RU88670U1 - INSTALLATION AND DEVICES OF DEPTHE PROCESSING OF HYDROCARBON RAW MATERIALS - Google Patents

Abstract

1. Installation for in-depth processing of hydrocarbon raw materials, including preparation (preliminary purification from water and harmful impurities), supply and heating of raw materials, separation of raw materials into fractions, removal of separation products, characterized in that a separation apparatus is built into the processing unit, in which the hydrocarbon mixture is separated into two parts — the light vapor-gas separation part (low boiling fractions of NKF) and the heavy high molecular weight liquid part of separation (high boiling fractions of VKF), the raw materials are preheated in heat recovery units heat exchangers due to the heat of one or all separation products (NKF and VKF), and / or in a separate or common (but separate from heating VKF coil) with heating of the VKF heating furnace (heater) to a temperature above 20 ° C or they are heated and subjected to thermal cracking, the high molecular weight liquid part of the separation (high boiling fractions of VKF) obtained after the separation apparatus is heated in a heating furnace (heater) separately from the raw material to a temperature above 300 ° C or heated and subjected to thermal cracking, the mass fraction of VKF subjected to heat cracking in a heating furnace or heater does not exceed 50%, then the raw materials are finally heated in a direct mixing device for the raw materials with the heated high molecular weight liquid separation part (high boiling fractions VKF), and the mixture is 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 ° С (depending on the composition and properties of the feedstock), i.e. heated so that uncontrolled thermal cracking has not yet begun, then the mixture of cheese

Description

The field of technology.

The utility model relates to the oil refining, petrochemical and chemical, 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, slate, 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. In addition, the application of the utility model allows solving many environmental problems and leads to an improvement in the environmental situation. The preparation and deep processing of oil, oil residues and other raw materials means not only the removal of harmful impurities from raw materials, but also, most importantly, an increase in the number of light target products higher than their potential content in the feedstock, which can further significantly increase the processing depth and profitability total processing industry. Light target products or fractions are understood as fractions for further processing and obtaining light target commercial products with a boiling point mainly up to 350-360 ° 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, etc.). In the future - light target fractions or products, from which, upon final processing, light target products are obtained (liquefied gas, gasoline, diesel fuel, petrochemical products, etc.). Heavy commercial products - coke, bitumen, bitumen emulsions, coatings, oils and other commercial products.

The prior art.

Technological schemes for oil refining have several options. There is a full technological cycle, which includes the following main industries: production of fuels, production of petrochemical products, production of lubricants and special oils, production of additives. Specialized variants of technological schemes are possible: only fuel or only fuel-oil (Dekhterman A.Sh. Oil refining according to the fuel option. M., "Chemistry", 1988, p.13). In all cases, devices for preliminary evaporation of oil are used at the beginning of the technological process. The preliminary evaporation of gas and the bulk of gasoline allows you to reduce the pressure at the inlet of the feed pump, relieve the furnace from heating light fractions, reduce the vapor velocity and reduce the diameter of the main distillation column. At large oil refineries (refineries), distillation column apparatuses are used for this purpose.

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 (Moscow, Chemistry, 1988, p. 41). The latter method is used most often, since it allows to increase the depth of distillate selection within the limits of their potential content in raw materials. We briefly consider the sequence of operations of primary distillation carried out according to the classical scheme.

Before the oil is fed to the separation, its preparation is required. 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).

To separate the hydrocarbon feed (including oil) it is heated. At the enterprises of the oil refining and petrochemical industries, this operation is performed by supplying heat through a dividing wall (coil) by burning fuel. For this purpose, various tube furnaces are used (Entus NR, Sharikhin VV. Tube furnaces in the oil refining and petrochemical industries. M., Chemistry, 1987, p.6, etc.). Liquid and gaseous hydrocarbons are heated in them. In this case, the following processes can occur: heating, evaporation, overheating. Heated hydrocarbon feed passes through the coils. Heat transfer to the raw material occurs, as noted, through its wall. There is a limitation on the thermal stress of the heating surface. Deposits of salts or coke on the coil walls cause a rapid increase in the temperature of the pipe walls, which ultimately leads to a sharp reduction in the service life of the chimneys. Therefore, for raw materials containing resinous compounds, the heat stress is set low. The decrease in oil reserves of traditional fields increases interest in the production and, consequently, the processing of heavy oil (Ratov AN, Nemirovskaya GB and others. Problems of oil development in the Ulyanovsk region. "Chemistry and technology of fuels and oils", No. 4, 1995 d). Therefore, the use of tubular heaters for such oil becomes problematic. In addition, coils require the use of high alloy, expensive steel. In general, a tube furnace is a complex and expensive equipment that has a limited resource.

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. For a clear separation of the mixture, 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 oil separation, it is advisable to use simpler devices, such as evaporators (A. Dekhterman, Oil refining according to the fuel version. M., "Chemistry", 1988, p.23). The evaporator is a cylindrical tank. At the bottom of its housing is an integrated tubular heat exchanger. A coolant is supplied inside the tubes of the heat exchanger to heat 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 the heat transfer conditions are significantly worsened. This process is significantly accelerated with increasing temperature of the coolant. Therefore, devices of this type have limitations in terms of intensifying the process of separation and evaporation of part of the liquid hydrocarbon feedstock. The temperature of the process is 200-230 ° C. This temperature corresponds to a certain evaporated part of the oil (feedstock). In this utility model, this apparatus is used as a prototype of an evaporation and separation apparatus.

However, such processing of oil and oil products does not allow solving the problem of deep processing of oil-containing fractions in order to maximize the extraction and efficient use of the obtained processing products (higher than their potential content in raw materials), and without deep processing, processing plants are practically unprofitable.

For the processing of heavy oil-containing fractions in order to obtain an additional amount of light oil products, 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 (see Rudin MG, Drabkin AE. Brief reference book of the oil refinery. L .: Chemistry . 1980, p. 70-73). The method includes heating the feedstock to a temperature of 470-550 ° 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 ° C.

However, the known method is expensive and difficult to implement.

A known installation for the implementation of catalytic cracking of petroleum products, which contains interconnected device for processing the feedstock, a device for separating the final products, communicated in turn with a device for cooling and condensation of the final product, communicated with the device for the separation of hydrocarbon gases (see Rudin M .G., Drabkin AE A brief guide to the oil refinery. L .: Chemistry. 1980, p. 70-73).

The specified installation is very cumbersome, difficult to maintain and does not allow to intensify the chemical-technological processes with processed raw materials.

Known methods for processing heavy oil-containing fractions using, along with thermal and catalytic, physical methods of exposure to activate the processed raw materials.

A known method of processing by sequential extraction of fractions from hydrocarbons using electromagnetic energy with a frequency of 300 MHz-300 GHz (US patent 5055180, class C10G 1/00, 1991).

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.

Known methods for refining petroleum products by exposing the latter to ionizing radiation (neutron flux or Y-radiation) followed by catalytic cracking of the reaction products (see, for example, RF patent 2100404, class C10G 15/10, 1995).

However, the application of the method is difficult in industrial production due to the complexity and difficulties of controlling the process. In addition, the method is not safe to use.

Known methods for processing heavy oil-containing fractions using wave exposure to a wide range of frequencies.

In the known method of processing fuel oil by vacuum distillation to obtain distillate fractions, the liquid phase of the still bottom is exposed to acoustic vibrations with a frequency of 0.1-200 KHz and a power of 0.2-3 W / cm ² at a residual pressure of 20-200 mm Hg (see ed. St. USSR 1377281, class C10G 7/06, 1988).

However, 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. In addition, 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.

There is also a method of cracking petroleum products using an ultrasonic frequency spectrum. According to this method, the raw material (oil-containing product) and dispersant are fed into the treatment zone, ultrasonic treatment is carried out with a radiation intensity of 1-10 MW / m ² in a closed circulation circuit at a static pressure in the range from 0.2 to 5 MPa, and the subsequent separation of the processed raw materials into liquid and vapor phases and obtaining the final product from the vapor phase (see RF patent 2078116, C10G 15/00, 1995).

Although this method allows to increase the yield of light oil products, however, it does not allow controlling the process of obtaining final products due to a closed cycle and has a number of technological disadvantages: it is carried out at high temperatures and pressures, it is difficult to implement, energy-intensive.

Installation for implementing the specified method for cracking oil products contains interconnected device for processing 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 refrigerating chamber. The emitter of ultrasonic frequencies are the mechanical components of the system (rotor, stator, bearings).

The disadvantage of this installation is the use of a complex mechanical system (rotor, stator, bearings) in the operation of the installation, which sharply reduces its reliability. In addition, the use of mechanical components as emitters with an intensity of more than 100 kW / m ² leads to intensive destruction of their surface due to the occurrence of cavitation processes.

Due to these drawbacks, methods of direct physical impact, for example, of a wave of various nature, have not been applied and are not used in industry. In addition, the methods of direct physical impact are unreasonably energetically expensive, because the conversion of thermal energy into wave energy has a very low efficiency and to activate vibrational levels of molecules, many times more energy is needed than when the same effect is achieved with direct heating.

A known method for the thermal processing of heavy oil-containing fractions, including thermal cracking of heavy oil-containing fractions into phases and obtaining final products from the vapor phase, characterized in that prior to thermal cracking, the feedstock is subjected to wave treatment in the processing medium by forming a wide range of frequencies from acoustic to the light range, after which the impact products are fed to thermal cracking, which is carried out in IU primary distillation at atmospheric pressure and a maximum heating temperature of 360 ° C (Russian patent RU 2215775).

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. In the thermal or catalytic process, the necessary energy is introduced by direct heating of the feed. Further, raw materials, for example in catalytic cracking, are fed to catalysts that reduce the activation energy of molecular bond breaking and contribute to the cracking process. In this method, the activation energy of molecules is introduced into the medium due to the "formation of a wide spectrum of frequencies from the acoustic to the light range in the medium being processed." Taking into account the fact that when raw materials are activated by direct heating, heat is directly used to excite vibrational levels of molecules, and to activate the same molecules by wave action, heat (energy) must first be spent on creating a wave effect, and this process has a very low efficiency , then the energy costs during the implementation of this method become unreasonably high. Those. To significantly excite vibrational levels of molecules (and this is equivalent to heating the raw materials hundreds of degrees) in this method, it is necessary to use much more energy than with direct thermal heating. Moreover, for the preliminary processing of raw materials it takes a long time, the process is periodic, which is a big obstacle to the industrial implementation of this method.

Known devices for acoustic treatment of liquid (patent SU 410823 "Hydrodynamic emitter of a vortex type", patent SU 546389 "Device for ultrasonic processing"). However, they do not give the effect of increasing the depth of processing, i.e. cracking, the main application is the creation of emulsions.

Known devices for acoustic and cavitation processing, in which the processing is carried out due to the movement of the rotor, the disk is rotary pulsation devices (patent RU 2115176 "Cavitation generator", patent RU 2111554 "Ultrasonic oscillation generator"). In these devices, 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 treatment of the liquid in such devices gives a small, within the limits of measurement error, increase in the processing depth and did not find a wide industry applications for cracking hydrocarbon feedstocks. Basically, such devices are used for emulsification of liquid media. Due to the fact that moving parts are present in the devices, the service life of such devices is insufficient.

The closest analogue (prototype) for the claimed device is the device according to patent RU 2164629 "Method of 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 maximum cross-sectional area of the working fluid in the plane perpendicular to the axis of the pipeline is more than 0.8 of the passage section of the pipeline, but is 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. At a certain critical flow rate, the pressure in the rear zone decreases to atmospheric, as a result of which bubbles form here, filled with gas or steam, and then a cavity. When the bubbles or caverns are separated from the cavitator, they fall into the region of increased flow pressure and cools, doing a certain job, which can be used as useful, for example, to intensify chemical and other processes. Because Since the working fluid (cavitator) occupies more than 0.8 of the pipeline cross-section, the cavitation process occurs only in this zone, which makes up no more than 20% of the total volume of the processed liquid, which does not allow thermomechanical cracking of the entire volume of raw materials. In addition, the cavitator is not fixed rigidly, but changes its position under the influence of a moving stream. 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.

As already mentioned, the most famous and widely used processes of deep processing are catalytic - catalytic cracking, hydrocracking, etc. (Sukhanov V.P. Catalytic processes in oil refining. M., "Chemistry", 1973. Prokopyuk S.G., Masagutov PM Industrial Catalytic Cracking Units. M., Chemistry, 1974.) The serious disadvantages of such processes include the following: high pressures (up to 15 MPa) and heating temperatures of raw materials (450-550 ° C and above) lead to a serious increase in capital costs catalyst poisoning the need for regeneration in a very large current operating costs. Suffice it to say that due to the high cost of such processes, most Russian refineries do not have the ability to implement them.

Thermal cracking has been known for a very long time (Smidovich EV, Oil and gas processing technology. Part 2. M., Chemistry, 1968. Parkhomenko VE 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. 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, etc., 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 ° 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 advanced processing scheme for the proposed utility model is thermal cracking.

Disclosure of the invention.

The technical result of the application of the utility model is an increase in the yield of light target products and an increase in the depth of industrial processing of raw materials, simplification and cheapening of the process and equipment for the preparation and advanced processing of raw materials, reduction of operating and capital costs with a high depth of further processing, saving 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, petrochemical products) 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 inter-space ntnogo path equipment, process continuity, improving the quality of thermomechanical cracking products for further processing as compared with thermal cracking, reduction of harmful impurities, the solution of environmental problems. The main goal is to increase the depth of processing 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 treatment of water and harmful impurities), supply and heating of raw materials, separation of raw materials into fractions, removal of separation products, a separation apparatus is integrated, in which the hydrocarbon mixture is separated into two parts — the light part of the separation (low boiling fractions of NKF) and the heavy high molecular weight part of the 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). If the heat of separation products or commercial products is used for other purposes (depends on the task), 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 ° C to reduce viscosity and increase the 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 the heating equipment does not begin, although in some cases (depending on the composition of the raw materials), the heating temperature of the raw materials may be higher. Simultaneously with heating, the raw material can also be subjected to thermal cracking. The heavy high molecular weight liquid separation part (high boiling fractions of VKF) obtained after the separation apparatus is heated in a heating furnace (heater) separately from the feed to a temperature above 300 ° C or heated and subjected to thermal cracking. Typically, 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 a heating furnace or heater does not exceed 50% to prevent intense formation of coke deposits on the surfaces of coil heaters. Preferably, 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 (VKF heating channel). Then 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 no more than 300 ° С (depending on the composition and properties of the initial raw materials), i.e. heated so that uncontrolled thermal cracking has not yet begun. Direct contact of VKF, heated to a high temperature (for example, up to 400 ° С and higher, depending on the process conditions), and colder oil or other liquid hydrocarbon raw materials (for example, at a temperature of 200 ° С) leads to the explosive nature of heating of the raw material, the occurrence of oscillations and local cavitation zones, which in turn initiates thermomechanical cracking of heavy molecules of raw materials and VKF already in the mixing device. Then the mixture of raw materials and VKF is sent to a thermomechanical cracking device, 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 according to the results of the analysis of separation products (NKF and VKF). The mixture processed in the thermomechanical cracking device is sent to a 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). To increase the interfacial surface of the separated media and to more effectively and quickly separate them, the mixture of raw materials and VKF is sprayed (dispersed) into the separation apparatus with a decrease in pressure. The heavy liquid part of the separation (high-boiling fractions of VKF) after the separation apparatus, mainly with a boiling point above 350-360 ° C, is partially sent to the block for producing heavy commercial products (such as coke, bitumen, bitumen emulsions, coatings, oils, etc.) to the place of preparation and processing of raw materials according to this utility model is either cooled and transported to a remote place for the receipt of heavy commercial products. Partially returned to the reprocessing according to this utility model at 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 - a separation apparatus, a heating furnace (heater), a separation apparatus, the ratio of the costs of circulating VKF and raw materials is in range 1 ÷ 100. 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 temperature of the boiling fractions of light target commercial products, for example 350-360 ° C for the diesel fraction. This boundary temperature can be changed depending on the task and the requirements for the resulting products. After the separation device, light reaction fractions, mainly with a boiling point of up to 350-360 ° С, are sent to the unit for producing light commercial products (such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products, etc.) at the place of preparation and processing of raw materials according to this utility model, or after cooling and condensation, they are transported to a remote place for receiving light commercial 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 speeds of the raw materials, the circulating liquid part of the VKF and their mixtures in the mixing and processing devices can be adjusted 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 VKF directed to obtain heavy commercial products, and the number of devices 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. It is quite effective to use a distillation column as a separation apparatus, while the heavy high molecular weight liquid part of the separation (high boiling fractions of VKF) is the bottom residue, and the sum of all other light fractions after the column is low boiling fractions of NKF.

It is possible to use rotary-pulsation devices (RPA), light and radioactive irradiation devices, sound and ultrasound exposure from various types of external sources (piezo-emitters, magneto-emitters, etc.) using reagents and catalysts as processing devices for raw materials, VKF and their mixtures.

Both parts of the separation (NKF and VKF) 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 can be integrated into the separation apparatus. After the unit for producing heavy commercial products (coke, bitumen, bitumen emulsions, coatings, oils, etc.), light distillation is usually obtained, which is returned to the beginning of the process for reprocessing along with raw materials to obtain an additional amount of light target products. The bottom (heavy) residue after the unit for obtaining light commercial products (such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products, etc.), 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 for obtaining additional amounts of light target products. Depending on the task and the raw materials can be pre-heated in recuperative heat exchangers due to the heat of commercial products. During the cracking process, 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. Together with liquid hydrocarbon feedstocks, gaseous hydrocarbons, which are also hydrocarbon feedstocks, such as associated or natural gas, gas fractions obtained in the process of oil refining, in particular according to this utility model, and solid hydrocarbons in the form of a fine powder can also be sent for advanced processing. A certain positive effect is also provided by the fact that the feedstock and / or circulating high boiling fractions of VKF are subjected to mechanical and wave processing before the mixing device.

Directly, the apparatus for separating hydrocarbon feedstock into a light vapor-gas separation part (low boiling fractions of NKF) and a heavy liquid part of separating (high boiling fractions of VKF) is a capacitive apparatus that contains a housing, fittings for input-output of working and product media, fittings and devices for monitoring technological parameters of the device (temperature, pressure, etc.). In addition, in the separation apparatus through additional fittings and nozzles are integrated: a device for mixing raw materials with a heated heavy high molecular weight liquid separation part (circulating VKF), a thermomechanical cracking device 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 gas-vapor separation part (NKF) is built-in to the upper part of the apparatus, after which the purified NKF leaves the apparatus and is sent to receive commercial products, and the filtrate by gravity enters the lower part of the apparatus and mixes with VKF 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 ° C for diesel fractions. 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 parameters of the process. In the lower part of the apparatus, a VKF separation device is built-in, part of the VKF is sent for the production of heavy commercial products (such as coke, bitumen, etc.), and the other part returns to the beginning of the process and circulates in a closed loop - separation apparatus, 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. Besides. A separator-settler is integrated in the lower part of the apparatus to separate from the VKF the part necessary for circulation and to clean the circulating part of the VKF from coke particles and other mechanical impurities. In order to optimize gas-vapor and liquid flows in the apparatus and the separator, to more clearly separate the liquid phase from the gas-vapor and rectification of the latter, internal devices such as distillation plates of various designs, Rashig rings, grids, etc. are built into the apparatus and separator. For commissioning, the apparatus separation has built-in heat exchangers or a jacket with steam heating. The structural dimensions of the separation apparatus, separator and other elements depend on the productivity of the processing complex, the composition of the raw materials and the task for its processing.

A mechanical and wave processing device is combined with a mixture mixing and dispersing device and can be called a “turbodynamic disintegrator” (TDD). 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.

As mentioned above, 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. 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. Because Since bubbles are formed in different sizes, when the bubbles collapse, waves of a wide spectrum of frequencies appear, i.e. there is a mechanical and acoustic impact on the medium. The cavitation phenomenon is widely used in various fields of technology, in particular, for the intensification of various chemical reactions and transformations.

Since 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 the transition to the zone of high pressure and the kinetic energy of the expanding fluid is exhausted, 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 not enough gas, the bubble completely closes in the first period of life. Therefore, a fairly clearly defined “cavitation zone” filled with moving bubbles is created near the streamlined body (obstacle).

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 velocity after the beginning of cavitation causes a rapid increase in the number of cavitation bubbles, after which they merge into a common cavitation cavity. If the cavitation cavity slams close to the streamlined body, then repeatedly repeated impacts lead to the destruction (to the so-called cavitation erosion) of the surface of the streamlined body, therefore, the velocity of the processed medium should be high enough (based on the experience of more than 5 m / s) so that the bubbles do not have time to slam near the body, and slammed away from the streamlined body, then cavitation will be voluminous and will not lead to the destruction of the streamlined body.

Cavitation more easily occurs in real liquids, as The low tensile strength of real liquids is associated with the presence of so-called cavitation nuclei in them: poorly wetted areas of the solid, solid particles with cracks filled with gas, microscopic gas bubbles that are protected from dissolution by monomolecular organic shells, and ionic formations that arise under the influence of cosmic rays. If atmospheric air or another gas is introduced into the cavity through the body near which cavitation occurs, then the size of the cavity increases. Cavitation flows resulting from the supply of gas into the cavity are called artificial cavitation. In the case of artificial cavitation when the body moves in a fluid (or fluid near a streamlined body) at a speed of 6 ÷ 10 m / s, the same effects of its flow around can be obtained as at speeds of about 100 m / s. In the case of processing a heated hydrocarbon liquid by this utility model and during its cracking, a gas phase always occurs, which is the nucleus of cavitation. The amount of the gas phase can be controlled by pressure in the processing device so that the amount of the gas phase does not exceed 25% by mass. (Kornfeld M., Elasticity and strength of liquids, M.-L., 1951; Birkhoff G., Sarantonello E., Jets, tracks and caverns, trans. From English, M., 1964: Pernik A.D., Problems cavitation, 2nd ed., L., 1966.)

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 immediately after the input swirls. The diameter of the mixing chamber is chosen so that the speed of the mixture does not exceed 10 m / s. 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 mixing process of 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 section. To increase the number of cavitation and acoustic treatment zones formed on the entire surface of the cavitator, through round holes with diameters from 0.1 to 100 mm were made as nodes for the formation of cavitation zones. To worsen the streamlining, the holes can be made with sharp jagged edges. The diameter and number of holes depend on the flow rate of the processed mixture, the diameter and number of holes is chosen so that the speed of the mixture in the holes exceeds 5 m / s. After the cavitator, 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 cavitator holes and swirl channels is determined by the analysis of fractions and products obtained as a result of processing, 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 the maximum intensity of cavitation and acoustic effects on the mixture of input media, determined experimentally. Instead of holes to increase the number of cavitation and acoustic treatment zones formed, the cavitator can be made in the form of filling balls, cylinders, parallelepipeds, sprockets, tori, dumbbells, Raschig rings and other rigid volumetric figures. Dimensions of 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 ..

In order to achieve 100% processing depth and reduce unsaturated hydrocarbons to almost zero level, fittings or nozzles are provided in the device body for introducing active hydrogen and / or light radicals into the mixing chamber and / or into the treatment zone before and / or behind the cavitator, or device (block) the production of active hydrogen and / or light radicals is integrated into the processing device. One of the most non-simple options that was used in the experiments is that the cavitator is made in the form of a cone or a convex 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 nodes Cavitation zones formed through holes with an effective diameter of 0.1 to 100 mm. At high consumption of raw materials for processing, so as not to reduce the quality of spraying the mixture, the number of outlet swirlers and / or nozzles built into the processing device can be more than one of each type. Not only 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 there is no avalanche-like breaking of molecules due to this excitation) are sent to a processing device in which the raw materials are subjected to mechanical (for example, cavitation) and wave action of various natures (sound, ultrasonic , cavitation, electromagnetic, light, radiation, etc.) and a wide range of resonant frequencies. 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 of raw materials is very large, and has not yet been studied in detail, so the number of different vibrational levels excited by preheating is also very large. The application of mechanical and wave action on the raw material heated by heat to a subcritical temperature allows initiating and activating the thermomechanical cracking process, i.e. the process of breaking bonds of already excited molecules, while, in contrast to conventional thermal cracking, the initiated process of breaking bonds by applying a resonant effect 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 products are better than thermal cracking products, 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 small. 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 only in one device, in any two or in all three.

For cavitation processing of oil (or other liquid hydrocarbon feedstock) heated to subcritical temperature and applying acoustic impact to it, various devices are used in the implementation of the proposed utility model: hydrodynamic devices, rotary-pulsation apparatuses (RPA), etc. In the framework of the proposed utility model, it is most optimal to use such special devices, the action of which is based on the hydrodynamic effects of medium motion with a high (more than 5 m / s) velocity along channels with obstacles and turns of various shapes, which leads to the appearance of local zones of reduced pressure, in which the process of evaporation and separation of the light cracking phase is more intense, and at sufficiently high temperatures, thermomechanical cracking of the feedstock takes place to obtain an additional amount of light fractions. With this approach, the cavitation and acoustic treatment process occurs in the entire volume of the treatment zone, and not only in the near-surface zones, as when using, for example, rotary-pulsation apparatuses (RPA).

After processing and carrying out the thermomechanical cracking process, 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 part (high boiling fractions of VKF). As the most optimal option, the heated mixture of raw materials and VKF is dispersed in the separation apparatus to increase the interfacial surface and more efficient separation of the gas-vapor part from the liquid.

As a result, after the separation apparatus, two main products are obtained: the light part of the gas-vapor separation (low boiling fractions of NKF), with a boiling point predominantly up to 350-360 ° 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% of the mass. Due to non-ideal separation) of fractions with a boiling point up to 350-360 ° C. During further processing by known methods, fuel products such as gasoline (range of boiling points: boiling point - 180-200 ° C), kerosene (range of boiling points: 180-200 ° C - 230-240 ° C), diesel fuel are produced from NKF (boiling point range: 230-240 ° С - 350-360 ° С), petrochemical products, such as toluene, benzene, etc. In the future - light commercial products. VKF consists of heavy fractions with a boiling point primarily above 350-360 ° C. During further processing by known methods from VKF it is possible to obtain heavy commercial products, such as coke, bitumen, bitumen emulsions, coatings, etc. In the future, heavy commercial products. The boundary separation temperature of 350-360 ° C is selected because the end of the boiling of diesel fuel is 350-360 ° C. If the guests and requirements for fuel products change over time, the separation boundary temperature can be changed accordingly. Units for the production of commercial products usually include the following well-known processes: hydrotreating, reforming, platforming, etc. (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 (C ravochnik petrochemist. In two volumes. Volume 1, under the. ed. Ogorodnikov SK L., Chemistry, 1978, s.53-55).

When implementing the proposed utility model, it is proposed, as one of the simplest and best options, to heat the feedstock to subcritical temperature, use the heavy residue of the separation of liquid hydrocarbon feedstock (liquid phase separation VKF), obtained directly during the implementation of the proposed utility model, the necessary part of which returns to the beginning process. The use of VKF for heating the liquid phase (it does not need to be specially prepared or purchased, it appears during the implementation of the utility model) with a boiling point mainly above 360 ° С allows increasing the operating temperature in the separation apparatus, intensifying thermal and / or thermomechanical cracking and, accordingly to increase the depth of processing and the yield of light products above their potential content in the feedstock, as well as to simplify and reduce the cost of equipment and reduce energy and operational costs, and also allows optimal and efficient 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. Direct contact of VKF, heated to a high temperature (for example, up to 400 ° С and higher, depending on the process conditions), and colder oil or other liquid hydrocarbon raw materials (for example, at a temperature of 200 ° С) leads to the explosive nature of heating of the raw material, the occurrence of oscillations and local cavitation zones, which in turn initiates thermomechanical cracking of heavy oil molecules already in the device for mixing raw materials and VKF and leads to an increase in the yield of light fractions (gasoline, kerosene, diesel, products eftehimii et al.) in 1.5-15 times depending on the composition of the feedstock (heavy oil, fuel oil, etc.). The circulating VKF must be heated not lower than 300 ° С, and the preliminary heating of the raw material before mixing it with the VKF should not be higher than 450 ° С in order to avoid coking. In this case, part of the VKF necessary for heating the raw material to a subcritical temperature is circulated in a closed circuit: the separation apparatus — the heating furnace (heater) VKF — the separation apparatus, and the ratio of the circulating VKF and raw materials is in the range of 1 ÷ 100. It should be borne in mind that 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 ° C, which ultimately leads to only 69-78% of light petroleum products from their potential content in the feedstock and talk here about increasing depth foreman heel, i.e. obtaining bright light product above its potential content of the feedstock 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 separation of NKF, due to the intensively conducted process of evaporation and separation, contains, in addition to light fractions in a gaseous form, and liquid droplets in which there are heavy high-boiling components with a boiling point above 350-360 ° C. Therefore (if necessary, because it depends on the properties of the raw materials and the task), NKF is first sent to separation devices (drop separation, filtration or rectification), usually built into the separation apparatus, then sent for further use and obtaining marketable products, etc. to. 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. 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 the spot, or, after cooling, they are sold as intermediates for further processing. Because the liquid part of the separation (VKF) due to non-ideal separation contains some small amount of light fractions with a boiling point below 360 ° C, then upon receipt of heavy commercial products (bitumen in a vacuum installation, etc.), light distillation may occur, which is returned if necessary (depends on the properties of the raw materials and the task), at the beginning of the process for reprocessing and obtaining an additional amount of light target products.

In the process of cracking the feed, unsaturated hydrocarbons are formed, which can subsequently condense, which limits the processing depth. For the most complete and deep processing and increase the yield of light target products and fractions, the processing scheme should be supplemented with a device that allows saturating open bonds with atomic hydrogen and / or light radicals with minimal costs. Using an earlier application for inventions (application for the PCT system RU 2009000074), the problem can be solved by organizing a process scheme in which the feed and the catalyst do not contact, so that 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. To achieve a high processing depth, the raw material or its part is subjected to the processing process according to this utility model repeatedly. For this, molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, associated gas, natural gas, including gas obtained in the process of preparation and advanced processing, pentane fractions, xylene, toluene, some light fractions, including and 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 water production unit ode), after which active hydrogen and / or light radicals are sent to cracking devices for the reaction — to a heating and cracking device for VKF, to a mixing device for heated VKF and raw materials, to a thermomechanical cracking device in which the mixture initiates a controlled process of breaking molecules (thermomechanical cracking) is subjected to mechanical and wave effects of various nature and a wide range of frequencies, for example, cavitation, sound, ultrasonic vibrations, and 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. The pressure in the reactor with the catalyst should be greater than the pressure in the cracking devices. At the same time, 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 commercial product production units, or sent to a separation apparatus, light target reaction fractions after the separation apparatus, mainly with a boiling point up to 350-360 ° С, are sent to a target commercial product preparation unit such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products, etc. at the place of preparation and deep processing of raw materials according to this utility model or transported to a remote processing site to obtain light commercial products. At the same time, such expensive processes as hydrotreating, rimming, etc. in the blocks for the production of light commercial products may not be used, because open bonds of the cracking radicals of the raw material are saturated to the unit for obtaining marketable products, and the properties and composition of the obtained fractions are adjusted by changing the mode and process parameters. In addition, during the processing of raw materials according to this utility model, the amount of harmful impurities, for example, sulfur compounds, decreases. during the processing, the bulk of the sulfur is transferred to hydrogen sulfide and then removed from the process by known methods with the further production of, for example, atomic sulfur and other useful by-products. The heavy residue after the separation apparatus (VKF), mainly with a boiling point of 350-360 ° C, is sent to the block for the production of heavy commercial products such as bitumen, coke, etc., or partially or completely sent for re-processing according to this utility model to the beginning of the process . Solid hydrocarbon feedstocks (e.g. coal, shale, vegetable products, etc.) are sent to the finely divided pulverization unit and introduced into the feedstock and / or heavy separation residue before it is processed again, gaseous hydrocarbons are also introduced into the feedstock and / or separation residue Before its repeated processing, liquid, solid and gaseous hydrocarbons can be processed according to this scheme 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.

Heavy raw materials do not come into direct contact with the catalyst, poisoning and coking do not occur, there is no need for catalyst regeneration, the process is simplified and becomes more reliable, the cost of the process and equipment is significantly reduced, i.e. there is a decrease in capital and operating costs, the processing depth can be increased to 100%. At the same time, there is a saving of raw materials in the development of the required number of target commodity products, in other words, the optimal and rational use of raw materials for their further processing in the implementation of this scheme. In addition, various residues and wastes that accumulate in the process, for example, oil production and refining, lead to environmental degradation, and their processing according to this utility model with highly liquid products allows solving environmental problems, as well as making additional profit.

To obtain atomic hydrogen and / or light radicals, the use of catalysts is most optimal. For this, gaseous molecular hydrogen, hydrogen-containing media and / or a reactor with a catalyst are heated to a temperature of 300-500 ° C, and sometimes higher (although more effective catalysts can be found over time that will allow the formation of hydrogen and / or light radicals at lower temperatures, for example, at 20-100 ° С and below). The processes of catalytic decomposition of hydrocarbons are widely known. At the same time, during the interaction of hydrogen and hydrogen-containing media with molybdenum, cobalt, zinc, vanadium, nickel, aluminosilicate, zeolite-containing and other catalysts, for example, based on aluminum oxide, or other types of catalysts, atomic hydrogen and / or light radicals are formed, which effectively interacts with hydrocarbon molecules and saturates open bonds of light radicals obtained as a result of cracking of hydrocarbons, resulting in the formation of saturated light targets good quality fraction. These light radicals, together with the light cracking radicals of the feed, form a light target product molecule. It also happens with other light hydrogen-containing media. 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 utility model, or partially or completely to obtain heavy commercial products such as coke, bitumen and others (depending on the task). However, much more light radicals are formed during cracking of raw materials than heavy ones, 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. This is evidenced, for example, by thermal cracking processes, as a result of which lighter fractions in larger quantities are obtained from heavy raw materials than heavy ones. Therefore, a significantly smaller amount of separation residue is sent for reprocessing than raw materials. Moreover, the separation residue can be sent for re-processing at the beginning of the process together with the feedstock, or separately for an additional processing unit according to this utility model. With repeated reprocessing of the heavy separation residue (VKF), the feedstock will be processed into light target products with an efficiency of up to 100%.

A reactor with a catalyst (in accordance with the earlier application for inventions No. 2009101883) can be made in the form of a cylinder, ball, annular cylinder, parallelepiped or other three-dimensional 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 shapes, 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. Or, 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 catalyst reactors (reactor packages) may be used. 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.

The distinctive features of this scheme 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.

A brief description of the figures.

In figures 1-5 presents enlarged schematic diagrams of the preparation and processing of hydrocarbons.

Figure 1-5 indicated: 1 - a heating device and thermal cracking 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 - a device for spraying (dispersing) a mixture into a separation apparatus; 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, diesel fuel, petrochemical products, etc. - reforming, platforming, etc.); 11 - unit for the preparation of heavy commercial products (bitumen, bitumen emulsions, coatings, coke, etc.); 12 - a separate heater for preheating raw materials; 13 is a block for the production of atomic hydrogen and / or light radicals. 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 well-known processes: hydrotreating, reforming, platforming, etc., 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 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. re . Ogorodnikov SK L., Chemistry, 1978, s.53-55).

If the raw materials are not supposed to be used at the site of in-depth processing to obtain marketable products, then it is advisable to use the variant of the scheme shown in figure 1. The circulating high-boiling VKF fractions after the separation apparatus are fed to the VKF heating and cracking device (FIG. 1, position 1), then to the raw material mixing and heating device (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). Then 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. 1, position 4) with a decrease in pressure to increase the interfacial surface of the separated media in the separation apparatus (Fig. .1, item 5). After the separation apparatus, the NCP are sent to the separation device (Fig. 1, position 6), after the separation device, light reaction fractions, mainly with a boiling point of up to 350-360 ° C, are sent (transported) after partial cooling on a regenerative heat exchanger (Fig. 1 , item 8) and final cooling and condensation (not shown in the diagram for simplicity) to the unit for producing light commercial products (such as liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products, etc.), the filtrate after the separator for the floor eniya additional amount of recycled light end products recycled to the beginning of the process together with the circulating part of the CCF. A 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 utility model 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 through closed loop - separation apparatus (figure 1, position 5), a heating furnace (heater) (figure 1, position 1) - 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 diagram for simplicity) to the unit for producing heavy commercial products (such as coke, bitumen, bitumen emulsions, coatings, oils and etc.).

If commodity products are produced at the place of processing according to this utility model, then such a scheme is presented in figure 2. NKF after partial cooling on a recuperative heat exchanger (figure 2, position 8) is sent to the unit for obtaining light commercial products (figure 2, position 10), and VKF after partial cooling on a recuperative heat exchanger (figure 2, position 9) is sent to the block receiving heavy commercial products (figure 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.

If, for technological reasons, the heat of NKF and VKF is not used for pre-heating the raw materials, or it is not necessary to cool them for supplying commercial products to the cooking units at the place of use of the utility model, then the preliminary heating of the raw materials is done on a separate heater (Fig. 3, position 12), or in the same heater (furnace) in which the circulating VKF is heated, but in a separate coil (Fig. 4, position 1). In these embodiments, 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, you can use the heat of commercial products.

In the process of cracking the feed, unsaturated hydrocarbons are formed, which can subsequently condense, which limits the processing depth. For the most complete and deep processing and increase the yield of light target products and fractions, the processing scheme 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 it is heated x VKF and raw materials (Fig. 5, position 2), into a thermomechanical cracking device (Fig. 5, position 3), and atomic hydrogen and / or light radicals can be directed only to one of the cracking devices, to any two devices and to all three cracking devices. At the same time, 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.

6 shows a separation apparatus. Heated to the required temperature VKF and heated raw materials are supplied to 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 thermomechanical cracking device (Fig.6, position 3), 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, Then the mixture is dispersed (sprayed) (Fig.6, position 4) with a decrease in pressure to increase the interfacial surface of the separated media in the separation apparatus. Moreover, the mixing, processing and spraying devices are combined in one apparatus, which can be called a turbodynamic disintegrator (TDD). 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 (filter, droplet separator) located in the upper part of the separation apparatus. The separated (filtered) NKF are sent to the unit for preparing light commercial products, and the filtrate flows by gravity to 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. In addition, various filtering devices may be provided in the VKF circulation loop, not shown in the diagrams for simplicity. Fittings for input-output of working and product media, fittings and devices for monitoring the technological parameters of the apparatus (temperature, pressure, level of phase separation, etc.) 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 ° C for the diesel fraction and is maintained automatically, the level of separation of the combined-gas phase of the NKF and the liquid phase of the VKF is below half the height of the separation apparatus. The phase separation temperature of 350-360 ° C is selected 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. Rectification plates, Raschig rings, etc. can be integrated in the separator. Then, not only the process of droplet separation and filtration, but also the rectification process will occur in the separator, which will lead to an improvement in the quality of NKF supplied for the production of light commercial products. Devices for mixing raw materials and VKF, processing (thermomechanical cracking) the mixture, dispersing (spraying), and also separating the gas-vapor part of the separation of NKF are built into the separation apparatus, i.e. make up one with it, which leads to a decrease in capital and operating costs, for example, to a decrease in metal consumption and heat loss. If a distillation column is used as a separation apparatus, then a spraying device may not be used, then the bottom residue after the column is VKF, and all light fractions in total comprise NKF.

The processing device is a turbodynamic disintegrator TDD is presented in Fig.7-10. In Fig.7-10 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. On Fig shows a device with alternating cylindrical, confuser and diffuser inserts for the movement of the medium 1, two cavitators with holes and a nozzle in the form of a cone. Figure 9 shows a device with alternating cylindrical, confuser and diffuser inserts for the movement of 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. Figure 10 shows a swirler with double-entry tangential channels (top view and section along section AA). 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 raw materials and VKF in the mixing chamber (Fig.7-9, position 16), the raw material and the whole mixture is heated to a critical temperature. Then the heated mixture of raw materials and VKF is sent to the cavitator (Fig. 7-9, position 17), in which the mixture is subjected to mechanical and wave effects of a different nature and a wide range of frequencies, for example, cavitation, to initiate a controlled process of breaking bonds of molecules (thermomechanical cracking), sound, ultrasonic vibrations. The treated mixture is sent to the outlet swirler (Figs. 7-9, item 18) to improve further atomization and dispersed through a nozzle (Figs. 7-9, item 19) with a decrease in pressure into the separation apparatus to increase the interfacial surface and to more effectively separate the mixture into NKF and VKF. The velocities in the channels of all swirlers, cavitators (cavitators) and nozzles (nozzles) should be sufficiently high, at least above 5 m / s. Specific speeds are selected empirically based on the composition and properties of the raw materials and the task. The confuser and diffuser inserts increase the transverse component of the speed of the mixture and intensify the mixing process. The parameters of the mixing chamber and inserts are determined empirically.

Embodiments of the invention.

The proposed utility model is implemented on 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 utility model are implemented. In addition, 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 figure 1, the separation apparatus in figure 6, the turbodynamic disintegrator in figure 7. The raw materials used were oil from the Vishenskoye deposit in the Ulyanovsk Region (Ratov AN, Nemirovskaya GB and other problems of oil development in the Ulyanovsk Region. "Chemistry and Technology of Fuels and Oils", No. 4, 1995). Oil contains many tarry compounds and impurities. Oil of other fields was used, for example, Nurlatneft oil and gas production unit with a different composition, as well as various bottoms, used oils, etc. The pressure of raw materials and circulating VKF in bench experiments was up to 1.0 MPa and higher, the temperature of circulating VKF was up to 450 ° С and higher, the temperature of raw materials up to 200 ÷ 250 ° C, the ratio of the costs of circulating VKF and raw materials was in the range up to 30 or more. At these pressures and temperatures, the linear feed rates of the feed and circulating VKF were more than 5 m / s. With an increase in the feed rate and feedstock feed rate, 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.

Before starting the process of separation of liquid hydrocarbon feedstock, VKF is prepared. VKF, which is essentially a heavy separation residue, 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. From the separation apparatus (FIGS. 1, 6, position 5), the mixture is pumped to an electric heater — an analog of an industrial furnace (FIG. 1, position 1) and returned. At the same time, light fractions are continuously removed, accumulating the liquid phase of VKF. With continuous circulation and a certain temperature, a heavy residue (VKF) after a certain time (process parameters depend on the composition of the initial mixture of hydrocarbons) acquires all the necessary properties. The end of the process is controlled by determining the physicochemical properties and composition of the liquid phase of the HCF.

Preheated raw materials and heated to the required temperature (Fig. 1, position 1) 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). The 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 the raw material is also carried out, then the processed mixture is sent to the output 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). After the separation apparatus, the circulating VKF is again sent to the heating device (Fig. 1, 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 (drop separation, filtration or rectification), (Figs. 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 (Figs. 1, 6, position 6) is sent for cooling and condensation and is analyzed. The liquid separation part (VKF) after the separation apparatus (Fig. 1, position 5) and the separation from the VKF of the circulating part (Fig. 1, 6, position 7) is sent for cooling and analyzed. Devices for mixing and heating raw materials by circulating VKF, mechanical and wave treatment, evaporation and separation into gas-vapor and liquid phases, and the separation device for NKF are combined in one apparatus. This reduces the amount of equipment and, accordingly, capital and operating costs.

The following are some of the results of the separation process.

Example 1

Oil fields of the Ulyanovsk region.

Separation effect: NKF - 78.5% of the mass., VKF - 20% of the mass., Gas yield - 1.5% of the mass. The enlarged fractional composition of oil and NKF after processing according to the proposed utility model (in terms of oil, taking into account the separation coefficient) and some characteristics are shown in table 1.

Table 1 Selection limits The output of fractions for oil,% of the mass. Source oil The easy part of the separation (NKF) The beginning of the boil, ° C 68 43 up to 200 ° C 10.6 32,3 up to 250 ° C 15.1 43.5 up to 300 ° C 22.2 58.9 up to 350 ° C 29.9 71.7 Density, kg / cubic m 941.2 787.6 Kinematic viscosity, cSt, at 20 ° С 87.9 1,2 The sulfur content,% of the mass. up to 5.0 up to 1.3 Chloride Content, mg / L up to 2000 up to 50

Example 2

Oil NGDU Nurlatneft.

Separation effect: NKF - 77% of the mass., VKF - 21.5% of the mass., Losses - 1.5% of the mass. The enlarged fractional composition of oil and NKF after processing according to the proposed utility model (in terms of oil, taking into account the separation coefficient) and some characteristics are shown in table 2.

table 2 Selection limits The output of fractions for oil,% of the mass. Source oil Easy Parting (NCF) The beginning of the boil, ° C 38 35 up to 180 ° C 11.9 34.7 up to 240 ° C 19.9 49.5 up to 350 ° C 36.7 68.9 up to 360 ° С 37.8 70.3 Density, kg / cubic m 910.5 788.7 Kinematic viscosity, cSt, at 20 ° С 140.1 1.4 The sulfur content,% of the mass. 3.64 1.4 Chloride Content, mg / L up to 2000 up to 50

In tables 1 and 2, the amount of obtained NKF was 77-78.5% of the mass., And the total number of fractions up to 350-360 ° C is 70.3-71.7% of the mass. This is due to the fact that the separation process into NKF and VKF is not ideal (even on a distillation column), therefore, a small part of heavy fractions with a boiling point above 350-360 ° C also get into the NKF. The amount of unsaturated hydrocarbons corresponds to the lower boundary of unsaturated hydrocarbons generated during catalytic cracking.

Example 3

Characteristics of the results of the analysis of the VKF oil separation NGDU Nurlatneft are shown in table 3.

Table 3 Name of indicator Value Test method Needle penetration depth 0.1 mm: at 25 ° C 76 GOST 11501 at 0 ° С 10 The softening temperature of the ring and ball, ° C 47.6 GOST 11506 Elongation, cm: at 25 ° C > 100 GOST 11505 At 0 ° C 2 Fragility temperature, ° С minus 7.7 GOST 11507 with the addition of clause 3.2 Flash point, ° С > 250 GOST 4333 Change in softening temperature after heating, ° C 0.1 GOST 18180, GOST 11506 with the addition of clause 3.3 Penetration index minus 0.7 Appendix 2 Mass fraction of water-soluble compounds,% 0.445 GOST 11510 Adhesion to stone material (control sample), points 3 GOST 11508

Example 4

Atmospheric-vacuum distillation of the bottoms of Ulyanovsk oil after AT (fuel oil) showed the absence of a gasoline fraction in it, the content of the kerosene fraction (240-360 ° C) amounted to 2.9% by weight, the diesel fraction (240-360 ° C) - 11, 8% of the mass. The treatment of the investigated bottoms by the proposed utility model showed the following results: the number of low boiling fractions (NKF - the easy part of the separation) was 74-79% of the mass. depending on the process parameters. The NKF content of the target fuel compositions was 88-90% by mass, of which the gasoline fraction (NK - 180 ° C) was 20.8% by mass and kerosene (180-240 ° C) was 17.4% by mass ., diesel (240-360 ° C) - 61.8% of the mass. The total content of the target products with a boiling point up to 360 ° C increased from 14.7% of the mass. up to 71% of the mass. in terms of the original product.

Example 5

Atmospheric-vacuum distillation of unused M-8B oil (universal motor oil) 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 of 380-500 ° C. The thermomechanical cracking of the test oil according to this utility model led to the formation of approximately 22% gasoline, 9% kerosene and 46% diesel fractions, i.e. the content of the target products with a boiling point up to 360 ° C during processing according to the proposed utility model increased from 5.2 to 77%, i.e. about 15 times. Thus, the fundamental possibility of thermomechanical cracking of high-boiling (above 360 ° С) oil components into target products with a boiling point up to 360 ° С was shown. The study of the composition of the used oil M-8B, which was processed according to this utility model, showed the presence of 19% gasoline, 15% kerosene and 38% diesel fractions in it. In general, the content of the target components with a boiling point of up to 360 ° C during the thermomechanical cracking of used oil was 72%.

Example 6

In the process of cracking the feed, unsaturated hydrocarbons are formed, therefore, for the most complete and deep processing and increase the yield of light target products and fractions, open bonds must be saturated with atomic hydrogen and / or light radicals. The scheme of such an installation is supplemented by a unit with a catalyst (according to the PCT application RU 2009000074, RU No. 2009101883) for producing atomic hydrogen and / or light radicals and is shown in FIG. 5. Hydrogen from the balloon is heated, fed to the unit for producing atomic hydrogen and / or light radicals (Fig. 5, position 13), then sent to the cracking device (Fig. 5, position 1, 2, 3), the reacted mixture is dispersed (Fig. 5 , position 4) with decreasing pressure in the separation apparatus (Fig. 5, position 5). After the separation apparatus (Fig. 5, position 5), the VKF completely returns to the beginning of the process for repeated repeated processing, and the NFC is fed to the separation device (Fig. 5, position 6), after which the NFC is cooled and analyzed. The process is continuous. Some results are shown in table 4. The processing depth reaches 97-98%. Taking into account the generated non-condensed gases, one can confidently speak of almost 100% depth of processing of raw materials using this utility model. Unsaturated hydrocarbons within the measurement error were not detected.

Table 4 Selection limits The output of fractions,% of the mass. Source oil Reaction products The beginning of the boil, ° C 65 34 up to 180 ° C 10.9 40.7 up to 240 ° C 17.6 48,4 up to 350 ° C 34.2 97.3 up to 360 ° С 35.9 97.9 The sulfur content,% of the mass. up to 4,5 up to 0.1

To achieve almost the same results in this utility model, instead of hydrogen, you can use a propane-butane mixture from a balloon and other light products enriched with hydrogen or fractions. When using a propane-butane mixture from a cylinder instead of hydrogen, the total yield of light target fractions practically did not change and amounted to 97.3% of the mass. The number of gasoline fractions (with a boiling point up to 180 ° C) decreased by 1.6% by mass., And the number of diesel fractions (with a boiling point from 240 ° C to 360 ° C) increased by 1.7% by mass. kerosene fractions (with a boiling point from 180 ° C to 240 ° C) practically did not change. With the addition of a propane-butane mixture in the feedstock up to 3%, the yield of the gasoline fraction increased slightly (up to 1%). With the addition of up to 3% shale crushed to the size of 0.05-1 micrometer to the feedstock, the yield of light target fractions remained practically unchanged, i.e. part of the solid hydrocarbons was processed into light liquid hydrocarbons.

Example 7

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, if necessary partially cooled, are mixed again. The resulting “synthetic” oil contains about two or more times more fuel fractions than the original product. In addition, if the density of the initial oil is 950 kg / m ³ (API = 17), then the density of the “synthetic” oil decreases to 850 kg / m ³ (API = 35), and the kinematic viscosity, respectively, from 83 cSt to 6 cSt. As a result of such an operation, the cost of “synthetic” oil increases significantly; it is easier to transport and process. This approach is especially promising for enterprises remote from refineries and producing heavy and viscous oil, such as, for example, in South America, Canada, and in some regions of Russia. In the same way, relatively cheap fuel oil and still cheaper still bottoms, oil sludge can be processed into much more expensive high-potential oil. In this case, environmental problems are solved.

Industrial applicability.

Thus, the proposed utility model makes it possible to carry out industrial in-depth (in this case, the depth of further processing is increased by 1.5-15 times depending on the feedstock — heavy oil, fuel oil, etc.) and highly profitable oil preparation and processing, including heavy, residues of oil refining and petrochemical industries, oil sludge, waste oils, natural bitumen and other liquid and gaseous organic media with obtaining tested commercial products and can be used in oizvodstve 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. Almost 100% of the processing depth (calculated by the yield of light target fractions and products) can be achieved by repeated processing of heavy fractions of VKF using a unit for producing atomic hydrogen and / or light radicals. In this case, solid hydrocarbons can also be processed efficiently. The proposed installation and devices are easy to operate and do not require large capital and operating costs.

Claims (25)

1. Installation for in-depth processing of hydrocarbon raw materials, including preparation (preliminary purification from water and harmful impurities), supply and heating of raw materials, separation of raw materials into fractions, removal of separation products, characterized in that a separation apparatus is built into the processing unit, in which the hydrocarbon mixture is separated into two parts — the light vapor-gas separation part (low boiling fractions of NKF) and the heavy high molecular weight liquid part of separation (high boiling fractions of VKF), the raw materials are preheated in heat recovery units heat exchangers due to the heat of one or all separation products (NKF and VKF), and / or in a separate or common (but separate from heating VKF coil) with heating of the VKF heating furnace (heater) to a temperature above 20 ° C or they are heated and subjected to thermal cracking, the high molecular weight liquid part of the separation (high boiling fractions of VKF) obtained after the separation apparatus is heated in a heating furnace (heater) separately from the raw material to a temperature above 300 ° C or heated and subjected to thermal cracking, the mass fraction of VKF subjected to heat cracking in a heating furnace or heater does not exceed 50%, then the raw materials are finally heated in a direct mixing device for the raw materials with the heated high molecular weight liquid separation part (high boiling fractions VKF), and the mixture is 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 ° С (depending on the composition and properties of the feedstock), i.e. heated so that uncontrolled thermal cracking has not yet begun, then the mixture of raw materials and VKF is sent to a thermomechanical cracking device in which the mixture is subjected to mechanical and wave action of a different nature and a wide range of frequencies, for example, cavitation, to initiate a controlled process of breaking bonds of molecules (thermomechanical cracking) exposure, sound, ultrasonic vibrations, and for cavitation processing of raw materials heated to subcritical temperature and application of acoustic air The effects use such devices, the action of which is based on the hydrodynamic effects of the motion of multiphase media with velocities of more than 5 m / s along channels of various shapes, the mixture of raw materials and VKF processed in the thermomechanical cracking device is dispersed to increase the interphase surface of the separated media and disperse them more efficiently and quickly ( sprayed) into the separation apparatus with decreasing pressure, the high molecular weight liquid part of the separation (high-boiling fractions of VKF) after the separation apparatus, mainly at a rate with boiling water at temperatures above 350-360 ° С, they are partially sent to the block for producing heavy commercial products (coke, bitumen, bitumen emulsions, coatings, oils and other heavy products) at the place of preparation and processing of raw materials according to this utility model, or they are cooled and transported to a remote site the place of receipt of heavy commercial products, and partially returned for reprocessing according to this utility model at the beginning of the process (to the heater) to increase the yield of light products and the depth of processing, and the returned part of the HCF is circulated on a closed loop — a separation apparatus, a heating furnace (heater), a separation apparatus, the ratio of the flow rates of circulating HCF and raw materials is in the range of 1–100, the light steam-gas part of the NCF after the separation apparatus, which contains both light fractions of the feedstock and light fractions of products thermal cracking VKF and thermomechanical cracking a mixture of raw materials and VKF, sent to the separation device (filtration, droplet separation, distillation), and the temperature in the separation device corresponds to the maximum temperature To boil the fractions of light target commercial products, for example 350-360 ° С for a diesel fraction, after the separation device, light reaction fractions, mainly with a boiling point up to 350-360 ° С, are sent to the unit for producing light commercial products (liquefied gas, gasoline, kerosene, diesel fuel, petrochemical products and other light products) at the place of preparation and processing of raw materials according to this utility model or after cooling and condensation are transported to a remote place for receiving light commercial products, the filtrate after the separator, to obtain an additional amount of light target products, they are returned for reprocessing at the beginning of the process together with the circulating part of the VKF, and devices for mixing raw materials and circulating VKF, wave and mechanical processing of the mixture, dispersion, as well as separation of the gas-vapor part of the separation of NKF are built into the mixture separation apparatus on liquid (VKF) and gas-vapor (NKF) parts, and the quality of the separation products and their ratio, depending on the properties of the feedstock, are regulated by temperature and pressure we have 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 consumption of raw materials, the circulating liquid part of the VKF and their ratio, as well as the speeds of the raw material, the circulating liquid part of the VKF and their mixture in the devices mixing, processing, dispersing, the separation level of the vapor-gas phase of the NKF and the liquid phase of the VKF in the separation apparatus is supported at a given value of the above technological parameters, the value of the flow of VKF sent to obtain t heavy commercial products, and the number of devices built into the apparatus for mixing raw materials and VKF, processing and dispersing the mixture can be more than one of each type, depending on the productivity of the processing industry. 2. Installation according to claim 1, characterized in that a distillation column is used as the separation apparatus, while the heavy liquid part of the separation (high boiling fractions of VKF) is the bottom residue, and the sum of all light fractions after the column is low boiling fractions of NKF. 3. Installation according to claim 1, characterized in that the processing scheme is supplemented by 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 gasoline fractions obtained during processing, which are sent to cracking devices - to a heating and / or cracking device for circulating VKF and raw materials, to a mixing device for heated VKF and raw materials, to a thermomechanical cracking device and, and 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 at the same time. 4. Installation according to claim 1, characterized in that the adjustment of the speeds of the raw materials, the circulating liquid part of the VKF and their mixtures in the mixing, processing and dispersing devices is carried out by changing the mechanical parameters of the design of these devices. 5. Installation according to claim 1, characterized in that rotary-pulsation apparatuses (RPA), devices of light, radiation, exposure to sound and ultrasound from various types of external sources (piezo-emitters, magneto-emitters) are used as raw material processing devices, VKF and their mixtures etc.), devices using reagents and catalysts. 6. Installation according to claim 1, characterized in that both parts of the separation of NKF and VKF are sent to the mixing unit to produce 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 advanced processing, and the processing and mixing devices can be integrated into the separation apparatus. 7. Installation according to claim 1, characterized in that the light distillation after the block for producing heavy commercial products is returned to the beginning of the process for reprocessing together with raw materials and / or circulating HCFs to obtain an additional amount of light target products. 8. Installation according to claim 1, characterized in that the still (heavy) residue after the block for producing light commercial products is returned to the beginning of the process for reprocessing together with raw materials and / or circulating HCFs to obtain an additional amount of light target products. 9. Installation according to claim 1, characterized in that the raw materials are preheated in recuperative heat exchangers due to the heat of commercial products. 10. Installation according to claim 1, characterized in that in the circulation circuit of the VKF part there is a built-in device for cleaning VKF from harmful impurities, mechanical particles and coke particles. 11. Installation according to claim 1, characterized in that, together with liquid hydrocarbon raw materials and / or circulating HCFs, gaseous hydrocarbons, for example associated or natural gas, gas fractions obtained in the oil refining process, in particular, according to this utility model, are also sent for advanced processing as well as solid hydrocarbons in the form of a fine powder. 12. Installation according to claim 1, characterized in that the feedstock and / or circulating high boiling fractions of the VKF are subjected to mechanical and wave processing before the mixing device. 13. A device for separating hydrocarbon feedstock into a light vapor-gas separation part (low boiling fractions of NKF) and a high molecular weight liquid part of separation (high boiling fractions of VKF), containing 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, and other parameters), characterized in that a device for mixing raw materials with a heated high molecular weight liquid part is built into the separation apparatus through additional fittings and nozzles separation (by circulating high boiling fractions of VKF), a thermomechanical cracking device in which a mixture heated to a certain subcritical temperature 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, a device for dispersing (spraying) the mixture into the apparatus to increase the interfacial surface In the upper part of the apparatus, a separation device (filter, droplet separator) of the vapor-gas separation part (NFC) is installed, after which the purified NFC is sent to obtain light commercial products, and the filtrate by gravity enters the lower part of the apparatus and mixes with VKF, and 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 ° C for a diesel fraction, part of the VKF is sent for production of heavy commercial products, and the other part returns to the beginning of the process and the separation apparatus circulates in a closed circuit, the heating furnace (heater), separation apparatus, a fitting is integrated into the apparatus’s body for monitoring the phase separation level and maintaining it at a predetermined value by the VKF flow rate, sent to the production units of heavy commodity products at specified values of other technological process parameters, the number of devices for mixing raw materials and VKF, processing and mixture extraction (spraying) can be more than one of each type, depending on the productivity of the processing industry, and for commissioning, the separation apparatus has built-in heat exchangers or a steam-heated jacket. 14. The apparatus according to claim 13, characterized in that a separator-settler is integrated in the lower part of the separation apparatus for separating from the VKF the part necessary for circulation and for cleaning the circulating part of the VKF from coke particles and other mechanical impurities. 15. The apparatus according to claim 13, characterized in that, in order to optimize the gas-vapor and liquid flows in the separation apparatus and separation device, to more clearly separate the liquid phase of the VKF from the combined-gas phase of the NKF and rectify the latter, internal devices are built into the separation apparatus and separation device types of distillation plates of various designs, Raschig rings, nets, etc. 16. The device of acoustic and cavitation processing (turbodynamic disintegrator), including a pipe for inputting the medium to be treated, a cavitator, a pipe for outputting the processed medium, characterized in that the device is equipped with two inlet pipes for two inlet media, two vortex inserts (swirlers) for two inlet media, a cylindrical mixing chamber of the input media, and the diameter of the mixing chamber is chosen so that the speed of the mixture does not exceed 10 m / s, the mixing chamber is installed immediately after the input swirls, the cavitator is installed after the mixing chamber and is made in the form of a flat, concave or convex (for example, in the form of a cone) along the movement of the mixture of two input media of the figure, mounted across the flow and covering the entire cross section of the flow, to increase the number of cavitation zones formed and acoustic processing on the entire surface of the cavitator as nodes of the formation of cavitation zones made through circular holes (as one of the options with sharp jagged edges) with a diameter of from 0.1 to 100 mm, and the diameter and the number of holes depends on the flow rate of the medium, the diameter and number of holes is chosen so that the mixture velocity in the holes exceeds 5 m / s, after the cavitator there is an outlet swirler for the mixture of input media and a nozzle, and all swirlers and nozzle are made so that the flow velocity in swirl channels and nozzles were higher than 5 m / s, swirl channels made in the form of two-input or multi-input tangential channels or channels in the form of Archimedes spirals, screw or screw spirals, twisting the flow of channels of another shape, and 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, 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. 17. The device according to clause 16, characterized in that the holes in the cavitator are 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 selected so that the ratio of the perimeter of the figure to its area was maximum, the size of the holes (the minimum and maximum distance between the two points of the perimeter of each hole) are in the range from 0.1 to 100 mm, and the velocity of the medium in each hole exceeds 5 m / s. 18. The device according to clause 16, characterized in that the device has 2 or more cavitators, the distance between them, 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 effects on the mixture of input media. 19. The device according to clause 16, characterized in that to increase the number of cavitation and acoustic treatment zones formed, the cavitator is made in the form of filling balls, cylinders, parallelepipeds, stars, tori, dumbbells, Rashig rings and other rigid volumetric figures, and the dimensions of volumetric figures are in the range from 0.1 to 100 mm, the velocity of the medium in all the gaps between the backfill elements exceeds 5 m / s, and the backfill can be inserted into a container, for example, mesh, for the convenience of changing elements of different backfill and moving the cavitator (container EPA) along the axis of the processing apparatus for finding the optimal location for creating maximum intensity acoustic cavitation and subjecting the mixture input media, and the number of containers may be more than one. 20. The device according to clause 16, characterized in that the gas part of the mixture in the device does not exceed 25% mass and is regulated by the pressure in the device. 21. The device according to clause 16, wherein the nozzle is made in the form of a cylinder, cone or Laval nozzle. 22. The device according to clause 16, characterized in that the device body has fittings or nozzles for introducing active hydrogen and / or light radicals into the mixing chamber and / or into the treatment zone before and / or behind the cavitator, or device (unit) for receiving active hydrogen and / or light radicals are integrated into the processing device. 23. The device according to clause 16, characterized in that the cavitator is made in the form of a cone or a truncated cone in the form of a cone or a truncated cone with an angle at the apex of the cone of more than 10º, and on the entire surface of the cavitator as nodes of formation of cavitation zones are made through holes (as one of the options - with sharp jagged edges) with sizes from 0.1 to 100 mm. 24. The device according to clause 16, characterized in that the number of output swirls and / or nozzles integrated in the processing device, more than one of each type. 25. The device according to clause 16, wherein the cylindrical sections of the mixing chamber, as well as the cylindrical sections of the movement of both media before mixing are alternated with confuser and / or diffuser inserts.