RU2149266C1 - Method for producing and utilizing steam at oil- or gas-, or oil-and-gas-extracting plant - Google Patents

Abstract

FIELD: thermal engineering, oil, gas, and chemical industries. SUBSTANCE: method involves combustion of gaseous fuel and steam production in at least one steam generator, at least part of generated steam being used in at least some of extraction, and/or treatment, and/or conveying processes for raw materials, as well as feeding steam generator with chemically treated water additionally passed through circulating loop. Novelty is that at least part of gaseous fuel is oil gas contained in raw material and/or combustion process gas emitted in the course of processing raw material and/or intermediate products; gas burned in steam generator amounts to 15-40%; and that in process plants of enterprise, to 60-85%; chemically treated water is additionally introduced in circulation loop by adding it to cooled- down and cleaned return condensate and heated by thermal energy released in the process of residual heat extraction from return condensate while cleaning it. All these measures have made it possible to reduce labor and material consumption due to lower consumption of chemically treated water for boiler feeding (100-110 cu. m/h compared with 150 cu. m/h planned), make it unnecessary to normalize quality of chemically treated water and condensate used for boiler feeding with respect to silicon content which enables dispensing with demineralizing plant using hydrogen/cation and anion exchangers by replacing them with sodium/cation exchangers and so to obviate need of using chemically active agents (sulfuring acid and alkali) by replacing them with common salt. EFFECT: improved economic efficiency and 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 ways of generating steam (see, for example, Semenenko N.A., Sidelkovsky L.N., Yurenev V.N. Boiler plants of industrial enterprises, Moscow, Leningrad, State Energy Publishing House, 1960, pp. 229-240).

 The closest to the invention in technical essence and the achieved result is a method for producing and selling steam at an oil or gas or oil and gas producing enterprise, including burning gaseous fuels and generating at least one steam generator, at least part of which is used at least in terms of technological processes of extraction, and / or processing, and / or transportation of extracted raw materials and supplying a steam generator with chemically purified water additionally put into circulation (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 for producing and selling steam at an oil or gas or oil and gas producing enterprise, including burning gaseous fuels and generating at least one steam generator, at least part of which is used, at least as far as technological processes of extraction and / or processing, and / or transportation of extracted raw materials and steam generator feed are additionally put into circulation with chemically purified water, according to the invention as at least part of the gaseous livas use associated gas contained in the raw materials and / or fuel process gas released during the processing of raw materials and / or intermediate products, with 15-40% of the gas burned in a steam generator, and 60-85% in the technological installations of the enterprise, and chemically The purified water is additionally put into circulation by adding to the technologically cooled purified return condensate and heating it with the heat energy released in the technologically necessary process of selecting the residual heat of the return condensate in the process of purification ki last.

Gas can be supplied with a temperature of mainly 20-70 ^o C and a pressure of 3.0-5.0 kg / cm ² , and before combustion can be heated to a temperature of at least 100 ^o C.

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 pollution, in particular 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 μg / kg, sulfates (SO ₄ ^-2 ) of 1.78 meq / kg of silicic acid of 0.15 meq / kg, calcium (Ca ⁺²⁾ 3,0 mg-eq / k , Magnesium (Mg ⁺²⁾ 1,8 mg-eq / kg, and permanganate oxidability 3,84-5,12 mg / kg of O _2, wherein the raw water to the chemical cleaning is fed under pressure to 5 kg / cm ² at the pumps raw water, at least one of which is left standby, and then pumped water through a pair of heat exchangers with fixed tube sheets and heated water to a temperature of 25-30 ^o C, and at least one condensate collected from the territory of the enterprise is used with a temperature of 80-85 ^o C, while the amount of raw water passed through this heat exchange nnik, they are regulated until the condensate cools to a temperature of 25-35 ^o C, and the rest of the raw water is passed through another heat exchanger and heated to a temperature of 25-30 ^o C due to the use of heating water in this heat exchanger having a heating water temperature of in accordance with the season, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and the suspended particles are removed from the water until the water reaches transparency less than 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters with a "hungry" regeneration loaded with sulfonated coal, and hardness salts are removed from the water to 1-2 mEq / kg constant and the bicarbonate ion is destroyed with only carbonate alkalinity reduced to 0.7 mEq / kg and ion exchange of hardness, alkalinity salts present in water and chemical reactions with hydrogen sulfide carbon cation, after which softened water is fed to self-regulating buffer filters, which protect the filtrate from acid leakage, loaded sulfonated carbon, and then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and air is separated with carbon dioxide, which is taken into the atmosphere, and decarbonized water by gravity into the tank, after which this water is pumped through pumps through two-stage sodium cation filters , in the filters of the first stage, stiffness cations up to 0.1 mEq / kg are removed, and in the second stage, deeper cations of stiffness Ca ⁺² , Mg ⁺² are removed to 0.01 mEq / kg and chemically obtained 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 fed into tanks, and then pumped to the steam boiler room.

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-cationic filters, which also regenerate the filter material with saline solution with a concentration of 6-8%.

The mechanical filters used for chemical water purification can be 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 rays from a polymeric material for distributing water over the filter cross section, and on the lower bottom there is a drainage system in the form of a collector with slotted 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 hole for mounting and repairing the upper and lower drainage systems, at the same time, a fitting for hydroloading is placed on the filter housing at the level of the slit tubes, the source water pipes, loosening, the 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, filtering 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 assigned with the flow of water on its own needs and preparation of regeneration solutions - at least 200 m ³ / h, the filtration rate during operation of all filters is at least 7 m / h and the maximum during loosening washing is at least 10 m / h at a flow rate for loosening of compressed air of 5 m ³ / h and pressure up to 1 5 kgf / cm ² ; 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, 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 filtration rate is not less than 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is performed comp implicit 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 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 a steam boiler room with a temperature of 25-30 ^o C, and part of the chemically purified water is sent to the sampling coolers for continuous and periodic blowing of the boilers, and from there to the deaerator head, another part of the chemically purified water is sent to the gravity condensate cooler, wherein in use the heat of condensation coming from the company facilities, and exiting the coolant water is separated into two streams, one of which is heated to 90 ^o C, is fed into the head of the deaerator, and the other serves to cool continuous purge spruce using 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 fed to the deaerator head and steam is bubbled through chemically purified water, heating it to a temperature close to saturation, and removed of water ₂ O gas, 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 heaters chemically cleaned in dy carried switching network water heaters for heating the chemically treated 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.

 In the presence of excess crushed steam at the enterprise, part of the crushed steam can be supplied to chemically treated water heaters and network water heaters, and 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 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 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 to 350 mg / kg, oil content to 80 mg / kg and pH value to 8.0 u, and by the non-condensing these parameters it is sent to the drain, and the junction with the condensate directed combs sequence it is necessary to separate the tank into the tank and the tank for collecting pure condensate separated from oil products, and as the condensate floats up onto the surface of the oil particles, it is collected using a collecting funnel 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 μg / kg is pumped through the control unit, in which the flows are distributed to those the biological treatment and loosening of filters of three stages of de-oiling, on clarification filters loaded with anthracite, in which suspended mechanical particles and "oil products" are removed to 4-5 μg / 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 μg / 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 carried condensate cooling to a temperature of 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting unit, wherein deoiled condensation temperature is maintained between 35 to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the filter material using t highly basic KU-2.8 cation exchanger with a loading layer height of 1.5 m and a filtration speed of 35 m / h, in which stiffness cations and iron are retarded, and periodically, the exchange ability of the filters is restored by regeneration of the filter material with a 3-4% sulfuric solution 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 filter material and the condensate is removed from the silicic acid compounds, moreover 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 the anion exchange resin, and after the anion exchange filters, the purified condensate with a content of silicic acid is not more than 150 μg / kg, iron (in terms of Fe ⁺³ ) is not more than 100 μg / kg, oil products of not more than 0.5 μg / kg and total hardness of not more than 10 μg / kg are sent to the condensate storage tank, from where they are pumped mainly to the CHPP and steam boiler room, as well as to the sulfur installation and waste heat boilers, and for corrector onnoy processing desalted condensate to a value of pH 8,5-9,5 units. and to reduce the corrosion of metal pipelines, a 1% ammonia solution is dosed into the collector by metering pumps.

The clarification filters used in condensate cleaning can be double-chamber, consisting of a housing and a lower and upper drainage 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 ingress of activated carbon in the condensate; when condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; 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, hydraulic overload fittings and upper and lower distribution devices, 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 — covered 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 100% - return condensate to the steam generator, switch from the need to use a desalination plant with the use of 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.

 Gaseous fuel is burned and steam is generated in at least one steam generator, at least part of which is used, at least in part, for technological processes of production, and / or processing, and / or transportation of the extracted raw materials and supply of the steam generator additionally introduced into turnover of chemically purified water. As at least part of the gaseous fuel, associated gas is used in the raw materials and / or fuel process gas released during the processing of raw materials and / or intermediate products, with 15-40% of the gas being burned in a steam generator, and 60-85 % - in the technological installations of the enterprise, and chemically purified water is additionally put into circulation by adding to the technologically cooled purified return condensate and heating it with heat energy released in the technologically necessary process of selection of residual oth heat of return condensate in the process of cleaning the latter.

The gas is supplied with a temperature of mainly 20-70 ^o C and a pressure of 3.0-5.0 kg / cm ² , and before burning is heated to a temperature not lower than 100 ^o C.

Raw water is used from a flowing and / or non-flowing reservoir. Chemically purified water is heated by taking off the heat of the return steam condensate before or after cleaning the raw water from suspensions and after cleaning the return steam condensate from oil pollution, in particular water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 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 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. The amount of raw water passed through this heat exchanger is controlled until the condensate cools to a temperature of 25-35 ^o C, and the rest of the raw water is lowered 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, alkaline STI available 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 are removed to 0.1 mEq / kg, and in the second stage, deeper cations of hardness Ca ^{+ 2} , Mg ^{+ 2} to 0 are removed. 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. Chemically purified water is fed into tanks, and then pumped to a steam boiler room by 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 cationic 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 the distribution of water over the cross section of the filter. 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. A hatch is formed in the upper part of the filter housing to inspect the surface of the filter material, and in the lower part there is a hole for mounting and repairing the upper and lower drainage systems, and a fitting for hydraulic overloading is located on the filter housing at the level of slotted tubes, the source water piping and loosening are brought to the filter , an air vent of the upper and lower drainage systems, connect pressure gauges at the inlet and outlet of the collector, samplers and valves, and the filter backfill is double-layer, consisting of a layer of quartz sand with a height of 700 mm and volume 6.4 ohm m ³ and anthracite layer 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 of compressed air 5 m ³ / h and a pressure of 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 assigned at least 180 m ³ / h, and the filtering rate is not less than 25 m ³ / 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, a filter speed of at least 34 m / h is assigned, and the cations of hardness Ca ⁺² , Mg ⁺² up to 0 are removed , 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 a steam boiler room with a temperature of 25-30 ^o C. 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 the chemically purified water is sent to a gravity condensate cooler, in which the heat of the condensate from the plants is used. The water leaving the cooler is divided into two streams, one of which, heated to 90 ^° C, is fed to the deaerator head, and the other is fed to the continuous purge cooler using heat from 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, and network heating water is supplied to suction of network pumps, then through 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.

 If there is an excess of 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 condenser tanks in them, 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. First, steam is condensed in the steam-water heat exchanger, while the level of condensate 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. Chemically purified or network water is first passed through a water-water heat exchanger, and then through a steam-water .

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 up to 180 μg / kg, silicon acid content 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 settling 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. In both tanks, a given volume of liquid is maintained due to the difference in the levels of overflow troughs - filling nozzles, after which pure condensate with an oil content of 10-15 μg / kg is pumped through the control unit through the control unit, in which the flows are distributed for technological processing and loosening of three-stage filters de-oiling, on clarifying filters loaded with anthracite, in which the removal of suspended mechanical particles and "oil products" up to 4-5 μg / 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 μg / 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 which 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 to 40 ^° C. and first it is 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 m is used as filter material. hour, which produce the retention of cations of stiffness and iron. Periodically, the exchange ability of the filters is restored by regeneration of the filter material with a 3-4% solution of sulfuric acid. After the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as filter material and the condensate is removed from the silicic acid compounds, and the exchange capacity of the anion exchange filters is periodically restored by passing 3-5% anion exchange through the filter layer sodium hydroxide solution. 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, oil products not more than 0.5 μg / kg and a total hardness of not more than 10 μg / kg sent to the condensate reserve tank, from where it is pumped mainly to the CHPP and the steam boiler room, as well as to the sulfur unit and to waste heat boilers. For corrective treatment of desalted condensate to a pH of 8.5-9.5 units. and to reduce the 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 a lower and upper drainage switchgear. 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 filtering material, it is first laid in the lower chamber, and then in the upper one. The lower switchgear is in the form of a collector to which thirty-two beams with slotted holes 0.25-0.4 mm wide are attached, which are closed with perforated plates to prevent entrainment of the filter material. Four single-chamber filters are used as sorption filters of the first stage, which are connected 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. 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 generatrices with a diameter of 8 mm, which is overlapped by a weldable trough plate with a slit 0.25-0.4 mm wide to prevent the ingress of activated carbon into the conden Sat 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 hydraulic loading and upper and lower distribution devices, the upper of which performed in the form of a "glass in a glass", and the lower one is in the form of a collector into which distribution tubes are inserted — rays with holes along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.

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

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

 The production of own steam ensures a reduction in the cost of produced hydrocarbon raw materials by reducing the cost of steam (up to 50% of the cost of purchased steam), increases the reliability of providing the producing 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, etc.

Claims (14)

 1. A method of producing and selling steam at an oil, or gas, or oil and gas producing enterprise, including burning gaseous fuels and generating at least one steam generator, at least some of which is used, at least in part, for processing processes and supplying the steam generator with chemically purified water additionally introduced into circulation, characterized in that at least part of the gaseous fuel uses associated gas contained in the feedstock and / or fuel process gas, released during the processing of raw materials and / or intermediates, with 15 - 40% of the gas being burned in a steam generator, and 60 - 85% in the technological units of the enterprise, and chemically purified water is additionally put into circulation by adding to the technologically cooled purified return condensate and its heating with thermal energy released in the technologically necessary process for the selection of residual heat of the return condensate in the process of purification of the latter. 2. The method according to claim 1, characterized in that the gas is supplied with a temperature of mainly 20 - 70 ^o C and a pressure of 3.0 - 5.0 kg / cm ² , and before burning is heated to a temperature not lower than 100 ^o C.  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, 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 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 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 a pair of heat exchangers with movable tubular gratings and heat water to 25-30 ^o C, and 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 regulated before cooling condensate to 25 - 35 ^o C, and the remainder of the raw water is passed through another heat exchanger and heated it to 25 - 30 ^o C by using the heat exchanger as a heat carrier heating water, the heating water having a temperature acc After 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, and then the clarified water is fed to hydrogen-cationite 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 salt hardness, alkalinity present in the water, and chemical reactions with a sulfonic carbon hydrogen cation, after which softened water is fed to self-regulating buffer filters loaded with sulfonic carbon protecting 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 plane into the tank, after which this water is pumped through the pumps in two stages Sodium cation 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 get chemically purified water with a transparency of at least 40 cm, a total hardness of 2 - 5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 μg / kg and a pH of 8.0, after which chemically purified water is fed into tanks and then pumped to the steam boiler room. 5. The method according to any one of claims 3 and 4, characterized in that, 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 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 dampers, and chemical Such water purification is carried out only using sodium cationic filters, in which the filter material is also regenerated with saline with a concentration of 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 height 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 flow for own needs and preparation of regeneration solutions of at least 200 m ³ / h, the filtration rate when all filters are 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 for loosening compressed air and pressure up to 1.5 kgf / cm ² , and the hydrogen-cation exchange filters used 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, 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, 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 Raschig 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 of this water with a capacity of at least 400 m ³ , sodium used The ycationite filter is performed in two stages with an upper, consisting of beams, 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 with a cation hydrogen 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 to 0.1 mEq / kg, and the second stage of the filter is made up of two filters di meter 2600mm, was charged with a filter material layer height of 1200 mm, equipped with a filter upper distribution device, wherein the prescribed rate of filtration at least 34 m / h, and the removal is carried hardness cations Ca ^+2, Mg ⁺² to 0.01 meq / kg, while in all ion-exchange filters for chemical water purification on the lower drainage device an underlying layer of anthracite with a height exceeding the level of the arrangement of beams with perforation by at least 10 cm is located. 7. The method according to claim 1, characterized in that the chemically purified water is fed to a steam boiler room with a temperature of 25-30 ^° C, and part of the chemically purified water is directed to sampling coolers for continuous and periodic blowing of boilers, and from there to the deaerator head, another part of the chemically treated water fed to gravity condensate cooler, which uses the heat of condensation coming from the company facilities, and exiting the coolant water is separated into two streams, one of which is heated to 90 ^o C, is fed into the head deaerat RA, and the other is fed to a continuous purge cooler using heat from the purge water from the continuous purge separator, and then chemically purified water is passed through the deaerator vapor cooler, and then it is fed into the deaerator head and the chemically purified water is barbated 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-heating teley chemically purified water is carried switching network water heaters for heating the chemically treated water. 8. The method according to p. 6, 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 6, characterized in that in the presence of excess crushed steam at the enterprise, part of the crushed steam is fed to chemically purified water heaters and 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 any of paragraphs.8 and 9, characterized in that when the chemically purified water heater and network water heaters are operated on a reduced steam from the boilers, at least a part of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head for replacement equivalent amount of heated chemically purified water. 11. The method according to any one of paragraphs.8 and 9, characterized in that the heaters of the network and chemically treated water are in the form of a block of steam and water and water body 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 a water-water heat exchanger and it is 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 and a steam boiler room is piped to a distribution comb, and condensate with a total hardness of 100 μg-eq / 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 units, and if the condensate does not correspond to the specified parameters, it is sent to the drain, and from the distribution comb to The condensate is sent sequentially to the sump tank and the tank for collecting pure condensate separated from oil products, and as the condensate floats up to the surface of the oil particles, it is collected using a collecting funnel 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 nozzles, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, into which They distribute the flows for technological processing and loosening of filters of three stages of de-oiling, for lighting filters loaded with anthracite, in which they remove suspended mechanical particles and "oil products" up to 4-5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which are interconnected in parallel and loaded with activated carbon, and then onto 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 oily condensate with a temperature of 85 ^o C is sent to the annulus of heat exchangers, through which cold raw water is used, used for technological needs of chemical water treatment and the condensate is cooled to 40 ^o C, after which it is sent to a tank of oil-free condensate, from where the condensate is pumped to the desalting unit moreover, the temperature of the oil-free condensate is maintained in the range of 35 - 40 ^o C and first sent to hydrogen-cation exchange filters, in which, as a filter material and they use highly basic KU-2.8 cation exchange resin with a loading layer height of 1.5 m and a filtration speed of 35 m / h, in which stiffness cations and iron are retarded, and periodically, the exchange ability of the filters is restored by regeneration of the filter 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 filter material and the condensate is removed from the silicon compounds slots, moreover, periodically restore the exchange capacity of anion exchange filters by passing a 3–5% sodium hydroxide solution through the filtering 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, oil products not more than 0.5 μg / kg and 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 CHPP and steam boiler room, as well as to the sulfur unit and boilers utilizers moreover, for correcting the treatment of desalted condensate to a pH of 8.5 - 9.5 units and reducing corrosion of the metal pipelines, a 1% solution of ammonia is dosed into the collector with 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 are used with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ² ; 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 the distribution tubes are inserted — rays with holes along the lower generatrix of an overlapped plate having a slit 0.25-0.4 mm wide.  14. The method according to item 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 filter material on the lower distribution device of the sorption filters, a litter layer of coarse anthracite is spread over the entire surface of the filter with a height of 10 cm

Images