RU2155205C1 - Method of producing mazut from low-sulfur and/or sulfur, and/or high- sulfur petroleums - Google Patents

Abstract

FIELD: petroleum processing. SUBSTANCE: crude oil is subjected to desalting and dehydration in electrical dehydrators and then to atmosphere-vacuum distillation wherefrom following intermediate products are withdrawn: straight-run gasoline, kerosene, and diesel, mazut, straw oil, lube oil fractions and tar oil. At least part of products are compounded with products from other installations. Heat carrier used in at least atmosphere-vacuum distillation process is water steam produced in steam generator by at least partly superheating of water by combustion of associated gas and/or process gas from thermal processes taking part in petroleum processing, and/or intermediate products. Gas is supplied into gas network at temperature 50-70 C and pressure 3-5 kg/sq.cm and, before combustion, gas is preheated to temperature not below 100 C. 60- 85% of gas is burned in process furnaces and 15-40% in steam generator. At last partly return condensate added to chemically purified water is used to generate steam. To preheat chemically purified water and/or original petroleum, residual heat of process spent steam and/or steam condensate, and/or tar oil withdrawn from column is utilized. EFFECT: improved flash temperature and viscosity of mazut because of removal of clear petroleum products, and simultaneously reduced power consumption. 19 cl, 1 tbl

Description

 The invention relates to oil refining, and in particular to methods for producing fuel oil from oils with different sulfur contents.

 Known accepted as the closest analogue is a method for producing fuel oil from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes: electric desalting and dehydration of oil in electric dehydrators, atmospheric-vacuum distillation with the conclusion of intermediate products: straight-run gasoline, kerosene, diesel fractions, the withdrawal of fuel oil fractions, vacuum solarium and oil distillates, tar, at least partial compounding of oil fractions of the ELOU-AVT plants, tar, asphalt from the propane deasphalting units, the phenol selective oil purification extract, paired solvent extraction oils, petrolatum from the oil dewaxing units, bitumen using at least during atmospheric vacuum distillation as a vapor coolant obtained in the steam generator and the formation of condensate, at least partially returnable, as a result of the selection of heat, mainly during technological processes APIS oil (see. for example, Erich V.N., Rasina M.G., Rudin M.G. Chemistry and technology of oil and gas, Leningrad, Chemistry, L.O., 1985, pp. 385-398).

 The disadvantages of this method are the high energy costs, as well as the high cost due to the need to purchase the steam required at certain stages of production outside this production, as well as significant unjustified heat losses from the processing effluent due to fuel gas flaring, which, in addition, leads to environmental degradation the setting.

 The objective of the present invention is to reduce the energy intensity and cost of production due to the use of steam of own production in a number of production processes, as well as ensuring the rational use of heat from the processing effluent and reducing the amount of fuel gas flared, improving the environmental situation in the region while reducing the amount of chemically cleaned water and providing deeper oil refining.

The problem is solved due to the fact that in the method for producing fuel oil from low-sulfur, and / or sulfur, and / or high-sulfur oils, including thermal and thermo-destructive technological processes: electric desalting and dehydration of oil in electric dehydrators, atmospheric-vacuum distillation with the conclusion of intermediate products: straight-run gasoline , kerosene, diesel fractions, the withdrawal of fuel oil fractions, vacuum solarium and oil distillates, tar, at least partial compounding of the oil fractions of the ELOU-AV units , tar, asphalt from propane deasphalting units, phenol selective oil purification extract, paired solvent selective oil extract, petrolatum from oil dewaxing units, bitumen using at least during atmospheric vacuum distillation steam obtained in the steam generator and the formation of condensate, at least partially returnable, as a result of the selection of heat, mainly during technological processes of distillation of oil, according to According to the invention, the steam used in the technological processes is at least partially obtained by burning the associated gas and / or fuel-technological gas contained in the thermal processes of oil refining, and / or thermal destructive processes of oil refining 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 ² , and before combustion, the gas is heated to a temperature not lower than 100 ^o C, while 60-85% of the gas is burnt in the furnaces of technological processes, and 15-40% of the gas is burnt in steam generator with is the use of return condensate as water with the addition of chemically purified raw water, at least in the amount necessary to compensate for the non-return condensate, while the residual heat of the steam used in the technological processes of distillation of oil is used to heat the chemically purified raw water and / or source oil, and / or steam condensate and / or tar removed from the vacuum column.

In this case, electric desalting and dehydration of oil can be carried out in electric dehydrators by passing the oil flow through a system of mesh and / or mesh located at least 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 height gradient between the levels of the electrodes the path of the upward flow of oil is 0.05-0.1 conventional section of the path, which coincides with the average vector of movement of the oil flow in the zone of the greatest midship an electrodehydrator, which is driven by the flow per hour at an average speed of the process of electric desalting and dehydration, while electric desalting and oil dehydration are carried out in electric dehydrators with a horizontally oriented cylindrical or composite body and a working volume of 80-200 m ³ , or in electric dehydrators with a spherical or spheroidal body and / or ellipsoidal and / or ovoid and / or drop-shaped, or in electric dehydrators with a cylindrical body and convexly curved and ends mi portions and / or toroidal shape or in electrical dehydrators, a longitudinal axis of the body, at least a portion of which is oriented vertically or in electrical dehydrators, a longitudinal axis of the body, at least a portion of which is oriented horizontally or at an angle to the horizontal.

At distillation of desalted oil, atmospheric and / or atmospheric vacuum distillation columns equipped with cross-flow nozzle packs placed with a high-altitude or high-angle bias can be used that are adequate to the temperature zones of vapor condensation, while at least some of the packets are placed in the condensation zone of the gasoline fraction 120- 180 ^o C, distillation is carried out when oil is supplied to the columns, at least through two nozzles tangentially located in the column body in the supply zone, equipped with an internal cylindrical a flow reflector, the diameter of which corresponds to the diameter of the column body in the feed zone as (0.59-0.75): 1, and the altitude range for introducing oil flows is 0.21-0.28 the height of the column from the bottom of the bottom of the column, 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, equal to 0.37-0.53 of the height of the column relative to the axis in ode oil supply nozzles in the column feed zone, the output of the diesel fraction 240-350 ^o C or diesel fractions 240-300 ^o C and 300-350 ^o C is performed in the height range of atmospheric distillation column constituting a column height of 0,32-0,62 , counting from the bottom or with 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 feed zone columns, oil is supplied to the atmospheric distillation column through nozzles located with an angle p the introduction of the points of intersection of the axes of the nozzles with the column body in the range of 30-180 ^o C one-sided tangential swirl of the feed stream, or oil is supplied to the atmospheric distillation column through the nozzles, the axis and the inner neck of one of which direct the flow of oil supplied through it in the feed zone of the column directly at the intersection with a similar stream supplied through another branch pipe mainly in the zone of its exit from the inner neck of the latter, or oil supply to the atmospheric and / or atmospheric column spherical-vacuum distillation is carried out through nozzles whose axes are oriented parallel to the tangent to the body of the internal cylindrical reflector with a radial distance from the conditional contact point with the reflector body for consideration b, satisfying the condition b ≥ 0.25 (R _k -R _о ), where R _k is the radius of the column in the supply zone, R _о is the radius of the reflector, or distillation is carried out in the column, a cylindrical reflector in the supply zone of which is set by an eccentric system relative to the longitudinal axis of the column, or distillation is carried out in the column of atmospheric Oh and / or atmospheric vacuum distillation, the cylindrical reflector of which is performed with a variable radius of curvature in cross section, or distillation is carried out in a column of atmospheric and / or atmospheric vacuum distillation, the cylindrical reflector of which is connected to the column body with a circular and / or polygonal annular membrane , and / or a curvilinear and / or combined configuration in cross section, or during distillation, an atmospheric and / or atmospheric vacuum distillation column is used in which the cross-flow nozzle packs in suppl spatially deformed elements of stainless steel sheet, wherein the overlap provides a package height of temperature gradients 2-8 ^o C along the column height, and the area of the passage of vapor through them is 38-81% with respect to the cross section of the column, wherein the distillation column in the atmospheric and / or atmospheric-vacuum distillation is carried out at a vapor velocity of the accelerated fractions of at least 1.0-1.7 m / s.

 The compounding of fuel oil can be carried out in one, two, or three stages, while the compounding in the first stage is carried out either directly in the vacuum distillation column by adding oil fractions to the tar and / or in the process pipeline connecting the vacuum distillation column to the fuel oil storage tank, with supply in the pipeline of flows of oil fractions, compounding in the second stage is carried out directly in the fuel oil storage tank by feeding tar, and / or fuel oil, and / or diesel fraction, and / or asphalt from installations of deasphalting oils with propane, an extract of selective purification of oils by phenol, an extract of selective purification of oils by paired solvents, petrolatum from installations of dewaxing of oils, bitumen supplied under overpressure, while compounding in a technological pipeline with a diesel fraction is carried out in stages or discretely in at least two pipe, cut into the main pipeline from different sides, and / or spaced along the length and oriented at an acute angle along the mixed fractions, and when compounding, use pipes for introducing components mixed with tar located in the pipeline and providing unidirectional or counter-directional tangentially vortex swirl of the mixed flows, or when compounding in the pipeline in its internal section, in the area immediately after the location of the nozzles supplying components mixed with tar, install at least one fixed impeller, or when compounding in the pipeline, in the internal section it is not installed less than two impellers with opposite directional swirling of the blades fixed relative to the pipe body or fixedly fixed one relative to the other with the possibility of free joint rotation when an imbalance occurs, created or vortex countercurrents intensifying the process of compounding fuel oil, and when the tar is removed from the vacuum distillation column, the selection of excess resulting heat mainly before the start of the first compounding stage, the second compounding stage lead into the fuel oil storage tank by directly mixing the components supplied to the tank, either through an injector introduced into the bottom zone of the tank with a separate supply of fuel oil and diesel fraction, or an injector is used in the second compounding stage, 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 flow, or in the first stage of compounding the fuel oil, atmospheric vacuum distillation of the component, and in the second stage of compounding, a reservoir is used, the injector is introduced into it by means of a tangentially installed nozzle, or compounding in the fuel oil storage tank is carried out by means of at least two injectors which are fixed on tangentially installed nozzles with oncoming swirling flows, or by at least two injectors that are movably rotationally mounted in the bottom or bottom of the tank.

In the production of fuel oil, the selection of oil distillate can be carried out from a vacuum column in a high temperature range of 280-320 ^o C, the distillate is purified using selective solvents - phenol, or furfural, or N-methylpyrrolidone with a ratio of solvent to raw material (1.5-2) : 1 to obtain the raffinate and extract, which is mixed with fuel oil, by dewaxing the raffinate using acetone and / or methyl ethyl ketone solvents and / or methyl isobutyl ketone with a solvent to feed ratio (1.5-2.5): 1 with cooling to t temperatures below the required pour point of the oil, after which the oil is filtered off from high-molecular-weight solid hydrocarbons - paraffins, and then sent to compounding with fuel oil.

In the production of distillate oils based on a machine fraction, the selection of oil distillate can be carried out from a vacuum column in a high temperature range of 320-328 ^o C, the distillate is purified using selective solvents - phenol, or furfural, or N-methylpyrrolidone with a solvent to feed ratio ( 2-2.5): 1 by obtaining an extract aimed at mixing with oil by dewaxing of the oil with cooling it to a temperature below the required pour point of the oil, after which the oil is filtered off from the solid Macromolecular-paraffin hydrocarbons, which is sent to blending with fuel oil.

In the production of fuel oil, tar can be selected from the lower part of the vacuum column in the high temperature range of 330-340 ^o C, tar is removed from asphalt hydrocarbons using selective solvents - liquefied propane, gasoline fraction with a ratio of solvent to tar 4.0-8.0 : 1, followed by purification of the obtained deasphalizate with selective solvents - phenol or furfural, or N-methylpyrrolidone with a phenol to deasphalting ratio of 3.0-5.0: 1 to obtain a raffinate and subsequent dewaxing lowering it using solvents - acetone, and / or methyl ethyl ketone, and / or methyl isobutyl ketone with a solvent to feed ratio of 3.0-4.5: 1 with cooling to a temperature lower than the required pour point of the oil, after which the oil is filtered off from high molecular weight solid hydrocarbons - paraffins, which are sent for mixing with fuel oil.

In the production of fuel oil, tar can be selected from the lower part of the vacuum column in the high temperature range of 330-340 ^o C, and the tar is cleaned with paired solvents of various nature, one of which is propane for the extraction of valuable hydrocarbons, and the other is a mixture of 35-60% phenol and 65-40% cresol for dissolving undesirable components of the raw material with a multiplicity of solvent-propane to tar 3.0-4.0: 1, and the solvent - a mixture of phenol and cresol to raw materials 4.0-6.0: 1 to obtain raffinate and its subsequent dewaxing using solvents - acetone, and / or methyl ethyl ketone, and / or methyl isobutyl ketone with a multiplicity of the solvent to the tar 1.5-2.0: 1 with cooling to a temperature below the required pour point of the oil, after which the oil is filtered from solid high-molecular hydrocarbons - paraffins, which direct to mix with fuel oil.

 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 the permanganate oxidation rate is 3.84-5.12 mg / kg in O ₂ , moreover, the raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to the raw water pumps, at least one of which is left standby, and then pumped water through two heat exchangers with fixed tube sheets and and water is heated to a temperature of 25-30 ^o C, moreover, 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 rest of the raw water is passed through another heat exchanger and heated to a temperature of 25-30 ^o C due to the use in this heat exchanger as heating medium, heating water having a heating water temperature in accordance with the season, and the last 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 removed from water of 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 of acidity buffers, self-regulating buffer filters loaded with sulfonated coal, and then water is directed 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 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 f hardness cations Ca ⁺² , Mg ⁺² up to 0.01 mEq / kg with obtaining 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 to a steam generator.

At least during the flood period, they can pre-treat water that is produced 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, mainly lime dough with a capacity of 100 m ³ , lime milk cells with a capacity of 60 m ³ and metering pumps and / or centrifugal pumps with additional control dampers, and chemical water treatment is carried out only using the use of sodium-cation exchange filters, in which the filter material is also regenerated with saline with a concentration of 6-8%.

For chemical water treatment, 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 there is a feed water supply fitting and an upper distribution device in the form of beams made of polymer material for distribution 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 a hatch is formed in the upper part of the filter housing to inspect the surface of the filter material, and in the lower - 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 located, source 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 layer, 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 is set taking into account the water flow for own needs and the preparation of regeneration solutions of 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 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 / hour, and the filtering speed is not less than 25 m / hour, 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 erhnim switchgear and filtration speed is at least 34 m / h, wherein all ion exchange filters, chemical treatment of water on the bottom of the drainage device has 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 perform bubbling of chemically purified water steam, heating it to a temperature close to saturation, and removed from the water the gases O ₂ , CO, and the district 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 to odes 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 into deaerators.

 In the presence of excess spent steam, part of it can be fed to chemically treated water heaters and 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.

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 and water and water heat exchangers, and first, steam is condensed in the steam and 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 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.

A steam boiler room can be used as a steam generator, and steam condensate is piped 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 silicic acid content to 350 is used. mg / kg, oil content up to 80 mg / kg and pH up to 8.0 units, 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 sump tank and the collection tank of the oil tank products of pure condensate, and as the condensate floats up to the surface of the oil, 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, loading containing 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 stage of decontamination of the condensate to the content the oils in it are not more than 0.05 mg / kg, and the oil-free condensate with a temperature of 85 ^o C is sent to the annular space of the heat exchangers through which cold raw water used for the process is passed technical 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, it is used in 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. The exchange ability of the filters is restored 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 and silicon compounds are removed from the condensate acid, and periodically carry out the restoration of the exchange capacity of anion exchange filters by passing through the filter layer of anion exchange resin 3-5% sodium hydroxide solution, and after an onite 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 more than 10 mg / kg, they are sent to the condensate reserve tank, from where they are pumped to the CHPP and the steam boiler room and to waste heat boilers, and for correcting the desalted condensate to a pH value of 8.5-9.5 units and reducing corrosion of the piping metal, a 1% solution is dosed into the collector ammonia 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 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 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 invention is to reduce the energy intensity and cost of production due to the use of steam of own production in a number of production processes, the cost of which is lower than the cost of steam purchased on the side, up to 50%, as well as ensuring the rational use of heat from the processing effluent and reduce the amount fuel gas flared, which additionally improves the environmental situation while reducing the required amount chemically purified water by providing the possibility of 100% use of return condensate in deeper oil refining. In addition, it provides improved characteristics of the resulting fuel oil, namely, an increase in flash point and viscosity, due to a more complete removal of light oil products from the fuel oil.

 Example.

 The method is as follows.

 Oil is subjected to thermal and thermo-destructive processes: electrodesalting and dehydration in electric dehydrators, atmospheric vacuum distillation with the conclusion of intermediate products - straight-run gasoline, kerosene, diesel fractions and fuel oil.

 After that, part of the obtained tar is cleaned with liquid propane (deasphalting process) or it is cleaned with paired solvents to produce asphalt, which are sent for mixing with fuel oil. Purification of the oil fractions is carried out with selective solvents to obtain a raffinate, which is sent to be mixed with fuel oil, dewaxing of raffinates of both distillate and residual oils to obtain solid paraffins, which are sent to be mixed with fuel oil. Then, compounds are compounded - tar, asphalt, paraffins and substandard bitumen.

The use of the heat of water vapor is envisaged, at least in the process of atmospheric-vacuum distillation of oil obtained by burning associated gas contained in the feedstock and / or fuel and process gas generated during the distillation of oil,
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 boiler, which is used as a steam generator, 80% - in furnaces of the process of atmospheric vacuum distillation.

Before combustion, the gas is heated to 100 ^o C. Provides for the supply of steam in an atmospheric vacuum column.

 As water in the production of steam, return condensate is used, which is formed during heat extraction in the indicated technological processes, with the addition of heated water from the Ural River, which is previously subjected to chemical water 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.

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

 The feedstock is Shpakovskoye oil, the sulfur content is 2.2%.

 As a result of the method, the energy consumption for its implementation decreased by about 50%, the yield of fuel oil and intermediate products in the calculation of the fuel used in their production increased by about 3%, and the environmental situation improved.

Claims (19)

1. A method of producing fuel oil from low-sulfur and / or sulfur and / or high-sulfur oils, including thermal and thermo-destructive technological processes: electric desalting and dehydration of oil in electric dehydrators, atmospheric vacuum distillation with the conclusion of intermediate products: straight-run gasoline, kerosene, diesel fractions, output fractions of fuel oil, vacuum solarium and oil distillates, tar, at least partial compounding of oil fractions of ELOU-AVT, tar, asphalt from dea sphalization of oils with propane, an extract of selective purification of oils with phenol, an extract of selective purification of oils with paired solvents, petrolatum from oil dewaxing plants, bitumen using at least during atmospheric vacuum distillation as a heat carrier steam obtained in a steam generator and the formation of condensate, at least partially returnable, as a result of heat extraction, mainly during technological processes of oil distillation, characterized in that it is used in technological steam, at least partially, is obtained by burning the associated petroleum gas and / or process gas contained in the thermal processes of oil refining, and / or thermal destructive processes of oil refining and / or intermediate products, which are supplied to 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, while 60 - 85% of the gas is burnt in the furnaces of technological processes, and 15 - 40% of the gas is burnt in a steam generator using as water in return condensate with the addition of chemically purified raw water, at least in an amount necessary to compensate for non-returnable condensate, while the residual heat of the steam and / or steam used in the technological distillation processes is used to heat the chemically purified raw water and / or the source oil condensate, and / or the tar removed from the vacuum column. 2. The method according to claim 1, characterized in that the electric desalting and dehydration of the oil is carried out in electric dehydrators by passing the oil flow through a system of mesh and / or mesh located at least two electrode levels, covering in aggregate the height range of the electric dehydrator mainly in the upper half of the height its body, and the height gradient between the levels of the electrodes on the path of the upward flow of oil is 0.05 - 0.1 of the conventional section of the path, which coincides with the average vector of movement of the oil flow in the zone the greatest midship of the electric dehydrator, which is driven by the flow per hour at an average speed of the process of electric desalting and dehydration, while electric desalting and dehydration of oil is carried out in electric dehydrators with a horizontally oriented cylindrical or composite body and a working volume of 80 - 200 m ³ , or in electric dehydrators with a spherical body or spheroidal, and / or ellipsoidal, and / or ovoid, and / or teardrop-shaped, or in electric dehydrators with a cylindrical body and convex rivolineynym and end portions, and / or toroidal shape or in electrical dehydrators, a longitudinal axis of the body, at least a portion of which is oriented vertically or in electrical dehydrators, a longitudinal axis of the body, at least a portion of which is oriented horizontally or at an angle to the horizontal. 3. The method according to claim 1, characterized in that during the distillation of desalted oil, atmospheric and / or atmospheric vacuum distillation columns are used, equipped with packages of cross-flow nozzles placed with high-altitude or high-angle displacement adequate to the temperature zones of vapor condensation, at least , some packages are placed in the condensation zone of the gasoline fraction 120 - 180 ^o C, distillation is carried out when oil is supplied to the columns through at least two nozzles tangentially located in the column body in the supply zone, equipped with the internal cylindrical reflector of the flow, the diameter of which correlates with the diameter of the column body in the feed zone as (0.59 - 0.75): 1, and the altitude range for introducing oil flows is 0.21 - 0.28 the height of the column from the bottom of the bottom of the column, 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 of 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 about tons of column height relative to the axis of the input of oil supply pipes to the column feed zone, 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 the altitude range of the atmospheric distillation column of 0.32 - 0 , 62 from the height of the column, counting from the bottom or with 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 the nozzle entry oil supply to the feed zone of the column, oil was supplied to the atmospheric distillation column removed through tubes disposed with an angle of dilution points of intersection of the axes of the pipes with the column shell in the range of 30 - 180 ^o C sided tangential swirling feed stream or feed oil into atmospheric distillation column is carried out through the nozzles, the axis and the inner neck of one of which is oriented stream supplied through oil 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 villa oil atmospheric column and / or atmospheric and vacuum distillation is carried out through nozzles whose axes are orientated parallel to the tangent to the body of the inner cylindrical reflector with radial distance from the notional point of tangency with the reflector housing to the b, satisfying the condition b ≥ 0,25 (R _k - R _o ), where R _k is the radius of the column in the supply zone, R _o is the radius of the reflector, or distillation is carried out in the column, a cylindrical reflector in the supply zone of which is set by eccentricity relative to the longitudinal axis of the column, and whether the distillation is carried out in an atmospheric and / or atmospheric vacuum distillation column whose cylindrical reflector is made with a variable radius of curvature in cross section, or the distillation is carried out in an atmospheric and / or atmospheric vacuum distillation column whose cylindrical reflector is connected to the column body by a flat circular membrane , and / or a broken and / or curvilinear and / or combined configuration in cross section, or during distillation, an atmospheric and / or atmospheric vacuum distillation column is used, in which The packages of cross-flow nozzles are made of spatially deformed elements of sheet stainless steel, and the height of the packages provides overlapping temperature gradients of 2-8 ^° C along the height of the column, and the vapor passage through them is 38 - 81% relative to the cross section of the column, while the column of atmospheric and / or atmospheric vacuum distillation is carried out at a vapor velocity of the accelerated fractions of at least 1.0 - 1.7 m / s.  4. The method according to claim 1, characterized in that the compounding of the fuel oil is carried out in one, two, or three stages, while the compounding in the first stage is carried out either directly in the vacuum distillation column by adding oil fractions to the tar and / or in the process pipeline, connecting the vacuum distillation column to the fuel oil storage tank, with the supply of oil fractions to the pipeline, compounding in the second stage is carried out directly in the fuel oil storage tank by feeding tar, and / or fuel oil, and / or diesel flax fraction and / or asphalt from propane deasphalting units, selective phenol oil treatment extract, paired solvent selective oil extraction extract, petrolatum from oil dewaxing plants, bitumen supplied under overpressure, while compounding in a process pipeline with a diesel fraction is carried out in stages or discretely, not less than through two nozzles cut into the main pipeline from different sides, and / or spaced along the length and oriented at an acute angle along the fractions, and when compounding, nozzles for introducing components mixed with tar are used, located in the pipeline and providing unidirectional or counter-directional tangentially vortex swirl of the mixed flows, or when compounding in the pipeline in its internal section in the area immediately after the location of the nozzles supplying mixed with tar components, install at least one fixed impeller, or when compounding in the pipeline, in the internal at least two impellers with opposite directional swirling of the blades fixed relative to the pipe body or fixedly fixed relative to one another with the possibility of free joint rotation when an imbalance occurs, created or vortex countercurrents intensifying the fuel oil compounding process, and when withdrawing tar from the vacuum distillation column, it is selected excess resulting heat is predominantly before the start of the first compounding stage, T The new compounding stage is carried out in the fuel oil storage tank by directly mixing the components supplied to the tank, either through an injector introduced into the bottom zone of the tank with a separate supply of fuel oil and diesel fraction, or an injector is used in the second compounding stage, 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 flow, or in the first stage of compounding the fuel oil is added to the tar removed from vacuum columns of atmospheric-vacuum distillation of the component, and in the second stage of compounding, a reservoir is used, the injector is introduced into it by means of a tangentially mounted nozzle, or compounding in the fuel oil storage tank is carried out by means of at least two injectors that are fixed on tangentially installed nozzles with oncoming swirling streams, or by means of at least two injectors, which are movably rotationally mounted in the bottom or bottom of the cut the boulder. 5. The method according to claim 1, characterized in that in the production of fuel oil, the selection of oil distillate is carried out from a vacuum column in a high temperature range of 280 - 320 ^o C, the distillate is purified using selective solvents - phenol, or furfural, or N-methylpyrrolidone with the ratio of solvent to raw materials (1.5 - 2): 1 to obtain the raffinate and extract, fed to the mixture into fuel oil, by dewaxing the raffinate using solvents - acetone and / or methyl ethyl ketone and / or methyl isobutyl ketone with a solvent multiplicity of raw materials (1.5 - 2.5): 1 with cooling to a temperature below the required pour point of the oil, after which the oil is filtered off from solid high molecular weight hydrocarbons - paraffins, then sent for compounding with fuel oil. 6. The method according to claim 1, characterized in that in the production of distillate oils based on a machine fraction, the selection of oil distillate is carried out from a vacuum column in a high temperature range of 320 - 328 ^o C, the distillate is purified using selective solvents - phenol, or furfural , or N-methylpyrrolidone with a ratio of solvent to raw material (2 - 2.5): 1 to obtain an extract directed to mix with oil by dewaxing of the oil with cooling it to a temperature below the required pour point of the oil, after which filter the oil from solid high molecular weight hydrocarbons, paraffins, which are sent to mix with fuel oil. 7. The method according to claim 1, characterized in that in the production of fuel oil the tar is selected from the bottom of the vacuum column in the high temperature range of 330 - 340 ^o C, the tar is cleaned of asphalt hydrocarbons using selective solvents - liquefied propane, gasoline fraction the ratio of the solvent to tar 4.0 - 8.0: 1, followed by purification of the obtained deasphalting agent with selective solvents - phenol or furfural, or N-methylpyrrolidone with the ratio of phenol to deasaltizate 3.0 - 5.0: 1 to obtain raffinate and its subsequent dewaxing using solvents - acetone, and / or methyl ethyl ketone, and / or methyl isobutyl ketone with a solvent to feed ratio of 3.0 - 4.5: 1 with cooling to a temperature below the required pour point of the oil, after which the oil is filtered off from solid high molecular weight hydrocarbons, paraffins, which are sent for mixing with fuel oil. 8. The method according to claim 1, characterized in that in the production of fuel oil, the tar is selected from the lower part of the vacuum column in a high temperature range of 330 - 340 ^o C, and the tar is cleaned with paired solvents of various nature, one of which is propane for the extraction of valuable hydrocarbons, and the other is a mixture of 35 - 60% phenol and 65 - 40% cresol to dissolve undesirable components of the feed with a multiplicity of propane solvent to tar 3.0 - 4.0: 1, and the solvent - a mixture of phenol and cresol to feed 4, 0 - 6.0: 1 to obtain the raffinate and its subsequent dewaxing using solvents - acetone, and / or methyl ethyl ketone, and / or methyl isobutyl ketone with a multiplicity of solvent to tar 1.5 - 2.0: 1 with cooling to a temperature below the required pour point of the oil, after which the oil is filtered off from high molecular weight solid hydrocarbons - paraffins, which are sent for mixing with fuel oil.  9. The method according to any one of claims 1 to 8, characterized in that they 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. 10. The method according to any one of claims 1 to 10, 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 raw water pumps, at least one of which is left standby, and then pumped water through two heat exchangers ennika 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 of from of heating water in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to the 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, then softened water is supplied to the self-regulating buffer filters loaded with sulfonated carbon that protects 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 the 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 of up to 0.1 mg are removed equiv / kg, and in the second stage, they remove the hardness cations Ca ⁺² Mg ⁺² to 0.01 mEq / kg to obtain chemically purified water with a transparency of at least 40 cm, total hardness 2 - 5 mEq / kg, content iron 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 the tanks, and then pumped into the steam generator. 11. The method according to any one of claims 1 to 10, characterized in that, at least during the flood period, preliminary water is purified, which is produced 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, the two measuring tanks coagulant 10 ^m3 each, lime wet storage cell, preferably lime putty capacity of 100 m ³ of milk of lime cell capacity of 60 m ³ and metering pumps, and / or centrifugal pumps with additional regulating valves, and the chemical kuyu produce only water purification using sodium cation filters, which also produce regeneration of the filter material with the concentration of brine 6 - 8%. 12. The method according to any one of claims 1 to 11, characterized in that for the chemical treatment of water, mechanical filters are used in the form of cylindrical vessels with an internal anti-corrosion coating, mainly of epoxy resin, with two spherical steel bottoms, in the upper of which 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 steel, along the axis of which holes are formed, overlapped by casings with slits 0.25 - 0.4 mm wide, with a hatch formed in the upper part of the filter housing to inspect the surface of the filter material, and in the lower part a manhole for mounting and repairing the upper and lower drainage systems, while on the filter housing at the level of the slit tubes there is a fitting for hydroloading, source 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 in ventiles, and the filter flap 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 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 preparation of regeneration solutions of 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 of 5 m ³ / h of compressed air for loosening and pressure 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, 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 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 they switchgear 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 rays location level with perforations not less than 10 cm. 13. The method according to any one of claims 1 to 12, 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 sent to sampling coolers for continuous and periodic blowing of boilers, and from there to 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 is fed to a continuous purge cooler using the heat of purge water from a 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 chemically purified by barbation, heating it to a temperature close to saturation and removed from water O ₂ gases, CO, and 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 implement yayut switching network water heaters for heating the chemically treated water. 14. The method according to any one of claims 1 to 13, characterized in that the steam from the boilers through the collectors is fed into the steam pipelines, and part of the steam from the collectors through a reducing device with a pressure p = 4 kgf / cm ^{2 is} fed to the network water heater, to the heater chemically purified water, to the fuel gas heater, to heat the fuel separator and to deaerators.  15. The method according to any one of claims 1 to 14, characterized in that, in the presence of excess spent steam, part of it is fed to chemically purified water heaters and to network water heaters, and the condensate is sent to condenser tanks in them, from where they are pumped out by condenser pumps for cleaning condensate. 16. The method according to p. 15, 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. 17. 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 first passed through a water-water heat exchanger, and then through a steam-water one. 18. The method according to any one of claims 1 to 17, characterized in that a steam boiler room is used as a steam generator, and steam condensate is piped to a distribution comb, and condensate is used with a total hardness of 100 mEq / kg, Fe content in terms of on Fe ⁺³ up to 180 mg / kg, silicic acid content up to 350 mg / kg, oil content up to 80 mg / kg and pH up to 8.0, moreover, if the condensate does not match the specified parameters, it is sent to the drain, and condensate from the distribution comb send sequentially to the tank sucks ik and a collection tank of pure condensate separated from oil products, and as the condensate floats up to the surface of the oil, 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 clean 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 oil-free three-stage filters nivaniya, on clarification filters loaded with anthracite, in which suspended mechanical particles and oil products are removed up to 4 - 5 mg / kg, after which the condensate is sent to four sorption filters of the first stage loaded with activated carbon, and then to four sorption filters deoiling second stage condensate to the oils contained less than 0.05 mg / kg and deoiled condensate at a temperature of 85 ^o C fed to the shell space of heat exchangers, through which is passed the cold th tap 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 in the range of 35 - 40 ^o C and they direct it 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 it is 35 m / h, moreover, the exchange ability of the filters is periodically restored by regenerating the filter material with a 3-4% sulfuric acid solution, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17- is used as the filter material. 8 and the silicic acid compounds are removed from the condensate, and periodically, the exchange capacity of the anion exchange filters is restored by passing 3-5% through the filter layer of the anion exchange resin sodium hydroxide solution, and after anion exchange filters, purified condensate with a content of silicic acid of not more than 150 mg / kg, iron (in terms of Fe ⁺³ ) not more than 100 mg / kg, oil products - not more than 0.5 mg / kg and general hardness not more than 10 mg / kg is sent to the condensate reserve tank, from where it is pumped to the CHPP and the steam boiler room and waste heat boilers, and for correcting the treatment of desalted condensate to a pH of 8.5 - 9.5 and reducing the corrosion of the metal in the pipelines, it is dosed to the collector 1% ammonia solution by metering pumps. 19. The method according to p. 18, characterized in that the clarifying filters used when cleaning the condensate are double-chamber, consisting of a housing, a lower and an upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and an anchor are rigidly attached 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 first stage is 2.5 m with a grain size of 2-6 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 distribution the device is 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 generatrices with a diameter of 8 mm, overlapped by a trough plate slit width of 0.25 - 0.4 mm to avoid contact with the activated carbon in the condensate; when condensate is supplied to the desalination plant, 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 of which 2.6 m in diameter is equipped with upper and lower manholes, fittings for hydroloading and upper and lower distribution devices, the upper of which is made in 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 - beams with holes along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.

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