RU2150587C1 - Method for producing and using steam at oil-, gas-, or gas/oil processing plants - Google Patents

Abstract

FIELD: thermal engineering; oil, gas, and chemical industries. SUBSTANCE: method involves combustion of gaseous fuel and production of steam by at least one steam generator, at least some portion of this gas being used for at least part of extraction, and/or processing, and/or conveying raw material produced at plant as well as feeding steam generator with chemically treated water introduced in circulating loop. Novelty is that at least part of gaseous fuel is casing- head gas contained in raw material and/or process fuel gas emitted in the course of heat treatment of raw material and/or as result of destructive thermal processes occurring during processing raw materials; gas is usually supplied at temperature of 50-70 C and pressure of 3.0-5.0 kg/sq. cm; prior to combustion it is heated to at least 100 C and chemically demineralized water is additionally introduced into circulating loop together with cooled-down return condensate and heated by residual heat energy released by return condensate in the course of its polishing. Provision is made for saving chemically demineralized boiler feedwater and for obviating the need for specifying quality of chemically demineralized water and condensate with respect to silicon content which makes it possible to dispense with demineralizing units using hydrogen- cation and anion exchangers and to replace them by sodium-cation exchangers with 100% condensate returned to steam generator and, hence, to do without chemically active agents such as sulfuric acid and alkali by replacing them with common salt; steam generated in the process enables 50% reduction in cost of oil products due to its low prime cost compared with purchased steam. EFFECT: improved economic efficiency due to reduced labor consumption and material input, improved environmental friendliness of process, reduced cost of end product. 14 cl, 1 tbl

Description

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

 There are various methods for 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 terms of technical nature and the achieved result is a method for producing and selling steam at an oil or gas or oil refinery, including burning gaseous fuels and generating at least one steam generator, at least part of which use, at least in part of the technological processes of extraction, and / or processing, and / or transportation of the extracted raw materials at the enterprise and supplying the steam generator additionally chemically cleaned water (see., RU 2090769 C1, 20.09.97).

 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 refinery, including burning gaseous fuels and generating at least one steam generator, at least some of which is used for at least in terms of technological processes of extraction and / or processing and / or transportation of extracted raw materials at the enterprise and supplying the steam generator with chemically purified water additionally put into circulation, according to the invention, at least , parts of the gaseous fuel use associated gas contained in the feedstock and / or fuel process gas released during the heat treatment of the feedstock and / or as a result of thermal destructive processes for processing the feedstock, the gas being supplied at a temperature of preferably 50-70 ^° C and a pressure of 3 , 0-5.0 kg / cm ^2, and before combustion is preheated to a temperature not lower than 100 ^o C, and chemically treated water is further introduced into the circulation by adding to the condensate of the cooling returnable and its heating by the thermal energy recovered emoy in technologically necessary residual heat of the process of selection of the return condensate to the cleaning process of the latter. At the same time, 15-40% of gas can be burned in a steam generator, and 60-85% - in the technological installations of the enterprise.

They can 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 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, silicas 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq sq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84-5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² raw water pumps, at least one of which is left standby, and then pumped water through a pair of heat exchangers with fixed tube sheets and heated water to a temperature of 25-30 ^o C, and at least one heat exchanger uses collected from the territory Business condensate with temperature 80-85 ^o C, wherein the amount of raw water flowing through this heat bmennik, 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 transparency and not 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 a decrease in carbonate only alkalinity up to 0.7 mEq / kg and ion exchange of hardness salts, alkalinity, available in water and chemical reactions with hydrogen sulfide carbon cation, after which softened water is fed to self-regulating buffer filters protecting the filtrate from acid leakage, loading sulfonated carbon, and then water is directed 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 a first stage produce filters removing hardness cations to 0.1 meq / kg, and in the second stage is carried out deeper removal of hardness cations Ca ^+2, mg ⁺² to 0.01 meq / kg was prepared and chemical cally purified water transparency of at least 40 cm, total hardness of 2-5 mg-eq / kg, the content of iron in terms of Fe ⁺³ to 300 .mu.g / kg and the amount of pH = 8,0, and then chemically purified water is fed into the tanks, and then pumped to the steam boiler room with pumps.

At least during the flood period, they can pre-treat water that is produced using at least two clarifiers with a capacity of 250 m ³ / h, 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 cells of milk of lime with a capacity of 60 m ³ and metering pumps and / or centrifugal pumps with additional control dampers, and chemical treatment of water is carried out only using the use of sodium-cation 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 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 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, while the filter efficiency is assigned considering the water consumption by cooking and regeneration solutions are not less than 200 m ³ / h, the filtration rate during operation of all filters is at least 7 m / h and the maximum during loosening flushing is at least 10 m / h with a flow rate for loosening of compressed air of 5 m ³ / h and a pressure of up to 1.5 kgf / cm ² ; used hydrogen-cation exchange filters are performed with a filtering area of at least 7 m ^{2 with 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 and the inner surface of the filter is made with a rubber gum coating, while the filter performance is assigned at least 80 t / h and the filtering speed is at least 13 m / h; the used buffer filters are loaded with sulfonated coal with a loading layer height of 2000 mm and are self-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 carried out 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 made two-stage with the upper one consisting of beams, and lower distribution devices, the first stage of this filter is made up of three filters with a diameter of 3000 mm and is loaded with filter material with a layer height of 1900 mm to replace cation of Ca ^{+ 2} , Mg ^{+ 2} cations to a hydrogen cation H ⁺ , while the filter performance is assigned at least 90 m ³ / h, and the filtration rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is 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 switchgear, the filtering speed is set to at least 34 m / h and Ca ^{+ 2} stiffness cations are removed , Mg ⁺² to 0.01 mEq / kg, while in all ion exchange x filters for chemical water purification on the lower drainage device have an underlying layer of anthracite with a height exceeding the level of the arrangement of rays with perforation of 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, in which the heat of the condensate from the plant’s units is used, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed to the deaerator head, and the other is fed to cool continuous blower, using the heat of the purge water from the 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 the chemically purified water is bubbled with steam, heating it to a temperature close to saturation, and removed from water gases O ₂ , CO, and network heating water are fed to the inlet of the network pumps, and then through the network water heaters to the enterprise’s heating system, while repairing heaters chemically cleaned in Odes switch network water heaters to heat chemically purified water.

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

 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-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the condensate level in the heat exchanger is maintained by a level regulator, and then the condensate is sent to the water-water heat exchanger and it is cooled to a temperature 80-90 ^o C, while chemically purified or network water is first passed through a water-water heat exchanger, and then through steam and water.

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, the silicon content of SiO ₂ acid is up to 350 μg / kg, the oil content is up to 80 μg / kg and the pH is up to 8.0 units, and if the condensate does not match the specified parameters, it is sent to the drain, and the condensate is sent from the distribution comb specifically in the settling 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 due to the difference in the levels of overflow troughs - filling pipes, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed to the biological treatment and loosening of filters of three stages of de-oiling, to 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 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 kg / kg, and then the oil-free condensate with temperature uroi 85 ^o C is sent to the annulus of heat exchangers, through which cold raw water is passed, used for technological needs of chemical water purification and the condensate is cooled to a temperature of 40 ^o C, after which it is sent to a tank of oil-free condensate, from where the condensate is pumped to the desalting unit, and deoiled condensation temperature is maintained in the range of from 35 ^o C to 40 ^o C and is sent first to a hydrogen-cation exchanger, which in use as a filter material KU-2.8 highly basic 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 regenerating the filter material with a 3-4% sulfuric acid solution and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as filter material and the condensate is removed from the silicic acid compounds, and iodically, the exchange capacity of anion exchange filters is restored by passing through a filtering layer of anion exchange resin a 3-5% solution of sodium hydroxide, and after the anion exchange filters, the purified condensate containing silicic acid is 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, 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 , and for correction constant processing desalted condensate 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 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 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 bottoms y and into which distribution pipes are inserted with holes along the lower generatrices with a diameter of 8 mm, which are covered with a weld-trough 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-cation exchange and anion exchange filters are designed as single-chamber cylindrical apparatuses having a capacity of 115 m ³ / h, each of which 2.6 m in diameter is equipped with upper and lower manholes, fittings for hydroloading and upper and lower switchgears, the upper of which are in the form of a "glass in a glass", and the lower one - in the form of a collector into which distribution tubes are inserted - beams with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide.

 In the case of the formation of a slit hole at the weld point of the trough plate to prevent entrainment of the filter material, a litter layer of coarse anthracite can be spread over the entire surface of the filter with a height of 10 cm to the lower switchgear of the sorption filters.

The technical result provided by the above set of features is to increase the efficiency of production by saving labor and material costs due to savings in the consumption of chemically purified water for boiler supply (from the planned 150 m ³ / h to 100-110 m ³ / h), as well as improvement of the environmental situation at the enterprise and surrounding territories due to the fact that it becomes possible to eliminate the need to standardize the quality of chemically treated water and condensate by silicon content, which makes it possible at 100% the return of condensate to the steam generator, switch from the need to use a desalination plant using hydrogen-cation exchange and anion exchange filters to sodium-cation exchange filters, and, therefore, it is possible to refuse the use of aggressive reagents: sulfuric acid and alkali and switch to the use of sodium chloride, At the same time, the production of own steam ensures a reduction in the cost of produced oil products due to its low cost compared to purchased steam up to 50%.

 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 extracted raw materials at the enterprise and supplying the steam generator with additional input chemically purified water. As at least part of the gaseous fuel, associated gas is used in the feedstock and / or fuel process gas released during the heat treatment of the feedstock and / or as a result of thermal destructive processes in the processing of the feedstock. The gas is supplied with a temperature of mainly 50-70 ^o C and a pressure of 3.0-5.0 kg / cm ² , and before burning it is heated to a temperature not lower than 100 ^o C. Chemically purified water is additionally put into circulation by adding to the technologically cooled return condensate and its heating by the thermal energy released in the technologically necessary process of selecting the residual heat of the return condensate in the process of purification of the latter. 15-40% of the gas is burned in a steam generator, and 60-85% - in the technological installations of the enterprise.

Use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking 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, use water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 mcg / kg, sulfates (SO ₄ ^-2 ) of 1.78 mg -eq / kg, silicas 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq / kg, ma decay (Mg ⁺² ) 1.8 mEq / kg, and permanganate oxidation 3.84-5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to raw pumps water, at least one of which is left reserve, 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. At least one heat exchanger uses condensate collected from the territory of the enterprise with a temperature of 80 -85 ^o C, wherein the amount of raw water flowing through this heat exchanger, the controller ruyut to condensation temperature of cooling to 25-35 ^o C. The remainder of the raw water is passed through another heat exchanger, and heated to a temperature of 25-30 ^o C by using the heat exchanger as a heat carrier heating water having a temperature of the heating water according to 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 the suspended particles are removed from the water until the water reaches a transparency of at least 40 cm. O water-borne water is fed to hydrogen-cation exchange filters with a "hungry" regeneration loaded with sulfonated coal, 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, alkalinity salts present in water and chemical reactions with a hydrogen carbon sulfide 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 directed to remove free carbon dioxide to 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 the 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 stiffness cations Ca ⁺² , Mg ^{+2 are} removed to 0.01 mEq / kg and get chemically purified water with a transparency of at least 40 cm, a total hardness of 2-5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 mcg / kg and pH = 8.0, after which chemically purified water is supplied to the tanks, and then pumped to the steam boiler room with pumps.

At least during the flood period, preliminary water treatment is carried out, which is carried out using at least two clarifiers with a capacity of 250 m ³ / h, two lime milk mixers with a capacity of 15 m ³ each, two coagulant measuring tanks of 10 m ³ each, and wet lime storage cells , preferably lime putty capacity of 100 m ³ of milk of lime cell capacity of 60 m ³ and metering pumps, and / or centrifugal pumps with additional regulating valves, and the chemical purification of water produced only using m sodium cation filters, which also produce regeneration of the filter material with brine at a concentration of 6-8%.

The mechanical filters used for chemical water purification are made in the form of cylindrical vessels with an internal anticorrosive coating, mainly of epoxy resin, and two spherical steel bottoms, in the upper of which a feed water supply fitting and an upper distribution device, which are made in the form of polymer beams, are placed material for distributing water along the filter cross section, and on the lower bottom there is a drainage system in the form of a collector with slotted stainless steel tubes along the axis which holes are formed that overlap with casings with slits 0.25-0.4 mm wide. A hatch is formed in the upper part of the filter housing to inspect the surface of the filter material, and in the lower part there is a 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 a layer of anthracite height of 500 mm and a volume of 4.6 m ^3, the filter performance is prescribed in view of the water consumption by preparation and regeneration solutions of at least 200 m ³ / h, the filtration rate during operation of the filter - at least 7 m / h and the maximum during loosening flushing - at least 10 m / h at a flow rate for loosening of compressed air of 5 m ³ / h and a pressure of up to 1.5 kgf / cm ² . Used hydrogen-cation exchange filters are performed with a 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 water flow over the surface of the filtering material of the system, and the inner surface of the filter is made with a rubber gum coating, while the filter performance is assigned at least 80 t / h, and the filtering speed is not less than 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 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-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} on 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. 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 switchgear, at the same time, a filter speed of at least 34 m / h is assigned and stiffness cations Ca ^{+ 2} , Mg ^{+ 2} are removed up to 0.01 mEq / kg. In all ion-exchange filters for chemical water treatment, 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, and part of the chemically purified water is sent to the sample coolers for continuous and periodic blowing of the boilers, and from there to the deaerator head, another part of the chemically purified water is sent to the gravity condensate cooler, in wherein a heat of 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 is fed to a cooler nep eryvnoy blowing using blowing warm water from a continuous purge of the separator. Chemically purified water is passed through a deaerator vaporizer cooler, and then it is supplied to the deaerator head and steam is chemically cleaned with steam, heated to a temperature close to saturation, and O ₂ , CO gases are removed from the water, and network heating water is fed to the suction network pumps. Then, through the network water heaters to the heating system of the enterprise, while repairing chemically treated water heaters, the network water heaters are switched to the heating of chemically purified water.

Steam from the boilers through the collectors is supplied to the enterprise’s 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, chemically purified water heater, fuel gas heater, and separator heating fuel gas and deaerators.

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

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

Heaters of network and chemically treated water are implemented as a block of steam-water and water-water heat exchangers, and first, steam is condensed in the steam-water heat exchanger, while the condensate level in the heat exchanger is maintained by a level regulator, and then the condensate is sent to the water-water heat exchanger and it is supercooled to a temperature of 80 -90 ^o C, while chemically purified or network water is first passed through a water-water heat exchanger, and then through steam and 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, and condensate with a total hardness of 100 μg-eq / kg, Fe content in terms of Fe ₃ up to 180 μg / kg, content silicon acid SiO ₂ - up to 350 μg / kg, oil content up to 80 μg / kg and a pH value of 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 floats up to the surface of the oil particles, it is collected using a collecting funnel that is adjustable at least once per shift, while both tanks maintain a predetermined volume of liquid due to the difference in the levels of overflow troughs - filling nozzles. Pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of the 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 mg / kg. The condensate is sent to four sorption filters of the first stage, which are connected in parallel and loaded with activated carbon, and then to four sorption filters of the second stage of decontamination of the condensate until the oil content in it is not more than 0.05 mg / kg. Oil-free 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 a temperature of 40 ^o C, after which it is sent to a tank of oil-free condensate, from where the condensate is pumped to the desalting condensate installation. The temperature of the oil-free condensate is maintained in the range from 35 ^° C. 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 filtration rate of 35 are used. m / h, which produce the retention of cations of stiffness and iron. Periodically, the exchange ability of the filters is restored by regenerating the filter material with a 3-4% solution of sulfuric acid, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-8 is used as the filter material and 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 the anion exchange resin, and after the anion exchange filters, the purified condensate containing silicic acid is not more than 150 μg / kg, iron (in terms of 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 to correct ion treatment 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 the condensate cleaning are 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 firmly attached inside the housing, and air is removed 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 condensation that 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, and the lower distribution device is made in the form of a collector to which thirty-two beams with slotted holes 0.25-0.4 mm wide are closed, which are closed with perforated plates to prevent entrainment of filter material; Four single-chamber filters are used as sorption filters of the first stage, which are connected 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. 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, in which the bottom is placed horizontally and into which distribution pipes with holes are inserted along the lower with a diameter of 8 mm, which is overlapped by a weld-trough plate with a slit 0.25-0.4 mm wide to prevent activated carbon from entering the conda 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 made in the form of single-chamber cylindrical apparatuses having a capacity of 115 m ³ / h, each of which with a diameter of 2.6 m is equipped with upper and lower manholes, fittings for hydroloading and upper and lower distribution devices, the upper of which is made in 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 — 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 oil products due to its low cost, which is up to 50% compared to the cost of purchased steam, increases the reliability of providing the enterprise with steam, ensures the rational use of the generated fuel gas, reduces losses during oil refining, while steam is used in as a coolant to maintain the bottom temperature of stripping columns, gasoline hydrotreatment units, kerosene and diesel fractions, rectification gas columns, gas fractionation units, primary oil refining units, oil production, as a coolant in the production of oils, steam satellites, for spraying fuel, creating a vacuum, to ensure safety, fire safety, in preparing equipment for repair, for utility needs, etc. .

Claims (14)

1. A method of producing and selling steam at an oil or gas or oil refinery, 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 of extracted raw materials at the enterprise and supply of the steam generator with chemically purified water additionally put into circulation, characterized in that associated gas is used as at least part of the gaseous fuel Rieux, and / or fuel process gas is emitted during the thermal treatment of raw materials and / or as a result termodekstruktivnyh processes in the processing of raw materials, wherein the gas is supplied at a temperature preferably of 50 - 70 ^o C and the pressure 3.0 - 5.0 kg / cm ² , and before burning, they are heated to a temperature of at least 100 ^o C, and chemically purified water is additionally introduced into circulation by adding to the technologically cooled return condensate and heating it with the heat energy released in the technologically necessary process for the selection of residual heat You return condensate during the last cleaning process.  2. The method according to claim 1, characterized in that 15 - 40% of the gas is burned in a steam generator, and 60 - 85% - in the technological installations of the enterprise.  3. The method according to claim 1, characterized in that they use raw water from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after purification of the raw water from suspensions and after purification of return steam condensate from oil pollution. 4. The method according to claim 1 or 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 an iron content 628 mcg / 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 permanganate oxidizability of 3.84 - 5.12 mg / kg in O ₂ , and the raw water for chemical treatment is fed under pressure up to 5 kg / cm ² to the raw water pumps, at least least one of which is left standby, and then water is pumped through a pair of stationary heat exchangers tubular bars and preheated water up to 25 - 30 ^o C, wherein at least one heat exchanger is used assembled with the premises condensate with temperature 80 - 85 ^o C, wherein the amount of raw water flowing through this heat exchanger is adjusted until the condensation of cooling to 25 - 35 ^o C, and the remainder of the raw water is passed through the other heat exchanger is heated and its 25 - 35 ^o C by using the heat exchanger as a heat carrier heating water, the heating water having a temperature in accordance with ces 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 in water and chemical reactions with a hydrogen carbon cation of sulfonated coal, after which softened water is supplied to the self-regulating buffer filters loaded with sulfonated carbon to protect the filtrate from acid leakage, and then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings and air is separated 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 s-cationization, in the filters of the first stage produce remove hardness cations to 0.1 meq / kg, and in the second stage is carried out deeper removal of hardness cations Ca ^+2, Mg ⁺² to 0.01 meq / kg t obtained 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 claim 3 or 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 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 dampers and chemical CLEAR DIR water ku produce only using natriykationovyh filters, which also produce regeneration of the filter material with the concentration of brine 6 - 8%. 6. The method according to p. 4 or 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 steel bottoms of cold water and an upper switchgear, which is performed in in the form of rays from a polymeric material for distributing water along the filter cross section, and on the lower bottom there is a drainage system in the form of a collector with slotted stainless steel tubes along the axis of which are formed from versts 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 - a hole for mounting and repairing the upper and lower drainage systems, while on the housing at the level of the slotted tubes, a fitting for hydraulic overloading is placed, feed water pipes, loosening, an air vent of the upper and lower drainage systems are connected to the filter, pressure gauges at the inlet and outlet of the collector, samplers and valves are connected, and the filter filling is filled a two-layer layer consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and an anthracite layer with a height of 500 mm and a volume of 4.6 m ³ is taken, while the performance of the filters is prescribed taking into account the water flow for own needs and the preparation of regeneration solutions of at least 200 m ³ / h, the filtration rate during operation of all filters is at least 7 m / h and the maximum during loosening flushing is at least 10 m / h with a flow rate for loosening of compressed air of 5 m ³ / h and a pressure of up to 1.5 kgf / cm ² ; used hydrogen-cation exchange filters are performed with a filtering area of at least 7 m ³ , 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 used sodium cationite filter is performed in two stages with an upper, consisting of rays, and lower distribution devices, the first stage of this filter is made up of three filters with a diameter of 3000 mm and loaded with filter material with a layer height of 1900 mm to replace the cations Ca ⁺² 6, Mg ⁺² on a hydrogen cation H ⁺² , while the filter performance is assigned at least 90 m ³ / h, and the filtration rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is performed from two f filters with a diameter of 2600 mm, they are loaded with filter material with a layer height of 1200 mm, the filter is equipped with an upper switchgear, the filtering speed is set at least 34 m / h and stiffness cations Ca ⁺² , Mg ⁺² are removed to 0.001 mEq / kg Moreover, in all ion-exchange filters for chemical water purification, an underlying layer of anthracite with a height exceeding the level of arrangement of beams with perforation by at least 10 cm is located on the lower drainage device. 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, the other part of chemically purified water is sent to a gravity condensate cooler, in which the heat of the condensate from the plant’s units is used, and the water leaving the cooler is divided into two streams, one of which, heated to 90 ^o C, is fed into the deaerate head ora, and the other is fed to the continuous purge cooler using heat from the purge water from the continuous purge separator, and then chemically purified water is passed through the deaerator vapor cooler, and then it is fed into the deaerator head and the chemically purified water is barbed with steam, heating it to a temperature, close to saturation, and water is removed from the gases O _2, CO, and network district heating water is supplied to suction line pumps, and then through a network of water heaters in the heating system of the enterprise, while the repair heaters it is chemically treated water 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 condensed tanks in them, from where they are pumped out by condenser pumps for condensate treatment. 10. The method according to claim 8 or 9, characterized in that when the chemically purified water heater and network water heaters are operated on a reduced steam from boilers, at least a part of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head to replace an equivalent amount heated chemically purified water. 11. The method according to claim 8 or 9, characterized in that the heaters of the mains and chemically treated water are in the form of a block of steam-water and water-water heat exchangers, and steam is first condensed in the steam-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 the 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. moreover, 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 the pure condensate separated from the oil products, and as the condensate emerges onto the surface of the oil particles, it is collected using a collecting funnel , adjustable at least once per shift, while in both tanks maintain a given volume of fluid due to the difference in the levels of overflow troughs - filling pipes, after h its pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed for technological processing and loosening of the filters of three de-oiling levels, for lighting filters loaded with anthracite, in which suspended mechanical particles are removed and of petroleum products "up to 4 - 5 mg / kg, after which the condensate is sent to four first-stage serration filters, which are connected in parallel and loaded with activated carbon, and then four orbtsionnyh second filter stage condensate to deoiling contained "oils" is not more than 0.05 mg / kg and then deoiled condensate at a temperature of 85 ^o C fed to the shell space of heat exchangers, through which is passed the cold raw water used for the technological needs and demineralizer condensation is carried out cooling to 40 ^o C, after which it is sent in deoiled condensate tank from which condensate is pumped by pumps to a desalting unit, wherein the condensation temperature is maintained deoiled in the range from 35 to 40 ^o C and is sent first to a hydrogen-cation exchanger, in which as the filter material is a highly basic cationite KU-2,8 with a height of 1.5 m layer load and speed of filtration of 35 m / h, in which stiffness cations and iron are retained; moreover, the exchange ability of the filters is periodically restored by regenerating the filter material with a 3-4% sulfuric acid solution, and after the hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which, as The filter medium using highly basic anion exchange resin AB-17-8 and condensate of silicic acid compounds is removed, and the exchange capacity of anion exchange filters is periodically restored by passing a 3–5% sodium hydroxide solution through the filter layer of anion exchange resin, and after the anion exchange filters, the purified condensate containing silicic acid does 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 with a total hardness of not more than 10 μg / kg, condensate is sent to the reserve tank and from where it is pumped mainly to a thermal power station and a steam boiler room, as well as to a sulfur unit and to waste heat boilers, moreover, for correcting the treatment of demineralized condensate to a pH value 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. 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; 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 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 in which horizontally the bottom CB and inserted distribution tubes with holes along the lower generatrix of 8 mm diameter which overlap privarivaemo trough-plate with a gap width of 0.25 - 0.4 mm to avoid contact with the activated carbon in the condensate; when condensate is supplied to the desalination plant, K 100, 65, 200, SUKHLU pumps with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ^{2 are used} ; hydrogen 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 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 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

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