WO2011005145A1 - Procédé de séparation de systèmes hétérogènes liquides et gazeux, et colonne de fractionnement mécano-thermo-chimique pour sa mise en œuvre - Google Patents

Procédé de séparation de systèmes hétérogènes liquides et gazeux, et colonne de fractionnement mécano-thermo-chimique pour sa mise en œuvre Download PDF

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Publication number
WO2011005145A1
WO2011005145A1 PCT/RU2010/000296 RU2010000296W WO2011005145A1 WO 2011005145 A1 WO2011005145 A1 WO 2011005145A1 RU 2010000296 W RU2010000296 W RU 2010000296W WO 2011005145 A1 WO2011005145 A1 WO 2011005145A1
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WO
WIPO (PCT)
Prior art keywords
mixture
cells
cavity
shelf
gas
Prior art date
Application number
PCT/RU2010/000296
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English (en)
Russian (ru)
Inventor
Василий Иванович РЕВА
Original Assignee
Reva Vasilij Ivanovich
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Publication date
Application filed by Reva Vasilij Ivanovich filed Critical Reva Vasilij Ivanovich
Publication of WO2011005145A1 publication Critical patent/WO2011005145A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/505—Screws
    • B29C48/56—Screws having grooves or cavities other than the thread or the channel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/505—Screws
    • B29C48/565—Screws having projections other than the thread, e.g. pins
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/505—Screws
    • B29C48/63—Screws having sections without mixing elements or threads, i.e. having cylinder shaped sections
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/68—Barrels or cylinders
    • B29C48/685—Barrels or cylinders characterised by their inner surfaces, e.g. having grooves, projections or threads
    • B29C48/686—Barrels or cylinders characterised by their inner surfaces, e.g. having grooves, projections or threads having grooves or cavities
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/695—Flow dividers, e.g. breaker plates
    • B29C48/70—Flow dividers, e.g. breaker plates comprising means for dividing, distributing and recombining melt flows
    • B29C48/71—Flow dividers, e.g. breaker plates comprising means for dividing, distributing and recombining melt flows for layer multiplication
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/505—Screws
    • B29C48/59—Screws characterised by details of the thread, i.e. the shape of a single thread of the material-feeding screw
    • B29C48/60—Thread tops
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
    • B29C48/50—Details of extruders
    • B29C48/505—Screws
    • B29C48/64—Screws with two or more threads
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4081—Recycling aspects

Definitions

  • the invention relates to methods for producing clarified products from petroleum feedstocks as motor fuel, organic binders and lubricating oils, functional and semi-functional applications.
  • the invention also relates to devices for fractional separation of petroleum products according to the critical critical properties of materials in a destructive chemical manner.
  • a known method of producing a destructive material and a worm-disk extruder to obtain a product (RU M> 2159179, publ. 20.11.2000).
  • the method includes the destruction of high molecular weight compounds (VIS), which are in the melt, in the disk nozzle by mechanical and thermal effects on the high molecular weight compound, prior to the destruction of the high molecular weight compounds in the disk nozzle, their preliminary destruction in the screw extruder is carried out, and the high molecular weight compounds in the disk nozzle are destroyed, melt temperature equal to or lower than at the exit of the screw extruder.
  • VIS high molecular weight compounds
  • the disadvantage of this method is the duration of the process, as well as the inability to use to accelerate the process of surface-active substances (surfactants) and separation material by fractions.
  • the device used consists of two devices, in one of which the IUD is subjected to preliminary destruction, and in the second device, the final destruction is performed, which reduces the efficiency of the destruction processes and does not allow the effective management of the destruction process.
  • the known technical solution does not provide the necessary set of technological processes for the separation of raw materials into fractions, due to its single-speed rotation of the shaft along the entire length of the device, the melt does not release low-boiling fractions of the gases of the first stage and light products when moving along the channels of the structure, which causes the melt to send to the surface of the cooled cylinder and additional costs for the separation of the melt into fractions in the columns of circulation and requires the use of many blades remote from the inside cylinder surface. Disclosure of invention
  • the objective of the invention is to develop a method and device to reduce energy consumption and metal consumption, separation in a single apparatus of a heterogeneous system into separately functional products, by mechanothermothermic exposure using catalysts and increasing the ratio of hydrogen to carbon (N / C) at each stage of the process, in order to obtain purified high-quality product, which relates to the physical stages of processing of raw materials, and through the recycling of boiling and high boiling fractions, make a deep separation Leniye molecules and obtain a high quality distillate fuels and motor oils, which relates to chemical processing of materials at elevated local temperatures and local pressure in the device thin channels.
  • the proposed method for producing the product involves the phased destruction of macromolecular compounds with the aim of local redistribution of hydrogen between the hydrocarbon molecules in the starting material in each accelerating unit, by means of mechanothermochemical effects using catalysts and donor hydrogen.
  • the mechanothermal effect on the group composition of the material increases the density according to the extremely critical properties of each fraction.
  • hydrocarbons decompose into components due to the active penetration of the gas-vapor composition into the mixture due to the shaft rotation speed and formation of partial pressure.
  • Preliminary destruction begins to be carried out at the entrance to the conical cavity of the device at a boiling point (T.V.) of a light gaseous fraction with a low molecular weight.
  • T.V. boiling point
  • a decrease in viscosity and an increase in the density of oil in the cylindrical part of the device allows mixing with a solution of alkali and steam, which ensures desulfurization of the material at a preliminary stage of the process.
  • Distinctive features of the proposed method is that at stage I, before separation of the fractions, the starting material is preheated by a screw device with the simultaneous formation of gas bubbles and partial increasing pressure at the top of the conical worm device, and the destruction of the material is carried out from surface friction from a screw groove interacting with a screw groove in a cone-shaped sleeve, triangular activators located on the falling side of the screw spiral, from compression compression at the top of the cone and from the action of the heating medium warming up the core and details of the conical shaft, which rotates from the drive with a speed equal to or less than the 2nd screw shaft.
  • the material undergoes preliminary degradation with the release of a gas-vapor component with a boiling point up to 60 C and higher.
  • partially destructible material is supplied through the conical openings of the unregulated disk die to the cylindrical riser body, undergoes a complex stress shift in the material movement cavity, and is mixed with alkali solution and other required agents.
  • wedge-shaped activators the side surface of which is made in the form of a wave, and the back part is made with a semi-arc sampling, they create a bubble loop and actively mix the gas-vapor component with the liquid fraction, while additional generation of a light vapor-gas fraction occurs, the gas density, temperature and desulfurization of the material increase .
  • the degraded material up to 100 ° C is fed into the screw cavity of the reactor, where due to the helical grooves in the sleeve, the converted substance is filled and unloaded from the evaporation cells located on the worm helix into the cavity.
  • the sleeve is made with slotted diffusion slots such as unloading a gas-vapor mixture with a boiling point up to 100 ° C.
  • Slotted slots of the gas-vapor discharge are made with an inclination along the rotation of the catalyst around the cylindrical sleeve, and the catalyst, when rotating in the cavity around the sleeve, constantly restores its properties due to the internal comb on the reactor vessel, where forced processes take place collisions of catalyst particles between themselves and the surface of the comb wall of the housing, in addition, a special agent can be supplied through the pipeline to restore the properties in the catalyst.
  • the resulting gas-vapor mixture tends from high pressure in the reactor cavity to a fractionation column with lower pressure, where the vapor-gas mixture partially condenses through the float valves in the valve plate fluid, with each fraction condensing on its own plate, the lightest fractions rise up, the heaviest fraction through the lower overflow pipe fed into the cavity of the riser body for recycling
  • the remaining mixture with a certain density and the boiling range of the fraction is directed along the screw channels, fills the cells in the sleeve and the worm spiral, in the booster block, where due to the rotation of the screw, the mechanical energy of the material in the contact areas heats up, and the compression compresses the material between two cells, additionally allocates temperature and gas-vapor mixture, which is released from the cells, is evenly distributed in the relaxation system.
  • the relaxation of the stress field occurs by heat generation, the formation of new surfaces and excitation selection of the gasoline fraction by microchemical synthesis reactions in the liquid phase.
  • the main goal of mechanothermal synthesis is to initiate microchemical reactions of molecular cleavage in the liquid phase with the evolution of a gas-vapor fraction of 90 ° - 220 ° C and diffuse saturated vapor and gas into the annular cavity of the reactor through a lateral slotted slots of the discharge onto a rotating fluidized catalyst.
  • the gas-vapor mixture is transferred to a separation column, where all processes are carried out in the likeness of the second stage.
  • the remaining mixture of a certain density and with a boiling point of 220 ° - 315 0 C and higher is moved by a screw spiral to the naphtha (ligrein) fractionation reactor, where in a cylindrical cavity the viscous material is mixed with donor hydrogen-containing gases.
  • the reaction of hydrocarbons with hydrogen is associated with a redistribution of hydrogen between molecules and leads to an increase in the H / C ratio in processed products.
  • Selective gas-vapor fractions diffuse onto the rotating catalyst through lateral slotted slots with a directed discharge angle under high pressure.
  • the mixture is enriched with hydrogen and through the filter enters the cavity of the separation column, where product is taken from the first and subsequent plates through the side unloadings, while the heavy fraction is fed through the discharge pipe into the cavity of the booster unit for recycling.
  • 315-450 C and higher is moved by a helical spiral to the reactor "fractionation of kerosene" along the accelerating block enriched with donor hydrogen, increases the temperature due to the local thermochemical reaction (synthesis) that occurs in the filled cells of the sleeve and the helix, while the vapor-gas mixture is additionally released to produce new surfaces with ion implantation of hydrogen in the bulk of the material, which further increases pressure and temperature .
  • the material entering the reactor is mixed by wedge-shaped activators, and the formed saturated gas-vapor fraction with a boiling point of 315-450 ° C under pressure and high speed diffuses through the lateral slit-like discharge into the annular cavity on the rotating catalyst, it condenses into saturated vapor, where the catalyst additionally acts to the incoming fraction and through the filter, the fraction enters the cavity of the separation column, where, according to the known scheme, it moves along the bubble trays and through the side selects manual ultrasonic inspection of the finished product and the heavy fraction through the overflow pipes is returned to the booster cavity.
  • thermochemical processes of separation and conversion of the residue into distillate fuel with a boiling point of 450 - 550 0 C (heavy gas oil) with a boiling point are carried out 550-700 0 C (Catholic cracking) - residue with a boiling point of 700-750 0 C (straight run) with T.V. 750-800 0 C (coking of oil residue) with T.V.
  • the heat removal from the material being decomposed through the structural elements of the device leads to a decrease in temperature to the temperature of the fraction at each stage.
  • a decrease in viscosity with heat removal allows to obtain a low molecular weight product from a high molecular weight composition than without heat removal, the required depth of degradation of the resulting product at all stages of the process depends on the complex composition of the remaining mixture.
  • the mechanothermochemical fractionator contains a cone-shaped body with an internal screw groove, step
  • the shaft end includes a landing hole for the neck of the oncoming shaft, while on the other hand, a riser body, a reactor block with a separation column with a boiling point fraction up to 90 ° C, an accelerating block, are connected in series
  • the shelf reactor for the multi-temperature destruction of high molecular weight compounds is driven into rotation from an external drive at a shaft rotation speed greater than the rotation speed of the shortened conical shaft.
  • Distinctive features of the claimed device is that the shortened housing and the feed shaft are conical with an axial cavity for the coolant to function, and the worm cut on the surface contains a deep groove, the pitch and volume of which corresponds to the pitch and volume of the groove made on the helical spiral cone shaft with rotation wedge-shaped activators with a wavy surface, and a shortened conical shaft is contained in a conical sleeve with a groove and a conical body with an external system heat transfer medium, and the volume of the inter-screw cavity of the apex of the screw is not less than 2 times less than the volume at the entrance to the housing, which is equal to a ratio of at least 2 to 1 or more.
  • the end of the shaft is centered by a die with tapered floor holes.
  • wedge-shaped activators are installed on the rotation shaft, moreover, the activators are made with a wavy surface with a step of 3 to 1 or more and a semi-cast sample from 2 to 10 mm at the base of the wedge, which allows the selection of the gas-vapor fraction with a low boiling point at the preliminary stage.
  • the successively connected units for fraction fraction distillation are capable of degrading the mixture at each stage to its maximum boiling point.
  • the reactors are capable of passing under pressure a corresponding fraction from a cylindrical cavity through directional slots at a scattering angle relative to the horizon of 20 ° or more with a clearance of 0.02 or more onto the catalyst rotating around the sleeve in a suspended state.
  • the catalyst acts on the fraction under conditions of rotation, which significantly increases its reactivity, the reacted product entering the cavity of the valve fractionator (separation column) is taken through side unloadings in the column body.
  • a sequentially connected shelf reactor is capable of rotating at least one comb disk by means of a shaft between the shelves of another shelf disk, the other shelf disk being fixed motionless and the combs are asymmetrically with end grooves and the possibility of mechanical cracking of the material to a molecular state with effusion exhaustion with lower temperature and reaction process.
  • the device is based on a combined shaft passing through all the cavities of the booster blocks and reactors, which is made in the form of a screw spiral with gaps in the area of the separation column, which contains wedge-shaped activators, and the screw spiral in the acceleration zone, it is made with evaporation cells and cells containing purge channels directed to the shaft surface, and wedge-shaped activators are made with a wavy surface and evaporation cells in the screw breaks.
  • Accelerating blocks contain cylindrical liners, the inner surface of which is made corresponding
  • compression compression cells performing the functions of stores for cells made on a screw spiral.
  • the sleeves contained in the reactor blocks are made with diffusion slots and screw grooves, which serve as stores for evaporation cells located on the surface of wedge-shaped activators with a wavy side surface.
  • the evaporation cells on the surface of the worm spiral (screw) are filled with a mixture of reciprocal cells in the body of the sleeve, and the evaporation cells are unloaded into the gap between the parts at a high speed of rotation when the cells are aligned, and a gas-hydrodynamic microwave occurs in a local confined space of a spherical type.
  • the kinetic energy of the particles of the material additionally generates a gas-vapor fraction, and when it expires, the gas-vapor composition of the boundary material is saturated, which It was placed in a cavity wedge activators.
  • the gas-vapor composition evenly spreads in the liquid fraction, including filling the helical grooves in the reactor sleeves, from where the activator cells are filled with selected components and delivered to the lumen (gap) to the diffusion slots, through which the gas-vapor fraction throttles into the annular cavity with more low pressure and the catalyst contained in it, and the catalyst constantly rotates around the liner of the reactor is in a dry state.
  • the shelf reactor is based on the annular shelves of a rotating disk with transverse slots of the diffusion type and the annular shelves of the fixed disk, which form channels (gaps) between them that can during the rotation of one of the disks cause cavitation and displacement of microscopic bubbles from the liquid phase, forming the effect of “mechanically” cracking ”and synthesis of viscous material in thin films at high local pressure, which increases in proportion to the radial speed and distance from the center of rotation, while became viscous material liquefies agent and alternately supplied through the transverse slit throttles rotating shelves selektsioniruet gas-vapor mixture of defined composition according to the limiting temperature boiling fraction and the distance from the axis of rotation.
  • the high molecular weight connection from the loading pipe enters the cavity of the cone-shaped body, is captured by a worm conical thread and fed into the conical cavity, where it partially receives temperature from the preheated surface of the device parts, and is subjected to mechanical cracking using screw grooves in the cone sleeve and the surface of the worm spiral , as well as the effect of wedge-like activators of the material, partially improving the viscosity properties with the release of light vapor and gas second mixture that lends itself to local pressure by reducing the volume of conical cavity, 2 to 1, and the conical shaft is made hollow and contains movable pistons address temperature control.
  • the riser cavity destructive acceleration compartment
  • the back contains a semicircular sampling, which creates a constant collapse loop, due to which the mixture continues to warm up and effectively see deal with donor agents through feed channels.
  • the liquefied mixture is captured by worm cutting and transported to the reactor block, the cavity of which contains a sleeve with side slots for throttling the vapor-gas mixture at the molecular level, a screw sample in the sleeve for loading the mixture into the worm's evaporation cells.
  • the riser casing, the reactor casing and the fractionator are equipped with a jacket with the possibility of functioning of the coolant.
  • the fluidized catalyst located in the annular cavity of the reactor operates with the possibility of rotation around the sleeve recovery (regeneration) of its own properties, which are carried out due to the supplied hydrogen, steam and performed braking combs on the opposite side of the reactor vessel from slot discharge, where catalyst particles may collide with each other and with the surface of the combs, discharges carbon.
  • Carbon under the influence of hydrogen forms a hydrocarbon gas (or, without access of hydrogen, turns into dioxide of monoxide), which, together with saturated vapors of the light fraction, is lifted through a filter into a butane separation column onto a plate float valve, where gas conversion processes take place.
  • the valve plate is provided with openings with float valves installed in them.
  • the remaining mixture with a boiling point of 90 0 C and above, with a worm spiral through adjustable conical holes of the die moves into the next cylindrical accelerating block, where the sleeve is made with cells, like a worm spiral, which are instantly and constantly filled with a liquid mixture and serve as a store for filling evaporative cells made on a worm spiral.
  • the mixture moves through the conical openings of the die under the mechanical action of a spiral into the mixing mixing zone with a boiling range of 90 - 220 C and higher, which is affected by wedge-shaped activators with cells in the end part that is in contact with a sleeve with screw selection and slotted lateral discharge of the gas-vapor mixture, unloading occurs on a rotating catalyst in a fluidized state, and if in the mixing cavity there is not enough pressure to extrude the gas-vapor mixture, a slide shutter is produced e conical holes in the die until the desired temperature and pressure in the reactor cavity are set.
  • the gas-vapor mixture interacts with the rotating catalyst and tends through the filter to the cavity of the separation column, where the valve plate senses the vapor pressure, rises and passes the mixture into the lower compartment of the bubble bath (plate), heavy molecules settle in the liquid (condensate) environment and through lateral discharge are sent to the booster unit for reprocessing, and the lungs rise up through the next float valve, the next compartment of the bubbler plate is also filled with liquid (okol about 10 cm), which allows the product to be separated, the heavier product remains in the liquid, and the light one rises in the next bubbler plate.
  • the lightest gas-vapor fractions through the upper valve go to the gas fractionation unit (HFC), if it is advisable by the technology of chemical processes. Processing of high molecular weight raw materials with boiling limits of 220 -315 0 C and 315 -450 0 C occurs according to the scheme of technology for processing high molecular weight raw materials with a boiling range of 90 -220 0 C.
  • the separation of products in a shelf-connected reactor connected in series is carried out by creating active aerodynamic frictional friction in the thin channels of the device of the distributed material in the form of a film and cavitation of microscopic bubbles, causing breaks in surface stresses and the formation of new surfaces with increasing local temperature and pressure in each channel, and the further from the axis of rotation, the higher the force of impact on the material and the speed of receipt of the product.
  • a high molecular weight mixture with a boiling point of 450 0 C and higher enters from the shaft rotation center through rotating conical holes into a thin annular cavity, where under pressure it penetrates into the second row of the annular shelf into the slotted slots, the prism-like slot being directed from the center to the periphery, this allows to form breaks in the surface stresses of the substance with the formation of selective gases and to distribute the viscous mixture evenly with a thin layer on the surface of a rotating annular shelf (comb), and form a space between them, a heavy fraction with a boiling point of 550 0 C and above is pressed against the body of the shelf under the action of centrifugal forces, and lighter saturated gases are squeezed onto the surface of the material and are collected in the semicircular cavity of the shelf located at the bottom of the fixed disk and under pressure tend towards lower pressure to lateral discharge of “distillate” fuel ”to the condenser.
  • a pipeline for supplying a reagent (or other agents) is made in order to accelerate the
  • the thin channels between themselves are sealed with a ring.
  • the remaining mixture with a boiling range of 550 -700 C and above moves to the next thin U-shaped channel, where the material is distributed with a thinner film than in the previous channel, the heavier, more viscous material due to centrifugal forces and local pressure, it is pressed against the body of the rotating annular shelf, and the light gas fraction in the form of microscopic bubbles is displaced onto the surface of the material and enters into thin channels smallness fixed shelves where moves toward the annular lower pressure side to generate unloading "tyazhelogo gazoylya" on storage.
  • a reagent (hydrogen) or other agents are fed through the corresponding pipeline in the upper part of the channel, which contribute to the technological process of instant fraction separation in thin films of a substance.
  • a reagent (hydrogen) is supplied through the corresponding pipeline in the lower part of the channel, which contributes to the technological process of instant reaction separation in thin films of the substance.
  • the heavier fraction with a boiling point of 750-800 ⁇ and higher under the action of centrifugal forces and local pressure moves to the next thin cavity of “direct residue”, where the reagent liquefies through the upper pipeline, the light fraction in the form of saturated vapor moves through thin channels into a semicircular channel lateral unloading of a stationary, and a heavier fraction through conical openings under the influence of centrifugal forces and pressure moves into the thin channel of the next shelf “oil residues)), fraction with a limit of Ipanema 800 0 C and above is hydrogenated through the upper conduit supplying reactant (hydrogen), significantly accelerates the process of separating fraction in thin channel devices liquefied semisolid fraction and supersaturated vapor moves to the annular channel side unloading, where the local pressure centrifugal forces discharged onto the
  • Figure 1 shows an arbitrary section of the left side of the mechanothermochemical fractionator; figure 2 is the same, the right part; on Fig.3 shows a diagram of the stages of the distillation of fractions; figure 4, shows a section aa in figure 1; figure 5 shows the node B in figure 1; figure 6 shows a section B-B in figure 1; Fig.7 shows a section G-
  • FIG. 8 shows a section DD; 9-12 illustrate activators; on Fig shows a section E-E; on Fig - section F; FIG. 15 shows a side section of the discs; on Fig, shows a section of the poses 24; in FIG. 17 shows a section 3-3 in FIG. 4; in FIG. 18 is a cross-sectional view of II in FIG.
  • the mechanothermochemical fractionator contains a cone-shaped body 1 and a receiving cup 2 for loading the source material.
  • the housing 1 there is a screw conical shaft 3 containing a worm spiral 4 with a screw selection 5, which interacts with the screw groove 6 of the housing 1.
  • triangular activators are fixed 7.
  • the top of the conical housing 1 contains a centering die 8 with conical half-openings 9 moreover, the shaft 3 on the drive side (the drive is not shown) is hollow and contains a movable piston 10 for local operation of the coolant.
  • On the opposite side of the conical shaft 3 made a centering bore hole 1 1 to accommodate the neck of the through shaft 12, which originates in the riser pipe 13.
  • the shaft 12 contains wedge-shaped activators 14 s a wavy surface and a semicircular selection 15 and a worm spiral 16, on the supply side of which are made triangular activators 17 with a wavy surface, and on the surface of the worm spiral 16 there are evaporation cells 18, to a depth of no more than their own diameter and through cells 19.
  • the riser body 13 contains nozzles for supplying agents 20.
  • a series-connected reactor vessel 21 comprises a continuation of the through shaft 12, with an ongoing screw spiral 16, which interacts with the sleeve 22, and shortened by grooves 23, moreover, slotted slots 24 are made in the sleeve 22, and the reactor vessel 21, on the opposite side, contains a comb 25 for interacting with the catalyst 26.
  • the reactor vessel 21 contains a pipe 27 for supplying an agent 28 and a pipe 29 for supplying a new catalyst .
  • the upper part of the housing 21 is made in the form of a cup 30 with a filter 31 and an attached separation column 32 with valve plates 33 with float valves 34 installed in them.
  • pipes 35 for lateral product selection and overflow pipe 36 are made.
  • the dome 37 contains a divider 38 at the outlet of the reactor.
  • the housing 21 comprises a slide die 39 with conical half-openings 40.
  • An accelerating housing 41 is connected to the reactor housing 21 in series, which comprises a sleeve 42 with cells 43, a worm spiral 44 of the shaft 12 with evaporative and through cells 45 and 46, respectively, and a nozzle for the donor agent 47.
  • a reactor vessel 48 is connected in series, which comprises a sleeve 49 with a screw set 50, the screw set 50 smaller in volume of the screw sample 23.
  • the wedge-shaped activators 51 contain cells 52 where a vapor-gas mixture is selected, which is squeezed out through the side slots 53 into the fluidized catalyst medium 54.
  • the housing 48 contains a gate die 55 with external adjustment of the size of the conical half-openings 56.
  • Upper part of the reactor vessel 48 is made in the form of a glass 57 and contains a filter 58.
  • the separation column 59 contains a valve plate 60 with a float valve 61, a side discharge pipe 62 and a overflow willow nozzles 63.
  • dome 64 contains a divider (valve) 65.
  • An accelerating body (block) 66 is attached to the reactor 48, which at the inlet contains a gate die 67 with external adjustment of the size of the conical holes 68, a sleeve 69 with cells 70.
  • Through the shaft 12 contains a worm spiral 71, on the surface of which evaporative and blow-through cells 72 are made; 73 respectively.
  • the housing 66 contains a pipe 74 for supplying the desired agent.
  • a reactor vessel 75 is connected with a boiling range of 220–315 0 C. 80 interacts with cells 81 and lateral slot discharge 82.
  • a fluidized rotary catalyst 84 is contained in the annular cavity 83.
  • the reactor body 75 contains a comb 85 on the inside and a pipe 86 for supplying agent to it a, and pipe 87 for supplying fresh catalyst.
  • the housing 75 contains a filter 89 and the housing of the separation column 90 with valve plates 91 and floating valves 92, and for unloading the finished product, the column 90 contains a pipe 93 and an overflow pipe 94, and at the top of the column 90 there is a dome 95 and a divider valve 96.
  • the housing of the booster block 99 which contains a sleeve 100 with cells 101 with a smaller mesh size 70, is connected in series to the housing 75.
  • a screw spiral 102, n wherein the evaporator surface and through the cell 103, 104 sized larger than the cells 101, arranged on the sleeve body 100.
  • the booster 99 comprises a sliding sleeve 105 and a die 106 with adjustable conical poluotverstiyami 107.
  • a reactor vessel 108 is attached to the booster 99 with a boiling point of the fraction 315 -450 0 C, which in turn contains a sleeve 109 with a screw groove 110 shorter than the screw grooves 79, which, through the activators 11 1, interact with the cells 112, and with a slot discharge 113, the annular cavity 114 and the catalyst 1 15.
  • the inner wall of the reactor vessel 108 is made with a comb 116 for rejuvenating the fluidized catalyst 115.
  • Below the completed comb 116 contains a pipe 117 for supplying steam and other agents required to perform the technology gical process. Above the comb 116 is a pipe 118 for supplying fresh catalysis.
  • the reactor vessel 108 in its upper part is made in the form of a glass 1 19 and contains a filter 120 and a housing of the separation column 121, which, in turn, contains valve plates 122, float valves 123, side unloading 124, overflow nozzles 125 and a dome 126 with a separation valve 127.
  • An accelerating block 128 is connected in series to the reactor housing 108, which at the inlet contains a gate die 129 with external adjustment of the tapered half-holes 130, a sleeve 131 s compression cells 132, which are smaller than the size of the previous cells and interact with the cells 133 of the screw spiral 134, which correspond to the size of the cells 132 or more, and the hollow shaft 12, which contains the worm spiral 134, is made with a conical transition 135 with an increase in diameter and forms a conical cavity 136 towards the shelf reactor body, and the gate die 137 is made with external adjustment of the conical floor holes.
  • the processing of the high-boiling fraction is based on a shelf reactor with a boiling point of 450-800 C, which consists of a sealed housing 138 mounted on the rotation shaft 12, the shelf disk 139, and the first shelf 140 from the rotation shaft 12 forms an annular cavity 141.
  • a shelf reactor with a boiling point of 450-800 C
  • the housing 138 comprises a stationary shelf disk 143, which together with a rotating shelf disk 139 forms annular channels (labyrinths) 144 for moving and separating the mixture 145.
  • Fixed ring floor 146 above the shaft of rotation 12 contains a through L-shaped hole 147, and below the shaft 12 it is sampled and forms an expanded cavity 148, which can occupy an area of up to 50% or more of the outer area of the shelf.
  • the shelf 149 of the rotating disk contains at least two trapezoidal slots 150, and the side wall of each sample of the rotating disk 139 contains screw grooves 151 that interact with the annular grooves 152.
  • a semicircular cavity 148 in the lower part is connected to the side hole 153 for unloading products with a boiling point of 450-650 ⁇
  • the next annular shelf 154 of the fixed disk 143 together with the annular shelf 155 form a flow channel with an increase in the volume of the cavity 156 in the lower part.
  • the annular shelf 156 contains at least two trapezoidal slots 157 directed by the base to the stationary shelf 158, which is partially sampled to form a cavity 159.
  • the disk 139 contains an annular shelf 160 with a trapezoidal slot 161.
  • the fixed annular shelf 162 in the lower part is sampled with the purpose of the formation of the cavity 163, and the annular shelf 164 of the disk 139 contains at least 2 trapezoidal slots 165, which, under the action of centrifugal forces and pressure, supply the mixture to the inner surface of the stationary shelf 166 of the disk 143, and the lower part of this shelf is sampled to form a cavity 167.
  • the shelf 168 of the rotation disk 139 contains at least two trapezoidal slots 169.
  • the housing of the fixed disk 143 in the region of the annular shelves 149, 155, 168 contains rings 170, 171 and 172 s external regulation of the extension in the direction of the respective shelves, and the housing parts 138,143 are configured to control the temperature through the channels 173, in addition, for local temperature control in the hollow shaft 12 are performed by movable pistons 174, 175 through the corresponding favoring pipelines.
  • Acceleration Block 128 provided with a nozzle 176 emergency discharge of the mixture, the body 138 of the shelf reactor contains nozzles 177 and 178.
  • the mechanothermochemical fractionator operates as follows.
  • the pre-warmed up to 90 0 C cone-shaped body 1 through the receiving cup 2 is forced to supply the source material (oil) to the pre-pre-warmed up to 90 0 C conical shaft 3, which contains a conical worm spiral 4 and is driven in rotation from an external drive (not shown in the drawing )
  • the material fills the screw inter-screw cavity, the groove of the screw set 5 and the groove of the screw set 6 in the housing 1.
  • the material moved by the screw spiral 4 is compressed to the top of the cone, the bubbles of the gas-vapor fraction under pressure decrease in size, and the narrower the cone, the higher the compression pressure and temperature, which is controlled by the movable piston 10 and supplied by an external source of heat transfer agent into the cavity of the screw shaft 3.
  • the first stage of the dispersal of the material ends by pumping through the conical floor of the hole 9, the centering die 8, while this is achieved temperature up to 90 0 C.
  • the mixture of material entering the cavity of the riser pipe 13 is supplied by mechanical action of the shaft 12, which is fixed in the bore hole 1 1 of the shaft 3 with the possibility of rotation from the drive from the opposite side (not shown).
  • Wedge-like activators 14 having a wavy surface and semicircular samples in the rear part 15, when the shaft rotates more than 100 rpm, under barrel pressure conditions contribute to the collapse of the material, additional gas bubbles and an increase in temperature of at least 90 ° C, and the evaporation cells 18, execution on the surface of the activator 14, capture the mixture from the helical groove 23 and under the influence of friction, the selection of the gas-vapor fraction, which is unloaded when you re-enter the helical groove 23, and simultaneously Menno loaded liquid mixture.
  • the light-gas vapor fraction formed in the mixture with a boiling point of up to 100 C and above is captured by a screw spiral 16, which contains triangular activators 17, to form a gas loop along the screw spiral of the screw 16, evaporation cells 18 and through blowdown cells 19, and the wavy surface of the activators 17 additionally contributes to the dispersal of the liquid mixture, and the evaporation cells 18 perform selection of the gas-vapor fraction on the surface of the sleeve 22.
  • Through-purge cells 19 due to the m channel overpressure of the medium dilute the mixture located in the vicinity of the shaft 12, thereby achieving uniformity of the mixture in the inter-screw cavity.
  • the required agents (alkali solution, steam, and other elements) are supplied through the pipe 20 to neutralize molecular sulfur.
  • the mixture Under the influence of a screw spiral 16, the mixture enters the reactor vessel 21, where the sleeve 22 contains slotted slots 24, through which the mixture is susceptible to molecular diffusion transfer, while the concentration of the medium in the inter-screw cavity is equalized.
  • a medium with a boiling point of 100 0 C or more remains in the inter-screw cavity for further movement, and a fraction with a boiling limit of up to 100 0 C located near the sleeve wall condenses onto the circulating catalyst 26.
  • a fresh or restored catalyst 26 is supplied through the pipe 29 which functions in the cavity until it is completely worn out or is replaced through lower hatch.
  • the gas-vapor light fraction located in the glass 30, through the filter 31, tends to the cavity of the separation column 32 and through the float valve 34 in the valve plate 33 enters the bubbling liquid with a layer thickness of 10 cm and above.
  • the bubbling of a gas-vapor mixture through a layer of liquid is called rectification, where partially heavy molecules condense, and the light components of the product rise higher, and through the side pipes (discharge) 35, they enter the condenser (not shown in the drawing) and then to the warehouse of the finished components.
  • the remaining heavy product in the bubbling liquid through the overflow side pipes 36 enters the original cavity of the riser pipe 13 for a second process, which does not prevent some molecules in the form of steam from traveling back and forth several times.
  • the lightest fraction of butane and lighter hydrocarbons with a boiling point of less than 90 C rises in the cavity of the dome 37, where through the divider 38 can go to gas fractionation plants or to the consumer.
  • the remaining liquid mixture in the inter-screw cavity is supplied to the gate die 39 and through the conical holes enters the cavity of the booster body 41, where the sleeve 42 contains cells 43.
  • the mixture is captured by a worm spiral 44, fills the cells 43 of the sleeve 42, through which the evaporation cells 45 of the screw 44 are filled and purge (through) cells 46, and through pipe 47, the mixture is enriched with the required agent to accelerate and mitigate the process.
  • the shaft rotates 12 to 1000 rpm. and more, the mixture of the evaporation cell 45 is destroyed by friction against the surface of the sleeve 42, and a molecular gas-vapor component is formed, which when entering the next cell 43 of the sleeve 42 generates a microhydrodynamic shock.
  • the result is an instant jump in temperature and pressure in the enclosed space of two cells.
  • a mixture with a boiling range of up to 220 ° C and more from the accelerating body 41 through the semiconical openings 56 of the slide die 55 enters the compartment of the reactor vessel 48, where wedge-shaped activators 51 with evaporation cells 52 and a wavy surface support the mixture parameters achieved in the accelerating compartment of the housing 41, while the evaporation cells 52 during rotation are loaded with a mixture from the cavity of the screw sample 50 of the sleeve 49 and are discharged through the lateral slots 53 by flash evaporation into the annular cavity formed by the sleeve 49 and housing 48, to a fluidized catalyst 54.
  • the gas-vapor mixture of components interacts with the catalyst 54.
  • the elemental carbon present condenses onto the catalyst particles (if any) and tends to circle in a circle 25 (hereinafter, all technological operations are performed according to the described scenario, and the light fraction with a boiling point up to 220 0 C from the glass 57 through the filter 58, tends to the cavity of the separation column 59 and through the float valve 61 in the valve plate 60, enters the bubbler liquid with temperature 220 C and above, where partially heavy molecules condense, and the light components of the product rise higher above the liquid and through the side unloadings 62 enter the condenser and then compound the gasoline fraction.
  • the ekul through the overflow nozzles 63 are returned to the booster housing 41 for reuse.
  • the lightest fraction of this column enters the dome 64 and through the divider 65 to the gas fractionation units (not shown in the drawing) or to the nozzle 20 for reuse.
  • the remaining liquid mixture with a boiling point more than 220 0 C in the cavity of the sleeve 49 under local pressure enters the booster casing 66 via the sliding die 67 and the semi-conical holes 68.
  • the mixture fills the cavity of the sleeve 69 and disposed therein a cell 70 is trapped a screw coil 71, in the body of which contain evaporation cells 72 and purge cells 73, through the channels of which the gas-vapor mixture enters the shaft wall 12, which ensures uniform distribution of gas bubbles, and the evaporation cells 72, when combined with cells 70, are loaded with the mixture and when the spiral is rotated 71, frictional friction and compression compression occur, where when the evaporation cells 72 enter cells 70, a microdynamic shock occurs in a closed cavity, which instantly selects the gas-vapor components of the product with the limit boiling up to 315 C, and when cells 70 and 72 are opened, the boundary layer is saturated with gas-vapor bubbles, which, under the mechanical action of the screw spiral 71, moves along the channel of the sleeve 69, and the pipe 74, made in the housing 66, serves to relieve excessive pressure or supply the required an agent for accelerating a chemical process in the reactor chamber 75.
  • the catalyst interacts with the components of the vapor-gas mixture during rotation around the sleeve 78, which allows it to constantly restore its properties by impacting between itself and the body of the comb 85.
  • the heavy components through the overflow nozzles 94 are sent to the booster body 66 for recycling, and the lightest fraction is raised into the dome 95 and through the divider valve 96 to the gas fractionation unit or to the nozzle 20 for reuse.
  • the mixture remaining in the reactor 75 with a boiling point of 315 ° C and above, is supplied under pressure to the gate die 97 and is fed through conical half-holes 98 to the cavity of the booster block body 99, in which the sleeve 100 with cells 101 is placed, with cells 101 of a third in size fewer cells 70.
  • the screw spiral 102 captures the mixture and moves it along the shaft 12, while the mixture fills the cells 101, which are the store for the evaporation cells 103 and the purge cells 104, where the mixture captured by the evaporation cells 103 frictionally rotates on the surface of the liner, and when the evaporation cell 103 and the stationary cell 101 are combined, microhydrocompression compression of the mixture occurs in a confined space, and there is a lot of heat generation and selection of the vapor-gas fraction with a boiling point up to 315 0 C and higher.
  • the mixture evenly spreads in the boundary layer of the inner diameter of the sleeve, and the captured mixture by the cells 104 moves along the channels from the periphery (inner diameter of the sleeve) to the axis of the shaft 12, which ensures uniform mixing of the medium in the inter-screw volume.
  • the agents supplied through the pipe 105 allow you to accelerate or slow down the chemical reaction in the reactor vessel.
  • the mixture is heated to 315 0 C and above, it is supplied to the gate die 106 and through conical half-holes 107 enters the reactor vessel 108 and into the cavity of the sleeve 109, fills the screw grooves of the software through which the evaporation cells 1 12 of the activators 1 1 1 are fed, and when the evaporation cells 1 12 are combined with the side slotted unloadings 113, the vapor-gas mixture is injected into the annular cavity 114 onto the catalyst 115 in suspension in the cavity of the housing 108. The reacted catalyst 1 15 moves in a circle around the cavity to the comb 116 of the housing 108.
  • the remaining mixture with a boiling point of 450 ° C and above under pressure enters the booster housing 128 through a slide gate 129 and semiconical openings 130, where it fills the cavity of the sleeve 131 and the cells of the sleeve 132, from which the evaporation cells 133 of the screw spiral 134 are filled, while the mixture friction friction and microhydrocompression impacts heats up above 450 0 C, and under the mechanical influence of a screw spiral 134, the mixture is fed to the conical passage 135, where in the conical cavity 136 the mixture is compressed in compression and the temperature rises to 500 C and higher.
  • the mixture enters the slide gate 137 and through the semiconical openings is fed into the sealed housing 138, and, in order to reduce the force of the return flow from the housing 138, the holes of the die 137 with the base of the diffuser are directed along the mixture.
  • the shaft 12 contains a rigidly mounted shelf disk 139, which rotates up to 1000 rpm. min and more in conjunction with the shaft 12.
  • the first shelf 140 of the shaft 12 forms an annular cavity 141, through which the mixture 145 enters the conical holes 142 and evenly fills the annular channels 144 formed in conjunction with the stationary shelf disk 143, the first annular gap 144 from the shaft 12, according to the conditional throughput, it is 2-a times larger than the second channel from the shaft 12.
  • the mixture 145 which entered the gap between the rotating shelf of the disk 139 and the stationary shelf of the disk 143, is evenly (pressed) uniformly (pressed) under the influence of centrifugal forces in morning diameter flange 149 of the rotating disk 139, the gas bubbles as the lighter fraction (without weight) are allocated to the surface and concentrate in the floor of the annular cavity 148 with a boiling range of 450 -550 0 C and under a local pressure at the open tverstii fed to condenser 153 .
  • an agent is accelerated through the ⁇ -shaped hole 147 of the shelf 146, accelerating the technological process of obtaining a gas-vapor fraction with a boiling point of 450 - 550 0 C.
  • the remaining mixture through the edge of the rotating shelf 149 falls into the gap between the wall of the rotating disk 139 and the shelf of the fixed disk 143, at the end of which at least two annular grooves 152 are made.
  • the spiral grooves 151 of the countercurrent mixture are made, contributes to additional frictional friction, heat and gas-vapor generation mixture, which under local pressure enters the next thin channel together with the mixture entering through the trapezoidal slots 150, where due to friction with a fixed shelf 154, the heavy mixture is rolled along the channel y and is shifted to the edge of the shelf 154, where it also falls over the edge into the gap between the end of the shelf 154 and the wall of the rotation disk 139.
  • the grooves 152 and the spiral 151 additionally act on the mixture, and the gas fraction is molecularly released with a boiling point of 550 -700 0 C , which accumulates in the cavity 156, and the light fraction floats up and through the side hole 153 enters the heavy gas oil condenser (not shown), and the heavy fraction is pressed against the inner wall of the shelf 155 due to centrifugal forces and enters through the trapezoidal slots 157 into the thin channel of the next shelf 158, which in the lower part forms a cavity (sinus) 159, for concentration of the gas fraction with a boiling range of 700 - 750 0 C, which through the side hole 153 tends to the cooling system, and through the L-shaped hole in this channel an agent (such as hydrogen) is supplied to facilitate an instant chemical process (if one is required).
  • an agent such as hydrogen
  • Net balance is used in the construction industry. In the event of a dangerous pressure for the device, it can be regulated through the valve of the nozzles 176, 178.
  • the thin channel of the shelf 154 can partially be blocked by the external regulation ring 170, after which the remainder of the channels can only enter through the trapezoidal slots 150, 157, 161, 165 , 169, which allows to reduce the number of products with a boiling point of 550 C and above and increase the number of products with the boiling range is up to 550 0 C.
  • the external regulation ring 171 allows you to block the shelf channel 158 and increase the output with the boiling range from 550 C to 700 ° C.
  • the external regulation ring 172 allows you to block the return current of the residue when washing the cavity with a solid residue.
  • the temperature of the housing 138 is controlled by a system of channels 173, and the temperature of the shaft 12 is controlled by the movable pistons 174, 175.
  • the invention provides high-quality components of motor fuel from oil using chemical transformations using catalysts in the preparation of each fraction.
  • the composition changes as follows:
  • - naphthenes are converted to aromatic hydrocarbons, including benzene.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L’invention se rapporte au domaine de l’industrie chimique, et concerne notamment un procédé de production d’un produit en phase liquide et en phase gazeuse à partir de composés ayant un poids moléculaire élevé, lequel consiste à appliquer une action mécano-thermo-chimique sur le matériau de départ en utilisant des catalyseurs et un agent contenant de l’hydrogène à chaque étape du processus de manière à obtenir un produit purifié de haute qualité, et permet, par le recyclage des fractions ayant un point d’ébullition élevé ou très élevé, d’effectuer une décomposition supplémentaire des molécules et d’obtenir un distillat de haute qualité pour carburants et huiles de moteur. L’invention concerne également une colonne de fractionnement mécano-thermo-chimique permettant de mettre en œuvre ce procédé.
PCT/RU2010/000296 2009-07-06 2010-06-07 Procédé de séparation de systèmes hétérogènes liquides et gazeux, et colonne de fractionnement mécano-thermo-chimique pour sa mise en œuvre WO2011005145A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2009125462 2009-07-06
RU2009125462/04A RU2467053C2 (ru) 2009-11-20 2009-11-20 Способ разделения жидких и газовых гетерогенных систем и механотермохимический фракционатор для его осуществления

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Publication number Priority date Publication date Assignee Title
CN114307222A (zh) * 2021-12-29 2022-04-12 深圳市百瑞空气处理设备有限公司 一种内置可调式分布器的nmp精馏提纯设备
CN117225354A (zh) * 2023-11-13 2023-12-15 吉林建筑大学 用于生产聚羧酸减水剂的反应釜及制备方法

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Publication number Priority date Publication date Assignee Title
RU2078112C1 (ru) * 1994-05-23 1997-04-27 Юрий Гаврилович Тузов Способ извлечения углеводородов из нефтесодержащего сырья и устройство для его осуществления
EA003082B1 (ru) * 1998-10-16 2002-12-26 Карбон Рисурсес Лимитед Способ конверсии углеводородов и устройство для его осуществления
RU2220847C2 (ru) * 1999-08-04 2004-01-10 Джеймс Д. ФОГАРТИ Экструдерный червяк, повышающий гомогенность термопластичного пенопласта
RU75712U1 (ru) * 2008-04-02 2008-08-20 Общество с ограниченной ответственностью Научно-производственная фирма "Экотеплосервис" Устройство подачи твердого топлива в топку

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RU2280847C2 (ru) * 2004-06-21 2006-07-27 Российская Федерация, от имени которой выступает государственный заказчик - Министерство Российской Федерации по атомной энергии, Датчик силы

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Publication number Priority date Publication date Assignee Title
RU2078112C1 (ru) * 1994-05-23 1997-04-27 Юрий Гаврилович Тузов Способ извлечения углеводородов из нефтесодержащего сырья и устройство для его осуществления
EA003082B1 (ru) * 1998-10-16 2002-12-26 Карбон Рисурсес Лимитед Способ конверсии углеводородов и устройство для его осуществления
RU2220847C2 (ru) * 1999-08-04 2004-01-10 Джеймс Д. ФОГАРТИ Экструдерный червяк, повышающий гомогенность термопластичного пенопласта
RU75712U1 (ru) * 2008-04-02 2008-08-20 Общество с ограниченной ответственностью Научно-производственная фирма "Экотеплосервис" Устройство подачи твердого топлива в топку

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114307222A (zh) * 2021-12-29 2022-04-12 深圳市百瑞空气处理设备有限公司 一种内置可调式分布器的nmp精馏提纯设备
CN117225354A (zh) * 2023-11-13 2023-12-15 吉林建筑大学 用于生产聚羧酸减水剂的反应釜及制备方法
CN117225354B (zh) * 2023-11-13 2024-01-23 吉林建筑大学 用于生产聚羧酸减水剂的反应釜及制备方法

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