670 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.

A method and apparatus for the rapid analysis of the molecular components of naphtha. The method comprises: receiving scanning spectrum data of target naphtha (S201); using a calibration spectrogram data set to calibrate the scanning spectrum data, wherein the calibration spectrogram data set is obtained by means of scanning a plurality of naphtha samples under preset detection conditions by using a plurality of spectrometers, and the scanning spectrum data is obtained by means of scanning the target naphtha on the basis of a first scanner among the plurality of spectrometers (S202); and performing, from a preset naphtha molecular composition library, matching to obtain a molecular composition corresponding to the calibrated scanning spectrum data, and obtaining predicted molecular properties of the target naphtha on the basis of the molecular composition, so as to determine macroscopic properties of the target naphtha, wherein the naphtha molecular composition library is obtained by using comprehensive two-dimensional gas chromatography technology (S203). The analysis of fraction molecular components of naphtha fractions and the characterization of macroscopic physical properties of petroleum fractions can be accurately and efficiently implemented.

The invention relates to the technical field of gasoline processing, in particular to a method and a device for producing diesel oil with a low freezing point by taking heavy aromatics and mixed diesel oil as raw materials, the method comprises the following steps of: 1, mixing the heavy aromatics, the mixed diesel oil and hydrogen, feeding into a hydrofining unit, and carrying out hydrofining reaction under the action of a hydrofining catalyst, a hydrofining reaction product is obtained; step 2, the hydrofining reaction product enters a hydro-upgrading unit and is subjected to hydro-upgrading reaction under the action of a hydro-upgrading catalyst, and a hydro-upgrading reaction product is obtained; and 3, feeding the hydro-upgrading reaction product into a rectification unit, and carrying out rectification separation to obtain naphtha and-35 # diesel oil with a low freezing point. The heavy aromatics, the hydrogen and the mixed diesel oil are mixed, the obtained mixed material is subjected to hydrofining and hydro-upgrading treatment, the-35 # low-freezing-point diesel oil is obtained, the method has the advantages of being short in technological process and small in equipment investment, the field process does not need to be greatly transformed, and the quality improvement and efficiency improvement effects are remarkable.

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.

[Problem] To provide a method capable of producing a monocyclic aromatic hydrocarbon such as benzene or xylene effective as a base raw material, with a naphtha raw material containing renewable naphtha. [Solution] A method for producing at least one monocyclic aromatic hydrocarbon of benzene or xylene with a naphtha raw material containing renewable naphtha, the method including step (A-1) of pyrolyzing the naphtha raw material in the presence of water vapor, to produce and separate toluene, and step (A-2) of subjecting toluene to disproportionation reaction or transalkylation reaction, to produce and separate at least one monocyclic aromatic hydrocarbon of benzene or xylene.

The invention discloses a wax oil hydrotreating method. Reaction products are timely removed and separated, and catalyst grading setting is performed according to different components, so that raw oil can be subjected to echelon targeted hydrogenation reaction in the reactor, and the problem that the blending ratio is limited due to the fact that the hydrogenation depth cannot be better controlled during blending of catalytic diesel oil and wax oil raw materials is solved; the aromatic hydrocarbon content in heavy naphtha in a hydrocracking product is greatly increased, and the product quality of diesel oil and tail oil is improved.

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.

The invention provides a method for pretreating a Fischer-Tropsch synthesis catalyst and a method for converting Fischer-Tropsch synthesis gas by using the pretreated catalyst obtained by the method for pretreating the Fischer-Tropsch synthesis catalyst. The method for pretreating the Fischer-Tropsch synthesis catalyst comprises the following steps: 1) reducing a main catalyst which is an iron-based catalyst; 2) carbonizing the main catalyst; (3) passivating the main catalyst; and 4) impregnating a mixture of an auxiliary agent and the main catalyst obtained in the step 3) with liquid wax, naphtha or heavy diesel oil. In the method for pretreating the Fischer-Tropsch synthesis catalyst, a passivation process is introduced after reduction and carbonization, the activity of the catalyst is stably and slowly released, and rapid deactivation is avoided; after the main catalyst is reduced, carbonized and passivated, the auxiliary agent is added and mixed, so that the auxiliary agent does not participate in the reduction and carbonization process of the iron oxide and does not influence the reduction and carbonization effect; the liquid wax or naphtha or heavy diesel oil is mixed with the mixture slurry of the main catalyst and the auxiliary agent, so that transportation and pipeline transportation are facilitated.

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.

A process for improving yield of kerosene from a renewable feedstock involves directing a to a lead stripper to separate a lead stripper bottoms stream comprising naphtha and higher boiling point range hydrocarbons and a lead stripper overhead stream. The lead stripper bottoms stream is passed to a naphtha recovery column to separate a vapor stream comprising naphtha and water in an overhead stream from a heavy hydrocarbon product stream. The vapor stream is condensed and water is removed to produce a product naphtha stream. Kerosene and diesel boiling point range product streams are separated from the heavy hydrocarbon product stream in a vacuum fractionator.

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%.

A low-pressure condensed water treatment device of a naphtha separation system comprises a pressure-bearing tank and a condensed water output assembly, the pressure-bearing tank is located on the ground, a water inlet of the pressure-bearing tank is connected with a low-pressure condensed water main pipe of the naphtha separation system, and the condensed water output assembly is connected to a water outlet of the pressure-bearing tank. And a water inlet main gate valve is arranged on a pipeline between the water inlet of the pressure-bearing tank and a low-pressure condensed water main pipe of the naphtha separation system. The condensed water output by the naphtha separation system is collected through the pressure-bearing tank, steam contained in the condensed water is liquefied by increasing pressure, meanwhile, the pressure-bearing tank is placed on the ground to exchange heat with the ground, liquefaction of the steam in the condensed water is accelerated, it is guaranteed that no steam is contained in the output condensed water, and energy is saved. Therefore, leakage caused by flushing of pipelines and elbows is avoided, and stable operation of the naphtha separation system is guaranteed.

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.