RU2467053C2 - Method of separating liquid and heterogeneous gas systems and mechanical fractionator to this end - Google Patents

Abstract

FIELD: process engineering.

SUBSTANCE: invention relates to production of motor fuel and lubricants from crude oil and other heterogeneous systems and may be used in chemical industry in production of multicomponent products at simple equipment in destructive process. Particularly, it relates to thermomechanical and chemical fractionator including sequential oil or oil product pre-destruction zone, riser, alternating 100°C, 220°C, 315°C and unit of multiple-shell reactor with final boiling point of 450°C to 850°C that allows lateral discharge of finished product. Invention relates also to method of separating liquid and heterogeneous gas systems.

EFFECT: production of motor fuels from heterogeneous system.

6 cl, 18 dwg

Description

Application area

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.

State of the art

A known method of producing a destructive material and a worm-disk extruder to obtain a product (RU No. 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, before the destruction of the high molecular weight compounds in the disk nozzle, they are preliminarily destroyed in a screw extruder, and the high molecular weight compounds in the disk nozzle are destroyed at a temperature a melt equal to or lower than at the exit of the screw extruder.

The disadvantage of this method is the length of the process, as well as the inability to use to accelerate the process of surface-active substances (surfactants) and the separation of the material into fractions. In addition, 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 destruction processes and does not allow the effective management of the destruction process.

The closest in technical essence to the claimed technical solution is the description of the invention to patent RU 2220847 C2, an extruder screw that increases the homogeneity of thermoplastic foam, related to the prior art in the field of mixing molten thermoplastics with a blowing agent such as fluorocarbon or hydrocarbons (propane, butane, pentane and etc.), and also possibly with other agents, in an isolated medium the material moves along the cylinder, being in frictional contact and shear, heats the material to melting phrases. This problem is solved by an elongated worm shaft located in the extruder cylinder.

However, the known device 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 when moving along the construction channels does not release low-boiling fractions of the gases of the first stage and light products, 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 many blades remote from the inner surface of the cylinder.

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 (crude oil) into separately functional products by mechanothermal treatment using catalysts and increasing the ratio of hydrogen to carbon (n / s) at each stage of the process the purpose of obtaining a 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 deep cleavage of oil molecules and get high-quality distillate of motor fuels and oils, which relates to the chemical processing of raw materials at elevated local temperatures and local pressure in the thin channels of the device. All chemical processes for producing distillates from oil are associated with the redistribution of hydrogen between hydrocarbon molecules, this can be expressed by the ratio N / C in hydrocarbon molecules. At elevated temperatures in thin channels, the execution of technological processes in the presence of catalysts hydrocarbons decompose instantly into components. One part of them will be enriched with hydrogen, and the other depleted, which must be enriched with them. Thus, during thermal degradation or thermocatalytic processing of raw materials, we obtain hydrocarbons with different H / C ratios. Forced reactions of hydrocarbons with hydrogen lead to an increase in the H / C ratio in the residual products of their processing. Consequently, if the required amount of hydrogen is introduced into the reaction zone, then it is possible to obtain a heterogeneous system with a composition close to the composition of the original oil or oil fractions from residual solids rich in aromatic compounds, operating with the H / C ratio, choose the processing of raw materials.

The proposed method for producing the product involves the phased destruction of high molecular weight compounds with the aim of local redistribution of hydrogen between hydrocarbon molecules located in the oil feed in a series-connected pre-destruction zone, riser and in each booster unit and reactor by mechanothermochemical treatment using catalysts and donor hydrogen, see sheet 1, figure 1.

The mechanothermal effect on the group composition of the material increases the density according to the extremely critical properties of each fraction, at the ultimate pressure and critical temperature in the presence of a catalyst or without it, hydrocarbons decompose into components due to the active penetration of the gas-vapor composition into the mixture at 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 (TB) of a light gaseous fraction with a low molecular weight (see sheet 1, figure 1), a decrease in viscosity and an increase in the density of oil in the cylindrical part of the device allows mixing with an alkali solution and steam, which provides desulfurization of the material at the 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 a partial increase in pressure at the top of the conical screw device, and the destruction of oil is performed from surface friction from the screw groove interacting with helical groove in a cone-shaped sleeve, triangular activators located on the falling side of the screw screw Ali, by compression at the compression top cone and on the effects of coolant, and warming up the core parts of the conical shaft which is rotated by a drive at a speed equal to or less than 2 minutes screw shaft. As a result, at stage I, the material undergoes preliminary degradation with the release of a gas-vapor component with a boiling point up to 60 ° С and higher.

At the II stage, partially destructible material is fed through the conical openings of the unregulated disk die into the cylindrical riser body, undergoes a complex stress shift, where additional generation of the light-gas fraction is generated, mixes with alkali solution and other required agents using wedge-like activators. The lateral surface of the activators is made in the form of a wave, and the rear part is made with a semi-arc sampling, which allows you to create a bubble loop and actively perform mixing of the gas-vapor component with the liquid fraction, while additional generation of a light vapor-gas fraction, an increase in gas density, temperature, as well as oil desulfurization raw materials with subsequent supply from the riser body to the screw cavity of the reactor with the unloading of the gas-vapor fraction from it.

From the riser cavity, degraded material up to 100 ° C is fed into the screw cavity of the reactor with a fractionation column, where due to the helical groove in the sleeve, the converted substance is filled and unloaded from the evaporation cells located on the worm spiral, into the cavity. The sleeve is made with slotted slots of the diffusion type of unloading the vapor-gas mixture with a boiling point up to 100 ° C, see l.9, Fig.15. item 24. Slotted slots of the gas-vapor unloading 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 to the reactor vessel, where the processes of forcing the collisions of the catalyst particles between themselves and the surface of the comb the wall of the housing, in addition, a special agent can be supplied through the pipeline to restore the properties of the catalyst. The resulting gas-vapor mixture tends from high pressure in the reactor cavity to a fractionation column with a 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 is fed into the cavity of the riser body for re-processing, the remaining liquid mixture is fed into a series-connected unit.

At stage III, the remaining crude oil with a certain density and boiling limit of the fraction is directed along the shaft and the screw channels, fills the cells in the sleeve and the screw 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 the compression of the material between the two cells additionally releases the temperature and the gas-vapor mixture, which, released from the cells, tends to be evenly distributed in the relaxation system.

The relaxation of the stress field occurs by heat generation, the formation of new surfaces and the excitation of the 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. Next, the gas-vapor mixture is transferred to a separation column, where all processes are carried out in the likeness of the second stage.

At stage IV, the remaining liquid mixture of a certain density and with a boiling point of 220 ° -315 ° C and above is moved by a screw spiral to the naphtha (ligrein) fractionation reactor, where in the 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 the 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 (H) and through the filter enters the cavity of the separation column, where through the side unloading the product is taken from the first and subsequent plates, while the heavy fraction is fed through the discharge pipe into the cavity of the booster unit for recycling.

At stage V, the remaining mass of the mixture with a boiling point of 315-450 ° C and above is moved by a screw spiral to the “kerosene fractionation” reactor, enriched with donor hydrogen in the upper stage, increases the temperature due to a local thermochemical reaction (synthesis) that occurs in filled the cells of the sleeve and the worm spiral, in this case, the vapor-gas mixture is additionally released to obtain new surfaces with ion implantation of hydrogen in the bulk of the material, which additionally increases the 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 temperature of 315-450 ° С under pressure and high speed diffuses through the lateral slit-like discharge into the annular cavity onto the rotating catalyst, it condenses into saturated steam, 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 manual ultrasonic inspection selects the finished product and the heavy fraction is returned through the overflow pipes to the upper stage cavity.

At stage VI, the remaining mass of the mixture with a boiling point of 450 ° C and above is transferred to a shelf hydrocracking conversion reactor, where the thermochemical processes of separation and conversion of the residue into distillate fuel with a boiling point of 450-550 ° C (heavy gas oil) with a boiling point of 550 are carried out -700 ° С, (catalytic cracking) - residue with a boiling point of 700-750 ° С, (straight run residue) with TV 750-800 ° С (coking of oil residue) with TV 800 ° С and higher due to the chaotic thermal energy received from aerodynamic friction Nogo via friction before and supersonic gas outflow from elongated nozzles formed beam expanding jets directed into a narrow clearance shelves. The flow moves in the direction from the base of the slit-like nozzle to the buffer wall of each shelf and spreads in a thin layer on the fixed shelves, which leads to cooling on each shelf and transformation into a supersaturated vapor of a certain fraction depending on the temperature limit of the product boiling point, in addition, through the nozzles in fixed shelves the required agent is supplied in order to accelerate the process of hydrogen enrichment of the combined hydrocarbons. Distillate fuel with a boiling point of 450-550 ° C, (heavy gas oil) with a boiling point of 550-700 ° C; (catalytic cracking) - residue with a boiling point of 700-750 ° C; (straight run) with a boiling point of 750-800 ° C; (coke oil residue) with a boiling point of 800 ° C and above. Unloading of each product is carried out through the lateral branches in the column housing from each separation cavity separately.

Heat removal from the material being destroyed 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 you to get 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.

Thus, when moving a high molecular weight composition with a boiling point of 90 ° C or higher through a device with a conical screw, with a shaft rotating from an external drive at one speed and rotating the coaxial shaft from another external drive at a different speed, in the riser housing and placed in it wedge-shaped activators, turning into a worm spiral with activators and evaporation cells on a spiral, with an accelerating unit and a reactor for each fraction separately, through the structural elements of the annular cavity, with a rotating kata izatorom with a diffusion slit landings, with the separation column and the high-temperature decomposition reactor shelving fraction achieved great depth decomposition processes in a single device at each stage of the finished product.

The device achieves the goal by the fact that the mechanothermochemical fractionator contains, at the inlet of the liquid raw material, a pre-destruction zone successively made, including a cone-shaped body with an internal helical groove, the step of which corresponds to the helical helix, which also contains a helical groove on the surface of the screw, equal in volume to the groove made in conical housing, placed in it and connected to the rotation drive, a shortened conical worm shaft, which is made hollow with the possibility of keeping moving piston, local temperature control. The end face of the shaft contains a landing hole for the neck of the oncoming shaft, on the other hand, a riser body, a reactor block with a separation column, with a fraction boiling range up to 90 ° С, an acceleration block, a cylindrical material destruction body, a reactor block with a separation column, with a boiling limit up to 220 ° C, an accelerating block, a cylindrical body for material destruction, a reactor block with a separation column with a boiling range of a fraction of up to 315 ° C, an upper stage, a cylindrical destruction body for m terial, a reactor block with a separation column, with a boiling range of a fraction of up to 450 ° С, an accelerating block, a cylindrical body for material destruction, a shelf reactor unit with a boiling range of a fraction from 450 to 850 ° С is attached to it, with each shelf degrading the material to its own the maximum boiling point, which is issued through the side pipes in the form of distillate fuel. Shelf reactor of multi-temperature destruction of high molecular weight compounds is driven into rotation from an external drive (not shown) 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 made conical with an axial cavity for the coolant to function, and the worm cut on the surface of the screw contains a deep groove, the pitch and volume of which correspond to the pitch and volume of the groove made on the helical spiral cone shaft with the possibility rotation together with wedge-shaped activators with a wavy surface, and a shortened conical shaft is contained in a conical sleeve with a groove and a conical shape sensor body with an external coolant system (not shown), the volume of the cavity mezhshnekovoy screw tops not less than 2 times less than the volume at the inlet of the housing, which is equal to the ratio of not less than 2 to 1 or more. The end of the shaft is centered by a die with conical half-openings. In the series-connected part of the riser, wedge-shaped activators are installed on the rotation shaft, and the activators are made with a wavy surface with a pitch of 3 to 1 or more and a semi-ring sampling 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 sequentially connected fraction acceleration blocks are made with the possibility of destruction of 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 on 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 sampled through side discharge in the column body. A sequentially connected shelf reactor is capable of rotating at least one comb disk using a shaft between the shelves of another shelf disk, the other shelf disk being fixed, and the combs are asymmetrically formed with end grooves and the possibility of mechanical cracking of the material to a molecular state with effusion over more than low 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 is made with evaporation cells and cells containing purge channels directed to the surface of the shaft, and wedge-shaped activators made with a wavy surface and evaporation cells in the breaks of the screw. Accelerating blocks contain cylindrical sleeves, the inner surface of which is made by appropriate (compression compression) cells, performing the functions of magazines 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. When the shaft rotates, 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 in 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. where 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 emeschaetsya the cavity wedge activators. The gas-vapor composition evenly spreads in the liquid fraction, including filling the screw grooves in the reactor sleeves, from where the activator cells are filled with the selected components and delivered to the lumen (gap) to the diffusion slots, through which the gas-vapor fraction throttles into the ring cavity with lower pressure and contained in it, the catalyst, and the catalyst constantly rotates around the reactor sleeve and 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, capable of causing the effect of cavitation and the displacement of microscopic bubbles from the liquid phase during the rotation of one, forming the effect " mechanical 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, In this case, the remaining viscous material is liquefied by the supplied agent and throttled alternately through the transverse slots of the rotating shelves, selects a gas-vapor mixture of a certain composition depending on the limiting temperature of the boiling fraction and the distance from the axis of rotation. During operation of the device, 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 mechanically cracked 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 the conical cavity 2 to 1, wherein the tapered shaft is hollow and comprises movable pistons address temperature control. The pre-destructible high molecular weight mixture through the conical holes of the die, under pressure, enters the riser cavity (destructive acceleration compartment), formed by rotating wedge-shaped shaft activators and a cylindrical body, and the wavy surface of the activators in order to increase the frictional effect on the material is made in steps of at least 1-3, and the back contains a semicircular sampling, which creates a constant collapse loop, due to which the mixture continues to warm up and effectively mixes interlinked with donor agents supplied through feed channels. The liquefied mixture is captured by screw 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. Moreover, the riser casing, the reactor casing and the fractionator are provided with a jacket with the possibility of functioning of the coolant. The removal of the light fraction vapor-gas mixture with a boiling point up to 90 ° C from the worm cavity occurs at the molecular level through the lateral slots in the reactor sleeve under pressure, which is formed due to the content of soluble gases and resins in the oil medium. The fluidized catalyst located in the annular cavity of the reactor operates with the possibility of rotation around the liner recovery (regeneration) of its own properties, which are carried out due to the supplied hydrogen, steam and braking comb on the opposite side of the reactor vessel from the slot discharge, where the collision of the catalyst particles among themselves and with the surface of the comb, dumps 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 equipped with holes with float valves installed in them. Under the action of the steam flow, they rise, so that the steam is gushed into the liquid through the side openings in the base of the valve. If the steam flow is too small, the valves close until the required steam pressure is reached again. This allows you to make the appropriate settings depending on the available flow.

Further, the remaining mixture with a boiling point of 90 ° C and higher with a worm spiral through the conical openings of the die moves into the next cylindrical accelerating block, where the sleeve is made with cells, like in a worm spiral, which are instantly and constantly filled with a liquid mixture and serve as a store for filling evaporation cells made on a worm spiral. When the mixture moves radially in spiral cells, it undergoes a complex mechanical shear of high intensity, and when the compression and evaporation cells coincide, a microhydrodynamic shock occurs with the release of heat and pressure, which leads to the transformation of the material into a supersaturated vapor with a boiling point fraction, inside which clusters can nucleate, which are mixed with the material of the mixture, select a hydrogen-containing mixture in the liquid phase. The mixture moves through the conical openings of the die under the mechanical action of a spiral into the mixing reactor zone with a boiling range of 90-220 ° C and above, which is affected by wedge-shaped activators with cells in the end part that is in contact with a sleeve with a screw sample and slotted lateral discharge of a gas-vapor mixture, unloading takes place 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 shut-off is performed conical holes in the die to set the desired temperature and pressure in the reactor cavity. 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 ° C and 315-450 ° C is carried out according to the scheme of technology for processing high molecular weight raw materials with a boiling range of 90-220 ° 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 ° С 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 base of 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 smoothly 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 ° 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 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. In order to accelerate the process, a pipeline for supplying a reagent (or other agents) is made in the upper part of this channel, which allows reducing the viscosity of the material and accelerating the separation of liquid material and saturated vapor-gas mixture.

To prevent uncontrolled flow of fractions, thin channels between themselves are sealed with a ring. The remaining mixture with a boiling range of 550-700 ° C and above through prism-like slots of a rotating shelf under pressure of centrifugal forces and local pressure moves to the next thin U-shaped channel, where the material is distributed by a thinner film than in the previous channel, a 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 the floor through thin channels the spine of the fixed shelf, where it moves in the direction of lower pressure of the ring working towards the lateral unloading of "heavy gas oil" to the warehouse. In order to speed up the process, 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.

The remaining “catalytic hydrocracking” material (residue) with a boiling point limit of 700–750 ° C and higher along thin channels and slotted slots moves to the next cavity of thinner channels of the previous shelf. Under the action of centrifugal forces and local pressure in the channel, the material is distributed through prism-like openings with a thinner layer than in the previous channel, the light fraction is squeezed out onto the surface of the material according to the scheme of the previous shelf and, through the transverse channels of the stationary ring shelf, tends towards the ring sample towards lateral unloading of the finished product. In order to accelerate the separation process, a reagent (hydrogen) is supplied through the corresponding pipeline in the lower part of the channel, which contributes to the process of instant reaction separation in thin films of the substance. The heavier fraction with a boiling point of 750-800 ° С and higher under the action of centrifugal forces and local pressure moves to the next thin cavity of the “straight run residue”, where it is diluted with reagent 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 heavier fraction through conical openings under the influence of centrifugal forces and pressure moves into the thin channel of the next shelf "coking oil residues", the fraction with boiling scrap 800 ° С and higher is hydrogenated through the upper reagent (hydrogen) supply pipe, which significantly accelerates the process of fraction separation in the thin channels of the device, the liquefied semi-solid fraction and supersaturated steam are moved to the annular side discharge channel, where it is unloaded to the warehouse under local pressure of centrifugal forces finished products or for possible vacuum distillation.

Brief Description of the Drawings

Figure 1 shows an arbitrary section of the left side of the mechanothermochemical fractionator; figure 2 is the same, the right part; figure 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 bb in figure 1; in Fig.7 shows a section GG in Fig.2; on Fig shows a section DD; Figures 9-12 depict activators; on Fig shows a section EE; on Fig - section F; Fig. 15 shows a side section of disks; in Fig.16 shows a section of pos.24; on Fig shows a section 3-3 in figure 4; in Fig.18 shows a cross section of II in Fig.16.

The best embodiment of the invention

The mechanothermochemical fractionator contains a cone-shaped body 1 and a receiving cup 2 for loading the source material. In 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. On the working side of the worm spiral 4, 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, a centering bore 11 is made to accommodate the neck of the through shaft 12, which originates in the riser pipe 13. In turn, the shaft 12 contains wedge-shaped activators 14 with a wavy surface and a semicircular selection 15 and a worm spiral 16, on the feed the side of which is made of 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 not more than their own diameter and through cells 19. In addition, a riser The housing 13 contains nozzles for supplying agents 20. The series-connected reactor housing 21 comprises a continuation of the through shaft 12 with an ongoing screw spiral 16, which interacts with the sleeve 22, and shortened helical grooves 23, with slotted slots 24 made in the sleeve 22 and the reactor vessel 21 on the opposite side, contains a comb 25 for interaction with the catalyst 26. In addition, the reactor vessel 21 includes a pipe 27 for supplying the 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. In the column 32, there are nozzles 35 for lateral product selection and an overflow nozzle 36. At the top of the column, the dome 37 contains divider 38 at the outlet of the reactor. The housing 21 comprises a slide gate valve 39 with conical half-openings 40. An acceleration housing 41 is successively connected to the reactor housing 21, 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 pipe for the donor agent 47. To the booster body 41, a reactor vessel 48 is connected in series, which comprises a sleeve 49 with a screw set 50, the screw set 50 being smaller in volume of the screw set 23. The wedge-shaped activators 51 contain cells 52, where a vapor-gas mixture is injected, which is squeezed out through the side slots 53 into the fluidized catalyst medium 54. At the inlet of the reactor, the vessel 48 contains a vane die 55 with external adjustment of the size of the conical half-openings 56. The upper part of the reactor vessel 48 is made in the form of a glass 57 and contains a filter 58. Separator the column 59, in turn, contains a valve disc 60 with a float valve 61, a side discharge pipe 62 and overflow pipes 63. At the top of the column 59, the dome 64 contains a divider (valve) 65. Connections to the reactor 48 there is an accelerating case (block) 66, which at the inlet contains a slide die 67 with external adjustment of the size of the conical holes 68, a sleeve 69 with cells 70. The through shaft 12 contains a worm spiral 71, on the surface of which evaporative and blow-through cells 72 are made; 73 respectively. In addition, the housing 66 includes a nozzle 74 for supplying the desired agent. Prior to the booster block (body) 66, a reactor vessel 75 is connected with a boiling range of 220–315 ° C. At the inlet, the reactor vessel 75 contains a gate die 76 with external adjustment of the size of the conical half-openings 77 and a sleeve 78 with a screw groove 79, which through wedge-shaped activators 80 interacts with the cells 81 and the lateral slot discharge 82. The fluidized rotating catalyst 84 is contained in the annular cavity 83. The housing the reactor 75 on the inside contains a comb 85, and from the outside there is a pipe 86 for supplying the agent and a pipe 87 for supplying fresh catalyst. The upper cup 88 of the housing 75 contains a filter 89 and the body 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. At the exit from the housing 75, a slide die 97 with external adjustment of the conical half-holes 98 is contained. The housing of the booster block 99, which contains a sleeve 100 with cells 101 smaller than the size of the cells 70, is connected in series to the housing 75. a helical spiral 102, on the surface of which evaporation and through cells 103, 104 are larger than the cells 101 located on the sleeve 100. In addition, the case of the booster block 99 includes a nozzle 105 and a gate die 106 with adjustable conical half-openings 107.

A reactor vessel 108 is attached to the booster 99 with a boiling range of the fraction 315-450 ° C, which in turn contains a sleeve 109 with a screw groove 110 shorter than the screw grooves 79, which interact with the cells 112 through activators 111, and with a slot discharge 113 , an annular cavity 114 and a catalyst 115. 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 process esky 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 cup 119 and contains a filter 120 and a separation column housing 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. A booster block 128 is connected in series to the reactor vessel 108, which at the inlet contains a slide die 129 with external adjustment of the conical half-holes 130, a sleeve 131 with compression cells 132, which are smaller than the size of the previous cells and the interaction they are guided with cells 133 of the screw spiral 134, which correspond to the size of the cells 132 or more, and the hollow shaft 12, on which the screw spiral 134 is contained, 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 slide gate 137 is made with external adjustment of the conical half-openings.

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. In the annular shelf 140, at least two cone-like holes 142 are made. The housing 138 comprises a fixed 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 ka 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. On each shelf of the fixed disk 143, a semi-circular cavity 148 in the lower part is connected to the side hole 153 for unloading products with a boiling point of 450-650 ° C. 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 the cavity 159. The disk 139 contains the annular shelf 160 with the 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. In addition, the housing of the stationary 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 made with the possibility of temperature control through the channels 173, in addition, for local temperature control in the hollow shaft 12 are performed by movable pistons 174, 175 through sponding pipes. The booster block 128 is provided with a nozzle 176 for emergency discharge of the mixture, the housing 138 of the shelf reactor contains nozzles 177 and 178. The mechanothermochemical fractionator operates as follows. The pre-warmed up to 90 ° C cone-shaped body 1 through the receiving cup 2 is forced to supply the source material (oil) to the pre-warmed up to 90 ° C conical shaft 3, which contains a conical worm spiral 4 and is driven in rotation from an external drive (not shown ) The material fills the screw inter-screw cavity, the groove of the screw selection 5 and the groove of the screw selection 6 in the housing 1. When the shaft rotates 3 hundred revolutions per minute or more in the cavity of the housing 1, an excess liquid pressure is created in the conical screw spiral 4, in which the activators 7 function, forming a trace of gas-vapor bubbles of a light fraction, while the screw sample 5 interacts with the screw groove 6 to shear the material, which contributes to the additional selection of the vapor-gas mixture. The moved material in the cavity of the housing 1 interacts with the parts of the device that perceive the selected temperature during friction under pressure from a liquid medium. 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 through an external source of heat transfer agent into the cavity screw shaft 3. The first stage of the dispersal of the material ends by pumping through the conical half-holes 9 of the centering die 8, while reaching a temperature of up to 90 ° C. The mixture of material entering the cavity of the riser pipe 13 is amenable to mechanical action of the shaft 12, which is mounted in the bore hole 11 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 lateral 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, made 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 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 further contributes to the acceleration of the liquid mixture, and the evaporation cells 18 perform selection of the gas-vapor fraction on the surface of the liner 22. Through purge cells 19 due to the Channel excess fluid pressure liquefied mixture is disposed in the vicinity of the shaft 12, thus achieving uniformity of the mixture in mezhshnekovoy cavity. In order to regulate the reaction process, the required agents (alkali solution, steam, and other elements) are fed through the pipe 20 to neutralize molecular sulfur. 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 ° C or more remains in the inter-screw cavity for further movement, and a fraction with a boiling point of up to 100 ° C, located near the liner wall, condenses onto a circulating catalyst 26. In the annular cavity between the liner 22 and the reactor vessel 21, molecular vapor the light fraction with a boiling point of 100 ° C tends up, and the catalyst 26 in a circle tends down and enters comb 25, swirls and shakes off carbon (if any) from its surface, and the comb on the reactor vessel 21 made at an angle from 30 ° to 90 ° relative to the wall with the aim of the formation of vortex flows, which create conditions for the collision of the catalyst particles 26 with each other. The pipeline 27, through which the required agents 28 are supplied under excess pressure, ensures the stability of the suspended state of the catalyst 26 in the annular cavity of the reactor 21. If it is necessary to update the catalyst 26, a fresh or restored catalyst 26 is supplied through the pipe 29, which operates in the cavity until it is completely worn out or 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 bubbler liquid with a layer thickness of 10 cm and above. The bubbling of a gas-vapor mixture through a liquid layer is called rectification, where partially heavy molecules condense, and the light components of the product rise higher and through the side pipes (discharge) 35 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. When the shaft 12 rotates to 1000 rpm or more, the mixture of the evaporation cell 45 degrades upon friction against the surface of the sleeve 42, and a molecular gas-vapor component is formed, which, upon entering the next cell 43 of the sleeve 42, generates a microhydrodynamic shock. The result is an instantaneous jump in temperature and pressure in the enclosed space of two cells. When the evaporation cell 45 is displaced, the mixture spreads uniformly and saturates the boundary layer with its vapor. When the cell 46 enters the cell 43, the saturated mixture is captured and, due to the compression-temperature properties, expands through the through purge channels, which ensures the mixture flows to the wall of the shaft 12, where it is mixed with a low-saturated mixture. In this way, uniform saturation with the gas-vapor bubbles of the mixture is achieved along the entire length of the cavity of the booster body 41. Triangular activators 17, which also form an additional gas loop in the inter-screw cavity, have an additional effect on the mixture. In the case of insufficient parameters of the mixture parameters, it is possible to partially control the movement of the mixture into the next cavity by overlapping the semiconical openings 56 with a die plate 55, while the mixture in the accelerating case 41 reaches the required parameters, which allows monitoring the quality of the mixture parameters at almost every stage. Next, 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 selection 50 of the sleeve 49 and through the side slots 53 are discharged by flash evaporation into the annular cavity formed by the sleeve 4 9 and housing 48, onto a fluidized catalyst 54.

The gas-vapor mixture of the components interacts with the catalyst 54. The elemental carbon present condenses onto the catalyst particles (if any) and in a circle tends to comb 25 (then all technological operations are performed according to the described scenario, and the light fraction with a boiling point up to 220 ° C from the glass 57 through the filter 58, it tends to the cavity of the separation column 59 and through the float valve 61 in the valve disc 60 enters the bubbling liquid with a temperature of 220 ° C and above, where partially heavy molecules condense, and the light components of the product rise above the liquid and through the side unloadings 62 enter the condenser and then compound the gasoline fraction. The remaining heavy compounds of the molecules through the overflow nozzles 63 are returned to the booster body 41 for reuse. The lightest fraction of this column enters the dome 64 and through a divider 65 to gas fractionation plants (not shown in the drawing) or to a pipe 20 for reuse. The remaining liquid mixture with a boiling range of more than 220 ° C in the cavity of the sleeve 49 under local pressure enters the booster body 66 through the slide valve 67 and semiconical openings 68. The mixture fills the cavity of the sleeve 69 and the cells 70 located therein, is captured by the worm spiral 71, in the body which contains the evaporation cells 72 and the purge cells 73, through the channels of which the gas-vapor mixture enters the wall of the shaft 12, which ensures uniform distribution of gas bubbles, and the evaporation cells 72 when combined with the cells 70 zag are loaded with a mixture and during the rotation of spiral 71, frictional friction and compression compression occur, where when evaporation cells 72 approach cells 70, a microdynamic shock occurs in a closed cavity, which instantly selects gas-vapor components of the product with a boiling point of up to 315 ° C, and when cells 70 and 72 there is a saturation with gas-vapor bubbles of the boundary layer, which, under the mechanical action of a screw spiral 71 moves along the channel of the sleeve 69, and the pipe 74, made in the housing 66, serves to discharge excessively pressure or supplying the required agent to accelerate the chemical process in the cavity of the reactor 75. At the inlet of the reactor 75 there is a slide die 76 with conical half-openings 77, through which the mixture enters the zone of the sleeve 78 with a boiling range of 315 ° C and above fills the screw grooves (sample ) 79, from which the evaporation cells 81 of activators 80 with a corrugated surface are filled, which during rotation are combined with longitudinal slots (slots) 82, through which molecular gases from the evaporation cells 81 tend to the annular cavity 83 by a fluidized catalyst 84, while 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. Through the pipe 86, agents are constantly fed into the annular cavity to support the catalyst in suspension and to accelerate the chemical process in the annular cavity, and through the pipe 87 serves a new or restored catalyst. The light gas-vapor fraction from the glass 88 through the filter 89 enters the cavity of the separation (distillation) column 90 and through the float valve 92 located in the valve plate 91, enters the bubbling liquid, where heavy components are partially condensed, and light components rise up along the valve plates where through the side nozzles 93 receive the components of the desired fraction. The heavy components through the overflow nozzles 94 are sent to the booster body 66 for recycling, and the lightest fraction is lifted 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 ° С and higher is supplied under pressure to the slide gate 97 and, through conical half-holes 98, is fed into the cavity of the booster block 99, in which the sleeve 100 with cells 101 is placed, and the cells 101 are one third smaller in size 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 fractionates about the surface of the sleeve, and when the evaporation cell 103 and the stationary cell 101 are combined, microhydrocompression compression of the mixture takes place 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 ° C and above. When the cells open, the mixture spreads uniformly 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. Next, the mixture, heated to 315 ° C and higher, is fed to the slide gate 106 and through conical half-holes 107 enters the reactor vessel 108 and into the cavity of the sleeve 109, fills the screw grooves 110, through which the evaporation cells 112 of the activators 111 are fed, and when the evaporative is combined cells 112 with lateral slotted discharge 113, the vapor-gas mixture is injected into the annular cavity 114 onto the catalyst 115, which is suspended in the cavity of the housing 108. The reacted catalyst 115 moves in a circle around the cavity on the comb 116 of the housing 108, where it is rejuvenated (restored) due to collisions with each other and due to the agent supplied through the pipeline 117. In the case of the need for a new catalyst, it is supplied through the pipe 118. The vapor-gas mixture from the glass 119 through the filter 120 enters the cavity of the separation column 121 float valve 123. The heavy molecules condense in the liquid, and the light fraction rises higher and is discharged through the side pipes 124 as a finished product, and the remaining heavy components are fed through the overflow pipes 125 into the cavity booster 99 for recycling. The lightest fraction enters the dome 126 and through the divider valve 127 is fed to the hydrotreatment or pipe 20 for recycling. The remaining mixture with a boiling point of 450 ° C and higher 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 due to frictional friction and microhydrocompression impacts, it is heated above 450 ° C, and under the mechanical influence of a screw spiral 134, the mixture is fed to the conical transition 135, where in the conical cavity 136 the compression of the mixture is higher and higher temperature up to 500 ° С and higher. Next, 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 backflow force from the housing 138, the openings of the die 137 are directed along the diffuser base.

On the shaft 12 contains a rigidly mounted shelf disk 139, which rotates up to 1000 rpm and more together 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 together with the stationary shelf disk 143, and the first annular gap 144 from the shaft 12 in conditional throughput is 2 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, under By means of centrifugal forces, it is evenly (pressed) distributed in a thin layer along the inner diameter of the rotating flange 149 of the disk 139, while gas bubbles as a lighter fraction (without weight) are released to the surface and concentrated in the semicircular cavity 148 with a boiling point of 450-550 ° C and under local pressure with an open hole 153 enters the capacitor. At the same time, an agent is accelerated through the L-shaped hole 147 of the shelf 146, accelerating the process of obtaining a gas-vapor fraction with a boiling point of 450-550 ° C. The remaining mixture over 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. On the wall of the disk 139, the spiral grooves 151 of the countercurrent mixture contribute to additional frictional friction, heat and vapor-gas 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 not rolled along the channel and 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 range of 550-700 ° 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 by the centrifugal forces against the inner wall of the shelf 155 and through the trapezoidal the slots 157 enter the thin channel of the next shelf 158, which in the lower part forms a cavity (sinus) 159 for concentrating the gas fraction with a boiling range of 700-750 ° C, which tends to the cooling system through the side opening 153, and through the L-shaped hole in This channel receives an agent (for example, hydrogen) that promotes an instant chemical process (if one is required). The remaining residue with a boiling point of 750-800 ° C and above, located on the shelf of revolution 160, passes through the trapezoidal slot 161 and through the edge of the shelf into the thin channel of the fixed shelf 162, where due to aerodynamic friction and local pressure in the presence of a reagent entering through Г -shaped hole147 an instantaneous chemical process occurs with the evolution of a gas fraction (straight runner residue) into a semicircular cavity 163, and from it passes through a side hole 153 for cooling. The residue with a boiling point of 800 ° C and higher in the narrow channel of the shelf 164 due to aerodynamic friction and local pressure in the presence of a reagent entering through the hole 147, instantly heats up to a temperature of 800 ° C and above and through trapezoidal slots 165 and through the edge of the shelf enters the thin channel of the shelf 166 and the semicircular cavity 167, where the gas fraction displaces (floats) and enters cooling through the side discharge hole 153, and the remainder together with the remaining catalyst due to centrifugal forces and local pressure at it extends to the shelf 168, where it is heated by friction and fed into the trapezoidal slot 169, from where it throttles onto the wall of the housing 138, while the gas fraction can be taken through the side discharge 153, and the liquid fraction can be drained through the pipe 177 and subsequently goes to the extraction of the catalyst ( if required). 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. In addition, the thin channel of the shelf 154 can partially be blocked by the external regulation ring 170, after which the residue can only enter the subsequent channels through the trapezoidal slots 150, 157, 161, 165, 169, which allows to reduce the number of products with a boiling range of 550 ° C and above and to increase the number of products with a boiling range of up to 550 ° C. The ring 171 external regulation allows you to block the channel shelf 158 and increase production with a boiling point from 550 ° C to 700 ° C. The ring 172 external regulation allows you to block the reverse 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.

Industrial applicability

The invention provides high-quality components of motor fuel from oil using chemical transformations using catalysts in the preparation of each fraction. During the passage of crude oil from loading to the complete separation of molecules into components, the composition changes as follows:

- paraffins are converted to isoparaffins;

- paraffins turn into naphthenes;

- naphthenes are converted to aromatic hydrocarbons, including benzene.

These are economically useful processes, since isoparaffins, naphthenes, and aromatic compounds have higher octane numbers than the substances from which they formed. Thus, the preparation of colorless products occurs due to deep thermal degradation, thermocatalytic degradation and the hydrogenation effect on petroleum feedstocks in one device.

Claims (6)

1. The mechanothermochemical fractionator for the separation of liquid and gas heterogeneous systems, including the destruction of petroleum feedstocks or petroleum products, contains a feeding cylinder with a cooling jacket placed in it and connected with a rotary drive a screw worm, characterized in that the device contains a series of pre-destruction of the liquid feedstock - petroleum feedstock or petroleum product, riser, alternating zones of reactors and booster blocks with a boiling point limit, respectively, up to 100 ° C, up to 220 ° С, up to 315 ° С, up to 450 ° С and a sequentially connected shelf reactor block with a boiling range of a fraction from 450 ° С to 850 ° С, including a cone-shaped body with a tapered sleeve with a screw thread, a shaft and a screw spiral at the inlet of liquid raw materials containing triangular activators with a wavy surface on the supply side, and the top of the conical shaft is centered by an unregulated disk die with conical half-openings, the vertices of which are directed towards the supply of crude oil, from the rotation drive side in the pre-drive zone of destruction, the shaft is hollow and equipped with a movable piston; on the opposite side, the top of the conical shaft contains a bore with the possibility of rotation of the neck of another coaxial shaft and the subsequent supply of liquid raw materials through the conical openings of the unregulated disk die into the cylindrical riser housing, where additional generation of light vapor-gas fraction with the subsequent supply of liquid raw materials from the riser body to the auger cavity of the reactor with unloading from it a gas-vapor fraction with a temperature boiled away up to 100 ° С and feeding the remaining liquid raw materials into the booster block, the shaft periodically in the reactor zone along the entire length periodically containing wedge-shaped activators with wavy sides and a screw spiral in the booster block with evaporation and blow-off cells on the surface that can interact with the sleeves booster blocks and rectors, where the inner surface of the liners is made with a helical groove, and in the shells of successive shell reactors contains at least three lateral slotted unloadings diffusion of this type and each forms an annular cavity with the reactor vessel for rotation of the catalyst around the liner, in addition, each upper stage of the booster contains inlet pipes of donor agents, and the reactor vessel is provided on the inside with a comb with a directional angle of at least 60 ° and not more than 90 ° relative to surface, below the comb contains a pipeline for supplying working agents, and above is a pipe for supplying fresh catalyst, the upper part of the reactor is made in the form of a glass and contains a filter, the casing of the separation column fr minifunctions of product types with plates designed with a float valve, and lateral nozzles discharging the finished products, nozzles overflow fraction in the upper stage for recycling, the top of the column housing is provided with a divider valve. 2. The mechanothermochemical fractionator according to claim 1, characterized in that the wedge-shaped activators on the sides of the friction friction in the series-connected housing for accelerating the mixture to 100 ° C comprise a wavy surface and semi-ring samples in the rear part, the surface of activators and a worm spiral interacting with the surface of the sleeve , contains cells with a depth of not more than its diameter, where the loading and unloading of the product from the cells is performed by rotation around the axis and interacts with a spiral groove in the sleeve, the width Torah not greater than the diameter of the cell, and the cell depth greater than the depth, the lateral discharge slit in the sleeve-type diffusion reactor unit is formed with a directional angle of dispersion of not less than 20 ° and not more than 60 ° from the horizon. 3. The mechanothermochemical fractionator according to claim 1, characterized in that in a series-connected casing of the accelerating block of the mixture up to 220 ° C there is a sleeve with round cells on the inner surface, at a distance of at least two diameters from each other, where the depth of the round cells is not greater than diameters that interact with cells made on the surface of the worm spiral, moreover, the evaporation cells on the surface of the worm spiral are made of larger diameter cells made on the surface of the sleeve, and the purge eyki formed with an opening directed towards the shaft wall in the dead zone. 4. The mechanothermochemical fractionator according to claim 1, characterized in that the sequentially connected shelf reactor with a boiling range of 450 ° C and above is made in an airtight housing that contains at least one rotary shelf on the shaft and can be rotated and at least one stationary a shelf disk, which is part of the hermetic casing, the shelves of the fixed disk in the upper part provided with lateral feed channels of the reagent, and in the lower part contain a sample for the formation of an expanded cavity from the side and holes for unloading products, in turn, the shelves of the rotating disk are made with trapezoidal slots or conical holes of diffusion type, which are directed to the center of rotation with the top of the cut trapezoid (cone), and the size of the cut top of each shelf of the movable disk is smaller than the size of the top of the previous shelf, remote from of the center, in addition, the wall of each sample of the movable disk is made anti-sublimation helical groove interacting with the annular groove at the end of the fixed disk, and portionwise e regulation of the flow of the mixture between the end face of the shelf of the movable disk and the sampling wall of the stationary shelf disk is regulated by the retractable side rings of the external regulation. 5. The method of separation of liquid and gas heterogeneous systems, including the destruction of petroleum feedstocks or petroleum products, carried out in a mechanothermochemical fractionator according to claim 1, in which, by mechanical and thermal treatment, the material is converted into a liquid-phase product of semi-functional use, in which the liquid feedstock is petroleum feedstock or the oil product is pre-degraded to the limit of boiling of the light fraction with a conical screw device with the simultaneous formation of gas bubbles in the intern worm cavity by mechanical impact on the material with a screw groove and at least one identical groove on the inner wall of the conical sleeve, additional selection of gas bubbles is performed by wedge-like activators with a wavy surface pitch of 3 to 1 or more half-ring sampling at the base of the wedge, and the temperature at the top of the cone occurs due to compression compression of the medium and a decrease in the volume of the inter-screw cavity of at least 2 to 1 or more, and frictional friction of the liquid oil system with parts of the cone device, and in booster blocks when the shaft rotates up to 1000 rpm or more with parts, and interaction with the parts of the device body, it is possible to mix the liquid and gas fractions to the equilibrium state, and the cellular surface of the parts of the screw spiral, cylindrical cavity of the booster blocks and wedge-like parts with evaporation cells in the reactor blocks are made with the possibility of selection of the gas-vapor fraction from liquid raw materials at the maximum local temperature and under the maximum local pressure, which corresponds to its limit value at each stage of the technological process of separation of material, alternating zones of reactors and booster blocks, which allows gas-vapor fractions to be supplied through the slots of the diffusion type in the sleeves into the annular cavity of each reactor with a boiling point limit, respectively, up to the boiling point 100 ° С, up to 220 ° С, up to 315 ° С, up to 450 ° С, a fraction with a boiling point of 450 ° С-850 ° С and higher is isolated in a shelf reactor. 6. The method of separating a liquid system in the reactor zone of the method according to claim 5, characterized in that the fraction separation in the shelf reactor is performed by radially made trapezoidal holes in the annular disks when the shaft rotates up to 1000 rpm or more, where in the thin channels of the gaps between the shelves when the mixture is subjected to centrifugal forces directed from the center along the tangent rotation, diffusion of matter and cavitation of microscopic bubbles occurs, causing discontinuities in surface tension and instantaneous release of energy in the cavity of the canal lan, and forced hydrogenation affects the redistribution of hydrogen between hydrocarbon molecules in thin films of material at elevated local temperature and pressure, and the farther from the center of rotation, the thinner the film in thin channels and the higher the limit of local destruction and the boiling rate of a fraction close to the composition of the original oil .

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