the metal component and the refractory material layer. Also disclosed are methods for operating such an olefinic material production system.

The invention provides an iron-pollution-resistant catalytic cracking catalyst and a preparation method thereof, and the iron-pollution-resistant catalytic cracking catalyst comprises the following raw materials: a mesoporous and macroporous material, a zinc-aluminum composite material and a molecular sieve, wherein the mesopore and macropore material comprises kaolin and first zinc salt loaded in pores of the kaolin; the zinc-aluminum composite material is obtained by performing solid-phase ball milling on pseudo-boehmite and second zinc salt. The catalytic cracking catalyst provided by the invention has abundant mesopore and macropore structures and excellent iron resistance.

An addition system for introducing particulate material into an industrial process is disclosed. The addition system comprises a vessel for holding the particulate material, wherein the vessel has a top and a bottom; one or more weighing devices; a controller for controlling operation of the addition system; a base plate to support the vessel and optionally the controller; and three or more legs, each leg having an uppermost section that connects to the vessel and a foot that is connected to the base plate. The widest diameter of the vessel is less than the diameter of a circle drawn through the feet of the legs. The one or more weighing device are mounted on the base plate and support the legs of the vessel.

A fluidized catalytic cracking unit system includes: a fluidized catalytic cracking unit assembly including a first catalyst regenerator and a cracking unit, the cracking unit configured to output spent catalyst to the first catalyst regenerator; and a reformer-electrolyzer-purifier assembly comprising a reformer-electrolyzer-purifier cell, the reformer-electrolyzer-purifier cell comprising an anode section and a cathode section.

A process for upgrading a naphtha feed includes separating the naphtha feed into at least a light naphtha fraction, contacting the light naphtha fraction with hydrogen in the presence of at least one cyclization catalyst, and contacting the cyclization effluent with at least one cracking catalyst. Contacting the light naphtha fraction with hydrogen in the presence of at least one cyclization catalyst may produce a cyclization effluent comprising a greater concentration of naphthenes compared to the light naphtha fraction. Contacting the cyclization effluent with at least one cracking catalyst under conditions sufficient crack at least a portion of the cyclization effluent may produce a fluid catalytic cracking effluent comprising light olefins, gasoline blending components, or both. A system for upgrading a naphtha feed includes a naphtha separation unit, a cyclization unit disposed downstream of the naphtha separation unit, and a fluid catalytic cracking unit disposed downstream of the cyclization unit.

The invention relates to a computer-implemented method for generating and / or providing a target catalyst composition to be used in a production plant, the method comprising the steps of:-providing a digital representation associated with the production plant, one or more target plant properties of the production plant and a starting catalyst composition; -determining a target catalyst composition by optimizing the starting catalyst composition with respect to the one or more target device performance using the digital representation associated with the production device; and-generating and / or providing the target catalyst composition for use in the production plant.

A pyrolysis oil is contacted with a hydrocracking catalyst disposed within a hydrocracking unit to convert at least a portion of the pyrolysis oil into a lower alkane to produce a hydrocracking product stream. The hydrocracking product stream is separated into an ethane feed stream comprising ethane and a C3+ feed stream comprising at least one of a C3 alkane, a C4 alkane, or a higher alkane. The C3+ feed stream is diluted with steam to form a steam cracking feed stream. The steam cracking feed stream is heated in a steam cracker to convert at least a portion of the C3+ feed stream to ethylene. The ethane feed stream is diluted with an oxidant to form an oxidative dehydrogenation (ODH) feed stream. The ODH feed stream is contacted with an ODH catalyst disposed within an ODH reactor to convert at least a portion of the ethane to ethylene.

The invention provides a combined process method for improving the yield of vacuum residue catalytic cracking products, which comprises the following steps: determining the asphaltene dispersion coefficient d of vacuum residue according to a formula (1), where w asphaltene, w colloid and w aromatics respectively represent the mass fractions of asphaltene, colloid and aromatics in vacuum residue; and carrying out modification and catalytic cracking reaction on the vacuum residue. According to the combined process method, the asphaltene dispersion coefficient d is ingeniously designed, and d is smaller than or equal to 0.5 and dgt; the vacuum residue of which the content is 0.5 is modified by adopting different modification methods, and then catalytic cracking reaction is performed under different conditions, so that the density of a catalyst in a reactor is improved, oil-agent contact in the reactor is improved, the contact instantaneous effective agent-oil ratio can be improved, the catalytic cracking reaction ratio can be remarkably improved, thermal cracking and condensation coke generation reactions are reduced, and the catalytic cracking efficiency is improved. Conversion of inferior heavy oil is promoted, meanwhile, the coke yield is remarkably reduced, and the yield of high-value products is increased.

This invention provides a sulfur transfer aid, its preparation method, and its application. The sulfur transfer aid comprises 30%-70% magnesium oxide, 15%-60% aluminum oxide, 10%-15% cerium oxide, and 2%-5% vanadium pentoxide. The magnesium oxide is provided by a first magnesium source and a magnesium-aluminum matrix material, and the aluminum oxide is provided by a first aluminum source and a magnesium-aluminum matrix material. On a dry basis, the mass of the magnesium-aluminum matrix material is 5%-30% of the total mass of the raw materials of the sulfur transfer aid. The magnesium-aluminum matrix material is obtained by crystallizing a mixture of a second magnesium source and a second aluminum source after sol-treatment, and the magnesium-aluminum matrix material comprises magnesium oxide and aluminum oxide in a mass ratio of 0.2-0.8:1. This invention also provides a preparation method for the above-mentioned sulfur transfer aid and its application in catalytic cracking processes. This sulfur transfer aid can efficiently desulfurize and is suitable for industrial production.