48results about "Effluent separation" patented technology

Disclosed herein are methods and systems for producing hydrocarbon products through reactor platforms utilizing a catalyst suspended in the reacting fluids, where the feedstock to the reactor may be a renewable feedstock, circular feedstock, and / or a blend of renewable and circular feedstocks. The disclosed methods and processes include a recycle pump system within the ebullated bed reactor vessel. This internal recycle dilutes olefins, thereby mitigating explosive olefin hydrogenation without limiting the flow of fresh feedstock to the ebullated bed reactor. The disclosed methods and processes include catalyst recovery systems for recovering the suspended catalyst and returning it to the reactor feed.

The application discloses a processing method of aromatic raffinate oil. The method comprises the following steps: (1) contacting and reacting aromatic raffinate oil, hydrogen and a hydroconversion catalyst in a hydroconversion reaction zone, wherein the hydroconversion catalyst is a molecular sieve catalyst, and the molecular sieve is selected from any one of mordenite or ZSM-5 molecular sieve; (2) separating the hydroconversion reaction effluent obtained in the step (1) to obtain a hydrogen-rich gas and a liquid phase stream; and (3) separating the liquid phase stream obtained in the step (2) to obtain a liquid phase product and a gas phase product. The method can effectively convert isomeric alkanes in the aromatic raffinate oil into n-alkanes, and improve the ethylene raw material quality.

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 discloses a hydroconversion method of sulfur-containing naphtha. The method comprises the following steps: mixing the sulfur-containing naphtha with hydrogen and performing hydroconversion reaction through a hydroconversion reaction zone; the reaction effluent enters a separation system to obtain hydrogen-rich gas and a hydroconversion product through separation; the hydroconversion reaction zone is sequentially filled with a hydroconversion catalyst I and a hydroconversion catalyst II along the flow direction; and the volume ratio of the hydroconversion catalyst I to the hydroconversion catalyst II is 1:3-3:1. The method can effectively convert isomeric alkanes in the naphtha into normal alkanes, improve the ethylene raw material quality, and solve the problem of sulfur injection in the ethylene production device.

The application discloses a processing method of sulfur-containing naphtha. The method comprises the following steps: (1) mixing the sulfur-containing naphtha with hydrogen, and passing the mixture through a hydroconversion reaction zone, wherein the hydroconversion reaction zone is filled with at least two hydroconversion catalyst beds, and the mass content of active metals in the downstream catalyst bed is 1-25 percentage points lower than that in the upstream catalyst bed in terms of oxides; (2) carrying out high-pressure separation on the hydroconversion reaction effluent obtained in the step (1), and separating hydrogen-rich gas and liquid phase effluent, wherein the liquid phase effluent enters a separation system, and ethane, propane and n-butane are separated. The method can solve the problem of sulfur injection in an ethylene production device by using hydrogen sulfide-containing hydrogenation products as ethylene raw materials.

The utility model discloses a biomass tar cracking device under hydrogen-rich atmosphere, which relates to the technical field of biomass tar cracking, and comprises a reaction tank body, a mounting pipe is rotatably arranged in the middle of the upper end of the reaction tank body, a plurality of air inlets are arranged on the mounting pipe, and filter screen plates are fixedly arranged in the air inlets. A cleaning mechanism is arranged at the upper end in the reaction tank body, a rotary connecting pipe is rotationally arranged on the mounting pipe, and a material turning mechanism is arranged at the bottom end of the mounting pipe. According to the reaction tank disclosed by the utility model, the filter screen plates are arranged at the gas inlets in the mounting pipe, so that impurities in cracked gas can be conveniently filtered, and cracked materials at the bottom end in the reaction tank body can be conveniently turned over circularly by arranging the transmission pipe and the spiral plate.

This invention discloses a hydrogenation process and system for animal and vegetable oils. The process includes the following steps: 1) Animal and vegetable oil raw materials are mixed with hydrogen and then fed into a fluidized bed hydrogenation reactor for reaction. The reaction effluent is separated to obtain gaseous and liquid phase effluents; 2) The liquid phase effluent obtained in step 1) is processed in a purification unit to obtain purified oil; 3) The purified oil obtained in step 2) is fed into a hydrorefining reactor for hydrorefining reaction. The reaction effluent is fractionated to obtain jet fuel and biodiesel. The hydrogenation process provided by this invention, combined with the characteristics of hydrogenation of animal and vegetable oils, offers a highly efficient technical route for the hydrogenation of animal and vegetable oils to produce biodiesel.

The application discloses a method for converting sulfur-containing naphtha. The method comprises the following steps: mixing the sulfur-containing naphtha with hydrogen, and then passing the mixture through a hydroconversion reaction zone; and separating a reaction product to obtain hydrogen-rich gas and a hydroconversion product, wherein the sulfur content in the hydroconversion product is 50-200 mg / kg, and the hydroconversion reaction zone is filled with at least two hydroconversion catalyst beds, and the active metal content in the catalysts decreases in sequence along the flow direction. The hydroconversion product containing a certain amount of hydrogen sulfide is used as ethylene raw material, so that the problem of sulfur injection in an ethylene production device can be solved.

The present invention relates to a method for treating plastic pyrolysis oil, comprising the steps of: hydrotreating a feedstock in the presence of hydrogen and a catalyst; separating / washing the hydrotreated effluent in the presence of an aqueous solution; obtaining a first aqueous effluent and a hydrotreated hydrocarbon effluent; separating H2S contained in the first aqueous effluent; obtaining a gas phase containing H2S and a second aqueous effluent; the gas phase containing H2S can be at least partially recycled upstream of step b); separating NH3 contained in the second aqueous effluent; obtaining a gas phase containing NH3 and a third aqueous effluent. The present invention makes it possible to reduce the consumption of sulfurizing agents to maintain the catalyst in sulfide form in a low sulfur content feedstock by recycling the H2S resulting from the method.

The application discloses a conversion method of light naphtha. The method comprises the following steps: (1) mixing light naphtha, optionally added olefins and hydrogen through a hydroconversion reaction zone, and controlling the olefin content in the total feed of the light naphtha and the optionally added olefins to be 1% to 8% of the total feed weight; the hydroconversion reaction zone is filled with a hydroconversion catalyst containing ZSM-5 molecular sieve; (2) the hydroconversion reaction effluent of step (1) enters a high-pressure separator, the obtained hydrogen-rich gas is used as circulating hydrogen, and the liquid phase effluent enters a separation system to obtain ethane, propane and n-butane. The method can increase the proportion of C2-C4 normal alkanes in the hydrogenation product, and reduce the content of by-product methane.

A process for treating a feedstock comprising a pyrolysis oil from plastics and / or tires and / or solid recovered fuels containing halogenated compounds, comprising: a) a hydrotreating step to obtain a partially hydrotreated effluent having a reduced halogenated compound content, b) a separation step, fed by the hydrotreated effluent from step a) and an aqueous solution to obtain a gaseous effluent, an aqueous effluent and a partially hydrotreated hydrocarbon effluent, c) a fluidized bed catalytic cracking or hydrorefining step of a petroleum feedstock and / or a feedstock from biomass conversion in which the partially hydrotreated hydrocarbon effluent is introduced as a co-feedstock without undergoing another hydrotreating step carried out beforehand at higher temperature and / or pressure,the mixture of petroleum feedstock and / or biomass and partially hydrotreated hydrocarbon effluent having a halogenated compound content less than or equal to 10 ppm by weight.

The present invention describes a process for producing at least one kerosene fraction by co-treating a feedstock from a renewable source selected from vegetable or animal oils and fats, or mixtures of such feedstocks, containing triglycerides and / or free fatty acids and / or esters mixed with a fossil feedstock comprising at least one hydroisomerization step of said feedstock in the presence of a bifunctional fixed-bed hydroisomerization catalyst, said catalyst comprising a sulfide phase of at least one metal from Group VIII in combination with at least one metal from Group VIB of the periodic table and a support comprising at least one zeolite selected from IZM-2 zeolites and MTW structural-type zeolites, alone or in mixtures, and at least one binder, said hydroisomerization step being carried out at a temperature between 200°C and 400°C, at a pressure between 1 MPa and 10 MPa,at an hourly spatial velocity between 0.1 and 10 h-1 and in the presence of a total quantity of hydrogen mixed with the feed such that the hydrogen / feed ratio is between 30 and 1500 Nm3 / m3 of feed, then a separation step of the hydroisomerized effluent to obtain at least one kerosene cut.

A process for steam cracking a whole crude including a volatilization step performed to maintain a relatively large hydrocarbon droplet size. The process may include contacting a whole crude with steam to volatilize a portion of the hydrocarbons, wherein the contacting of the hydrocarbon feedstock and steam is conducted at an initial relative velocity of less than 30 m / s, for example. The resulting vapor phase, including volatilized hydrocarbons and steam may then be separated from a liquid phase comprising unvaporized hydrocarbons. The hydrocarbons in the vapor phase may then be forwarded to a steam pyrolysis reactor for steam cracking of the hydrocarbons in the vapor phase.

The application discloses a method for improving the quality of lubricating oil base oil. The method is a hydrocracking process in which a hydrofining reactor and a hydrocracking reactor are connected in series, a hydrocracking catalyst bed and a post-hydrofining catalyst bed are arranged in the hydrocracking reactor, and the method comprises the following steps: feeding a wax oil raw material and hydrogen into the hydrofining reactor, and performing a hydrofining reaction on the raw material and the hydrogen by using the hydrofining catalyst to obtain a hydrofining stream; feeding the hydrofining stream into the hydrocracking reactor, and feeding the material P into the hydrocracking reactor between the hydrocracking catalyst bed and the post-hydrofining catalyst bed; performing air cooling on the obtained product, and performing water injection on the product in the air cooling process so that the material P in the product is carried out of the reaction system by the water phase; and performing separation and fractionation on the oil phase after the air cooling to obtain a tail oil fraction heavier than diesel oil, and using the tail oil fraction as the lubricating oil base oil. The method can improve the quality of the lubricating oil base oil product while ensuring the yield of the lubricating oil base oil in the hydrocracking device.

The invention provides a preparation method of isododecane solvent oil. The preparation method comprises the following steps: 1) removing an oxygen-containing compound from isododecene through an adsorption tank; 2) reacting isododecene with hydrogen in the pre-hydrogenation reactor to remove alkadiene; 3) carrying out hydrodeoxygenation, olefin saturation, aromatic hydrocarbon saturation and other reactions in the hydrofining reactor; and 4) separating the reaction product to obtain a high-purity isododecane solvent naphtha product. The isoparaffin solvent oil obtained by the method is high in yield, high in isoparaffin content and high in isobranching degree. The content of aromatic hydrocarbon, sulfur and nitrogen compounds in the product is extremely low. By arranging the pre-hydrogenation reactor, the coking of the hydrofining reactor is effectively reduced; by arranging the circulating pump, the temperature difference in the reactor is effectively reduced; by arranging the reaction effluent / pre-hydrogenation reaction feeding heat exchanger and the reaction effluent / hydrofining reaction feeding heat exchanger, reaction heat is effectively utilized, arrangement of a reaction feeding heating furnace is omitted, and the operation energy consumption of the device is reduced.

A method for the desulfurization and separation of a catalytic cracking light product includes the steps of: 1) contacting a catalytic cracking light product with a desulfurization adsorbent in an adsorption desulfurization reaction unit in the presence of hydrogen for desulfurization, and optionally carrying out gas-liquid separation on the resulting desulfurization product, to obtain a desulfurized rich gas and a desulfurized crude gasoline, wherein the catalytic cracking light product is an overhead oil-gas fraction from a catalytic cracking fractionator, or a rich gas and a crude gasoline from a catalytic cracking fractionator; and 2) separately sending the desulfurized rich gas and the desulfurized crude gasoline obtained in the step 1) to a catalytic cracking absorption stabilization system for separation, to obtain a desulfurized dry gas, a desulfurized liquefied gas and a desulfurized stabilized gasoline.

A process for treating pyrolysis oil from plastics and / or tires comprising: a) hydrogenating said feedstock to obtain a hydrogenated effluent, b) separating the hydrogenated effluent at a temperature above the precipitation temperature of ammonium halides and at high pressure to obtain a gaseous effluent and a liquid effluent, c) hydrotreating said liquid effluent to obtain a hydrotreated effluent, d) separating the hydrotreated effluent at a temperature above the precipitation temperature of ammonium halides and at high pressure to obtain a gaseous effluent and a liquid effluent, e) separating at a temperature below the precipitation temperature of ammonium halides and at high pressure, fed by the gaseous effluents from steps b) and d) and the liquid effluent from step d) and an aqueous solution, to obtain a gaseous effluent.an aqueous effluent and a hydrocarbon effluent.

The present invention relates to a process for treating a pyrolysis oil from plastics and / or tires comprising: a) hydrogenating said feedstock in the presence of hydrogen and a catalyst to obtain a hydrogenated effluent, b) separating the hydrogenated effluent at a temperature above the precipitation temperature of the ammonium halides formed in step a) and at high pressure to obtain a gaseous effluent and a liquid effluent, c) separating at a temperature below the precipitation temperature and at high pressure and fed by the gaseous effluent and at least a part of the liquid effluent from step b) and an aqueous solution, to obtain at least a gaseous effluent, an aqueous effluent and a hydrocarbon effluent, d) hydrotreating said hydrocarbon effluent in the presence of hydrogen and a catalyst to obtain a hydrotreated effluent.

The invention relates to an apparatus and a process for separating components of a multiphase hydrocarbon stream (27), the apparatus comprising: - an outer vessel (1) having a top end (2) comprising a top outlet (3), a bottom end (4) comprising a bottom outlet (5), with a longitudinal axis (6) extending between the top end (2) and the bottom end (4) and an outer vessel body (7) disposed between the top end (2) and the bottom end (4) and having an outer vessel internal volume (8) in fluid communication with the top outlet (3) and the bottom outlet (5); wherein the outer vessel body (7) comprises: - a first section (9) comprising a tangential inlet (10) arranged to introduce the multiphase hydrocarbon stream (27) tangentially into the outer vessel internal volume (8) to create a vortex flow, and - a second section (11) arranged closer to the bottom end (4) than the first section (9), wherein the outer vessel internal volume (8) has a smaller cross-sectional circumference in the second section (11) than in the first section (9); an inner vessel (15) disposed within the outer vessel body (7), said inner vessel (15) comprising: - an inner vessel body (16) having an inner vessel internal volume (17), and - an inner bottom inlet (18) oriented toward the bottom end (4) of the outer vessel (1) and in fluid communication with the inner vessel internal volume (17) and with the outer vessel internal volume (8); and - a traversing conduit (21) in fluid communication with the inner vessel internal volume (17) and traversing the outer vessel body (7).

The application discloses a method for producing ethylene cracking raw material by hydrocracking. The method is a one-stage series hydrocracking process, which comprises the following steps: a hydrocracking reactor is fed with a hydrocracking feedstock in an upward feeding mode, a material P is introduced into the hydrocracking reactor between a hydrocracking catalyst bed and a post-hydrorefining catalyst bed, the product obtained from the hydrocracking reactor is first subjected to air cooling, the material P in the product is taken out of the reaction system by water phase through the method of water injection in the air cooling device, the oil phase after air cooling is separated and fractionated to obtain light naphtha, heavy naphtha, aviation kerosene, diesel oil and tail oil fraction, and the tail oil fraction is used as the raw material for producing ethylene by steam cracking; the material P is one or more of C23-C35 phenols, aromatic alcohols, aromatic aldehydes, aromatic ketones and aromatic esters. The method can improve the quality of the tail oil product under the condition of producing the tail oil in the hydrocracking device, so as to prolong the operation cycle of the ethylene cracking furnace.

The application discloses a conversion method of hydrocracking light naphtha. The method comprises the following steps: (1) mixing the hydrocracking light naphtha with hydrogen and passing the mixture through a hydroconversion reaction zone to perform a hydroconversion reaction, wherein the hydroconversion reaction zone is filled with at least two hydroconversion catalyst beds, the active metal content of the hydroconversion catalysts decreases in sequence along the flow direction, and the active metal content of the hydroconversion catalysts filled in two adjacent catalyst beds differs by 1-25 percentage points in terms of oxides; (2) the reaction effluent of step (1) enters a separation system to obtain hydrogen-rich gas and a hydroconversion product; and the hydroconversion product comprises C2-C6 alkanes, wherein the mass percentage of the n-alkane yield to the fresh raw material is 0.5-0.7:1. The method can effectively convert isomeric alkanes in the hydrocracking light naphtha into n-alkanes, and improve the ethylene raw material quality.

Processes herein may be used to thermally crack various hydrocarbon feeds, and may eliminate the refinery altogether while making the crude to chemicals process very flexible in terms of crude. In embodiments herein, crude is progressively separated into at least light and heavy fractions. Depending on the quality of the light and heavy fractions, these are routed to one of three upgrading operations, including a fixed bed hydroconversion unit, a fluidized catalytic conversion unit, or a residue hydrocracking unit that may utilize an ebullated bed reactor. Products from the upgrading operations may be used as feed to a steam cracker

The application discloses a processing method of light naphtha. The method comprises the following steps: (1) mixing light naphtha, optionally added olefins and hydrogen through a hydroconversion reaction zone, and controlling the olefin content in the total feed of the light naphtha and the optionally added olefins to be 1% to 8% of the total feed weight; (2) the hydroconversion reaction zone effluent of step (1) enters a separation system, and hydrogen and a hydroconversion product are obtained through separation. The method uses light naphtha as a raw material, can effectively convert isomeric alkanes in the light naphtha into normal alkanes, and improves the ethylene raw material quality.

The present invention relates to a three-phase reactor for the reaction of a hydrocarbon feedstock with hydrogen and a hydroconversion process, for example of the H-Oil™ type, implementing it, comprising a vessel (10) with an upper end (48) and a gas / liquid separation device comprising: - a recycle cup (30), above the catalytic reaction zone and delimiting with the upper end (48) a recycle zone (39), comprising a cylindrical upper part (42) extended by a lower part of decreasing cross-section and variable angle of inclination (43), provided with vertical conduits (27) for the passage of a gas / liquid mixture from a catalytic reaction zone, and having a fixed angle of inclination β between 50° and 85° with respect to the axis (Z) of the cylindrical part (42), - a recycle line (25) for the liquid at the apex of the lower part,in fluidic communication with the lower end of the enclosure by means of recirculation. Figure 2 to be published.

The utility model provides an olefin hydrogenation saturation system in pentane oil components. The olefin hydrogenation saturation system comprises a hydrogen inlet pipeline and a pentane oil feeding pipeline, a pentane oil feeding pipeline is connected to a hydrogenation reactor, and a C4 raw material buffer tank, a hydrogenation feeding pump, a start-up heater and a raw material oil heat exchanger are sequentially connected to the pentane oil feeding pipeline; the hydrogen inlet pipeline is connected to the pentane oil feeding pipeline, and the hydrogen inlet pipeline is arranged between the start-up heater and the raw oil heat exchanger; an outlet of the hydrogenation reactor is connected to the deisobutanizer through a hydrogenated product discharging pipeline; a tower bottom outlet of the deisobutanizer is connected to a normal isomerization device through an alkylated oil pipeline; the alkylated oil pipeline is sequentially connected with an alkylated oil separation tower air cooler, an alkylated oil separation tower return tank, a refrigerant circulating pump and a light alkylated oil cooler; the problem that the bromine index in normal and isomeric products exceeds the standard due to the fact that the olefin content in the components of the reformed pentane oil is too high can be solved.

The utility model discloses a small coal tar hydrogenation product separation device, and relates to the technical field of hydrotreatment. The small coal tar hydrogenation product separation device comprises a supporting assembly, the supporting assembly comprises a supporting plate, the top of the supporting plate is fixedly connected with a first supporting plate, the top of the first supporting plate is fixedly connected with a connecting ring, the top of the connecting ring is fixedly connected with a second supporting plate, and the top of the second supporting plate is provided with a reaction assembly. The reaction assembly comprises a mixing box, the mixing box is fixedly connected to the top of the second supporting plate, according to the small coal tar hydrogenation product separation device, the motor is started to enable the output end of the motor to drive a rotating shaft to rotate, the rotating shaft rotates to drive spiral stirring blades to rotate, and internal substances are evenly mixed through the spiral stirring blades; in addition, the temperature rise of the spiral heating pipe is controlled through the controller, uniform preheating treatment of the coal tar is achieved, and the preheating efficiency is improved.

The application discloses a hydrocracking method for improving the quality of heavy naphtha. The method comprises the following steps: (1) feeding a wax oil raw material and hydrogen into a hydrofining reactor, and reacting with a hydrofining catalyst to obtain a hydrofining stream; (2) feeding the hydrofining stream into a hydrocracking reactor, and separating and fractionating the obtained product to obtain heavy naphtha and the like; wherein a hydrocracking catalyst bed is arranged at the upstream of the hydrocracking reactor, and a post-hydrofining catalyst bed is arranged at the downstream of the hydrocracking reactor; a material P is introduced between the hydrocracking catalyst bed and the post-hydrofining catalyst bed, the material P is one or more of C7-C11 olefin alcohol, olefin aldehyde, acetylene alcohol and acetylene aldehyde; and an air cooling device is arranged before fractionation of the obtained product, wherein the air cooling device is water injected so that the material P in the product is taken out of the reaction system by the water phase. The method can improve the bromine index of the heavy naphtha without changing the distribution and yield of the hydrocracking product.