RU2153522C1 - Rocket fuel production process (versions) - Google Patents

Abstract

FIELD: petroleum processing; propellants. SUBSTANCE: crude oil is subjected to electrical desalting and dehydration, atmospheric and atmospheric vacuum distillation to give kerosene fraction, which is hydrofined. When conducting process, heat carrier is steam that is partially produced by combustion of associated gas and/or combustible process gas releasing thermal petroleum processing and/or and/or in thermodestructive processing of petroleum and/or intermediate products, which steam is fed into process network at 50-70 C and pressure 3-5 kg/sq.cm. 60-85% of gas is burned in process furnaces and 15-40% in steam generator to form condensate. The latter, supplemented by preheated chemically purified water, is used in steam generator. EFFECT: reduced power consumption, and increased yield of product per 1 unit weight of fuel, and improved quality of product. 23 cl, 1 tbl

Description

 The invention relates to oil refining and, specifically, to the production of jet fuel.

 Closest to the first embodiment of the method according to the invention in essence and the achieved result is a method for producing jet fuel from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electrodesalting and dehydration of the latter by passing an oil stream through an electrode system, located in electric dehydrators, atmospheric and / or atmospheric vacuum distillation of desalted oil using atmospheric distillation columns , with the separation of the kerosene fraction, hydrotreating the obtained kerosene fraction in the presence of a catalyst using hydrotreating reactors, followed by compounding the fractions obtained in the distillation and hydrotreating processes (see Erich V.N., Rasina MG, Rudin MG Chemistry and technology oil and gas, L., Chemistry, 1985, S. 96-152).

Closest to the second variant of the method according to the invention, in essence and the achieved result is a method for producing jet fuel from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of the latter by passing an oil stream through a net , and / or cellular electrodehydrators located in at least two levels of electrodes, covering in aggregate the altitude range of electrodehydrators RA, mainly in the upper half of the height of its body, and the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05-0.1 conventional section of the path, which coincides with the average vector of displacement of the oil flow in the zone of the largest midship of the electric dehydrator, passed by the flow per hour moving at an average rate of the process of desalination, atmospheric and / or atmospheric vacuum distillation of desalted and dehydrated oil using atmospheric distillation columns equipped with cross-accurate packages x nozzles placed with a high-altitude or high-angle displacement adequate to the temperature zones of vapor condensation, at least a part of the packages are placed in the condensation zone of the kerosene fraction with distillation when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the zone a power supply equipped with an internal cylindrical flow reflector, the diameter of which is related to the diameter of the column body in the supply zone as (0.59-0.75): 1, with the release of a kerosene fraction, hydrotreating the obtained kerosene fraction in the presence of a catalyst using hydrotreatment reactors, followed by compounding the fractions obtained in the distillation and hydrotreatment processes (see RU 2033418 C1, 04.20.95)
The disadvantages of the known methods are increased energy costs for technological processes, increased labor and material costs for performing individual processes, which is associated with the need to standardize the quality of chemically purified water and condensate in terms of silicon content, as well as the unsatisfactory environmental situation at the enterprise and surrounding territories due to the need to use in separate processes of various aggressive reagents.

 The objective of the present invention is to reduce energy consumption, increase efficiency by providing the ability to reduce the consumption of chemically purified water to power the steam generator by 100% return of condensate to the steam generator, simplifying work by eliminating the need to standardize the quality of chemically purified water and, therefore, the condensate used in technological processes, as well as improving the environmental situation.

The problem in terms of the first variant of the method is solved due to the fact that in the method for producing jet fuel from low-sulfur, and / or sulfur, and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalination and dehydration of the latter by passing an oil stream through a system of electrodes located in electrodehydrators, atmospheric and / or atmospheric vacuum distillation of desalted and dehydrated oil using atmospheric distillation columns, with the release of kerosene FR hydrotreating the obtained kerosene fraction in the presence of a catalyst using hydrotreating reactors, followed by compounding the fractions with additives obtained during hydrotreating, in which according to the invention at least electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, hydrotreating reactors supply process heat, including the use of steam as a coolant, which is at least partially obtained by burning the associated material about gas and / or fuel-technological gas released as a result of the thermal oil refining process and / or thermo-destructive oil refining processes and / or intermediate products: gasoline, kerosene, diesel fractions, which are supplied to the network with a temperature of 50-70 ^o C and pressure 3-5 kg / cm ² , and before combustion, the gas is heated to a temperature not lower than 100 ^o C, 60-85% of the gas is burned in the furnaces of technological processes, and 15-40% of the gas is burned in a steam generator with the formation of condensate at least partially returning to result selection and heat, mainly during technological processes of oil distillation, while the water in the steam generator uses return condensate with the addition of heated chemically purified raw water, at least in the amount necessary to compensate for non-returnable condensate, for heating chemically purified raw water and / or the initial oil uses the residual heat of the steam and / or steam condensate spent in the technological processes of distillation of oil.

Electric desalting and oil dehydration can be carried out by passing a stream through a system of mesh and / or mesh electrodes located in at least two levels of electrodes, which together cover the altitude range of the electric dehydrator mainly in the upper half of the height of its body, and the height gradient between the levels of the electrodes in the ascending path the oil flow is 0.05-0.1 conditional length of the path, coinciding with the average displacement vector of the oil flow in the zone of the largest midship of the electric dehydrator, passable the flow per hour of movement at an average rate of the process of electric desalination and dehydration; electric desalting and dehydration of oil is carried out in electric dehydrators with a horizontally oriented case of cylindrical or composite configuration and a working volume of 80-200 m ³ , or electric desalting and dehydration of oil is carried out in electric dehydrators with a body of spherical, or spheroidal, and / or ellipsoidal, and / or ovoid, and / or a drop-shaped form, or electric desalting and oil dehydration is carried out in electric dehydrators with a cylindrical body and convex-curved end sections, and / or toroidal form, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented horizontally or at an angle to the horizon.

At distillation of desalted and dehydrated oil, atmospheric and / or atmospheric vacuum distillation columns equipped with cross-precision nozzle packs placed with vertical or vertical-angular displacement can be used that are adequate to the temperature zones of vapor condensation, while at least some of the packages are placed in the condensation zone the kerosene fraction and distillation is carried out when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the supply zone equipped with internal cylin a flow reflector, the diameter of which correlates with the diameter of the column body in the feed zone as (0.59-0.75): 1, and the altitude range for introducing oil flows is 0.21-0.28 the height of the column from the bottom of the column bottom, while the oil supply in the atmospheric and / or atmospheric vacuum distillation column is carried out through nozzles that are arranged with a dilution angle of the points of intersection of the axes of the nozzles with the column body in the range of 30-180 ^° with a one-sided tangential swirl of the feed stream, or oil is supplied to the column by atmospheric and / or atmosphere The vacuum-vacuum distillation is carried out through nozzles, the axis and the inner neck of one of which orient the flow of the vapor-liquid oil mixture supplied through it in the feed zone of the column directly to the intersection with a similar flow supplied through another nozzle mainly in the zone of exit from the inner neck of the latter, or supply oil in the column of atmospheric and / or atmospheric vacuum distillation is carried out through pipes, the axes of which are oriented parallel to the tangent to the body of the inner cylindrical of the reflector, are radially removed from the conditional contact point with the reflector body by a distance b satisfying the condition b ≥ 0.25 (R _k - R _о ), where R _k is the radius of the column in the supply zone, R _о is the radius of the reflector or that distillation is carried out in a column, a cylindrical reflector in the feed zone of which is installed an eccentric longitudinal axis of the column, or distillation is carried out in a column of atmospheric and / or atmospheric vacuum distillation, the cylindrical reflector of which is performed with a variable radius of curvature in the cross section, or distillation dressed in an atmospheric and / or atmospheric vacuum distillation column, the cylindrical reflector of which is connected to the column body with an annular membrane of a flat and / or broken and / or curved and / or combined configuration in cross section, or an atmospheric and / or column is used for distillation or atmospheric-vacuum distillation, equipped with packages of cross-precision nozzles, which are made of spatially deformed elements made of sheet stainless steel, providing overlapping height of the packages of temperature g radiants 2-8 ^o C along the height of the column, and the area of the passage of vapor through them, comprising 38-81% relative to the cross section of the column; distillation in a column of atmospheric and / or atmospheric vacuum distillation is carried out at a vapor velocity of the accelerated fractions of at least 1.0-1.7 m / s; the withdrawal of the kerosene fraction with a boiling point of 140-240 ^o C is carried out in the altitude range of the primary distillation column of 0.57-0.81, counting from the bottom of the bottom of the column or exceeding the lower and upper marks of the output range of the kerosene fraction by 0.37 -0.53 relative to the axis of entry of the pipes supplying oil to the feed zone of the column, the separated kerosene fraction is divided into three target streams in their volume ratio (1.2-8.5) :( 12.8-15.5) :( 9 , 5-11.8), respectively, for subsequent supply to the hydrotreating of the third stream in a mixture with 30-35 wt.% the exact kerosene fraction obtained by the secondary distillation of the gasoline fraction.

 When hydrotreating a kerosene fraction passed through at least one reactor, a reactor can be used, at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-, gas-permeable element from an inert or corrosion-resistant material or a combination of materials with similar properties moreover, at least the inlet surface of the catalyst layer in the path of the steam-, gas-product flow is greater than the cross-sectional area of the hydrotreating reactor, or during hydrotreatment at least one reactor is used in the source, in which the catalyst layer is sloped with at least part of at least the upper surface, or at least one reactor is used in hydrotreating, in which at least the upper catalyst layer is filled with a conical, and / or alternately broken, and / or alternately curved, and / or combined slopes from the central zone to the walls of the reactor vessel, or at least one reactor is used in hydrotreating, in which the catalyst is at least in the upper part The bulk array is supplied with inclusions of inert elements with an aero- and hydraulic resistance less than that of a catalyst layer equivalent in volume, or at least one reactor is used during hydrotreating, in which the elements with increased aero-, hydraulic permeability are made in the form of mesh and / or perforated cylindrical or multifaceted glasses or nozzles, or during hydrotreating, at least one reactor is used, in which part of the aero-, hydraulically permeable elements are made in bulk sprays of inert particles with a radius greater than the radius or reduced radius of the catalyst particles, or during hydrotreating, at least one reactor is used in which at least some of the elements with increased air and hydraulic permeability are combined with a bulk core and a flexible or rigid retina or a perforated shell, or at hydrotreating use at least one reactor in which at least in the upper zone at least part of the catalyst layer is mixed with larger with inert material, the particle ratio is advantageously made variable with a decrease in the percentage of inert particles in the direction of movement of the steam and gas product stream subjected to hydrotreating, or during hydrotreating, at least part of the hydrotreating reactors are installed with the longitudinal axis inclined relative to the horizon, or at least hydrotreating is used one reactor with a horizontally oriented longitudinal axis, or when hydrotreating at least one sea hydrotreating reactor oidal, and when hydrotreating in a hydrotreating reactor, alumina-cobalt or alumina-nickel-molybdenum hydrotreating catalysts or combinations thereof are used, and a pre-prepared concentrate of a mixture of naphthenic acids and ionol additives in an amount of 0.007-0.008 wt.% and a weight ratio of additives in their mixture are introduced into the hydrotreating product (1.0-1.5): 2.

 Compounding of kerosene fractions can be carried out in a tank equipped with at least one injector, in which the tank is installed in the lower half at an angle to the horizontal axis, or compounding is carried out in the tank in which the injector is mounted on a rigid inner pipe in the lower third of the central zone of the tank with the upward slope of the injected kerosene stream, or compounding is carried out in a tank in which the injector is installed by means of a tangentially mounted pipe, or compounding is carried out using at least two injectors fixed on tangentially mounted nozzles with counter-flow swirls, or mounted with the possibility of reactive rotation in the lower or bottom part of the tank.

They can use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after purification of the raw water from suspensions and after cleaning the return steam condensate from oil pollution, in particular, use water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 mg / kg, sulfates (SO ₄ ^-2 ) 1, 78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (C a ⁺² ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84-5.12 mg / kg O ₂ , and raw water for chemical cleaning is supplied under pressure up to 5 kg / cm ² to the raw water pumps, at least one of which is left standby, and then water is pumped through two heat exchangers with fixed tube sheets and the water is heated to a temperature of 25-30 ^o C, at least one heat exchanger uses condensate collected from the territory of the enterprise with a temperature of 80-85 ^o C, while the amount of raw water passed through this the heat exchanger is regulated until the condensate cools to a temperature of 25-35 ^o C, and the rest of the raw water is passed through another heat exchanger and heated to a temperature of 25-30 ^o C due to the use of heating water in this heat exchanger having a heating water temperature of in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and the suspended particles are removed from the water until the water reaches the clear of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters with a "hungry" regeneration loaded with sulfonated coal, and hardness salts are removed from the water to 1-2 mEq / kg constant and the bicarbonate ion is destroyed with a decrease in carbonate only alkalinity up to 0.7 mEq / kg and ion exchange of hardness salts, alkalinity, available in water, and chemical reactions with hydrogen sulfide carbon cation, after which softened water is supplied to the self-regulating buffer filters protecting the filtrate from acid leakage, loaded with sulfonated carbon, and then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and air is separated with carbon dioxide, which is vented to the atmosphere, decarbonized water is directed by gravity into the tank, after which this water is pumped through pumps with two-stage sodium cation filters , in the filters of the first stage, stiffness cations up to 0.1 mEq / kg are removed, and in the second stage, deeper cations of stiffness Ca ⁺² , Mg ^{+2 are} removed to 0.01 mEq / k g and get chemically purified water with a transparency of at least 40 cm, a total hardness of 2-5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 mg / kg and a pH of 8.0, after which chemically purified water is fed into tanks, and then pumped into the steam generator, while at least during the flood period, preliminary water treatment is carried out using at least two clarifiers with a capacity of 250 m ³ / h, two mixers of milk of lime with a capacity of 15 m ³ each, two coagulant measuring devices 10 m ³ each, wet cells storing lime, mainly lime dough with a capacity of 100 m ³ , lime milk cells with a capacity of 60 m ³ and metering pumps and / or centrifugal pumps with additional control valves, and chemical water treatment is carried out only using sodium cation exchange filters, which also regenerate filtering material with a saline solution with a concentration of 6-8%, and for chemical water purification use mechanical filters made in the form of cylindrical vessels with an internal anti-corrosion coating m, mainly made of epoxy resin, and two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device are placed, which are made in the form of beams of polymeric material for distributing water over the filter cross section, and a drainage system is located on the lower bottom in the form of a collector with slotted tubes of stainless steel, along the axis of which holes are formed that overlap with casings with slits 0.25-0.4 mm wide, and in the upper part of the filter housing form a hatch for viewing the surface of the filter material, and in the lower one there is a hole for mounting and repairing the upper and lower drainage systems, while on the filter housing at the level of the slit tubes there is a fitting for hydraulic overloading, feed water piping, loosening, an air vent of the upper and lower drainage systems, manometers are connected at the inlet and outlet of the collector, samplers and valves, and the filtering filling is performed in two layers, consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and a layer of anthracite with a height of 500 mm and a volume of 4.6 m ³ , while the performance of the filters, taking into account the water flow for own needs and the preparation of regeneration solutions, is at least 200 m ³ / h, the filtering speed for all filters is at least 7 m / h and the maximum during loosening washing is at least 10 m / h with a flow rate for loosening of compressed air of 5 m ³ / h and a pressure of up to 1.5 kgf / cm ² ; use hydrogen-cation exchange filters with a filtration area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm, and the filter is equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the water flow over the surface of the filtering material of the system and the inner surface of the filter is performed with a rubber gum coating, while the filter performance is at least 80 t / h and the filtering speed is at least 13 m / h; the used buffer filters are loaded with sulfonated coal with a loading layer height of 2000 mm and are self-regenerating, with an upper dispenser in the form of a "glass in a glass", moreover, the performance of one filter is assigned at least 180 m ³ / h and the filtering speed is at least 25 m / h ; the used decarbonizer is filled with Rashig rings and is carried out with a lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to a collection tank for this water with a capacity of at least 400 m ³ using a two-stage sodium cation exchange filter with an upper one consisting of rays and a lower one distribution devices, the first stage of this filter being made up of three filters with a diameter of 3000 mm and loaded with filter material with a layer height of 1900 mm to replace the cation in Ca ⁺² , Mg ⁺² per hydrogen cation H ⁺ , while the filter performance is at least 90 m ³ / h, and the filtering rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is made up of two filters with a diameter of 2600 mm, is loaded with filter material with a layer height of 1200 mm, the filter is equipped with an upper switchgear, at the same time, a filter speed of at least 34 m / h is assigned and stiffness cations Ca ^{+ 2} are removed, Mg ⁺² to 0.01 mEq / kg, while in all ion-exchange filters In the case of chemical water treatment, an underlying layer of anthracite with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm is located on the lower drainage device.

Chemically purified water can be fed to a steam boiler room with a temperature of 25-30 ^o C, and part of the chemically purified water is sent to the sampling coolers for continuous and periodic blowing of the boilers, and from there to the deaerator head, another part of the chemically purified water is sent to the gravity condensate cooler, in which steam condensate heat is used, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed to the deaerator head, and the other is fed to a continuous purge cooler, using using the heat of purge water from the continuous purge separator, and then chemically purified water is passed through a deaerator vapor cooler, and then it is supplied to the deaerator head and steam is chemically purified by bubbling, heating it to a temperature close to saturation, and O gases are removed from the water ₂ , CO, and the network heating water is supplied to the network pumps, and then through the network water heaters to the heating network, while during the repair of chemically treated water heaters, the heaters are switched network water for heating chemically purified water.

Steam from the steam generator through the collectors can be supplied to steam pipelines for technological needs, and part of the steam from the collectors is supplied through a reducing device with a pressure of P = 4 kgf / cm ² to the network water heater, to the chemically purified water heater, to the fuel gas heater, to the separator fuel gas and deaerators; in the presence of excess spent steam, part of the steam is supplied to chemically purified water heaters and network water heaters, and the condensate formed in them is sent to condenser tanks, from where they are pumped out by condenser pumps for condensate treatment; during operation of the chemically purified water heater and network water heaters using reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^° C is sent directly to the deaerator head to replace an equivalent amount of heated chemically purified water, while the network and chemically purified water heaters are made in the form steam-water and water-water heat exchanger unit, and first, steam is condensed in the steam-water heat exchanger, while the condensate level in the heat exchanger is supported by p gulyatorom level, and then the condensate is directed to water-water heat exchanger and subcooled to a temperature 80 to 90 ^o C, wherein the chemically purified water or a network is first passed through a water-water heat exchanger, and then - through steam.

A steam boiler room can be used as a steam generator, and return condensate from the plants and the steam boiler room is piped to a distribution comb, and condensate with a total hardness of 100 mEq / kg, Fe content in terms of Fe ⁺³ up to 180 mg / kg is used, SiO ₂ content of silicon - up to 350 mg / kg, the oil content of up to 80 mg / kg and the pH value to 8.0, the mismatch of the condensate of these parameters it is sent to the drain, and the junction of the comb condensate fed successively in a slop tank k and a collection tank of pure condensate separated from the oil products, and as the condensate floats up to the surface of the oil particles, it is collected using a collecting funnel, while both tanks maintain a predetermined volume of liquid due to the difference in the levels of overflow troughs - filling pipes, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of the three-stage filters both oiling, on clarification filters loaded with anthracite, in which suspended mechanical particles and oil products are removed up to 4-5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which are connected together in parallel and loaded with activated carbon, and then - four sorption filters of the second stage of de-oiling the condensate to an oil content of not more than 0.05 mg / kg, and then the oil-free condensate with a temperature of 85 ^o C is sent to the annular space of the heat exchangers, p about which cold raw water is used, used for the technological needs of chemical water purification, and the condensate is cooled to a temperature of 40 ^o C, after which it is sent to a tank of oil-free condensate, from where the condensate is pumped to the desalination plant, and the temperature of the oil-free condensate is maintained in the range 35 ^o C to 40 ^o C and direct it first to hydrogen-cation exchange filters, in which KU-2.8 highly basic cation exchange resin with a loading layer height of 1 is used as a filter material, 5 m and a filtration speed of 35 m / h, in which the cation of stiffness and iron are held, and periodically, the exchange ability of the filters is restored by regenerating the filter material with a 3-4% solution of sulfuric acid, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which highly basic anion exchange resin AB-17-8 is used as a filter material and condensate of silicic acid compounds is removed, and the exchange capacity is periodically restored springs of anion exchange filters by passing through a filtering layer of anion exchange resin 3-5% sodium hydroxide solution, and after anion exchange filters the purified condensate with a content of silicic acid is not more than 150 mg / kg, iron (in terms of Fe ⁺³ ) not more than 100 mg / kg, petroleum products - not more than 0.5 mg / kg and with a total hardness not exceeding 10 mg / kg are sent to the condensate storage tank, from where they are pumped mainly to a thermal power plant (CHP) and a steam boiler room, as well as to a sulfur unit and to waste heat boilers, moreover for corrective treatment of desalted conde nsata to a pH value of 8.5-9.5 and reducing the corrosion of the piping metal, a 1% ammonia solution is dosed into the collector by metering pumps, while the clarification filters used in the condensate cleaning are double-chamber, consisting of a housing and a lower and upper drainage distribution device, inside the case, a deaf flat horizontal partition is rigidly fixed, dividing it into two chambers, and tubular anchor connections, through which air is removed from the lower chamber to the upper and maintained in the chamber total pressure, while the upper drainage distribution device is made in the form of a funnel for uniform distribution of condensate on the surface of the filter material, which is used anthracite, the layer height of which in one chamber is 0.9 m with a grain size of 2-6 mm, and at filling the filter with filter material, it is first laid in the lower chamber, and then in the upper, and the lower switchgear is in the form of a collector to which thirty-two beams are attached from the slit and a width of 0.25-0.4 mm holes that close perforated plates to avoid entrainment of filter material; as sorption filters of the first stage, four single-chamber filters are used, connected in parallel and loaded with filter material — activated carbon, a layer thickness of 2.5 m and a grain size of 2 to 6 mm, the filters being equipped with upper and lower distribution devices, the upper of which is made in the form rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower distribution device is in the form of a collector in which the bottom is placed horizontally and in which th inserted distribution tubes with holes along the lower generatrix of diameter 8 mm, overlapped welded trough plate with a slit width of 0.25-0.4 mm to avoid ingress of activated carbon in the condensate; when condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; they use hydrogen-cation exchange and anion exchange filters made in the form of single-chamber cylindrical devices having a capacity of 115 m ³ / h, each of which is equipped with an upper and lower manhole, fittings for hydroloading and upper and lower switchgears with a diameter of 2.6 m of which are made in the form of a “glass in a glass”, and the lower one is in the form of a collector into which distribution tubes-rays are inserted with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide, and in the case of e formation of a slit hole at the weld point of the trough plate to prevent entrainment of filter material on the lower distribution device of the sorption filters, a litter layer of coarse anthracite is poured over the entire surface of the filter 10 cm high.

The problem in terms of the second variant of the method is solved due to the fact that in the method for producing jet fuel from low-sulfur, and / or sulfur, and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of the latter by passing an oil stream through a net system, and / or in electrodehydrators located in at least two levels of electrodes, which together cover the altitude range of the electrodehydrator, mainly in the upper half of the height its body, and the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05-0.1 conventional section of the path, which coincides with the average vector of the movement of the oil flow in the zone of the greatest midsection of the electric dehydrator, traveled by the stream per hour of movement with an average speed of the process of desalination, atmospheric and / or atmospheric vacuum distillation of desalted and dehydrated oil using atmospheric distillation columns equipped with packages of cross-precision nozzles placed with high-altitude or high-altitude o-angular displacement is adequate to the temperature zones of vapor condensation, at least a part of the packages are placed in the condensation zone of the kerosene fraction with distillation when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the supply zone provided with an inner cylindrical a flow reflector, the diameter of which corresponds to the diameter of the column body in the feed zone as (0.59-0.75): 1, with the separation of the kerosene fraction, hydrotreating the obtained kerosene fraction in the presence of and a catalyst using a hydrotreating reactor, followed by compounding the fractions obtained in the distillation and hydrotreating processes, in which according to the invention at least electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, hydrotreating reactors supply process heat, including using as heat carrier steam, which is at least partially obtained by burning associated gas contained in the feed and / or process gas released as a result of Tate thermal refining process and / or thermodestructive oil refining processes, and / or intermediate products: gasoline, kerosene, diesel fractions, which are fed into the network with a temperature of 50-70 ^o C and pressure of 3-5 kg / cm ² and the front combustion gas is heated to a temperature not lower than 100 ^o C, 60 ÷ 85% of the gas is burned in furnaces processes and 15 ÷ 40% of the gas is burned in the boiler to form a condensate, at least partially as a result of recurrent selection of heat during the flow processes of distillation oil, in this case, return water condensate is used as water in the steam generator with the addition of heated chemically purified raw water, at least in the amount necessary to compensate for the non-returnable condensate, and the residual heat of the distillation spent in technological processes is used to heat the chemically purified raw water and / or feed oil steam and / or steam condensate oil and the process is carried out with sludge from the water and at least twice filtering the finished fuel.

In this case, electric desalting and dehydration of oil can be carried out in electric dehydrators with a horizontally oriented cylindrical or composite body and a working volume of 80-200 m ³ , or electric desalting and dehydration of oil is carried out in electric dehydrators with a spherical or spheroidal and / or ellipsoidal and / or ovoid and / or teardrop-shaped, or electric desalting and dehydration of oil is carried out in electric dehydrators with a cylindrical body and convex-curved end sections, and / or toroidal form, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented horizontally or at an angle to the horizon.

The altitude range of the input of oil flows can be 0.21-0.28 the height of the column from the bottom of the column, while the oil in the column is atmospheric and / or atmospheric vacuum distillation is carried out through pipes located at an angle of dilution of the points of intersection of the axes of the pipes with the column body in the range of 30-180 ^o with a one-sided tangential swirl of the feed stream, or oil is supplied to the atmospheric distillation column through nozzles, the axis and inner neck of one of which orient the flow supplied through it vapor-liquid oil mixture in the feed zone of the column directly at the intersection with a similar stream supplied through another nozzle mainly in the zone of its exit from the inner neck of the latter, or oil is supplied to the atmospheric distillation column through nozzles whose axes are oriented parallel to the tangent body of the inner cylindrical reflector and radially removed from the conditional point of contact with the reflector body by a distance b satisfying the condition b ≥ 0.25 (R _k - R _o ), where R _k is the radius of the column in the zone power, R _about - the radius of the reflector.

The distillation can be carried out in a column whose cylindrical reflector is installed in the feed zone of the column in an eccentric longitudinal axis, or the distillation is carried out in an atmospheric distillation column whose cylindrical reflector is made with a variable radius of curvature in cross section, or the distillation is carried out in an atmospheric distillation column whose cylindrical reflector is connected with the casing of the column annular membrane of a flat and / or broken, and / or curved, and / or combined configuration in cross section, and and is used in the distillation column atmospheric distillation, wherein the cross-packets accurate landings made of spatially deformed elements from stainless steel sheet, wherein the overlap provides a package height of temperature gradients 2-8 ^o C along the column height, and the area of the passage of vapor through them is 38- 81% relative to the cross section of the column; distillation in an atmospheric distillation column is carried out at a vapor velocity of the accelerated fractions of at least 1.0-1.7 m / s; the withdrawal of the kerosene fraction with a boiling point of 140-240 ^o C is carried out in the altitude range of the primary distillation column of 0.57-0.81, counting from the bottom of the column or exceeding the lower and upper marks of the output range of the kerosene fraction by 0.37 -0.53 relative to the axis of entry of the nozzles supplying oil to the feed zone of the column, the separated kerosene fraction is sent for subsequent hydrotreating together with the stream in a mixture with 30-35 wt.% Residual kerosene fraction 180-КК ^o C obtained by the secondary distillation of gasoline new fraction.

 When hydrotreating a kerosene fraction passed through one reactor, a reactor can be used, at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-, gas-permeable element from an inert or corrosion-resistant material or a combination of materials with similar properties, moreover at least the inlet surface of the catalyst bed along the path of the steam and gas product stream is greater than the cross-sectional area of the hydrotreating reactor, or at least one reactor is poured in which the catalyst layer is poured with at least a portion of at least the upper surface, or at least one reactor is used in hydrotreating in which at least the upper catalyst poured is tapered and / or alternately broken and / or alternately curved and / or combined slope from the central zone to the walls of the reactor vessel, or at least one reactor is used in hydrotreating, in which the catalyst is at least in the upper part of the bulk sivas are supplied with inclusions of inert elements with an aero- and hydraulic resistance less than that of a catalyst layer equivalent in volume, or at least one reactor is used for hydrotreating, in which elements with increased aero-, hydraulic permeability are made in the form of mesh and / or perforated cylindrical or multifaceted glasses or nozzles, or during hydrotreating, at least one reactor is used, in which part of the aero-, hydraulically permeable elements are made in the form of bulk inclusions of inert particles, with a radius greater than the radius or reduced radius of the catalyst particles, or during hydrotreating, at least one reactor is used in which at least part of the elements with increased air and hydraulic permeability are combined with a bulk core and a flexible or rigid retina or a perforated shell, or at hydrotreating use at least one reactor in which at least in the upper zone at least part of the catalyst layer is mixed with larger particles and of the inert material, the particle ratio being predominantly variable with a decrease in the percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreating, or at hydrotreating at least one hydrotreating reactor is installed with a longitudinal axis inclined relative to the horizon, or at least one reactor is used for hydrotreating with a horizontally oriented longitudinal axis, or during hydrotreating, at least one hydrotreating reactor is toroidal, or in the hydrotreatment reactor, alumina-cobalt or alumina-nickel-molybdenum hydrotreating catalysts, or combinations thereof are used, and a pre-prepared concentrate of a mixture of naphthenic acid and ionol additives in an amount of 0.007-0.008 wt.% and a weight ratio of additives in their mixture (1.0 -0.5): 2.

 Compounding of kerosene fractions can be carried out in a tank equipped with at least one injector, which is installed in the lower half of the tank at an angle to the horizontal axis, or compounding is carried out in a tank in which the injector is mounted on a rigid inner pipe in the lower third of the central zone of the tank with an upward by tilting the injected kerosene stream, or compounding is carried out in a tank in which the injector is installed by means of a tangentially mounted nozzle, or compounding is carried out using at least two injectors fixed on tangentially mounted nozzles with counter-flow swirls, or mounted with the possibility of reactive rotation in the lower or bottom part of the tank.

Can use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after cleaning the raw water from suspensions and after cleaning the return steam condensate from oil pollution, in particular, water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 mg / kg, sulfates (SO ₄ ^-2 ) 1.78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mg -eq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84-5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² for raw water pumps, at least one of which is left standby, and then pumped water through two heat exchangers with fixed tube sheets and heated water to a temperature of 25-30 ^o C, and at least one heat exchanger uses return condensate with a temperature 80-85 ^o C, wherein the amount of raw water flowing through this heat exchanger is adjusted to Zech lazhivaniya condensate to 25-35 ^o C temperature and the remainder of the raw water is passed through another heat exchanger and heat it to 25-30 ^o C temperature by using the heat exchanger as a heat carrier heating water having a temperature of the heating water in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then perishable water is fed to hydrogen-cation exchange filters with a "hungry" regeneration loaded with sulfonated coal, and hardness salts are removed from water to 1-2 mEq / kg constant and the bicarbonate ion is destroyed with only carbonate alkalinity reduced to 0.7 mEq / kg and ion exchange of hardness, alkalinity salts present in water and chemical reactions with a hydrogen carbon sulfide cation, after which softened water is fed to self-regulating buffer filters loaded with sulfonated carbon that protect the filtrate from acid leakage, and then water is sent to remove free carbon dioxide to a decarbonizer loaded with Rashig rings, and air is separated with carbon dioxide, which is vented to the atmosphere, decarbonized water is directed by gravity to the tank, after which this water is pumped through two-stage sodium-cation exchange filters, in the filters of the first stage produce removing hardness cations to 0.1 meq / kg, and in the second stage is carried out deeper removal of hardness cations Ca ^+2, mg ⁺² to 0.01 meq / kg was prepared and chemically cleaned in transparency at least 40 cm, total hardness of 2-5 mg-eq / kg, the content of iron in terms of Fe ⁺³ to about 300 mg / kg and the amount of pH 8,0, after which the chemically purified water is fed into the tanks, pumps and then pumped into the steam generator, at the same time, at least during the flood period, preliminary water treatment is carried out, which is carried out using at least two clarifiers with a capacity of 250 m ³ / h, two lime milk mixers with a capacity of 15 m ³ each, two coagulant measuring tanks of 10 m ³ each wet lime storage cells, mainly zvestkovogo test capacity of 100 m ³ of milk of lime cell capacity of 60 m ³ and metering pumps, and / or centrifugal pumps with additional regulating valves, and the chemical purification of water produced only using sodium cation filters, which also produce regeneration of the filter material with brine with a concentration of 6-8%.

For chemical water treatment, mechanical filters can be used, made in the form of cylindrical vessels with an internal anti-corrosion coating, mainly of epoxy resin, and two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device, which are made in the form of rays, are placed from a polymeric material for distributing water over the filter cross section, and on the lower bottom there is a drainage system in the form of a collector with slotted tubes made of stainless steel and, along the axis of which holes are formed, overlapped by casings with slits 0.25-0.4 mm wide, and in the upper part of the filter housing they form a hatch for inspecting the surface of the filter material, and in the lower part there is a manhole for mounting and repairing the upper and lower drainage systems Moreover, on the filter housing at the level of the slotted tubes, a fitting for hydraulic overloading is placed, feed water pipes, loosening, air vents of the upper and lower drainage systems are connected to the filter, pressure gauges at the inlet and outlet of the collector, samplers and valves are connected, and fi pouring filling is performed in two layers, consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and anthracite layer with a height of 500 mm and a volume of 4.6 m ³ , while the performance of the filters, taking into account the water flow for own needs and the preparation of regeneration solutions, is at least 200 m ³ / h, the filtration rate during operation of all filters is at least 7 m / h and the maximum during loosening washing is at least 10 m / h at a flow rate for loosening of compressed air of 5 m ³ / h and a pressure of up to 1, 5 kgf / cm ² ; using hydrogen-cation exchange filters made with a filtration area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm, and the filter is equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the flow of water over the surface of the filter the material of the system, and the inner surface of the filter is performed with a rubber gum coating, while the filter capacity is at least 80 t / h and the filtering speed is at least 13 m / h; use self-regenerating buffer filters loaded with sulfonated coal with a loading layer height of 2000 mm, with an upper dispenser in the form of a "glass in a glass", moreover, the performance of one filter is assigned at least 180 m / h and the filtering speed is at least 25 m / h; use a decarbonizer filled with Rashig rings and perform with a lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to a collection tank for this water with a capacity of at least 400 m ³ ; using a two-stage sodium-cation exchange filter with an upper, consisting of rays, and lower distribution devices, the first stage of this filter is made up of three filters with a diameter of 3000 mm and is loaded with filter material with a layer height of 1900 mm to replace the cations Ca ^{+ 2} , Mg ^{+ 2} on the hydrogen cation H ⁺ , while the filter performance is at least 90 m ³ / h, and the filtration rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is performed composite of two Filtering diameter of 2600mm, was charged with a filter material layer height of 1200 mm, equipped with a filter upper distribution device, the filtration rate is at least 34 m / h, and the removal is carried hardness cations Ca ^+2, Mg ⁺² to 0.01 mEq / kg, while in all ion-exchange filters for chemical water purification on the lower drainage device an underlying layer of anthracite with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm is located.

Chemically purified water can be supplied to a steam generator with a temperature of 25-30 ^o C, whereby part of the chemically purified water is sent to continuous and periodic boiler blowdown sampling coolers, and from there - to the deaerator head, another part of chemically purified water is sent to a gravity condensate cooler, in which uses the heat of steam condensate coming from the plants of the enterprise, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed to the deaerator head, and the other is fed to oh continuous blower, using the heat of the purge water from the continuous blowdown separator, and then chemically purified water is passed through a deaerator vapor cooler, and then it is fed to the deaerator head and steam is chemically purified by bubbling, heating it to a temperature close to saturation, and removed water from gases O _2, CO, and network heating water fed to the network pumps, heaters, and then through a network of water - in the heating system of the enterprise, while the repair heaters chemically cleaned in dy carried switching network water heaters for heating the chemically treated water.

Steam from the steam generator through collectors can be supplied to the enterprise’s steam pipelines for technological needs, and part of the steam from the collectors is supplied through a reducing device with a pressure of P = 4 kgf / cm ² to the network water heater, chemically purified water heater, fuel gas heater, and heating fuel gas separator and deaerators; in the presence of excess spent steam at the enterprise, part of the steam is fed to chemically treated water heaters and network water heaters, and the condensate formed in them is sent to condenser tanks, from where they are pumped out by condenser pumps for condensate treatment; during operation of the chemically purified water heater and network water heaters using reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^° C is sent directly to the deaerator head to replace an equivalent amount of heated chemically purified water, while the network and chemically purified water heaters are made in the form steam-water and water-water heat exchanger unit, and first, steam is condensed in the steam-water heat exchanger, while the condensate level in the heat exchanger is supported by p gulyatorom level, and then the condensate is directed to water-water heat exchanger and subcooled to a temperature 80-90 ^o C, wherein the chemically purified water or a network is first passed through a water-water heat exchanger, and then - through steam.

A steam boiler room can be used as a steam generator, and return condensate from the plants and the steam boiler house is piped to the distribution comb, and condensate with a total hardness of 100 mEq / kg Fe content in terms of Fe ⁺³ to 180 mg / kg is used, silica content (SiO ₂₎ - to 350 mg / kg, the oil content of up to 80 mg / kg and the pH value to 8.0, and by the non-condensing these parameters it is sent to the drain, and the junction of the comb condensate fed sequentially into the tank sucks IR and a collection tank of pure condensate separated from oil products, and as the condensate floats up to the surface of the oil particles, it is collected using a collecting funnel regulated at least once per shift, while both tanks maintain a given volume of liquid due to the difference in levels overflow troughs - filling nozzles, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed to the process unit ku and loosening the filters of the three stages of de-oiling, on clarification filters loaded with anthracite, in which the suspended mechanical particles and oil products are removed to 4-5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which are connected to each other in parallel and loaded activated carbon, and then to four sorption filters of the second stage of de-oiling the condensate to an oil content of not more than 0.05 mg / kg, and then the oil-free condensate with a temperature of 85 ^o C is sent to the tube space of heat exchangers through which cold raw water is passed used for the technological needs of chemical water treatment and the condensate is cooled to a temperature of 40 ^o C, then it is sent to a tank of oil-free condensate, from where the condensate is pumped to the desalting unit, and the temperature of the oil-free condensate is maintained in the range from 35 ^o C to 40 ^o C and direct it first to hydrogen-cation exchange filters, in which highly basic are used as filter material KU-2.8 cation exchanger with a loading layer height of 1.5 m and a filtration speed of 35 m / h, in which stiffness cations and iron are held, and periodically, the exchange ability of the filters is restored by regenerating the filter material with a 3-4% sulfuric acid solution and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as filter material and the condensate is removed from the silicic acid compounds, moreover, recovery is carried exchange capacity anion exchange filter by passing through the filter bed anion exchanger 3-5% sodium hydroxide solution, and after the anion exchange filters with purified condensate content of silicic acid is not more than 150 mg / kg of iron (calculated as Fe ⁺³⁾ is not more than 100 mg / kg, of petroleum products - not more than 0.5 mg / kg and with a total hardness not exceeding 10 mg / kg are sent to the condensate reserve tank, from where they are pumped mainly to the thermal power station and steam boiler room, as well as to the sulfur production unit and waste heat boilers, for correction Desalted condensate operation up to pH 8.5–9.5 and reduction of pipeline metal corrosion, a 1% ammonia solution is dosed into the collector by metering pumps, while the clarification filters used in condensate cleaning are double-chamber, consisting of a housing and lower and upper drainage distribution devices moreover, a blind flat horizontal partition dividing it into two chambers and tubular anchor ties through which air is removed from the lower chamber to the upper and maintaining the total pressure in the chambers, while the upper drainage distribution device is made in the form of a funnel for uniform distribution of condensate on the surface of the filter material, which is used anthracite, the layer height of which in the same chamber is 0.9 m with a grain size of 2-6 mm, moreover, when filling the filter with filtering material, it is first placed in the lower chamber, and then in the upper, and the lower distribution device is made in the form of a collector to which t idtsat two slotted beam width of 0.25-0.4 mm, which are closed by perforated plates to avoid entrainment of filter material; as sorption filters of the first stage, four single-chamber filters are used, connected in parallel and loaded with filter material — activated carbon, a layer thickness of 2.5 m and a grain size of 2 to 6 mm, the filters being equipped with upper and lower distribution devices, the upper of which is made in the form rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower distribution device is in the form of a collector in which the bottom is placed horizontally and in which th inserted distribution tubes with holes along the lower generatrix of diameter 8 mm, overlapped welded trough plate with a slit width of 0.25-0.4 mm for a hit exception activated carbon
condensate; when condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; they use hydrogen-cation exchange and anion exchange filters made in the form of single-chamber cylindrical apparatuses with a capacity of 115 m ³ / h, each of which is equipped with an upper and lower manhole, fittings for hydroloading and upper and lower switchgears with a diameter of 2.6 m, upper of which are made in the form of a "glass in a glass", and the lower one is in the form of a collector into which distribution tubes-rays with holes along the lower generatrix are inserted with an overlapped plate having a slit 0.25-0.4 mm wide, and in the case of formation slotted holes in place of welding trough plate to avoid entrainment of the filter material on the lower dispenser sorption filter layer of poured litter coarsely crushed anthracite throughout the height of 10 cm of the filter surface.

 The technical result provided by the process options consists in reducing energy costs for the process, reducing the cost of production, in increasing efficiency by providing the ability to reduce the consumption of chemically purified water to power the steam generator by 100% return of condensate to the steam generator, eliminating the need to normalize the quality of chemically purified water and, therefore, condensate used in technological processes, the use of heat from waste processing streams and the reduction of combustible the flare amounts of fuel and process gas, which also helps to improve environmental situation.

 Example.

 The method is as follows.

The original oil is sent to a block of electrodesalting and dehydration. Then served on the block atmospheric (AT) or atmospheric vacuum vacuum (ABT) distillation. The obtained kerosene fraction is sent together with the 180-KK ^o C fraction withdrawn from the gasoline secondary distillation unit to the hydrotreatment unit, from where to the compounding unit. The finished fuel is subjected to sediment from water and double filtration.

 Electrodehydrators, atmospheric and / or atmospheric vacuum distillation columns, hydrotreatment reactors supply process heat, including using steam as a heat carrier.

 Associated gas contained in the raw materials, and fuel-technological gas generated during thermal and thermo-destructive technological processes of oil refining and intermediate products - during the distillation of oil, are used in steam hydrotreatment for steam production.

When this gas is fed into the fuel network at a temperature of 60 ^o C, a pressure of 3.6 kg / cm ² . 20% of the gas is burned in a steam generator - a steam boiler, 80% - in process furnaces.

Before combustion, the gas is heated to 100 ^o C. As the water in the production of steam, return condensate is used, which is formed during the selection of heat in technological processes with the addition of heated water from the Ural River, which is previously subjected to chemical treatment.

 To heat the source oil and chemically purified raw water, the residual heat of the steam and steam condensate spent during the distillation of the oil is used.

 Steam is provided in the atmospheric column of the AT and ABT plants, in the stripping sections (or stripping columns) of the main column K2 of these plants, for hydrotreating kerosene fractions in the stripping column of hydrotreating plants, as a coolant to maintain the required temperature of the bottom of the columns, in the section or in blocks for cleaning hydrocarbon gases from hydrogen sulfide, for spraying fuel in process furnaces.

 The modal conditions for the stages of the method are shown in the table.

 The feedstock is the oil of the Shkapovskoye field, the sulfur content is 2.2%.

 The implementation of the method of producing jet fuel according to the invention allows to reduce energy consumption by traditional energy carriers by 3 times per unit output of refined products and 2 times in value terms by replacing the corresponding amount of traditional energy sources (natural gas and fuel oil) with previously refined oil refining process gas .

Claims (23)

1. A method of producing jet fuel from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of the latter by passing an oil stream through a system of electrodes located in electric dehydrators, atmospheric and / or atmospheric-vacuum distillation of desalted and dehydrated oil using atmospheric distillation columns, with the separation of a kerosene fraction, hydrotreating the resulting kerosene fraction in the presence of catalyst using hydrotreating reactors with subsequent compounding of fractions with additives obtained during hydrotreating, characterized in that at least electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, hydrotreating reactors supply process heat, including using as a heat transfer medium for steam, which, at least partially, is obtained by burning associated gas contained in the raw material and / or process fuel gas generated as a result Cesky process of refining and / or thermodestructive processes of refining and / or intermediate products: gasoline, kerosene, diesel fractions, which is fed into the network at a temperature 50 - 70 ^o C and a pressure of 3 - 5 kg / cm ^2, wherein prior to the gas combustion is preheated to a temperature not lower than 100 ^o C, 60 - 85% of the gas is burned in furnaces processes, while 15 - 40% of the gas is burnt in the steam condensate to form at least partially a result of recurrent selection of heat, advantageously at a flow of processes distillation of oil, while the water in the steam generator uses return condensate with the addition of heated chemically purified raw water, at least in the amount necessary to compensate for the non-return condensate, to heat the chemically purified raw water and / or source oil, the residual heat of the spent technological processes of steam distillation and / or steam condensate. 2. The method according to claim 1, characterized in that the electric desalting and dehydration of the oil is carried out by passing a stream through a system of mesh and / or mesh located at least two levels of electrodes, covering in aggregate the height range of the electric dehydrator mainly in the upper half of the height of its body, moreover, the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05 - 0.1 of the conventional section of the path, which coincides with the average vector of the displacement of the oil flow in the zone of the largest midsection electrode a dehydrator traversed by the flow per hour of movement at an average rate of the process of electric desalination and dehydration; electric desalting and dehydration of oil is carried out in electric dehydrators with a horizontally oriented case of cylindrical or composite configuration and a working volume of 80 - 200 m ³ , electric desalting and dehydration of oil is carried out in electric dehydrators with a body of spherical or spheroidal, and / or ellipsoidal, and / or ovoid, and / or a drop-shaped form, or electric desalting and dehydration of oil is carried out in electric dehydrators with a cylindrical body and convex curvilinear end sections, and / or toroidal forms, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the casing, at least parts of which are oriented vertically, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the casing, at least parts of which are oriented horizontally or at an angle to the horizontal . 3. The method according to p. 1, characterized in that during the distillation of desalted and dehydrated oil, atmospheric and / or atmospheric vacuum distillation columns are used, equipped with packages of cross-flow nozzles placed with high-altitude or high-angle displacement adequate to the temperature zones of vapor condensation, while at least a part of the packages are placed in the condensation zone of the kerosene fraction and distillation is carried out when oil is supplied to the columns through at least two pipes tangentially located in the column body in the feed zone equipped with an internal cylindrical flow reflector, the diameter of which corresponds to the diameter of the column body in the feed zone as (0.59 - 0.75): 1, and the altitude range for introducing oil flows is 0.21 - 0.28 of the column height from the bottom of the column bottom , while the oil supply in the column of atmospheric and / or atmospheric vacuum distillation is carried out through nozzles that are arranged with the angle of dilution of the points of intersection of the axes of the nozzles with the body of the column in the range of 30 - 180 ^o with one-sided tangential swirl of the feed stream, or oil atmospheric and / or atmospheric vacuum distillation is carried out through nozzles, the axis and the inner neck of one of which direct the flow of the vapor-liquid oil mixture through it in the feed zone of the column directly to the intersection with a similar stream fed through another nozzle mainly in the exit zone from it the inner neck of the latter, or the supply of oil to the column of atmospheric and / or atmospheric vacuum distillation is carried out through nozzles whose axes are oriented parallel to the tangent to the body of the inner cylindrical reflector, radially removed from the conditional point of contact with the body of the reflector by a distance b satisfying the condition b ≥ 0.25 (R _k - R _o ), where R _k is the radius of the column in the supply zone, R _o is the radius of the reflector, or that distillation is carried out in a column, a cylindrical reflector in the feed zone of which is installed an eccentric longitudinal axis of the column, or distillation is carried out in a column of atmospheric and / or atmospheric vacuum distillation, the cylindrical reflector of which is performed with a variable radius of curvature in the butt The final cross-section or distillation is carried out in a column of atmospheric and / or atmospheric vacuum distillation, the cylindrical reflector of which is connected to the column body with an annular membrane of a flat and / or broken, and / or curvilinear and / or combined configuration in a cross section, or during distillation using a column of atmospheric and / or atmospheric vacuum distillation, equipped with packages of cross-flow nozzles, which are made of spatially deformed elements of sheet stainless steel, providing overlap height packets temperature gradients 2 - 8 ^o C along the column height, and the area of the passage of vapor through them is 38 - 81% relative to the cross section of the column; distillation in a column of atmospheric and / or atmospheric vacuum distillation is carried out at a passage speed of vapors of the accelerated fractions at least equal to 1.0 - 1.7 m / s, output of the kerosene fraction with a boiling point of 140 - 240 ^o C is carried out in the altitude range the primary distillation column, comprising 0.57 - 0.81, counting from the bottom of the bottom of the column or exceeding the lower and upper marks of the output range of the kerosene fraction by 0.37 - 0.53, respectively, relative to the input axis of the pipes supplying oil to the feed zone of the column isolated kerosene fra the share is divided into three target streams in their volume ratio (1.2 - 8.5): (12.8 - 15.5): (9.5 - 11.8), respectively, for subsequent supply to the hydrotreating of the third stream in a mixture with 30 to 35 wt.% Of the residual kerosene fraction obtained by the secondary distillation of the gasoline fraction.  4. The method according to p. 1, characterized in that when hydrotreating a kerosene fraction passed through at least one reactor, a reactor is used, at least in the upper zone of which the catalyst layer is immersed with a discrete and / or combined vapor-, gas-permeable element from an inert or corrosion-resistant material or a combination of materials with similar properties, moreover, at least the inlet surface of the catalyst layer along the path of the steam-, gas-product stream is greater than the reactor cross-sectional area hydrotreating, or at hydrotreating use at least one reactor in which the catalyst layer is poured with an inclination of at least part of at least the upper surface, or at least one reactor is used during hydrotreating, in which at least the upper catalyst layer is poured with a conical and / or alternately broken, and / or alternately curved, and / or combined slope from the central zone to the walls of the reactor vessel, or at least one reactor is used in hydrotreating, in which p, at least in the upper part of the bulk array, they are supplied with inclusions of inert elements with an aero- and hydraulic resistance less than that of a catalyst bed equivalent in volume, or at least one reactor is used in hydrotreating, in which elements of increased aero- , hydraulic permeability is performed in the form of mesh and / or perforated cylindrical or multifaceted glasses or pipes, or during hydrotreating, at least one reactor is used, in which part of aero-, hydraulically permeable elements are made in the form of bulk inclusions of inert particles with a radius greater than the radius or the reduced radius of the catalyst particles, or at least one reactor is used in hydrotreating, in which at least part of the elements with increased air and hydraulic permeability they are combined with a bulk core and a flexible or rigid retina or perforated shell, or at least one reactor is used in hydrotreating, in which at least in the upper zone at least part of the layer the catalyst is mixed with larger particles of inert material, while the particle ratio is advantageously made variable with a decrease in the percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreating, or during hydrotreating, at least part of the hydrotreating reactors are installed with the longitudinal axis inclined relative to the horizon, or when hydrotreating, at least one reactor with a horizontally oriented longitudinal axis is used, or when hydrotreating, at least At least one hydrotreating reactor is toroidal, and hydrotreating in a hydrotreating reactor uses alumina-cobalt or aluminium-nickel-molybdenum hydrotreating catalysts, or combinations thereof, and a pre-prepared concentrate of a mixture of naphthenic acid and ionol additives in an amount of 0.007 - 0.008 wt. is introduced into the hydrotreating product. % and mass ratio of additives in their mixture (1.0 - 1.5): 2.  5. The method according to p. 1, characterized in that the compounding of the kerosene fractions is carried out in a tank equipped with at least one injector, which is installed in the lower half of the tank at an angle to the horizontal axis, or the compounding is carried out in a tank in which the injector is mounted on a rigid inner pipe in the lower third of the central zone of the tank with an upward slope of the injected kerosene stream, or compounding is carried out in a tank in which the injector is installed by means of tangent of a fully installed nozzle, or compounding, is carried out using at least two injectors fixed on tangentially installed nozzles with a counter flow swirl, or installed with the possibility of reactive rotation in the lower or bottom part of the tank.  6. The method according to any one of claims 1 to 5, characterized in that they use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after the raw water treatment is performed from suspensions and after cleaning the return steam condensate from oil pollution. 7. The method according to any one of claims 1 to 6, characterized in that water from the Ural River is used with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and iron content 628 mg / kg, sulfates (SO ₄ ^-2 ) 1.78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84 - 5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to raw water pumps at least one of which is left standby, and then water is pumped through two heat exchangers with fixed tube sheets and heat water to a temperature of 25 - 30 ^o C, and at least one heat exchanger uses return condensate with a temperature of 80 - 85 ^o C, while the amount of raw water passed through this heat exchanger is regulated until the condensate cools down to temperature 25 - 35 ^o C, and the remainder of the raw water is passed through another heat exchanger, and heated to a temperature of 25 - 30 ^o C by using the heat exchanger as a heat carrier heating water having the temperature of heating water in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then clarified water is fed to the cation exchange filters with hydrogen "hungry" regeneration, loaded with sulfonated coal, and carry out the removal of hardness salts from water to 1 - 2 mEq / kg constant and the destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and ion exchange of hardness salts, alkalinity, available in water, and chemical reactions with a hydrogen carbon cation of sulfonated coal, after which softened water is fed to self-regulating buffer filters loaded with sulfonated carbon to protect the filtrate from acid leakage, and then water is sent to remove free carbon dioxide in a decarbonizer loaded with rings Rashiga, and carry out the separation of air with carbon dioxide, which is discharged into the atmosphere, decarbonized water is directed by gravity to the tank, after which this water is pumped by pumps They pass through two-stage sodium-cation exchange filters, in the filters of the first stage they remove stiffness cations up to 0.1 mEq / kg, and in the second stage they carry out a deeper removal of stiffness cations Ca ⁺² , Mg ⁺² to 0.01 mEq / kg and get chemically purified water with a transparency of at least 40 cm, a total hardness of 2 - 5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 μg / kg and a pH of 8.0, after which chemically purified water is fed in tanks, and then pumped into the steam generator. 8. The method according to any one of claims 1, 6 and 7, characterized in that during the flood period a preliminary water purification is carried out, which is carried out using at least two clarifiers with a capacity of 250 m ³ / h, two lime milk mixers with a capacity of 15 m ³ each two measuring tanks coagulant 10 ^m3 each, lime wet storage cell, preferably lime putty capacity of 100 m ³ of milk of lime cell capacity of 60 m ³ and metering pumps, and / or centrifugal pumps with additional regulating valves, and the chemical water purification They are produced only with the use of sodium-cation exchange filters, in which the filter material is also regenerated with saline with a concentration of 6-8%, and mechanical filters are used for chemical water purification in the form of cylindrical vessels with an internal anti-corrosion coating, mainly from epoxy resin, with two steel spherical bottoms, in the upper of which is placed a feed water supply fitting and an upper distribution device, which is made in the form of beams of polymer material To distribute water over the filter cross-section, and on the lower bottom there is a drainage system in the form of a collector with slotted stainless steel tubes along the axis of which holes are formed, overlapped by casings with slits 0.25 - 0.4 mm wide, and in the upper part of the filter housing they form a hatch for inspecting the surface of the filter material, and in the lower one there is a hole for mounting and repairing the upper and lower drainage systems, while on the filter housing at the level of the slot tubes there is a fitting for hydroloading, pipelines are brought to the filter hydrochloric water backwash, the air vent of the upper and lower drainage systems, pressure gauges at the inlet is connected and a collector output, and sampler valves and filter backfill operate bilayer consisting of the layer of quartz sand of 700 mm and a volume of 6.4 m ³ and a layer of anthracite height 500 mm and a volume of 4.6 m ³ , while the performance of the filters, taking into account the water consumption for own needs and the preparation of regeneration solutions, is at least 200 m ³ / h, the filtration rate for all filters is at least 7 m / h and the maximum during explosions -governing washing - not less than 10 m / h at a flow rate of backwashing compressed air to 5 m ³ / h and pressure up to 1.5 kgf / cm ^2; use hydrogen-cation exchange filters with a filtration area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm, and the filter is equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the water flow over the surface of the filtering material of the system , and the inner surface of the filter is performed with a rubber gum coating, while the filter performance is at least 80 t / h, and the filtering speed is at least 13 m / h, they use self-regulating Xia buffering filters sulpho loaded with a height of 2000 mm loading layer, with the upper distribution device as "glass in glass", the performance of the filter is not less than 180 m ³ / h, and the filtration rate - not less than 25 m / h; use a decarbonizer filled with Rashig rings, with a lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to a collection tank for this water with a capacity of at least 400 m ³ ; using a two-stage sodium-cation exchange filter with an upper, consisting of rays, and lower distribution devices, the first stage of this filter is made up of three filters with a diameter of 3000 mm and is loaded with filter material with a layer height of 1900 mm to replace the cations Ca ^{+ 2} , Mg ^{+ 2} on a hydrogen cation H ⁺ , while the filter performance is at least 90 m ³ / h, and the filtering rate is at least 25 m / h, and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is performed composite of two fil ters diameter of 2600mm, was charged with a filter material layer height of 1200 mm, equipped with a filter upper distribution device, the filtration rate is at least 34 m / h, and the removal is carried hardness cations Ca ^+2, Mg ⁺² to 0.01 mg- equiv / kg, while in all ion-exchange filters for chemical water purification on the lower drainage device, an anthracite layer with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm is located. 9. The method according to any one of claims 7 and 8, characterized in that the chemically purified water is supplied to a steam boiler room with a temperature of 25-30 ^° C, and part of the chemically purified water is sent to sample coolers for continuous and periodic blowing of boilers, and from there - a head deaerator, another portion of the chemically treated water fed to gravity condensate cooler, which uses the heat of the steam condensate, and exiting the coolant water is separated into two streams, one of which is heated to 90 ^o C, is fed into the head of the deaerator, and the other of they are fed to the continuous purge cooler using heat from the purge water from the continuous purge separator, and then chemically purified water is passed through the deaerator vapor cooler, and then it is fed to the deaerator head and the chemically purified water is bubbled with steam, heating it to a temperature close to saturation, and O ₂ , CO gases are removed from the water, and the network heating water is supplied to the network pumps, and then through the network water heaters to the heating network, while repairing chemically purified water heaters switch network water heaters to heat chemically purified water. 10. The method according to any one of claims 6 to 9, characterized in that the steam from the steam generator through the collectors is supplied to the steam pipelines for technological needs, and part of the steam from the collectors through a reducing device with a pressure of P = 4 kgf / cm ^{2 is} fed to the network water heater , to a chemically purified water heater, to a fuel gas heater, to heat a fuel gas separator and to deaerators; in the presence of excess spent steam, part of the steam is supplied to chemically purified water heaters and network water heaters, and the condensate formed in them is sent to condenser tanks, from where they are pumped out by condenser pumps for condensate treatment; when the chemically purified water heater and network water heaters are operated on reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^° C is sent directly to the deaerator head to replace an equivalent amount of heated chemically purified water, while the network and chemically purified water heaters perform in the form of a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the level of condensate in the heat exchanger is maintained Knob level, and then the condensate is directed to water-water heat exchanger and subcooled to a temperature 80 - 90 ^o C, wherein the chemically purified water or a network is first passed through a water-water heat exchanger and then through the steam. 11. The method according to any one of claims 1, 6 to 10, characterized in that a steam boiler room is used as a steam generator, and return condensate is piped to a distribution comb, and condensate with a total hardness of 100 mEq / kg, Fe content is used in terms of Fe ⁺³ up to 180 mg / kg, silicon content (SiO ₂ ) - up to 350 mg / kg, oil content up to 80 mg / kg and pH up to 8.0, and if the condensate does not correspond to the specified parameters, it is sent to the drain , and from the distribution comb, the condensate is sent sequentially to the tank ynik and a tank for collecting pure condensate separated from oil products, and as the condensate floats up to the surface of the oil particles during collection, it is collected using a collecting funnel, while both tanks maintain a given volume of liquid due to the difference in the levels of overflow troughs - filling pipes, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed, to technological processing and loosening of filters of three degrees de-oiling, on clarification filters loaded with anthracite, in which they remove suspended mechanical particles and oil products up to 4 - 5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which are connected in parallel and loaded with activated carbon, and then - four sorption filters of the second stage of de-oiling the condensate to an oil content of not more than 0.05 mg / kg, and then the oil-free condensate with a temperature of 85 ^o C is sent to the annulus of heat exchange cold water, which is used for the technological needs of chemical water treatment, is passed through and the condensate is cooled to a temperature of 40 ^o C, then it is sent to a tank of oil-free condensate, from where the condensate is pumped to a desalination plant, and the temperature of the oil-free condensate is maintained at ranging from 35 to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the filter material is a highly basic cationite KU-2,8 Retrieve layer with altitude and 1.5 m and a filtration speed of 35 m / h, in which the stiffness cations and iron are held, and periodically, the exchange ability of the filters is restored by regeneration of the filter material with a 3-4% sulfuric acid solution, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as a filter material and condensate is removed from silicic acid compounds, and the exchange tank is periodically restored STI anion exchange filter by passing through the filter bed anion exchanger 3 - 5% solution of sodium hydroxide, and after the anion exchange filters with purified condensate content of silicic acid is not more than 150 mg / kg of iron (calculated as Fe ⁺³⁾ is not more than 100 mg / kg, petroleum products - not more than 0.5 mg / kg and with a total hardness not exceeding 10 mg / kg are sent to the condensate storage tank, from where they are pumped mainly to a thermal power plant (CHP) and a steam boiler room, as well as to a sulfur unit and to waste heat boilers, moreover for corrective treatment of desalted cond nsata to a pH of 8.5 - 9.5 and reducing the corrosion of the piping metal, a 1% ammonia solution is dosed into the collector by metering pumps, while the clarification filters used in the condensate purification are double-chamber, consisting of a housing and a lower and upper drainage distribution device, inside the case, a deaf flat horizontal partition is rigidly fixed, dividing it into two chambers, and tubular anchor links, through which air is removed from the lower chamber to the upper and maintained in amers of general pressure, while the upper drainage distribution device is made in the form of a funnel for uniform distribution of condensate on the surface of the filter material, which is used anthracite, the layer height of which in one chamber is 0.9 m with a grain size of 2-6 mm, and at filling the filter with filter material, it is first laid in the lower chamber, and then in the upper, and the lower distribution device is made in the form of a collector to which thirty-two beams are attached with a click evy holes 0.25 - 0.4 mm wide, which are closed with perforated plates to prevent entrainment of the filter material; four single-chamber filters connected in parallel and loaded with filter material — activated carbon with a layer thickness of 2.5 m and a grain size of 2-6 mm are used as sorption filters of the first stage, and the filters are equipped with upper and lower distribution devices, the upper of which is made in the form rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower distribution device - in the form of a collector in which the bottom is horizontally placed and in which insert distribution pipes with holes along the lower generatrix with a diameter of 8 mm, overlapped by a weldable gutter plate with a slit 0.25-0.4 mm wide to prevent activated carbon from entering the condensate; when condensate is supplied to the desalination plant, pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; they use hydrogen-cation exchange and anion exchange filters in the form of single-chamber cylindrical devices having a capacity of 115 m ³ / h, each of which with a diameter of 2.6 m is equipped with upper and lower manholes, fittings for hydroloading and upper and lower distribution devices, the upper of which They are made in the form of a "glass in a glass", and the lower one is in the form of a collector, in which distribution tubes-rays are inserted with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide, and in case of formation a gap hole in the weld point of the trough plate to prevent entrainment of filter material on the lower switchgear of the sorption filters, a litter layer of coarse anthracite is poured over the entire surface of the filter 10 cm high. 12. A method of producing jet fuel from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of the latter by passing a stream of oil through the net, and / or at least two levels in a mesh located in electric dehydrators electrodes covering in aggregate the altitude range of the electric dehydrator, mainly in the upper half of the height of its body, and the height gradient between the levels of the electrodes on p The amount of ascending oil flow is 0.05 - 0.1 of a conventional path segment, which coincides with the average vector of oil flow displacement in the zone of the largest midship of the electric dehydrator, passed by the flow during an hour of displacement with the average rate of the process of desalination, atmospheric and / or atmospheric-vacuum distillation of desalted and dehydrated oil using atmospheric distillation columns equipped with packages of cross-flow nozzles placed with high-altitude or high-angle displacement adequate to the temperature zones of steam condensation s, while at least part of the packages are placed in the condensation zone of the kerasin fraction with distillation when oil is supplied to the columns through at least two nozzles tangentially located in the column housing in the supply zone equipped with an internal cylindrical flow reflector, diameter which correlates with the diameter of the column body in the feed zone as (0.59 - 0.75): 1, with the separation of the kerosene fraction, hydrotreating the obtained kerosene fraction in the presence of a catalyst using a hydrotreating reactor with after by compounding the fractions obtained in the distillation and hydrotreating processes, characterized in that, at least in the electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, hydrotreatment reactors supply process heat, including using steam, which, at least partially obtained by burning associated gas contained in the feedstock and / or process gas emitted as a result of the thermal oil refining process and / or are thermally destructive x oil refining processes and / or intermediate products: gasoline, kerosene, diesel fractions, which are supplied to the network with a temperature of 50 - 70 ^o C and a pressure of 3 - 5 kg / cm ² , and before burning the gas is heated to a temperature of at least 100 ^o C , 60 - 85% of the gas is burned in the furnaces of technological processes, and 15 - 40% of the gas is burned in the steam generator with the formation of condensate, at least partially recovered as a result of heat extraction during the process of oil distillation, while the water used in the steam generator is return the condensate with the addition of heated chemically purified raw water, at least in the amount necessary to compensate for the non-returning condensate, to heat the chemically purified raw water and / or feed oil, the residual heat of the steam and / or steam condensate spent in the distillation of the oil is used and the process is carried out with sediment from the water and at least twice filtering the finished fuel. 13. The method according to p. 12, characterized in that the electric desalting and dehydration of oil is carried out in electric dehydrators with a horizontally oriented case of cylindrical or composite configuration and a working volume of 80 to 200 m ³ , or the electric desalting and dehydration of oil is carried out in electric dehydrators with a spherical or spheroidal body, and / or ellipsoidal, and / or ovoid, and / or teardrop-shaped, or electric desalting and dehydration of the oil is carried out in electric dehydrators with a cylindrical body and convex curvilinear end sections, and / or a toroidal shape, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically, or electric desalting and dehydration of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of Orient horizontally or at an angle to the horizontal. 14. The method according to p. 12, characterized in that the altitude range of input oil flows is (0.21 - 0.28) of the height of the column from the bottom of the column, while the oil in the column is atmospheric and / or atmospheric vacuum distillation through tubes disposed with an angle of dilution points of intersection with the axes of the nozzles of the column body in the range of 30 - 180 ^o with unilateral tangential swirling feed stream or feed oil into atmospheric distillation column is carried out through the nozzles, the axis of the neck and the inner one of which is orientable the flow of the vapor-liquid oil mixture supplied through it in the feed zone of the column directly at the intersection with a similar stream fed through another nozzle mainly in the zone of exit from the inner neck of the latter, or the oil is supplied to the atmospheric distillation column through nozzles whose axes are oriented parallel to the tangent to the body of the inner cylindrical reflector and radially removed from the conditional point of contact with the body of the reflector at a distance b satisfying the condition b ≥ 0.25 (R _k - R _o ), where R _k is the radius of the column in the feed zone, R _o is the radius of the reflector. 15. The method according to PP.12 and 14, characterized in that the distillation is carried out in a column, a cylindrical reflector in the feed zone of which is set eccentrically to the longitudinal axis of the column, or distillation is carried out in a column of atmospheric distillation, a cylindrical reflector which is performed with a variable radius of curvature in cross section or distillation is carried out in an atmospheric distillation column, the cylindrical reflector of which is connected to the column body with an annular membrane flat and / or broken, and / or curved, and / or combined figuration in cross-section, or at distillation using atmospheric distillation column, wherein the cross-flow landings packages made of spatially deformed elements from stainless steel sheet, the package height provides overlapping temperature gradients 2 - 8 ^o C by adjustment of the column and the passage of vapors area therethrough is 38 - 81% relative to the cross section of the column; distillation in an atmospheric distillation column is carried out at a vapor velocity of the accelerated fractions of at least 1.0 - 1.7 m / s; the withdrawal of the kerosene fraction with a boiling point of 140 - 240 ^o C is carried out in the altitude range of the primary distillation column of 0.57 - 0.81, counting from the bottom of the column or exceeding the lower and upper marks of the output range of the kerosene fraction by 0.37, respectively - 0.53 relative to the axis of entry of the nozzles supplying oil to the feed zone of the column, the extracted kerosene fraction is sent for subsequent hydrotreating together with the stream in a mixture with 30 - 35 wt.% Residual kerosene fraction 180 KK ^o C obtained by secondary distillation without nzine fraction.  16. The method according to p. 12, characterized in that when hydrotreating a kerosene fraction passed through one reactor, a reactor is used, at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-, gas-permeable element from an inert or a corrosion-resistant material or a combination of materials with similar properties, and at least the inlet surface of the catalyst layer along the path of the steam and gas product stream is larger than the cross-sectional area of the hydrotreating reactor ki, or when hydrotreating, use at least one reactor in which the catalyst layer is poured with an inclination of at least part of at least the upper surface, or when hydrotreating, use at least one reactor in which, at least the upper catalyst layer is poured with a conical and / or alternatingly broken, and / or alternatingly curved and / or combined inclination from the central zone to the walls of the reactor vessel, or at least one reactor is used in hydrotreating, in which the catalyst at the extreme To the least, in the upper part of the bulk array they are supplied with inclusions of inert elements with an aero- and hydraulic resistance less than that of an equivalent volume catalyst bed, or at least one reactor is used in hydrotreating, in which elements with increased aero-, hydraulic permeability is carried out in the form of mesh and / or perforated cylindrical or multifaceted glasses or pipes, or during hydrotreating, at least one reactor is used, in which part of the aero-, hydraulically permeable elements c is carried out in the form of bulk inclusions of inert particles with a radius greater than the radius or reduced radius of the catalyst particles, or at least one reactor is used in hydrotreating, in which at least part of the elements with increased air and hydraulic permeability perform combined with a bulk core and a flexible or rigid retina or perforated shell, or at least one reactor is used in hydrotreating, in which at least in the upper zone at least part of the catalysis layer the torus is mixed with larger particles of inert material, the particle ratio being predominantly variable with a decrease in the percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreating, or during hydrotreating, at least one hydrotreating reactor is installed with the longitudinal axis inclined relative to the horizon, or when hydrotreating, at least one reactor with a horizontally oriented longitudinal axis is used, or when hydrotreating, at least one hydrotreating fluids are toroidal, or hydrotreating reactors use alumina-cobalt or alumina-nickel-molybdenum hydrotreating catalysts, or combinations thereof, and a pre-prepared concentrate of a mixture of naphthenic acid and ionol additives in an amount of 0.007 to 0.008 wt.% in a weight ratio of additives is introduced into the hydrotreating product mixtures thereof (1.0 - 0.5): 2.  17. The method according to p. 12, characterized in that the compounding of the kerosene fractions is carried out in a tank equipped with at least one injector, which is installed in the lower half of the tank at an angle to the horizontal axis, or the compounding is carried out in a tank in which the injector is mounted on a rigid inner pipe in the lower third of the central zone of the tank with an upward slope of the injected kerosene stream, or compounding is carried out in a tank in which the injector is installed by means of tangential A flax mounted pipe, or compounding, is carried out using at least two injectors fixed to tangentially mounted pipes with a counter flow swirl, or mounted with the possibility of reactive rotation in the bottom or bottom of the tank.  18. The method according to any of paragraphs.12 to 17, characterized in that they use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after the raw water treatment is performed from suspensions and after cleaning the return steam condensate from oil pollution. 19. The method according to any one of paragraphs.12 to 18, characterized in that water from the Ural River is used with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and iron content 628 mg / kg, sulfates (SO ₄ ^-2 ) 1.78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84 - 5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to raw water pumps at least one of which is left standby, and then water is pumped through two heat exchangers with fixed tube sheets and heat water to a temperature of 25 - 30 ^o C, and at least one heat exchanger uses return condensate with a temperature of 80 - 85 ^o C, while the amount of raw water passed through this heat exchanger is regulated until the condensate cools down to a temperature of 25 - 35 ^o C, and the rest of the raw water is passed through another heat exchanger and heated to a temperature of 25 - 30 ^o C due to the use in this heat exchanger of heating water with a heater temperature water in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters with "hungry" regeneration, loaded with sulfonated coal, and carry out the removal of hardness salts from water to 1 - 2 mEq / kg constant and the destruction of bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and exchange of hardness and alkalinity salts present in water and chemical reactions with a hydrogen carbon cation of sulfonated coal, after which softened water is fed to self-regulating buffer filters loaded with sulfonated carbon to protect the filtrate from acid leakage, and then water is sent to remove free carbon dioxide in a decarbonizer loaded with rings Rashiga, and carry out the separation of air with carbon dioxide, which is discharged into the atmosphere, decarbonized water is directed by gravity to the tank, after which this water is pumped Chiva over sodium cation-stage filters, in the filters of the first stage produce the removal of hardness cations to 0.1 meq / kg, and in the second stage is carried out deeper removal of hardness cations Ca ^+2, Mg ⁺² to 0.01 mEq / kg and get chemically purified water with a transparency of at least 40 cm, a total hardness of 2 - 5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 μg / kg and a pH of 8.0, after which chemically purified water is fed in tanks, and then pumped into the steam generator, while at least during the wasp flood estvlyayut preliminary water purification, which is carried out using at least two brighteners capacity of 250 m ³ / h, two mixers lime milk capacity of 15 m ³ each, the two measuring tanks coagulant 10 ^m3 each, wet lime storage cell, preferably lime putty capacity of 100 m ^3, lime milk cell capacity of 60 m ³ and metering pumps, and / or centrifugal pumps with additional regulating valves, and the chemical purification of water produced only using sodium cation filters, a koto s also produce regeneration of the filter material with the concentration of brine 6 - 8%. 20. The method according to claim 19, characterized in that for the chemical treatment of water, mechanical filters are used in the form of cylindrical vessels with an internal anti-corrosion coating, mainly of epoxy resin, with two spherical steel bottoms, in the upper of which a feed water supply fitting is placed and an upper distribution device, which is made in the form of beams of polymer material for distributing water along the filter cross section, and on the lower bottom there is a drainage system in the form of a collector with slotted tubes made of stainless steel, along the axis of which holes are formed, overlapped by casings with slits 0.25 - 0.4 mm wide, and in the upper part of the filter housing they form a hatch for examining the surface of the filter material, and in the lower part there is a manhole for mounting and repairing the upper and lower drainage systems, while on the filter housing at the level of the slit tubes, a fitting for hydroloading is placed, feed water pipes, loosening, air vents of the upper and lower drainage systems are connected to the filter, pressure gauges at the inlet and outlet of the collector are connected, sampler ki and valves, and the filter operate filling bilayer consisting of the layer of quartz sand of 700 mm and a volume of 6.4 m ³ and a layer of anthracite height of 500 mm and a volume of 4.6 m ^3, the filter performance considering the water consumption by and the preparation of regeneration solutions is not less than 200 m ³ / h, the filtering rate during operation of all filters is not less than 7 m / h and the maximum during loosening washing is not less than 10 m / h with a flow rate of 5 m ³ / h for loosening compressed air and pressure up to 1.5 kgf / cm ² ; use hydrogen-cation exchange filters with a filtration area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm, and the filter is equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the water flow over the surface of the filter material and the inner surface of the filter is performed with a rubber gum coating, while the filter performance is at least 80 t / h and the filtering speed is at least 13 m / h; use self-regulating buffer filters loaded with sulfonated coal with a loading layer height of 2000 mm, with an upper dispenser in the form of a "glass in a glass", moreover, the performance of one filter is at least 180 m ³ / h and the filtering speed is at least 25 m / h; use a decarbonizer filled with Rashig rings and perform with a lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to a collection tank for this water with a capacity of at least 400 m ³ ; using a two-stage sodium cationite filter with an upper, consisting of rays, and lower distribution devices, the first stage of this filter is made up of three filters with a diameter of 3000 mm and is loaded with filter material with a layer height of 1900 mm to replace the cations Ca ⁺² , Mg ⁺² with cation hydrogen H ⁺ , while the filter capacity is at least 90 m ³ / h, and the filtration rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is made of two fil trench 2600 mm diameter was charged with a filter material layer height of 1200 mm, equipped with a filter upper distribution device, the filtration rate is at least 34 m / h, and the removal is carried hardness cations Ca ^+2, Mg ⁺² to 0.01 mEq / kg, while in all ion-exchange filters for chemical water purification on the lower drainage device, an anthracite layer with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm is located. 21. The method according to any one of paragraphs 12, 19 and 20, characterized in that the chemically purified water is supplied to a steam generator with a temperature of 25 - 30 ^o C, and part of the chemically purified water is sent to the sampling coolers for continuous and periodic blowing of boilers, and from there - into the deaerator head, another part of chemically purified water is sent to a gravity condensate cooler in which steam condensate heat is used, and the water leaving the cooler is divided into two streams, one of which is heated to 90 ^o C, is fed into the deaerator head, and the other they are fed to the continuous purge cooler using heat from the purge water from the continuous purge separator, and then chemically purified water is passed through the deaerator vapor cooler, and then it is supplied to the deaerator head and steam is chemically cleaned by steam, heating it to a temperature close to saturation, and water is removed from the gases O _2, CO and network heating water fed to the network pumps, heaters, and then through the heating water in the heating system of the enterprise, while the repair heaters chemically eyes ennoy water carried switching network water heaters for heating the chemically treated water. 22. The method according to any one of paragraphs 12, 18 to 21, characterized in that the steam from the steam generator through the collectors is fed into the steam pipelines of the enterprise for technological needs, and part of the steam from the collectors through a reducing device with a pressure of P = 4 kgf / cm ^{2 is} fed to network water heater, to a chemically purified water heater, to a fuel gas heater, to heat a fuel gas separator and to deaerators; in the presence of excess spent steam, part of the steam is supplied to chemically purified water heaters and network water heaters, and the condensate formed in them is sent to condenser tanks, from where they are pumped out by condenser pumps for condensate treatment; when the chemically purified water heater and network water heaters are operated on reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^° C is sent directly to the deaerator head to replace an equivalent amount of heated chemically purified water, while the network and chemically purified water heaters perform in the form of a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the level of condensate in the heat exchanger is maintained Knob level, and then the condensate is directed to water-water heat exchanger and subcooled to a temperature 80 - 90 ^o C, wherein the chemically purified water or a network is first passed through a water-water heat exchanger and then through the steam. 23. The method according to any one of claims 12, 19 to 22, characterized in that a steam boiler room is used as a steam generator, and return condensate is piped to a distribution comb, and condensate with a total hardness of 100 mEq / kg, Fe content is used in terms of Fe ⁺³ up to 180 mg / kg, silicon content (SiO ₂ ) - up to 350 mg / kg, oil content up to 80 mg / kg and pH up to 8.0, and if the condensate does not correspond to the specified parameters, it is sent to the drain , and from the distribution comb, the condensate is sent sequentially to the sludge tank an oinnik and a tank for collecting pure condensate separated from oil products, and as the condensate floats up to the surface of the oil particles, it is collected using a collecting funnel, while both tanks maintain a given volume of liquid due to the difference in the levels of overflow troughs - filling pipes, after which pure condensate with a petroleum product content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of filters of three stages de-oiling, on clarification filters loaded with anthracite, in which they remove suspended mechanical particles and oil products up to 4 - 5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which are connected in parallel and loaded with activated carbon, and then - sorption filter into four second-stage condensate to the deoiling oil contained not more than 0.05 mg / kg and then deoiled condensate at a temperature of 85 ^o C is directed into the annulus teploobmennyh Cove, which passed the cold raw water used for the technological needs of the chemical treatment and is carried condensate cooling to a temperature of 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting unit, wherein deoiled condensation temperature is maintained within a from 35 to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the filter material is a highly basic cationite KU-2,8 Retrieve layer with altitude and 1.5 m and a filtration speed of 35 m / h, in which stiffness cations and iron are held, and periodically, the exchange ability of the filters is restored by regenerating the filter material with a 3-4% sulfuric acid solution, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as a filter material and condensate is removed from silicic acid compounds, and exchange capacities of anion exchange filters by passing through a filtering layer of anion exchange resin a 3-5% solution of sodium hydroxide, and after anion exchange filters, purified condensate with a content of silicic acid of not more than 150 mg / kg, iron (in terms of Fe ⁺³ ) not more than 100 mg / kg, petroleum products - not more than 0.5 mg / kg and with a total hardness of not more than 10 mg / kg are sent to the condensate reserve tank, from where they are pumped mainly to a thermal power station (CHP) and a steam boiler room, as well as to a sulfur production unit and waste heat boilers, moreover, for corrective processing of obesso of condensate to a pH of 8.5 - 9.5 and a decrease in the corrosion of the piping metal, a 1% ammonia solution is dosed into the collector with metering pumps, while two-chamber clarification filters consisting of a housing and lower and upper drainage distributors are used for condensate cleaning, inside the case, a deaf flat horizontal partition is rigidly fixed, dividing it into two chambers, and tubular anchor connections, through which air is vented from the lower chamber to the upper and maintained in total pressure chambers, while the upper drainage distribution device is made in the form of a funnel for uniform distribution of condensate on the surface of the filter material, which is used anthracite, the layer height of which in one chamber is 0.9 m with a grain size of 2-6 mm, and filling the filter with filter material, it is first placed in the lower chamber, and then in the upper and lower distribution devices in the form of a collector to which thirty-two beams are attached with a slit bubbled hole width of 0.25 - 0.4 mm, which close the perforated plates to avoid entrainment of filter material; four single-chamber filters connected in parallel and loaded with filter material — activated carbon with a layer thickness of 2.5 m and a grain size of 2-6 mm are used as sorption filters of the first stage, and the filters are equipped with upper and lower distribution devices, the upper of which is made in the form rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower distribution device in the form of a collector in which the bottom is horizontally placed and in which stavlyayut distribution tubes with holes along the lower generatrix of diameter 8 mm, overlapped welded trough plate with a gap width of 0.25 - 0.4 mm to avoid contact with the activated carbon in the condensate; when condensate is supplied to the desalination plant, pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; they use hydrogen-cation exchange and anion exchange filters in the form of single-chamber cylindrical apparatuses with a capacity of 115 m ³ / h, each of which with a diameter of 2.6 m is equipped with upper and lower manholes, fittings for hydroloading and upper and lower switchgears, the upper of which They are made in the form of a “glass in a glass”, and the lower one is in the form of a collector into which distribution tubes are inserted — beams with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide, and in case of formation slot openings in the trough spot welding the plate to avoid entrainment of the filter material on the lower dispenser sorption filters poured krupnodroblennogo litter layer of anthracite over the entire surface of the filter height 10 cm.

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