235 results about "Naphtha" patented technology

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.

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 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.

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.

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 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 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 relates to the field of petrochemical catalytic desulfurization technology, specifically disclosing a high-efficiency desulfurizing agent, its preparation method, and its application in the desulfurization of heavy naphtha. The desulfurizing agent provided by this invention has a "two-level" metal active center. The first level is a cobalt center in biochar, and the second level is a nickel-copper bimetallic center introduced through impregnation on the surface of a composite carrier. The desulfurizing agent provided by this invention has excellent desulfurization effect. Under conditions of 140°C and no hydrogen, it can simultaneously remove inorganic sulfur such as hydrogen sulfide and organic sulfur such as thiols, thioethers, and thiophenes from heavy naphtha obtained by hydrocracking of heavy diesel oil, wax oil, or mixed diesel and wax oil, reducing the total sulfur content from 25-40 μg·g. ‑1 Reduced to 0.2 μg·g ‑1 The following methods can effectively protect bimetallic (multimetallic) reforming catalysts from sulfur poisoning, and the preparation process is green and controllable, making it suitable for large-scale industrial applications.

A dividing wall column or a pair of conventional columns can be used to separate an unstabilized naphtha stream to produce an aromatics-free light naphtha stream as a feed for a catalytic cracking unit for olefins production.

The application belongs to the technical field of new materials, and relates to a catalyst based on Sn modified KL molecular sieve as well as a preparation method and application thereof. An aluminum source and a potassium source are added into water to prepare a KAlO2 solution, an ethanol solution of a divalent tin salt is added into a silicon source to uniformly mix to obtain a mixed solution, the KAlO2 solution is added into the mixed solution to fully stir to obtain an initial sol, the initial sol is subjected to crystallization treatment, and then is heated to 450-650 DEG C to perform calcination treatment to obtain Sn modified KL molecular sieve, and Pt is loaded on the Sn modified KL molecular sieve by using an atomic layer deposition method. The catalyst based on the Sn modified KL molecular sieve prepared by the application has better catalytic performance in a naphtha reforming reaction for preparing aromatic hydrocarbons.

To provide a method for recycling the insulating layers of collected insulated wires and cables without performing complicated processing or incurring excessive costs. [Solution] A method for recycling the insulating layer of an insulated electric wire or cable that solves the above-mentioned problems is a method for recycling the insulating layer of an insulated electric wire or cable that has at least a conductor and an insulating layer containing polyethylene or cross-linked polyethylene arranged around the conductor, and includes the steps of separating the conductor from the insulating layer, producing recycled naphtha from the separated insulating layer, and mixing the recycled naphtha with new naphtha to form a new insulating layer of an insulated electric wire or cable. In the recycling method, impurities are removed in the step of producing the recycled naphtha.

Provided is a method for preparing synthesis gas, and more particularly, a method for preparing synthesis gas including: supplying a pyrolysis fuel oil (PFO) stream including a PFO and a pyrolysis gas oil (PGO) stream including a PGO discharged from a naphtha cracking center (NCC) process to a distillation column as a feed stream (S10); and supplying a lower discharge stream from the distillation column to a combustion chamber for a gasification process to obtain synthesis gas (S20).

This invention discloses a method for hydroconversion of catalytic cracking diesel, the method comprising the following steps: (1) catalytic cracking diesel is fractionated to obtain light fraction and heavy fraction of catalytic cracking diesel; (2) the heavy fraction of catalytic cracking diesel first enters the hydrorefining reaction zone and is contacted with the hydrorefining catalyst in the presence of hydrogen to carry out the hydrorefining reaction. When the bed temperature of the hydrorefining reaction zone increases by 40°C to 100°C compared with the inlet temperature of the hydrorefining reaction zone, the light fraction of catalytic cracking diesel is introduced and mixed with the heavy fraction of catalytic cracking diesel after the hydrorefining reaction to continue the hydrorefining reaction; (3) the stream after the hydrorefining reaction in step (2) enters the hydrocracking reaction zone and is contacted with the hydrocracking catalyst to carry out the hydrocracking reaction; (4) the stream obtained in step (3) is separated to obtain light naphtha, heavy naphtha and tail oil. The heavy naphtha is extracted with aromatics to obtain BTX. The method can effectively reduce the loss of aromatics in catalytic cracked diesel during the hydrogenation process and increase the content of BTX components in the hydrogenation products.

The invention relates to the field of aluminum oxide preparation, and discloses modified aluminum oxide as well as a preparation method and application thereof. The modified aluminum oxide comprises aluminum oxide, a first modified component and a second modified component; the first modified component is selected from at least one of IVB group metal elements; the second modified component is a sulfur element; the mass content of the first modification component is 0.01-5% and the mass content of the second modification component is 0.1-5% by element on the basis of the alumina dry basis weight of the modified alumina. The catalyst prepared by using the modified alumina as the carrier is used in the field of catalytic reforming, especially in the field of naphtha catalytic reforming, and has high reaction activity and aromatic hydrocarbon selectivity.

The invention relates to a C4 hydrocarbon fraction fine desulfurization method and a reaction device. The C4 hydrocarbon fraction fine desulfurization method comprises the following steps: (1) mixing an oxidant with naphtha to obtain oxidant carrying oil; (2) mixing the C4 hydrocarbon fraction with the oxidant carrying oil, then adding a mercaptan conversion auxiliary agent, entering an oxidation reactor to be in contact with an oxidation catalyst to carry out oxidation reaction, and converting mercaptan into disulfide; and (3) carrying out rectification separation on the material flow after the oxidation reaction to obtain a fine desulfurized C4 hydrocarbon fraction and sulfur-containing naphtha. According to the method provided by the invention, the safety of the C4 hydrocarbon fraction oxygen dissolving process is improved by virtue of the oxidant carrying oil, the boiling point difference between sulfide and C4 hydrocarbons is increased by virtue of the mercaptan oxidation reaction, the fine desulfurized C4 hydrocarbon fraction with the total sulfur content not greater than 1mg / kg is obtained by adopting a rectification method, and a high-quality raw material can be provided for chemical utilization of the C4 hydrocarbon fraction.

The invention relates to a C4 hydrocarbon fraction fine desulfurization method and a reaction device. The method comprises the following steps: mixing an oxidizing agent with naphtha to obtain oxidizing agent carrying oil; the C4 hydrocarbon fraction, the oxidant carrying oil and a mercaptan conversion auxiliary agent enter an oxidation reactor to be subjected to an oxidation reaction, and mercaptan is converted into disulfide; the material flow after the oxidation reaction is subjected to two-stage rectification separation, a high-quality fine desulfurization light C4 hydrocarbon fraction is obtained after first-stage rectification, and a fine desulfurization heavy C4 hydrocarbon fraction and sulfur-containing naphtha are obtained after second-stage rectification. According to the C4 hydrocarbon fraction fine desulfurization method provided by the invention, the possibility that the C4 hydrocarbon fraction and the oxidant are mixed to form explosive gas is avoided, and the safety of the oxidative desulfurization process is improved. And carrying out two-stage rectification separation to obtain a high-grade fine desulfurization light C4 hydrocarbon fraction with isobutene as a main component and a fine desulfurization heavy C4 hydrocarbon fraction with cis-2-butene / trans-2-butene as a main component, so as to meet the requirements of different users for utilizing the C4 hydrocarbon fractions.

The present application relates to the technical field of aviation gasoline, and discloses unleaded aviation gasoline and a preparation method thereof.The unleaded aviation gasoline comprises: 75-85 wt% of polymethylbenzene, and 15-25 wt% of at least two of alkylate, a side line distillation component of an alkylate device, light naphtha and isopentane; wherein the motor octane number of the polymethylbenzene is not less than 108.The product quality index of the unleaded aviation gasoline meets the standard of the American Society for Testing and Materials, that is, the technical requirement of ASTM D7719-2018 high-aromatic unleaded aviation gasoline.The unleaded aviation gasoline has the characteristics of good component continuity, stable combustion and high motor octane number, and meets the high-standard use requirement of unleaded and high-octane aviation gasoline.

The present invention relates to the process for upcycling synthetic and organic waste into valuable commodities. This invention offers method capable of transferring and managing mixed feedstock streams, including plastic waste, biological waste, municipal solid waste, municipal sewage sludge, and shredder residue, to produce gas, oil, light hydrocarbons, e.g., circular naphtha, specialty chemicals, and carbon solids that can be utilized directly or subjected to further refinement.

A gas supply device for the feed heater and thermal oil furnace of a naphtha hydrogenation unit is characterized by: a valve assembly installed on the inlet pipeline of the fuel gas separator; the inlet pipeline of the valve assembly is divided into two lines, one for natural gas and the other for the main fuel gas pipeline; the outlet pipeline of the fuel gas separator is also divided into two lines, one connected to the feed heater and the other connected to the thermal oil furnace. This invention, by adding a natural gas pipeline, switches the gas supply to the feed heater and thermal oil furnace to natural gas when flue gas indicators are abnormal, avoiding abnormal flue gas from the heater due to changes in fuel gas composition. This ensures stable operation of the unit and compliant flue gas emissions, meeting environmental protection requirements and reducing environmental risks for enterprises. It largely maintains the original structure of existing equipment, requiring no major modifications, and features low modification costs and high economic benefits.

Provided is a method for efficiently manufacturing a chemical product from a waste material including waste tires, which enables long-term operation of a process by improving each step in a series of processes. A method for producing a chemical product, the method comprising: a thermal cracking step for obtaining a first gas component, a pyrolytic oil, and a residue component by thermally cracking a crushed waste material including a waste tire; a low-temperature hydrogenation step in which a low-temperature hydrogenated oil is obtained by subjecting a raw oil containing at least a portion of the pyrolytic oil to low-temperature hydrogenation at 180-350 DEG C; a separation step for separating into a naphtha fraction and another fraction by atmospheric distillation of a raw oil for atmospheric distillation containing at least a portion of the low-temperature hydrogenated oil and crude oil; and a steam cracking step for obtaining a chemical product by subjecting a steam cracking raw oil containing at least a portion of the naphtha fraction to a steam cracking treatment. In the thermal cracking step, the amount of the pyrolytic oil is 40% by mass or more with respect to the total amount of the first gas component, the pyrolytic oil, and the residue component.

The present application relates to supported platinum, tin reforming catalyst and its preparation method and application and naphtha catalytic reforming method. The supported platinum, tin reforming catalyst includes inorganic oxide carrier and the components with the content as follows: 0.1-1.0 mass% of platinum, 0.1-1.0 mass% of group IVA metal and 0.1-2.0 mass% of halogen, wherein the total amount of platinum in the surface layer of the catalyst accounts for 0.1-30% of the total amount of platinum in the catalyst, and the total amount of group IVA metal in the surface layer of the catalyst accounts for 25-70% of the total amount of group IVA metal in the catalyst; the surface layer of the carrier refers to the layer from the surface of the carrier to the inside of the carrier, the thickness of which accounts for 0.1-30% of the total thickness of the carrier. When used for catalytic reforming reaction, the catalyst of the application can significantly improve C5 + Liquid product yield, catalyst aromatic yield and carbon deposition rate are low.

The invention discloses a preparation method of isohexadecane solvent naphtha, which comprises the following steps: treating a raw material isohexadecane mixture by a feed adsorption tank and a feed filter, feeding into a feed buffer tank, boosting by a hydrogenation feed pump, mixing with recycle hydrogen, exchanging heat with reaction generated oil, and feeding into a pre-hydrogenation reactor; a pre-hydrogenation reaction product is mixed with high-pressure circulating oil and circulating hydrogen, is subjected to heat exchange with reaction generated oil, is fed into a hydrofining reactor, is subjected to heat exchange, is cooled, and is fed into a high-pressure separator; the reaction generated oil and the hydrogenation generated oil at the bottom of the high-pressure separator are sent to a product separation tower after components are removed by a light component removal tower; the product separation tower is provided with a side stream stripping tower, isohexadecane solvent oil is extracted from the bottom of the side stream stripping tower, and byproducts such as isododecane solvent oil and isoeicosane solvent oil are extracted from the top and the bottom of the separation tower respectively. The method prolongs the service life of the catalyst and the operation cycle of the device, reduces the operation energy consumption of the device, reduces the carbon emission and saves the investment.