RU2149258C1 - Method for recovery of hydrocarbon-bearing material - Google Patents

Abstract

FIELD: oil production industry. SUBSTANCE: method relates to development of oil deposits and can be used in development of deposits containing high-viscous oil. According to method, delivered through injection wells is steam ensuring heating of bed with recovery of hydrocarbon-containing primary material through producing wells. Steam is produced by heating fresh water and/or by heating accompanying mineralized brine water and/or by heating return steam condensate, also by burning of fuel-technological gas contained in primary material and which is accompanying and/or emitted in process of thermal treatment of primary material. This fuel-technological gas is supplied for burning at temperature of 50-70 C under pressure of 3.0-5.0 kg/sq. cm. Prior to burning, gas is heated to temperature of not below 100 C. 15-40% of gas is burnt in boiler house of production enterprise, and remaining 60-85% is burnt in technological equipment of production enterprise. Steam is supplied in cyclic procedure and in surplus amount. Steam is condensed by 90-95%. Initial cycle is discontinued when level of recovery of hydrocarbon-bearing primary material is reduced. Pause is undertaken during at least 23 h, and after that, delivery of steam is continued. Application of method and procedure allows for increasing oil recovery from bed, removing depositions of asphaltene-resin-paraffin, increasing temperature of oil recovery with simultaneous reduction of loosed product, reduction of power input and production cost. This is achieved due to utilization of locally produced steam. Cost of this team is lower than cost of steam taken from outside by up to 50%. In addition, harmful outbursts to atmosphere are reduced, and general ecological situation in area is improved. EFFECT: higher efficiency. 17 cl, 1 tbl

Description

 The invention relates to the development of oil fields, in particular to methods for producing hydrocarbon-containing raw materials - oil, and can be used in the oil industry in the development of fields with high viscosity oils.

 A known method for the production of hydrocarbon-containing raw materials - oil by mine development of oil fields, including heating the treated area and oil displacement by periodically alternating injection of steam and hot water into the reservoir through a system of injection wells and oil selection through a system of production horizontally rising wells, and in order to increase the rate of selection oil and increase the efficiency of the heat treatment process before it is injected into the formation of hot water, it is aerated (see SU 937711 A, 28.06.82).

 The closest to the invention in terms of technical nature and the achieved result is a method for producing hydrocarbon-containing raw materials - oil, which includes supplying at least steam through the injection wells, which allows the formation to be heated, and selection of hydrocarbon-containing raw materials through production wells (see SU 933957 A, 07.06.82) .

 The disadvantage of this method is the reduction of oil recovery due to the harmful effects of asphaltene-tar-paraffin deposits (AFS), which are formed both in the layers and are deposited in the process equipment.

 The objective of the present invention is to increase oil recovery by reducing the harmful effects of asphaltene-tar-paraffin deposits (AFS), which are formed both in the layers and deposited in the process equipment.

The problem is solved due to the fact that in the method for producing hydrocarbon-containing raw materials, comprising supplying at least steam through the injection wells, which ensures heating of the formation, and selection through the producing wells of hydrocarbon-containing raw materials, according to the invention, steam is produced by heating fresh water and / or simultaneously achieving mineralized formation water, and / or return steam condensate by burning associated and / or fuel-technological gas contained in the raw materials during the heat treatment of the raw materials, which is supplied for combustion at a temperature of 50-70 ^o C at a pressure of 3.0-5.0 kg / cm ² , and before combustion, the gas is heated to a temperature not lower than 100 ^o C, while 15-40% of the gas is burned in the boiler room of the mining enterprise and 60-85% - in the technological equipment of the producing enterprise, steam is supplied cyclically in excess, while the steam condenses by 90-95% and the first cycle is completed with a decrease in the production of hydrocarbon-containing raw materials, soak for at least 23 hours, after which the steam supply is continued. In this case, steam can be supplied to the well in a mixture with a solvent, for example kerosene, and / or diesel fuel, and / or methanol. Steam can be mixed with a water-soluble polymer. First, a rim of steam with a solvent can be fed into the well, and then a rim of steam with a water-soluble polymer. Acrylic polymers, acrylic copolymers, a copolymer of styrene and maleic anhydride, and xanthan polymers can be used as water-soluble polymers.

In this case, fresh raw water from a flowing and / or non-flowing reservoir can be used, and the chemically purified water is heated by removing 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, 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 , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² for raw water pumps, at least one of which is reserved, 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, and at least one heat exchanger uses the premises condensate with temperature 80- 85 ^o C, wherein the amount of raw water flowing through the t ploobmennik, condensate of cooling is adjusted to up to 25-35 ^o C temperature 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 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 a transparent at least 40 cm, and then the clarified water is fed to hydrogen cationite filters with a "hungry" regeneration loaded with sulfonated charcoal, and hardness salts are removed from 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 and alkalinity salts present in water and chemical reactions with a hydrogen carbon sulfide cation, after which softened water is supplied to the self-regulating buffer filters protecting the filtrate from acid leakage, s loaded with sulfonated charcoal, and then the water is sent to remove free carbon dioxide to 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 with two-stage sodium cation filters into the filters of the first stage remove stiffness cations up to 0.1 mEq / kg, and in the second stage carry out a deeper removal of stiffness cations Ca ⁺² , Mg ⁺² 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.

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%.

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 polymer 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, and the filtering filling is performed by a two-layer filter consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and anthracite layer with a height of 500 mm and a volume of 4.6 m ³ , while the performance of the filters is prescribed taking into account the water flow for own needs and the preparation of regeneration solutions not less than 200 m ³ / h, the filtration rate during operation of all filters - not less than 7 m / h and maximum during loosening washing - not less than 10 m / h with a flow rate for loosening of compressed air of 5 m ³ / h and pressure up to 1, 5 kgf / cm ² ; used hydrogen cationite 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 filtering material of the system, 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 performed self-regenerating with the 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 a two-stage one 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 the cations Ca ^{+ 2} , Mg ^{+ 2} with a cation hydrogen H ^+, wherein the output of the filter is assigned at least 90 m ³ / hr, and filtration rate - not less than 25 m / h and produce removing hardness cations to 0.1 meq / kg, and the second filter stage operates amounted hydrochloric 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 supplied to the boiler room, which is a steam generator, to produce steam 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 chemically purified water gravity fed to the 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 a deaerator, 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 to the deaerator head and the chemically purified water is barbated with steam, heating it to a temperature close to saturation, and O ₂ , CO gases are removed from the water, and the network heating water is fed to the inlet of the network pumps, and then through the network water heaters to the enterprise’s heating system, while repairing chemically purified water heaters switch network water heaters to heat chemically purified water.

Steam from boiler rooms in collectors can be supplied to enterprise steam pipelines for technological needs, and part of the steam from the collectors is supplied through a reducing device with a pressure of P = 4 kgf / cm ² to the network water heater, to the chemically purified water heater, to the fuel gas heater, to heating of the fuel gas separator and into 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.

Production condensate from the technological equipment of the enterprise and the boiler-steam generator is piped to the distribution comb, and condensate with a total hardness of 100 μg-eq / kg, Fe content in terms of Fe ₃ to 180 μg / kg, silicon content of SiO ₂ acid is used up to 350 μg / kg, oil content up to 80 μg / kg and a pH value of up to 8.0 units, and if the condensate does not match the specified parameters, it is sent to the drainage, and from the distribution comb, the condensate is sent sequentially to the settling tank and the collection tank of pure condensate emerging from oil products, and as the condensate emerges upon settling on the surface of the oil particles, it is collected using a collecting funnel regulated at least once per shift, while both tanks maintain a given volume of liquid due to the difference in the levels of overflow troughs filling of pipes, after which 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 fi liters of three stages of de-oiling, to clarification filters loaded with anthracite, in which suspended mechanical particles and "petroleum products" are removed to 4-5 mg / kg, after which 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 - by four sorption filter second stage condensate to the deoiling contained "oils" is not more than 0.05 mg / kg and then deoiled condensate at a temperature of 85 ^o C is sent to the tube pros of the space heat exchanger through which is passed the cold tap water used for process needs demineralizer, and cooling is condensate to a temperature of 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting unit, wherein deoiled condensation temperature is maintained within a from 35 ^o C to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the filter material is a highly basic cationite KU-2,8 with a high the loading layer of 1.5 m and a filtration speed of 35 m / h, in which stiffness cations and iron are retained, and the exchange ability of the filters is periodically restored by regenerating the filter material with a 3-4% sulfuric acid solution, and after the hydrogen cationite 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 condensate of silicic acid compounds is removed, and recovery is periodically performed ix exchange capacity anion exchange filter by passing through the filter bed anion exchanger 3-5% sodium hydroxide, and after the anion exchange filters with purified condensate content of silicic acid is not more than 150 mg / kg of iron (calculated as Fe ⁺³⁾ is not more than 100 g / kg, of petroleum products - not more than 0.5 μg / kg and 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 CHPP and steam boiler room, as well as to the sulfur unit and to the waste heat boilers, and for correction desalted con processing ensata to a value of pH 8,5-9,5 units and reduce metal corrosion in piping manifold is dosed 1% ammonia solution dosing pumps.

The clarification filters used during condensate cleaning can be performed by two-chamber ones, consisting of a housing and a lower and upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and tubular anchors are connected rigidly inside the casing, through which air is removed from the lower chamber 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: as The sorption filters of the first stage use four single-chamber filters, 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, and the filters are equipped with upper and lower distribution devices, the upper of which performed in the form of rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower distribution device in the form of a collector, which is placed horizontally on the bottom and in which th inserted distribution tubes with holes along the lower generatrix of 8 mm diameter which overlap privarivaemo trough plate with a slit 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 cationite and anionite filters are made in the form of single-chamber cylindrical apparatus 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 distribution devices, the upper of which is made in the form of " glass in a glass ", and the bottom - 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 given set of features consists in increasing oil recovery, ensuring the removal of deposits of asphaltene-tar and paraffins, increasing the rate of oil extraction while reducing the loss of these products and reducing the energy intensity and cost of production by ensuring the possibility of using steam of own production, the cost of which is lower than the cost of purchased steam side up to 50%, reducing harmful emissions and improving the environmental situation in the region.

 The method is as follows.

The method includes supplying steam, at least through injection wells, for heating the formation, and selection of hydrocarbon-containing raw materials through production wells. Steam is produced by heating fresh water and / or associated mineralized formation water and / or return steam condensate by burning associated and / or fuel-technological gas contained in the raw material during heat treatment, which is supplied for combustion at a temperature of 50-70 ^o C at a pressure of 3.0-5.0 kg / cm ² . Before combustion, the gas is heated to a temperature not lower than 100 ^o C, while 15-40% of the gas is burned in the boiler room of the producing enterprise, and 60-85% - in the technological equipment of the producing enterprise. The steam supply is carried out cyclically in excess, while the steam condenses by 90-95% and the first cycle ends when the production of hydrocarbon-containing raw materials decreases, hold for at least 23 hours, after which the steam supply is continued. Steam is fed into the well in a mixture with a solvent, for example kerosene, and / or diesel fuel and / or methanol. The steam is mixed with a water-soluble polymer. First, a steam rim with a solvent is fed into the well, and then a steam rim with a water-soluble polymer. As water-soluble polymers, acrylic polymers, acrylic copolymers, a styrene-maleic anhydride copolymer, and xanthan polymers are used.

Use fresh raw water 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 in O ₂ . 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. Then, water is pumped through a pair of heat exchangers with fixed tube sheets and 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 regulate until the condensate cools to a temperature of 25-35 ^o C. The rest of the raw water is passed through another heat exchanger and heated to a temperature of 25-30 ^o C due to the use of heat exchanger in this heat exchanger heating water having a heating water temperature in accordance with the season. 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. Then, the clarified water is fed to hydrogen-cationite filters with "hungry" regeneration loaded with sulfonated coal and removal of hardness salts from water to 1-2 mEq / kg constant and destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and ion exchange of hardness salts, alkalinity and available in water, and chemical reactions with hydrogen cation sulfonated coal. Softened water is supplied to the self-regulating buffer filters loaded with sulfonated charcoal to protect the filtrate from acid leakage. Then, the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings, and air is separated with carbon dioxide, which is vented to the atmosphere, and decarbonized water by gravity into the tank. This water is pumped through two-stage sodium cation filters. In the filters of the first stage, stiffness cations are removed 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 chemically purified water is obtained by transparency not less than 40 cm, with 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 cation-exchange filters, in which they also regenerate the filter material with saline solution with a concentration of 6-8%.

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 bottom place the supply pipe of the source water and the upper distribution device, which is made in the form of beams of polymer 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 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 by a two-layer one consisting of a quartz sand layer with a height of 700 mm and a volume of 6.4 m ³ and an anthracite layer with a height of 500 mm and 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 cationite 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 performed in the form of a beam that evenly distributes the flow of water over the surface of the filtering material of the system. The inner surface of the filter is performed with a rubber gum coating. The filter performance is prescribed at least 80 t / h, and the filtering speed - 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 a top 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 . The sodium cationic filter used is a two-stage filter with an upper one 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 filtration rate of not less than 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 boiler room, which is a steam generator, to produce steam 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 plants is used. The water leaving the cooler is divided into two streams, one of which is heated to 90 ^o 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. Network heating water is fed to the suction of the 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 the boiler houses through the 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 portion 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.

Production condensate from the technological equipment of the enterprise and the boiler-steam generator is piped to the distribution comb. Use condensate 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. 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. Pure condensate with an oil product content of 10-15 μg / kg is pumped through a control unit, in which the flows are distributed for technological processing and loosening of filters of three de-oiling levels, for clarification filters loaded with anthracite, in which suspended mechanical particles and oil products are removed "up to 4-5 mcg / kg. 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 of 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 m / 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 the filter material and the condensate is removed from the silicic acid 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 demineralized condensate to pH 8.5–9.5 units and reduction of metal corrosion in 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 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. The lower switchgear in the form of a collector, which is horizontally placed on the bottom and into which the distribution pipes are inserted with holes along the lower generatrix with a diameter of 8 mm, which is closed by a welded gutter-like plate with a slit 0.25-0.4 mm wide to prevent activated carbon from entering the condensate. When condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} . Hydrogen-cationite and anionite 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 device is made in the form of a "glass in a glass", and the lower one is in the form of a collector into which distribution tubes are inserted — 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.

 A method of producing hydrocarbon-containing raw materials is illustrated by the example presented in the table.

 The implementation of the method of producing hydrocarbon-containing raw materials can significantly reduce operating costs when servicing oil wells and oil pipelines by reducing the content of corrosive agents, the use of associated petroleum gases as fuel.

Claims (17)

1. A method of producing hydrocarbon-containing raw materials, comprising supplying, at least through injection wells, steam, providing heating of the formation, and selection through production wells of hydrocarbon-containing raw materials, characterized in that the steam is obtained by heating fresh water and / or simultaneously produced mineralized formation water, and / or return steam condensate by burning the associated fuel and / or fuel-process gas released during the heat treatment of the feed, which is fed to eraturoy 50 - 70 ^o C at a pressure of 3.0 - 5.0 kg / cm ^2, wherein before the combustion gas is heated to a temperature not lower than 100 ^o C, with 15 - 40% of the gas is burned in the boiler mining enterprises, and 60 - 85 % - in the technological equipment of the producing enterprise, the steam is supplied cyclically in excess, while the steam condenses by 90 - 95% and the first cycle is completed with a decrease in the production of hydrocarbon-containing raw materials, holding for at least 23 hours, after which the steam is continued .  2. The method according to claim 1, characterized in that the well is supplied with steam mixed with a solvent, for example, kerosene and / or diesel fuel and / or methanol.  3. The method according to claim 1, characterized in that the steam is fed in a mixture with a water-soluble polymer.  4. The method according to any one of claims 1 to 3, characterized in that a rim of steam with a solvent is first fed into the well, and then a rim of steam with a water-soluble polymer.  5. The method according to any one of claims 3 and 4, characterized in that acrylic polymers, acrylic copolymers, a copolymer of styrene and maleic anhydride, xanthan polymers are used as water-soluble polymers.  6. The method according to claim 1, characterized in that they use fresh 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 cleaning the return steam condensate from oil pollution. 7. The method according to claim 6, 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 an iron content of 628 μg / kg, sulfates (SO ₄ ^-2 ) 1.78 mEq / kg, silicas 0.15 mEq / kg, calcium (Ca ^{+ 2} ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg and a permanganate oxidation rate of 3.84-5.12 mg / kg O ₂ , the raw water for chemical treatment being supplied under pressure up to 5 kg / cm ² to the raw water pumps, at least one of which they reserve, and then pump water through a pair of heat exchangers with fixed heat with lattice 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 the 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 in this heat exchanger of heat-transfer water having a heating water temperature in accordance with the season nom, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to the hydrogen-cation exchange filters with “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, alkalinity present in water and chemical reactions with a hydrogen carbon cation of sulfonated coal, after which softened water is fed to 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 separation is carried out 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 the pumps through two-stage filters atrium cations, in the filters of the first stage, stiffness cations are removed 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 value of 8.0, after which chemically purified water is fed into tanks, and then pumped to the steam boiler room. 8. The method according to claim 6, 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 measuring tanks coagulant 10 ^m3 each, lime wet storage cell, preferably lime putty capacity of 100 m ³ of milk of lime cell capacity of 60 m ³ and metering pumps, and / or centrifugal pumps with additional regulating valves, and a chemical treatment dy produce only using sodium cation filters, which also produce regeneration of the filter material with the concentration of brine 6 - 8%. 9. The method according to any one of claims 7 and 8, 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 ; 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 beams that uniformly 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 Ca ^{+ 2} , Mg ⁺ cations 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 structure second of the 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 rate of filtration at least 34 m / h, and the removal is carried hardness cations Ca ^+2, Mg ⁺² 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. 10. The method according to any one of claims 1 to 6, characterized in that the chemically purified water is supplied to the boiler room, which is a steam generator, to produce steam with a temperature of 25 - 30 ^o C, and part of the chemically purified water is sent to continuous and periodic sampling coolers blowing boilers, and from there to the deaerator head, another part of chemically purified water is sent to a gravity condensate cooler, which uses the heat of condensate from the plant’s units, and the water leaving the cooler is divided into two streams, one of which heated to 90 ^o C, is fed into the deaerator head, and the other is fed to a continuous purge cooler using 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 to the deaerator head and carried out bubbling chemically purified water with steam, heating it to a temperature close to saturation, and O ₂ , CO gases are removed from the water, and the network heating water is fed to the inlet of the network pumps, and then through the network water heaters to the enterprise’s heating system, while repairing chemically purified water heaters, the network water heaters are switched to chemically purified water heating. 11. The method according to p. 10, characterized in that the steam from the boilers of the boiler room 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, a heater for chemically purified water, to a fuel gas heater, to heat a fuel gas separator and to deaerators.  12. The method according to claim 10, 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 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. 13. The method according to any one of paragraphs.11 and 12, characterized in that when the chemically purified water heater and network water heaters are operated on a reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head for replacement equivalent amount of heated chemically purified water. 14. The method according to any one of paragraphs.11 and 12, 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 heat exchangers, and first, steam is condensed in the steam and water heat exchanger, while the level of condensate in the heat exchanger is supported by a level regulator, and then the condensate is sent to 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. 15. The method according to any one of claims 1 to 6, characterized in that the production condensate from the technological equipment of the enterprise and the boiler-steam generator is piped to a distribution comb, and condensate is used with a total hardness of 100 μg-eq / kg, Fe content in terms of on Fe ₃ up to 180 μg / kg, silicon content of SiO ₂ acid - up to 350 μg / kg, oil content up to μg / kg and pH up to 8.0, and if the condensate does not match the specified parameters, it is sent to the drain, and from the distribution comb condensate is directed n consequently, a settling tank and a collection tank of pure condensate separated from oil products are collected in the tank; moreover, 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 the difference between the levels of overflow trough-filling pipes, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flow is distributed and for technological processing and loosening of filters of three stages of de-oiling, for clarification filters loaded with anthracite, in which suspended mechanical particles and "oil products" are removed to 4-5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which connect with each other in parallel and loaded with activated carbon, and then 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 oil-free condensate temperature 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 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting unit, the temperature deoiled condensate is maintained in the range of from 35 to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the height of the filter material used co-basic cation exchanger KU-2.8 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 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 silicic acid compounds, and the period cally performed reconstitution exchange capacity anion exchange filter by passing through the filter bed anion exchanger 3 - 5% solution of sodium hydroxide, and after the anion exchange filters with purified condensate content of silicic acid is not more than 150 mg / kg of iron (calculated as Fe ⁺³⁾ is not more than 100 μg / kg, of petroleum products - not more than 0.5 μg / kg and 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 CHPP and steam boiler room, as well as to the sulfur unit and waste heat boilers, moreover for corrective treatment of demineralized condensate to a pH of 8.5 - 9.5 and reduction of metal corrosion of pipelines, a 1% ammonia solution is dosed into the collector by metering pumps. 16. The method according to clause 15, characterized in that the clarifying 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; Four single-chamber filters are used as sorption filters of the 1st 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 being 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 into which distribution pipes with holes along the lower generatrices with a diameter of 8 mm are inserted, which are sealed with a weld-in trough plate with a slit 0.25 - 0.4 mm wide to prevent the ingress of activated carbon into the condensate, when the condensate is supplied to the desalination plant, brand K pumps are used 100, 65, 200, SUHLU capacity of at least 100 m ³ / h and a pressure P = 5.0 kgf / cm ^2, hydrogen-cation and anion exchange filters is performed in a single chamber having a capacity of 115 m ³ / h of cylindrical apparatuses to housing 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 in the form of a "glass in a glass", and the lower one is in the form of a collector into which distribution tubes-rays are inserted with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide.  17. The method according to clause 16, characterized in that in the case of the formation of a slit hole in 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

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