Method of cleaning alkaline effluents of oil processing


FIELD: process engineering.

SUBSTANCE: invention relates to treatment of industrial effluents. Oil products are separated in separators 3, 4 and afterpurified in ultra filtration unit 10. Clarified alkaline effluents are directed into electrolytic cells 13. alkali is concentrated in electrolytic cell cathode chamber 14 while sulphides are reduced to elementary sulfur in anode chamber 15. Concentrated alkali and sulfur are discharged into service bins 17, 20, respectively. Downstream of electrolytic cells 13, effluents are treated in reverse-osmosis unit 22. Purified water is collected in tanks 23. Concentrate is fed back into tank 21 for clarification.

EFFECT: alkali recover, water purification and elementary sulfur without use of extra reagents.

2 cl, 1 dwg

 

The invention relates to methods of treatment of industrial wastewater, namely, the processing in the target products of sulfur-alkaline waste water (boiling) oil refineries that use alkaline cleaning. Sulfur-alkaline effluents are the most contaminated runoff, because contain phenols, neutral hydrocarbons, naphthenate and sulfur compounds in the form of sulfides, sulfates, sulfites and mercaptides. Phenol concentration exceeds the average of 6 g/l, sulfites to 30 g/L.

For decontamination of sulfur-alkaline waste water used methods of oxidation, carbonization, bog and others. However, a large number of sulfur compounds belonging to the category of the most toxic components of industrial wastewater, complicates the use of traditional cleaning methods, calls for a reset on the biochemical treatment facilities for further oxidation. The use of biological treatment is complicated by the extreme toxicity of sulfides in relation to the microflora of treatment facilities and, as a consequence, the necessity of a large dilution of treated wastewater.

Known methods of purification of sulfur-alkaline waste waters do not provide zero-discharge wastewater treatment with the possibility of separation and recycling of valuable components (Proskuryakov, VA, Schmidt LI Clearing stock the x water chemical

industry. Chemistry, Leningrad branch, 1977, s-396). As a prototype adopted a method of processing sulfur-alkaline waste water (U.S. Pat. Of the Russian Federation No. 2245849, C07F 1/66, publ. 10.02.2005).

A method of processing sulfur-alkaline waste water includes wastewater neutralization of the acid with the separation and Stripping with an inert gas volatile sulfur-containing and other compounds, wastewater neutralization carried out with sulfuric acid or its aqueous solution in two stages at a temperature not exceeding 70°C, obtained after neutralization of the waste water is subjected to extraction with an organic solvent with the separation of the aqueous layer containing sodium sulfate, and the organic layer containing naphthenic acid; the aqueous layer containing sodium sulfate, neutralized with alkali and then dried to obtain a crystalline sulfate, and the organic layer containing naphthenic acid, is subjected to re-extraction with alkali the selection of the aqueous layer, containing naphthenate sodium, and organic solvent, which return to the stage extraction; the aqueous layer containing naphthenate sodium, recycle at the stage of Stripping with the conclusion of naphthenates sodium from the recirculation cycle. The method provides the ability to create a waste-free processing of sulfur-alkaline waste water in the target products suitable for implementation.

One is to use sulfuric acid and an organic solvent kerosene for extraction of wastewater and the withdrawal of gaseous products of the reaction has a negative impact on the ecological characteristics of the process. In addition, not paid attention to the separation of oil products in the first stage, although this process is likely to be present.

These disadvantages are eliminated by the proposed solution.

Task - improving the environmental performance of the method.

The technical result - the possibility of obtaining a regenerated alkali, purified water and elemental sulfur without the use of additional reagents.

This technical result is achieved in that in the method of purification of alkaline effluents of oil refineries, including the division of oil, regenerative alkali solution, the emissions of sulphur and oil sludge, Department of petroleum perform first separation, and then carry out the purification by ultrafiltration, the clarified alkaline wastewater is sent to the electrolysis cells, in a cathode chamber which is the concentration of alkali, as in the anode - recovery of sulfides to elemental sulfur, a concentrated alkali and sulfur, assign to the appropriate storage capacity, and runoff after the pots cleaned in the reverse osmosis installation, purified water is collected in the appropriate storage capacity, and concentrate return in cumulative capacity for clarified effluent. The electrolysis is carried out at a cathode current density of 2700-2750 a/m2, anode current density 8100-8250 a/m2at a temperature of 55-65°C for one hour and continuous circulation of the solution at a flow rate of 1000-1100 l/h

Proposed reagentless method of purification of alkaline wastewater. The use of separators (separators) allows the first stage to separate the oil from the alkaline waste water and to separate the oil, sludge and alkaline effluents. Ultrafiltration makes cleaning even more subtle, and processing in cells almost completely clears the alkaline effluent from the sulfur. The process ends with the collection in appropriate storage containers recycled (14%) alkali treated water and elemental sulfur, which can be used for various purposes.

The method can be implemented with the system shown in the drawing.

It contains the accumulation tank 1, 2 for the initial boiling. Capacity 1, 2 reported by pipeline separators (separators) 3, 4 for separating oil contained in the effluent from alkaline wastewater. Oil collected in the tank 5. Heavy substance (solids) fall to the bottom of the separators 3, 4, forming a precipitate, and with the help of the pump 6 and notchfilter 7 are loaded into the chamber 8 and to collect sediment. After separators installed cumulative capacity 9 for alkaline waste water, followed by the UF plant 10, reported by pipelines with a cumulative capacity of 11 cleared from oil alkaline drains and separators 3, 4. From the storage tank 11 CTE is found pipelines with pressure gauges and pressure sensors to the accumulation tank 12 for the clarified effluent. Accumulation tank 12 is equipped with a sensor alarm pH (not shown). The node separation of sulfur and site neutralization represented by cells 13 connected to tap water from the highway.

The cell 13 is composed of a bipolar electrode (not shown), which is insoluble anode made of platinized titanium, and on the other the cathode is made of titanium. The cell 13 is divided cation exchange membrane (not shown) on the cathode 14 and anode 15. In the cathode chamber 14 is the concentration of alkali, and the anode 15 recovery of sulfides to elemental sulfur. At the outlet of the cathode chamber 14 is installed concentrator 16 and 17 for collecting alkali. The anode chamber 15 is communicated with the pipe, provided with a pump 18 and cinemafilter 19 with a storage capacity of 20 to elemental sulfur. From the working space of the storage tank 21 for clarified effluent withdrawn tubing to reverse osmosis installation 22 for separating the clarified wastewater to clean water, which is collected in the holding tank 23, and concentrate, which is returned to the holding tank for the clarified effluent 21. All nodes are equipped with alarm systems.

The method is realized in the following way.

Out of storage tanks 1, 2 alkaline effluents pic is upaut in the separators (separators) 3, 4, where the separation of oil products contained in the effluent from alkaline wastewater. Oil collected in the tank 5, heavy substance (solids) fall to the bottom of the separators 3, 4, forming a precipitate, and with the help of the pump 6 and notchfilter 7 are received in the chamber 8 to collect precipitation. Refined oil products from alkaline water enters the holding tank 9. From the storage tank 9 alkaline wastewater coming into the UF plant 10, where the fine purification of alkaline waste water from the residue of petroleum products. Cleared from oil alkaline waste water is collected in the cells 13 (up to 50% of the volume of alkaline water going to the UF plant 10). The oil contained in the alkaline effluent returned to the separators 3, 4. In the electrolytic cell 13 is the concentration in the cathode chamber 14 3% alkali (NaOH), and the anode 15 - recovery of sulfides to elemental sulfur. It involves continuous monitoring of pH. From the cathode chamber through concentrator 16 alkaline solution enters the tank 17 for collecting alkali. Sulfur by a pump 18 and cinemafilter 19 going to the holding tank 20 to elemental sulfur. From the electrodialysis unit 13 clarified effluent is directed through the accumulation tank 21 for clarified effluent by reverse osmosis installation 22, where PR is coming separation of the clarified flow on the filtrate (purified water) and concentrate.

An example of the method

The method is implemented when cleaning alkaline waste water from plants MERICAT" and "NAPFINING", having the following composition:

water toof 92.8 wt.
NaOH1,3-6,7
Na2S0,1-2,3
Na2CO30,3-3,6
chloride-ionof 0.1 to 1.9
oilof 0,005 0,002

Raw material is pumped into a separator (neftegasgeodesia), from which discharged oil capacity of 5, mechanical impurities into the tank 8 and purified from them the alkali solution in the tank 9. In Nutrilite 7 is divided by a perforated partition with chlorin cloth precipitate from the liquid, which recirculating pump is pumped back into the cage. Cleaned from oil alkaline solution flows by gravity into the accumulation tank 9 and then on the UF plant 10, passes through the cleaning mechanical filter, which separates particles larger than 20 microns, two mechanical polypropylene cartridge filter where they separate the I particles greater than 5 microns, and ultrafiltration membrane. Obtained filtrate (purified from mechanical particles of alkaline runoff) and concentrate (alkaline runoff from mechanical particles). The filtrate (clarified effluent) flows into the accumulation tank 12, the concentrate in the separators. From the accumulation tank 12 clarified alkaline runoff enters the cells 13. The cells 13 are a volume of 23.5 liters each. The electrolysis takes place at a cathode current density 2700-2750 a/m2, anode current density 8100-8250 a/m2the temperature of 55-65°C for 1 hour and continuous circulation of the solution at a flow rate of 1000-1100 l/h. When the cathode density is less than 2700 a/m2and anode density less 8100 a/m2the capacity of the unit decreases. When the cathode density more 2750 a/m2and anode density more 8250/m2the process of destruction of the membrane. The resistance material of the cell is directly dependent on the process temperature. At temperatures less than 55°C (for example 53-50°C) material loses its properties (soft). At temperatures over 65°C (e.g. 68-70°C) there is a strong evaporation, which leads to increased corrosion, and this leads to the complexity of the design and cost of the electrolyzer. When carrying out electrolysis for 1 hour reduced the concentration of the NaOH solution from 1.3% to 0,00013%. PR is time less than 1 hour (for example 55-50 minutes) residual concentration of NaOH increases. When time greater than 1 hour (e.g. 65-70 minutes) the efficiency of the process decreases. When the flow velocity of the solution is less than 1000 l/h (for example 990-980 l/h) performance of the electrode decreases and increases cleaning time of alkaline wastewater. When the flow rate of the solution more l/hour (for example 1110-1120 l/h), it is necessary to change the design (to complicate the construction of the cell), and this increases the cost of the installation, which implements the proposed method. In the cathode chamber is the concentration of alkali, as in the anode - recovery of sulfides to elemental sulfur. Concentrated alkali and sulfur, assign to the appropriate storage tank 17, 20. Waste water after electrolysis cells purified in a reverse osmosis installation 22, from which are selected the purified water in the accumulation tank 23, and the concentrate return in cumulative capacity for clarified effluent 21. Thus, the regenerated alkaline, purified water and sulfur are separated, collected in a separate tank and can be used in various processes. The products at the exit position: alkali 14.3 wt.%, sulfur pasty 60 wt.%.

1. The method of purification of alkaline effluents of oil refineries, including the division of oil, regenerative alkali solution, the emissions of sulphur and oil sludge, characterized in that the separation of petroleum products is carried sakalakala, and then carry out the purification by ultrafiltration, the clarified alkaline wastewater is sent to the electrolysis cells, in a cathode chamber which is the concentration of alkali, as in the anode - recovery of sulfides to elemental sulfur, a concentrated alkali and sulfur, assign to the appropriate storage capacity, and runoff after the pots cleaned in the reverse osmosis installation, purified water is collected in the appropriate storage capacity, and concentrate return in cumulative capacity for the clarified effluent.

2. The method according to claim 1, characterized in that the electrolysis is carried out at a cathode current density of 2700-2750 a/m2, anode current density 8100-8250 a/m2at a temperature of 55-65°C for 1 h and continuous circulation of the solution at a flow rate of 1000-1100 l/H.



 

Same patents:

FIELD: process engineering.

SUBSTANCE: invention relates to environmental protection and may be used for treatment of effluents and wastes. Proposed device comprises dehydration scraper conveyor, crosswise partitions, process water cleaning devices of two types, water electrical cleaning devices and device to adjust water bleed and discharge depth. Water cleaning devices are arranged in inclined trench that water flow at 0.35±0.10 m/s-rate. Said scraper conveyor is arranged at trench bottom to discharge dewatered slurry into filtration hopper. Water cleaning device are arranged in pairs, that is, louvers-type cleaner - electrical cleaner, and lengthwise finely-dispersed precipitation module - water electrical treatment module, total number of pairs making 6-12. Note here that electrical treatment modules voltage between electrodes varies with distance there between to make 2.5±0.5 V/cm and adjacent pair electrodes polarity being opposite. Positive potential of 10-12 V is fed to crosswise electrically conducting filter while negative potential is fed to scraper conveyor casing.

EFFECT: reduced costs and higher reliability.

1 dwg

FIELD: chemistry.

SUBSTANCE: method involves steps for homogenising the filtrate, alkaline treatment of the filtrate with lime with subsequent reagent normalisation of pH of the filtrate using aqueous spent etching solutions from metal-processing factories which contain FeCl2 or FeSO4 with concentration of 17-25 wt %, with specific consumption of 1.0-5.0 mg/l of filtrate, bubbling the filtrate, blowing ammonia and biogenous compounds and electroflotocoagulation of the filtrate, after which the cleaned filtrate is taken to an evaporation pond.

EFFECT: higher environmental safety with high degree of purification of complex multi-component effluents, reduced treatment costs.

3 tbl, 2 ex

FIELD: treatment facilities.

SUBSTANCE: invention relates to water treatment and decontamination. The water treatment plant provides for affecting treated water volume by electric field. The plant consists of a reactor, three ejector pumps, stirrer and additional tank. There is a group of top electrodes and limiting screen installed inside reactor. The first ejector pump is connected to the reactor and provided with an outlet nozzle and two inlet nozzles. One of the inlet nozzles acts as an outlet nozzle of reactor, while the second one is intended for treated liquid supply. The second ejector pump is placed between the first ejector pump and stirrer and provided with an outlet nozzle acting as an inlet nozzle of the stirrer, and two inlet nozzles. One of said inlet nozzles is an outlet nozzle of the first ejector pump, while the other one is designed to supply hydrogen peroxide. The third ejector pump is placed in the additional circuit including additional tank for the treated liquid treatment and a pump to enable treated liquid circulating in the additional circuit. The third ejector pump is provided with an outlet nozzle to supply air into additional tank, and two inlet nozzles. One of said inlet nozzles is an outlet nozzle of the treated liquid circulation pump, while the other one is designed to supply air hydrogen peroxide.

EFFECT: invention allows for increasing water cleaning effectiveness and plant output.

1 dwg

FIELD: chemistry, water purification.

SUBSTANCE: invention refers to water treatment and can be used for tap water purification and activation in food industry, medicine, for sea water conversion, etc. Water treatment method is implemented in closed operating capacity and includes heat rejection enabling water local bulk crystallisation by ice crystals silvering in amount 50÷70 % of initial water weight surrounding heat exchanger, contaminated water drain through the port in capacity bottom and through the channel 0.5÷2 cm above capacity bottom, and removal of frost accumulation. Level of operating capacity filling with initial water is determined by height of channel port draining surplus initial water resulted from operating capacity filling and during initial water crystallisation due to its volume increase to additional capacity. Frost accumulation is removed by heating the ten shaped by multistage coil pipe and mounted in working capacity to surround heat exchanger directly in ice zone. During removal of frost accumulation, melt water is exposed to electrochemical activation carried out in special electrochemical activation tank separated with diaphragm to anode and cathode chambers. Herewith cathode chamber is pipeline connected to working capacity.

EFFECT: water purification from dissolved cancerogens, mutagens and gases, heavy hydrogen isotope, deuterium and tritium.

2 cl, 1 dwg, 1 ex

FIELD: chemistry.

SUBSTANCE: proposed method of purifying oily water effluents involves treatment of water in convection streams, formed by hydrogen bubbles, the number of which is equal to the number of cathode elements, subsequent mixing of the treated effluent water with a stream of clean water, saturated with oxygen bubbles, and filtration of the obtained mixture in a granular bed with catalytic properties. Part of the purified water is returned by recirculation for saturation with oxygen bubbles, and gaseous hydrogen and oxygen are taken out separately. The device for electrochemical purification of oily effluents comprises a case with vertical partition walls and connection pipes for inlet of the water to be purified and outlet of purified water, a receiving chamber, floatation chamber with horizontal electrodes, a chamber for collecting pure water, chamber for collecting sludge and a foam-collecting device in form of a series of truncated pyramids. The device also has a catalytic chamber filled with catalyst, connection pipes for letting purified water into the anode chamber, as well as connection pipes for outlet of gaseous hydrogen and oxygen. The floatation chamber is divided by a horizontal membrane into a cathode and anode chamber. The anode is a solid plate and lies at the bottom of the anode chamber. The gauze cathode is made from separate elements which are parallel to the anode.

EFFECT: increased efficiency and safer water purification process.

8 cl, 1 dwg, 1 tbl

FIELD: chemistry, process procedures.

SUBSTANCE: apparatus for producing purified water and water for injection comprises sterilizer, ion-exchange filter, tank for purified water and tank for water for injection. In addition, the device comprises feed water supply valve, connected to holding tank rapid filling valve, which interacts with a float-type gate valve and is connected to feed water holding tank, which is connected to the valve for supplying feed water from the holding tank to the pump line, and to the valve for discharging feed water from the holding tank. Feed water supply valve is connected to feed water pump, discharge of which is connected to the bypass valve inlet. Pressure indicator, which indicates current bypass control pressure, is connected to bypass valve inlet, to feed water pump discharge and to water flow meter, which is used to monitor the ion-exchange filter service life, while the flow meter is connected to multiway valve, which interconnects the ion-exchange column, a salt-dissolving apparatus, supply and discharge lines. The said multiway valve is connected to the supply rate control valve for the salt solution used for ion-exchange filter regeneration. The valve is connected to the salt solution flow rate indicator, which is connected to the salt dissolving apparatus. Outlet of the salt-dissolving apparatus, via the second outlet of the multiway valve, is connected to the inlet of the ion-exchange filter, the outlet of which is connected to the second inlet of the multiway valve via electric oxidizer. The third outlet of the multiway valve is connected to the valve, which controls operating capacity of the first and second electrodialyzers, and the said valve is connected to an electric-contact pressure gauge and to a continuous electric heater. The electric heater outlet is connected to the first electrodialyzer, outlet thereof is connected to the second electrodialyzer, the first outlet of which is connected to the second inlet of the first electrodialyzer, while the second outlet of the second electrodialyzer is connected to conductivity sensor. Outlet of the latter is connected to the second inlet of the second electrodialyzer via water flow rate meter, which measures water used for washing concentration cells of electrodialyzers. Outlet of the conductivity meter, via the valve which controls water supply to concentration cells of electrodialyzers, is connected to the resulting purified water flow meter. Outlet of the latter is connected to solenoid valve, which controls purified water supply to the purified water holding tank, which comprises sterilising lamp, and to the purified water return solenoid valve. The first outlet of purified water holding tank, via purified water take-off valve, is connected to portable tank for purified water take-off and transportation to area of consumption. The second outlet of purified water holding tank, via aseptic purified water supply valve and economizer, which is a shutoff-float level control device, is connected to an electric evaporative distilling apparatus. The latter is connected to a gas-liquid heat exchanger for water for injection production. Outlet of evaporative distilling apparatus, via gas-liquid heat exchanger, is connected to portable tank for water for injection takeoff and transportation to area of consumption. Outlet of coolant reservoir, via coolant pump connected to the distilling apparatus heat exchanger, is connected to the first inlet of liquid cooling liquid-air radiator, to the second inlet of which cooling air is supplied, while the radiator outlet is connected to the coolant reservoir inlet.

EFFECT: improved compactness and reliability of the apparatus; less energy consumption.

1 dwg

FIELD: different branches of industry; methods and devices used for the complex purification of the industrial waste waters.

SUBSTANCE: the invention is pertaining to the field of the complex purification of the industrial waste waters and may be used in the capacity of the local waste waters purification facilities used in the different branches of industry. The method of the industrial waste waters purification provides for their preliminary purification in the reactor by the coagulation-active iron-containing sediment of the pulp of the galvanic coagulator produced at the subsequent purification of the industrial waste waters and the flocculant, the further sedimentation of the previously purified waste waters in the settlersump and the subsequent purification of their clarified part in the galvanic coagulator with the charge of iron and coke. The deep afterpurification of the industrial waste waters conduct by the spinel ferritization at the expense of alkalization of the produced pulp of the galvanic coagulator up to рН 8.5÷9.0 with the settling and the routing of the sediment of the pulp to the preliminary purification, and the obtained liquid phase - to its filtration. The purification process is conducted in the device containing the sequentially connected reactor of the preliminary purification, the primary settler, the galvanic coagulator, the reactor-ferritizer, the secondary settler and the mechanical filter. At that the in series connected sediment collector and the press-filter are linked to the primary settler sediment outlet; the sediment outlet of the galvanic coagulator through the reactor- ferritizer is connected to the reactor of the preliminary purification; the reactor of the preliminary purification and the reactor-ferritizer are linked to the mains of the air supply. The technical result of the invention is the decreased salt-content of the purified industrial waste waters to the level of the quality of the water of the recycling water supply and production at the waste waters purification of the really reutilizable sediment.

EFFECT: the invention ensures the decreased salt-content of the purified industrial waste waters to the level of the quality of the water of the recycling water supply, production in the process of the waste waters purification of the really reutilizable sediment.

3 cl, 1 dwg, 4 tbl

FIELD: different branches of the national economy; methods and the devices for purification of the water from the harmful impurities.

SUBSTANCE: the invention is pertaining to the method and the installation for purification of the water from the harmful impurities. The method of purification of the water provides for the water aeration by the water feeding in the jet device for aeration mixing with the air. At that the aeration is conducted in two stages: at the first stage the aeration is conducted by commixing of the being purified water with the air or the air treated in the ozone installation with the air containing from 5 up to 40 % of ozone, then the produced mixture is gated through the swirler of the flow intensifying the process of the dissolution of the air or the air-ozone mixture in the water. Then conduct the second stage of the water treatment with the air or the air-ozone mixture with production of the water with рН from 9 up to 9.5. The produced aerated water is fed into the electrocoagulator, where conduct its electrochemical treatment with coagulation of the impurities and production of the outlet water with pH from 9.5 up to 10. After that they conduct clarification and ozonization of the water with its simultaneous treatment with the vapors of the nitric acid with recuperation of pH of the water up to 6.5 - 7. After that they conduct the water purification in the system of the ponds. The installation of the water purification contains the jet device for the water aeration, which outlet is connected to the flow swirler, which in turn is connected to the second jet apparatus for the water aeration. The latter outlet is connected to the electrocoagulator. The electrocoagulator is connected to the system of the water clarification, which outlet is connected to the jet apparatus for the water ozonization, which is supplied from the side of its air inlet with the ozonizing apparatus and the outlet of the jet apparatus is linked with the system of the ponds. The technical result of the invention is reduction of the prime cost of the water purification and the increased reliability of operation of the water purification installation.

EFFECT: the invention ensures the reduced prime cost of the water purification, the increased reliability of operation of the water purification installation.

5 cl, 1 dwg

The invention relates to the disposal of toxic chemicals used in agriculture, medicine, industry, and chemical warfare agents

The invention relates to methods for purification of groundwater for drinking water supply, in particular to methods of treatment of natural waters from iron, manganese and hardness salts, and can be used for producing demineralized water for cooking the battery electrolyte

FIELD: chemistry.

SUBSTANCE: invention relates to disinfectant compositions and specifically to a highly stable acidic aqueous solution, a method and apparatus for production thereof. The solution is prepared using a fluid medium treatment apparatus having at least one chamber (7), at least one anode (4) and at least one cathode (3) inside the chamber (7). The anode (4) and the cathode (3) are at least in part made from a first metallic material. At least one of said at least one cathode (3) and anode (4) have a coating with nanoparticles (5) of one or more metals.

EFFECT: obtained electrolytic acid water has high stability of its disinfecting action for a relatively long period of time, has low cost of production and is easy to produce.

16 cl, 5 dwg, 10 tbl, 8 ex

FIELD: process engineering.

SUBSTANCE: invention may be used in local drinking water treatment systems in municipal water supply systems. Proposed device comprises two coaxial cylinders 8 making tight hollow casing 9, dirty water inlet branch pipe 1, decontaminated water discharge branch pipe 2, compressed air feed branch pipe 3, and flushing solution drain branch pipe 4. Chamber between coaxial hollow cylinders 8 houses means for UV radiation of water composed of hollow vessels 7 from quartz glass filled with mix if inert gases. Two rings 10 from porous ceramic are arranged at top and bottom of said cylinders 8. HF current generator 5 connected via electrodes 6 to coaxial cylinders 8 is located outside casing 9.

EFFECT: higher efficiency of decontamination, nonpolluting process.

1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to treatment of flows of used materials. Proposed plant comprises the following components: a) vertical column divided into three zones: mixing zone, settling zone and mass exchange zone; b) waste discharge outlet communicated with mixing zone; c) organic material discharge outlet communicated with settling zone to remove organic phase from the plant; d) fluid transfer line communicating settling zone with mass exchange zone to transfer liquid phase from settling zone to mass exchange zone; e) vapor line communicating mass exchange zone with settling zone; f) inert gas inlet communicated with mass exchange zones, and g) waste discharge outlet communicated with mass exchange zone to allow discharge of fluid material.

EFFECT: decreased capital and operating costs.

9 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: in an electrolysis cell for producing chlorine, bipolar electrode elements are made from a bimetallic sheet (steel+titanium); frames of bipolar chambers are made from shaped tubes; anode and bipolar chambers are made from a bimetallic sheet which is made by welding sheets with insert bimetallic (steel+titanium) elements; the anode and the cathode chambers are equipped with built-in heat exchangers, one part of which is formed by placing shortened metallic separating strips inside the chambers and hermetic sealing of the outer surface of the chambers with a metal sheet; the second part is formed by making supporting frames of the chambers hollow, which enables to use water cooling.

EFFECT: intense process of producing chlorine, easier and higher air-tightness of the electrolysis cell.

2 dwg

FIELD: oil and gas industry.

SUBSTANCE: method involves obtainment of nuclei of oxidising compound, which are obtained by granulation in fluidised bed with atomisation; atomisation of water solution of metal silicate on nuclei of oxidising compound in fluidised bed, where water solution of metal silicate contains at least 15 wt % of metal silicate, and drying so that the covering coat of metal silicate is obtained on nuclei of oxidising compound. Granule obtained by means of the above method. Working liquid for well treatment, which contains at least one hydrated polymer, thickening agent to control the liquid viscosity, above described granules. Hydraulic fracturing method of underground formation, which involves introduction of fracturing liquid being the above described treatment liquid; formation of fractures, dilution of granules; reduction of liquid viscosity and removal of liquid from the formation. Cleaning method of waste water mud or dehydrated waste, which involves their contact with the above described granules. Invention is developed in dependent claims.

EFFECT: increasing stability and effectiveness of granules.

23 cl, 16 ex, 6 tbl, 6 dwg

FIELD: chemistry.

SUBSTANCE: inventions can be used in production of bottled drinking water from natural water. Method of water obtaining includes supply of water from tank for untreated water into buffer tank, pumping of ozone before buffer tank, bottling of ozonated water. Consumption of water is supported constant, with ozone being pumped with constant concentration. Water from tank for untreated water is supplied to buffer tank by means of pump, equipped with frequency variator, minimal working period for pump constituting 5 min, more preferably 10 min, and maximal non-working period constitutes 45 minutes, more preferably 20 min. Consumption of water, supplied by pump is set equal 105-110% of maximal pump consumption, used for filling buffer tank, with limit for time of presence of treated water in buffer tank being maximum 45 min. Before supplying water into buffer tank with ozone, it is passed through static mixer and at least 5 m long tube. Ozone concentration at water entry into buffer tank constitutes from 0.10 to 1.00 mg/l, more preferably from 0.20 to 0.60 mg/l.

EFFECT: decontaminated and bottled water, obtained by claimed method, contains less than 10 mcg/l of bromate, more preferably les than 5 mcg/l of bromate and contains less than 25 mcg/l acetaldehyde, more preferably less than 15 mcg/l of acetaldehyde.

22 cl, 14 dwg, 9 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: inventions can be used in production of bottled drinking water from natural water. Method of water obtaining includes supply of water from tank for untreated water into buffer tank, pumping of ozone before buffer tank, bottling of ozonated water. Consumption of water is supported constant, with ozone being pumped with constant concentration. Water from tank for untreated water is supplied to buffer tank by means of pump, equipped with frequency variator, minimal working period for pump constituting 5 min, more preferably 10 min, and maximal non-working period constitutes 45 minutes, more preferably 20 min. Consumption of water, supplied by pump is set equal 105-110% of maximal pump consumption, used for filling buffer tank, with limit for time of presence of treated water in buffer tank being maximum 45 min. Before supplying water into buffer tank with ozone, it is passed through static mixer and at least 5 m long tube. Ozone concentration at water entry into buffer tank constitutes from 0.10 to 1.00 mg/l, more preferably from 0.20 to 0.60 mg/l.

EFFECT: decontaminated and bottled water, obtained by claimed method, contains less than 10 mcg/l of bromate, more preferably les than 5 mcg/l of bromate and contains less than 25 mcg/l acetaldehyde, more preferably less than 15 mcg/l of acetaldehyde.

22 cl, 14 dwg, 9 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention relates to field of water treatment. Source water is supplied through branch pipe 11 into device for purification and disinfection of aquatic media. Device includes hermetic hollow case with upper 12 and lower 10 covers, into which two coaxial cylinders 1 and 4 are placed. In internal cylinder 4 located is wire winding 5, in which HF current from inductor 2 is induced. In order to produce pulse corona discharge generator 3 produces pulses. Compressed air is supplied through branch pipe 8 into porous ceramic cylinder 7. Water passes through coal filter 15, is purified from admixtures and saturated with ozone in lower part of device. Purified water is discharged through branch pipe 9.

EFFECT: invention makes it possible to increase efficiency and effectiveness of water purification and disinfection by means of ozonation.

1 dwg

FIELD: chemistry.

SUBSTANCE: invention can be used for improvement of membrane and sorption technologies, in water preparation, in elaboration of technologies for utilisation of ions of heavy metals from water solutions and sewage waters. Method of modification of cellulose-based sorbents includes their successive treatment with solutions of oxidiser, hydroxylamine hydrochloride, hydrogen peroxide and sodium hydroxide with washing with water after each stage. Interaction of sorbents with oxydiser is realised with microwave irradiation with power 300 W, with frequency 2.45 GHz and temperature 25-55°C for 5-15 minutes in solution with concentration 0.1-0.3 M at pH 2.5-4.5 and module solution/sorbent 15-50. Treatment with hydroxylamine hydrochloride is carried out with 0.3-1 M water solution at pH 3-5, module solution/sorbent 15-50 for 40-60 min. treatment with hydrogen peroxide id performed with its 30% solution at pH 5-7 for 30-60 min at room temperature and module solution/sorbent 15-50. Treatment with sodium hydroxide solution is carried out at pH 8-9 for 5 min at room temperature. As oxidiser preferably used is sodium metaperiodate, periodic acid or sodium hypochlorite, and as sorbents - cotton or wood cellulose, short flax fibre or sawdust.

EFFECT: invention makes it possible to increase degree of extraction of ions of heavy metals from solutions with concentration of metal ions to 1,5 mmol/l by 13-15% and reduce sorption time to 1-20 min.

2 cl, 1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention can be used for improvement of membrane and sorption technologies, in water preparation, in elaboration of technologies for utilisation of ions of heavy metals from water solutions and sewage waters. Method of modification of cellulose-based sorbents includes their successive treatment with solutions of oxidiser, hydroxylamine hydrochloride, hydrogen peroxide and sodium hydroxide with washing with water after each stage. Interaction of sorbents with oxydiser is realised with microwave irradiation with power 300 W, with frequency 2.45 GHz and temperature 25-55°C for 5-15 minutes in solution with concentration 0.1-0.3 M at pH 2.5-4.5 and module solution/sorbent 15-50. Treatment with hydroxylamine hydrochloride is carried out with 0.3-1 M water solution at pH 3-5, module solution/sorbent 15-50 for 40-60 min. treatment with hydrogen peroxide id performed with its 30% solution at pH 5-7 for 30-60 min at room temperature and module solution/sorbent 15-50. Treatment with sodium hydroxide solution is carried out at pH 8-9 for 5 min at room temperature. As oxidiser preferably used is sodium metaperiodate, periodic acid or sodium hypochlorite, and as sorbents - cotton or wood cellulose, short flax fibre or sawdust.

EFFECT: invention makes it possible to increase degree of extraction of ions of heavy metals from solutions with concentration of metal ions to 1,5 mmol/l by 13-15% and reduce sorption time to 1-20 min.

2 cl, 1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to disinfectant compositions and specifically to a highly stable acidic aqueous solution, a method and apparatus for production thereof. The solution is prepared using a fluid medium treatment apparatus having at least one chamber (7), at least one anode (4) and at least one cathode (3) inside the chamber (7). The anode (4) and the cathode (3) are at least in part made from a first metallic material. At least one of said at least one cathode (3) and anode (4) have a coating with nanoparticles (5) of one or more metals.

EFFECT: obtained electrolytic acid water has high stability of its disinfecting action for a relatively long period of time, has low cost of production and is easy to produce.

16 cl, 5 dwg, 10 tbl, 8 ex

Up!