RU74916U1 - SCHEME OF OIL REFINING PRODUCTION WITH A DEEP-TREATMENT UNIT - Google Patents

Abstract

1. Scheme of oil refining production with an in-depth processing unit for the preparation and processing of oil, including heavy oil, residues of oil refining and petrochemical industries and other liquid organic media, including preparation blocks (degassing, purification from mechanical and other impurities, desalination and dehydration) and preliminary heating, as well as fractionation units and production of commercial products, characterized in that in the production scheme before the fractionation unit, or after it, include a block about processing of raw materials in which thermomechanical cracking is carried out by heating the raw material to a certain subcritical temperature, which is lower than the start temperature of an avalanche-like uncontrolled thermal cracking by several fractions of a degree Celsius or more, for example, 0.01-400 ° C (depending on the composition and properties of the raw material ), i.e. they are heated so that uncontrolled thermal cracking has not yet begun, to initiate a controlled process of breaking bonds of molecules (thermomechanical cracking), mechanical and acoustic resonant effects of various nature and a wide range of frequencies are applied to the raw materials, 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, whose action is based on hyd dynamic effects of multiphase media movement through the channels of different shapes, materials after processing by mechanical and wave action in the processing unit it is directed to the separation unit, wherein the separated

Description

The utility model relates to the oil refining industry, and specifically to the field of oil preparation and refining, including heavy oil, residues of oil refining and petrochemical industries, oil sludge, used oils and other liquid organic media for their further in-depth processing to produce guest products and can be used in the production of hydrocarbon fuels, petrochemicals, bitumen, etc.

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).

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 (degassing, purification from mechanical and other harmful impurities, desalination, dehydration). Oil preparation is carried out by various methods, the most famous of which is the preparation 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 N.R., Sharikhin V.V.

Tube furnaces in the refining and petrochemical industries. M., "Chemistry", 1987, p. 6, etc.). Liquid and gaseous hydrocarbons are heated in them.

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. The considered operations (preparation, heating, proper separation of the low boiling fraction) in the process of hydrocarbon separation occur sequentially, that is, are not combined in time. Each of them requires a separate sophisticated equipment. Some types of equipment have a limited resource.

Units for the production of commercial products usually include the following well-known processes: hydrotreating, reforming, platforming, etc., or at the first stage a compounding unit, a bitumen block for the production of oxidized bitumen or a bitumen block combined with a vacuum block for the production of non-oxidized bitumen, as well as equipment for the production of bitumen coatings, emulsions, boiler fuels, oils and other commercial products (Petrochemical Handbook. In two volumes. Volume 1, under the editorship of Ogorodnikov S.K.L., Chemistry, 1978, p. 53-55).

In the most general case, the oil refining production scheme consists of the following blocks described above: preparation blocks (degassing, cleaning of mechanical and other harmful impurities, desalination, dehydration), heating blocks, and fractionation blocks (atmospheric AT or atmospheric vacuum AVT tube , or other fractionation options, for example, using a system of heat exchangers or cooling devices) and obtaining marketable products (hydrotreating, reforming, platforming, etc.) - gasoline, kerosene, diesel Lib, petrochemicals, bitumen, bituminous emulsions, coatings, oils, and others.

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.

Widely used schemes for advanced processing are schemes using catalytic processes - blocks of catalytic cracking, hydrocracking, etc. (Sukhanov V.P.

Catalytic processes in oil refining. M., “Chemistry”, 1973. Prokopyuk S.G., Masagutov P.M. Industrial catalytic cracking plants. M., “Chemistry”, 1974.) 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 and the need their regeneration to 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.

Schemes of in-depth processing using thermal cracking units have been known for a very long time (Smidovich E.V. Technology of oil and gas processing. Part 2. M., Chemistry, 1968. Parkhomenko V.E. Technology of oil and gas processing. 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 technical result, which is achieved by the claimed utility model, is to reduce capital and operating costs, to increase the yield of high-quality light fuel products above their potential content in the feedstock, in the controllability of the cracking process and the simplicity of the design of the equipment of the thermomechanical cracking process in manufacturing and operation.

The aim of the invention is to increase the yield of light light fractions (gasoline, kerosene and diesel, petrochemicals) higher than their potential content in raw materials and increase the depth of processing, which leads to optimal and rational use of raw materials for their further processing, reducing operating and capital costs, simplicity and reliability of equipment design, simplicity and reliability of control and

adjustments to the thermomechanical cracking process, reducing coking and increasing the overhaul of equipment, process continuity, improving the quality of thermomechanical cracking products for further processing compared to thermal cracking.

This goal is achieved by the fact that in the technological scheme for the preparation and processing of liquid hydrocarbon raw materials, which includes blocks for the preparation (degassing, purification of mechanical and other impurities, desalination and dehydration) and preheating of the raw materials, fractionation and production of commercial products, in front of the fractionation unit (before feeding atmospheric AT or atmospheric vacuum AVT tubing or other fractionation options, for example using a system of heat exchangers or cooling devices), or thereafter, a unit for in-depth processing of raw materials is included. In the in-depth processing unit, the raw materials are heated thermally, i.e. the most economical in this case, a method to a certain temperature, which is lower than the start temperature of an avalanche-like uncontrolled thermal cracking by a few fractions of a degree, degrees or tens and hundreds of degrees Celsius, for example, 0.01-400 ° C (depending on the composition and properties of the raw material) , i.e. heated so that uncontrolled thermal cracking has not yet begun. Heating can be carried out in a fire or electric furnace, or another type of furnace, as well as in heat exchangers of various designs, in which the raw material is heated with a coolant. As a coolant can be used various high-temperature coolants (gas, steam, liquid metal, molten salts, organic).

Raw materials heated (for example, by heat carrier) to a subcritical temperature (vibrational levels of molecules are already excited, but there is no avalanche-like breaking of molecules due to this excitation) is sent to a processing unit in which the raw material is subjected to mechanical (e.g., 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 low. Chemical reagents and catalysts are not used in the process.

For cavitation processing of oil (or other liquid hydrocarbon feedstock) heated to subcritical temperature and applying acoustic influence 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 the medium moving at high speed through 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 goes more intensively. 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 feed is sent to the evaporation and separation unit, in which the vapor-gas part (low boiling fractions of NKF) is separated from the liquid (high boiling fractions of VKF). The unit for heating the raw material with a coolant to a subcritical temperature, it is advisable to combine the processing and separation of the raw materials into the gas-vapor and liquid phases in one apparatus, or, in the case of heating the raw materials using firing or electric furnaces, it is advisable to combine the processing and separation of the raw materials in the same apparatus, which leads to reduce the amount of equipment, 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 360 ° C. Therefore (if necessary, because it depends on the properties of raw materials and

of the assigned task), the NKF is first sent to separation devices (droplet separation, filtration or rectification), usually built into the separation unit, then sent for further use and obtaining marketable products, because NKF contains mainly gas, gasoline, kerosene and diesel fractions, petrochemical products. The filtrate after separation devices is sent for reprocessing 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 unit 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. It is also advisable that the liquid separation part (VKF) be fully or partially submitted for re-treatment to the same or a separate processing unit to further increase the yield of light products (the process can be repeated many times depending on the composition of the raw materials, the results obtained and the task).

Distinctive features of this scheme for the preparation and processing of liquid hydrocarbon raw materials allow several processes: 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 future use.

The proposed schemes with an in-depth processing unit are implemented on a pilot plant with a capacity of up to 0.2 t / h (up to 1500 t / year). 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 coolant and cooling products, pumping equipment and instrumentation.

In figures 1-6 presents enlarged schematic diagrams of the preparation and processing of liquid organic raw materials with a block of in-depth processing.

Figure 1-6 is indicated: 1 - block preparation of raw materials (degassing, dehydration, desalination, purification from mechanical and other harmful impurities) and its preheating; 2 - block advanced processing of raw materials; 3 - block separation into liquid and gas-vapor parts; 4 - fractionation unit (atmospheric AT or atmospheric vacuum AVT tube, other fractionation options); 5 - a unit for producing light commercial products (gasoline, kerosene, diesel fuel, petrochemical products, etc. - reforming, platforming, etc.); 6 - unit for the preparation of heavy commercial products (bitumen, bitumen emulsions, coatings, oils, etc.); 7 - block mixing the liquid and gas-vapor separation; 8 - block cooling mixture; 9 - cooling unit for the gas-vapor separation part (low boiling fractions of NKF); 10 - cooling unit for the liquid separation part (high boiling fractions VKF); 11 is an additional fractionation unit.

If the raw material is heavy oil or oil residues (fuel oil, oil sludge, waste oil, etc.), then it is advisable to use a variant of the oil refining production scheme with an in-depth processing unit shown in Fig. 1. Raw materials after the preparation and preheating unit (Fig. 1, position 1) are supplied to the in-depth processing unit (Fig. 1, position 2) and after in-depth processing to the separation unit (Fig. 1, position 3). After the separation unit, the low boiling fractions of the NKF are sent to the fractionation unit (Fig. 1, position 4) and to the preparation unit for light commercial products (Fig. 1, position 5). The bottom residue (fuel oil) after the fractionation unit (Fig. 1, position 4) is returned to the processing unit (Fig. 1, position 2) for secondary processing in order to obtain additional light products. The high boiling fractions of the VKF are sent to the unit for the preparation of heavy commercial products (Fig. 1, position 6), the light distillation after which (if it is formed) is also returned to the processing unit (Fig. 1, position 2) for secondary processing in order to additionally obtain light products . Part of the high boiling fractions VKF (or VKF completely, depending on the task and the properties of the raw materials) after the separation unit (Fig. 1, position 3) is returned (shown by a dotted line) to the processing unit (Fig. 1, position 2) for secondary processing with the aim of additional receiving light products. The liquid separation part (VKF) or part of it can be submitted for reprocessing to an additional separate processing unit (not shown in the figure for simplicity) to further increase the yield of light products (the process can be repeated many times depending on the composition of the raw material, the results obtained and the task )

If the raw material is light or medium oil, gas condensate, then it is advisable to use a variant of the scheme of oil refining production with a block of advanced processing, presented in figure 2. The raw material after the preparation and preheating unit (FIG. 2, position 1) is supplied to the rectification unit (FIG. 2, position 4) and then to the preparation unit for light commercial products (FIG. 2, position 5). The bottom residue (fuel oil) after the fractionation unit (FIG. 2, position 4) is sent to the processing unit (FIG. 2, position 2) and after in-depth processing is fed to the separation unit (FIG. 2, position 3). After the separation unit, the low boiling fractions of the NKF are returned to the fractionation unit (Fig. 2, position 4) and to the preparation unit for light commercial products (Fig. 1, position 5). The high boiling fractions of the VKF after the separation unit (FIG. 2, position 3) are sent to the heavy commodity product preparation unit (FIG. 2, position 6), the distillation after which (if it is formed) is also returned to the processing unit (FIG. 2, position 2 ) for secondary processing in order to obtain additional light products. Part of the high boiling fractions VKF (or VKF completely, depending on the task and the properties of the raw materials) after the separation unit (Fig. 2, position 3) is returned (shown by a dotted line) to the processing unit (Fig. 2, position 2) for secondary processing for the purpose additional receiving light products. The liquid separation part (VKF) or part of it can be submitted for reprocessing to an additional separate processing unit (not shown in the figure for simplicity) to further increase the yield of light products (the process can be repeated many times depending on the composition of the raw material, the results obtained and the task )

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 a variant of the scheme of oil refining production with a block of in-depth processing, presented in figure 3. The raw material after the preparation and preheating unit (Fig. 3, position 1) is supplied to the in-depth processing unit (Fig. 3, position 2) and after in-depth processing to the separation unit (Fig. 3, position 3). After the separation unit, the low boiling fractions of the NKF and high boiling fractions of the VKF are sent to the mixing unit (Fig. 3, position 7) and then to the cooling unit (Fig. 3, position 8). The “synthetic” oil obtained as a result of mixing NKF and VKF is transported for further in-depth processing and production of marketable products. It 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. Especially promising

such an approach is for enterprises remote from oil 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 bottoms can be processed into significantly more expensive high-potential oil. Part of the high boiling fractions VKF (or VKF completely, depending on the task and the properties of the raw materials) after the separation unit (Fig. 3, position 3) is returned (shown by a dotted line) to the processing unit (Fig. 3, position 2) for secondary processing for the purpose additional receiving light products. The liquid separation part (VKF) or part of it can be submitted for reprocessing to an additional separate processing unit (not shown in the figure for simplicity) to further increase the yield of light products (the process can be repeated many times depending on the composition of the raw material, the results obtained and the task )

If it is necessary to transport NKF and VKF separately for further processing and obtaining marketable products, then it is advisable to use a variant of the oil refining production scheme with an in-depth processing unit, shown in Fig. 4. Raw materials after the preparation and preheating unit (Fig. 4, position 1) are supplied to the in-depth processing unit (Fig. 4, position 2) and after in-depth processing to the separation unit (Fig. 4, position 3). After the separation unit, low-boiling fractions of NKF are sent to the cooling unit of NKF (figure 4, position 9) and high-boiling fractions of VKF are sent to the cooling unit of VKF (figure 4, position 10). Then both parts (NKF and VKF) are transported for further in-depth processing, possibly to production located in different places. Part of the high boiling fractions VKF (or VKF completely, depending on the task and the properties of the raw materials) after the separation unit (Fig. 4, position 3) is returned (shown by a dotted line) to the processing unit (Fig. 4, position 2) for secondary processing for the purpose additional receiving light products. The liquid separation part (VKF) or part of it can be submitted for reprocessing to an additional separate processing unit (not shown in the figure for simplicity) to further increase the yield of light products (the process can be repeated many times depending on the composition of the raw material, the results obtained and the task )

If the return of the NKF after the separation unit to the fractionation unit leads to overload and intense or unstable operation of the fractionation unit, it is advisable to use the variant of the oil refining production scheme with the in-depth processing unit shown in Fig. 5. The raw material after the preparation and preheating unit (Fig. 5, position 1) is supplied to the rectification unit (Fig. 5, position 4) and then to the light commercial product preparation unit (Fig. 5, position 5). VAT residue (fuel oil)

after the fractionation unit (Fig. 5, position 4) it is sent to the processing unit (Fig. 5, position 2) and after in-depth processing is fed to the separation unit (Fig. 5, position 3). After the separation unit, the low boiling fractions of the NKF are sent to an additional independent fractionation unit (Fig. 5, item 11) and to the unit for preparing light commercial products (Fig. 5, item 5). The high boiling fractions of the VKF after the separation unit (Fig. 5, position 3) are sent to the cooking unit for heavy commercial products (Fig. 5, position 6), the distillation after which (if it is formed) is also returned to the processing unit (Fig. 5, position 2 ) for secondary processing in order to obtain additional light products. Part of the high boiling fractions VKF (or VKF completely, depending on the task and the properties of the raw materials) after the separation unit (Fig. 5, position 3) is returned (shown by a dotted line) to the processing unit (Fig. 5, position 2) for secondary processing with the aim of additional receiving light products. The liquid separation part (VKF) or part of it can be submitted for reprocessing to an additional separate processing unit (not shown in the figure for simplicity) to further increase the yield of light products (the process can be repeated many times depending on the composition of the raw material, the results obtained and the task )

In some cases, depending on the task and the properties of the raw materials (for example, if heavy fractions of the raw materials are suitable for the preparation of heavy commercial products such as bitumen), it is advisable to use a variant of the oil refining production scheme with the advanced processing unit shown in Fig.6. The raw material after the preparation and preheating unit (Fig.6, position 1) is supplied to the in-depth processing unit (Fig.6, position 2) and after in-depth processing to the fractionation unit (Fig.6, position 4), then to the light commodity preparation unit products (Fig. 6, position 5) and a unit for preparing heavy commercial products (Fig. 6, position 6), the distillation after which (if it is formed) is returned to the processing unit (Fig. 6, position 2) for secondary processing for the purpose of additional receiving light products. Part of the bottom residue (or the bottom residue in full, depending on the task and the properties of the raw materials) after the fractionation unit (Fig. 6, position 4) is returned (shown by a dotted line) to the processing unit (Fig. 6, position 2) for secondary processing for the purpose additional receiving light products. The bottom residue after the fractionation unit (Fig. 6, position 4) or part of it can be submitted for reprocessing to an additional separate processing unit (not shown in the figure for simplicity) to further increase the yield of light products (the process can be repeated many times depending on the composition raw materials, the results obtained and the task).

As the initial raw material was used heavy 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. Used oil and other fields, such as NGDU "Nurlatneft", with a different composition, as well as various bottoms, waste oils, etc.

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

Example 1

Samples of heavy oil and NKF after oil processing according to the proposed schemes were analyzed. The studied oil and NKF samples differ significantly in quantitative and qualitative indicators. The initial oil sample is characterized by a lower potential content of light fractions, a higher content of sulfur and asphalt-resinous substances (table 1).

The light part (NCF) of oil separation after thermomechanical cracking according to the proposed utility model contains a large yield of light fractions (gasolines and diesel components). The content of fractions n.k. - 180 ° C is 45.81% of the mass, while only 11.95% of the mass is released from oil, (table 2). According to its physicochemical characteristics (density, viscosity, pour point, content of resins of silica gel and asphaltenes, as well as the yield of light fractions), NKF is close to condensates. Reducing the sulfur content in a wide fraction by 2.5 times is a very urgent task for oil workers and oil refiners (table 3).

Table 1
The distillation (ITC) of the original heavy oil in the apparatus ARN-2 and the characteristics of the obtained fractions Fraction number Tempera
fraction boiling round at 760 mm Hg Oil yield% mass Viscosity mm ² / s P ²⁰ ₄ N ²⁰ ₄ Temperature ° C Content Separate Total At 20 ° C At 50 ° C solidification outbreaks sulfur,% of the mass. n.k. 38 ° C one n.k. -fifty 0.71 0.04 2 50-60 0.57 1.28 680.7 1.3930 0.06 3 60-70 0.61 1.89 685.5 1.3940 0.08

four 70-80 0.76 2.65 692.2 1.3950 0.09 5 80-90 1.05 3.70 710.0 1,3990 0.10 6 90-100 2,32 6.02 721.5 1,4015 0.11 7 100-110 0.51 6.53 730.7 1,4100 0.13 8 110-120 0.67 7.20 738.6 1.4137 0.19 9 120-130 0.98 8.18 750,2 1.4192 0.25 10 130-140 1.10, 9.28 759.0 1.4240 0.39 eleven 140-150 1.45 10.73 767.9 1.4278 0.44 12 150-160 0.95 11.68 773.7 1,4300 0.65 13 160-170 0.12 111.80 779.5 1.4410 0.78 fourteen 170-180 0.15 11.95 785.1 1.4420 0.90 fifteen 180-190 0.13 12.08 791.3 1.4430 Bottom
e-65 49 0.96 16 190-200 0.88 12.96 1.29 0.87 796.5 1,4438 -60 54 1.15 17 200-210 1.35 14.31 1.88 1.23 802.3 1,4442 -fifty 59 1.24 eighteen 210-220 2.15 16.46 2,30 1.41 811.1 1.4510 -48 62 1.38 19 220-230 1.86 18.32 2.64 1,58 820.5 1,4554 -47 65 1,53 twenty 230-240 1,57 19.89 2.91 1,60 824.2 1.4590 -39 81 1.68 21 240-250 1.35 21.24 3.37 2.03 828.4 1,4600 -32 95 1.90 22 250-270 2.45 23.69 6.26 3.14 849.6 1.4722 -26 112 2.24 23 270-290 3.25 26.94 8.67 3.44 862.6 1.4764 -21 121 2.68 24 290-310 3,58 30.52 10.54 4,56 872.6 1.4848 -16 131 2.75 25 310-330 3.27 33.79 14.45 5.41 881.7 1.4900 -four 150 2.97 26 330-350 2.94 36.73 26.28 8.44 896.1 1.4970 -one, 165 3.24 table 2
Acceleration (ITC) of NKF processed in the block of advanced processing of the original oil in the apparatus ARN-2 and the characteristics of the obtained fractions Fraction number Tempera
fraction boiling round at 760 mm Hg Oil yield% mass Viscosity,
mm ² / s P ²⁰ ₄ N ²⁰ ₄ Tempera
round, ° С Containing
nie Separate Total At 20 ° C At 50 ° C stagnation yvan flash shki sulfur,% of the mass. n.k. 36 ° C one n.k. -fifty 0.42 - 0.006

2 50-60 0.57 0.99 662.1 1.3850 0.01 3 60-70 2.85 3.84 682.6 1.3860 0,03 four 70-80 3.71 7.55 687.5 1.3840 0.04 5 80-90 2.79 10.34 692.3 1.3919 0.05 6 40-100 2.83 13.17 704.6 1.3960 0.06 7 100-110 4.19 17.36 717.0 1,4020 0.08 8 110-120 3.70 21.06 726.5 1,4069 0.12 9 120-130 3.80 24.86 736.1 1.4110 0.14 10 130-140 5.66 30.52 747.4 1.4171 0.16 eleven 140-150 2.97 33.49 758.3 1.4210 0.24 12 150-160 4.06 37.55 765.8 1.4266 0.35 13 160-170 3.97 41.52 774.3 1.4310 0.44 fourteen 170-180 4.29 45.81 780.9 1,4342 0.68 fifteen 180-190 1.45 47.26 1.34 0.93 787.5 1,4355 Bottom
e-65 48 0.77 16 190-200 1.86 49.12 1,58 1,07 796.2 1,4392 -63 52 0.96 17 200-210 3.89 53.01 1.98 1.27 805.7 1.4427 -51 60 1,02 eighteen 210-220 3.53 56.54 2.08 1.35 809.6 1.4463 -fifty 65 1,08 19 220-230 4,56 61.10 2,35 1.40 813.2 1.4512 -49 70 1.14 twenty 230-240 4,55 65.65 2,56 1,52 822.5 1.4549 -40 79 1.20 21 240-250 5.30 70.95 3.16 1.85 831.9 1,4608 -35 94 1.38 22 250-270 6.14 77.09 4.23 2,35 846.6 1,4686 -29 102 1,54 23 270-290 5.45 80.54 5.77 2.92 856.7 1,4753 -twenty 140 1.96 24 290-310 2.23 82.77 7.60 3,51 863.3 1.4780 -fifteen 143 2,34 25 310-330 2.20 84.97 9.64 4.21 866.8 1,4803 -5 146 2,52 26 330-350 3,51 88.48 14.21 5.63 878.8 1.4862 -2 150 2.60

Table 3
Physico-chemical characteristics of oil and NKF No. l / p Characteristic unit of measurement Value Oil NKF one Density kg / m ³ 910.5 791.8 2 Kinematic viscosity: Mm ² / s (cSt) at 20 ° C 140.07 1.79 at 50 ° C 39.37 1.19 3 Content: % of the mass. Sulfur 3.64 1.45 Silica gel resins 18,4 1,1 Asphaltenov 3.0 0.06 four Coking % 8.6 0.20 5 Ash content % 0,069 0.002 6 Fractions yield % of the mass. Up to 200 ° C 12.96 49.12 Up to 360 ° С 37.80 89.92

Example 2

Thermomechanical cracking of fuel oil was carried out according to the proposed utility model. Atmospheric-vacuum distillation of the initial fuel oil showed the absence of a gasoline and kerosene fraction in it, the content of the diesel fraction (boiling point up to 360 ° C) was 8.1% of the mass. The thermomechanical cracking of the fuel oil under study in the in-depth processing unit showed the following results: the number of low boiling fractions of NKF was 68-72% of the mass. depending on the process mode. The NKF content of the target fuel compositions was 85-86% by mass, of which 19.9% by mass of the gasoline (NK - 180 ° C) and 14.7% by mass of kerosene (180-240 ° C) ., diesel (240-360 ° C) - 65.4% of the mass. The total content of the target products with a boiling point up to 360 ° C during thermomechanical cracking increased from 8.1% of the mass. up to 58-62% of the mass. in terms of the original product.

Example 3

A study of the quality of gasoline and diesel fractions in NKF after applying thermomechanical cracking according to the proposed utility model showed that the content of aromatic hydrocarbons in gasoline fractions is 10-12%, in diesel fractions 19-22%, olefin contents 25-28% and 5-7%, respectively .

The content of aromatic hydrocarbons in catalytic cracking gasolines is 30–40%, olefin — 25–35%, in thermal cracking gasolines the content of unsaturated is much higher.

From the above it follows that the quality of thermomechanical cracking products after the processing unit is much better than thermal and similar to the quality of catalytic cracking products at significantly lower (10-100 times) capital and operating costs.

The vapor-gas phase (NKF) is a distillate containing gasoline and diesel fractions, petrochemical products. It can be seen that the effect of the processing process according to the proposed schemes is significant: the content of fuel fractions with a boiling point up to 360 ° C in the vapor-gas phase of separation (NFC) is approximately two times higher (in terms of the initial heavy oil taking into account the separation coefficient) than in the original oil , and when processing fuel oil, this figure is 10-15. The depth of selection of the distillate (the amount of the evaporated part of the hydrocarbons) depends on the temperature, pressure and flow rate of the coolant, that is, on the technological mode of the process. At the pilot plant, the depth of extraction of the evaporated part of the oil of the Vishenskoye field was reached - up to 85%, NGDU "Nurlatneft" - up to 80% (in contrast to the processing depth of about 30% in the classical processing scheme without an in-depth processing unit).

In order to optimize gas-vapor and liquid flows in the separation unit, to more clearly separate the liquid phase from gas-vapor and preliminary separation, filtering and rectifying the latter (NKF), internal separation devices such as distillation plates of various designs, Rashig rings, nets and etc. (for simplicity, the separation and filtration unit is not shown in the schemes).

Thus, the proposed utility model - a scheme of oil refining with an in-depth processing unit - allows for in-depth (this increases the depth of further processing by 1.5-15 times depending on the feedstock - heavy oil, fuel oil, etc.) and highly profitable preparation and processing of oil, including heavy oil, residues of oil refining and petrochemical industries, oil sludge, waste oils and other liquid organic media to produce guest products and can be used in the production of hydrocarbon fuels, petrochemicals, bitumen, etc. Accordingly, the yield of the most valuable fuel compositions — gasoline, kerosene and diesel fractions, and petrochemical products — is also increasing.

Claims (5)

1. Scheme of oil refining production with an in-depth processing unit for the preparation and processing of oil, including heavy oil, residues of oil refining and petrochemical industries and other liquid organic media, including preparation blocks (degassing, purification from mechanical and other impurities, desalination and dehydration) and preliminary heating, as well as fractionation units and production of commercial products, characterized in that in the production scheme before the fractionation unit, or after it, include a block about processing of raw materials in which thermomechanical cracking is carried out by heating the raw material to a certain subcritical temperature, which is lower than the start temperature of an avalanche-like uncontrolled thermal cracking by several fractions of a degree Celsius or more, for example, 0.01-400 ° C (depending on the composition and properties of the raw material ), i.e. they are heated so that uncontrolled thermal cracking has not yet begun, to initiate a controlled process of breaking bonds of molecules (thermomechanical cracking), mechanical and acoustic resonant effects of various nature and a wide range of frequencies are applied to the raw materials, 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, whose action is based on hyd dynamic effects of the movement of multiphase media through channels of various shapes, after processing the raw materials by mechanical and wave action in the processing unit, it is sent to the separation unit, in which the raw materials are divided into gas-vapor and liquid parts, gas-vapor part after separation (filtration, droplet separation, rectification) on internal devices in the separation unit, they are sent to fractionation and production of light commodity products (gasoline, kerosene, diesel fuel, petrochemical products, etc.), the filtrate is returned for re-use processing at the beginning of the process, the liquid part is sent to the blocks for the production of heavy commodity products (bitumen, bitumen emulsions, coatings, oils, etc.), and (or) they are sent partially or completely for re-processing to the in-depth processing block to further increase the depth of processing of raw materials moreover, the wave and mechanical processing unit and the separation unit for liquid and combined cycle parts with integrated separation devices for combined cycle parts are combined in one apparatus. 2. The scheme according to claim 1, characterized in that both parts of the separation are sent to a mixing unit to produce synthetic oil with an increased potential content of light fuel products and a significantly lower density and viscosity compared to the feedstock, which is then sent for further advanced processing, moreover, the processing, separation and mixing units can be combined in one or different devices. 3. The scheme according to claim 1, characterized in that one or both parts of the separation are sent to cooling units to obtain intermediates for the purpose of their transportation to the place of further in-depth processing and obtaining marketable products. 4. The scheme according to claim 1, characterized in that the combined-cycle part after the separation unit is sent to an additional independent fractionation unit before being fed to the commodity product receiving units, and the commercial product receiving units can be either general or independent. 5. The scheme according to claim 1, characterized in that the light distillation after the block for producing heavy commercial products (bitumen, bitumen emulsions, coatings, oils, etc.) is returned to the beginning of the process for reprocessing and obtaining an additional amount of light target products.