405 results about "Naphtha" 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.

The invention relates to the technical field of fraction optimization, and discloses a catalytic isomerization-based fraction optimization regulation and control device and method.The catalytic isomerization-based fraction optimization regulation and control device comprises a rectifying tower, the outer wall of the rectifying tower is in through connection with an air inlet, the outer wall of the rectifying tower is in through connection with a liquid inlet, the outer wall of the rectifying tower is in through connection with a reflux inlet, and the top of the rectifying tower is in through connection with an air outlet; when a gas phase passes through the gas outlet, the gas phase jacks the floating valve shell to move upwards, makes contact with the inner wall of the top of the floating valve shell, is blocked by the limiting plate and flows out of the gas outlet groove, and a plurality of gas holes are formed in a catalyst, so that the contact time of the gas phase and the catalyst is prolonged; the problems that when a conventional float valve rectifying tower is used, the contact time of a gas phase in a catalyst layer is short, the deep isomerization reaction time of light naphtha is usually long, only low-carbon hydrocarbon isomerization or simple etherification reaction can be treated, and deeper catalytic isomerization cannot be carried out are effectively solved.

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.

Naphtha reforming catalysts are described. The catalyst includes a support comprising a solid solution or a homogenous mixture of atoms in solid state having a single crystal structure comprising AI2O3, and / or 0.01 to 3 wt% of a first metal of Group 2 or Group 15 of the Periodic Table, or a combination thereof. It also includes 0.05 to 5.0 wt% Pt and 0.05 to 5.0 wt% Re; 0.01 to 2 wt% of at least one additional metal from Groups 1, 2, 3, 9, or 15 of the Periodic Table, or combinations thereof; 0.03 to 1.0 wt% S; and 0.5 to 2 wt% of a halogen. The catalyst has an average bulk density in a range of 0.25 - 1.50 g / cc and a surface area in a range of 50-300 m2 / g. Catalytic reforming processes are also described.

The utility model belongs to the technical field of petrochemical engineering, and particularly provides a system for controlling the blending hydrogenation crude gasoline proportion of a reforming device, which comprises a normal pressure naphtha control pipeline, a hydrogenation crude gasoline control pipeline, a raw material buffer tank, a gasoline mixing unit, a liquid level controller I and a liquid level controller II, the problems that a traditional blending mode is not timely in adjustment, poor in precision, poor in reforming reaction effect, unstable in product quality and increased in equipment operation risk are solved, the liquid level in the raw material buffer tank is accurately, stably and effectively adjusted and controlled, and a solid guarantee is provided for efficient and stable operation of the device and improvement of the product quality.

The invention discloses a high-yield and low-carbon-deposition regulation and control method and system for a continuous regenerative catalytic reforming reaction. The method comprises the following steps: at the beginning, setting a weighted average inlet temperature for the four-in-one reforming reactor and setting an inlet temperature of each bed layer; measuring the content of naphthenic hydrocarbon in naphtha to be added at the beginning, and setting the initial average pressure of the four-in-one reforming reactor according to the content of naphthenic hydrocarbon in naphtha to be added; naphtha is added into the four-in-one reforming reactor for a reaction; in the reaction process, the weighted average inlet temperature of the four-in-one reforming reactor, the inlet temperature of each bed layer, the catalyst circulation rate and the average pressure are regulated and controlled in real time; and ending the experiment. The method breaks through the critical path of the current technical bottleneck, and has important significance for improving the product selectivity of the continuous regeneration catalytic reforming process, reducing the energy consumption and prolonging the service life of the catalyst.

The application provides a method for removing oxygen-containing compounds from Fischer-Tropsch naphtha, which comprises the following steps: (1) reacting Fischer-Tropsch naphtha, a catalyst, isopropyl alcohol and glycol in a stirring reactor, and then standing and separating; (2) extracting the upper hydrocarbon phase after standing with an extractant to obtain an extraction phase and a raffinate phase; (3) recovering the solvent in a solvent recovery column, obtaining oxygen-containing compounds at the top of the column, and recycling the solvent obtained at the bottom of the column as the extractant; (4) washing the raffinate phase with water to obtain Fischer-Tropsch naphtha from which the oxygen-containing compounds are removed and washed water, recycling the washed water to the water washing column for water washing, and recycling the product at the bottom of the water recovery column as the extractant; the extractant is a mixture of ester compounds and glycol compounds, and the content of the glycol compounds is 40-70%; and the method can reduce the oxygen-containing compounds in the Fischer-Tropsch naphtha to 5 ppm, and the oil recovery rate reaches more than 95%.

The present application relates to the technical field of catalyst recovery, in particular to a recycling method of waste aluminum-based platinum-rhenium catalyst, a reforming catalyst and its application, and a method for catalytic reforming of naphtha. The recycling method comprises the following steps: S1, the waste aluminum-based platinum-rhenium catalyst is divided into two parts, one part is dissolved with an acid solution, and a first filtrate and a first filter residue are obtained by filtration; the other part is mixed with a hydroxide and then melted, the melt is dissolved with water, and a second filtrate and a second filter residue are obtained by filtration; S2, rhenium and platinum in the first filter residue and the second filter residue are separated; platinum and rhenium in the first filtrate are separated, and a tail liquid is obtained; S3, the second filtrate is mixed with the tail liquid obtained in step S2 to prepare alumina; S4, platinum and rhenium from the first filtrate, the first filter residue and the second filter residue in step S2 are enriched and loaded on the alumina prepared in step S3. The present application has high platinum and rhenium recovery rate, high economic benefit, and can realize full life cycle utilization of waste aluminum-based platinum-rhenium catalyst.

The application relates to a method for efficient utilization of solid waste, in particular to a catalytic method for polyolefin waste. The application provides a preparation method of a catalyst for catalyzing polyolefin waste, which comprises the following steps: 1) mixing an acid molecular sieve and an active metal precursor, and roasting to obtain a catalyst precursor; and 2) reducing the catalyst precursor by a reducing agent to obtain the catalyst. In the application, the acid molecular sieve is used as a carrier, solid ion exchange is carried out through high-temperature roasting, the active metal component is solidified in the molecular sieve channel structure, the reduced catalyst has rich acid sites, defect sites and high-dispersed active metals, and in combination with the shape selection and confinement of the molecular sieve structure, efficient conversion of the polyolefin waste into naphtha can be realized.

A process is described for synthesising hydrocarbons comprising the steps of: (a) feeding a gas mixture comprising hydrogen and carbon dioxide to a reverse water-gas shift unit to form a crude synthesis gas comprising hydrogen, carbon monoxide carbon dioxide and steam, (b) cooling the crude synthesis gas to condense water and removing water, and optionally carbon dioxide, from the crude synthesis gas to produce a feed stream comprising hydrogen and carbon monoxide, (c) passing the feed stream though a hydrocarbon synthesis unit comprising a reactor containing a Fischer-Tropsch catalyst to form a product stream comprising a mixture of liquid hydrocarbons, a co-produced water stream, and a tail gas stream containing hydrogen, carbon monoxide and gaseous hydrocarbons, and (d) upgrading the product stream in an upgrading unit to produce an upgraded product stream, wherein a naphtha stream is separated from the product stream or the upgraded product stream, at least a portion of the tail gas stream is fed with steam to a first derichment vessel containing a derichment catalyst to form a first gas mixture containing methane, at least a portion of the naphtha stream is fed with hydrogen and steam to a second derichment vessel containing a derichment catalyst to form a second gas mixture containing methane, and the first and second gas mixtures containing methane are fed to the reverse water gas shift unit. A system for performing the process is also provided.

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.

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 preparation, and discloses a catalytic cracking catalyst, its preparation method, and its application. The catalytic cracking catalyst comprises a molecular sieve, a binder, and clay; based on the total mass of the catalyst, the mass content of the molecular sieve is 60-85%, the mass content of the clay is 5-20%, and the mass content of the binder is 10-35%; the mesopore size of the catalyst is 3-50 nm; in the catalyst, the volume of mesopores with a pore size of 6-10 nm accounts for 8-30% of the total mesopore volume; in the catalyst, the volume of mesopores with a pore size of 30-35 nm accounts for 10-30% of the total mesopore volume. This catalyst exhibits excellent catalytic performance and, when applied to catalytic cracking reactions, especially naphtha catalytic cracking reactions, demonstrates high conversion rates and low-carbon olefin yields.

The invention discloses a catalytic cracking light naphtha processing method. The method comprises the following steps: (I) mixing catalytic cracking light naphtha with hydrogen, and then feeding the mixture into a hydrofining reaction zone for hydrofining reaction to obtain a refined naphtha material flow; (II) the refined naphtha material flow obtained in the step (I) enters a hydro-conversion reaction zone to be subjected to a hydro-conversion reaction, converted catalytic cracking light naphtha is obtained, and the temperature of the hydro-conversion reaction is 100-300 DEG C higher than that of the hydrofining reaction. According to the present invention, the olefin in the catalytic cracking light naphtha product is completely saturated, the normal hydrocarbon content is increased, and the triene yield can be substantially improved when the catalytic cracking light naphtha product is adopted as the ethylene raw material through steam cracking.

The invention discloses a method for preparing industrial hexane with ultralow benzene content through pre-hydrogenation. The method comprises the following steps: light naphtha, hydrogen and a hydrogenation catalyst are subjected to a hydrogenation reaction in a hydrogenation reactor for desulfurization and dearomatization, and a first mixture is obtained; feeding the first mixture into a gas-liquid separator to respectively obtain a liquid-phase product and a hydrogen-containing gas-phase product, and separating hydrogen from the gas-phase product through a circulating hydrogen compressor for recycling; and sequentially carrying out second rectification and third rectification on the liquid-phase product to obtain a heavy component substance, and adsorbing the heavy component substance through a molecular sieve. According to the method, by means of front hydrogenation reaction and rear molecular sieve adsorption, on one hand, the reaction load of molecular sieve adsorption is greatly reduced while the reaction activity of the hydrogenation reaction is improved; on the other hand, an extracting agent does not need to be added, other gas-phase and liquid-phase components are not introduced except hydrogen, the preparation process is greatly simplified, and the benzene content in the obtained cyclohexane is smaller than 5 ppm.

This invention discloses a molybdenum-based slurry-bed hydrocracking catalyst for inferior oil, its preparation method, and its application method. The preparation method includes: mixing slurry-bed hydrocracking tailings with naphtha obtained from the process, separating and removing oil from the tailings to obtain a solid residue; calcining in air to obtain a solid powder; dissolving each gram of solid powder in 2-6 ml of ammonia water under stirring conditions, controlling the dissolution temperature at 50-100°C and dissolving for 1-6 hours to obtain a first mixture; filtering to obtain a solution; and... Under stirring conditions, a methanol solution of zinc nitrate and dimethylimidazole was added to the solvent; the reaction was carried out at room temperature for 4–12 h to obtain a second mixture; the mixture was filtered to obtain a precipitate; the precipitate was dried at 60–150 °C for 1–12 h to prepare a ZIF-8 coated molybdenum salt catalyst precursor; the ZIF-8 coated molybdenum salt catalyst precursor was calcined at 400–800 °C for 1–6 h in an oxygen-free atmosphere to obtain a molybdenum-based low-quality oil slurry bed hydrocracking catalyst.

Diesel fuel and / or fuel blending compositions are provided that have improved emissions profiles by blending a narrow boiling range fraction of an alkylate product into the diesel fuel and / or fuel blending composition. The narrow boiling range alkylate fraction that is blended into the product has a reduced or minimized content of both light naphtha components and diesel boiling range components. As a result, the narrow boiling range alkylate fraction is a fraction that contains a substantial portion of C5 to C12 branched paraffin while generally having little or no aromatics content of aromatics as well as having a reduced or minimized sulfur content. Blending of the narrow boiling range alkylate fraction in diesel results in lower T10 values, lower T90 values, lower aromatic content, higher heating value, and a higher molar ratio of hydrogen to carbon as compared to conventional diesel.

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 the technical field of molecular sieve synthesis, in particular to a sheet ZSM-5 molecular sieve as well as a preparation method and application thereof. The preparation method of the sheet ZSM-5 molecular sieve comprises the following steps: S1) uniformly mixing an aqueous solution of a silicon source, a mineralizer, an aluminum source and a seed crystal to obtain gel; and S2) mixing the gel with a growth inhibitor, crystallizing, and calcining to obtain the sheet ZSM-5 molecular sieve. A mineralizer and a growth inhibitor are introduced in a molecular sieve crystallization process, and the sheet ZSM-5 molecular sieve is directly prepared by a one-pot method. The method is simple and convenient to operate and simple in step, and the prepared sheet molecular sieve has the characteristics of high specific surface area and short b axis, and is beneficial to reducing the diffusion resistance of macromolecular substrates and products. The molecular sieve is used as an active component in a naphtha cracking catalyst, and shows excellent conversion rate and diene selectivity in a naphtha cracking reaction.

The utility model provides a structure is prevented to come out in naphtha hydrogenation equipment, corrosion inhibitor jar has connected pipeline on intercommunication, the corrosion inhibitor jar in corrosion inhibitor is filled with naphtha hydrogenation equipment by connected pipeline to corrosion inhibitor, the outside of corrosion inhibitor jar with the outside of connected pipeline all is provided with heat preservation layer, the bottom of corrosion inhibitor jar is provided with radiant heat structure. Compared with prior art, in the scheme, the corrosion inhibitor jar and the connecting pipeline are heat preserved, and the corrosion inhibitor jar is heated, so that the corrosion inhibitor can maintain a certain temperature, and the paste-shaped substance is not separated out due to the low temperature environment, and the supply is not affected to cause the equipment failure.

The application discloses a method for producing ethylene raw material. The method comprises the following steps: mixing hydrocracking light naphtha and hydrogen into a first hydroconversion reaction zone to react, and then the reaction effluent enters a separation system to obtain hydrogen-rich gas and a first hydroconversion product; the first hydroconversion product is separated to obtain ethane, propane, isobutane, isopentane and n-pentane; the isobutane is mixed with hydrogen into a second hydroconversion reaction zone, and the reaction effluent is separated to obtain n-butane; the second hydroconversion reaction zone is filled with a hydroconversion catalyst containing ZSM-35 molecular sieve; and the isopentane is recycled to the inlet of the first hydroconversion reaction zone. The first hydroconversion reaction zone is filled with a hydroconversion catalyst containing mordenite, and at least two catalyst beds are filled; and the active metal content of the hydroconversion catalyst decreases in turn along the flow direction. The method can effectively improve the proportion of normal alkanes in the product and improve the quality of the ethylene raw material.

The application provides a naphtha adsorption arsenic removal agent and a preparation method thereof. The preparation method comprises the following steps: taking Al2O3 as a carrier, impregnating treatment is conducted by using a solution containing copper ions, and then drying and calcination are conducted to obtain a CuO / Al2O3 arsenic removal agent; the CuO / Al2O3 arsenic removal agent is subjected to a reduction reaction with a low-carbon alcohol to obtain the naphtha adsorption arsenic removal agent; wherein the carbon number of the low-carbon alcohol is 1-4; wherein the ratio of the CuO / Al2O3 arsenic removal agent to the alcohol is 1g:(1-10)ml. The naphtha adsorption arsenic removal agent has excellent arsenic removal efficiency and arsenic capacity.

The present disclosure relates to a method for separating naphtha, comprising: feeding naphtha and a first desorbent into a first adsorption separation tower for first adsorption separation to obtain a first extract and a first raffinate; feeding the first raffinate into a first rectifying tower for first rectification treatment to obtain a first stream mainly containing cycloalkanes and alkanes; feeding the first stream and a second desorbent into a second adsorption separation tower for second adsorption separation to obtain a second extract and a second raffinate; feeding the second raffinate into a second rectifying tower for second rectification treatment to obtain a second stream mainly containing alkanes; feeding the first extract and the second extract into a third rectifying tower for third rectification treatment to obtain a third stream mainly containing aromatic hydrocarbons and cycloalkanes; wherein the first desorbent is selected from heavy aromatic hydrocarbon components, and the second desorbent is selected from light hydrocarbon components. The method of the present disclosure has low cost, simple process, high separation purity and high yield.

The application discloses a wax oil hydroprocessing method. By timely removing reaction products and separating, and setting catalyst grading according to different components, the raw oil can be subjected to step-by-step targeted hydrogenation reaction in the reactor, so that the problem that the blending ratio is limited due to the incapability of better controlling the hydrogenation depth of the blended catalytic diesel and wax oil raw material is solved, the content of aromatic hydrocarbons in heavy naphtha in the hydrocracking product is greatly increased, and the product quality of diesel and tail oil is improved.

The invention discloses a light naphtha conversion catalyst as well as a preparation method and application thereof. The catalyst comprises a ZSM-5 molecular sieve and macroporous alumina loaded with group VIB metal and group VIII metal, and the molar ratio IA / Imt of the amount IA of the B acid in the light naphtha conversion catalyst to the total amount Imt of the group VIB metal and the group VIII metal of the catalyst body phase is 0.5-5.0. The content of n-alkanes in a product obtained by treating light naphtha with the catalyst is obviously increased, so that the yield of triene when the catalyst is used as a raw material for preparing ethylene through steam cracking can be greatly improved.

Methods and systems for improving operation of a gasoline desulfurization system may include receiving gasoline blending pool data, the gasoline blending pool data indicative of one or more of a sulfur concentration, a current inventory, or an octane number of each current component of a gasoline blending pool. A machine learning model generates a light naphtha sulfur target for a light naphtha produced from a selective hydrogenation reactor of a gasoline desulfurization system based on the gasoline blending pool data and generates a heavy naphtha sulfur target for a desulfurized heavy naphtha produced from a hydrodesulfurization reactor of the gasoline desulfurization system based on the gasoline blending pool data. The machine learning model may be trained on historical data of the gasoline blending pool and historical data of operating parameters, resulting product attributes, and composition from the gasoline desulfurization system, including sulfur concentration and octane number.

The invention discloses an in-situ synthesized naphtha catalytic cracking agent material and a preparation method thereof, and belongs to the field of petrochemical engineering catalytic materials. According to the method, the porous LaF3 composite material is synthesized in situ on the surface of ZSM-5 through a process route of PVP soft template in-situ attachment, hydroxyl modification, LaF3 in-situ deposition and hydrothermal synergistic crystallization. According to the material, through a weak acid-medium strong acid synergistic acidic system and a porous structure, the problems that a traditional catalyst is insufficient in acid sites, mass transfer is blocked and carbon deposition is serious are solved, the initial conversion rate of naphtha is larger than 90%, the total yield of ethylene and propylene is larger than 52%, the carbon deposition amount is only 9.4% after circulation is conducted five times, the structure is stable, the preparation process is simple, and the material has industrial application potential.

The invention belongs to the technical field of aviation fuel, and particularly relates to a C11-C16 cycloalkane component as well as a preparation method, a preparation device and application thereof. The preparation method of the C11-C16 cycloalkane component provided by the invention comprises the following steps: carrying out a hydrodesulfurization and denitrification reaction on a coal tar light fraction and a hydrodesulfurization and denitrification catalyst in a hydrogen-containing atmosphere to obtain refined light oil; carrying out alkylation reaction on the refined light oil, naphtha and a hydrogen type molecular sieve catalyst to obtain an aryl mixture; carrying out hydrogenation reaction on the aryl mixture and a hydrogenation catalyst in a hydrogen-containing atmosphere to obtain a cycloalkane mixture; and the cycloalkane mixture is subjected to fractionation, such that the C11-C16 cycloalkane component is obtained. According to the preparation method provided by the invention, the coal tar light fraction and naphtha are taken as raw materials and can be directionally converted into C11-C16 cycloalkane components, so that the novel aviation fuel with high density and calorific value is prepared.

This invention discloses a combined processing method for alkali metal treatment and fixed-bed hydrotreating of residual oil. The method includes the following steps: reacting residual oil feedstock with alkali metals; separating the reacted material into a liquid phase, which then enters a fixed-bed residual oil hydrotreating unit; and separating the products from the fixed-bed residual oil hydrotreating unit to obtain gas, hydrotreated naphtha, hydrotreated diesel oil, and hydrotreated residual oil. This method can process low-quality residual oil feedstock and extend the operating cycle of the fixed-bed residual oil hydrotreating unit.

The present application provides a method for maximum production of propylene by catalytic cracking of hydrocarbons and a reaction system thereof, which comprises contacting light petroleum hydrocarbons such as diesel oil with a mesoporous molecular sieve catalyst in an isokinetic fluidized bed reactor, and maintaining self-heating balance by recycling regeneration flue gas to maximum production of propylene and the like. The method of the present application can process not only light hydrocarbons such as diesel oil, but also heavy oils such as naphtha, wax oil and residual oil, has high propylene yield, and can achieve self-heating balance, thereby not only solving the problem of excess production capacity of refinery diesel oil, but also making up for the deficiency of chemical materials.