RU2154086C1 - Diesel fuel production process - Google Patents

Abstract

FIELD: petroleum processing. SUBSTANCE: diesel fuel is prepared from low-sulfur and/or sulfur, and/or high-sulfur crude oils involving thermal and thermodestructive processes. Electrodesalting and dehydration of crude oil are carried out by passing crude oil flow through system of electrodes arranged in screen- or cellular manner in electrical dehydrators with differently oriented longitudinal casing axes. The thus treated crude oil is subjected to atmosphere and/or atmosphere and vacuum distillation, followed by hydrofining of diesel fractions and alkalization of a part of diesel fraction to be further compounded. Water steam generated in steam generator is used in the processes as heat carrier to form condensate, which at least partly is returned into steam-generation process. Steam is at least partly formed by superheating of water provided by combustion of associated gas releasing in thermal processing of crude oil and/or in thermodestructive petroleum processing. Gas is fed into gas network at temperature 50-70 C and pressure 3-5 kg/sq.cm and is further heated to temperature at least 100 C. 60-85% of gas is used for combustion to produce steam as heat carrier and 15-40% of gas is used for combustion in steam generator to recover steam from return steam condensate, which is supplemented by required amount of chemically purified crude water. Heat from gas combustion is also used to preheat chemically purified crude water and/or original crude oil. Simultaneously, residual heat of waste steam and/or steam condensate is recuperated. In the crude oil distillation stage, use of rectification columns provided with packets of crossing-point fillings is preferred. Hydrofining of diesel fuel involves use of alumino-cobalt and alumino-molybdenum catalysts. Alkalization of diesel fractions is accomplished with 3-5-% sodium hydroxide aqueous solution at diesel fraction-to-alkali solution volume ratio from 0.5: 1 to 2.0: 1. Diesel fraction is advantageously compounded with straight-run kerosene fraction and/or straight-run vacuum straw oil components. EFFECT: increased economical efficiency of process. 25 cl, 1 tbl

Description

 The invention relates to oil refining, specifically to the production of diesel fuel from oils with different sulfur contents.

 Closest to the invention in its essence and the achieved result is a method for producing diesel fuel from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of oil by passing a stream through an electrode system in electro-dehydrators, atmospheric and / or atmospheric-vacuum distillation of demineralized oil in distillation columns, hydrotreating of diesel fractions, alkalization of a portion of the obtained diesel fractions followed by compounding of the fractions with feeding, at least, to electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, alkalization reactors as the heat carrier of the steam obtained in the steam generator, and the formation of condensate, at least partially returning, as a result of selection heat mainly during technological processes of oil distillation (see Erich V.N., Rasina MG, Rudin MG, Chemistry and technology of oil and gas, L., Chemistry, 1985, p. 385-398).

 The disadvantages of the known methods are the high cost due to the need to purchase the required external steam in a number of technological processes, as well as large heat losses due to the burning of a significant amount of fuel gas in a flare, which additionally leads to environmental degradation in the region.

 The objective of the present invention is to increase the efficiency and at the same time deeper refining of oil, increasing the yield and improving the environmental situation in the region.

The problem is solved due to the fact that in the method for producing diesel fuel from low-sulfur, and / or sulfur, and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of oil by passing a stream through an electrode system in electric dehydrators, atmospheric and / or atmospheric vacuum distillation of desalted oil in distillation columns, hydrotreating of diesel fractions, alkalization of part of the obtained diesel fractions, followed by compounding of fractions with at least to electric dehydrators, atmospheric and / or atmospheric vacuum distillation columns, alkalization reactors as a heat carrier for the steam obtained in the steam generator, and the formation of condensate, at least partially returning, as a result of heat extraction, mainly during technological processes distillation of oil, according to the invention, the steam used in technological processes is at least partially obtained by burning associated gas and / or process gas contained in oil thermal processes and / or thermo-destructive processes and / or intermediate products, which are supplied to the network with a temperature of 50-70 ^o C and a pressure of 3-5 kg / cm, are heated to a temperature not lower than 100 ^o C and 60-85% are fed to combustion to produce steam in technological processes, and 15-40% of the gas is fed to combustion in a steam generator to produce steam by heating the return steam condensate with the addition of heated chemically purified raw water in the amount necessary to compensate for non-returnable condensate and to heat the chemically purified cheese water and / or source oil, use the residual heat of the steam and / or steam condensate spent in the technological processes of distillation of oil.

In this case, oil electrodesalting can be carried out by passing a stream through a system of mesh and / or mesh electrodes located in at least two levels of electrodes, which together cover the altitude range of the electric dehydrator, mainly in the upper half of the height of its casing, and the height gradient between the electrode levels in the path of the upward oil flow is 0.05-0.1 conditional length of the path, which coincides with the average displacement vector of the oil flow in the zone of the largest midship of the electric dehydrator, traveled by the stream per hour moving at an average speed elektroobessolivaniya and dehydration process, the dehydration and elektroobessolivanie oil electrical dehydrators is carried out in a horizontally-oriented cylindrical housing or an integral configuration and a working volume of 80-200 m ^3, or the housing in electrical dehydrators spherical or spheroidal and / or ellipsoidal , and / or ovoid and / or teardrop-shaped, or electrodesalting of oil is carried out in electrodehydrators of a spheroidal and / or ellipsoidal and / or ovoidal and / or ka pleural, and / or composite with a cylindrical body and convex curvilinear end sections, and / or toroidal shape, or electric desalting of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically, or horizontally, or at an angle to the horizontal.

At distillation of desalted and dehydrated oil, atmospheric and / or atmospheric vacuum distillation columns can be used, which provide packages of cross-precision nozzles placed with a vertical or vertical-angular displacement adequate to the temperature zones of vapor condensation, while at least some of the packages are placed in the condensation zone of the diesel fraction and distillation is carried out when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the supply zone provided with an internal a cylindrical flow reflector, the diameter of which correlates with the diameter of the column body in the feed zone as (0.59-0.75): 1, and the altitude range for introducing oil flows is (0.21-0.28) of the column height from the bottom of the column bottom while feeding oil in an atmospheric tower and / or atmospheric and vacuum distillation is carried out through the nozzles, are arranged at an angle dilution points of intersection with the axes of the nozzles of the column body in the range from 30-180 ^o sided tangential swirling feed stream or flow of oil into the column atmospheres Oh and / or atmospheric vacuum distillation is carried out through the nozzles, the axis and the inner neck of one of which orient the flow of oil supplied through it in the feed zone of the column directly to the intersection with a similar stream supplied through another nozzle mainly in the zone of exit from the inner neck of the latter, or oil is supplied to the atmospheric and / or atmospheric vacuum distillation column through nozzles, the axes of which are oriented parallel to the tangent to the body of the internal cylindrical reflection at a distance b satisfying the condition b ≥ 0.25 (R _к - R _о ), where R _к is the radius of the column in the feed zone, R _о is the radius of the reflector, oil is introduced into the column through nozzles cut into the column body in parallel with the dilution of their axes at a distance of 0.5-0.85 of the diameter of the column in the feed zone, and distillation is carried out in the column, a cylindrical reflector in the feed zone of which is set to an eccentric longitudinal axis of the column, or distillation is carried out in the column atmospheric and / or atmospheric o-vacuum distillation, the cylindrical reflector of which is carried out with a variable radius of curvature in cross section, or the distillation is carried out in an atmospheric distillation column, the cylindrical reflector of which is connected to the column body of a circular, membrane, and / or broken, and / or curved, and / or a combined configuration in cross section, or distillation is carried out in a column whose oil flow reflector is made in the form of a two-leaf symmetrical shell of variable curvature or a composite configuration, according to At least in cross-section or during distillation, an atmospheric distillation column is used, in which packets of cross-precision nozzles are regularly made of spatially deformed stainless steel sheet elements, ensuring that the height of the packets of temperature gradients 2-8-C is overlapped by column height and area the passage of vapors through them, comprising 38-81% relative to the cross section of the column, while distillation in the column of atmospheric and / or atmospheric vacuum distillation is carried out at a vapor velocity of of combustible fractions of at least 1.0-1.7 m / s, and the output of a diesel fraction with a boiling point of 240-350 ^o C or a separated diesel fraction of 240-300 ^o C and 300-350 ^o C are in the altitude range primary distillation columns, constituting (0.32-0.62), counting from the bottom of the column or exceeding, respectively, the lower mark and the upper mark of the output range by (0.06-0.12) and (0.23-0, 41) from the height of the column relative to the axis of entry of the nozzles supplying oil to the feed zone of the column.

 Hydrotreating can be carried out in a hydrogen-containing gas medium in the presence of hydrotreating catalysts, while the gas-feed stream is introduced predominantly axially.

 When hydrotreating a diesel fraction, passed through one or two reactors, the latter or the latter can be tied along the gas-steam 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 operation adequately to the specified volumes and degree of gasoline hydrotreating fractions.

 Hydrotreating reactors may use cobalt-aluminum or nickel-aluminum-molybdenum hydrotreating catalysts, or combinations thereof.

 At least one hydrotreating reactor can be used, at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-permeable element of an inert or corrosion-resistant material, or a combination of materials with similar properties, at least , the input surface of the catalyst layer on the path of the gas-vapor flow is performed exceeding the cross-sectional area of the hydrotreatment reactor.

 In hydrotreating, at least one reactor may be used in which a catalyst layer is poured with the slope of at least a portion of at least the upper surface.

 During hydrotreating, at least one reactor can be 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 .

 Hydrotreating can use at least one 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 that of a catalyst layer equivalent in volume.

 During hydrotreating, at least one reactor can be used in which elements with increased aero-hydraulic permeability are made in the form of mesh and / or perforated cylindrical or polyhedral glasses or nozzles.

 When hydrotreating, at least one reactor can be 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.

 When hydrotreating, at least one reactor can be 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.

 In hydrotreating, at least one reactor can be used in which at least in the upper zone at least part of the catalyst bed is mixed with larger particles of inert material.

 When hydrotreating, at least one reactor can be used in which the particle ratio is variable with decreasing percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreating.

 During hydrotreating, at least a portion of the hydrotreating reactors can be installed with a slope of the longitudinal axis relative to the horizon.

 In hydrotreating, at least part of the hydrotreating reactors with a horizontally oriented longitudinal axis can be used.

 In hydrotreating, at least one hydrotreating reactor can be toroidal.

 When alkalizing, a 3-5% sodium hydroxide solution can be used with the diesel fraction supplied to the at least two reactors in parallel flows, the diesel fraction is treated with sodium hydroxide in stages, while the first stage is carried out by injection through an injector installed outside the alkalization reactor at a volume ratio diesel fraction and caustic soda equal to 0.5-2.0, and the resulting mixture is introduced into the bottom layer of a solution of caustic soda, and carry out the second stage of mixing using the mother liquor, consisting of a distribution the second collector, equipped with a distribution pipe system with a selective perforation system, when the caustic soda solution is filled with the reactor volume at 0.5-0.75 of its height and the rate of introduction of the diesel fraction into the solution layer equal to 0.6-7.9 m / s, compounding carried out in one, two or three stages, while alkalizing high-sulfur fractions, use a solution of 3.0-5.0% sodium hydroxide solution when supplying a diesel fraction to at least two reactors in parallel streams, or use a reactor with a diesel fraction supplied to the 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 level of the alkaline solution in the alkalization reactor, or when alkalizing, a reactor with distribution pipes supplying a diesel fraction placed at a height of 0.05-0.75 from a height is used sodium hydroxide solution, or when alkalizing, a reactor is used in which the perforation holes in the mother liquor distribution pipes are made with a variable pitch and / or diameter and / or effective flow area with by the growth of 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, a reactor is used in which at least part of the perforation holes are oriented to the flow outflow axis along the sides of the horizon, or when alkalizing, a reactor is used in which at least part of the perforation openings of the distribution pipes are oriented at downward angles of the horizon or, when alkalizing, a reactor is used in which at least a part of the perforations is arranged in a spiral with constant or variable pitch, and at least part of the perforations in the distribution pipes of the mother liquor are circular cylindrical and / or ovoidal and / or combined configurations, either slit-like or when alkalizing, use a reactor 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 a diesel mixture fraction and alkali solution into the alkalization reactor are carried out with variable speed in different zones of the reactors, or when alkalizing, at least one alkalization reactor is used, the oscillation of the height of the liquid layer in which during input / output of the diesel fraction is carried out within 16-20% of the initial level of sodium hydroxide solution in the reactor at the time the alkalization process begins, or when alkalizing, at least one alkalizing reactor is used, which is horizontal with a cylindrical or ellipsoidal, and whether an ovoid or teardrop-shaped cross-section, or when alkalizing, use at least one alkalization reactor, which is made by a broken or curved axis in plan or toroidal in the form of a closed or open torus, or when alkalizing, use at least one reactor, which 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 is provided with a screen, horizontally oriented or inclined, open from at least one end, immersed within the upper third in the alkalized fraction, when alkalizing, use at least one reactor and / or settling tank, which is performed with a larger cross-section axis oriented vertically or obliquely, while the mixture of the diesel fraction with the alkali solution is supplied to the alkalization reactor by pulses, and after alkalization, the diesel fraction treated with the alkali solution is removed from the upper zone of the alkalization reactor and subjected to bottom washing, and / or sludge in the tank for water washing, and / or in the settling tank, while using water washing and / or sludge, use at least one additional settling tank in series with the first, and when settling, use at least one settling tank that is horizontally or hollowly inclined with a circular cylindrical or ellipsoidal cross-section, or at least one settling tank that is made with a broken or curved axis in plan, or roidal in the form of a closed or open torus, or in case of sedimentation, at least one settling tank is used, which is equipped with a partition screen open from one end, and immersed in the surface layer of the diesel fraction, horizontally oriented, or inclined, and / or at least one sedimentation tank is used vertically, or when it settles, which is equipped with at least two pairs of electrodes that intensify the deposition of suspensions and impurities from the diesel fraction, and cleaned in the alkalization reactor for zelnuyu fraction is fed into at least one settling tank, kept there for at least 50-80 min and passed to blending.

Compounding in the first stage can be carried out either directly in the atmospheric and / or atmospheric vacuum distillation column by adding at least part of the straight-run kerosene fraction to the diesel fraction, and / or in the process pipeline connecting the primary atmospheric and / or atmospheric vacuum column distillation with an alkalization reactor by feeding a straight-run kerosene fraction, compounding of the second stage is carried out after alkalization of the diesel fraction directly in the diesel storage tank fuel by supplying straight-run and / or hydrotreated kerosene fraction under excess pressure to the zone located in the lower quarter of the tank height, mainly with a jet inclined toward the tank bottom at an angle of at least 30 ^o to the horizontal, while compounding in the process pipeline supplies kerosene fractions and / or vacuum solarium are phased or discrete through at least two nozzles cut into the main pipeline from different sides and / or spaced along the length and oriented along acute angle along the mixed distillates, or when compounding, use nozzles for introducing components mixed to the diesel fraction, cut into the main pipeline and providing unidirectional or counter-directional tangential vortex swirl of the mixed flows, or when compounding in the pipeline in its internal section at the compounding section of the first stage immediately after the insertion zone of nozzles supplying kerosene and / or vacuum-solar lumps mixed with the diesel fraction onents install at least one fixed impeller, or when compounding in the pipeline in the internal section, install at least two impellers with counter-directional swirling of the blades, fixed relative to the pipeline body or fixedly fixed one relative to the other with the possibility of free joint rotation in case of imbalance created or vortex countercurrents intensifying the process of compounding the diesel distillate, and when the diesel fraction is withdrawn and from the atmospheric and / or atmospheric vacuum distillation column, the excess resulting heat is predominantly selected before the first compounding stage is started, the second compounding stage is carried out in the diesel fuel storage tank by directly mixing the flows of the diesel fraction and the kerosene fraction supplied to the tank, or through an injector introduced injected 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, injecto 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 solar oil is removed from the vacuum column atmospheric from the vacuum column and / or into its mixture with straight-run kerosene fraction -vacuum distillation; in the second stage of compounding, a reservoir is used, the injector in which is arranged 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 mounted 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 jet rotation mounted in the bottom or bottom second part diesel fuel storage tank.

 Can use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated before or after purification of the raw water from suspensions and after cleaning the return steam condensate from oil pollution.

They can use water, for example, 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 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 pump water through two heat exchangers with fixed tube sheets and 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 controlled until the condensation cools 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 then preheated water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters loaded with sulfonated coal and removed from water hardness salts up to 1-2 mEq / kg constant and destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg, after which softened water is fed to protect the filtrate from leakage acidity buffer self-regulating filters loaded with sulfonated charcoal, and then water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and air is separated with carbon dioxide, which is vented to the atmosphere, and decarbonized water is fed by gravity into the tank, after which this water is pumped they are pumped through two-stage sodium-cation exchange filters, and in the filters of the first stage, stiffness cations are removed to 0.1 mEq / kg, and in the second stage, they are removed hardness cations Ca ^+2, Mg ⁺² to 0.01 meq / kg to obtain chemically purified water transparency of at least 40 cm, total hardness of 2-5 mg-eq / kg, the content of iron in terms of Fe ⁺³ to 300 mg / kg and a pH value of 8.0, after which chemically purified water is supplied to the tanks, and then pumped into the steam generator, while at least during the flood period, preliminary water treatment is carried out using at least two clarifiers with a capacity of 250 m ³ / h, two lime milk mixers with a capacity of 15 m ³ each, two dregs coagulant for each 10 m ³ each, wet lime storage cells, mainly lime paste with a capacity of 100 m ³ , lime milk cells with a capacity of 60 m ³ and metering pumps and / or centrifugal pumps with additional control valves, and chemical water treatment is carried out only using sodium-cation exchange filters, in which the filter material is also regenerated with a saline solution with a concentration of 6-8%, and mechanical filters in the form of cylindrical vessels with internal anti-corrosion coating, mainly made of epoxy resin, with two spherical steel bottoms, in the upper of which there is a feed water supply fitting and an upper distribution device in the form of beams of polymer material for distributing water over the filter cross section, and on the lower bottom there is a drainage system in in the form of a collector with slotted tubes of stainless steel, along the axis of which holes are formed, overlapped by casings with slits 0.25-0.4 mm wide, and in the upper part of the filter housing is formed to inspect the surface of the filter material, and at the bottom - a hole for mounting and repairing the upper and lower drainage systems, while on the filter housing at the level of the slotted tubes there is a fitting for hydraulic overload, the piping of the source water, loosening, air duct of the upper and lower drainage are connected to the filter systems, pressure gauges at the inlet and outlet of the collector, samplers and valves are connected, and the filtering bed is double-layer, consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and an anthracite layer with a height of 500 mm and volume volume of 4.6 m ³ , while the performance of the filters is set taking into account the water flow for own needs and the preparation of regeneration solutions of at least 200 m / h, the filtering speed for all filters is at least 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 ² ; used hydrogen-cation exchange filters are performed 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, moreover, the filter is equipped with an upper distribution device 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 capacity is at least 80 t / h and the filtering speed is at least 13 m / h; the self-regulating buffer filters used are loaded with sulfonated coal with a loading layer height of 2000 mm and are made with a top 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 made with a lower air inlet pipe, a spray separator and a decarbonized water outlet 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, while the filter capacity 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, and the filter is equipped with a top Switchgear them, and filtration speed is at least 34 m / h, wherein all ion exchange filters, chemical treatment of water in the lower drainage unit a layer of anthracite height exceeding the level rays arrangement with perforations at least 10 cm.

Chemically purified water can be supplied to a steam generator with a temperature of 25-30 ^o C, and part of the chemically purified water is sent to the sampling coolers for continuous and periodic blowing of 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, and exiting the coolant water is separated into two streams, one of which is heated to 90 ^o C, is fed into the deaerator head, and the other is fed to a continuous purge cooler ispol'uet yn heat backwash water from a continuous purge of the separator, and then chemically purified water is passed through a vapor deaerator cooler, and then fed to the head of the deaerator and carried barbatirovanie chemically purified water steam, heating it to a temperature close to saturation, and removed from the water the gases O ₂ , CO ₂ , and the network heating water is supplied to the network pumps, then through the network water heaters to the heating network, while repairing chemically treated water heaters, the network heaters are switched water for heating chemically purified water.

Steam from the boilers through the collectors can be supplied to the steam pipelines, 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 the chemically purified water heater, to the fuel gas heater, to heat the fuel gas separator and in deaerators; in the presence of excess spent steam, part of it is fed to heaters of chemically purified water and to network water heaters, and in them the condensate is sent to condenser tanks, from where they are pumped out by condenser pumps to clean the condensate; when the chemically treated water heater and network water heaters are operated on a reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head to replace an equivalent amount of chemically purified water heated, while the network and chemically purified water heaters perform in the form of a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the level of condensate in the heat exchanger is maintained with a level controller, and then the condensate is sent to a 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 a steam-water one, using a steam boiler room and a steam generator condensate in pipelines is fed to a distribution comb, wherein the condensate is used with a total hardness of 100 meq / kg, the content of Fe, based on Fe ⁺³ to 180 mg / kg, the content of silicic acid to 350 mg / kg, the content of m of oils up to 80 mg / kg and a pH value of up to 8.0 units, and if the condensate does not match the specified parameters, it is sent to the drainage, and from the distribution comb, the condensate is sent sequentially to the settling tank and the collection tank of pure condensate separated from the oil products, and as when condensate settles to the surface of the oil, it is collected using a catching funnel, while both tanks maintain a predetermined volume of liquid due to the difference in the levels of overflow troughs - filling pipes, after which condensate with an oil content of 10-15 mg / kg is pumped through a control unit, in which the flows are distributed for technological processing and loosening of filters of three de-oiling levels, 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 in parallel, loaded with activated carbon, and then to four sorption filters of the second stage foam condensate de-oiling to an oil content of not more than 0.05 mg / kg, and oil-free condensate with a temperature of 85 ^o C is sent to the annulus of heat exchangers, through which cold raw water used for technological needs of chemical water treatment is passed, 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 oil-free condensate is maintained in the range of 35 ^o C to 40 ^o C and direct it first to hydrogen-cation exchange filters, in which KU-2.8 highly basic cation exchange resin with a loading layer height of 1.5 m and a filtration rate of 35 m / h are used as filter material, and periodically restoration of the exchange ability of the filters by regeneration of the filter material with a 3-4% solution of sulfuric acid, and after the hydrogen cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as the filter material They remove silicic acid compounds from the condensate, and periodically restore the exchange capacity of anion exchange filters by passing through a filter layer of anion exchange resin 3-5% sodium hydroxide solution, and after the anion exchange filters, purified condensate with silicic acid content of not more than 150 mg / kg, iron (in in terms of Fe ⁺³ ) not more than 100 mg / kg, oil products - not more than 0.5 mg / kg and with total hardness not more than 10 mg / kg sent to the condensate reserve tank, from where they are pumped to the CHPP and steam boiler room and to waste heat boilers insulators, and for correcting the treatment of desalted condensate to a pH of 8.5–9.5 units and reducing corrosion of the metal in the pipelines, a 1% ammonia solution is dosed into the collector by metering pumps.

The clarifying filters used in condensate cleaning can be performed by two-chamber ones, consisting of a housing, a lower and upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and tubular anchor pipes through which air is removed from the lower chamber is rigidly attached to the housing in the upper and maintaining in the chambers of general pressure, while the upper drainage distribution device is made in the form of a funnel for uniform distribution of densate 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 made 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; the thickness of the activated carbon layer of the filters of the first stage is 2.5 m with a grain size of 2 to 6 mm, and the 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 switchgear - in the form of a collector, which is parallel to the bottom and into which the distribution pipes are inserted with holes along the lower generatrix with a diameter of 8 mm, overlapped by a trough with a slit 0.25-0.4 mm wide to prevent the ingress of activated carbon into the condensate; when supplying condensate to a desalination plant, for example, pumps of the K 100, 65, 200, SUKHLU brands 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 housing 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 is made in the form of a “glass in a glass”, and the lower one 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.

 The technical result provided by the given sets of features is to increase efficiency by reducing the need to purchase steam on the side and use in some technological processes of return condensate and steam of own production, the cost of which is lower than the cost of purchased on the side of steam to 50%, reducing the amount of burned by fuel gas flare and environmental improvement in the region.

 The method is as follows.

The original oil is sent to a block of electrodesalting and dehydration. Then it is fed to the atmospheric or atmospheric vacuum distillation unit, after which it is fed to the hydrotreating and / or alkalizing unit, from where the diesel fraction is fed to the compounding unit. Moreover, the steam used in technological processes is at least partially obtained by burning associated gas and / or process gas contained in oil of thermal processes and / or thermo-destructive processes, and / or intermediate products, which are supplied to a network with a temperature of 50-70 ^o C and a pressure of 3-5 kg / cm ² , it is heated to a temperature not lower than 100 ^o C and 60-85% is fed for combustion to produce steam in technological processes, and 15-40% of the gas is fed for combustion in a steam generator to produce steam by heating return steam to ndensata heated with addition of chemically treated raw water in an amount necessary to compensate for non-refundable for heating condensate and chemically purified raw water and / or oil source, use residual heat in the waste oil distillation processes of steam and / or steam condensate.

 Separate operations of the method are carried out according to the technological options described above.

 The operating conditions of the processes are presented in the table.

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

 The original oil is sent to a block of electrodesalting and dehydration. Then served on the block of atmospheric or atmospheric vacuum distillation. The resulting diesel fraction is sent to the hydrotreating unit. Part of the straight-run fraction of diesel fuel, a vacuum solarium is subjected to alkalization in reactors with a NaOH solution.

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

 This method allows to obtain diesel fuel in accordance with the requirements of GOST with consistently high performance while reducing technological energy consumption by 5% at various stages of distillation, hydrotreatment of diesel fuel, while the sulfur content in the initial diesel fraction is reduced from 1 wt.% To 0.05 wt.%, which improves the environmental situation in the region and significantly improves the quality of petroleum products, favorably affects the operation of engines, vehicles, while the cost of steam itself production is 50% of the cost of purchased steam side, which leads to a significant reduction in production costs and enables efficient use of exhaust heat processing flows reduce flaring fuel gas and improve environmental conditions.

Claims (25)

1. A method of producing diesel fuel from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes of electric desalting and dehydration of oil by passing a stream through an electrode system in electric dehydrators, atmospheric and / or atmospheric-vacuum distillation of desalted oil in columns distillation, hydrotreating of diesel fractions, alkalization of a part of the obtained diesel fractions, followed by compounding of the fractions with the supply, at least, to the electric hydrants, atmospheric and / or atmospheric vacuum distillation columns, alkalization reactors as a heat carrier of steam produced in the steam generator and the formation of condensate, at least partially returning, as a result of heat extraction, mainly during oil distillation processes, characterized in that used in technological processes, steam is at least partially produced by burning the associated gas and / or process gas contained in the oil of thermal processes and / or the thermode structural processes, and / or intermediate products, which are fed into the network with a temperature of 50 - 70 ^o C and a pressure of 3 - 5 kg / cm ² , it is heated to a temperature of at least 100 ^o C and 60 - 85% is fed to combustion to produce steam in technological processes, and 15 - 40% of the gas is supplied for combustion in a steam generator to produce steam by heating the return steam condensate with the addition of heated chemically purified raw water in the amount necessary to compensate for the non-returning condensate and for heating the chemically purified raw water and / or source oil use the residual heat of steam and / or steam condensate spent in the technological processes of distillation of oil. 2. The method according to claim 1, characterized in that the electric desalting of the oil is carried out by passing a stream through the system of mesh and / or mesh located at least two levels of electrodes, covering in aggregate the height range of the electric dehydrator mainly in the upper half of the height of its body, and the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05 - 0.1 of the conventional segment of the path, which coincides with the average vector of movement of the oil flow in the zone of the largest midship of the electric dehydrator, dimogo flow for 1 h moving at an average speed elektroobessolivaniya process and dehydration, thus elektroobessolivanie and dehydration of oil carried in electrical dehydrators with a horizontally oriented cylindrical body or a composite configuration and a working volume of 80 - 200 m ^3, or in electrical dehydrators with housing spherical or spheroidal, and / or ellipsoidal, and / or ovoid, and / or teardrop-shaped, or electric desalting of oil is carried out in electrodehydrators of a spheroidal and / or ellipsoidal, and / or ovoid, and / or tear-shaped, and / or composite with a cylindrical body and convex-curved end sections, and / or toroidal shape, or electric desalting of oil is carried out in electric dehydrators, the longitudinal axis of the body, at least parts of which are oriented vertically or horizontally, or at an angle to the horizon. 3. The method according to p. 1, characterized in that the distillation of desalted and dehydrated oil using columns of atmospheric and / or atmospheric vacuum distillation, which provide packages of cross-precision nozzles placed with a height or altitude-angle offset adequate temperature zones of vapor condensation at the same time, at least part of the packages are placed in the condensation zone of the diesel fraction and distillation is carried out when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the pi zone titanium equipped with an internal cylindrical flow reflector, the diameter of which corresponds to the diameter of the column body in the feed zone as (0.59 - 0.75): 1, and the altitude range for introducing oil flows is 0.21 - 0.28 of the column height from the bottom mark column bottoms, while the supply of oil in an atmospheric tower and / or atmospheric and vacuum distillation is carried out through the nozzles, are arranged at an angle dilution points of intersection with the axes of the nozzles of the column body in the range of 30 - 180 ^o, with single-sided tangential swirling feed stream yl oil is supplied to the atmospheric and / or atmospheric vacuum distillation column through nozzles, the axis and the inner neck of one of which orient the flow of oil supplied through it in the feed zone of the column directly to the intersection with a similar stream supplied through another nozzle mainly in the zone of its exit from the inner neck of the latter, or the supply of oil to the column of atmospheric and / or atmospheric vacuum distillation is carried out through nozzles whose axes are oriented parallel to the tangent to the body in internal cylindrical reflector with a radial distance from the conditional point of contact with the reflector body at a distance b satisfying the condition
b ≥ 0.25 (R _k - R _o ),
where R _to is the radius from the column in the feed zone;
R _o is the radius of the reflector,
oil is introduced into the column through nozzles cut into the column body in parallel with the dilution of their axes at a distance of 0.5 - 0.85 of the diameter of the column in the feed zone, and distillation is carried out in the column, a cylindrical reflector in the feed zone of which is set eccentrically to the longitudinal axis of the column, or distillation is carried out in an atmospheric and / or atmospheric-vacuum distillation column, the cylindrical reflector of which is carried out with a variable radius of curvature in a cross section, or distillation is carried out in an atmospheric distillation column, cylindrical the th reflector of which is connected to the casing of the column of an annular, membrane flat, and / or broken, and / or curvilinear, and / or combined configuration in cross section, or distillation is carried out in a column whose oil flow reflector is made in the form of a two-leaf symmetric shell of variable curvature or a composite configuration, at least in cross section, or during distillation, an atmospheric distillation column is used, in which packets of cross-precision nozzles are regularly made of spatially deformed stainless steel sheet elements with overlapping height of temperature gradient packets 2 - 8 ^o C along the column height and vapor passage through them, comprising 38 - 81% relative to the cross section of the column, while distillation in the column is atmospheric and / or atmospheric vacuum distillation is carried out at a passage speed of vapors of the accelerated fractions of at least 1.0 - 1.7 m / s, and the output of a diesel fraction with a boiling point of 204 - 350 ^o C or a separated diesel fraction of 240 - 300 and 300 - 350 ^o C lead in the altitude range count primary acceleration, constituting 0.32 - 0.62, counting from the bottom of the column, or exceeding, respectively, the lower mark and the upper mark of the output range by 0.06 - 0.12 and 0.23 - 0.41 of the height of the column relative to the axis of entry of the pipes supplying oil to the feed zone of the column.  4. The method according to claim 1, characterized in that the hydrotreating is carried out in a hydrogen-containing gas medium in the presence of hydrotreating catalysts, while the gas-feed stream is introduced mainly axially.  5. The method according to p. 4, characterized in that when hydrotreating a diesel fraction, passed through one or two reactors, the latter or 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 their parallel or alternately separate inclusion in the work adequately given volumes and degree of hydrotreatment of the gasoline fraction.  6. The method according to claim 4 or 5, characterized in that the hydrotreating reactors use aluminum-cobalt or aluminum-nickel-molybdenum hydrotreating catalysts, or combinations thereof.  7. The method according to any one of claims 4 to 6, characterized in that at least one hydrotreating reactor is used, at least in the upper zone of which the catalyst layer is loaded with a discrete and / or combined vapor-permeable element of an inert or corrosion-resistant material or a combination of materials with similar properties, and at least the inlet surface of the catalyst layer in the path of the vapor-gas product flow is greater than the cross-sectional area of the hydrotreatment reactor.  8. The method according to any one of claims 4 to 7, characterized in that at least one reactor is used in hydrotreating, in which the catalyst layer is poured with the slope of at least part of at least the upper surface.  9. The method according to any one of claims 4 to 8, characterized in that at least one reactor is used in hydrotreating, in which at least the upper catalyst layer is poured with a conical and / or variable broken, and / or variable curved, and / or combined slope from the Central zone to the walls of the reactor vessel.  10. The method according to any one of claims 4 to 9, characterized in that at least one reactor is used in hydrotreating, 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 than the equivalent volume catalyst layer.  11. The method according to any one of claims 4 to 10, characterized in that at least one reactor is used in hydrotreating, in which elements with increased aerohydraulic permeability are made in the form of mesh and / or perforated cylindrical or polyhedral glasses or nozzles.  12. The method according to any one of claims 4 to 11, characterized in that at least one reactor is used in hydrotreating, 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 particle radius catalyst.  13. The method according to any one of claims 4 to 12, characterized in that at least one reactor is used in hydrotreating, 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.  14. The method according to any one of claims 4 to 13, characterized in that at least one reactor is used in hydrotreating, in which at least in the upper zone at least part of the catalyst layer is mixed with larger particles inert material.  15. The method according to any one of claims 4 to 14, characterized in that at least one reactor is used in hydrotreating, in which the particle ratio is variable with decreasing percentage of inert particles in the direction of movement of the gas-vapor product stream subjected to hydrotreating.  16. The method according to any one of claims 4 to 15, characterized in that during hydrotreating, at least a portion of the hydrotreating reactors are installed with the longitudinal axis inclined relative to the horizon.  17. The method according to any one of claims 4 to 16, characterized in that at least part of the hydrotreating reactors with a horizontally oriented longitudinal axis are used in hydrotreating.  18. The method according to any one of claims 4 to 17, characterized in that during hydrotreating, at least one hydrotreating reactor is made toroidal.  19. The method according to claim 1, characterized in that when alkalizing use a 3 - 5% solution of caustic soda with the supply of diesel fraction in at least two reactors in parallel streams, the treatment of the diesel fraction with caustic soda is carried out in stages, with the first stage they are injected through an injector installed outside the alkalization reactor with a volume ratio of diesel fraction and sodium hydroxide equal to 0.5 - 2.0, and the resulting mixture is introduced into the bottom layer of sodium hydroxide solution and the second mixing stage is carried out using ma a manbook, consisting of a distributor manifold equipped with a distribution pipe system with a selective perforation system, when caustic soda solution is filled with the reactor volume by 0.5 - 0.75 of its height and the rate of introduction of the diesel fraction into the solution layer equal to 0.6 - 7.9 m / s, compounding is carried out in one, two or three stages, at the same time, when alkalizing high-sulfur fractions, a solution of 3.0 - 5.0% sodium hydroxide solution is used when the diesel fraction is supplied to at least two reactors in parallel flows, or a reactor is used with di feed fraction into an external injector, the outlet nozzle of which is installed with a negative difference in nozzle height to a height of not less than 1 m relative to the lower level of the alkaline solution in the alkalization reactor, or when alkalizing, a reactor with distribution pipes supplying the diesel fraction placed at a height of 0.05 0.75 of the height of the caustic soda solution, or when alkalizing, a reactor is used in which the perforation holes in the mother liquor distribution pipes are made with a variable pitch and / or diameter, and / or the effect the apparent flow area with increasing of the above parameters as the distance from the input zone of the dispensing manifold to the alkalization tank is adequate to the drop in hydraulic pressure in the elements of the diesel distillate input system, or when alkalizing, a reactor is used in which at least part of the perforation holes are oriented to the flow axis flow along the sides of the horizon, or when alkalizing, use a reactor in which at least part of the perforation holes of the distribution pipes comfort at descending angles of the horizon, or when alkalizing, use a reactor in which at least part of the perforation holes are arranged in a spiral with constant or variable pitch, and at least part of the perforation holes in the distribution pipes of the mother liquor are circular cylindrical, and / or ovoid and / or combined configurations, either slit-like or alkalizing, using a reactor in which the mother liquor distributor is made in the form of a pipe of variable cross-section along the length of the reactor and alkalization, and the mixture of the diesel fraction and the alkali solution is supplied to the alkalization reactor at a variable speed in different zones of the reactors, or at alkalization, at least one alkalization reactor is used, the fluid layer height fluctuation in which during the input and output of the diesel fraction is carried out in within 16 - 20% of the initial level of caustic soda solution in the reactor by the time the alkalization process begins, or when alkalizing, use at least one alkalization reactor, which is performed horizontally with a round at least one alkalization reactor is used, which is formed by a broken or curved axis in plan or toroidal in the form of a closed or open torus, or when alkalizing, use at least one alkalizing, or toroidal, axis at least one reactor that is tilted 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 that is equipped with with a screen horizontally oriented or inclined, open from at least one end, immersed within the upper third in the alkalized fraction, when alkalizing, use at least one reactor and / or settling tank, which is performed with a larger transverse axis the section oriented vertically or obliquely, while the mixture of the diesel fraction with the alkali solution is supplied to the alkalization reactor by pulses, and after the alkalization of the treated alkali solution, the diesel fraction is removed from the upper zone p alkalization actors and is subjected to water washing and / or sludge in a tank for water washing and / or in a settling tank, while using water washing and / or sludge, use at least one additional settling tank in series with the first, and when settling, use at least one settling tank that is horizontally or hollowly inclined with a circular cylindrical or ellipsoidal cross-section, or at least one settling tank that is made with a broken line either with a curved axis in the plan, or toroidal in the form of a closed or open torus, or with sludge, use at least one settling tank, which is equipped with a baffle screen, open from one end, and immersed horizontally oriented in the surface layer of the diesel fraction , or inclined, and / or vertical, or with sludge, use at least one settling tank, which is equipped with at least two pairs of electrodes, intensifying the deposition of suspensions and impurities from the diesel fraction, and The diesel fraction cleaned in the alkalization reactor is fed to at least one settling tank, kept there for at least 50 - 80 minutes and sent for compounding. 20. The method according to claim 1, characterized in that the compounding in the first stage is carried out either directly in an atmospheric and / or atmospheric vacuum distillation column by adding at least part of the straight-run kerosene fraction to the diesel fraction, and / or in the process pipeline connecting the primary atmospheric and / or atmospheric vacuum distillation column to the alkalization reactor by feeding a straight-run kerosene fraction, compounding of the second stage is carried out after the diesel fraction is alkalized directly but in reservoir storing diesel fuel by supplying virgin and / or hydrotreated kerosene fraction under excess pressure zone located in the lower quarter of the height of the tank, preferably with jet inclination directed towards the bottom of the tank at an angle of not less than 30 ^o to the horizontal, wherein the compounding in the process pipeline, the supply of kerosene fraction and / or vacuum solarium is carried out in stages or discretely through at least two nozzles cut into the main pipeline from different sides and / or spaced along the length and oriented at an acute angle along the miscible distillates, or when compounding, use nozzles for introducing components mixed to the diesel fraction, cut into the main pipeline and providing unidirectional or counter-directional tangential vortex swirl of the mixed flows, or when compounding in the pipeline in its internal section in the compounding section of the first stage immediately after the insertion zone of the nozzles supplying kerosene mixed to the diesel fraction and / or vacuum-solar components, install at least one fixed impeller, or when compounding in the pipeline in the internal section, install at least two impellers with counter-directional swirling of the blades fixed relative to the pipeline body or fixedly fixed one relative to the other with the possibility of free joint rotation with the occurrence of an imbalance created or vortex countercurrents intensifying the process of compounding diesel distillate and when the diesel fraction is removed from the column of atmospheric and / or atmospheric vacuum distillation, the excess resulting heat is predominantly selected before the start of the first compounding stage, the second compounding stage is carried out in the diesel fuel storage tank by directly mixing the flows of the diesel fraction and the kerosene fraction supplied to the tank, 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 at the second stage a compound They use an injector, 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 solar oil is removed from the diesel fraction and / or its straight run kerosene fraction. atmospheric vacuum distillation vacuum columns; in the second stage of compounding, a reservoir is used, the injector in which is arranged 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 mounted nozzles with an opposite flow swirl, or compounding in a diesel fuel storage tank carried out by means of at least two injectors movably rotatably mounted in the bottom or bottom part of the diesel fuel storage tank.  21. The method according to any one of claims 1 to 20, characterized in that raw water is used from a flowing and / or non-flowing reservoir, and the chemically purified water is heated before or after purification of the raw water from suspensions and after cleaning the return steam condensate from oil pollution. 22. The method according to any one of claims 1 to 21, characterized in that water is used, for example, 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 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 the pumps raw water, at least one of which is left standby, and then pumped water through two heat bmennika with fixed tubular grates and preheated water to a temperature 25 - 30 ^o C, wherein at least one heat exchanger using a return condensate from the temperature 80 - 85 ^o C, wherein the amount of raw water flowing through this heat exchanger is adjusted to of cooling condensate to a temperature 25 - 35 ^o C, and the remainder of the raw water is passed through another heat exchanger, and heated to a temperature of 25 - 30 ^o C by using the heat exchanger as a heat carrier heating water having a temperature heating water in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters loaded with sulfonated coal, and carry out the removal of hardness salts from water to 1 - 2 mEq / kg constant and the destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg, and then softened self-regulating buffer filters loaded with sulfonated charcoal are used to protect the filtrate from acid leakage, and then the water is sent to remove free carbon dioxide into a decarbonizer loaded with Rashig rings, and air is separated with carbon dioxide, which is vented to the atmosphere, and the decarbonized water is fed by gravity into tank, after which this water is pumped through the pumps through two-stage sodium-cation exchange filters, and in the filters of the first stage, hardness cations are removed to 0.1 mEq / kg, and in the second stage, the hardness 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, total hardness 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 supplied to the tanks, and then pumped into the steam generator, while at least during the flood period, preliminary water purification, which is produced using at least two brighteners capacity of 250 m ³ / h, two interfered a lime milk capacity of 15 m ³ each, the two measuring tanks coagulant 10 ^m3 each, wet lime storage cell, preferably lime putty capacity of 100 m ^3, cell lime milk capacity of 60 m ³ and the metering pumps and / or centrifugal pumps with additional regulatory dampers, and chemical water purification is carried out only using sodium-cation exchange filters, in which the filter material is also regenerated with saline with a concentration of 6-8%, and furs are used for chemical water purification filters in the form of cylindrical vessels with an internal anticorrosion coating mainly made of epoxy resin, with two spherical steel bottoms, in the upper of which there is a feed water supply fitting and an upper distribution device in the form of beams of polymer material for distributing water over the filter cross section, and the bottom bottom is a drainage system in the form of a collector with slotted tubes made of stainless steel, along the axis of which holes are formed, overlapped by casings with slits 0.25 - 0 wide , 4 mm, moreover, a hatch is formed in the upper part of the filter housing to inspect 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, and a fitting for hydraulic overload is located on the filter housing at the level of the slit tubes, pipelines of source water, loosening, air vents of the upper and lower drainage systems, pressure gauges at the inlet and outlet of the collector, samplers and valves are connected, and the filtering filling is performed in two layers, consisting of a layer of silica sand with a height 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 is set taking into account the water flow for own needs and the preparation of regeneration solutions of at least 200 m ² / h, the filtering speed during operation of all filters - at least 7 m / h and maximum during loosening washing - at least 10 m / h with a flow rate for loosening of compressed air of 5 m ³ / h and a pressure of up to 1.5 kgf / cm ² ; used hydrogen-cation exchange filters are performed with a filtering area of at least 7 mm 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 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 capacity is at least 80 t / h and the filtering speed is at least 13 m / h; the self-regulating buffer filters used are loaded with sulfonated coal with a loading layer height of 2000 mm and are made with a top 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 made with a lower air inlet pipe, a spray separator and a decarbonized water outlet 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, 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, and the filter is equipped with a top distribution device and the filtering speed is not less than 34 m / h, while in all ion-exchange filters for chemical water treatment on the lower drainage device there is an anthracite layer with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm. 23. The method according to any one of claims 1, 21 and 22, characterized in that the chemically purified water is supplied to a steam generator with a temperature of 25-30 ^° C, and part of the chemically purified water is directed to sampling coolers for continuous and periodic blowing of boilers, and from there - into the deaerator head, another part of chemically purified water is sent to a gravity condensate cooler, which uses steam condensate heat, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed into the deaerator head, and the other hearth they are fed to the continuous purge cooler using heat from the purge water from the continuous purge separator, and then chemically purified water is passed through the deaerator vapor cooler, then it is fed into the deaerator head and steam is chemically cleaned by steam, heating it to a temperature close to saturation, and water is removed from the CO ₂ gas O ₂ and the network heating water fed to the network pumps, heaters then through the heating water in the heating system, while the repair chemically treated water heaters wasp estvlyayut switching network water heaters for heating the chemically treated water. 24. The method according to any one of claims 1, 21 to 23, characterized in that the steam from the boilers through the collectors is fed into the steam lines, and part of the steam from the collectors through a reducing device with a pressure of P = 4 kgf / cm ^{2 is} fed to the network water heater, to a chemically purified water heater, to a fuel gas heater, to heat a fuel gas separator and to deaerators; in the presence of excess spent steam, part of it is fed to heaters of chemically purified water and to network water heaters, and in them the condensate is sent to condenser tanks, from where they are pumped out by condenser pumps to clean the condensate; when the chemically treated water heater and network water heaters are operated on a reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head to replace an equivalent amount of chemically purified water heated, while the network and chemically purified water heaters perform in the form of a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the level of condensate in the heat exchanger is maintained with a level regulator, and then the condensate is sent to a 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 a steam-water one, using a steam generator boiler and steam condensate is fed through pipelines to a distribution comb, wherein the condensate is used with a total hardness of 100 meq / kg, the content of Fe, based on Fe ⁺³ to 180 mg / kg, the content of silicic acid to 350 mg / kg, containing oils 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, and from the distribution comb, the condensate is sent sequentially to the settling tank and the collection tank of pure condensate separated from the oil products, and as it floats up when condensate settles to the surface of the oil, it is collected using a catching funnel, while in both tanks a predetermined volume of liquid is maintained due to the difference in the levels of overflow troughs - filling pipes, after which condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of the filters of three de-oiling levels, 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, loaded with activated carbon, in parallel, and then to four sorption filters of the second dullness of condensate de-oiling to an oil content of not more than 0.05 mg / kg, and oil-free condensate with a temperature of 85 ^o C is sent to the annulus of heat exchangers, through which cold raw water used for technological needs of chemical water treatment is passed and the condensate is cooled to a temperature of 40 ^o C, after which it is sent in deoiled condensate tank from which condensate is pumped by pumps to a desalting unit, said deoiled condensation temperature is maintained within a 35 to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the filter material is a highly basic cationite KU-2,8 load with height of 1.5 mm and a layer filtering rate is 35 m / h, wherein the recovery is carried out periodically the exchange ability of the filters by regenerating the filter material with a 3-4% sulfuric acid solution, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as the filter material and the silicic acid compounds are removed from the condensate; moreover, the exchange capacity of the anion exchange filters is periodically restored by passing a 3 - 5% sodium hydroxide solution through the anion exchange filter layer, and after the anion exchange filters, the purified condensate containing silicic acid is not more than 150 mg / kg, iron ( based on Fe ⁺³⁾ is not more than 100 mg / kg, petroleum products - not more than 0.5 mg / kg and the total hardness not greater than 10 mg / kg is directed to a condensate storage tank, pumped from CHP and steam boiler and kotly- tilizatory, wherein for corrective processing desalted condensate to pH 8.5 - 9.5 and to reduce corrosion of metal pipes in the manifold is dosed 1% ammonia solution dosing pumps. 25. The method according to p. 24, characterized in that the clarifying filters used in the condensate cleaning are double chamber, consisting of a housing, a lower and upper drainage distribution device, and a blind flat horizontal partition is rigidly attached inside the housing, separating it into two chambers, 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 made 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 is made 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 uyuschego material; the thickness of the activated carbon layer of the filters of the 1st stage is 2.5 mm with a grain size of 2 to 6 mm, and the 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 switchgear - in the form of a collector, which is parallel to the bottom and into which the distribution pipes are inserted with holes along the lower generatrix with a diameter of 8 mm, overlapped by a gutter-shaped formation another with a slit 0.25-0.4 mm wide to prevent the ingress of activated carbon into the condensate; when condensate is supplied to the desalination plant, for example, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and pressure P = 5.0 kgf / cm ^{2 are used} , the hydrogen-cation exchange and anion exchange filters are made in the form of single-chamber having a capacity of 115 m ³ / h of 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 switchgears, the upper of which is made in the form of a "glass in a glass", and the lower - in the form of a collector, in to distribution tubes-rays are inserted with holes, along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.

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