RU2155208C1 - Light-oil products' production process - Google Patents

Abstract

FIELD: petroleum processing and petrochemistry. SUBSTANCE: crude oil is subjected to electrodesalting and dehydration and/or atmospheric and vacuum distillation. Gasoline fractions are subjected to stabilization and secondary distillation; gasoline, kerosene, and diesel fraction to hydrofining; and hydrofined gasoline fraction to reforming. When conducting operations, steam used as heat carrier is partly produced by combustion of associated gas and/or process gas releasing in petroleum processing thermal processes, and/or petroleum processing thermodestructive processes, and/or intermediate products. Gas is supplied into gas network at 50-70 C and pressure 3-5 kg/sq. cm. 60 to 85% of gas is burnt in process furnaces and 15 to 40% of steam generator to form condensate. The latter in mixture with preheated chemically purified water is used in steam generator. EFFECT: reduced power consumption, increased yield of products and improved their quality. 20 cl, 1 tbl

Description

 The invention relates to a method for producing light petroleum products - gasoline, kerosene and diesel fractions - processing low-sulfur, sulfur and high-sulfur oils and can be used in petrochemicals.

 A known method of producing light petroleum products from low-sulfur and / or sulfur, and / or high-sulfur oils by electric desalting and dehydration of the latter by passing a stream of oil through a system of electrodes located in electric dehydrators, atmospheric and / or atmospheric-vacuum distillation of desalted oil using atmospheric distillation columns, output from the last straight run gasoline, kerosene, diesel fractions, stabilization of gasoline fractions, secondary distillation of stable fractions, hydrotreatment b gasoline and kerosene fractions in the presence of a catalyst using hydrotreating reactors, reforming hydrotreated gasoline fractions in the presence of a catalyst in reforming reactors, alkalizing diesel fractions by treatment with sodium hydroxide solution using an alkalization reactor and compounding fractions obtained at the process stages, and auxiliary materials (B. N. Erich and others. Chemistry and technology of oil and gas. - L.: Chemistry, 1985, p. 96-152).

 The specified method is characterized by such disadvantages as the relatively low quality and yield of the target products, as well as increased energy consumption for the process and the lack of efficiency of structural solutions to technological schemes.

Closest to the invention in its essence and the achieved result is a method for producing light oil products 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 a mesh and / or mesh located in electrodehydrators in not less than two levels of 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 the path of the upward oil flow is 0.05-0.1 conventional section of the path, which coincides with the average vector of the oil flow in the zone of the greatest midship of the electric dehydrator, which the stream travels per hour of movement at an average speed the process of desalination, atmospheric and / or atmospheric vacuum distillation of desalted oil using atmospheric distillation columns equipped with packages of cross-precision nozzles placed with high or high the relative-angular displacement is adequate to the temperature zones of vapor condensation, while at least part of the packages are placed in the condensation zone of the kerosene fraction 120-180 ^o C and distillation when oil is supplied to the columns through at least two pipes tangentially located in column housing in the area supply, provided with inner cylindrical reflector stream whose diameter corresponds with the diameter of the column in the housing as the supply zone (0,59-0,75): 1, with separation of the kerosene fraction, the kerosene fraction withdrawal 140-240 ^o C impl they melt in the altitude range of the atmospheric and / or atmospheric vacuum distillation column, which is 0.58-0.81 of the column height, counting from the bottom of the column, or exceeding the lower and upper marks of the output range of the kerosene fraction by an amount equal to 0.37 -0.53 from the height of the column relative to the axis of entry of the oil supply pipes into the feed zone of the column, and the extracted kerosene fraction is divided into three streams with a volume ratio of the first stream: second stream: third stream, respectively (1.2-8.5): (12.8-15.5): (9.5-11.8), output of diesel fra tion 240-350 ^o C or diesel fractions 240-350 ^o C and 300-350 ^o C is performed in the height range of the atmospheric column and / or atmospheric and vacuum distillation, 0,32-0,62 constituting the column height, measured from the bottom of the bottom , or exceeding the lower and upper marks of the output range by an amount equal to (0.06-0.12) and (0.23-0.41), respectively, from the height of the column relative to the axis of entry of the oil supply pipes into the supply zone of the column, stabilization of gasoline fractions, the secondary distillation of a portion of the stable gasoline fraction of the distillation of desalted oil in an amount of 0.51-0.61 from about its amount fraction in which the fractions boiling in the temperature range of SC-85 ^o C, 85-180 ^o C and a residual, hydrotreating in hydrotreater reactors gasoline and kerosene fractions in the presence of a catalyst, wherein the hydrotreating gasoline fraction 85-180 ^o C part it is passed through one hydrotreating reactor, and the other part in an amount of 0.4-0.6 of the total amount is passed through at least two hydrotreating reactors with selective variation in the flow in the latter, reforming the hydrotreated gasoline fraction, according to in at least three reactors, at least the last of which has a deep radial introduction of the gas product mixture into the catalyst, and when hydrotreating the kerosene fraction in a mixture with the residual fraction of the secondary distillation, taken in an amount up to 30-35% of the initial kerosene fraction, in a hydrotreating product is introduced through a damper tank to a pre-prepared concentrate of a mixture of additives of naphthenic acids and ionol in an amount of 0.007-0.008 wt.% and a mass ratio of additives in their mixture (1.0-1.5): 2, alkalization of diesel fractions Uteem NaOH treatment in the reactor alkalization and compounding fractions (see. RU 2033421 C1, 04.20.95).

 The known method, providing higher quality light petroleum products and reducing energy costs at the intermediate stages of obtaining various oil distillation fractions, is nevertheless expensive due to the need to purchase steam used in technological processes for the production of light petroleum products outside this production, as well as significant heat losses of fuel gas flared.

 The objective of the present invention is to reduce energy consumption, increase the yield of petroleum products per fuel used, reduce the cost of the process due to the rational production of steam, use of heat from the waste streams of processing and reduce the amount of fuel gas burned on a flare, as well as improve the environmental situation.

The problem is solved due to the fact that in the method for producing light oil products 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 mesh and / or mesh located in electric dehydrators than in 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 gradient cell between the electrode levels on the path of the upward flow of oil is 0.05-0.1 conventional section of the path, which coincides with the average displacement vector of the oil flow in the zone of the greatest midship of the electric dehydrator, traveled by the stream per hour of movement with an average rate of desalination, atmospheric and / or atmospheric -vacuum distillation of demineralized oil using atmospheric distillation columns equipped with packages of cross-precision nozzles placed with a vertical or vertical-angular displacement adequate to the temperature vapor condensation, while at least part of the packages are placed in the condensation zone of the kerosene fraction 120-180 ^o C and distillation when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the supply 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, with the extraction of the kerosene fraction, and the output of the kerosene fraction 140-240 ^{o is} carried out in the altitude range of the column of atmospheric and / or atmospheric-vacuum distillation, comprising 0.58-0.81 of the column height, counting from the bottom of the bottom, or exceeding the lower and upper marks of the output range of the kerosene fraction, respectively, by an amount equal to 0.37-0.53 of the column height relative to the axis of entry of the oil supply nozzles into the feed zone of the column, and the extracted kerosene fraction is divided into three streams with a volume ratio of the first stream: second stream: third stream, respectively (1.2-8.5): (12.8-15.5 ): (9.5-11.8), the output of the diesel fraction 240-350 ^o C or diesel fractions 240-300 ^o C and 300-350 ^o C OS they are installed in the altitude range of the column of atmospheric and / or atmospheric vacuum distillation of 0.32-0.62 of the height of the column, counting from the bottom of the bottom, or exceeding the lower and upper marks of the output range by an amount equal to (0.06- 0.12) and (0.23-0.41) from the height of the column relative to the axis of entry of the oil supply pipes into the feed zone of the column, stabilization of the gasoline fractions of the secondary distillation of a portion of the stable gasoline fraction of the distillation of desalted oil in an amount of 0.51-0.61 from the total number of fractions, which receive fractions ii, boiling in the temperature range of SC-85 ^o C, 85-180 ^o C and a residual, hydrotreating in hydrotreater reactors gasoline and kerosene fractions in the presence of a catalyst, wherein the hydrotreating gasoline fraction 85-180 ^o C part of it is passed through a hydrotreating reactor, and the other part in the amount of 0.4-0.6 of the total amount is passed through at least two hydrotreating reactors with selective variation in the flow in the latter, reforming the hydrotreated gasoline fraction in at least three reactors, at least the ice of which has a deep radial introduction of the gas product mixture into the catalyst, and when hydrotreating the kerosene fraction in a mixture with the residual fraction of the secondary distillation taken in an amount of up to 30-35% of the initial kerosene fraction, a pre-prepared additive mixture concentrate is introduced into the hydrotreating product through a damper tank naphthenic acids and ionol in an amount of 0.007-0.008 wt. % and the mass ratio of additives in their mixture (1.0-1.5): 2, alkalization of diesel fractions by treatment with caustic soda solution in the alkalization reactor and compounding fractions, according to the invention, diesel fractions are further hydrotreated, at least, in electric dehydrators , atmospheric and / or atmospheric vacuum distillation columns, hydrotreating reactors and reforming reactors supply process heat, including using steam, which is at least partially obtained by Zhiganov contained in the raw material passing gas and / or fuel and process gas released from the thermal process of refining and / or refining processes thermodestructive and / or intermediate products: gasoline, kerosene, diesel fractions, which is fed into the network at a temperature of 50-70 ^o C and a pressure of 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 recoverable as a result of heat extraction, mainly during oil distillation processes, while return 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-return condensate, and to chemically heat purified raw water and / or source oil using the residual heat of steam and / or steam condensate spent in the technological processes of distillation of oil.

 In this case, oil electrodesalting and dehydration can be carried out in electric dehydrators with a spherical or spheroidal body, and / or ellipsoidal, and / or ovoid, and / or teardrop-shaped, and / or in composite electric dehydrators with a cylindrical body and convex-curved end sections, and / or toroidal shape, and / or in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically, and / or in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented horizontally or horizontally.

Oil can be supplied to atmospheric and / or atmospheric vacuum distillation columns through nozzles located at an angle of dilution 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 twist of the feed stream, or oil can be supplied to the atmospheric distillation column through the nozzles, the axis and the inner neck of one of which orient the flow of oil supplied in the feed zone of the column directly to the intersection with a similar flow supplied through another nozzle predominantly in the zone of 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 internal cylindrical reflector with a radial distance from the conditional contact point with the reflector body at a distance b satisfying the condition b ≥ _{0,25 (R k - R o)} , where R _k - radius of columns in the zone power, R _o - radius of the reflector, wherein the cylindrical reflector in supply zone is set with an eccentricity relative to the longitudinal th column axis or cylindrical reflector operate with a variable radius of curvature in cross section, or cylindrical reflector column is connected with the housing an annular membrane flat and / or polygonal and / or curved and / or the combined cross-sectional configuration; regular packages of cross-precision nozzles are made of spatially deformed elements of stainless steel sheet with overlapping height of the package of temperature gradients 2-8 ^o C along the height of the column and the area of passage of vapors through them, comprising 38-81% relative to the cross section of the column, or distillation in the atmospheric distillation column is carried out at a passage speed of vapors of the accelerated fractions of at least 1.0-1.7 m / s, and during secondary distillation, the condensation of gasoline vapors is carried out in condensate ah air cooling.

Upon stabilization, a gaseous fraction of NK-62 ^° C can be obtained, which is purified from sulfur-containing impurities by a solution of monoethanolamine, followed by separation in a gas fractionation unit with the release of a gasoline component for compounding gasolines.

 When hydrotreating a gasoline fraction, passed through at least two reactors, the latter can bind along the gas-vapor product mixture with the possibility of direct or reverse passage of the latter through the catalyst beds, or with the possibility of their parallel or alternately separate inclusion in the work adequately given volumes and degree of hydrotreating of gasoline fractions, or during hydrotreating, at least one hydrotreating reactor is used, at least in the upper zone of which the catalyst layer is loaded with disc with an inert and / or combined vapor-gas-permeable element made of an inert or corrosion-heat-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 vapor-gas product flow is greater than the cross-sectional area of the hydrotreating reactor, or at least one hydrotreating reactor in which a catalyst bed is sloped with at least part of at least the upper surface, or during hydrotreating at least one hydrotreating reactor is used 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 during hydrotreating, at least one hydrotreating reactor is used, in which the catalyst, at least in the upper part of the bulk array, is provided with inclusions of inert elements with aerohydraulic resistance less than that of equivalent volume catalyst, or during hydrotreating, at least one hydrotreating reactor is used, in which elements with increased aerohydraulic permeability are made in the form of mesh and / or perforated cylindrical or multifaceted cups or pipes, or at least one reactor is used during hydrotreating, in which part of the aerohydraulically permeable elements is performed 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 aero-hydraulic permeability are combined with a bulk core and a flexible or rigid retina or perforated shell, or at least one hydrotreating reactor is used in hydrotreating, which, at least in the upper zone, at least part of the catalyst layer is mixed with larger particles of inert material, or at least one reactor is used in hydrotreating, in which the ratio the particles are carried out alternating 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 a portion of the hydrotreating reactors are set with an inclination of the longitudinal axis relative to the horizon, or at least some hydrotreating reactors are used during hydrotreating with a horizontally oriented longitudinal axis, or during hydrotreating, at least one hydrotreating reactor is toroidal; when the amount of gasoline fraction subjected to hydrotreating exceeds the installed capacity of the catalytic reforming unit, an excess amount of hydrotreated gasoline fraction is sent to compounding to produce automobile gasolines, while hydrotreating reactors use aluminum-cobalt or aluminum-nickel-molybdenum, or zeolite-containing hydrotreating catalysts, or

 When reforming at least one reforming unit, at least the last two reactors can be tied in parallel along the steam-gas mixture, or when reforming, at least one reforming reactor is used, at least in the upper zone of which the catalyst layer they are loaded with a discrete and / or combined vapor-permeable element of an inert or corrosion-heat-resistant material or a combination of materials with similar properties, and at least the input surface of the layer is catalyzed and along the path of the gas-vapor product stream, they exceed the cross-sectional area of the reforming reactor, or at least one reforming reactor is used in the reforming, in which the catalyst layer is poured with at least part of at least the upper surface, or at least one reforming reactor is used in which at least the upper catalyst layer is poured with a conical and / or alternately broken and / or alternately curved and / or combined tilt from the chain the neutral zone to the walls of the reactor vessel, or when reforming, at least one reforming reactor is used, in which the catalyst, at least in the upper part of the bulk array, is provided with inclusions of inert elements with aerohydraulic resistance less than that of a layer equivalent in volume catalyst, or when reforming using at least one reforming reactor, in which elements with high aerohydraulic permeability are in the form of a mesh and / or perforated cylindrical or many early glasses or nozzles, or when reforming, at least one reforming reactor is used, in which part of the aerohydraulically permeable elements is performed in the form of bulk inclusions of their inert particles with a radius greater than the radius or reduced radius of the catalyst particles, or when reforming at least one reforming reactor, in which at least part of the elements with enhanced aero-hydraulic transparency is performed combined with a bulk core and a flexible or rigid retina, or at least one reforming reactor, in which at least in the upper zone, at least part of the catalyst layer is mixed with larger particles of inert material, while the particle ratio is advantageously performed by varying with by decreasing the percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to reforming, or during reforming, at least a portion of the reforming reactors are installed with a slope of the longitudinal axis flax horizon, or when reforming use at least part of the reactors with a horizontally oriented longitudinal axis, or when reforming, at least one reactor is toroidal, or when reforming into the stream of steam product mixture passed through the catalyst bed in reforming reactors, periodically a solution of an organochlorine compound is introduced to restore the activity of the catalyst, while dichloroethane or trichloroethane is used as the organochlorine compound, at least in part reforming reactors use platinum-alumina catalysts or platinum-rhenium catalysts, or combinations thereof.

 The treatment of the diesel fraction with sodium hydroxide solution can be carried out in stages, while the first stage is carried out by injection through an injector installed outside the alkalization reactor, with a ratio of the volumes of the diesel fraction and sodium hydroxide equal to 0.5-2.0, the resulting mixture is introduced into the bottom layer of the caustic solution sodium and carry out the second stage using the mother liquor, consisting of a distribution manifold equipped with a distribution pipe system, when filling with caustic soda solution the reactor volume is 0.5-0.75 of its height and speed growth of introducing a diesel fraction into the solution layer equal to 0.6-7.9 m / s, compounding of the diesel fraction is carried out in one or two or three stages, while compounding in the first stage is carried out either directly in an atmospheric and / or atmospheric column vacuum distillation by adding a straight-run kerosene fraction to the diesel fraction of the first stream and / or in a process pipeline connecting the atmospheric and / or atmospheric vacuum distillation column to the alkalization reactor by supplying a second straight stream to the pipeline of the kerosene fraction, compounding in the second stage is carried out after alkalizing the diesel fraction directly in the diesel fuel storage tank by supplying straight-run and / or hydrotreated kerosene fraction under excessive pressure, while using alkalization of high sulfur fractions using 3.0-5.0% sodium hydroxide solution when supplying the diesel fraction to at least two reactors in parallel flows, or when alkalizing, use at least one reactor with the supply of the diesel fraction through external engineering a core, the output nozzle of which is installed with a negative difference in the height of the nozzle to a height of at least 1 m relative to the lower level of the alkaline solution in the alkalization reactor, or when alkalizing, use at least one reactor with distribution pipes supplying the diesel fraction located at a height of 0, 05-0.75 of the height of the caustic soda solution, while the diesel fraction purified in the alkalization reactor is fed into at least one settling tank, kept there for at least 50-80 minutes and sent for compounding, or when alkalizing, at least one alkalizing reactor is used, the perforation in the mother liquor distribution pipes is performed at least partially in the form of round-cylindrical and / or ovoid and / or combined configurations, or slit-like openings, or when alkalizing, at least one reactor in which the perforations in the mother liquor distribution pipes are made with a variable pitch and / or diameter, and / or with an effective flow area with increasing listed pairs When removing from the input zone of the dispensing manifold into the alkalization tank, it is adequate to drop the hydraulic pressure in the elements of the diesel distillate input system, or when alkalizing, at least one reactor is used in which at least part of the perforation holes are oriented with the flow outflow axes along at least one reactor, in which at least part of the perforation holes of the distribution pipes are oriented at downward angles, or when alkalizing and horizon alkalization or by using at least one reactor, wherein at least a portion of perforations disposed in a spiral with a constant or variable pitch; while alkalizing, the supply of the mixture of diesel fraction with alkali solution to the alkalization reactor is carried out by pulses or when alkalizing, at least one reactor is used, in which the mother liquor distributor is made in the form of a pipe of variable cross-section along the length of the alkalization reactor, and the supply of the mixture of diesel fraction and the alkali solution into the alkalization reactor is carried out at a variable speed in different zones of the reactors, or at least one alkalization reactor is used for alkalization; in which, during the input and output of the diesel fraction, they are kept within 16-20% of the initial level of sodium hydroxide solution in the reactor by the time the alkalization process begins, or when alkalizing, at least one alkalizing reactor is used, which is horizontal with a cylindrical or ellipsoidal or ovoid, or tear-shaped cross-section, or when alkalizing, use at least one alkalization reactor, which is performed with a broken or curved axis in plan or toroidal in shape e closed or open torus, or when alkalizing, use at least one reactor, which is performed with an inclination to the horizontal or with at least one fracture of the longitudinal axis in the vertical plane, or when alkalizing, use at least one reactor, which provide a screen horizontally oriented or inclined, open at least from one end, immersed within the upper third in the alkalized fraction.

 After alkalization, the alkali-treated diesel fraction can be removed from the upper zone of the alkalization reactor and subjected to water washing and / or sludge in a tank for water washing and / or in a settling tank, at least one is used for water washing and / or sludge at least one settling tank, which is horizontally or hollowly inclined with a cylindrical or ellipsoidal cross-section, or when settling, use at least one settling tank, which is made with a broken or curved axis in plan, or toroidal in the form of a closed or open torus, or when settling, at least one settling tank is used, which is provided with a screen-partition, open from one end and immersed in the surface layer of the diesel fraction, horizontally oriented or inclined, and / or vertical, or with sludge, use at least one settling tank, which crammed with at least two pairs of electrodes, intensifying the deposition of suspensions and impurities from the diesel fraction.

 Compounding in the technological pipeline of the kerosene fraction and / or vacuum solarium can be carried out stepwise or discretely through at least two nozzles cut into the main pipeline from different sides, and / or spaced apart along the length and oriented at an acute angle along the mixed fractions, or when compounding use nozzles for introducing components mixed with the diesel fraction located in the pipeline and providing unidirectional or opposite directional tangentially vortex swirl of the mixed outflows, or when compounding in the pipeline in the inner section of it in the area immediately after the zone of the nozzles supplying kerosene and / or vacuum-solar components mixed with the diesel fraction, at least one fixed impeller is installed, or when compounding in the pipeline in the internal section at least two impellers with counter-directional swirling of the blades, fixed relative to the body of the pipeline or motionlessly fixed one relative to another with the possibility of free joint rotation when an imbalance occurs, the vortex countercurrents created by them intensify the process of compounding the diesel fraction, and when the diesel fraction is removed from the column of atmospheric and / or atmospheric vacuum distillation, the selection of excess resulting heat is carried out mainly before the start of the first compounding stage, the second stage compounding is carried out in a diesel fuel storage tank by directly mixing the flows of diesel fuel supplied to the tank and the kerosene fraction, either through an injector introduced into the bottom zone of the tank when the diesel fraction and the kerosene fraction are separated in time, or in the second compounding stage, an injector is used, which is introduced into the tank and fixed on a rigid inner pipe in the lower third of the central zone of the tank with an upward slope of the injected stream, or in the first compounding step, a vacuum solarium removed from the vacuum column is added to the diesel fraction and / or its mixture with the straight-run kerosene fraction NNA atmospheric vacuum distillation; in the second stage of compounding, a reservoir is used, the injector into which is introduced by means of a tangentially mounted nozzle, or compounding in a diesel fuel storage tank is carried out by means of at least two injectors fixed on tangentially installed nozzles with an opposite flow swirl, or compounding in a diesel fuel storage tank carried out by means of at least two injectors movably with the possibility of reactive rotation installed in the bottom or bottom bottom ti tank.

 Raw water can be used 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 contaminants.

They can 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 (Ca ⁺² ) 3.0 mEq / kg, magnesium (Mg ²⁺ ) 1.8 mEq / kg, and oxidizability of permanganate 3.84-5.12 mg / kg in 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 heating water is heated 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 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 a temperature of the heating water in accordance with the season, and after heating water is sent for filtration to mechanical filters with a 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, then the clarified water is fed to hydrogen-cationite filters with "hungry regeneration" loaded with sulfonated coal and carried out removal of hardness salts from water to 1-2 mEq / kg constant and destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and ion exchange of hardness and alkalinity salts available in water, and chemical reactions with a hydrogen cation of sulfonated carbon, after which softened water is fed to self-regulating buffer filters loaded with sulfonated carbon that protects the filtrate from acid leakage, 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 discharged into the atmosphere, decarbonized water is directed by gravity into the tank, after which this water is pumped through the pumps with two-stage sodium-cationite fil Secondly, in the filters of the first stage, stiffness cations are removed up to 0.1 mEq / kg, and in the second stage, deeper stiffness cations (Ca ⁺² , Mg ⁺² ) are removed to 0.01 mEq / kg to obtain 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 value of 8.0, after which chemically purified water is fed into tanks, and then pumped into the steam generator by pumps.

At least during the flood period, they can pre-treat water, which is carried out using at least two clarifiers with a capacity of 250 m ³ / hour, two lime milk mixers with a capacity of 15 m ³ each, two coagulant measuring tanks of 10 m ³ each, wet storage cells lime, lime putty preferably, a 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 is carried out only with the use aniem sodium cation filters, which also conduct regeneration of the filter material with brine at a concentration of 6-8%.

For chemical water purification, mechanical filters can be used in the form of cylindrical vessels with an internal anticorrosive coating, mainly made of epoxy resin, with two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device in the form of beams made of polymer material for distribution are placed water along 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 are formed Holes covered by casings with slits 0.25-0.4 mm wide, and in the upper part of the filter housing form a hatch for inspecting the surface of the filter material, and in the lower part a hole 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, an air vent 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 two filtering filling a layered one, 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 not less than 7 m / h and the maximum during loosening washing is not less than 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 ³ ; can use hydrogen-cation exchange filters with a filtering 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 systems, 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-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; can 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 the collection tank for this water with a capacity of at least 400 m ³ ; can use 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 loaded with filter material with a layer height of 1900 mm to replace the cations Ca ^{+ 2} , Mg ^{+ 2} on the H ⁺ cation, while the filter performance is not less than 90 m ³ / h, and the filtration rate is not less than 25 m / h and stiffness cations are removed to 0.1 mEq / kg, and the second stage of the filter is made of two filters with a diameter of 2600 mm, they are loaded with filter material with a layer height of 1200 mm, the filter is equipped with an upper distribution device, while the filtering speed is at least 34 m / h and stiffness cations are removed up to 0.1 mEq / kg, while in all ion-exchange filters for chemical water treatment on the lower drainage device have an anthracite underlying layer with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm.

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 steam condensate heat, 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 I heat the purge water from the continuous purge separator, then chemically purified water is passed through the deaerator vapor cooler, and then it is supplied to the deaerator head and the chemically purified water is bubbled with steam, heating it to a temperature close to saturation, and O ₂ gases are removed from the water , CO _2, and network heating water is supplied to the input line pumps, heaters, and then through the heating water in the heating system, while the repair heaters chemically purified water is performed with switching the heaters tevoy water for heating chemically purified water.

Steam from the steam generator through the collectors can be fed into 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 separator heater fuel gas and deaerators.

 In the presence of excess spent steam, part of the steam can be supplied to chemically treated water heaters and network water heaters, and the condensate formed in them is sent to condensate tanks, from where they are pumped out by condensate 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 can be sent directly to the deaerator head to replace an equivalent amount of heated chemically purified water.

Heaters of network and chemically treated water can be implemented as a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the condensate level in the heat exchanger is maintained by a level regulator, and then the condensate is sent to the water-water heat exchanger and it is cooled to a temperature 80-90 ^o C, while chemically purified or network water is first passed through a water-water heat exchanger, and then through steam and water.

A steam boiler room can be used as a steam generator, and return condensate from technological processes and a steam boiler room through pipelines is fed 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 , the content of silicon (SiO ₂₎ 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 directed to the drain of the distributor comb condensate fed sequentially from a tank- a toy tank and a collection tank of pure condensate separated from oil products, and as the condensate floats up onto 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 an oil 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 in three stages de-oiling, to clarification filters loaded with anthracite, in which 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, connected in parallel and loaded with 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, then de-oil condensate with a temperature of 85 ^o C is sent to the annular space of the heat exchangers, through which the cold raw water used for the technological needs of chemical water purification is lowered 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 desalination plant, and the temperature of the oil-free condensate is maintained in the range of 35 ^o C 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 with bed height of 1.5 m and the load rates filtering at 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% solution of sulfuric acid, after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which filter material using highly basic anion exchange resin AB-17-8 and conduct removal of silicic acid compounds from the condensate, and periodically restore the exchange capacity of the anion filter by passing through a filtering layer of anion exchange resin 3-5% sodium hydroxide solution, and after anion exchange filters purified condensate with a content of silicic acid 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 total hardness - not higher than 10 mg / kg are sent to the condensate reserve tank, from where they are pumped mainly to a thermal power plant (CHP) and a steam boiler room, as well as to a sulfur production unit and waste heat boilers moreover, for corrective treatment of desalted con Densate to a pH value of 8.5–9.5 and a reduction in the corrosion of the metal in the pipelines, a 1% ammonia solution is dosed into the collector by metering pumps.

The clarification filters used in condensate cleaning can be double chamber, consisting of a housing and a lower and upper drainage switchgear, and a blind flat horizontal partition dividing it into two chambers and tubular anchors are connected rigidly inside the housing, and air is removed from the lower chamber in the upper and maintaining the total pressure in the chambers, while the upper drainage distribution device is in the form of a funnel for uniform distribution of ndensate 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 when filling the filter with filter material, it is first placed 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 with slotted holes 0.25-0.4 mm wide are attached, 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 to 6 mm — are used as sorption filters of the first stage; moreover, the filters are equipped with upper and lower distribution devices, the upper of which is made in in the form of beams 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, which is parallel to the bottom and in which distribution pipes are inserted with holes along the lower generatrix with a diameter of 8 mm, overlapped by a weldable trough 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, 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} ; hydrogen-cation exchange and anion exchange filters are made in the form of single-chamber cylindrical apparatuses having a capacity of 115 m ³ / h, each of which 2.6 m in diameter is equipped with upper and lower manholes, fittings for hydroloading and upper and lower switchgears, the upper of which are in the form of a “glass in a glass”, and the lower one in the form of a collector into which the distribution tubes are inserted — rays with holes along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.

 In the case of the formation of a slit hole at the weld point of the trough plate to prevent entrainment of the filter material, a litter layer of coarse anthracite is poured onto the lower distribution device of the sorption filters over the entire surface of the filter 10 cm high.

 The technical result provided by the invention consists in increasing the yield of the resulting product and reducing its cost due to the fact that the technologically necessary energy costs obtained and used by traditional methods are reduced by 50% by the use of the invention, i.e. using steam generated by burning extraneous energy at an external thermal power plant (natural gas, fuel oil), which leads to an increase in the output per unit of consumed traditional energy due to the rational production of steam directly in the production of light oil products due to the possibility of reducing the consumption of chemically purified water for supplying the steam generator by returning condensate to the steam generator required at various technological stages, using heat outgoing processing flow and reduce flaring fuel gas, which further improves the ecological environment. The quality of petroleum products also increases by reducing the sulfur content from 1 wt.% To 0.05 wt.% While increasing their yield.

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 (AVT) distillation. The resulting gasoline fraction is sent to the stabilization unit. The stable gasoline fraction is subjected to secondary distillation. The gasoline fraction of 85-180 ^o C served on the hydrotreatment unit. Hydrotreated gasoline fraction is sent to the reforming unit. The target product is obtained by compounding the reforming product and various products (straight-run gasoline fraction, fraction of the secondary distillation of gasoline, gas separation). The kerosene fraction is sent to the hydrotreatment unit and then to the jet fuel production unit, which is diverted to the mixing unit with additives. Part of the diesel fraction is fed to the alkalization and sludge unit. Part of the straight-run kerosene fraction is also sent here. The main stream of the diesel fraction is directed to a hydrotreatment unit to reduce the sulfur content from 1 wt.% To 0.05 wt.%. Target diesel fuel is obtained by compounding diesel hydrotreated and straight-run diesel fractions after alkalization.

 Associated gas contained in the feedstock and fuel-technological gas generated during thermal and thermo-destructive technological processes of oil refining and intermediate products during oil distillation are used for steam production in hydrotreating and reforming processes.

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.

 Moreover, to conduct at least part of the technological processes, raw water is used from a flowing and / or non-flowing reservoir. The heating of chemically purified water, carried out by taking the heat of the return steam condensate, is carried out before or after the purification of raw water from suspensions and after cleaning the return steam condensate from oil pollution.

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 (Ca ⁺² ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and oxidizability permanganate 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 pumped water through two heat exchangers with fixed tube sheets and heat water at a temperature of 25-30 ^o C, moreover, at least one heat exchanger uses return 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 heat exchanger is controlled before cooling the condensate 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 with a heating water temperature corresponding to ai with the season. After heating, the water is sent for filtering to mechanical filters with a 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, then the clarified water is fed to hydrogen-cation exchange filters with a "hungry" regeneration loaded with sulfonated coal and they remove hardness salts from water to 1-2 mEq / kg constant and destroy the bicarbonate ion with a decrease in carbonate alkalinity to 0.7 mEq / kg and ion exchange of hardness, alkalinity, water, and chemical reactions with a hydrogen cation of sulfonated coal, after which softened water is fed to self-regulating buffer filters loaded with sulfonated carbon that protect the filtrate from acid leakage, then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and air is separated from carbon dioxide with gas that is taken into the atmosphere, decarbonized water is directed by gravity into the tank, after which this water is pumped through the pumps with two-stage sodium cation exchanger filters in the filters of the first stage remove stiffness cations up to 0.1 mEq / kg, and in the second stage carry out a deeper removal of stiffness cations (Ca ⁺² , Mg ⁺² ) up to 0.01 mEq / kg s obtaining 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 value of 8.0, after which chemically purified water is fed into tanks and then pumped into the steam boiler room with pumps.

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 lime dough , with a capacity of 100 m ³ , cells of lime milk with a capacity of 60 m ³ and metering pumps and / or centrifugal pumps with additional control valves, and the chemical treatment of water is carried out only using sodium cation exchange resin new filters, which also carry out the regeneration of the filter material with a saline solution with a concentration of 6-8%.

For chemical water treatment, mechanical filters are used in the form of cylindrical vessels with an internal anticorrosive coating, mainly of epoxy resin, with two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device in the form of beams made of polymer material for distribution of water are placed along 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, covered 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, while on the filter housing slotted tubes have a fitting for hydroloading, feed water pipes, loosening, air vents of the upper and lower drainage systems to the filter, pressure gauges at the inlet and outlet of the collector, samplers and valves are connected, and the filter filling is performed in two layers Consisting of a 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 preparation and 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 ; 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; 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; the used decarbonizer is filled with Rashig rings and is performed with the lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to the 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 loaded with filter material with a layer height of 1900 mm to replace the cations Ca ⁺² , Mg ⁺² by 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 made 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 distribution device, the filtration rate is not less than 34 m / h and stiffness cations (Ca ⁺² , Mg ⁺² ) are removed to 0.01 mEq / kg, and a base layer is placed in all ion-exchange filters for chemical water treatment on the lower drainage device anthracite higher than th level of the location of the rays with perforation of at least 10 cm.

Chemically purified water is 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 wherein a heat of the steam condensate originating from the enterprise settings, leaving the water cooler is divided into two streams, one of which is heated to 90 ^o C, is fed into the head of the deaerator, and the other serves to cool continuous purge spruce using the heat of purge water from the continuous purge separator, and then chemically purified water is passed through a deaerator vapor cooler, then it is fed to the deaerator head and steam is bubbled through chemically purified water, heating it to a temperature close to saturation, and removed from water, gases O ₂ , CO ₂ , and network heating water is supplied to the network pumps, then through the network water heaters to the enterprise heating network, while repairing chemically treated water heaters, They switch the network water heaters to the heating of chemically purified water.

Steam from the steam generator through the collectors is fed into 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, and to heat the fuel separator gas and deaerators.

 In the presence of excess spent steam at the enterprise, part of the steam is supplied to chemically treated water heaters and network water heaters, and the condensate formed in them is sent to condensate tanks, from where they are pumped out by condensate 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.

Heaters of network and chemically treated water are implemented as a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the condensate level in the heat exchanger is maintained by a level regulator, and then the condensate is sent to the water-water heat exchanger and it is supercooled to a temperature of 80 -90 ^o C, while chemically purified or network water is first passed through a water-water heat exchanger, and then through steam and water.

Production (return) condensate from technological processes and a steam boiler house through pipelines is fed to a distribution comb, and condensate with a total hardness of 100 mEq / kg, Fe content in terms of Fe ⁺³ to 180 mg / kg, and silicon content (SiO ₂ ) up to 350 mg / kg, an oil content of up to 80 mg / kg and a pH value of up to 8.0, moreover, if the condensate does not match the specified parameters, it is sent to the drain, from the distribution comb, the condensate is sent sequentially to the settling tank and the collection tank of the oil that has remained tons of pure condensate, and as the condensate floats up onto 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 with the help of pumps is fed through the control unit, in which the flows are distributed for technological processing and loosening of filters of three stages of de-oiling, for clarification filters, filling charged 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, connected in parallel and loaded with activated carbon, and then to four sorption filters of the second stage of decontamination of condensate to the oil content in it is not more than 0.05 mg / kg, then the oil-free condensate with a temperature of 85 ^o C is sent to the annulus of the heat exchangers through which cold raw water used for t 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 from 35 ^o C to 40 ^o C and directed first, into hydrogen-cation exchange filters, in which KU-2.8 highly basic cation exchange resin with a loading layer height of 1.5 m and a filtration rate of 35 m / h is used as a filter material, in which they hold the formation of stiffness cations and iron, moreover, periodically restore the exchange ability of the filters by regenerating the filter material with a 3-4% solution of sulfuric acid, 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 the filter material and carry out the removal of silicic acid compounds from the condensate, and periodically restore the exchange capacity of the anion exchange filters by passing through a filter a layer of anion exchange resin of 3-5% sodium hydroxide solution, and after anion exchange filters, purified condensate with a content of silicic acid not more than 150 mg / kg, iron (in terms of Fe ⁺³ ) not more than 100 mg / kg, oil products - not more than 0, 5 mg / kg and a total hardness of not higher than 10 mg / kg are sent to the condensate storage tank, from where they are pumped mainly to a thermal power station and a steam boiler room, as well as to a sulfur production unit and waste heat boilers, moreover, for correcting the treatment of desalted condensate to pH = 8.5-9.5 and reduce metal corrosion pipelines to the collector are dosed 1% ammonia solution by metering pumps.

When cleaning the condensate, clarification filters are used, made by two-chamber, consisting of a housing and a lower and upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and tubular anchors are connected rigidly inside the casing, through which air is removed from the lower chamber in the upper and maintaining the total pressure in the chambers, while the upper drainage distribution device is in the form of a funnel for uniform distribution of condens 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 when filling the filter with filter material, it is first placed 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 with slotted holes 0.25-0.4 mm wide are attached, which are closed with perforated plates to prevent entrainment of the filter material. Four single-chamber filters are used as sorption filters of the first stage, which are connected in parallel and loaded with filter material - activated carbon with a layer thickness of 2.5 m and a grain size of 2 to 6 mm. Filters are equipped with upper and lower distribution devices, the upper of which is made in the form of beams 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, which is parallel to the bottom and into which distribution pipes with holes are inserted along the lower forming diameter 8 mm, which is covered with a weldable trough 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 K 100, 65, 200, SUKHLU with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} . Hydrogen-cation exchange and anion exchange filters are made 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 are in the form of a “glass in a glass”, and the lower one in the form of a collector into which the distribution tubes are inserted — rays with holes along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.

 In the case of the formation of a slit hole at the weld point of the trough plate to prevent entrainment of the filter material, a litter layer of coarse anthracite is poured onto the lower distribution device of the sorption filters over the entire surface of the filter 10 cm high.

 Thus, steam is supplied to the atmospheric column of the AT and ABT units, to the stripping sections (or stripping columns) of the main column K2 of these plants, to hydrotreat kerosene fractions, diesel fractions, gasoline fractions in the stripping column of hydrotreating units, as a heat carrier to maintain the required temperature of the bottom of the columns, in a section or in blocks for cleaning hydrocarbon gases from hydrogen sulfide, for spraying fuel in process furnaces, for vacuum-creating devices, stripping in a vacuum column, drives of some of those biological pumps.

 The cost of steam during the method is 50% of the cost of steam purchased outside the production of light petroleum products, which leads to a significant reduction in the cost of production and ensures the rational use of heat from the waste streams of processing, reduction of the amount of fuel gas flared and improvement of the environmental situation.

 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 for producing light petroleum products according to the invention allows to reduce energy consumption by traditional energy carriers by approximately 3 times per unit output of oil products and by approximately 2 times in cost terms by replacing the corresponding amount of traditional energy carriers (natural gas and fuel oil) with a previously useless flare process gas refining. In addition, the invention provides improved quality of petroleum products.

Claims (20)

1. A method for producing light oil products 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 mesh and / or mesh located in the electrohydrators in at least two electrode levels, tearing together 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 ascending flow rate of oil is 0.05 - 0.1 of a conventional path segment, which coincides with the average displacement vector of the oil flow in the zone of the greatest midship of the electric dehydrator, traversed by the flow per hour of movement with the average speed of the process of desalination, atmospheric and / or atmospheric-vacuum distillation of desalted oil using atmospheric distillation columns equipped with packages of cross-precision nozzles placed with altitude or altitude-angular displacement adequate to the temperature zones of vapor condensation, while at least a portion of the packets are placed in the condensation zone of the kerosene fraction 120-180 ^° C, and by distillation when oil is supplied to the columns through at least two pipes tangentially located in the column body in the supply zone provided with an internal cylindrical flow reflector, the diameter of which corresponds to the diameter of the column casing in the supply zone as (0.59 - 0.75): 1, with the extraction of a kerosene fraction, and the output of the kerosene fraction 140 - 240 ^o C is carried out in the altitude range of the column of atmospheric and / or atmospheric vacuum distillation, comprising 0.58 - 0.81 of the height of the column, counting from the bottom of the bottom, or exceeding, respectively, the lower and upper marks of the output range of the kerosene fraction by an amount equal to 0.37 - 0.53 of the height of the column relative to the axis of entry of the supply pipes oil in the feed zone of the column, and the separated kerosene fraction is divided into three streams with a volume ratio of the first stream: second stream: third stream, respectively (1.2 - 8.5): (12.8 - 15.5): (9 5 - 11.8), the output of the diesel fraction 240 - 350 ^o C or diesel fractions 240 - 300 ^o C and 300 - 350 ^o C is carried out in elevation Ohm interval of atmospheric and / or atmospheric vacuum distillation columns, amounting to 0.32 - 0.62 of the column height, counting from the bottom of the bottom, or exceeding the lower and upper marks of the output range by an amount equal to (0.06 - 0, 12) and (0.23 - 0.41) from the height of the column relative to the axis of entry of the oil supply pipes into the feed zone of the column, stabilization of gasoline fractions, secondary distillation of a portion of the stable gasoline fraction of distillation of desalted oil in an amount of 0.51 - 0.61 of the total the amount of fraction at which the boiling fractions are obtained in the temperature range of SC-85 ^o C, 85 - 180 ^o C and the residual, hydrotreating reactors hydrorefining gasoline and kerosene fractions in the presence of a catalyst, wherein the hydrotreating gasoline fraction 85 - 180 ^o C a part of it is passed through a hydrotreating reactor and another part in the amount of 0.4 - 0.6 of the total amount is passed through at least two hydrotreating reactors with selective variation of the flow in the latter, reforming the hydrotreated gasoline fraction in at least three reactors, at least the last of which has a deep radial introduction of the gas product mixture into the catalyst, and when hydrotreating the kerosene fraction in a mixture with the residual fraction of the secondary distillation taken in an amount of up to 30-35% of the initial kerosene fraction, a pre-prepared concentrate of the mixture of naphthenic acid additives is introduced into the hydrotreating product through a damper tank and ionol in an amount of 0.007 - 0.008 wt.% and a mass ratio of additives in their mixture (1.0 - 1.5): 2, alkalization of diesel fractions by treatment with caustic soda solution in the reactor fractionation and compounding, characterized in that the diesel fractions are additionally subjected to hydrotreating in at least electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, hydrotreating reactors and reforming reactors supply process heat, including using steam as a heat carrier , which, at least partially, is obtained by burning associated gas contained in the feedstock and / or fuel-technological gas released as a result of the thermal process ki of oil and / or thermo-destructive processes of oil refining and / or intermediate products: gasoline, kerosene, diesel fractions, which are fed into 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 not lower than 100 ^o C, 60 - 85% of the gas is burned in furnaces in technological processes, and 15 - 40% of the gas is burned in a steam generator with the formation of condensate, at least partially returned as a result of heat extraction, mainly during oil distillation processes, while in the quality of 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, and the residual heat of the steam processed in the technological processes of distillation is used to heat the chemically purified raw water and / or feed oil 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 in electric dehydrators with a spherical or spheroidal and / or ellipsoidal and / or ovoid and / or teardrop-shaped body and / or in a composite dehydrator with a cylindrical body and convex-curvilinear end sections, and / or toroidal shape, and / or in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically, and / or in the electric dehydrators, the longitudinal axis of the body, at least parts of They are oriented horizontally or at an angle to the horizon. 3. The method according to claim 1, characterized in that the oil is supplied to the atmospheric and / or atmospheric vacuum distillation columns through nozzles located at an angle of dilution of the points of intersection of the axes of the nozzles with the column body in the range of 30 - 180 ^° C with a one-sided tangential twist the feed stream, or the supply of oil to the atmospheric distillation column is carried out through nozzles, the axis and inner neck of one of which orient the flow of the supplied oil in the feed zone of the column directly to the intersection with a similar stream, fed through another nozzle mainly in the zone of 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 internal cylindrical reflector with a radial distance from the conditional contact point with the reflector body at a distance b satisfying condition _{b ≥ 0,25 (R k - R} o), where R _k - column radius zone power, R _o - radius of the reflector, wherein the cylindrical reflector area is set with the power ekstsen risitetom respect to the longitudinal axis of the column or cylindrical reflector operate with a variable radius of curvature in cross section, or cylindrical reflector column is connected with the housing an annular membrane flat and / or polygonal and / or curved and / or the combined cross-sectional configuration; regular packages of cross-precision nozzles are made of spatially deformed stainless steel sheet elements with overlapping temperature gradients of 2-8 ^° C over the height of the column and the vapor passage through them, 38 - 81% relative to the cross section of the column, or distillation into the atmospheric distillation column is carried out at a passage speed of vapors of the accelerated fractions of at least 1.0 - 1.7 m / s, and during secondary distillation, the condensation of gasoline vapors is carried out in condensate PAX air cooling. 4. The method according to claim 1, characterized in that during stabilization a gaseous fraction of HK-62 ^° C is obtained, which is subjected to purification from sulfur-containing impurities with a solution of monoethanolamine, followed by separation in a gas fractionation unit with the release of a gasoline component for compounding gasolines.  5. The method according to claim 1, characterized in that when hydrotreating a gasoline fraction, passed through at least two reactors, the latter are tied along the gas-vapor product mixture with the possibility of direct or reverse passage of the latter through the catalyst layers, or with the possibility of parallel or alternating separate operation of the gasoline fraction adequately for the specified volumes and degree of hydrotreating, or at least one hydrotreating reactor is used for hydrotreating, at least in the upper zone of which there is a layer the catalyst is loaded with a discrete and / or combined vapor-gas-permeable element made of an inert or corrosion-heat-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 gas-vapor product stream is greater than the cross-sectional area of the hydrotreating reactor, or when hydrotreating is used at least one hydrotreating reactor, in which the catalyst layer is poured with the slope of at least part of at least the upper surfaces, or during hydrotreating, use at least one hydrotreating reactor, 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 the reactor vessel, or during hydrotreating, use at least one hydrotreating reactor, in which the catalyst, at least in the upper part of the bulk array, is provided with inclusions of inert elements with aerohydraulic resistance less than at least equivalent in volume of the catalyst bed, or during hydrotreating, at least one hydrotreating reactor is used, in which elements with increased aerohydraulic permeability are made in the form of mesh and / or perforated cylindrical or multifaceted glasses or tubes, or at least one hydrotreating is used , one reactor, in which part of the aerohydraulically permeable elements is performed in the form of bulk inclusions of inert particles with a radius greater than the radius or reduced radius of the catalysis particles torus, or during hydrotreating, at least one reactor is used, in which at least part of the elements with increased aerohydraulic permeability are combined with a bulk core and a flexible or rigid mesh or perforated shell, or at least one hydrotreating reactor in which at least in the upper zone, at least part of the catalyst bed is mixed with larger particles of inert material, or at least one of them is used for hydrotreating a reactor in which the particle ratio is 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 a portion of the hydrotreating reactors are installed with a slope of the longitudinal axis relative to the horizon, or at least hydrotreating is used , a part of hydrotreating reactors with a horizontally oriented longitudinal axis, or during hydrotreating, at least one hydrotreating reactor is toroidal; if the amount of gasoline fraction subjected to hydrotreating exceeds the installed capacity of the catalytic reforming unit, an excess amount of hydrotreated gasoline fraction is sent for compounding to produce automobile gasolines, while hydrotreating reactors use aluminum-cobalt or aluminum-nickel-molybdenum, or zeolite-containing hydrotreating catalysts, or  6. The method according to claim 1, characterized in that when reforming at least one reforming unit, at least the last two reactors are tied in parallel along the steam-gas mixture, or at least one reforming reactor is used during reforming at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-gas-permeable element of an inert or corrosion-heat-resistant material or a combination of materials with similar properties, at least the surface of the catalyst layer along the path of the gas-vapor product stream is larger than the cross-sectional area of the reforming reactor, or at least one reforming reactor is used in the reforming, in which the catalyst layer is poured with at least part of at least the upper surface or, when reforming, at least one reforming reactor is used, in which at least the upper catalyst layer is poured with a conical and / or alternately broken and / or alternately curved, and / or with a combined slope from the central zone to the walls of the reactor vessel, or during reforming, at least one reforming reactor is used, in which the catalyst, at least in the upper part of the bulk array, is provided with inclusions of inert elements with aerohydraulic resistance lower than the equivalent the volume of the catalyst bed, or when reforming, at least one reforming reactor is used, in which elements with increased aerohydraulic permeability are in the form of mesh and / or perforated cylindrical or multifaceted cups or pipes, or when reforming, at least one reforming reactor is used, in which part of the aerohydraulically permeable elements is 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 at least one reforming reactor is used in reforming, in which at least part of the elements with enhanced aero-hydraulic transparency are combined with a bulk core and flexible or with a rigid retina or perforated shell, or during reforming, at least one reforming reactor is used, in which at least in the upper zone at least part of the catalyst layer is mixed with larger particles of an inert material, the ratio particles are preferably performed variable with a decrease in the percentage of inert particles in the direction of movement of the gas-steam product stream being reformed, or during reforming, at least a portion of the reforming reactors are set to of the longitudinal axis relative to the horizon, or when reforming, at least a part of the reactors with a horizontally oriented longitudinal axis is used, or when reforming, at least one reactor is toroidal, or when reforming into the steam-product mixture stream passed through the catalyst bed in the reactors of reforming, a solution of an organochlorine compound is periodically introduced, which restores the activity of the catalyst, while dichloroethane or trichloroethane is used as the organochlorine compound; om at least part of the reforming reactors used aljumoplatinovyh platinovorenievye catalysts or catalysts, or combinations thereof.  7. The method according to claim 1, characterized in that the treatment of the diesel fraction with sodium hydroxide solution is carried out in stages, while the first stage is carried out by injection through an injector installed outside the alkalization reactor with a volume ratio of diesel fraction and sodium hydroxide equal to 0.5 - 2.0 , the resulting mixture is introduced into the bottom layer of sodium hydroxide solution and the second stage is carried out using the mother liquor, consisting of a distributor equipped with a distribution pipe system, when filling with caustic soda solution the volume of ctor at 0.5 - 0.75 of its height and speed of introducing the diesel fraction into the solution layer equal to 0.6 - 7.9 m / s, compounding of the diesel fraction is carried out in one or two or three stages, with compounding at the first the stages are carried out either directly in the atmospheric and / or atmospheric vacuum distillation column by adding a straight-run kerosene fraction to the diesel fraction and / or in a process pipeline connecting the atmospheric and / or atmospheric vacuum distillation column to the alkalization reactor by feeding it to the pipe harnessing the second stream of straight-run kerosene fraction, compounding in the second stage is carried out after alkalization of the diesel fraction directly in the diesel fuel storage tank by supplying straight-run and / or hydrotreated kerosene fraction under excess pressure, while 3.0 - 5.0% is used when alkalizing high-sulfur fractions caustic soda solution when feeding the diesel fraction in at least two reactors in parallel streams, or when alkalizing, use at least one reactor with a diesel feed fraction of the fraction through an external injector, the output nozzle of which is installed with a negative difference in the height of the nozzle to a height of at least 1 m relative to the lower mark of the alkaline solution in the alkalization reactor, or when alkalizing, use at least one reactor with distribution pipes supplying the diesel fraction placed at a height of 0.05 - 0.75 of the height of the sodium hydroxide solution, while the diesel fraction cleaned in the alkalization reactor is fed to at least one settling tank, it is kept there for at least 50 - 80 minutes and sent for compounding, or when alkalizing, use at least one alkalizing reactor, the perforation in the mother liquor distribution pipes is performed at least partially in the form of round-cylindrical and / or ovoid, and / or combined configurations, or slit-like openings, or, when alkalizing, at least one reactor is used in which the perforations in the mother liquor distribution pipes are made with a variable pitch and / or diameter, and / or with an effective flow area with an increase in the above parameters as the distance from the input zone of the dispensing manifold into the alkalization tank is adequate to a drop in hydraulic pressure in the elements of the diesel distillate input system, or when alkalizing, at least one reactor is used in which at least part of the perforation holes are oriented by the outflow axes flow along the sides of the horizon, or when alkalizing, use at least one reactor in which at least part of the perforation holes of the distribution pipes oriented at a downward angle to the horizontal, or alkalization using at least one reactor, wherein at least a portion of perforations disposed in a spiral with a constant or variable pitch; while alkalizing, the supply of the mixture of diesel fraction with alkali solution to the alkalization reactor is carried out by pulses, or when alkalizing, at least one reactor is used, in which the mother liquor distributor is made in the form of a pipe of variable cross-section along the length of the alkalization reactor, and the supply of the mixture of diesel fraction and alkali solution into the alkalization reactor are conducted at a variable speed in different zones of the reactors, or when alkalizing, at least one alkalizing reactor is used, fluctuation of the height of the liquid layer in which, during the input and output of the diesel fraction, they are kept within 16 - 20% of the initial level of sodium hydroxide solution in the reactor by the time the alkalization process begins, or when alkalizing, at least one alkalizing reactor is used, which is horizontal with a circular cylinder, or ellipsoidal, or ovoidal or teardrop-shaped cross-section, or when alkalizing, use at least one alkalizing reactor, which is performed with a broken or curved axis in plan or toroidal in de closed or open torus, or when alkalizing use at least one reactor, which is performed with an inclination to the horizon or at least one fracture of the longitudinal axis in the vertical plane, or when alkalizing use at least one reactor, which provide a screen that is horizontally oriented or inclined, open from at least one end, immersed within the upper third in the alkalized fraction.  8. The method according to any one of claims 1 to 7, characterized in that after alkalizing the alkali-treated solution, the diesel fraction is removed from the upper zone of the alkalization reactor and subjected to water washing, and / or sludge in a tank for water washing, and / or in the tank at the same time, with one washing and / or settling, at least one additional settling tank is used in series with the first, or at settling, at least one settling tank is used, which is horizontally or hollowly inclined with a circle with a globular-cylindrical or ellipsoidal cross-section, or with sludge, at least one sump tank is used that performs with a broken or curved axis in plan, or toroidal in the form of a closed or open torus, or with sludge, at least one sump tank, which is equipped with a baffle screen, open from one end and immersed in the surface layer of the diesel fraction, horizontally oriented, or inclined, and / or vertical, or at sludge use least one settling tank which is provided with at least two pairs of electrodes, intensifying deposition slurries and impurities from the diesel fraction.  9. The method according to claim 1, characterized in that the compounding in the process pipeline of the kerosene fraction and / or vacuum solarium is carried out in stages or discretely through at least two pipes cut into the main pipe from different sides and / or spaced apart and oriented at an acute angle along the miscible fractions, or when compounding, use the input pipes of components miscible with the diesel fraction located in the pipeline and providing unidirectional or opposite direction tangentially in the boiling twist of the mixed flows, or when compounding in the pipeline in its internal section in the area immediately after the nozzle supply zone supplying kerosene and / or vacuum-solar components mixed with the diesel fraction, install at least one fixed impeller, or when compounding in the pipe in the internal at least two impellers with a counter-directional swirl of the blades fixed relative to the pipeline body or fixedly fixed one relative to the other with the possibility of free joint rotation when an imbalance occurs, they create vortex countercurrents that intensify the process of compounding the diesel fraction, and when the diesel fraction is removed from the column of atmospheric and / or atmospheric-vacuum distillation, the selection of excess resulting heat is carried out mainly before the start of the first stage of compounding , the second compounding stage is carried out in a diesel fuel storage tank by direct mixing of feed a reservoir of flows of the diesel fraction and the kerosene fraction, either through an injector introduced into the bottom zone of the tank with a separate supply of diesel fraction and kerosene fraction in time, or in the second compounding stage, an injector is used, which is introduced into the tank and fixed on a rigid inner pipe in the lower third of the central areas of the tank with an upward slope of the injected stream, or in the first stage of compounding, vacuum salt is added to the diesel fraction and / or its mixture with straight-run kerosene fraction p outputted from vacuum column atmospheric-vacuum distillation; in the second stage of compounding, a reservoir or injector is introduced into which the tangentially installed nozzle is introduced, or compounding in the diesel fuel storage tank is carried out by means of at least two injectors fixed on the tangentially installed nozzles with counter flow swirling, or compounding in the diesel storage tank the fuel is carried out by means of at least two injectors movably with the possibility of jet rotation mounted in the bottom or bottom h STI tank.  10. The method according to any one of claims 1 to 9, characterized in that raw water is used 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. 11. The method according to any one of claims 1 to 10, 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 tubular grids and heat the 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 controlled until the condensate cools down to temperature 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 heat-transfer water having a heating temperature in this heat exchanger 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 transparency reaches at least 40 cm, then the clarified water is fed to hydrogen-cation exchange filters loaded sulfonated carbon 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 carbonate alkalinity to 0.7 mEq / kg, after which softened water is supplied to Buffer self-regulating filters, which are loaded with sulfonated coal, protecting the filtrate from acidity slippage, 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 pumps are pumped through two-stage sodium-cation exchange filters, in the filters of the first stage, hardness cations are removed to 0.1 mEq / kg, and in the second stage to 0.01 mEq / kg to obtain 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 to 300 mg / kg and a pH value of 8.0 then chemically purified water is supplied to the tanks, and then pumped into the steam generator by pumps. 12. The method according to claim 11, characterized in that, at least 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 dampers, and chemical treatment in s is carried out using only sodium cation filters, which also conduct regeneration of the filter material with the concentration of brine 6 - 8%. 13. The method according to any one of paragraphs.11 and 12, characterized in that in 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 there is a fitting feed water supply and an upper distribution device 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 blowing 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 inspecting the surface of the filter material, and in the lower part 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, 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, 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 consumption for own needs and preparation 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 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 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, while the filter performance is at least 90 m ³ / h, and the filtering speed is not less than 25 m / h, and the second stage of the filter is made of two filters with a diameter of 2600 mm, loaded with filter material with a layer height of 1200 mm, while the filtering speed is not less than 34 m / h, and in this case, in all ion-exchange filters for chemical water purification, an anthracite layer with a height exceeding the level of the arrangement of beams with perforation by at least 10 cm is located on the lower drainage device. 14. The method according to any one of paragraphs.11 to 13, characterized in that chemically purified water is supplied to a steam generator with a temperature of 25-30 ^° C, and part of the chemically purified water is sent to sampling coolers for continuous and periodic blowing of boilers, and from there to deaerator head, another portion of the chemically treated water fed to gravity condensate cooler, which uses the heat of the steam condensate 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 serves n continuous purge cooler using the heat of purge water from a continuous purge separator, 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 removed from water Gases O ₂ , CO ₂ , network heating water is fed to the input of the network pumps, and then through the network water heaters to the heating network, while repairing chemically purified water heaters They switch the network water heaters to the heating of chemically purified water. 15. The method according to any one of paragraphs.11 to 14, characterized in that the steam from the steam generator through the collectors is fed into 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.  16. The method according to any one of paragraphs.11 to 15, characterized in that in the presence of excess spent steam, part of the steam is fed to chemically treated water heaters and network water heaters, and the condensate formed in them is sent to condensate tanks, from where they are pumped out by condensate pumps to condensate cleaning. 17. The method according to clause 16, characterized in that when the chemically purified water heater and network water heaters are operated on a reduced steam from boilers, at least a portion of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head to replace an equivalent amount of chemically heated purified water. 18. The method according to clause 16, characterized in that the heaters of the network and chemically purified water are in the form of a block of steam and water and water heat exchangers, and first, steam is condensed in the steam and water heat exchanger, while the level of condensate in the heat exchanger is supported by a level regulator, and then the condensate is sent to water-water heat exchanger and supercool it to a temperature of 80 - 90 ^o C, while chemically purified or network water is passed through a water-water heat exchanger, and then through a steam-water one. 19. The method according to any one of paragraphs 10 and 11, characterized in that the steam boiler is used as a steam generator, and the return condensate from the technological processes and the steam boiler is piped to the distribution comb, and condensate with a total hardness of 100 mEq / kg, Fe content in terms of Fe ⁺³ up to 180 mg / kg, silicon content up to 350 mg / kg, oil content up to 80 mg / kg and pH up to 8.0, and if the condensate does not meet the specified parameters, it is sent to the drain, from distribution condenser comb t is sent sequentially to the sump tank and the 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 nozzles, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit through the control unit, in which the flows are distributed to the process unit and loosening the filters of three stages of de-oiling, to 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, connected in parallel and loaded with activated carbon, and then - into four sorption filter deoiling second stage condensate to the oils contained less than 0.05 mg / kg, then deoiled condensate at a temperature of 85 ^o C is sent to the tube pros of the space heat exchanger through which is passed the cold raw water used for the technological needs of the chemical treatment and cooling is condensate 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 the range of 35 - 40 ^o C and direct it first to hydrogen-cation exchange filters, in which the high-basic cation exchanger KU-2.8 with a high the load layer is 1.5 m and the filtration speed is 35 m / h, in which the cation of stiffness 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, after the hydrogen-cation exchange filters, the condensate is sent in anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as a filtering material, and silicic acid compounds are removed from the condensate, and Adding exchange capacity 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 total hardness not higher than 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 waste heat boilers, and for correcting the treatment of desalinated condensate ata pH to a value of 8.5 - 9.5 and to reduce corrosion of metal pipes in the manifold metered 1% ammonia solution dosing pumps. 20. The method according to claim 19, characterized in that the clarifying filters used in the condensate cleaning are double chamber, consisting of a housing and lower and upper drainage distribution devices, and a blind flat horizontal partition dividing it into two chambers is rigidly attached to the housing, and anchor tubular connections through which air is vented from the lower chamber to the upper and maintaining the total pressure in the chambers, while the upper drainage distribution device is in the form of a funnel for uniform distribution of condensate over 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 when filling the filter with filter material, it is first placed in the lower chamber, and then in the upper and lower switchgear are in the form of a collector to which thirty-two beams with slotted holes 0.25 - 0.4 mm wide are attached, which are closed with perforated plates to prevent filter entrainment -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 is in the form of a collector, which is parallel to the bottom and into which distribution pipes with openings along the lower generatrices with a diameter of 8 mm are blocked by a welded gutter-like plate with a slot 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} ; hydrogen-cation exchange and anion exchange filters are made in the form of single-chamber, having a capacity of 115 m ³ / h, cylindrical apparatuses, 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 into which distribution tubes are inserted — beams with holes along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.

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