597 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.

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.

The present disclosure relates to a process for removal of carbonyl impurities from a mixed hydrocarbon stream obtained from naphtha and gas stream cracking processes. The process of the present disclosure is simple, economical and environment friendly. The process of the present disclosure is efficient in removing higher amounts of carbonyl impurities. The process of the present disclosure can be easily scaled up for commercial purposes.

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.

A method for scheduling a naphtha cracking center by at least one processor, includes the steps of: obtaining input information; determining, by the at least one processor, incoming tank information using a first agent based on the input information, wherein the first agent is a first artificial intelligence device configured to be learned by reinforcement learning; determining, by the at least one processor, mixing tank combination information using a second agent, wherein the second agent is a second artificial intelligence device configured to be learned by reinforcement learning; and determining, by the at least one processor, cracking furnace operation information using a third agent, wherein the third agent is a third artificial intelligence device configured to be learned by reinforcement learning.

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.

A process for converting naphtha is disclosed. The process comprises contacting a naphtha stream and a hydrogen stream with a catalyst in a reactor to produce a paraffinic stream. The ethane present in the paraffinic stream is converted into ethylene in a steam cracking unit. An ethylene stream is separated from a C3+ hydrocarbon stream and the C3+ hydrocarbon stream is recycled to the reactor.

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.

A method for transporting hydrogen may comprise, at a first hydrocarbon processing facility, passing a heavy naphtha stream, a C9+ aromatic compounds-containing stream, and an input hydrogen-containing stream to a hydrotreater to form a hydrotreated effluent stream; passing the hydrotreated effluent stream to a separation unit to form a naphthenics-containing stream and a separation unit effluent stream; transporting the naphthenic stream to a second hydrocarbon processing facility; and at the second hydrocarbon processing facility, passing at least a portion of the naphthenic stream to a dehydrogenation unit to form a hydrogen product stream. The first hydrocarbon processing facility and the second hydrocarbon processing facility may be separated by a distance of at least 100 km. Further disclosed herein are methods of processing hydrogen which produce aromatic compounds, including C9+ aromatic compounds containing streams.

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 invention relates to the technical field of detection and sampling, in particular to a naphtha production multi-process detection and sampling system which comprises a closed sampler, the closed sampler comprises a liquid storage tank used for temporarily storing naphtha, and a liquid suction mechanism used for stretching into different depth positions in a reaction kettle for sampling is arranged on the lower side of the closed sampler. According to the closed sampler, a liquid guide pipe in the liquid suction mechanism is matched with an opening and closing assembly, the sliding depth of the liquid guide pipe and opening and closing of a flow guide opening of a blocking cover are manually adjusted, and the closed sampler can accurately stretch into different liquid layer positions in a reaction kettle for sampling; by adopting the synergistic effect of the annular floating plate, the scraping frame and the constant-force spring in the cleaning mechanism, the annular floating plate slides up and down along with the floating of the liquid level to drive the spiral scraping plate of the scraping frame to rotationally scrape the inner wall of the liquid storage tank, high-viscosity naphtha residues are effectively removed, and cross contamination of different batches of samples is avoided.

The invention relates to an absorption stabilization system and a separation method of a wax oil hydrocracking unit, which are characterized in that an original naphtha separation tower is changed into a heavy naphtha tower, a feed stream is adjusted into a mixture of top oil of a steam stripping tower, top oil of a pre-fractionating tower and top oil of a main fractionating tower, and heavy naphtha is produced at the bottom of the tower; tower top distillate and tower bottom oil of the deethanizer are mixed and then enter a debutanizer, liquefied gas is obtained at the tower top after separation, light naphtha is obtained at the tower bottom, and part of the light naphtha serves as an absorbent to be recycled. By changing the top oil feeding position of the main fractionating tower, reducing the processing amount and the energy consumption of the debutanizer, and adopting pure light naphtha as an absorbent in the absorption tower, the adsorption effect is better, and the composition of the bottom of the debutanizer is changed, so that a reboiling heat source is changed from middle-section reflux of the main fractionating tower to product diesel oil, and the heat consumption level is reduced. The method does not change the reaction and main fractionating tower system process, has strong applicability in the aspects of new device construction and old device transformation, effectively solves the problem of high energy consumption in the traditional process, and improves the overall benefits of the device.

The present invention provides a hydrocracking method and system for processing high-drying point wax oil. The system includes a feedstock separation unit, a hydropretreatment unit, a first hydrocracking unit, a separation unit, a second hydrocracking unit, and a product separation unit. The method comprises the following steps: first, the high-drying point wax oil feedstock is cut to obtain a light wax oil feedstock and a heavy wax oil feedstock; the light wax oil feedstock sequentially enters the hydropretreatment unit and the first hydrocracking unit for reaction, and the first hydrocracking stream obtained after the reaction enters the separation unit for separation to obtain gas, light naphtha, heavy naphtha, and tail oil; the heavy wax oil feedstock and tail oil enter the second hydrocracking unit for reaction, and the second hydrocracking stream obtained after the reaction is cut into light and heavy components. The heavy second hydrocracking stream obtained is circulated to the hydropretreatment unit, and the light second hydrocracking stream is circulated back to the separation unit. The hydrocracking method provided by the present invention can improve the long-term operation stability of the high-drying point wax oil hydrocracking unit and the product yield of high-quality reforming feedstock represented by heavy naphtha.

The present invention discloses a hydrocracking method for producing chemical raw materials. The method includes: (1) in the presence of hydrogen, a hydrocarbon oil raw material enters a first hydrocracking reaction zone to selectively crack the n-alkanes in the hydrocarbon oil raw material to obtain a first hydrocracking product; wherein, in the first hydrocracking product, the mass content of C7 + n-alkanes is controlled below 5.0%; (2) in the presence of hydrogen, the first hydrocracking product enters a second hydrocracking reaction zone to obtain a second hydrocracking product containing monocyclic cyclic hydrocarbons; (3) the second hydrocracking product is separated and fractionated to obtain a gas fraction, light naphtha, and heavy naphtha. When using the hydrocarbon oil as a raw material to produce chemical raw materials, this method can significantly improve the yield and quality of chemical raw materials.

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.