RU2150433C1 - Chemical water treatment process - Google Patents

Abstract

FIELD: water treatment. SUBSTANCE: process, consisting in chemically treating water used in mixture with treated steam condensate in enterprises wherein production and/or processing of hydrocarbon-containing stock is conducted, includes intake of fresh water from water pool or another source and successive treatment thereof with at least one once-occurring change temperature state of water before beginning of or in the course of its treatment by heat exchange with return steam condensate resulting from process cooling of steam. Novelty consists in that heating steam is at least partly produced by burning associated gas and/or process gas released during heat treatment and/or in thermal-destruction processes accompanying processing of oil raw material or intermediate products, this combustible process gas being fed into fuel system at temperature chiefly 50-70 C and pressure chiefly 3.0-5.0 kg/sq.cm. Prior to be burned, gas is preheated to at least 100 C. 15 to 40% of gas is burned in steam generator and 60-85% in process installations of enterprise. To heat chemically purified water, residual heat of spent steam from enterprise processes is used. Invention increases efficiency of production owing to reduced consumption of chemically purified water for feeding production equipment. Invention also improves environmental condition thanks to excluded necessity of adjusting quality of purified water and condensate with regard to silicon level, which enables 100% return of condensate to steam generator and replacing desalting installation with hydrogen-cationite and anionite filters by installation with sodium-cationite filters thereby replacing corrosive reagents (sulfuric acid and alkali) by sodium chloride. EFFECT: enhanced process efficiency and improved environmental condition. 13 cl, 1 tbl

Description

 The invention relates to methods for chemical purification of water and can be used in various industries, including petrochemical, in which the use of chemically purified water is required.

 There are various methods of chemical water treatment (see, for example, Nikoladze G.I., Mints D.M., Kastalsky A.A. Water treatment for drinking and industrial water supply.- M.: Higher School, 1984, p. 295- 339).

 Closest to the invention in technical essence and the achieved result is a method of chemical treatment of water used in a mixture with purified steam condensate in an enterprise producing and / or processing carbon-containing raw materials, including the intake of raw water from a reservoir or other source and sequential treatment operations at least a measure with a one-time change before or during the purification of the temperature state of water through heat exchange with return steam condensate formed and process steam cooling (see., e.g., RU 2102328 C1, 20.01.98).

 The disadvantages of this method are the high cost due to the emerging need for processing large amounts of water and heat losses due to the incomplete use of the resulting steam condensate, as well as large heat losses due to the large amount of fuel gas burned on a flare, which worsens the environmental situation at the same time.

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

The problem is solved due to the fact that in the method of chemical purification of water used in a mixture with purified steam condensate at an enterprise that produces and / or processes carbon-containing raw materials, which includes taking raw water from a reservoir or other source and sequential treatment operations with at least one a change before or during the cleaning process of the temperature state of water through heat exchange with return steam condensate formed during the technological cooling of steam, according to the invention South steam, at least partially, is obtained by burning the associated and / or released during the heat treatment and / or as a result of thermo-destructive processes in the processing of raw materials and / or intermediate products - fuel process gas, which is supplied to the network with a temperature 50-70 ^o C and 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 a steam generator, and 60-85% in technological installations of the enterprise, and for heating chemical cally treated water using the residual heat of steam exhaust in the processes of the enterprise.

 In this case, raw water from a flowing and / or non-flowing reservoir can be used, and the chemically purified water is heated by taking the heat of the return steam condensate out before or after cleaning the raw water from suspensions and after cleaning the return steam condensate from oil contaminants.

They can use water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 mcg / kg, sulfates (SO ₄ ^-2 ) 1 , 78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg and permanganate oxidation 3.84-5.12 mg / kg in O ₂ , and the raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to the raw water pumps, at least one of which is left standby, and then the water is pumped through a pair of heat exchangers with fixed tube sheets and heat up water to a temperature of 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 until the condensate cools to a temperature of 25- 35 ^o C, and the rest of the raw water is passed through another heat exchanger and heated to a temperature of 25-30 ^o C due to the use in this heat exchanger as heating medium of heating 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, u of 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 that protects the filtrate from acid leakage, and then the water is sent to remove free carbon dioxide in a decarbonizer loaded with Rashig rings and the 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 cations, in the filters of the first stage, stiffness cations are removed up to 0.1 mEq / kg, and in the second stage, deeper cations of stiffness Ca ⁺² , Mg ^{+2 are} removed to 0.01 mEq / kg and get chemically purified water with a transparency of at least 40 cm, a total hardness of 2-5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 μg / kg and a pH value of 8.0, after which chemically purified water is fed into tanks, and then pumped to the steam boiler room with pumps.

At least during the flood period, they can pre-treat water that is produced using at least two clarifiers with a capacity of 250 m ³ / 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 of lime test, 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 valves, 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 at 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 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 tubes made of stainless steel, about 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 carried out in two layers consisting of a layer of quartz sand with a height of 700 mm and a volume of 6.4 m ³ and an 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 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 , 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 evenly distributing the flow of water over the surface of the filtering material of the system and the inner surface of the filter is made with a rubber gum coating, 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 two-stage with the upper one consisting of beams and the lower distribution devices, and 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 for cations of Ca ^{+ 2} , Mg ^{+ 2} cations to the hydrogen cation H ⁺ , while the filter performance is assigned at least 90 m ³ / h, and the filtration rate is at least 25 m / h and stiffness cations are removed up to 0.1 mEq / kg, and the second stage of the filter is 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 filters of 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 by at least 10 cm.

Chemically purified water can be fed to a steam boiler room with a temperature of 25-30 ^o C, and part of the chemically purified water is sent to the sampling coolers for continuous and periodic blowing of the boilers, and from there to the deaerator head, another part of the chemically purified water is sent to the gravity condensate cooler, 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 into the deaerator head and the chemically purified water is bubbled with steam, heating it to a temperature close to saturation, and removed of water ₂ O gas, CO, and network heating water supplied to suction line pumps, and then through a network of water heaters in the heating system of the enterprise, while the repair heaters chemically cleaned in dy carried switching network water heaters for heating the chemically treated water.

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

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

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

Heaters of network and chemically treated water can be implemented as a block of steam and water and water heat exchangers, and first, steam is condensed in the steam and water heat exchanger, while the condensate level in the heat exchanger is maintained by a level regulator, and then the condensate is sent to the water-water heat exchanger and supercooled to a temperature of 80-90 ^o C, while chemically purified or network water is first passed through a water-water heat exchanger, and then through a steam-water one.

A steam boiler room can be used as a steam generator, and production condensate from the plants of the enterprise and a steam boiler room is piped to a distribution comb, and condensate with a total hardness of 100 μg-eq / kg, Fe content in terms of Fe ₃ up to 180 μg / kg is used, acid content of silicon SiO ₂ - 350 mg / kg, oil content to 80 mg / kg and pH value to 8.0, the mismatch of the condensate of these parameters it is sent to the drain, and the junction with the condensate directed comb Sequence it is collected in a sedimentation tank and a collection tank of 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 nozzles, after which pure condensate with an oil content of 10-15 mg / kg is pumped through the control unit, in which the flows are distributed to the technolo chemical 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 mg / kg, and then the oil-free condensate with 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 a temperature of 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 filter material used SEASON KU-2.8 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% solution 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 filter material and the condensate is removed from the silicic acid compounds, and The exchange capacity of the anion exchange filters is carried out by passing through a filtering layer of the anion exchange resin 3-5% sodium hydroxide solution, and after the anion exchange filters, the purified condensate with a content of silicic acid is not more than 150 μg / kg, iron (in terms of Fe ⁺³ ) is not more than 100 μg / kg, of petroleum products - not more than 0.5 μg / kg and with a total hardness of not more than 10 μg / kg are sent to the condensate storage tank, from where they are pumped mainly to the CHPP and steam boiler room, as well as to the sulfur installation and waste heat boilers , and for correction On-line treatment of desalted condensate to pH = 8.5–9.5 and reduction of pipeline metal corrosion, a 1% ammonia solution is dosed into the collector by metering pumps.

The clarification filters used in condensate cleaning can be double-chamber, consisting of a housing and a lower and upper drainage distribution device, and a blind flat horizontal partition dividing it into two chambers and tubular anchors are connected rigidly inside the housing, and air is removed from the lower chamber to the upper and maintaining in the chambers of general pressure, while the upper drainage distribution device is in the form of a funnel for uniform distribution of densate on the surface of the filter material, which is used anthracite, the layer height of which in one chamber is assumed to be 0.9 m with a grain size of 2-6 mm, and when filling the filter with filter material, it is first placed in the lower chamber and then in the upper and lower switchgear are in the form of a collector to which thirty-two beams with slotted holes 0.25-0.4 mm wide are attached, which are closed with perforated plates to prevent entrainment of the filter material; Four single-chamber filters are used as sorption filters of the first stage, which are connected to each other in parallel and loaded with filter material — activated carbon with a layer thickness of 2.5 m and a grain size of 2 to 6 mm, and the filters are equipped with upper and lower distribution devices, the upper of which are made in the form of rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower switchgear in the form of a collector in which horizontally arranged days y and which is inserted in the distribution tubes with holes along the lower generatrix of 8 mm diameter which overlap weld 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-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-rays are inserted 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 filter surface 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 to power production equipment, as well as improving the environmental situation at the enterprise and surrounding territories due to the possibility of eliminating the need standardization of the quality of chemically treated water and condensate by silicon content, which makes it possible at 100% return to ndensata for steam to pass from the need for desalting unit to use hydrogen-cation exchange and anion exchange filters to the sodium cation exchanger, and therefore it is possible to abandon the use of corrosive reagents: sulfuric acid and alkali, and go to the use of salt.

The method is as follows. Chemical water treatment used in a mixture with purified steam condensate at an enterprise producing and / or processing carbon-containing raw materials includes the collection of raw water from a reservoir or other source and sequential treatment operations with at least one change before or during the process of cleaning the temperature state water through heat exchange with return steam condensate formed during the technological cooling of steam. Steam, at least in part, is obtained by burning associated and / or released during the heat treatment and / or as a result of thermo-destructive processes in the processing of raw materials and / or intermediate products - fuel process gas, which is supplied to the network with a temperature of mainly 50 -70 ^o C and 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 a steam generator, and 60-85% - in the technological installations of the enterprise. To heat the chemically purified water, the residual heat of the steam used in the technological processes of the enterprise is used.

 Use raw water from a flowing and / or non-flowing reservoir. The heating of chemically purified water, carried out by taking the heat of the return steam condensate, is carried out before or after the purification of raw water from suspensions and after cleaning the return steam condensate from oil pollution.

Use water from the Ural River with a total hardness of 4.8 mEq / kg, a total alkalinity of 3.4 mEq / kg, a pH of 8.1 and an iron content of 628 mcg / kg, sulfates (SO ₄ ^-2 ) 1, 78 mEq / kg, silicic acid 0.15 mEq / kg, calcium (Ca ⁺² ) 3.0 mEq / kg, magnesium (Mg ⁺² ) 1.8 mEq / kg and permanganate oxidation 3 84-5.12 mg / kg 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 adjusted to condensation of cooling to a temperature of 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 eplofikatsionnoy water having a heating water temperature according to the season. After heating, the water is sent for filtration to mechanical filters with a two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm. Then, the clarified water is fed to 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 ty in water, and chemical reactions with a hydrogen cation of sulfonated coal. Softened water is supplied to the self-regulating buffer filters loaded with sulfonated charcoal to protect the filtrate from acid leakage. Water is then sent to remove free carbon dioxide to a decarbonizer loaded with Raschig rings, and air is removed 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 pH = 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, 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 the filter material is also regenerated with saline 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 tubes made of stainless steel, 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 determined 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 pressure up to 1.5 kgf / cm ² . Used hydrogen-cation exchange filters are performed with a filtration area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm. The filter is equipped with an upper distribution device, which is performed in the form of a beam evenly distributing 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 not less than 180 m ³ / h, and the filtering speed - not less than 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 filter with an upper consisting of beams and lower distribution devices. The first stage of this filter is made of three filters with a diameter of 3000 mm and is loaded with filter material with a layer height of 1900 mm to replace the Ca ^{+ 2} , Mg ^{+ 2} cations with the H ⁺ hydrogen cation. The filter performance is prescribed not less than 90 m ³ / h, and the filtering speed - 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 is located at least 10 cm on the lower drainage device.

Chemically purified water is fed to a steam boiler room with a temperature of 25-30 ^o C. Part of the chemically purified water is sent to sampling coolers for continuous and periodic blowing of boilers, and from there to the deaerator head. Another part of the chemically purified water is sent to a gravity condensate cooler, in which the heat of the condensate from the plants is used. The water leaving the cooler is divided into two streams, one of which, heated to 90 ^° C, is fed to the deaerator head, and the other is fed to the continuous purge cooler using heat from the purge water from the continuous purge separator. Then chemically purified water is passed through a deaerator vaporizer cooler, and then it is supplied to the deaerator head and the chemically purified water is bubbled with steam, heating it to a temperature close to saturation, and O ₂ , CO gases are removed from the water. The district heating water is fed to the inlet of the network pumps, then through the network water heaters to the enterprise heating system. When repairing chemically purified water heaters, the network water heaters are switched to the heating of chemically purified water.

Steam from boilers for collectors is supplied to the enterprise steam pipelines for technological needs. Part of the steam from the collectors through a reducing device with a pressure of P = 4 kgf / cm ^{2 is} fed to the network water heater, to the chemically purified water heater, to the fuel gas heater, to heat the fuel gas separator and to deaerators.

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

During operation of the chemically purified water heater and network water heaters using reduced steam from boilers, at least a 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.

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. 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. 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 settling tank and the collection tank of pure condensate separated from the oil products. As the condensate emerges when the condensate settles to the surface of the oil particles, it is collected using a collecting funnel regulated at least once per shift. 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 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 directed to four sorption filters of the first stage, which are connected together in parallel and loaded with activated carbon, and then to four sorption filters of the second stage of decontamination of the condensate until the oil content in it is not more than 0.05 mg / kg. Then the oil-free condensate with a temperature of 85 ^o C is sent to the annulus of the 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 the oil-free condensate tank, from where the condensate is pumped to desalination plant. The temperature of the oil-free condensate is maintained in the range of 35 to 40 ^° C. and first it is sent to hydrogen-cation exchange filters, in which KU-2.8 highly basic cation exchange resin with a loading layer height of 1.5 m and a filtering speed of 35 m are used as filter material. h, in which 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% sodium hydroxide solution through the filter layer of the anion exchange resin. After anion exchange filters, the 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 oil 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 the steam boiler room, as well as to the sulfur unit and to waste heat boilers. For corrective treatment of demineralized condensate to pH = 8.5–9.5 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 generatrices with a diameter of 8 mm, which are covered by a weld-in gutter 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 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 switchgears. 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-rays are inserted 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-cut 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 use of chemically purified water of our own production allows us to abandon its consumption from the outside, which reduces the cost of production of steam of our own production compared to purchased to 50% and favorably affects the cost of produced oil products, increases the reliability and flexibility of providing the refinery with steam.

Claims (13)

1. A method for the chemical treatment of water used in a mixture with purified steam condensate at an enterprise producing and / or processing hydrocarbon-containing raw materials, comprising collecting raw water from a reservoir or other source and sequential treatment operations with at least one change before or in the process of cleaning the temperature state of water through heat exchange with return steam condensate formed during the technological cooling of steam, characterized in that the steam, at least part but produced by combustion contained in the raw material associated and / or emitted during the heat treatment and / or as a result thermodestructive processes in the processing of raw materials and / or intermediates fuel process gas which is fed into the network at a temperature preferably of 50 - 70 ^o C and 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 a steam generator, and 60 - 85% - in the technological installations of the enterprise, and chemically for heating purified water ispol form a pair of residual heat, waste in the processes of the enterprise.  2. The method according to claim 1, characterized in that raw water is used from a flowing and / or non-flowing reservoir, and the chemically purified water is heated by taking heat from the return steam condensate before or after purification of the raw water from suspensions and after purification of return steam condensate from oil pollution. 3. The method according to claim 1, 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 oxidative permanganate 3.84 - 5.12 mg / kg O ₂ , and raw water for chemical treatment is supplied under pressure up to 5 kg / cm ² to the raw water pumps, at least one of which they reserve, and then pump water through a pair of heat exchangers with fixed t with ribbed grids and heat water up 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 as a heat carrier, heating water having a heating water temperature in accordance with season thereof, and after heating, the water is sent for filtration to mechanical filters with two-layer loading with quartz sand and anthracite and suspended particles are removed from the water until the water reaches a transparency of at least 40 cm, and then the clarified water is fed to hydrogen-cation exchange filters with a “hungry” regeneration loaded with sulfonated coal, and carry out the removal of hardness salts from water to 1 - 2 mEq / kg constant and the destruction of the bicarbonate ion with a decrease in only carbonate alkalinity to 0.7 mEq / kg and ion exchange of hardness salts 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 carried out separation of air with carbon dioxide, which is discharged into the atmosphere, and decarbonized water by gravity into the tank, after which this water is pumped through pumps through two-stage filters atriykationirovaniya, in the filters of the first stage produce the removal of 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 chemically purified water with a transparency of at least 40 cm, a total hardness of 2 - 5 mEq / kg, iron content in terms of Fe ⁺³ up to 300 mcg / kg and a pH of 8.0, after which chemically purified water is fed into tanks and then pumps pumped to the steam boiler room. 4. The method according to claim 1, 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%. 5. The method according to any one of claims 3 and 4, characterized in that the mechanical filters used for chemical water purification are made in the form of cylindrical vessels with an internal anti-corrosion coating, mainly of epoxy resin, and two spherical steel bottoms, in the upper of which are placed the source of water supply and the upper distribution device, which is made in the form of beams of polymer material to distribute water along the filter cross section, and a drainage system in the form of a collector is located on the lower bottom with slotted stainless steel tubes, along the axis of which holes are formed that overlap with casings with slits 0.25 - 0.4 mm wide, and in the upper part of the filter housing form a hatch for inspecting the surface of the filter material, and in the lower part there is a hole for mounting and repair of the upper and lower drainage systems, while on the filter housing at the level of the slit tubes there is a fitting for hydroloading, feed water pipes, loosening, an air vent of the upper and lower drainage systems to the filter, pressure gauges at the inlet and Exit manifold valves and samplers, and the filter operate filling bilayer consisting of the layer of quartz sand of 700 mm and a volume of 6.4 m ³ and a layer of anthracite height of 500 mm and a volume of 4.6 m ^3, the filter performance is assigned with the flow water for own needs and the preparation of regeneration solutions of at least 200 m ³ / h, the filtration rate during operation of all filters is at least 7 m / h and the maximum during loosening washing is at least 10 m / h at a flow rate of 5 m for loosening compressed air ³ / h and pressure up to 1.5 kgf / cm ² , the hydrogen-cation exchange filters used are performed with a filtering area of at least 7 m ² , a diameter of at least 3000 mm and a loading height of sulfonated coal equal to 2500 mm, and 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 the 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 3 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 compiled one of the two filters with a diameter of 2600 mm, is loaded with filter material with a layer height of 1200 mm, the filter is equipped with an upper switchgear, at the same time, a filtering speed of at least 34 m / h is assigned and stiffness cations Ca ⁺² , Mg ⁺² up to 0.01 are removed 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 rays with perforation by at least 10 cm. 6. The method according to claim 1, characterized in that the chemically purified water is supplied to the steam boiler room with a temperature of 25-30 ^° 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, 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 the heat of 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 bubbled with steam, heating it to a temperature, is 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 Chemically purified water consumers switch network water heaters to heat chemically treated water. 7. The method according to any one of claims 1 to 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 heater water, to a chemically purified water heater, to a fuel gas heater, to a heating of a fuel gas separator and to deaerators.  8. The method according to any one of claims 1 to 7, 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 by condenser pumps pumped out for condensate treatment. 9. The method according to claim 7, characterized in that when the chemically purified water heater and network water heaters are operated on a reduced steam from boilers, at least a portion of the condensate with a temperature of 90 ^o C is sent directly to the deaerator head to replace an equivalent amount of chemically heated purified water. 10. The method according to claim 8, 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 condensate level in the heat exchanger is supported by a level controller, and then the condensate is sent to water-water heat exchanger and supercool it 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. 11. The method according to claim 1, characterized in that a steam boiler room is used as a steam generator, and production condensate from the plants of the enterprise and a steam boiler 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, and if the condensate does not correspond to the specified parameters, it is sent to the drain, and distribution comb The nsat is sent sequentially to 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 the specified the 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 They determine the flows 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 up to 4–5 mg / kg, after which the condensate is sent to four sorption filters of the first stage, which interconnected in parallel and loaded with activated carbon, and then on four sorption filters of the second stage of decontamination of the condensate until the content of “oils” in it is not more than 0.05 mg / kg, and then lenny condensate at a temperature of 85 ^o C fed to the shell space of heat exchangers, through which is passed the cold tap water used for process needs demineralizer, and cooling is condensate to a temperature of 40 ^o C, and then send it to the deoiled condensate tank where pumps pumped condensation on desalting plant, and the temperature of the oil-free condensate is maintained in the range from 35 to 40 ^o C and first sent to hydrogen-cation exchange filters, in which as a filter The high-basic cation exchanger KU-2.8 with a loading layer height of 1.5 m and a filtration speed of 35 m / h are used in which the stiffness cations and iron are retarded, and the exchange ability of the filters is periodically restored by regeneration of the filtering material 3-4% sulfuric acid solution, and after hydrogen-cation exchange filters, the condensate is sent to anion exchange filters, in which the highly basic anion exchange resin AB-17-18 is used as a filter material and condensate is removed connected silicic acid, moreover, periodically restore the exchange capacity of anion exchange filters by passing through a filter layer of anion exchange resin a 3 - 5% sodium hydroxide solution, and after the anion exchange filters, purified condensate with silicic acid content of not more than 150 μg / kg, iron (in terms of Fe ⁺³ ) not more than 100 μg / kg, oil products not more than 0.5 μg / kg and total hardness not more than 10 μg / kg are sent to the condensate reserve tank, from where they are pumped mainly to the thermal power station and steam boiler room, as well as to the sulfur unit and to the boiler s-utilizers, and for correcting the treatment of desalted condensate to a pH of 8.5 - 9.5 and reducing the corrosion of the metal in the pipelines, a 1% solution of ammonia is dispensed into the collector by metering pumps. 12. The method according to claim 11, 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 tube 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 first stage, which are connected to each other in parallel and loaded with filter material — activated carbon with a layer thickness of 2.5 m and a grain size of 2 to 6 mm, and the filters are equipped with upper and lower distribution devices, the upper of which are made in the form of rays for uniform distribution of the condensate stream over the entire surface of the filter material, and the lower switchgear in the form of a collector, which is placed horizontally on the bottom and into which the distribution pipes are inserted with openings along the lower generatrix with a diameter of 8 mm, which are covered by a weldable 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 are used with a capacity of at least 100 m ³ / h and a pressure of P = 5.0 kgf / cm ² ; hydrogen-cation exchange and anion exchange filters are designed as single-chamber cylindrical apparatuses 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-rays are inserted with holes along the lower generatrix, overlapped by a plate having a slit 0.25-0.4 mm wide.  13. The method according to p. 12, characterized in that in the case of the formation of a slit hole at the weld point of the trough plate to prevent entrainment of the filter material, a litter layer of coarse-cut anthracite is spread over the entire surface of the filter with a height of 10 cm to the lower switchgear of the sorption filters.

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