WO2010117300A1 - Assemblage et dispositifs de traitement en profondeur de matiere premiere hydrocarbonee - Google Patents

Assemblage et dispositifs de traitement en profondeur de matiere premiere hydrocarbonee Download PDF

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Publication number
WO2010117300A1
WO2010117300A1 PCT/RU2010/000065 RU2010000065W WO2010117300A1 WO 2010117300 A1 WO2010117300 A1 WO 2010117300A1 RU 2010000065 W RU2010000065 W RU 2010000065W WO 2010117300 A1 WO2010117300 A1 WO 2010117300A1
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vkf
raw materials
separation
light
processing
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PCT/RU2010/000065
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Russian (ru)
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Владимир Андреевич ЗОЛОТУХИН
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Zolotukhin Vladimir Andreevich
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    • 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
    • C10G15/00—Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs
    • C10G15/08—Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs by electric means or by electromagnetic or mechanical vibrations

Definitions

  • the invention relates to the oil refining, petrochemical and chemical industries, as well as to the fuel and energy industry, and specifically to the field of preparation and deep processing of oil, including heavy oil, residues of oil refining and petrochemical industries, natural bitumen, coal, oil shale, vegetable products and other hydrocarbon media, solid, liquid, gaseous, hereinafter raw materials, and can be used in the production of hydrocarbon fuels, petrochemical and chemical products.
  • the application of the invention allows to solve many environmental problems and leads to improved environmental conditions.
  • Light target products or fractions are understood as fractions for further processing and obtaining light target commodity products with a boiling point mainly up to 350-360 0 C, containing fuel, i.e. the most expensive gas, gasoline, kerosene and diesel fractions, as well as products for the petrochemical and chemical industries (benzene, toluene and others).
  • light target fractions or products of which, when light final target products (liquefied gas, tested gasoline, diesel fuel, petrochemical products and others) receive final processing.
  • the primary distillation of oil at the refinery is carried out in two ways: by single evaporation in one distillation column and with preliminary evaporation of light fractions, or by double evaporation (Bagirov I.T. High-performance atmospheric and atmospheric-vacuum installations. M., Chemistry, 1964, p. 5; Dekhterman A.Sh. Oil refining according to the fuel variant. M., "Chemistry", 1988, p. 41). The latter method is used most often, since it allows you to increase the depth of selection of distillates within their potential content in raw materials. We briefly consider the sequence of operations of primary distillation carried out according to the classical scheme.
  • Oil preparation is carried out in blocks ELOU (electro-dehydrating and desalting plant). Equipment difficult to manufacture and operate, explosive (Dekhterman A.Sh. Oil refining according to the fuel version. M., "Chemistry", 1988, p. 36).
  • the separation of oil into fractions is based on the difference in the boiling point of its components.
  • the low-boiling part passes into the vapor phase and, after condensation, forms a distillate.
  • atmospheric or vacuum distillation is used (A. Dekhterman, Oil refining according to the fuel version. M., Chemistry, 1988, p. 26).
  • Rectification apparatus refers to a fairly technologically advanced and structurally-used equipment. However, it is sophisticated equipment. Column distillation apparatuses used at large refineries are quite expensive to manufacture and operate. Therefore, at the stage of preliminary separation of oil, it is advisable to use simpler devices, such as evaporators (Dekhterman A.Sh. Oil refining according to the fuel version.
  • the evaporator is a cylindrical tank. At the bottom of its housing is an integrated tubular heat exchanger. Inside the tubes of the heat exchanger serves a coolant for heating the product (oil). Typically, water vapor is used as a heat transfer medium. The light part of the oil (gasoline fraction) evaporates and is discharged through the upper fitting. The remaining oil is poured through the drain plate and is discharged through the corresponding fitting. The amount of evaporated part of the oil depends on the temperature in the apparatus, that is, on the surface of the heat exchanger and the temperature of the coolant. The surface of the heat exchanger during operation is covered by deposits of oil and heat transfer conditions are much worse.
  • the temperature of the process is 200 - 230 0 C. This temperature corresponds to a certain evaporated part of the oil (feedstock).
  • this apparatus is used as a prototype of an evaporation and separation apparatus.
  • the method of catalytic cracking of oil products is widely known - the method of thermal decomposition of heavy oil fractions in the presence of a catalyst (Rudin M.G., Drabkin A.E. Oil refinery quick reference guide. L.: Chemistry. 1980 , p. 70-73).
  • the method includes heating the feedstock to a temperature of 470-550 0 C, mixing it with water vapor and then with a catalyst, treating the mixture in a reactor, followed by catalytic decomposition of the feedstock and separating it into fractions, as well as isolating and regenerating the catalyst at a temperature of 590-670 0 C.
  • the specified installation is very cumbersome, difficult to maintain and does not allow to intensify the chemical-technological processes with processed raw materials.
  • the disadvantage of this method is the impossibility of a more complete use of raw materials in the processing process due to the dependence on the intensity of the electromagnetic field.
  • the known method is characterized by high energy costs for creating a deep vacuum, and the use of only the acoustic frequency range does not provide reliable destruction of highly viscous media, a long period of time is required for the processing of fuel oil.
  • this method is intended for the processing of fuel oil only and does not allow the processing of, for example, used motor or lubricating oils.
  • Installation for implementing the specified method of cracking oil contains interconnected device for processing of raw materials, which is simultaneously an ultrasonic generator, a separation chamber for separating spent raw materials and a device for condensing the vapor phase.
  • a device for processing raw materials is a housing in which interconnected chambers are formed, each of which has a rotor mounted on the drive shaft and a stator. The last chamber is communicated with the first, forming a closed loop. Behind the last chamber there is a separation chamber having a channel for diverting the resulting vapor phase for condensation in the refrigeration chamber.
  • the emitter of ultrasonic frequencies are the mechanical components of the system (rotor, stator, bearings).
  • a known method of thermal processing of heavy oily fractions including thermal cracking of heavy oily fractions into phases and obtaining from the vapor phase final products, characterized in that before thermal cracking, the feedstock is preliminarily subjected to a wave treatment in a separate treatment zone by forming a wide range of frequencies from the acoustic to the light range in the medium being processed, after which the impact products are fed to thermal cracking, which is carried out in the mode of primary oil refining at atmospheric pressure and a maximum heating temperature of 360 0 C (patent of the Russian Federation RU2215775).
  • the disadvantage of this method is that for the excitation of vibrational levels of molecules and their activation for further cracking, it is necessary to add a certain amount of energy to the processed medium.
  • the necessary energy is introduced by direct heating of the feed.
  • raw materials for example in catalytic cracking
  • catalysts that reduce the activation energy of molecular bond breaking and contribute to the cracking process.
  • the activation energy of molecules is introduced into the medium due to ((formation of a wide spectrum of frequencies from the acoustic to the light range in the medium being processed)).
  • Known devices for acoustic and cavitation processing in which the processing is carried out due to the movement of the rotor, the disk is a rotary pulsation apparatus (patent RU 2115176 ((Cavitation generator ”, patent RU 211 1554 ((Ultrasonic oscillation generator))).
  • acoustic and cavitation treatment of the liquid occurs in thin layers directly adjacent to the moving rotor or disk, and not in the entire volume, therefore, the liquid treatment in such devices gives a small, within the limits of measurement error, increase in the depth of processing and in the industry has not found wide use in hydrocarbon feedstock cracking purposes.
  • such devices are used to emulsify liquids. Due to the fact that the devices moving parts are present, life of such devices is insufficient.
  • the closest analogue (prototype) for the claimed device is the device according to patent RU 2164629 ((Method for cavitation of a fluid flow and a device for its implementation)).
  • the cavitation method is hydrodynamic. The process occurs due to the fact that a cavitator in the form of a working fluid of various shapes is placed in the flow of the processed fluid, and the area of the maximum cross section of the working fluid in a plane perpendicular to the axis pipeline, is more than 0.8 of the cross-section of the pipeline, but not equal to it. It is known that cavitation occurs during the flow around a poorly streamlined body, in the rear of which there is a zone of low pressure.
  • the streamlined body always strives to occupy a position in which the hydrodynamic drag is minimal, i.e. such a position in which the flow of fluid around this body will be the best for these conditions of movement of the medium. This will lead to an even greater reduction in the cavitation zone and a decrease in cavitation and acoustic effects on the raw materials.
  • Thermal cracking has been known for a very long time (Smidovich EV, Oil and gas processing technology. 4.2. M., Chemistry, 1968. VE Parkhomenko, Oil and gas processing technology. M., Gostoptekhizdat, 1959.).
  • the disadvantages of thermal cracking include the following. When the raw material is heated with increasing temperature, the number of bond breaks slowly and smoothly increases, but when a critical temperature is reached (depending on the properties and composition of the feedstock), this number increases sharply, the process of bond breaking is avalanche-like, uncontrollable. This leads to coking of the equipment and a decrease in the overhaul mileage, the process is periodic.
  • thermal cracking There are a lot of gases and unsaturated hydrocarbons in thermal cracking products, which increases the requirements for further equipment in obtaining marketable products - gasoline, diesel fuel and others, which, ultimately, leads to an increase in capital and operating costs. Therefore, recently, thermal cracking processes, especially in the fuel version, are rarely used. High temperatures of heating of raw materials (470-550 0 C and above) and pressure (up to 7 MPa) also lead to high capital costs, and coking of equipment and low overhaul mileage of equipment - to increase operating costs.
  • the closest analogue (prototype) for the installation of advanced processing according to the invention is thermal cracking.
  • the technical result of the application of the invention is to increase the yield of light target products and increase the depth of industrial processing of raw materials, simplify and cheapen the process and equipment for the preparation and advanced processing of raw materials, reduce operating and capital costs with a high depth of further processing, save and rational use of hydrocarbon raw materials.
  • the aim of the invention is to increase the yield of light light fractions (gasoline, kerosene and diesel, petrochemicals) higher than their potential content in raw materials and increase the depth of processing, which leads to optimal and rational use of raw materials for their further processing, reducing operating and capital costs, simplicity and reliability of equipment design, simplicity and reliability of control and adjustment of the thermomechanical cracking process, reduction of coking and increase of spacing ntnogo path equipment, the continuity of the process, improving the quality of thermomechanical cracking products for further processing as compared with thermal cracking, reduction of harmful impurities, the solution of environmental problems, recycling of free oil and other gases.
  • the main goal is to increase the processing depth of any hydrocarbon feedstock, which ultimately leads to an increase in the profitability of the entire processing industry.
  • This goal is achieved by the fact that in the installation for the preparation and processing of liquid hydrocarbon raw materials, including preparation (preliminary cleaning of water and harmful impurities), supply and heating raw materials, separation of raw materials into fractions, removal of separation products, a separation apparatus is built in, in which the hydrocarbon mixture is divided into two parts - the light separation part (low boiling fractions of NKF) and the heavy high molecular weight part of separation (high boiling fractions of VKF).
  • Raw materials are preheated in recuperative heat exchangers to optimize energy costs due to the heat of one or all separation products (NKF and VKF).
  • the raw materials are preheated in a separate or general (but separate from heating VKF coil) with heating VKF heating furnace (heater) to a temperature above 20 ⁇ 50 0 C to reduce viscosity and increase fluidity of raw materials, especially heavy and highly viscous.
  • Raw materials are usually heated to a temperature not exceeding 450 ° C so that coking of heating equipment does not begin, although in some cases (depending on the composition of the raw materials), the heating temperature of the raw materials can be even higher. Simultaneously with heating, the raw material can also be subjected to thermal cracking.
  • a heating furnace of VKF heats the heating of the liquid part of the separation in one pass through the coil of the furnace or heater does not exceed 250 ° C, but may be more, and the mass fraction of VKF subjected to thermal cracking in the heating furnace or heater does not exceed 50% to prevent intense formation of coke deposits on the surfaces of coil heaters.
  • the VKF speed in the furnace coil (heater) should be higher than 1 m / s (optimally 3 ⁇ 10 m / s), which can significantly reduce or even avoid coking of the coil (heating channel VKF).
  • the raw materials and heated VKF are sent to the direct mixing device, in which the raw materials are finally heated, and they are heated to a certain subcritical temperature, which is lower than the onset temperature of the avalanche-like uncontrolled thermal cracking, but not more than 300 0 C (depending on the composition and properties of the initial raw materials), i.e. heated so that uncontrolled thermal cracking has not yet begun.
  • a high temperature for example, up to 400 0 C and higher, depending on the process conditions
  • colder oil or other liquid hydrocarbon feedstocks for example, at a temperature of 200 0 C
  • thermomechanical cracking in which the mixture to initiate a controlled process of breaking the bonds of molecules (thermomechanical cracking) is subjected to mechanical and wave effects of a different nature and a wide range of frequencies, for example cavitation, sound, ultrasonic vibrations, and for cavitation processing heated to subcritical temperature of the raw material and the imposition of acoustic exposure use such devices, the action of which is based on hyd dynamic effects movement of multiphase fluids at speeds exceeding 5 m / s for channels of various shapes.
  • the specific speed value is chosen empirically based on the analysis of separation products (NKF and VKF).
  • thermomechanical cracking device sent to the separation apparatus, in which the processed mixture of raw materials and the heavy high molecular weight liquid separation part (high boiling fractions of VKF) are separated into the light vapor-gas part (low boiling fractions of NKF) and the heavy liquid part of separation (high boiling fractions of VKF).
  • a mixture of raw materials and VKF is sprayed (dispersed) into the separation apparatus with a decrease in pressure.
  • heavy commercial products such as coke, bitumen, bitumen emulsions, coatings, oils and others
  • the light gas-vapor part (NKF) which contains both light fractions of the feedstock and light fractions of the products of thermal cracking VKF and thermomechanical cracking of a mixture of raw materials and VKF, is sent to the separation device (filtration, droplet separation, rectification), and the temperature in the separation device corresponds to the maximum the end boiling temperature of light fractions of the desired commercial products, for example 350-360 0 C for the diesel fraction. This boundary temperature can be changed depending on the set tasks and requirements for the resulting products.
  • light reaction fractions mainly with a boiling point up to 350-360 0 C
  • light commercial products such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products
  • the filtrate after the separator to obtain an additional amount of light target products is returned to the reprocessing at the beginning of the process together with the circulating part of the VKF.
  • Devices for mixing raw materials and VKF, wave and mechanical processing of the mixture, dispersion (spraying), and separation of the combined gas and vapor separation of NKF are built into the apparatus for separating the mixture into liquid (VKF) and combined gas (NKF) parts, and the quality of the separation products and their ratio depending the properties of the feedstock are controlled by the temperature and pressure of the circulating VKF at the outlet of the furnace (heater) and raw materials, the temperature and pressure of the mixture in the separation apparatus, the temperature of the NKF in the separator, the flow of raw materials, circulating liquid Asti CCF and their ratio, and the raw speed of the circulating liquid portion CCF and mixtures thereof in the mixing device, processing the dispersion (spraying).
  • the speed control of raw materials, the circulating liquid part of the VKF and their mixtures in the mixing and processing devices can be carried out by changing the mechanical parameters of the design of these devices.
  • the separation level of the combined-cycle phase of the NKF and the liquid phase of the VKF in the separation apparatus is maintained at given values of the above technological parameters by the value of the consumption of HCF directed to obtain heavy commercial products, and the number of built-in the apparatus for mixing raw materials and VKF, processing and dispersing (spraying) the mixture can be more than one of each type and depends on the productivity of the processing industry.
  • RPA rotary-pulsation devices
  • light and radioactive irradiation devices sound and ultrasound from various types of external sources (piezo-emitters, magneto-emitters, and other devices) as reagents and catalysts as processing devices for raw materials, VKF, and their mixtures.
  • the installation may include a device for mixing preheated raw materials and circulating VKF to the furnace (heater) heating VKF.
  • the VKF heating furnace (heater) is used to heat the mixture of raw materials and VKF to subcritical temperature or to heat and thermally crack the mixture.
  • the mixture is then sent to a thermomechanical processing device, to a dispersant and to a separation apparatus, after which the NKF and VKF obtained after the separation apparatus are sent as described above.
  • Both parts of the separation can be sent to the mixing device to obtain synthetic oil with an increased potential content of light fuel products and significantly lower density and viscosity compared to the feedstock, which is then sent for further in-depth processing, and the mixing device VKF and NKF may be built into the separation apparatus.
  • the mixing device VKF and NKF may be built into the separation apparatus.
  • a light distillation is usually obtained, which is returned to the beginning of the process for reprocessing together with the raw material to obtain an additional amount of light target products.
  • the bottom (heavy) residue after the unit for producing light commercial products (such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemicals), for example, this is the bottom residue after the distillation column, is returned to the beginning of the process for reprocessing together with raw materials to obtain additional quantities light target products.
  • the raw materials can be preheated in recuperative heat exchangers due to the heat of commercial products.
  • coke particles and other mechanical impurities can be formed, the ingress of which is undesirable into the circulating VKF and further into the pump and heater, therefore, a device for cleaning VKF from harmful impurities, solids and coke particles is built into the circulation circuit of the VKF part.
  • gaseous hydrocarbons which are also hydrocarbon feedstocks, such as associated or natural gas
  • gas fractions obtained during the refining process, in particular according to this invention and solid hydrocarbons in the form of a fine powder can also be sent for advanced processing.
  • the positive effect is also provided by the fact that the feedstock and / or circulating high boiling fractions of the FCF are subjected to mechanical and wave processing and / or thermomechanical (non-catalytic) cracking in front of the mixing device.
  • the apparatus for the separation of hydrocarbons into the light vapor-gas separation part (low boiling fractions of NKF) and the heavy liquid part of separation (high boiling fractions of VKF) is a capacitive apparatus that contains a housing, fittings for input and output of working and product media, fittings and devices for monitoring the technological parameters of the apparatus (temperature, pressure).
  • thermomechanical cracking in which a mixture of raw materials and VKF is heated to a certain subcritical temperature to initiate a controlled process of breaking bonds molecules (thermomechanical cracking) are subjected to mechanical and wave effects of a different nature and a wide range of frequencies, for example, cavitation radiation, sound, ultrasonic vibrations, a device for spraying (dispersing) the mixture into the apparatus to increase the interfacial surface of the separated media and to more effectively and quickly separate them.
  • a separation device (filter, droplet separator) of the vapor-gas separation part (NKF) is built into the upper part of the apparatus, after which the purified NKF leaves the apparatus and is sent to obtain marketable products, and the filtrate by gravity enters the lower part of the apparatus and mixes with VKF.
  • unsaturated hydrocarbons are formed.
  • a block or device with a catalyst is built into the separator, for example, in the form of a basket with catalyst granules filled in it.
  • molecular hydrogen, light hydrogen-containing media enriched with hydrogen for example, natural or associated gas, light shoulder straps of gasoline fractions and others, are fed into the block with the catalyst.
  • the temperature in the separation device corresponds to the maximum temperature of the end of boiling fractions of light target commercial products, for example 350-360 0 C for a diesel fraction.
  • the separation level of the combined-cycle phase of the NKF and the liquid phase of the VKF is lower than half the height of the separation apparatus, and a fitting is built into the device’s body for controlling the level of the phase separation and maintaining it in the set value by the flow rate of the VKF sent to the production units of heavy commodity products with the given other values technological process parameters.
  • a VKF separation device In the lower part of the apparatus, a VKF separation device is built into parts, a part of the VKF is sent for the production of heavy commercial products (such as coke, bitumen and others), and the other part returns to the beginning of the process and circulates in a closed circuit - a separation apparatus, a heating furnace (heater), separation apparatus.
  • the number of devices for mixing raw materials and VKF, processing and spraying (dispersing) the mixture built into the device can be more than one of each type and depends on the productivity of the processing industry.
  • a separator is installed in the lower part of the apparatus - a sump for separating from VKF the part necessary for circulation and for cleaning the circulating part of VKF from coke particles and other mechanical impurities.
  • the device for mechanical and wave processing is combined with the device for mixing and dispersing the mixture and can be called as “Tyrbodinoamichesky Disintegrator)) (TDD).
  • TDD Tethyrbodinoamichesky Disintegrator
  • Its task is to carry out direct heating of the raw material (medium 1) due to the heat of the superheated VKF (medium 2), cavitation and acoustic treatment of the mixture of raw materials (medium 1) and VKF (medium 2) and dispersing (spraying) the treated mixture into the separation apparatus.
  • the phenomenon of cavitation occurs during the flow around obstacles and poorly streamlined bodies, especially with sharp edges and edges. There is a disruption of the flow with the appearance of a zone of low pressure and the formation of caverns, i.e. cavitation bubbles.
  • cavitation bubbles When the bubbles collapse, shock pulses of high pressure (hundreds of atmospheres and more), local areas of a strong increase in temperature (hundreds and thousands of degrees) arise.
  • shock pulses of high pressure high pressure
  • local areas of a strong increase in temperature (hundreds and thousands of degrees) arise.
  • waves of a wide spectrum of frequencies appear, i.e. there is a mechanical and acoustic impact on the medium being treated.
  • the cavitation phenomenon is widely used in various fields of technology, in particular, for the intensification of various chemical reactions and transformations.
  • tiny bubbles of gas or vapor are always present in a real liquid, moving with the flow and falling into the region of low pressure, they lose stability and acquire the ability to grow unlimitedly. After going to the zone increased pressure and exhaustion of the kinetic energy of the expanding fluid, the growth of the bubble stops and it begins to contract. If the bubble contains a lot of gas, then when it reaches the minimum radius, it is restored and performs several cycles of damped oscillations, and if there is little gas, then the bubble completely closes in the first period of life. Therefore, near the streamlined body (obstacle), a rather clearly defined “cavitation zone” is created, filled with moving bubbles.
  • the contraction of the cavitation bubble occurs at high speed and is accompanied by a sound pulse (water hammer), the stronger, the less gas the bubble contains. If the degree of cavitation development is such that many bubbles appear and collapse at random times, then the phenomenon is accompanied by strong noise with a continuous spectrum from several hundred Hz to hundreds and thousands of kHz. An increase in the flow rate after the onset of cavitation causes a rapid increase in the number of cavitation bubbles, after which they are combined into a common cavitation cavity.
  • the velocity of the processed medium should be sufficiently high (based on the experience of more than 5 m / s) so that the bubbles do not managed to slam close to the body, and slam away from the streamlined body, then cavitation will be voluminous and will not lead to the destruction of the streamlined body.
  • the acoustic and cavitation processing device (turbodynamic disintegrator) is equipped with two inlet pipes for two inlet media (medium 1 is raw material, medium 2 in this case, VKF), two vortex inserts (swirlers) for two inlet media, and a cylindrical mixing chamber for input media installed directly after the input swirls.
  • the diameter of the mixing chamber is chosen so that the speed of the mixture is greater than 0.1 m / s, usually from the range 0.1 - 10 m / s, but this speed may be greater.
  • the specific speed value is determined by the analysis of fractions obtained as a result of processing and products i.e. determined experimentally depending on the feedstock and the task.
  • Partial cavitation and acoustic treatment of the input media and their mixtures occurs already in swirls when the media move at high speeds, and in the mixing chamber, when raw materials and VKF are heated to a high temperature, but the effect is enhanced when the main cavitators are installed.
  • the cylindrical chamber can be interspersed with confuser and diffuser inserts, which leads to an increase in the velocity of the transverse motion of the media, an increase in the amplitude of the transverse vibrations and an increase in the process of mixing the two media (the parameters of the inserts are determined empirically depending on the composition of the raw material and the task).
  • the cavitator is installed after the mixing chamber and is made in the form of a flat, concave or convex (as one of the options - in the form of a cone) along the movement of the mixture of two input media of the figure, installed across the flow and closing the entire flow cross section.
  • a flat, concave or convex as one of the options - in the form of a cone
  • the cavitator is installed after the mixing chamber and is made in the form of a flat, concave or convex (as one of the options - in the form of a cone) along the movement of the mixture of two input media of the figure, installed across the flow and closing the entire flow cross section.
  • an outlet swirler is located for a mixture of input media (to improve dispersion of the mixture) and a nozzle.
  • the swirls and nozzle are designed so that the flow velocity in the channels of the swirls and nozzle is higher than 5 m / s.
  • the specific value of the velocities in the holes of the cavitator and the channels of the swirler is determined by the results of the analysis obtained as a result of processing fractions and products, i.e. determined experimentally depending on the feedstock and the task.
  • the swirl channels are made in the form of two-start or multi-start (the number of channels is at least two, optimally 2 ⁇ 3) tangential channels or channels in the form of Archimedes spirals (linear function in polar coordinates, easy to manufacture), screw or screw spirals, twisting channels of another shape .
  • the ratio of the height of the channel (spiral) to its width is in the range from 1 to 10.
  • the rotation of the medium in the channels can be either left or right, the direction of rotation of the two media can coincide and / or be multidirectional, this does not give a big difference in the results.
  • the location of the cavitator between the mixing chamber and the output swirl for the mixture of input media and the nozzle is selected from the condition of maximum intensity of cavitation and acoustic effects on the mixture of input media, which is also determined experimentally.
  • the holes in the cavitator can be in the form of rectangles, asterisks, ellipses and other flat figures (as one of the options with sharp jagged edges), and the shape and dimensions of the figures are chosen so that the ratio of the perimeter of the figure to its area is maximum to increase the zone of flow stall.
  • the dimensions of the holes (the minimum and maximum distances between the two points of the perimeter of each hole) are in the range from 0.1 to 100 mm, and the medium velocity in each hole exceeded 5 m / s.
  • the device can be installed 2 or more cavitators, which leads to an increase in the nodes and zones of formation of cavitation.
  • the distance between the cavitators, as well as the distance between the mixing chamber, cavitators and the nozzle, is selected from the condition of maximum intensity of cavitation and acoustic impact on the mixture of input media, determined empirically.
  • the cavitator can be made in the form of filling balls, cylinders, parallelepipeds, sprockets, tori, dumbbells, Raschig rings and other rigid volumetric figures.
  • volumetric figures are in the range from 0.1 to 100 mm, the velocity of the medium in all the gap between the backfill elements must exceed 5 m / s.
  • the filling can be inserted into a container, for example, mesh, for the convenience of changing elements of various filling and moving the cavitator (container) along the axis of the processing device to find the optimal location to create maximum intensity of cavitation and acoustic effects on the mixture of input media.
  • the number of containers may be more than one, and with various filling.
  • the gas part of the mixture at operating pressure should not exceed 25% (otherwise the cavitation effect worsens) mass and is regulated by the pressure in the device.
  • the nozzle is made in the form of a cylinder, cone or Laval nozzle, as well as another shape based on the goal of better atomization of the mixture.
  • a plant in which the raw materials and circulating VKF are mixed before the VKF heating furnace, and the heated mixture is further supplied to the acoustic and cavitation processing device (turbodynamic disintegrator), then a mixture of raw materials and VKF is fed to each inlet pipe of the processing device, and the number of inlet pipes may be more than two.
  • fittings or nozzles for introducing molecular hydrogen and / or light hydrogen-containing media and / or active hydrogen and / or light radicals into the mixing chamber and / or into the treatment zone in front of and / or behind the cavitator, or the device (unit) for producing active hydrogen and / or light radicals is integrated into the processing device.
  • the cavitator is made in the form of a cone or a convex along the flow of the figure in the form of a cone or a truncated cone with an angle at the apex of the cone of more than 10 degrees, and on the entire surface of the cavitator as the nodes of the formation of cavitation zones made through holes with an effective diameter of from 0.1 to 100 mm
  • the number of outlet swirlers and / or nozzles built into the processing device can be more than one of each type.
  • the cylindrical sections of the mixing chamber but also the cylindrical sections of the motion of both media before mixing can be interspersed with confuser and / or diffuser inserts. With a large gas part and high pressure in the device, the output swirl may not be used.
  • Raw materials heated by circulating VKF to subcritical temperature (vibrational levels of molecules are already excited, but avalanche-like breaking of molecules due to this excitation still does not occur) is sent to a processing device in which the raw materials are subjected to mechanical (for example, cavitation) and wave effects of various nature (sound, ultrasonic , cavitation, electromagnetic, light, radiation, etc.) and a wide range of resonant frequencies.
  • mechanical for example, cavitation
  • wave effects of various nature sound, ultrasonic , cavitation, electromagnetic, light, radiation, etc.
  • a wide range of frequencies is needed because the number of combinations of compounds of carbon atoms, hydrogen and other elements, especially in polyatomic molecules the raw material is very large, and has not yet been studied in detail; therefore, the number of different vibrational levels excited by preheating is also very large.
  • thermomechanical cracking process i.e. the process of breaking bonds of already excited molecules
  • the initiated process of breaking bonds by applying a resonant action is controlled by the intensity and nature of the applied effect.
  • the thermomechanical cracking process becomes controllable rather than avalanche-like, which leads to a decrease in coking of equipment, an increase in its overhaul mileage, the process is continuous. Because the raw materials are already heated almost to a critical state, processing it with any type of exposure does not require large energy costs, i.e. initiating resonant action allows you to control the process.
  • thermomechanical initiated cracking are better than the products of thermal cracking, they have fewer gases and unsaturated compounds, and the yield of light products is 1.5-15 times higher than their potential content in raw materials depending on the composition of the raw materials (heavy oil, fuel oil, etc.). d.). Because the wave action is applied to activate the breaking of bonds already in the excited molecules, its energy is spent only on the activation and control of the thermomechanical cracking process, then the energy costs are low. Chemical reagents and catalysts are not used in the process. Thus, cracking can occur in three devices: in a circulating VKF heating device, in a raw material and VKF mixing device, and in a processing device (thermomechanical cracking). Depending on the composition and properties of the raw materials, the technological parameters of the process and the task, cracking can occur in only one device, in any two or all three.
  • the raw materials are sent to the evaporation and separation apparatus, in which the vapor-gas part (low boiling fractions of NKF) is separated from the liquid (high boiling fractions of VKF).
  • the heated mixture of raw materials and VKF is dispersed (sprayed) into a separation apparatus to increase the interfacial surface and more efficiently separate the gas-vapor part from the liquid.
  • NKF the light part of the gas-vapor separation (low boiling fractions of NKF), with a boiling point predominantly up to 350-360 0 C, which can be called very light oil or gas condensate, and a heavy high molecular weight part or liquid separation residue (high-boiling fraction of VKF separation).
  • NKF consists mainly (80-90% due to non-ideal separation) of fractions with a boiling point up to 350-360 0 C.
  • fuel products such as gasoline are produced from NKF (boiling range: boiling point - 180- 200 0 C), kerosene (boiling range: 180-200 0 C - 230-240 0 C), diesel (boiling range: 230-240 0 C - 350-360 0 C), petrochemicals such as toluene benzene and others.
  • NKF boiling point - 180- 200 0 C
  • kerosene low-200 0 C
  • diesel boiling range: 230-240 0 C - 350-360 0 C
  • petrochemicals such as toluene benzene and others.
  • VKF consists of heavy fractions with a boiling point predominantly above 350-360 0 C.
  • VKF can produce heavy commercial products, such as coke, bitumen, bitumen emulsions, coatings. In the future - heavy commercial products.
  • the boundary separation temperature of 350-360 0 C is chosen because the end of boiling of diesel fuel is 350-360 0 C. If the guests and requirements for fuel products change over time, the boundary separation temperature can be changed accordingly.
  • Units for the production of commercial products usually include the following well-known processes: hydrotreating, reforming, platforming and other well-known processes (for producing gasoline, kerosene, diesel fuel), processes of the petrochemical and chemical industries, or at the first stage compounding, bitumen block for the production of oxidized bitumen or bitumen block, combined with a vacuum block for the production of non-oxidized bitumen, as well as equipment for the production of bitumen coatings, emulsions, boiler fuel, coke and other commercial products (Petrochemical Handbook. Two volumes. Volume 1, edited by Ogorodnikov CK. L. Chemistry, 1978, pp. 53-55).
  • VKF for heating the liquid phase (it does not need to be specially prepared or purchased, it appears during the implementation of the invention) with a boiling point predominantly above 360 0 C allows you to increase the operating temperature in the separation apparatus, to intensify thermal and / or thermomechanical cracking and, accordingly, increase the depth of processing and the yield of light products above their potential content in the feedstock, as well as simplify and reduce the cost of equipment and reduce energy and operational costs, and also allows optimal and rational use of raw materials, because with in-depth processing, a smaller amount of oil or other liquid hydrocarbon feedstock is required to obtain a certain amount of marketable products.
  • a high temperature for example, up to 400 0 C and higher, depending on the process conditions
  • colder oil or other liquid hydrocarbon feedstocks for example, at a temperature of 200 0 C
  • the circulating VKF must be heated not lower than 300 0 C, and the preliminary heating of the raw material before mixing it with the VKF should be no higher than 450 0 C in order to avoid coking.
  • part of the VKF necessary for heating the raw material to a subcritical temperature circulates in a closed circuit: the separation apparatus — the heating furnace (heater) VKF — the separation apparatus, and the ratio of the circulating VKF to the raw material is in the range of l ⁇ SO.
  • VKF must be heated before it is mixed with raw materials (in contrast to the method according to copyright certificate SU 1558879, in which a mixture of raw materials and a heavy separation residue is heated, which leads to an increase in pressure in the coil due to the presence of light fractions in the raw material, plugs, coking, etc., while the heating temperature cannot be raised above 380 0 C, which ultimately leads to only 69-78% of light petroleum products from their potential content in the feedstock and to speak here about increasing depth foreman edema, i.e. obtaining light light products above their potential content in raw materials, is not necessary).
  • Raw materials and VKF can be heated in the same furnace or heater, but in separate coils.
  • a device for heating raw materials by direct contact with VKF to a subcritical temperature devices for processing, dispersing and separating raw materials into combined-cycle and liquid phases are combined in one apparatus, which leads to a decrease in the amount of equipment and lower capital and operating costs.
  • the vapor-gas part of the NKF separation due to the intensively conducted process of evaporation and separation, contains, in addition to light fractions in a gaseous form, and liquid droplets containing heavy high-boiling components with a boiling point above 350 - 360 0 C. Therefore (if necessary, t. to.
  • NKF NKF sent to the separation device (drop separation, filtration or rectification), usually built into the separation apparatus, then sent for further use and receipt of goods ny products, since NKF contains mainly gas, gasoline, kerosene and diesel fractions, petrochemical products.
  • the filtrate after separation devices is sent for re-treatment to obtain an additional amount of light target fractions and increase the depth of processing.
  • the vapor phase of the NFC it is advisable to direct the vapor phase of the NFC to, for example, rectification and further production of light commercial fuel products or petrochemicals on the spot, or, after cooling, to realize for further advanced processing as high-grade oil, similar in composition to gas condensate (the content of light products - gasoline, kerosene and diesel fractions - up to 90% or more in the combined cycle gas condensate fraction).
  • the liquid part of the VKF after the separation apparatus is fed, for example, to a bitumen reactor with a vacuum column to obtain marketable bitumen or other heavy products such as bitumen emulsions, coatings, etc. on site, or, after cooling, they are sold as intermediates for further processing.
  • the processing unit In the process of cracking the feed, unsaturated hydrocarbons are formed, which can subsequently condense, which leads to a limitation of the processing depth.
  • the processing unit For the most complete and deep processing and increase the yield of light target products and fractions, the processing unit should be supplemented with a device that allows saturating open bonds with atomic hydrogen and / or light radicals with minimal costs.
  • the problem can be solved by such a process organization in which the feed and the catalyst do not contact, as a result of which the catalyst is practically not poisoned by harmful impurities and does not coke, which leads to an increase in the durability of the catalyst and the absence of the need for regeneration processes.
  • the raw material or part thereof is subjected to the processing process according to this invention repeatedly.
  • molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen for example, associated gas, natural gas, including gas obtained during preparation and advanced processing, pentane fractions, xylene, toluene, some light fractions, including obtained in the process of preparation and deep processing, etc., if necessary, they are heated and sent to produce active atomic hydrogen and / or light radicals to a reactor with a catalyst heated to the required temperature (atomic hydrogen production unit ode), after which the active hydrogen and / or light radicals are sent to the cracking devices for the reaction, to the heating device and VKF cracking, into a device for mixing heated VKF and raw materials, into a thermomechanical cracking device, in which a mixture for initiating a controlled process of breaking bonds of molecules (thermomechanical cracking) is subjected to mechanical and wave effects of a different nature and a wide range of frequencies, for example, cavitation, sound, ultrasonic vibrations moreover, atomic hydrogen and / or light radicals can be directed only to
  • atomic hydrogen and / or light radicals can be introduced into the separation device for reaction with NKF, in which there are radicals cracking raw materials and VKF. This will lead to a decrease in unsatisfactory in the NKF and improve the quality of the final products. It is also useful to introduce atomic hydrogen and / or light radicals in NKF and VKF after the separation apparatus to improve their quality. It is also useful to introduce molecular hydrogen and / or light hydrogen-containing media into all of the above devices and between them, but the effect will be much weaker, because the probability of the formation of atomic hydrogen and / or light radicals under the influence of cavitation and acoustic vibrations is much less than in a reactor with a catalyst.
  • the pressure in the reactor with the catalyst should be greater than the pressure in the cracking devices.
  • atomic hydrogen and / or light radicals saturate open bonds of unsaturated hydrocarbons to obtain light target fractions, and with repeated re-treatment of VKF, almost 100% of the processing depth and yield of light target products can be achieved.
  • the reaction products are sent to the units for obtaining marketable products, or sent to the separation apparatus, light target reaction fractions after the separation apparatus, mainly with an end temperature boiling up to 350-360 0 C, sent to the unit for obtaining the target marketable products such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products at the place of preparation and deep processing of raw materials according to this invention or transported to a remote processing site to obtain light marketable products.
  • the target marketable products such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products at the place of preparation and deep processing of raw materials according to this invention or transported to a remote processing site to obtain light marketable products.
  • the heavy residue after the separation apparatus (VKF), mainly with a boiling point of 350-360 0 C, is sent to the block for the production of heavy commodity products such as bitumen, coke, or partially or completely sent for re-processing according to this invention at the beginning of the process.
  • Solid hydrocarbon feedstocks e.g., coal, shale, vegetable products
  • gaseous hydrocarbons are also introduced into the feedstock and / or a separation residue before it is processed
  • liquid, solid and gaseous hydrocarbons can be processed in the proposed installation simultaneously, individually or in pairs.
  • Part of the gaseous and / or light products they are enriched with hydrogen and can replace the original hydrogen-containing media) separation can be returned to the beginning of the process in a reactor with a catalyst to produce active atomic hydrogen and light radicals.
  • Light radicals obtained by detaching active atomic hydrogen from used hydrogen-containing media also attach to light cracking radicals of the feed, saturate their open bonds and form target fractions. If they (or atomic hydrogen) are attached to the heavy radicals of the cracking of the feed, then after the separation apparatus the heavy reaction residue (VKF) is sent partially or completely to the reprocessing according to this invention, or partially or completely to obtain heavy commercial products such as coke, bitumen ( depending on the task).
  • VKF heavy reaction residue
  • much more light radicals are formed during cracking of raw materials, than heavy because most likely, a long raw material molecule breaks in about the middle, and with a much lesser probability is a very small and very large radical.
  • the separation residue can be sent for re-treatment at the beginning of the process together with the feedstock, or separately for an additional processing unit according to this invention.
  • VKF heavy separation residue
  • the reactor with the catalyst is made in the form of a cylinder, ball, annular cylinder, parallelepiped (plate) or other volumetric figure, for example, in the form of a tubular coil, with the catalyst placed in it in the form of granules of arbitrary size and shape, the surface of the reactor is permeable to hydrogen atoms and / or light radicals, or holes of arbitrary shape are made on the surface of the reactor, the holes being smaller than the size of the catalyst granules.
  • the walls of a reactor with a catalyst are made of porous material with various pore sizes, for example, in the nanometer range.
  • the reactor with the catalyst may not contain granules or powder of the catalyst, while the shell of the reactor or the entire reactor is made entirely of material that is a catalyst for carrying out the process of producing atomic hydrogen and / or light radicals from molecular hydrogen and / or hydrogen-containing media.
  • Multiple reactors with catalyst (reactor bags). Reactors or reactor packages can be located along the movement of raw materials, across or at an angle.
  • the catalyst body has a collector for distributing hydrogen and / or hydrogen-containing media.
  • the number of hydrogen atoms and / or light radicals produced in the reactor with the catalyst must exceed the number of open bonds of the cracking radicals of the feedstock, and the ratio of the surface of the reactor (reactor pack) with the catalyst to the volume of the heating and / or cracking zone is increased so as to maximize the reaction raw materials and atomic hydrogen and / or light radicals.
  • Distinctive features of this installation and devices for the preparation and processing of hydrocarbon raw materials allow several processes to be carried out: heat transfer, cavitation and acoustic treatment, evaporation, separation, separation, initiated thermomechanical cracking intensively and simultaneously in one apparatus with minimal capital and operating costs with an increase in the depth of further processing and obtaining high-quality intermediates for further use.
  • FIGS. 1 to 5 show enlarged schematic diagrams of a hydrocarbon feed preparation and processing unit.
  • FIG. 1 - 5 are indicated: 1 - a device for heating or heating and thermal cracking of VKF; 2 - a device for mixing heated VKF and raw materials and heating the raw materials to subcritical temperature; 3 - a processing and thermomechanical cracking device in which a mixture of raw materials and VKF to initiate a controlled process of breaking bonds of molecules (thermomechanical cracking) is subjected to mechanical and wave effects of a different nature and a wide range of frequencies, for example, cavitation, sound, ultrasonic vibrations; 4 - device for spraying (dispersing) the mixture into the apparatus separation; 5 - separation apparatus; 6 - separation device (filtration, droplet separation, rectification) NKF; 7 - a device for isolating the circulating part of VKF with a sump for cleaning from mechanical impurities and coke particles; 8, 9 - recuperative heat exchangers for preheating of raw materials; 10 - unit for the preparation of light target commercial products (gasoline, kerosene,
  • the unit for preliminary purification of raw materials (degassing, dehydration, desalination, purification from mechanical and other harmful impurities) is not shown in the figures for simplicity, nor are the final cooling and condensation units of NKF and VKF in case of their transportation to a remote place of production of marketable products.
  • Units for the production of commercial products usually include the following known processes: hydrotreating, reforming, platforming and others, processes of the petrochemical and chemical industries, or at the first stage a compounding unit, a bitumen block for the production of oxidized bitumen or a bitumen block combined with a vacuum block for the production of non-oxidized bitumen, as well as equipment for the production of bitumen coatings, emulsions, boiler fuel, coke and other commercial products (Handbook of Petrochemistry. In two volumes. Volume 1, under edited by Ogorodnikov CK. L., Chemistry, 1978, p. 53-55).
  • the circulating high-boiling fractions of the VKF after the separation apparatus are fed to the heating and cracking device of the VKF (Fig. 1, position 1), then to the mixing and heating device of the raw materials (Fig. 1, position 2).
  • Prepared raw materials after preheating in recuperative heat exchangers (Fig. 1, item 8, 9) are also fed to the mixing device with VKF (Fig. 1, item 2).
  • the mixture of raw materials and VKF is fed into the processing device (thermomechanical cracking) (Fig. 1, position 3), then the mixture is dispersed (sprayed) (Fig.
  • the filtrate after the separator for I receive an additional amount of light target products returned for reprocessing at the beginning of the process along with the circulating part of the VKF.
  • Part of the high boiling VKF fraction after the separation apparatus after the circulating VKF separation device (Fig. 1, position 7) is returned for reprocessing (recycling) according to this invention to the beginning of the process to increase the yield of light products and the processing depth, and the returned part of the VKF is circulated in a closed circuit - separation apparatus (Fig.
  • furnace heating (heater) (Fig. 1, position 1) is a separation apparatus.
  • the other part of the HCF is sent (transported) after partial cooling on a recuperative heat exchanger (Fig. 1, item 9) and final cooling (not shown in the installation diagram for simplicity) to the unit for producing heavy commercial products (such as coke, bitumen, bitumen emulsions, coatings, oils).
  • FIG. 2 NKF after partial cooling on a recuperative heat exchanger (Fig. 2, position 8) is sent to the unit for obtaining light commercial products (Fig. 2, position 10), and VKF after partial cooling on a recuperative heat exchanger (Fig. 2, position 9) is sent in the block receiving heavy commercial products (Fig. 2, position 11).
  • the bottom residue after the block for the preparation of light commercial products, as well as the light distillation after the preparation of heavy commercial products to increase the depth of processing and yield the target light products, are returned for reprocessing at the beginning of the process together with raw materials or circulating HCFs.
  • the raw materials are preheated on a separate heater (Fig. 3, item 12), or in the same heater (furnace) in which the circulating VKF is heated, but in a separate coil (Fig. 4, position 1).
  • the raw materials can not only be heated, but also subjected to thermal cracking. If necessary, you can use separate heaters in conjunction with recuperative heat exchangers to preheat raw materials. For Preheating can also use the heat of commercial products.
  • the processing unit is supplemented (Fig. 5) with a device for producing atomic hydrogen and / or light radicals from molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, natural or associated gas , in particular gas and light shoulder straps of gasoline fractions obtained during processing, which are sent to cracking devices — to the heating and cracking device VKF (Fig. 5, position 1), to the mixing device heated VKF and raw materials (Fig. 5, position 2), into the thermomechanical cracking device (Fig.
  • atomic hydrogen and / or light radicals can be sent only to one of the cracking devices, to any two devices and to all three cracking devices.
  • atomic hydrogen and / or light radicals saturate open bonds of unsaturated hydrocarbons with obtaining light target fractions, and with repeated reprocessing of VKF (VKF is completely sent for reprocessing and is not used for the production of heavy commodity products, as shown in Fig. 5) almost 100% of the processing depth and yield of light target products can be achieved.
  • FIG. 6 shows a separation apparatus. Heated to the required temperature VKF and heated raw materials are fed into the mixing device (Fig. 6, position 2), in which the raw material is heated to subcritical temperature. Then the mixture of raw materials and VKF is sent to the device thermomechanical cracking (Fig. 6, position 3), in which a mixture to initiate a controlled process of breaking bonds of molecules (thermomechanical cracking) is subjected to mechanical and wave effects of a different nature and a wide range of frequencies, for example, cavitation, sound, ultrasonic vibrations, Then the mixture is dispersed ( spray) (Fig. 6, position 4) with a decrease in pressure to increase the interfacial surface of the separated media in the separation apparatus.
  • the mixing device Fig. 6, position 2
  • thermomechanical cracking a mixture to initiate a controlled process of breaking bonds of molecules
  • mechanical and wave effects of a different nature and a wide range of frequencies, for example, cavitation, sound, ultrasonic vibrations
  • TDD turbodynamic disintegrator
  • the number of built-in TDD in the separation apparatus depends on the performance of one TDD and the total productivity of the processing industry.
  • NKF formed in the gas-vapor form are sent to the separator (Fig. 6, position 6) located in the upper part of the separation apparatus.
  • Separated (filtered) NKF are sent to the unit for the preparation of light commercial products, and the filtrate by gravity enters the lower part of the apparatus and mixes with VKF. All obtained VKF using a device for isolating the circulating part of the VKF (Fig. 6, position 7) are divided into 2 parts.
  • One part is sent to the blocks for obtaining heavy commodity products, the other is sent to heating and then to the mixing device with raw materials and reprocessing (for recycling), and this part circulates in a closed circuit: separation apparatus - VKF heater - separation apparatus.
  • the device for isolating circulating HCFs is made with a sump for purification of mechanical impurities and coke particles so that cleaner HCFs are selected for recycling.
  • various filtering devices can be provided in the VKF circulation loop, for simplicity on figures not shown. Fittings for input-output of working and product media, fittings and devices for monitoring the technological parameters of the apparatus (temperature, pressure, phase separation level) are built into the body of the separation apparatus.
  • the temperature in the separation device corresponds to the maximum boiling point of the fractions of light target commodity products, for example 350-360 0 C for the diesel fraction and is maintained automatically, the level of separation of the vapor-gas phase of the NKF and the liquid phase of the VKF is lower than half the height of the separation apparatus.
  • the temperature of the phase interface 350-360 0 C is chosen because at present the temperature of the end of boiling of diesel fuel is in this range. If the requirements change, then this temperature will also be changed in the right direction. Distillation plates, Raschig rings can be built into the separator.
  • FIG. 7 - 9 indicated: 14 - swirl for medium 1 (in this case, for raw materials); 15 - swirl for medium 2 (in this case, for heavy high-boiling fractions of VKF); 16 - mixing chamber; 17 - cavitator in the form of a truncated cone with holes; 18 - output swirl for a treated mixture of input media; 19 - nozzle.
  • FIG. 8 shows a device with alternating cylindrical, confuser and diffuser inserts for moving medium 1, two cavitators with holes and a nozzle in the form of a cone.
  • FIG. 9 shows a device with alternating cylindrical, confuser and diffuser inserts for moving medium 1 and a mixture of media 1 and 2, a cavitator in the form of a mesh basket with filling in the form of balls and a cylindrical nozzle.
  • the device operates as follows. Preheated raw materials (medium 1) are sent to a swirler for raw materials (Fig. 7-9, position 14), heated to high temperature VKF (raw materials 2) are sent to a swirler for VKF (Fig. 7-9, position 15). As a result of direct contact of the feed and VKF in the mixing chamber (Fig. 7-9, item 16), the feed and the entire mixture are heated to a critical temperature. Then the heated mixture of raw materials and VKF is sent to the cavitator (Fig.
  • the present invention is implemented in a pilot plant for the separation of oil and other liquid hydrocarbon feeds with a capacity of up to 30 kg / h, in which all processes and devices for implementing the invention are implemented.
  • the installation is equipped with various capacitive equipment for storing raw materials and collecting the resulting products, heat exchange equipment for heating the raw materials, heating circulating HCFs and cooling products, pumping equipment and instrumentation.
  • the layout of the bench installation is shown in FIG. 1, the separation apparatus — in FIG. 6, a turbodynamic disintegrator - in FIG. 7.
  • the feedstock used was the oil of the Vishenskoye deposit in the Ulyanovsk Region (Ratov AH, Nemirovskaya GB. Problems of oil development in the Ulyanovsk Region.
  • Oil contains many tarry compounds and impurities. Used oil and other fields, such as NGDU "Nurlatneft", with a different composition, as well as various bottoms, waste oils and other raw materials.
  • the pressure of raw materials and circulating HCFs in bench experiments was up to 1.0 MPa and higher, the temperature of circulating VKFs was up to 450 0 C and higher, the temperature of raw materials was up to 200 ⁇ 250 0 C, the ratio of flowing circulating VKF and raw materials was in the range up to 30 and more.
  • the linear feed rates of the feed and circulating VKF were more than 5 m / s
  • the separation and processing efficiency increases nonlinearly.
  • the choice of the value of the feed rates for a particular technological process depends on the properties of the raw materials, the task at hand and is optimized for several factors, including the economic factor.
  • VKF is prepared.
  • VKF which is essentially a heavy separation residue
  • VKF can be prepared in various ways, for example, using a simple process of single evaporation of a mixture of hydrocarbons.
  • the simplest method, which was used when working on a bench installation, is as follows.
  • the required amount of liquid hydrocarbon feed is poured into the separation apparatus.
  • the separation apparatus Fig. 1, 6, position 5
  • the mixture is pumped to an electric heater - an analog of an industrial furnace (Fig. 1, position 1) and returned.
  • light fractions are continuously removed, accumulating the liquid phase of VKF.
  • VKF heavy residue
  • circulating VKF pumps are fed to swirlers (Fig. 7, position 14, 15), then to the mixing device (Fig. 1, 6, position 2, Fig. 7 , position 16).
  • a mixture of raw materials and VKF is fed to a mechanical and wave processing device (Fig. 1, 6, position 3, Fig. 7, position 17), in which thermomechanical hydrodynamic cracking of raw materials, then the treated mixture is sent to the outlet swirler (Fig. 7, position 18) and dispersed through the nozzle (Fig. 1, 6, position 4, Fig. 7, position 19) into the separation apparatus (Fig. 1, position 5).
  • the circulating VKF is again sent to the heating device (Fig. L, position 1), i.e. for recycling.
  • the gas-vapor part (NKF) after the separation apparatus (FIG. 1, position 5) is sent to the separation device (droplet separation, filtration or rectification), (FIG. 1, 6, position 6), after which the filtrate returns to the beginning of the process together with circulating VKF for reprocessing and additional obtaining of light products above their potential content.
  • the gas-vapor part after the separation device (Fig. 1, 6, item 6) is sent for cooling and condensation and is analyzed.
  • the liquid separation part (VKF) after the separation apparatus (Fig. 1, position 5) and separation from the VKF of the circulating part (Fig. L, 6, position 7) is sent for cooling and analyzed.
  • Atmospheric - vacuum distillation of the bottoms of Ulyanovsk oil after an atmospheric column (fuel oil) showed the absence of a gasoline fraction in it, the content of the kerosene fraction (240 - 360 0 C) amounted to 2.9% of the mass, diesel fraction (240 - 360 0 C) - 11, 8% of the mass.
  • the number of low boiling fractions (NKF - the easy part of the separation) was 74 - 79% by weight, depending on the process parameters.
  • the NKF content of the target fuel compositions was 88 - 90% mass, of which gasoline (NK - 180 0 C) fractions - 20.8% mass, kerosene (180 - 240 0 C) - 17.4% mass, diesel (240 - 360 0 C) - 61, 8% of the mass.
  • the total content of the target products with a boiling point up to 360 0 C increased from 14.7% by mass to 71% by mass in terms of the initial product.
  • Atmospheric - vacuum distillation of unused oil M - 8B showed the absence of gasoline and kerosene fractions in it, the content of the diesel fraction was 5.2%, the bulk of the oil was distilled in the boiling range 380 - 500 0 C.
  • thermomechanical cracking of high-boiling above 360 0 C
  • oil components into the target products with a boiling point up to 360 0 C
  • the content of the target components with a boiling point up to 360 ° C during the thermomechanical cracking of used oil was 72%.
  • molecular hydrogen and / or light hydrogen-containing media for example, propane - butane from a cylinder
  • the yield of light light fractions will be much lower, and reaches values of 75 - 78%.
  • the amount of unsaturated hydrocarbons in the NKF after the separation apparatus was 27 - 31%, and with the use of a device with a catalyst in the separator (for simplicity in Fig. 6, the device with a catalyst shown) amounted to 18 - 20%. If molecular hydrogen or propane - butane is introduced from a balloon into a device with a catalyst in the separator, the unsaturated amount decreases to 10-12%, and when atomic hydrogen and / or light radicals are used after the reactor with the catalyst, the unsaturated amount decreases to less than 2% .
  • a promising option is that in which the vapor-gas part of the NKF and the liquid part of the VKF obtained after the separation apparatus partially chilled if necessary, mixed again.
  • the resulting “synthetic” oil contains about two or more times more fuel fractions than the original product.
  • the kinematic viscosity, respectively from 83 cSt to 6 cSt.
  • the cost of “synthetic” oil increases significantly; it is easier to transport and process.
  • the present invention allows for industrial in-depth (at the same time there is an increase in the depth of further processing by 1.5-15 times depending on the feedstock - heavy oil, fuel oil, etc.) and highly cost-effective preparation and processing of oil, including heavy, residues of oil refining and petrochemical industries, oil sludge, waste oils, natural bitumen and other liquid and gaseous organic media to produce tested commercial products and can be used in the production of hydrocarbon fuels, petrochemicals, coke, bitumen, etc. Accordingly, the yield of the most valuable and expensive fuel compositions — gasoline, kerosene and diesel fractions, and petrochemical products — is also increasing.

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Abstract

L'invention concerne les industries pétrolière, pétrochimique, chimique et des combustibles énergétiques, et plus particulièrement le traitement d'une matière première hydrocarbonée. La présente invention permet d'augmenter le rendement de produits cibles légers et d'augmenter la profondeur du traitement industriel de ladite matière. Cette dernière est chauffée par un contact direct avec des fractions à poids moléculaire et à point d'ébullition élevés, jusqu'à une température sous-critique inférieure à la température du début du craquage thermique incontrôlé à effet "boule de neige". Puis, un mélange de matière première et de fractions à poids moléculaire élevé destiné à initier un processus régulable de rupture de liaisons moléculaires, à savoir un craquage thermo-mécanique, est soumis à une action mécanique et ondulatoire de fréquences de spectre large et de nature diverse. L'invention permet également d'augmenter la profondeur de traitement de 1,5 à 15 fois, selon la composition de la matière première de départ. Ainsi, le rendement des compositions combustibles les plus précieuses et les plus chères augmente également, à savoir les compositions de fractions d'essence, de pétrole et de diesel et de produits pétrochimiques. L'assemblage et les dispositifs selon l'invention sont simples à exploiter et ne nécessitent pas de dépenses d'installation et d'exploitation importantes.
PCT/RU2010/000065 2009-04-06 2010-02-15 Assemblage et dispositifs de traitement en profondeur de matiere premiere hydrocarbonee WO2010117300A1 (fr)

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RU2534618C2 (ru) * 2012-09-14 2014-11-27 Владимир Сергеевич Баев Способ переработки углеродсодержащего и углеводородсодержащего сырья
RU2749262C1 (ru) * 2020-07-21 2021-06-07 Константин Витальевич Фёдоров Установка по глубокой переработке мазута
RU2768668C2 (ru) * 2020-05-26 2022-03-24 Василий Дмитриевич Мушенко Установка термического крекинга тяжелых нефтяных остатков

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RU2115176C1 (ru) * 1997-03-26 1998-07-10 Институт теплофизики СО РАН, Мальцев Леонид Иванович Генератор кавитации
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2534618C2 (ru) * 2012-09-14 2014-11-27 Владимир Сергеевич Баев Способ переработки углеродсодержащего и углеводородсодержащего сырья
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RU2749262C1 (ru) * 2020-07-21 2021-06-07 Константин Витальевич Фёдоров Установка по глубокой переработке мазута

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