RU2153079C1 - Heat energy generation process at oil-, oil/gas-, or gas-production enterprise - Google Patents

Abstract

FIELD: thermal engineering; oil, gas, and chemical industries. SUBSTANCE: process involves steam production in at least one steam generator due to at least partial combustion of gaseous fuel and at least some portion of products of raw materials obtained in the course of their extraction, and/or processing, and/or conveying. Novelty is that casing-head gas contained in extracted, and/or processed, and/or conveyed raw material, and/or that escaping during raw material processing is used as at least portion of gaseous fuel; casing-head gas is preheated before combustion to at least 100 C in one or more steam generators supplied with demineralized circulating water and demineralized return steam condensate; demineralization processes for water and steam condensate are combined at least by combining desired process of heat extraction from condensate and at the same time using heat extracted for heating demineralized circulating water. Such arrangement makes it possible to save demineralized water for feeding boilers (reduce its amount from planned 150 to 100-110 cu. m/h) and to do without specifying quality of demineralized water and condensate with respect to silicon content so that demineralizing units incorporating hydrogen-cation and anion exchangers can be replaced by sodium-cation exchangers thereby dispensing with chemically active agents (sulfuric acid and alkali) and using common salt for the purpose. EFFECT: improved economic efficiency end environmental friendliness of process. 14 cl, 1 tbl

Description

 The invention relates to a power system, and can also be used in the oil, gas and chemical industries.

 There are various methods of generating energy (see, for example, SU 1309919 A, 05/05/87, SU 1452490 A, 01/15/89, RU 2126891 C1, 02.27.99).

 The closest to the invention in terms of technical nature and the achieved result is a method of generating thermal and / or electric energy in an oil, oil and gas or gas producing enterprise, comprising generating at least steam in at least one steam generator, obtained at least partly due to the combustion of gaseous fuels and intended including for use, at least in terms of technological processes of processing raw materials at the enterprise (see RU 2090769 C1, 09/20/97).

 The disadvantage of this method is the increased consumption of chemically purified water to power a steam generator, which, complicating the technology, reduces the efficiency of the known method.

 The objective of the present invention is to increase efficiency by reducing the consumption of chemically purified water to power the steam generator, as well as simplifying the work by eliminating the need to standardize the quality of chemically purified water and, therefore, the condensate in silicon content and providing the possibility, at least in terms of technological operations when the condensate is 100% returned to the steam generator, switch from using a desalination plant using hydrogen-cation exchangers and anion exchange filters to sodium-cation exchange filters, that is, to abandon the use of aggressive reagents of sulfuric acid and alkali and switch to the use of sodium chloride.

The problem is solved due to the fact that in the method of generating thermal energy at an oil, oil and gas or gas producing enterprise, including generating at least one steam generator, steam obtained, at least in part, from the combustion of gaseous fuels and, at least at least partially intended including for use, at least in part of the technological processes of extraction, and / or processing, and / or transportation of the extracted raw materials, according to the invention, as at least part of the gaseous fuel and The user passing gas present in the produced and / or processed and / or transported raw materials and / or released during processing of raw materials, and passing the gas prior to combustion is heated to a temperature not lower than 100 ^o C and is burned in the boiler or steam generators which feed water, consisting of chemically purified water introduced into circulation and purified steam condensate, the processes of water purification and steam condensate combining, at least by combining the technologically necessary process of heat extraction from the condensate the sensate with the simultaneous use of the selected heat to heat the chemically purified water introduced into the circulation. At the same time, gas can be supplied with a temperature of mainly 50 - 70 ^o C and a pressure of 3.0 - 5.0 kg / cm ² , while 15 - 40% of the gas is burned in the boiler room of the enterprise, and 60 - 85% - in the technological installations of the enterprise . Raw water can be used from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after purification of the raw water from suspensions and after cleaning the return steam condensate from oil contaminants. They can use water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 mcg / kg, sulfates (SO ₄ ^-2 ) 1 , 78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (Ca ²⁺ ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and oxidizability permanganate 3.84 - 5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to raw water pumps, at least one of which is left standby, and then pumped water through a pair of heat exchangers with fixed tube sheets and heating ayut water to a temperature 25 - 30 ^o C, wherein at least one heat exchanger is used assembled with the premises condensate with temperature 80 - 85 ^o C, wherein the amount of raw water flowing through this heat exchanger is adjusted until the condensation of cooling 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 heating water in accordance and with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters with "regeneration, loaded with sulfonated coal, and carry out the removal of hardness salts from water to 1 - 2 mEq / kg constant and the destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and ion exchange of salts fineness, alkalinity present in the water, and chemical reactions with a hydrogen carbon cation of sulfonated coal, after which softened water is fed to the self-regulating buffer filters loaded with sulfonated carbon to protect the filtrate from acid leakage, and then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and carry out the separation of air with carbon dioxide, which is discharged into the atmosphere, and decarbonized water by gravity into the tank, after which this water is pumped through two-stage pumps Sodium cation filtration filters, in the filters of the first stage, stiffness cations are removed up to 0.1 mEq / kg, and in the second stage, deeper cations of stiffness Ca ⁺² , Mg ^{+2 are} removed to 0.01 mEq / kg and receive chemically purified water with a transparency of at least 40 cm, a total hardness of 2 - 5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 μg / kg and a pH of 8.0, after which chemically purified water is fed into tanks, and then pumped to the steam boiler room with pumps. 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 made in the form of cylindrical vessels with an internal anticorrosive coating, mainly made of epoxy resin, and two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device are placed, which are made in the form of polymer beams 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 stainless steel tubes along the axis of which holes are formed that overlap with casings with slits 0.25 - 0.4 mm wide, and in the upper part of the filter housing they form a hatch for inspecting the surface of the filter material, and in the lower part there is a manhole for mounting and repairing the upper and lower drainage systems, The filter housing at the level of the slit tubes has a fitting for hydroloading, feed water pipes, loosening, air vents of the upper and lower drainage systems to the filter, pressure gauges at the inlet and outlet of the collector, samplers and valves, and the filter backfill operate bilayer consisting of the layer of quartz sand of 700 mm and a volume of 6.4 m ³ and a layer of anthracite height of 500 mm and a volume of 4.6 m ^3, the filter performance is prescribed in view of the water consumption by preparation and regeneration solutions are not less than 200 m ³ hours, the filtration rate during operation of all filters is not less than 7 m / h and 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, and the filter is equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the water flow over the surface of the filter material systems, and the inner surface of the filter is performed with a rubber gum coating, while the filter performance is assigned at least 80 t / h and the filtering speed is at least 13 m / h; the used buffer filters are loaded with sulfonated coal with a loading layer height of 2000 mm and are self-regenerating, with an upper dispenser in the form of a "glass in a glass", moreover, the performance of one filter is assigned at least 180 m ³ / h and the filtering speed is at least 25 m / h ; the used decarbonizer is filled with Rashig rings and is performed with the lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to the collection tank for this water with a capacity of at least 400 m ³ ; The sodium-cation exchange filter used is performed in two stages with an upper one consisting of beams and a lower distribution device, the first stage of this filter being made up of three filters with a diameter of 3000 mm and loaded with filter material with a layer height of 1900 mm to replace Ca ^{+ 2} , Mg ^{+ 2} cations on the hydrogen cation H ⁺ , while the filter performance is assigned at least 90 m ³ / h, and the filtration rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is performed one of the two filters with a diameter of 2600 mm, is loaded with filter material with a layer height of 1200 mm, the filter is equipped with an upper switchgear, the filtering speed is set at least 34 m / h and the cations of hardness Ca ⁺² , Mg ⁺² are removed to 0.01 mEq / kg, while in all ion-exchange filters for chemical water treatment on the lower drainage device there is an underlying layer of anthracite with a height exceeding the level of the arrangement of beams with perforation by at least 10 cm. Chemically purified water can be fed to steam a boiler room with a temperature of 25 - 30 ^o C, whereby part of the chemically purified water is directed 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, which uses condensate heat, coming from the plants of the enterprise, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed to the deaerator head, and the other is fed to the continuous purge cooler using heat waste water from the continuous purge separator, and then chemically purified water is passed through a deaerator vapor cooler, and then it is supplied to the deaerator head and the chemical water is bubbled with steam, heating it to a temperature close to saturation, and O ₂ gases are removed from the water, CO _2, and network heating water supplied to suction line pumps, and then through a network of water heaters in the heating system of the enterprise, with the repair of chemically purified water heaters carried switching heaters etevoy water for heating chemically purified water. Steam from boilers through collectors can be supplied to steam pipelines of an enterprise for technological needs, and part of the steam from collectors is supplied through a reducing device with a pressure of P = 4 kgf / cm ² to a network water heater, a chemically purified water heater, a fuel gas heater, and heating fuel gas separator and deaerators. If there is an excess of crushed steam at the enterprise, part of the crushed steam can be fed to chemically treated water heaters and network water heaters, and the condensate is sent to them in condenser tanks, from where they are pumped out by condenser pumps for condensate treatment. During operation of the chemically purified water heater and network water heaters using reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^° C 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 it is cooled 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 production condensate from the plants of the enterprise and a steam boiler room is piped to a distribution comb, and condensate with a total hardness of 100 μg-eq / kg, Fe content in terms of Fe ₃ up to 180 μg / kg is used, acid content of silicon SiO ₂ -. 350 .mu.g / kg, oil content to 80 mg / kg and pH value to 8.0 units, wherein when said discrepancy condensate parameters it is sent to the drain, and the junction with the condensate directed comb placentas specifically, a settling tank and a collection tank of pure condensate separated from oil products are collected in the tank, and as the condensate floats up onto the surface of the oil particles, it is collected using a collecting funnel regulated at least once per shift, while both tanks maintain a predetermined volume of liquid per due to the difference in the levels of overflow troughs - filling nozzles, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed to those processing and loosening the filters of the three stages of de-oiling, on clarification filters loaded with anthracite, in which the suspended mechanical particles and “oil products” are removed to 4–5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which are interconnected in parallel and loaded with activated carbon, and then on four sorption filters of the second stage of de-oiling the condensate until the content of “oils” in it is not more than 0.05 mg / kg, and then the oil-free condensate at a rate Aturi 85 ^o C fed to the shell space of heat exchangers, through which is passed the cold tap water used for process needs demineralizer and carry condensate cooling to a temperature of 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting unit, wherein the temperature of the oil-free condensate is maintained in the range from 35 ^o C to 40 ^o C and first sent to hydrogen-cation exchange filters, in which, as a filter material, comfort of a highly basic KU-2.8 cation exchanger with a loading layer height of 1.5 m and a filtering speed of 35 m / h, in which stiffness cations and iron are retarded, and periodically, the exchange ability of the filters is restored by regenerating the filter material with a 3 - 4% sulfuric solution acid, and after hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as a filter material and the condensate is removed from the silicic acid compounds, They periodically restore the exchange capacity of anion exchange filters by passing a 3–5% sodium hydroxide solution through the filter layer of anion exchange resin, and after the anion exchange filters, purified condensate with silicic acid content of not more than 150 μg / kg, iron (in terms of Fe ⁺³ ) not more than 100 μg / kg, of petroleum products - not more than 0.5 μg / kg and with a total hardness of not more than 10 μg / kg, is sent to the condensate reserve tank, from where it is pumped mainly to the thermal power station and steam boiler room, as well as to the sulfur unit and boilers - utilizers, and for corrective treatment of desalted condensate to a pH value of 8.5 - 9.5 units. and to reduce the corrosion of the metal pipelines, a 1% ammonia solution is dispensed into the collector by metering pumps. The clarification filters used in condensate cleaning can be double-chamber, consisting of a housing and a lower and upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and tubular anchors are connected rigidly inside the housing, and air is removed from the lower chamber to the upper and maintaining in the chambers of general pressure, while the upper drainage distribution device is 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 assumed to be 0.9 m with a grain size of 2-6 mm, and when filling the filter with filter material, it is first placed in the lower chamber and then in the upper and lower switchgear are in the form of a collector to which thirty-two beams with slotted holes 0.25 - 0.4 mm wide are attached, which are closed with perforated plates to prevent entrainment of the filter material; Four single-chamber filters are used as sorption filters of the first stage, which are connected to each other in parallel and loaded with filter material — activated carbon with a layer thickness of 2.5 m and a grain size of 2 to 6 mm, and the filters are equipped with upper and lower distribution devices, the upper of which are made in the form of rays 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 in which horizontally arranged days y and which is inserted in the distribution tubes with holes along the lower generatrix of 8 mm diameter which overlap the trough-like plate welded with a gap width of 0.25 - 0.4 mm to avoid contact with the activated carbon in the condensate; when condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; hydrogen-cation exchange and anion exchange filters are designed as single-chamber cylindrical apparatuses having a capacity of 115 m ³ / h, each of which 2.6 m in diameter is equipped with upper and lower manholes, fittings for hydroloading and upper and lower switchgears, the upper of which are in the form of a “glass in a glass”, and the lower one in the form of a collector into which the distribution tubes are inserted — beams with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide. In the case of the formation of a slit hole at the weld point of the trough plate to prevent entrainment of the filter material, a litter layer of coarse anthracite can be spread over the entire surface of the filter with a height of 10 cm to the lower switchgear of the sorption filters.

The technical result provided by the above set of features is to increase the efficiency of production by saving labor and material costs due to savings in the consumption of chemically purified water for boiler supply (from the planned 150 m ³ / h to 100 - 110 m ³ / h), as well as improvement of the environmental situation at the enterprise and surrounding territories due to the fact that it becomes possible to eliminate the need to standardize the quality of chemically treated water and condensate by silicon content, which makes it possible at 10 With a 0% return of condensate to the steam generator, switch from the need to use a desalination plant using hydrogen-cation exchange and anion exchange filters to sodium-cation exchange filters, and, therefore, it is possible to refuse the use of aggressive reagents: sulfuric acid and alkali and switch to the use of sodium chloride .

 The method is as follows.

At least one steam generator is produced in steam, obtained at least partially by burning gaseous fuels and at least partially intended for use, at least in part, in production processes, and / or processing and / or transportation of extracted raw materials. As at least part of the gaseous fuel, associated gas is used which is found in the produced and / or processed and / or transported raw materials and / or released during processing of the raw materials. Associated gas before combustion is heated to a temperature not lower than 100 ^o C and burned in a steam generator or steam generators, which feed water consisting of chemically purified water introduced into the circulation and purified steam return condensate. The processes of water purification and steam condensate are combined, at least by combining the technologically necessary process of heat extraction from the condensate with the simultaneous use of the extracted heat to heat the chemically purified water introduced into the circulation.

Gas is supplied with a temperature of mainly 50 - 70 ^o C and a pressure of 3.0 - 5.0 kg / cm ² , while 15 - 40% of the gas is burned in the boiler room of the enterprise, and 60 - 85% - in the technological installations of the enterprise.

Raw water is used from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after purification of the raw water from suspensions and after cleaning the return steam condensate from oil contaminants, in particular, water is used 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 mcg / kg, sulfates (CO ₄ ^-2 ) of 1.78 mg -eq / kg, silicas 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq / kg, ma decay (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84 - 5.12 mg / kg O ₂ . Raw water for chemical cleaning is supplied under pressure up to 5 kg / cm ² to raw water pumps, at least one of which is left standby, and then water is pumped through a pair of heat exchangers with fixed tube sheets and the water is heated to a temperature of 25 - 30 ^o C At least one heat exchanger uses condensate collected from the territory of the enterprise with a temperature of 80-85 ^o C, while the amount of raw water passed through this heat exchanger is controlled before cooling the condensate to a temperature of 25 - 35 ^o C, and the rest of A swarm of 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. After heating, the water is sent for filtration to mechanical filters with a two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters with a "hungry" regeneration loaded with sulfonated coal and carry out the removal of hardness salts from water to 1 - 2 mEq / kg constant and the destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and ion exchange of hardness salts, alkali spine, existing in water, and chemical reactions with hydrogen cation sulfonated coal. After that, 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 decarbonized water by gravity to the tank. Then, this water is pumped through the pumps through two-stage sodium cation filters, in the filters of the first stage, hardness cations up to 0.1 mEq / kg are removed, and in the second stage, deeper cations of hardness Ca ⁺² , Mg ^{+2 are} removed to 0, 01 mEq / kg and get chemically purified water with a transparency of at least 40 cm, a total hardness of 2-5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 mcg / kg and a pH of 8.0, after which chemically purified water is supplied to the tanks, and then pumped to the steam boiler room with pumps.

At least during the flood period, water is pre-treated, 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, two coagulant measuring tanks of 10 m ³ each, and wet lime storage cells , 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. Chemical purification of water is carried out only using sodium-cation filters, in which they also regenerate the filter material with saline solution with a concentration of 6-8%.

The mechanical filters used for chemical water purification are made in the form of cylindrical vessels with an internal anticorrosive coating, mainly of epoxy resin, and two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device, which are made in the form of polymer beams, are placed 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 stainless steel tubes along the axis which holes are formed that overlap with casings with slits 0.25 - 0.4 mm wide. 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 manhole for installation and repair of the upper and lower drainage systems. On the filter housing, at the level of the slit tubes, a fitting for hydroloading is located, feed water pipes, loosening, air vents of the upper and lower drainage systems are connected to the filter, pressure gauges at the inlet and outlet of the collector, samplers and valves are connected. The filtering filling is performed in two layers, consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and a layer of anthracite with a height of 500 mm and a volume of 4.6 m ³ . The performance of the filters is prescribed taking into account the flow rate of water 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 at least 7 m / h and the maximum during loosening washing is at least 10 m / h at a flow rate for loosening compressed air 5 m ³ / h and pressure up to 1.5 kgf / cm ² . Used hydrogen-cation exchange filters are performed with a filtration area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm. The filter is equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the flow of water over the surface of the filtering material of the system, and the inner surface of the filter is made with a rubber gum coating. The filter performance is prescribed at least 80 t / h, and the filtering speed - at least 13 m / h. The buffer filters used are charged with sulfonated coal with a loading layer height of 2000 mm and are self-regenerating, with an upper dispenser in the form of a glass in a glass. The performance of one filter is prescribed at least 180 m ³ / h, and the filtering speed - at least 25 m / h. The used decarbonizer is filled with Raschig rings and is performed with the lower air supply pipe, a spray separator and a decarbonized water pipe that is connected to the collection tank for this water with a capacity of at least 400 m ³ . Used sodium cation exchange filter is performed in two stages with an upper, consisting of beams and lower distribution devices. The first stage of this filter is made of three filters with a diameter of 3000 mm and is loaded with filter material with a layer height of 1900 mm to replace the Ca ^{+ 2} , Mg ^{+ 2} cations with the H ⁺ hydrogen cation. The filter performance is prescribed not less than 90 m ³ / h, and the filtering rate - not less than 25 m / h and stiffness cations are removed up to 0.1 mEq / kg. The second stage of the filter is made of two filters with a diameter of 2600 mm, is loaded with filter material with a layer height of 1200 mm, the filter is equipped with an upper distribution device. At the same time, a filtration rate of at least 34 m / h is prescribed and stiffness cations Ca ⁺² , Mg ⁺² are removed to 0.01 mEq / kg. In all ion-exchange filters for chemical water purification, an underlying layer of anthracite with a height exceeding the level of the arrangement of beams with perforation by at least 10 cm is located on the lower drainage device.

Chemically purified water is fed to the steam boiler room with a temperature of 25 - 30 ^o C. 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 a gravity condensate cooler, in which the heat of the condensate from the plant’s units is used, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed to the deaerator head, and the other is fed to a continuous purge cooler using the heat of the purge water from the continuous purge separator. Then, chemically purified water is passed through a deaerator vaporizer cooler, and then it is supplied to the deaerator head and the chemically purified water is bubbled with steam, heating it to a temperature close to saturation, and O ₂ , CO gases are removed from the water. Network heating water is fed to the inlet of the network pumps, and then through the network water heaters to the heating system of the enterprise. When repairing chemically purified water heaters, the network water heaters are switched to the heating of chemically purified water.

Steam from boilers for collectors is supplied to the enterprise steam pipelines for technological needs. 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 to deaerators.

 In the presence of excess crushed steam at the enterprise, part of the crushed steam is fed to chemically treated water heaters and network water heaters, and the condensate is sent to them in condenser tanks, from where they are pumped out by condenser pumps for condensate treatment.

During operation of the chemically purified water heater and network water heaters using reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^° C is sent directly to the deaerator head to replace an equivalent amount of heated chemically purified water.

The heaters of the network and chemically treated water are in the form of a block of steam-water and water-water heat exchangers. Initially, steam is condensed in a steam-water heat exchanger, while the level of condensate in the heat exchanger is maintained by a level controller. Then the condensate is sent to a water-water heat exchanger and it is supercooled to a temperature of 80 - 90 ^o C. 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 is used as a steam generator, and production condensate from the facilities of the enterprise and a steam boiler room is piped to a distribution comb. The condensate is used with a total hardness of 100 μg-eq / kg, Fe content in terms of Fe ₃ to 180 μg / kg, silicon acid SiO ₂ - up to 350 μg / kg, oil content up to 80 μg / kg and pH up to 8, 0 units 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 sump tank and the collection tank of pure condensate separated from the oil products. As the condensate emerges when the condensate settles to the surface of the oil particles, it is collected using a collecting funnel regulated at least once per shift. Both tanks maintain a given volume of fluid due to the difference in the levels of overflow troughs - filling nozzles. After that, pure condensate with a petroleum product content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of the filters of three de-oiling levels, for clarification filters loaded with anthracite, in which suspended mechanical particles are removed and "petroleum products" up to 4 - 5 mg / kg. After this, the condensate is sent to four sorption filters of the first stage, which are connected together in parallel and loaded with activated carbon, and then to four sorption filters of the second stage of decontamination of the condensate until the oil content in it is not more than 0.05 mg / kg. Then the oil-free condensate with a temperature of 85 ^o C is sent to the annular space of the 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 that, it is sent to the oil-free condensate tank, from where the condensate is pumped by pumps on a desalination plant. The temperature of the oil-free condensate is maintained in the range from 35 ^° C to 40 ^° C and it is first sent 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 filtering speed of 35 is used m / h, in which stiffness cations and iron are retained, moreover, the exchange ability of the filters is periodically restored by regenerating the filter material with a 3-4% sulfuric acid solution, and after hydrogen-cation exchange filters al is directed to anion filter, in which a filtering material is a highly basic anion exchanger AB-17-8 and produce condensate removal silica compounds. Periodically, the exchange capacity of the anion exchange filters is restored by passing a 3-5% solution of sodium hydroxide through the filter layer of anion exchange resin. After anion exchange filters, purified condensate with a content of silicic acid of not more than 150 μg / kg, iron (in terms of Fe ⁺³ ) not more than 100 μg / kg, of petroleum products - not more than 0.5 μg / kg and a total hardness of not more than 10 μg / kg, they are sent to the condensate reserve tank, from where they are pumped mainly to the CHPP and the steam boiler room, as well as to the sulfur unit and to the waste heat boilers. For corrective treatment of desalted condensate to a pH value of 8.5 - 9.5 units. and reducing corrosion of metal pipelines, a 1% ammonia solution is dosed into the collector by metering pumps.

The clarification filters used in condensate cleaning are double chamber, consisting of a housing and lower and upper drainage distribution devices. Inside the case, a blank flat horizontal partition is rigidly fixed, dividing it into two chambers, and tubular anchor connections, through which air is vented from the lower chamber to the upper one and the pressure in the chambers is maintained. The upper drainage distribution device is made in the form of a funnel for uniform distribution of condensate on the surface of the filter material, which is used anthracite, the layer height of which in one chamber is assumed to be 0.9 m with a grain size of 2-6 mm. When filling the filter with filter material, it is first laid in the lower chamber, and then in the upper, and the lower distribution device is made in the form of a collector to which thirty-two beams with slotted holes 0.25 - 0.4 mm wide are closed, which are closed with perforated plates to prevent entrainment of filter material. Four single-chamber filters are used as sorption filters of the first stage, which are connected together in parallel and loaded with filter material - activated carbon with a layer thickness of 2.5 m and a grain size of 2 to 6 mm. 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 device is in the form of a collector, which is placed horizontally on the bottom and into which distribution pipes with holes are inserted along the lower forming diameter 8 mm, which is overlapped by a weld-in trough plate with a slit 0.25 - 0.4 mm wide to prevent activated carbon from entering the condensation t When condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} . Hydrogen-cation exchange and anion exchange filters are made in the form of single-chamber cylindrical apparatuses having a capacity of 115 m / ³ h, each of which 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 performed 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.

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

 The method is illustrated by the example presented in the table.

 The production of own steam ensures a reduction in the cost of produced petroleum products by reducing its price compared to purchased steam by up to 50%, increases the reliability of providing the enterprise with steam, ensures the rational use of fuel gas, and reduces losses in oil production.

 The generated steam is used as a coolant, for heating industrial and domestic premises, for spraying fuel gas during flaring, during equipment preparation, for fire purposes, for generating electricity, which is further used for pump drives, lighting, industrial and domestic needs, for rotating boring tools.

Claims (14)

1. A method of generating thermal energy in an oil, oil and gas or gas producing enterprise, comprising generating at least one steam generator of steam obtained at least partially by burning gaseous fuels and at least partially intended including for use, at least in part of the technological processes of processing the extracted raw materials, characterized in that as at least part of the gaseous fuel, associated gas is used in the produced and / or processed, / or transportable feedstock and / or released during processing of raw materials, and passing the gas prior to combustion is heated to a temperature not lower than 100 ^o C and is burned in the boiler or steam generators which feed water consisting of injected into circulation chemically purified water and purified return steam condensate, moreover, the processes of water purification and steam condensate combine, at least by combining the technologically necessary process of heat extraction from the condensate with the simultaneous use of the selected heat for heating introduced into circulation chemically purified water. 2. The method according to claim 1, characterized in that the gas is supplied with a temperature of mainly 50 - 70 ^o C and a pressure of 3.0 - 5.0 kg / cm ² , while 15 - 40% of the gas is burned in the boiler plant, and 60 - 85% - in the technological installations of the enterprise.  3. The method according to claim 1, characterized in that they use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after purification of the raw water from suspensions and after purification of return steam condensate from oil pollution. 4. The method according to any one of claims 1 and 3, characterized in that water from the Ural River is used with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and iron content 628 mcg / kg, sulfates (SO ₄ ² ) 1.78 mEq / kg, silicic acid 0.15 mcg eq / kg, calcium (Ca ² ) 3.0 mEq / kg, magnesium (Mg ² ) 1.8 μg-eq / kg, and permanganate oxidation 3.84 - 5.12 O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to the noses of raw water, at least one of which are left standby, and then pumped water through a pair of heat exchangers with GOVERNMENTAL tubular grates and preheated water up to 25 - 30 ^o C, wherein at least one heat exchanger is used assembled with the premises condensate with temperature 80 - 85 ^o C, wherein the amount of raw water flowing through this heat exchanger is adjusted to of cooling condensate to 25 - 35 ^o C, and the rest of the raw water is passed through another heat exchanger and heated to 25 - 30 ^o C due to the use of heating water in this heat exchanger with a heating water temperature corresponding to and with the season, and after heating, the water is sent for filtration to mechanical filters with a two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, then the clarified water is fed to hydrogen-cation exchange filters with a “hungry” filter regeneration, loaded with sulfonated coal, and carry out the removal of hardness salts from water to 1-2 μg-eq / kg constant and destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 μg-eq / kg and ion exchange of salts fineness, alkalinity present in the water, and chemical reactions with a hydrogen carbon cation of sulfonated coal, after which softened water is fed to the self-regulating buffer filters loaded with sulfonated carbon to protect the filtrate from acid leakage, and then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and carry out the separation of air with carbon dioxide, which is discharged into the atmosphere, and decarbonized water by gravity into the tank, after which this water is pumped through two-stage pumps the sodium cation filtration, in the filters of the first stage, stiffness cations are removed to 0.1 μg-eq / kg, and in the second stage, deeper cations of hardness Ca ⁺² , Mg ^{+2 are} removed to 0.01 μg-eq / kg and receive chemically purified water with a transparency of at least 40 cm, a total hardness of 2 - 5 μg-eq / kg, iron content in terms of Fe ³ up to 300 μg / kg and a pH of 8.0, after which chemically purified water is fed into tanks, and then pumped to the steam boiler room. 5. The method according to any one of claims 1, 3 and 4, characterized in that, at least during the flood period, a preliminary purification of water is carried out, which is performed using at least two clarifiers with a capacity of 250 m ³ / h, two mixers of milk of lime with a capacity of 15 m ³ each, two coagulant measuring tubes of 10 m ³ each, wet lime storage cells, mainly lime dough with a capacity of 100 m ³ , lime milk cells with a capacity of 60 m ³ and metering pumps and / or centrifugal pumps with additional control valves, and chemical ical produce only water purification using sodium cation filters, which also produce regeneration of the filter material with the concentration of brine 6 - 8%. 6. The method according to any of claims 4 and 5, characterized in that the mechanical filters used for chemical water purification are made in the form of cylindrical vessels with an internal anti-corrosion coating, mainly of epoxy resin, and two spherical steel bottoms, in the upper of which are placed the source of water supply and the upper distribution device, which is made in the form of beams of polymer material to distribute water along the filter cross section, and a drainage system in the form of a collector is located on the lower bottom with slotted stainless steel tubes, along the axis of which holes are formed that overlap with casings with slits 0.25 - 0.4 mm wide, and in the upper part of the filter housing form a hatch for inspecting the surface of the filter material, and in the lower part there is a hole for mounting and repair of the upper and lower drainage systems, while on the filter housing at the level of the slit tubes there is a fitting for hydroloading, feed water pipes, loosening, an air vent of the upper and lower drainage systems to the filter, pressure gauges at the inlet and Exit manifold valves and samplers, and the filter operate filling bilayer consisting of the layer of quartz sand of 700 mm and a volume of 6.4 m ³ and a layer of anthracite height of 500 mm and a volume of 4.6 m ^3, the filter performance is assigned with the flow water 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 at least 7 m / h and the maximum during loosening washing is at least 10 m / h at a flow rate of 5 m for loosening compressed air ³ / h and pressure up to 1.5 kgf / cm ² ; the hydrogen-cation exchange filters used 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 equipped with an upper distribution device, which is made in the form of a beam that evenly distributes the water flow over the surface of the filtering material of the system and the inner surface of the filter is made with a rubber gum coating, while the filter performance is assigned at least 80 t / h and the filtering speed is at least 13 m / h; the used buffer filters are loaded with sulfonated coal with a loading layer height of 2000 mm and are self-regulating, with an upper dispenser in the form of a "glass in a glass", moreover, the performance of one filter is assigned at least 180 m ³ / h and the filtering speed is at least 25 m / h ; the used decarbonizer is filled with Rashig rings and is performed with the lower air supply pipe, a spray separator and a decarbonized water pipe, which is connected to the collection tank for this water with a capacity of at least 400 m ³ ; The sodium-cation exchange filter used is performed in two stages with an upper, consisting of rays, and lower distribution devices, the first stage of this filter being made up of three filters with a diameter of 3000 mm and loaded with filter material with a layer height of 1900 mm to replace the cations Ca ^{+ 2} , Mg ^{+ 2} to the hydrogen cation H ⁺ , while the filter performance is assigned at least 90 m ³ / h, and the filtering rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is performed composite two filters 2600 mm diameter was charged with a filter material layer height of 1200 mm, equipped with a filter upper distribution device, wherein the prescribed filtration rate of at least 34 m / h, and the removal is carried hardness cations Ca ^+2, Mg ⁺² to 0.01 mg -eq / kg, while in all ion-exchange filters for chemical water purification on the lower drainage device there is an underlying layer of anthracite with a height exceeding the level of the arrangement of rays with perforation by at least 10 cm. 7. The method according to claim 1, characterized in that the chemically purified water is supplied to a steam boiler room with a temperature of 25-30 ^° C, and part of the chemically purified water is sent to continuous and batch boiler product sampling coolers, and from there to the deaerator head, another part of the chemically purified water is sent to a gravity condensate cooler, in which the heat of the condensate from the plant’s units is used, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed to the deaeration head a torus, 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, and then it is supplied to the deaerator head and the chemical water is bubbled with steam, heating it to a temperature, close to saturation, and water is removed from the gases O _2, CO, and network heating water supplied to suction line pumps, and then through a network of water heaters in the heating system of the enterprise, while the repair heati ers chemically purified water is carried switching network water heaters for heating the chemically treated water. 8. The method according to p. 1, characterized in that the steam from the boilers through the collectors is fed into the steam pipelines of the enterprise for technological needs, and part of the steam from the collectors through a reducing device with a pressure of P = 4 kgf / cm ^{2 is} fed to the network water heater, to the heater chemically purified water, to the fuel gas heater, to heat the fuel gas separator and to deaerators.  9. The method according to claim 7, characterized in that in the presence of excess crushed steam at the enterprise, part of the crushed steam is fed to chemically treated water heaters and to network water heaters, and the condensate is sent to condenser tanks in them, from where they are pumped to the condensate pump by condenser pumps. 10. The method according to claim 9, 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. 11. The method according to any one of claims 9 and 10, characterized in that the heaters of the network and chemically treated water are 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 condensate level in the heat exchanger is supported by a level controller, then the condensate is sent to a water-water heat exchanger and supercooled to 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. 12. The method according to claim 1, characterized in that a steam boiler room is used as a steam generator, and production condensate from the plants of the enterprise and a steam boiler house is piped to a distribution comb, and condensate with a total hardness of 100 mEq / kg, Fe content is used in terms of Fe ₃ up to 180 μg / kg, silicon content of SiO ₂ acid - up to 350 μg / kg, oil content up to 80 μg / kg and pH up to 8.0, and if the condensate does not correspond to the specified parameters, it is sent to the drain, and with distributor comb Sats are sent sequentially to the sump tank and the tank for collecting pure condensate separated from oil products, and as the condensate floats up to the surface of the oil particles, it is collected using a collecting funnel regulated at least once per shift, while both tanks maintain a predetermined volume liquids due to the difference in the levels of overflow troughs - filling pipes, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of filters of three stages of de-oiling, for clarification filters loaded with anthracite, in which the suspended mechanical particles and "oil products" are removed to 4-5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which interconnected in parallel and loaded with activated carbon, and then on four sorption filters of the second stage of decontamination of the condensate until the content of “oils” in it is not more than 0.05 mg / kg, and then dehydrated enny condensate at a temperature of 85 ^o C fed to the shell space of heat exchangers, through which is passed the cold tap water used for process needs demineralizer and, cooling the condensate to a temperature of 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting installation, and the temperature of the oil-free condensate is maintained in the range from 35 - 40 ^o C and sent first to hydrogen-cation exchange filters, in which as a filter of the material used, KU-2.8 highly basic cation exchanger with a loading layer height of 1.5 m and a filtering speed of 35 m / h, in which stiffness cations and iron are retarded, periodically, the exchange ability of the filters is restored by regeneration of the filtering material 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 condensate is removed by silicic acid, moreover, periodically restore the exchange capacity of anion exchange filters by passing through a filter layer of anion exchange resin a 3 - 5% solution of sodium hydroxide, and after anion exchange filters, purified condensate with a content of silicic acid of not more than 150 μg / kg of iron (in terms of Fe ^{+ 3} ) not more than 100 μg / kg, oil products - not more than 0.5 μg / kg and with a total hardness of not more than 10 μg / kg are sent to the condensate reserve tank, from where they are pumped mainly to the thermal power station and steam boiler room, as well as to the sulfur installation and boilers - utilizers, and for correcting the treatment of demineralized condensate to a pH of 8.5 - 9.5 and reducing the corrosion of the metal in the pipelines, a 1% ammonia solution is dispensed into the collector by metering pumps. 13. The method according to p. 12, characterized in that the clarification filters used in the condensate cleaning are double chamber, consisting of a housing and a lower and upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and tubular anchors are rigidly attached communication, through which the air is vented from the lower chamber to the upper and maintaining the total pressure in the chambers, while the upper drainage distribution device is in the form of a funnel for uniform distribution of condensate on the surface of the filter material, which is used anthracite, the layer height of which in one chamber is assumed to be 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, they are 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 filter material; As sorption filters of the 1st stage, four single-chamber filters are used, which are connected in parallel and loaded with filter material - activated carbon with a layer thickness of 2.5 m and a grain size of 2-6 mm, and the filters are equipped with upper and lower distribution devices, the upper of which performed in the form of beams for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower distribution device in the form of a collector in which the bottom is horizontally placed and which is inserted distribution tubes with holes along the lower generatrix of 8 mm diameter which overlap privarivaemo trough plate with a gap width of 0.25 - 0.4 mm to avoid contact with the activated carbon in the condensate; when condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; hydrogen-cation exchange and anion exchange filters are designed as 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 are 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, overlapping plates with a slit 0.25-0.4 mm wide.  14. The method according to p. 13, characterized in that in the case of the formation of a slit hole at the weld point of the trough plate to prevent entrainment of the filter material, a litter layer of coarsely crushed anthracite is poured onto the lower distribution device over the entire surface of the filter 10 cm high.

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