16results about "Hydrotreatment operations starting-up" patented technology

A heat exchange assembly for hydrogenation of diesel and wax oil, and a hydrogenation system. The heat exchange assembly comprises: a first heat exchanger, wherein an inlet of a first heat medium passage of the first heat exchanger is used for inputting a first-stage reaction effluent, an inlet of a first cold medium passage of the first heat exchanger is used for inputting a first-stage reaction influent, and an outlet of the first cold medium passage of the first heat exchanger is used for outputting the first-stage reaction influent having undergone heat exchange; a second heat exchanger, wherein an inlet of a second heat medium passage of the second heat exchanger is communicated with an outlet of the first heat medium passage, an outlet of the second heat medium passage of the second heat exchanger is used for being communicated with an inlet of a hot high-pressure separation tank, and an inlet of a second cold medium passage of the second heat exchanger is used for inputting a stripping tower bottom liquid; a third heat exchanger, wherein an inlet of a third heat medium passage of the third heat exchanger is used for inputting a second-stage reaction effluent, an inlet of a third cold medium passage of the third heat exchanger is communicated with an outlet of the second cold medium passage, and an outlet of the third cold medium passage of the third heat exchanger is used for being communicated with a downstream apparatus; and a fourth heat exchanger. Compared with the prior art, the present invention can reduce apparatus investment, and improve heat exchange efficiency.

The invention relates to the technical field of light oil gasification, in particular to a gasification device for hydrogen-doped gasification of light oil, comprising: a gasification module for mixing and reacting hydrogen and light oil to output gaseous fuel gas; a detection module, comprising a pressure sensor which is arranged in the gasification tank and is used for detecting the pressure in the gasification tank, and a liquid level meter which is arranged in the gasification tank and is used for detecting the liquid level height of light oil, the temperature sensor is arranged in the gasification tank and is used for detecting the temperature in the gasification tank; the flow meter is arranged below the oil drain valve and is used for detecting the discharge flow rate of the waste oil; and the control module is used for determining the liquid level height in the gasification tank according to the fluctuation amplitude of the pressure in the gasification tank, or determining the feeding flow of the light oil according to the average flow velocity of the waste oil and determining the feeding pressure of the hydrogen according to the temperature rise rate in the gasification tank. The operation stability of the gasification device is improved.

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 invention discloses a gasoline hydrogenation process start-up method which comprises the following steps: (1) in a gasoline hydrogenation reactor, sequentially arranging 1-n hydrofining catalyst bed layers from a raw oil inlet to a raw oil outlet, and filling sulfurized hydrofining catalysts in the hydrofining catalyst bed layers; (2) increasing the temperature of the reactor to a passivation temperature, introducing gasoline and hydrogen carrier mixed oil from a raw oil inlet, carrying out passivation treatment, introducing cold oil or cold hydrogen at an inlet of the (2-n) th bed layer in the passivation treatment process, controlling the temperature of the inlet of each bed layer, and carrying out passivation treatment for 0.5-2 hours; (3) after passivating treatment is finished, introducing a hydrogen carrier from a raw oil inlet, and carrying out activity recovery treatment; and (4) switching the raw oil, and carrying out gasoline hydrogenation reaction to produce a qualified product. According to the method, passivation, activity recovery and bed temperature rise are combined, and excessive loss of catalyst activity is avoided during passivation, so that the operation cycle of a device is prolonged.

This invention relates to the field of light oil gasification technology, and more particularly to a gasification device for light oil hydrogen-blended gasification, comprising: a gasification module for mixing hydrogen and light oil to produce gaseous fuel gas; a detection module including a pressure sensor disposed inside the gasification tank to detect the internal pressure, a level gauge disposed inside the gasification tank to detect the liquid level of the light oil, a temperature sensor disposed inside the gasification tank to detect the internal temperature, and a flow meter disposed below the drain valve to detect the discharge velocity of waste oil; and a control module for determining the liquid level in the gasification tank based on the fluctuation range of the internal pressure, or determining the feed flow rate of the light oil based on the average flow velocity of the waste oil, and determining the feed pressure of hydrogen based on the rate of temperature rise in the gasification tank. This invention improves the operational stability of the gasification device.

The present invention relates to the technical field of catalyst start-up, and discloses a start-up method of a hydrocracking unit, the method comprising: (1) loading a hydrocracking catalyst in a reaction bed of a hydrocracking unit; (2) introducing hydrogen into a reaction bed loaded with the hydrocracking catalyst, heating the reaction bed temperature to 100-140°C, then introducing a diesel fraction and optionally a vegetable oil to wet the reaction bed, and establishing a closed loop; (3) continuing to heat the reaction bed temperature described in step (2) to 300-350°C, then switching the feedstock oil, continuing to heat up to the hydrocracking reaction temperature, and the hydrocracking catalyst is an ammonia passivated sulfurized state hydrocracking catalyst. The method has the advantages of simple start-up process, safe, stable and environmentally friendly start-up process, and effectively avoiding the potential risks of injecting a vulcanizing agent and a passivating agent.

The invention discloses a reformate hydrogenation start-up method using a Pt-Pd bimetallic catalyst, which comprises the following steps: (1) at a certain temperature and in a hydrogen atmosphere, introducing a passivator and a solvent into a catalyst bed layer in a fixed bed reactor, and carrying out low-temperature passivation treatment; wherein a reduced Pt-Pd bimetallic catalyst is arranged in the catalyst bed layer; (2) after the low-temperature passivation treatment is finished, stopping feeding the passivator and the solvent, introducing a certain amount of adsorption gas, and carrying out high-temperature passivation treatment; (3) after the high-temperature passivation treatment is finished, stopping feeding the adsorption gas, and introducing a solvent to treat a catalyst bed layer; and (4) switching the raw oil to produce a qualified product. According to the method, bimetal is moderately passivated through low-temperature liquid vulcanization, high-temperature competitive adsorption and the like, the synergistic effect of the bimetal is protected, and aromatic hydrocarbon saturation loss of the catalyst during normal use is effectively avoided.

The invention discloses a diesel hydrogenation process start-up method which comprises the following steps: (1) keeping a hydrogenation reactor at a certain temperature, introducing secondary processing diesel and a hydrogen carrier into a sulfurized diesel hydrogenation catalyst bed layer, and after penetrating through the catalyst bed layer, raising the temperature of the reactor for passivating treatment; (2) after passivation is finished, a hydrogen carrier is introduced into the catalyst bed layer, and recovery treatment is carried out after penetration; and (3) switching the raw oil to produce a qualified product. The method can quickly stabilize the catalyst, so that the device can enter normal production, and meanwhile, the initial activity of the catalyst is prevented from being obviously reduced due to excessive carbon deposition.

The present invention relates to a composite startup catalyst, characterized in that, based on the dry weight of the composite startup catalyst, the composite startup catalyst comprises: 15-95% by weight of a component A catalyst selected from a catalytic pyrolysis or catalytic cracking equilibrium catalyst and / or a treated catalytic pyrolysis or catalytic cracking equilibrium catalyst, wherein the treatment comprises demetallization treatment and / or particle size adjustment treatment; 5-85% by weight of a component B catalyst selected from one or more fresh catalytic pyrolysis catalysts or catalytic cracking catalysts; and optionally a component C catalyst, wherein the component C catalyst contains 2-10% by weight of a modified metal oxide. The present invention also relates to a preparation method for the composite startup catalyst, a use of the composite startup catalyst in startup of a catalytic pyrolysis or catalytic cracking device, and a startup method for a catalytic pyrolysis or catalytic cracking device.

Embodiments of the present disclosure generally relate to methods and systems for purifying hydrocarbons, such as feedstock hydrocarbons containing one or more contaminants. In one or more embodiments, a method of purifying a hydrocarbon is provided and includes flowing a feedstock hydrocarbon stream through a heating unit, then combining the hydrocarbon stream and a primary solvent in a laminar flow reactor to produce a hydrocarbon-solvent stream, flowing the hydrocarbon-solvent stream through a cooling unit, and introducing the hydrocarbon- solvent stream into a separation unit to produce a scrubbed hydrocarbon stream and a solvent stream. The scrubbed hydrocarbon stream has a final contaminant concentration which is less than the initial contaminant concentration. The methods and systems for purifying hydrocarbons may be used to prepare a purified hydrocarbon product having the contaminant reduced by 10 times, about 40 times, about 100 times, or greater compared to the feedstock hydrocarbons.

The present invention relates to the technical field of hydrocracking, and discloses a method for starting a cracking unit. The method includes: (1) loading an ammonia-passivated sulfided hydrocracking catalyst into a reaction zone of a hydrocracking unit; (2) in the presence of hydrogen, heating the catalyst bed temperature to 140-180°C, then introducing kerosene fractions and optionally vegetable oil and secondary processed gasoline to wet the catalyst bed, and establishing a closed loop; (3) continuing to heat the catalyst bed temperature described in step (2) to 260-320°C, then replacing the feedstock oil, continuing to heat to the reaction temperature, and switching to production. The method provided by the present invention has a simple start-up process and can effectively improve the yield of BTX in the product.

The heat exchange assembly comprises a first heat exchanger, a second heat exchanger, a third heat exchanger, and a fourth heat exchanger. An inlet of a first hot medium passage is used for importing a first-stage reacting product, an inlet of a first cold medium passage is used for importing a first-stage reacting feedstock, and an outlet of the first cold medium passage is used for exporting the first-stage reacting feedstock after heat exchange. An inlet of a second hot medium passage communicates with an outlet of the first hot medium passage, an outlet of the second hot medium passage communicates with an inlet of a hot high separation tank, and an inlet of a second cold medium passage is used for importing bottom liquid of a stripping tower.

The invention relates to a petrochemical production process, and discloses a fluidized bed-fixed bed system and a starting method. The fluidized bed-fixed bed system comprises a reaction unit, the reaction unit comprises a fluidized bed reactor and a fixed bed reactor which are communicated with each other, and the starting method comprises the following steps: 1) filling the reaction unit with a catalyst; (2) introducing inert gas into the reaction unit in the step (1) to replace air, and after the replacement is qualified, continuously introducing the inert gas to carry out pressure boosting air tightness on the reaction unit; (3) introducing hydrogen to carry out pressure-boosting airtight and synchronous heating on the reaction unit until the pressure is boosted to the operation pressure and the airtight is qualified; 4) feeding start-up oil into the reaction unit, and flushing the catalyst bed layer; and (5) vulcanizing the catalyst in the reaction unit which is qualified after flushing in the step (4), and after the vulcanization is completed, feeding raw oil, thereby completing the start-up of the fluidized bed-fixed bed system. The method has the advantages of being safe, reliable and high in operability.

The present invention discloses a method for starting up an ebullated bed hydroprocessing unit. The ebullated bed hydroprocessing unit uses at least one ebullated bed hydrogenation reactor. The method includes catalyst loading and screen installation, airtightness, catalyst presulfurization, and feedstock switching. The catalyst loading and screen installation includes: installing a first screen made of a material with a melting point of 50 to 100°C at the bottom of the reactor; loading the hydrogenation catalyst into the reactor from the top of the reactor; installing a second screen made of a material with a melting point of 150 to 200°C close to the catalyst loading surface; and then installing a third screen made of a material with a melting point 2 to 15°C lower than the initial temperature of the reactor under normal operating conditions at a distance of 100 to 500 mm from the catalyst loading surface. The method of the present invention solves the effects of bed fluctuations caused by distributor blockage during the catalyst loading stage, catalyst loss during the airtightness stage, and changes in the sulfiding medium during the presulfidation stage. As the start-up temperature rises, the screens melt in sequence and are carried out with the liquid phase, significantly shortening the start-up time of the unit.

Embodiments of the present disclosure generally relate to methods and systems for purifying hydrocarbons, such as feedstock hydrocarbons containing one or more contaminants. In one or more embodiments, a method of purifying a hydrocarbon is provided and includes flowing a feedstock hydrocarbon stream through a heating unit, then combining the hydrocarbon stream and a primary solvent in a laminar flow reactor to produce a hydrocarbon-solvent stream, flowing the hydrocarbon-solvent stream through a cooling unit, and introducing the hydrocarbon-solvent stream into a separation unit to produce a scrubbed hydrocarbon stream and a solvent stream. The scrubbed hydrocarbon stream has a final contaminant concentration which is less than the initial contaminant concentration. The methods and systems for purifying hydrocarbons may be used to prepare a purified hydrocarbon product having the contaminant reduced by 10 times, about 40 times, about 100 times, or greater compared to the feedstock hydrocarbons.

The present application belongs to the technical field of polyolefin catalytic conversion, and relates to a process for preparing naphtha by polyolefin hydrocracking. In a closed state, hydrogen is dispersed into micro-bubbles by a membrane tube and then enters polyolefin in a molten state, and a hydrocracking reaction is carried out under the action of a catalyst. A Ni / Beta catalyst is used, and the polyolefin and the Ni / Beta catalyst are filled in the reaction kettle in the form of mixed fillers. The reaction product is continuously produced and separated into gas and liquid, and the liquid product is subjected to fractionation to obtain liquefied petroleum gas and naphtha.