RU2120412C1 - Method of producing drinking water and method and automated installation for treating industrial drains - Google Patents

Abstract

FIELD: water treatment. SUBSTANCE: producing drinking water and treating industrial drains are accomplished by integrated electric-reagent method, which would find wide application in national economy when producing foods, drugs, alcohol and alcohol-free beverages, and also high-quality industrial water from waste water. A two-step electrochemical treatment of initial water is followed by stepwise isolation of precipitate while adding acidic reagent mixture in the first step and alkaline reagent mixture in the second step. Process is largely provided with informational control and automated microprocessor regulation to ensure optimal conditions during start-up, shot-down, and operating-duty periods. EFFECT: reduced (5-10-fold) consumption of reagents and power, optimized mineral salt contents in drinking water, and conditions for recycling water supply provided. 2 cl, 1 dwg, 2 tbl

Description

 The invention relates to ecology, in terms of electrochemical technologies for producing drinking water and purification of industrial effluents, namely, a combined electro-reagent method in an automated installation for its implementation. The invention will be widely used in the national economy for the treatment of wastewater and drinking water, the preparation of food products, medicines, alcoholic and non-alcoholic drinks, and is an important preventive measure to prevent the spread of a wide range of diseases associated with an increased "environmental risk" of the environment, as well as using low-quality water with low sanitary and hygienic indicators, helping to increase the quality parameters of products Manufactured with the use of aqueous solutions in industrial sanitation optimum that eventually effectively contributes to solving the problem of modern human ecology.

 A large number of methods and installations for producing drinking water and treating industrial effluents are already known, each of which is related to the scope of the treated water, its initial composition, plant productivity, type of equipment and control systems used, as well as the level of scientific and technological progress achieved in the field technogenic ecology of sources of drinking water consumption, improvement of natural reservoirs of sanitary and fishery purposes.

 There are several ways of artificial methods of purification of natural waters. (See the book: Zhungietu G.I. Bread, Water and Chemistry: Chisinau: Shtinitsa. 1985. - 184 p. / S. 162-165).

 Known thermodistillation method for desalination of sea water, according to which desalination is carried out on a special installation consisting of a series-connected evaporator, condenser and receiver, and is widely used in anhydrous regions of the planet, as well as in objects with a closed volume.

Its disadvantages include:
1. Significant energy consumption;
2. Obtaining completely demineralized water.

There is an electrodialysis method for purifying medium-saline water - (2-10) • 10 ^-3 kg / dm ³ , based on the use of the valve properties of porous diaphragms (membranes), in which desalinated water accumulates in the interelectrode part, and brines in the chambers are closer to the electrodes .

Its disadvantages are:
1. Limited scope - only for the removal of electrolytes.

 2. Difficulties in eliminating organic substances of nonionic nature.

 A hyperfiltration method based on the reverse osmosis effect is also used, using a two-layer porous plastic located between the layers of a semi-impermeable membrane.

Its disadvantages are:
1. Poor installation performance.

 2. Difficulties in ensuring high mechanical strength of the membrane itself and its regeneration.

 3. Narrow membrane selectivity for types of contamination.

4. Sophisticated pre-treatment scheme,
5. High sensitivity to the composition of the source water.

 There is a method of freezing, in which, in one embodiment, upon receipt of an ice block, impurities accumulate on its surface and are removed by subsequent mechanical scraping, and in another, a deeply chilled “ice porridge” obtained in the mold falls into a hydrocyclone, where pure ice is separated from the contaminated solution and then due to irrigation already purified water in the wash column is thawed.

 The main disadvantages of this method are the high energy intensity, the complexity of the technology, the bulkiness of the installation and the cyclical nature of its operation.

 An electroflotation purification method is also used, which is based on the effect of rising hydrogen bubbles generated in the mesh bottom cathode on the impurities present in the flowing water and carrying them along through the anode zone.

Its disadvantages include:
1. Selectivity to wettable and non-wettable particles.

 2. The inability to remove dissolved salts.

 The ion-exchange purification method is widely used, the essence of which is the sequential passage of water through cation exchange filters, where cation exchange metals absorb hydrogen ions and, when passing through anion exchange filters, anion exchangers exchange their hydroxyl ions for acid residues of salts in water.

 Disadvantages: insensitivity to mechanical fine suspensions, low productivity, high cost.

Existing reagent cleaning methods have a number of disadvantages:
1. The required cleaning depth is not achieved.

 2. A large amount of sludge is formed, since, along with metal compounds extracted from water, coagulant and reagent mixtures co-precipitate.

 3. Are labor-intensive processes requiring significant costs and equipment.

 4. The need to use a large reagent farm.

 Also known is the electrochemical purification method based on the electrolysis of water and solutions, accompanied by two processes: anodic oxidation and cathodic reduction.

Its disadvantages include:
1. The need to manufacture the anode from insoluble alloys or coatings.

 2. The danger of toxic and explosive water electrolysis products.

 3. The implementation of the cathode of a material not subject to electrolytic dissolution and having a high overvoltage potential.

 4. High capital and operating costs caused by the significant cost of manufacturing and operating electrode systems and power supplies.

 5. The formation of deposits on the surface of the electrodes, conducting to their passivation.

 6. High power consumption.

 As the closest analogue to the method for producing drinking water and treating industrial effluents, the method of electrocoagulation of suspended and dissolved harmful impurities due to hydroxides of iron, zinc, aluminum and other metals released into the aqueous solution during the electrochemical oxidation of anode and cathode materials is described in the book: I.G. Krosnoborodko. Destructive wastewater treatment from dyes, 1988, 192 s./s. 172, 173, fig. 4.24.

The disadvantages of the method include:
1. Large specific consumption of the anode and cathode metal.

 2. Relatively high power consumption.

 3. Insufficient degree of water purification.

 4. Complex and expensive installations for the removal of fine suspensions of hydroxides of iron, zinc, aluminum and other metals.

 A device for controlling an electrolyzer for producing hydrogen and oxygen in a plant containing the actual electrolyzer, a distilled water supply pump, two receivers on the output lines of hydrogen and oxygen is known (see the book Rosenbrock H. et al. Computational methods for chemical engineers, M.: Mir, 1968.- 443 s / s. 418, Fig. 12.1; p. 419-420, Fig. 12.2; p. 421).

1. Control:
1.1. Discrete values of the water level in the electrolyzer for conductivity.

 1.2. The pressure of hydrogen at the outlet of the cell.

 1.3. The pressure drop between the hydrogen and oxygen lines at the outlet of the cell.

 1.4. The differential pressure between the hydrogen and oxygen lines at the outlet of the receivers.

2. Regulate:
2.1. The water level in the electrolyzer with a control effect on turning on and off the pump for its supply.

 2.2. The pressure in the hydrogen line at the outlet of the cell with a control action on the actuator of the control valve (RC) after the receiver on its output line.

 2.3. The pressure difference between the hydrogen and oxygen lines at the outlet of the electrolysis cell with a control action on the drives of the RK of opposite operating principles established on the corresponding lines in front of their receivers.

 2.4. The pressure difference between the hydrogen and oxygen lines at the output of the receivers with a control action on the drive of the RK installed on the output of the oxygen line.

The disadvantages of this device are:
1. A large consumption of electricity associated with the lack of information on the electrical parameters of the electrolyzer and the control actions on the change in the mode of its operation.

 2. The fluctuation of the level in the electrolyzer in a large range causes unjustified disturbing effects on the control object, which leads to additional energy consumption.

 3. The lack of parameters for assessing the quality of incoming water causes an excessive consumption of electricity.

 As the closest analogue to the device, an automated installation of the process of electrocoagulation water treatment was adopted, containing a drive, pumps for supplying untreated water, pumping purified water and sludge, a mixer, a supply tank with a reagent, an electrocoagulator with scrapers, a sludge collector, a settling tank, a rectifier (see the book: Smirnov D.N. Automatic control of the processes of purification of natural and wastewater. - M .: Stroyizdat. 1985. - 312 s / s. 226, 227, Fig. XII.4.).

 The following parameters are used as information parameters: levels in the wastewater storage tank, electrocoagulator and supply tank; pH at the outlet of the mixer and transparency of water by means of a photoelectric turbidimeter at the outlet of the electrocoagulator.

 Regulate: the level in the supply tank by the impact on the RK of water supply from the electrocoagulator to return; pH - on the RK supply of reagent from the supply tank; level in the electrocoagulator - on the RC water outlet from it; water transparency - on the RK of water supply to the mixer.

The disadvantages of this installation are:
1. Unstable operation due to the lack of consideration of influencing factors for each regulatory circuit.

 2. Significant cost overruns of electricity and reagents in the conditions of occurrence of abnormal processes of passivation of the materials of the anode and cathode, which causes an increase in salt content and corrosion activity of the treated water.

 3. Correction of electrocoagulation modes from the composition and concentration of harmful impurities in the treated water is not provided.

 The aim of the invention is to reduce by 5-10 times the costs of both reagents and electricity in the production of drinking water and purification of industrial effluents, as well as the production of drinking water of the optimal composition of mineral salts and organoleptic impurities.

The essence of the invention lies in the fact that in the method of producing drinking water and purifying industrial effluents by electrochemical treatment of contaminated aqueous solutions and suspensions with metered reagents while continuously feeding into the cathode-anode space, followed by separation of the precipitate, an additional two-stage dosage of reagents and electrochemical treatment at a direct current density (0.1-1.5) • 10 ³ A / m ² and the simultaneous exposure to an electromagnetic field with an alternating electric about the field (1-15) • 10 ⁴ V / m with separation of the precipitate after each stage of the electric treatment, while before the first stage of the electrochemical treatment, the aqueous solution is acidified to pH 4.5-6.5 with an acidic reagent mixture of calcium salts of phosphoric, sulfuric and carbon dioxide acids with an optimal molar ratio of 1: 2: 3, respectively, and a total flow rate (5-25) • 10 ^-2 kg / m ³ , the acid precipitate is separated, and before the second stage of the electrochemical treatment, the solution is alkalinized to pH 8.5-8.6 alkaline reagent mixture of hydroxides of calcium, magnesium and sodium at an optimal molar the ratio of 4: 1: 2 and the total flow rate (40-90) • 10 ^-2 kg / m ³ , the alkaline precipitate is separated.

 When implementing this method in an automated installation for producing drinking water and treating industrial effluents, consisting of the first series-connected electrochemical reactor (ECR) with an electrode system and level and pH meters, and a sedimentation apparatus (ABO), a supply and discharge line for the RK, a rectifier block and a block of magnetic starters, additionally contains a second ECR and a second ABO, connected in series and installed after the first, parameter meters, including: three flow meters, two pH meters, conductometers, four current meters, two power meters, two differential pressure meters for measuring the differential pressure at the inlet and outlet of the ABO and two discrete differential pressure regulators, flow regulators of the reagent mixture, two analog conductivity regulators, as well as a microprocessor device (MPU), electropneumatic discrete converters ( ЭДП), ЭХР is double-circuit and equipped with an intensive stirrer with a straightening unit and meters of power consumed by the motors of the mixers, flow meters installed at the entrances to the first and second ECR and at the output of the second ABO, the level meters in the ECR are made piezometric, and the flow rate controllers of the reagent mixture are made in the form of variable capacity dispensers, the electric-electronic sensors are located on the cases of the Republic of Kazakhstan, made by shut-off (SAM) and installed at the entrance to the first ECR and at the entrances and discharge lines of the first and second ABO, the rectifier block is made in the form of a block of thyristor converters (BTP), and the MPU contains control and logic blocks, while the MPU inputs are from the first to twenty l the first are connected to the information outputs of the parameter meters, and the outputs of the MPUs from the first to the thirteenth are connected to the dispensers and to the air defense system via the electronic converter, the outputs from the fourteenth to the seventeenth are connected to the corresponding electrode systems of ECR via the BTP, and the outputs from the eighteenth to the nineteenth are connected to the corresponding ECM engines through the block of magnetic starters.

In order to justify the conformity of the proposed technical solution with the criterion of "industrial applicability" we give the following evidence:
1. The level of water consumption, expressed in liters per day per person, is an objective indicator of the cultural and sanitary conditions of society.

 Today, a significant part of the world's population is deprived of the opportunity to use purified drinking water, which determines the sad factor why, in every four out of five cases of serious diseases, their cause is the use of untreated water.

 Water is a product of primary vital importance. In order to protect public health, it should be provided with water of optimal composition, safe in epidemiological terms, harmless in chemical composition and with pleasant organoleptic properties.

 2. The use of traditional methods of water purification requires significant costs of reagent mixtures (chlorine, ozone, ferric chloride, aluminum sulfate, organic coagulants and flocculants, soda, lime), the constant shortage of which is aggravated by their increasing consumption, which leads to an ever-increasing and expensive expert supply these reagent mixtures.

 3. The low technical and technological level of traditional wastewater treatment plants and the significant consumption of technical-grade reagents do not allow drinking water that meets epidemiological requirements and quality certification standards, in particular, in the presence and composition of harmful toxic and allergenic impurities.

4. The salt content of natural waters is mainly determined by the number of cations: Ca ⁺² , Mg ⁺² , Na ^{+ 1} , K ^{+ 1} , and anions: HCO $\genfrac{}{}{0ex}{}{\text{-1}}{\text{3}}$ SO $\genfrac{}{}{0ex}{}{\text{-2}}{\text{4}}$ , Cl ^-1 . A number of other inorganic and organic salts with toxic cations and anions are also in ionic form.

 5. The total content of dissolved salts, acids and bases in natural water is most easily determined by the total electrical conductivity of the water. The use of this parameter as a measure of the integral concentration of electrolytes is based on the fact that natural waters are diluted solutions when their specific electrical conductivity is linearly dependent on the concentration of dissolved components. The mobility of ions in such solutions is not noticeably inhibited by the forces of their interaction.

 6. Also of great importance is the content in water of active hydrogen ions, fixed by pH. By the value of this parameter, control and regulation of many stages of the natural water purification process is implemented, since many types of electrochemical treatment of water proceed more efficiently only at certain pH values.

 7. The essence of the cleaning method consists in the sequence of the following technological operations: acidification, electrical treatment, filtration, alkalization, electrical processing and filtering, determined by the type and composition of the reagent mixtures and modes of electrical processing.

8. An acidic reagent mixture (PC1) of calcium salts of phosphoric, sulfuric and carbonic acids is introduced into the initial stream of purified aqueous solutions and suspensions in order to acidify it in an optimal molar ratio of 1: 2: 3, respectively, and a total flow rate in the range of (5-25) • 10 ^-2 kg / m ³ in continuous or discrete modes with constant stirring of the resulting reagent mixture (OPC). The control of the amount of PC1 supplied to the OPC is carried out at a given pH value, which is in the range of 4.5-6.5 pH units and is specified depending on the type and composition of impurities in the purified aqueous solutions and suspensions according to the quality indicators of purified water. The resulting acidic reaction mixture (RRS) is fed into ECR 1 with recirculation of the stream with vigorous stirring, where it is repeatedly electrically processed in the anode-cathode space with the following parameters: DC current density (0.1-1.5) • 10 ² A / m ² and the simultaneous exposure to an electromagnetic field with an alternating electric field strength (0.1-1.5) • 10 ⁴ V / m, the value of which is selected depending on the type and composition of the ODP with the control of this stage of electric processing according to the results of analysis (pH, electrical conductivity and others parameters).

 9. Intensive mixing of cattle causes activation of reactions on the surface of the electrodes by mixing the products of the cathodic and anodic reactions and their mechanical removal, as well as the resulting passive and slurry films. The presence of multiple circulation of cattle through an electric field of variable intensity of the anode-cathode space, creating an electromagnetic field, improves its coagulation properties; due to the high electromagnetic susceptibility of the reagent mixture, dehydration of smaller structures occurs with the acceleration of their aggregation into larger complexes, which positively affects the next stage in the separation of the formed precipitate of structured harmful impurities.

 From the obtained cattle, the incoming and formed suspended solids are removed in the sediment separation apparatus - ABO (for example, sedimentation tank, filter, separator, etc.).

10. An alkaline reagent mixture (PC2) of hydroxides: calcium, magnesium and sodium is introduced into the clarified acidic liquid, purified from suspended solids in order to alkalize it, with an optimal molar ratio of 4: 1: 2, respectively, and a total flow rate (40-90) • 10 ^{- 2} kg / m ³ , providing complete precipitation of dibasic calcium phosphate with an excess of calcium ions in the treated water 7 • 10 ^-3 kg / m ³ and magnesium ions 3 • 10 ^-3 kg / m ³ to the concentrations established by the standards or MPC for purified aqueous solutions. The amount of PC2 supplied to the OPC is controlled at a given pH value, which is in the range of 8.4-8.8 pH units, and is set depending on the composition of the clarified acidic liquid, as well as on the type and regulated composition of purified alkaline water.

 The resulting alkaline reaction mixture (ALS) is fed into an ECR of the same design and principle of operation as in the treatment of cattle, and with the same electrical parameters of electric processing in the anode-cathode space.

 From the obtained SHRS is the removal of the formed suspended solids in the ABO.

 The invention is illustrated by a functional diagram of an automated installation for the production of drinking water and the treatment of industrial effluents, shown in FIG. 1, where material flows are denoted through Roman numerals IV, information channels from sensors to the IPC are indicated through the letter X with digital indices 1-21, and channels of control actions coming from the IPC, BTM, and BMP through the letter Y with digital indices 1-13 to SAM, OK drives to stirrer engines and electrode systems.

 An automated installation for the production of drinking water and purification of industrial effluents from harmful impurities consists of 2 ECRs 1 and 2 and 2 ABOs 3 and 4, dispensers 5 and 6 for supplying reagent mixtures PC1 and PC2, respectively.

 ECR 1 and 2 contain an intensive stirrer 7, an agitator motor 8, a straightening unit 9, two electrode systems 10.

 The installation is controlled using MPU 11: electrode systems 10 ECR 1 and 2 through BTP 12, the motors of the agitators 7 ECR 1 and 2 through BMP 13.

1. Control:
1.1. The parameters of the input stream 1 of untreated drinking water or industrial effluents supplied to the installation, namely: pH, electrical conductivity and flow rate using sensors 14, 15 and 16, respectively, with the registration of their values on MPU 11.

 1.2. SEC parameters 1.

 1.2.1. The current consumed by the electrode systems 10, by means of ammeters 17 and 18 with normalizing converters with the output signal to the MPU 11.

 1.2.2. The power consumed by the motor of the mixer 8, using a power meter 19 with the registration of its value on the MPU 11.

 1.2.3. The degree of filling of the ECR by means of a piezometric indicator of the PIU level, consisting of an air flow regulator (РРВ) 20, a piezometric tube (ПТ) 21 and a head 22, with the parameter value recorded on the MPU 11.

 1.2.4. The pH and electrical conductivity of the water at the outlet of the ECM using the corresponding flow sensors 23 and 24 with the registration of their values on the MPU 11.

 1.3. Parameters of the first ABO 3.

 1.3.1. The pressure drop at the inlet and outlet of the ABO by means of a differential pressure gauge 25 with registration of its value on the MPU 11.

 1.3.2. The electrical conductivity and water flow at the outlet of the ABO using a flow conductivity meter 26, a flow meter 27 with the registration of their values on the MPU 11.

 1.4. ECR parameters 2.

 1.4.1. The current consumed by the electrode systems 10, by means of ammeters 28 and 29 with normalizing signal converters with registration of their values on the MPU 11.

 1.4.2. The power consumed by the motor of the mixer 8, using a power meter 30 with the registration of its value on the MPU 11.

 1.4.3. The degree of filling of the ECR by means of a PIE, consisting of RRV 31, PT 32 and head 33, with its value recorded on MPU 11.

 1.4.4. pH and electrical conductivity of water at the outlet of the ECM using the appropriate sensors 34 and 35 with the registration of their values on MPU 11.

 1.5. Parameters of the second ABO 4.

 1.5.1. The pressure drop at the inlet and outlet of the ABO by means of a differential pressure gauge 36 with registration of its value on the MPU 11.

 1.5.2. The flow rate and electrical conductivity of treated drinking water or industrial effluents V at the outlet of the ABO using the appropriate sensors 37 and 38 with the registration of their values on MPU 11.

2. Regulate:
2.1. In ECR 1.

 2.1.1. The current strength in the electrode systems according to signals from current sensors 17 and 18 through the information channels X4 and X7 sent to the MPU 11, with the issuing of control actions through the BTP 12 through the channels Y2 and Y5 by the voltage supplied to the electrode systems 10, with correction for the value of the signal from the conductivity sensor 24 at the output of the ECM 1.

 2.1.2. pH at the outlet of the water from the ECM 1 according to the signal from the pH sensor 23 through the information channel X8 supplied to the MPU 11, with the issuing of a control action from it through the command channel Y3 to the dispenser 5 of the PC I supply with correction of the control action according to the pH values of the water in the input stream by the signal from the sensor 14 through the information channel X1 and its flow rate by the signal from the sensor 16 through the information channel X3.

 2.2. ECR 2.

 2.2.1. The current strength in the electrode systems 10 according to the signals from current sensors 28 and 29 through the information channels X12 and X15 sent to the MPU 11, with the issuance of control actions from it through the BTP 12 through the command channels Y8 and Y11 by the amount of voltage supplied to the electrode systems 10 , with correction for the value of the signal from the conductivity sensor 35 of the water at the outlet of the ECR 2.

 2.2.2. pH at the exit from ECR 2 by a signal from a pH sensor 34 through the information channel X16 supplied to the MPU 11, with the issuance of a control action from it through channel Y10 to the dispenser 6 supply PC II.

3. Manage:
3.1. ECR 1.

 3.1.1. The agitator engine 8, according to the signal from the PIU 22 via the information channel X6 to the MPU 11, followed by command action from the MPU 11 through the BMP 13 through channel Y4.

 3.1.2. SAM 39 supply of untreated drinking water or industrial effluents I to ECR 1 by command from the MPU 11 through channel Y1 through the EAF 40 with the action on the actuator of this valve to open it.

 3.1.3. By switching on the electrode systems 10 and the dispenser 5 according to a signal with a higher value compared to the signal for starting the mixer 8 with PIE 22 via the information channel X6 on the MPU 11 and by the signal from the power meter 19 consumed by the engine 8 of the working mixer 7 through the information channel X5 on MPU 11, where they implement the logical multiplication function "AND", followed by command action from MPU 11 on channel Y3 through BTP 12 on channels Y2 and Y5 on the corresponding actuators.

 3.2. ABO 3.

 3.2.1. SAM 41 water supply from the ECM 1 to ABO 3 by the increased value of the signal from the differential pressure gauge 25 through the information channel X10 to the MPU 11 with the subsequent command action from the MPU 11 through the channel Y6 through the EHP 42 to the actuator of this valve to close it.

 3.2.2. SAM 43 draining the contaminated sediment IV from the ABO according to the increased value of the signal from the differential pressure gauge 25 through the information channel X10 to the MPU 11 and by command from the MPU 11 through the channel Y7 through the EAF 44 with the action of the valve on its opening to open it.

 3.2.3. When the drop is reduced to the minimum value at the end of the sediment flush, the positions of the air defense missile defense rods 41 and 43 are reversed by the signal from the differential pressure gauge 25 and the command from the MPU 11.

 3.3. ECR 2.

 3.3.1. The agitator engine 8, according to the signal from the PIU 33 via the information channel X13 to the MPU 11, followed by command action from the MPU 11 through the BMP 13 through channel Y9.

 3.3.2. By turning on the electrode systems 10 and starting the dispenser 6 according to a signal with a higher value in comparison with the signal for starting the mixer motor with ПИУ 32 via the information channel X13 on the MPU 11 and by the signal from the power meter 30 consumed by the engine 8 of the working mixer 7 through the information channel X14 on MPU 11, where they implement the logical multiplication function "AND", followed by command action from MPU 11 on channel Y10, and through BTP 12 on channels Y8 and Y11 on the corresponding actuators.

 3.4. ABO 4.

 3.4.1, SAM 45 water supply from the ECR 2 to the ABO 4 by the increased value of the signal from the differential pressure meter 36 through the information channel X18 to the MPU 11 with the subsequent command action from the MPU 11 through the channel Y12 through the EHP 46 to the actuator of this valve to close it.

 3.4.2. SAM 47 discharge of contaminated sediment IV from the ABO by the increased value of the signal from the differential pressure meter 36 through the information channel X18 to the MPU 11 with the subsequent command action from the MPU 11 through the channel Y13 through the ЭДП 48 to the actuator of this valve to open it.

 3.4.3. When the drop is reduced to the minimum value at the end of the sediment flush, the positions of the SAM rods 45 and 47, by the signal from the differential pressure gauge 36 and the command from the MPU 11, are reversed.

The installation operates as follows:
1. In start-up mode.

 1.1. On command from MPU 11 through channel VI through EPD 39 OK 39 opens and untreated water enters ECR 1.

 1.2. As soon as the degree of filling of the ECM 1 reaches the value of the first setpoint in the MPU 11 reference block in the readings of the PIU 22 on channel X6, the command on channel Y4 to turn on the motor 8 of the mixer 7 follows from MPU 11.

 1.3. Upon reaching the degree of filling of EHR 1 of the second higher value of the set point in the MPU 11 set unit in the readings of the PIU 22 on channel X6 and the presence of a signal on the power consumed by the agitator motor 8 and measured by the sensor 19, on channel X5 and entering the MPU 11, where they are processed according to the logical multiplication scheme "I", from MPU 11, commands are sent through channels Y2 and Y5 to turn on the electrode systems 10 ECP 1, through channel Y3 to start the dispenser 5 of the feed PC I and through channel Y6 through the EPD 41 to open OK 40 water supply to ABO 3.

 1.4. When the ABO 3 is completely filled, which is recorded according to the readings of the differential pressure gauge 25 and the conductometer sensor 26 in the outlet pipe of the ABO through the channels X10 and X11 on the MPU 11, water flows to the next ECR 2.

 1.5. Upon reaching the filling level of ECR 2 of a lower value of the set point in the MPU 11 task unit according to the readings of the ISF 33 on channel X13 with MPU 11, a command on channel Y9 to turn on the motor 8 of the mixer 7 follows.

 1.6. As soon as the filling system of ECM 2 reaches a higher value of the set point in the MPU 11 reference unit in the readings of the PIU 33 on channel X13 and the presence of a signal on the power consumed by the agitator motor 8 and measured by the sensor 29 on channel X14 and entering the MPU 11, where they are processed on “I” logical multiplication scheme, from MPU 11, commands are sent through channels Y8 and Y12 to turn on the electrode systems 10 in ECM 2, through channel Y10 to start dispenser 6 for supply of PC II and through channel Y12 through EAF 46 to open OK 45 water supply to ABO 4.

 1.7. When the ABO 4 is completely filled, which is recorded according to the readings of the differential pressure meter 36 and the conductometer sensor 37 in the outlet pipe of the ABO through the channels X18 and X20 at MPU 11, the purified water IV is supplied to the consumer.

 2. In continuous operation.

 2.1. In continuous operation, the installation operates according to the algorithm set forth in the control and management systems of this installation.

 2.2. As soon as the pressure drop across ABOs 3 and 4 reaches the limit values recorded by means of differential pressure gauges 25 and 36 on channels X10 and X18 on the MPU 11, commands to close the channel through Y6 through the EHP 42 of the air defense system 41, and to open through the channel Y7 through the Y7 through EAF 44 SAM 43; to be closed by channel Y12 through an EHP 46 ADMS 45, and to open by channel Y13 through an EHP 48 SAMs 47: sediment is washed off from the surface of the air recirculation due to the volume of water in them.

 2.3. As soon as the pressure drop on the ABO 3 and 4 drops to the minimum values, commands are issued from the MPU 11 to switch the air defense systems to their original positions.

 The use of the invention will allow 5-10 times to reduce the consumption of reagents and electricity, significantly improving the quality of cleaning (tables 1 and 2), as well as rationalize the start-stop modes, which will additionally lead to savings in the consumption of reagents and electricity. In addition, this invention provides an optimal composition of mineral salts and organoleptic impurities in drinking water.

Claims (2)

1. A method of producing drinking water and purifying industrial effluents by electrochemical treatment of contaminated aqueous solutions and suspensions with metered reagents while continuously feeding into the cathode-anode space with subsequent separation of the precipitate, characterized in that they carry out a two-stage electrochemical treatment at a constant current density (0.1 - 1,5) • March ¹⁰ a / m ² and the simultaneous action of the electromagnetic field strength of the alternating electric field (1 - 15) • 10 ⁴ V / m sludge separation after each step elektroobrab tissue, while before the first stage of electrochemical treatment, the treated aqueous solution is acidified to pH 4.5 - 6.5 with an acidic reagent mixture of calcium salts of phosphoric, sulfuric and carbonic acids with an optimal molar ratio of 1: 2: 3, respectively, and a total flow rate (5 - 25 ) • 10 ^-2 kg / m ³ with reaching pH 4.5 - 6.5, the acid precipitate is separated, and before the second stage of electrochemical treatment, the solution is alkalinized to pH 8.5 - 8.6 with an alkaline reagent mixture of calcium, magnesium and sodium hydroxides with an optimal molar ratio of 4: 1: 2 and a total consumption e (40 - 90) • 10 ^-2 kg / m ^3, the precipitate is separated alkaline.  2. An automated installation for the production of drinking water and treatment of industrial effluents, consisting of the first series-connected electrochemical reactor with an electrode system and level and pH meters, a sedimentation apparatus, a supply and discharge line with control valves, a rectifier unit and a magnetic starter unit, characterized in which additionally contains a second electrochemical reactor and a second sludge separation apparatus, connected in series and installed after the first, parameter meters, VK Three flow meters, two pH meters, five conductometers, four current meters, two power meters, two differential pressure differential pressure gauges and two discrete differential pressure regulators installed at the inlet and outlet of sedimentation apparatus, reagent mixture flow regulators, two analog regulators electrical conductivity, as well as a microprocessor device and electropneumatic discrete converters, the electrochemical reactor is double-circuit and equipped with an agitator for intensive mixing with a straightening unit and power meters consumed by the electric motors of the mixers, flow meters are installed at the entrances to the first and second electrochemical reactors and at the output of the second sediment separation apparatus, level meters in electrochemical reactors are made piezometric, and the flow rate regulators of the reagent mixture are made in the form of variable capacity dispensers, electropneumatic discrete converters are located on the body of the control valves, made shut-off and installed At the entrance to the first electrochemical reactor, at the entrances and drainage outlets of the first and second precipitation apparatuses, the rectifier unit is made in the form of a thyristor converter unit, and the microprocessor device contains regulating and logical blocks the inputs of the microprocessor device from the first to the twenty first are connected to the information outputs of the meters parameters, and the outputs of the microprocessor device from the first to the thirtieth are connected to the dispensers and shut-off and control valves through elektropnev aticheskie digital converters, the outputs from the fourteenth to seventeenth connected to the respective electrode systems, the electrochemical reactors through the unit thyristor converters, and the outputs of the eighteenth nineteenth associated with the respective motors through the electrochemical reactor unit magnetic contactors.

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