Method of cleaning cationite filters from products of regeneration and iron compounds |
|||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||
IPC classes for russian patent Method of cleaning cationite filters from products of regeneration and iron compounds (RU 2332259):
    
 Method of purifying water, obtained in fischer-tropsch process / 2331592
Purified water is a water stream, with COD ranging from 20 to 500 mg/l, pH ranging from 6.0 till 9.0. Content of the above mentioned solid substances is less than 250 mg/l and the overall content of soluble solid substances is less than 600 mg/l. The method involves a primary treatment stage, which involves distillation to remove, at least, part of non-acidic oxygen containing hydrocarbons from the reaction Fischer-Tropsch water with obtaining primary enriched water stream; secondary treatment, involving extraction of the liquid for removal of at least, part of organic acids from at least, part of the primary enriched water stream with obtaining secondary enriched water stream; tertiary treatment, involving biological treatment for removal of at least, part of acidic oxygen containing hydrocarbons from at least, part of the secondary enriched water stream with obtaining of tertiary enriched water stream; and quaternary treatment, involving separation of the solid substances and liquid for removal of at least, part of the tertiary enriched water stream.
Method of waste water treatment from colorants / 2331590
Waste water treatment from colorants is performed using electrolytic process with supply of oxygen at pressure of 1.0 MPa, and current density 0.1 A/cm2 during 180 minutes in autoclave with bulk cathode from iron powder at its constant mixing in the magnetic field.
 Flow-through water electric activator / 2331589
Invention pertains to electrochemical treatment of water, used in industry and for economic needs. Flow-through water electric activator consists of housing, made from dielectric material and separated into anode and cathode chambers, with anode and cathode in it. The housing is also equipped with piping for separate discharge of processed water with negative and positive potentials. Each cathode and anode is done as perforated pipe of rectangular section, made from corrosion-resistant stainless steel. Inside the pipe fibered flow regulators are installed, which are perforated along all the area; fiber height is equal to pipe width; flow regulators are made from corrosion-resistant stainless steel. They have an electrical contact with inner surface of the pipe. To supply water into anode and cathode chambers, a supply piping with flow divider is installed; to discharge water from anode and cathode chambers, discharge sleeves are installed, that conjugated with chambers and discharge piping by cone reducers. Discharge piping is equipped with control valves.
 Device for cleaning water from oil products / 2331588
Device consists of a container and a sealed reservoir, linked by an overflow outlet. In the container, under the overflow outlet, there is transverse partition wall, with a gap to the bottom of the container. In the reservoir, there is a pipe shaped element, one of the walls of which is joined to the opening on the part of its perimeter, and the other wall is joined to the partition wall. One part of the pipe shaped element is designed for transmitting oil products, and the other is for water output.
 Method of processing highly polluted oily water, deposits and soil, and corresponding equipment / 2331587
Method includes preliminary processing of soil and/or deposits via washing it with technical cleansing agent (TCA)(TMC), cleaning the slurry from sand and its separation into three phases - sludge, used TCA solution and liquid petrochemicals, which are directed to allocation tank. Used TCA solution is refreshed, heated and sent back to first stage of the process. Oily water is processed simultaneously, filtered and then sent to allocation tank, where it is mixed with liquid petrochemicals. The mixture is heated, filtered and then sequentially evaporated. The mixture is first separated into water and antifloating emulsion with 60% of emulsion water, then processed by deemulsifying agent and modifier, at constant mixing and heating, and then evaporated until 1-10% of water remains. Separated and evaporated water is decanted and supplied sewers collecting main. Sludge, gathered by decanting and separated from slurry, is sent to sludge well. Sand, separated from slurry, is gathered and used in other processes. Additional water treatment to fishery waters bodies standard is also possible, as well as recovery of TCA solution using additionally treated water. The equipment used includes tank for contaminated soil and deposits, tank for oil contaminated water, as well as units, produced by industry, which include grit catcher, separators, heaters, filters etc.
 Plant for purifying underground and sewage water / 2331586
Plant consists of working valves 1 - 8, 11,12, valve-sample collection tap 9, pressure filter 15 with a heavy load, filtering load 22, holding tank 16, pressure holding pump 17, pressure valve for releasing air 13, and a supply pipe 25, which is an ascending arm at the same time, providing for an air gap in the holding tank 16. Injector 24 with a calibrated opening for water aeration and reverse valve 18 for air intake, are fitted on filter 15, between the upper and lower flanges of which are fitted with piezometer 14 for controlling complete filling of the filter with initial water. Electromagnetic valve 19 is inserted into the plat in the working network, for regulating operation for which automated control system 10 is connected to the electrodes of capacitor 16. Pressure regulator 20 for maintaining constant rate of filtration is fitted in front of electromagnetic valve 19.
Plant for purifying underground and sewage water / 2331586
Plant consists of working valves 1 - 8, 11,12, valve-sample collection tap 9, pressure filter 15 with a heavy load, filtering load 22, holding tank 16, pressure holding pump 17, pressure valve for releasing air 13, and a supply pipe 25, which is an ascending arm at the same time, providing for an air gap in the holding tank 16. Injector 24 with a calibrated opening for water aeration and reverse valve 18 for air intake, are fitted on filter 15, between the upper and lower flanges of which are fitted with piezometer 14 for controlling complete filling of the filter with initial water. Electromagnetic valve 19 is inserted into the plat in the working network, for regulating operation for which automated control system 10 is connected to the electrodes of capacitor 16. Pressure regulator 20 for maintaining constant rate of filtration is fitted in front of electromagnetic valve 19.
Method of hydration of biopolymers and product from hydrated biomass / 2331478
Method is characterised by the fact that before mixing with the biomass the aqueous solution of salts it is subjected to processing by ultrasonic cavitations with the set ratio of intensity of the ultrasound to a square of hydrostatic pressure in the solution, being the similarity parameter of the process. Mixing can be carried out during the crushing of the biomass by introduction of a solution in preliminary crushed biomass or immersing of the biomass into the solution. The product from the hydrated biomass, obtained as a result of the use of any of the methods of mixing will contain independent of the concentration and composition of the solution a quantity of the moisture connected with biopolymers.
 Method of cleaning water from weighed substances / 2331455
Water is cleaned from large-dispersed, medium-dispersed and from small-dispersed particles with the use of radiation with acoustic waves of sound and ultrasound diapasons of frequency in a sedimentation tank for reverse and waste water, in the first and second sedimentation tanks. In addition the realisation of its physical purification from large scale dispersion and fine dispersion of particles in the whole volume sedimentation for reverse and waste water by means of periodic with alternation of the scheduled radiation and interval radiation in the water medium in the whole volume of hydro-acoustic waves infrasonic frequency range. Additional realisation of its physiochemical cleaning from over self-dispersal - of the size 0.5-5 micrometers, particles in the first and second additional sedimentation tanks by means of continuous radiation of electromagnetic waves in the places of discharge of the upper layer of water. Additional realisation of its chemical cleaning from a colloid size 0.5 micrometers, particles in sedimentation tank by means of leading waters into discharge from the second additional sedimentation tank of chemical reagents: coagulants or flocculants are near insignificant, like minimum, in small order, than by regular cost of chemical reagents.
Method of cleaning water from weighed substances / 2331455
Water is cleaned from large-dispersed, medium-dispersed and from small-dispersed particles with the use of radiation with acoustic waves of sound and ultrasound diapasons of frequency in a sedimentation tank for reverse and waste water, in the first and second sedimentation tanks. In addition the realisation of its physical purification from large scale dispersion and fine dispersion of particles in the whole volume sedimentation for reverse and waste water by means of periodic with alternation of the scheduled radiation and interval radiation in the water medium in the whole volume of hydro-acoustic waves infrasonic frequency range. Additional realisation of its physiochemical cleaning from over self-dispersal - of the size 0.5-5 micrometers, particles in the first and second additional sedimentation tanks by means of continuous radiation of electromagnetic waves in the places of discharge of the upper layer of water. Additional realisation of its chemical cleaning from a colloid size 0.5 micrometers, particles in sedimentation tank by means of leading waters into discharge from the second additional sedimentation tank of chemical reagents: coagulants or flocculants are near insignificant, like minimum, in small order, than by regular cost of chemical reagents.
Method of regenerating basic anionite catalysts / 2322295
Invention relates to regeneration of basic anionite catalysts for process of production of alkylene glycols via hydration of corresponding alkylene oxides. Method according to invention consists in treatment of spent catalyst with aqueous solution of inorganic salts of iodine and inorganic acids or with hydroiodic acid aqueous solution.
Method of separating ion-exchange resins / 2315660
Invention is dealing with separation of cationite/anionite mixture utilized in multifunctional filters in deep water treating systems to be further regenerated. Method is based on difference in densities of the two ionites and employs composition constituted by fluorine-containing saturated acyclic hydrocarbon or fluorine-containing ether, which have densities within a range of 1.30-1.90 kg/dm3, and saturated acyclic hydrocarbon of general formula CnH2n+2 (n=6-9) having density between 0.65 and 0.8 kg/dm3.
Method of purification of the washing alkaline solution of the bottle washing machines / 2310612
The invention is pertaining to the methods of purification of the washing alkaline solution of the bottle washing machines from the suspended particles, the carbonates, the aluminates and other impurities introduced in it at washing of the reusable bottles. The method provides for batching into the polluted washing solution of the spent regeneration solutions (SRS) of the ion-exchange Na-cationite screens or N-cationite screens containing the calcium chloride and the magnesium chloride with the subsequent clarification of the liquid. The volume of the batched reclaim is accepted of not less than 3 % from the volume of the purified washing solution. The method of the invention allows to raise duration of usage of the washing alkaline solution without deterioration of its washing characteristics, to restore the chloride-containing reclaims, and also to diminish the discharge of the pollutants and to reduce expenditures on buying of the chemical reactants for purification of the washing alkaline solution. The settlings and the tailings formed at purification of the washing solution are subjected to dehydration and utilization.
 Method of water treatment / 2298529
Proposed method consists in passing water to be cleaned through layer of floating inert material and ion-exchange resin in downward direction and regeneration of ion-exchange resin by pressing its layer by liquid medium flow in upward direction, passing of regenerating solution, gravity sedimentation of resin and washing-off residues of regenerating solution. Filtration is performed through at least two filters mounted in succession; charge of ion-exchange resin is so selected that volume of resin in first filter is no more than 40% of total amount of resin used for cleaning; at regeneration, resin is so pressed that it passes through stage of formation of fluidized layer. In pressing the resin during raising it, rate of flow in first filter shall be below rate of flow required for piston-like raising of resin by at least 25%. Liquid is delivered to first filter in pulse mode or raising of resin is carried out simultaneously with bubbling of gas through it.
 Method of modification or regeneration of zeolites and the device for its realization / 2295388
The invention is pertaining to the methods and devices for modification or reregeneration of zeolites concerning the group of the ion-exchangers - cationites. The method provides, that the bosh is divided into two chambers by the partition having the properties of the fine filter of the water. The electrodes are introduced into the chambers. One of the chambers is loaded with the zeolites. The bosh is filled with the water. The chamber with zeolites is loaded with the salts, which cations are used for modification and regeneration of the zeolites in the quantities, which are necessary and sufficient for formation in the water of the concentration of these salts of 1 - 10 %. Then the direct current voltage of 5-35 V is fed to the electrodes: the negative voltage is fed to the electrode in the chamber with the zeolites, and the positive voltage is fed to other electrode, switch on the device used for the zeolites washing, wash the zeolites in the bosh with the water solutions of salts within 3-10 hours. The invention presents the device for realization of the method. The technical result of the invention is the increased intensity of the ion exchange process in zeolites, the reduced duration of the process, the decreased amount of the salts consumption for regeneration.
Method for reducing of hydroponic substrates / 2281648
Method for reducing of hydroponic substrate of natrolite and vermiculite involves washing substrate with water; preparing aqueous suspension of washed out substrate; providing bubbling thereof with air; performing supersonic processing; removing by means of water; washing substrate; drying and processing in electric field of 300-350 kV/m intensity.
 Method of regeneration of ion-exchange material / 2258563
Proposed method includes simultaneous treatment of material in DC field of high-frequency generator, continuous supply of water through layers of ion-exchange material located between electrodes; one of them performs function of anode; it is connected with high-frequency generator output; treatment of ion-exchange material is performed at constant DC magnitude equal to (0.1-12) V and frequency of AC fluctuations equal to (6.5-7.3)MHz at respective resonance frequency of water ion oscillation; cathode is connected with second output of high-frequency generator.
Method of regeneration of low-acid carboxylic cationites / 2257265
Invention relates to regeneration of cationites used on water-softening plants. In this process, of low-acid carboxylic cationites are converted into their H-Na form by consecutively passing (i) acid in stoichiometric proportion until pH 3.9-4.3 is achieved and (ii) 1.0-1.5% sodium chloride solution through cationite layer.
Fluorine-containing emulsifier regeneration method / 2255807
Invention relates to treatment of waste waters originated from fluorine-containing polymer production. Fluorine-containing emulsifiers, in particular perfluorooctanoic acid, are bound by anion-exchange resins. Further, indicated emulsifiers are washed out from anionite with water-organic mixture containing some amount of ammonia and having boiling temperature below 150°C. Ammonia-containing solvent is preferably distilled away and emulsifier and ammonia-containing solvent are reused.
Method of reusing h-cationite filter regenerates / 2244594
Invention relates to methods of removing hardness salts from regenerates and can be used in water treatment processes in heat-and-power engineering, chemical, petrochemical, food, and other industries provided with ion-exchange water-desalting filters. Method is accomplished by precipitation of hardness salts involving recycle of precipitate treated by alkali solution followed by passage of supernatant through H-cationite filter. Treated precipitate accumulated in preceding settling cycles is recycled into regenerate and settling-subjected solution is passed through cationite filter to produce purified sulfuric acid further used for regeneration of H-cationite filters in water-treatment cycle. Precipitate is treated with alkaline regenerate from OH-anionite filters or with alkali solution obtained from electrolysis of regenerates with pH not below 11. Amount of regenerate introduced into accumulator-settler should be at least 20 kg/m3.
Method of reusing na-cationite filter regenerates / 2244593
Invention concerns water-supply means for feeding power plants and boiler installations provided with ion-exchange water-desalting filters. Preparation of purified sodium chloride solution followed by reuse thereof as regeneration solution for Na-cationite filters is accomplished by passing regenerate through electrolyzer, then settling catholyte to precipitate hardness salts, neutralizing solution with hydrogen chloride formed in electrolysis process, and passing neutralized solution through supplementary Na-cationite filter. pH value of as-electrolyzed solution is maintained not below 11.0.
|
FIELD: technological processes. SUBSTANCE: invention pertains to methods of cleaning cationite filters from products of regeneration and iron compounds and is designed for use in an iron exchange system of water treating works, heat power engineering, public service boilers, as well as industries which use treated water in their technological processes. The method involves passing water from top to bottom through the cationite, with hardness of not less than 2.5 mg-eq/l as calcium, speed of 6-8 m/h and flow of water to residual hardness of 0.03 mg-eq/l as calcium, in the washing water. Cleaning is done with specific flow of not more than 3 m3/m3 of cationite in two stages. On the first stage, initial water is passed through the cationite, treated by a magnetic field to residual hardness of 0.7 mg-eq/l as calcium, in the washing water. The cationite is then cleaned in stagnant magnetic water for 1-2 hours. On the second cleaning stage, initial water is passed through the cationite without magnetic treatment. Magnetic treatment is done by passing initial water at a speed of 0.5-1.5 m/s through a pipe shaped magnetic device, based on permanent magnets with flux density of 0.2-0.35 tesla. The invention provides for increasing economical efficiency of the method and lowering ecological damage by reducing specific flow of cleaning water, increasing the working exchange capacity of the cationite due to increased speed and degree of cleaning from products of regeneration and iron compounds. EFFECT: increased economical efficiency of the method of cleaning cationite filters from products of regeneration and reduced ecological damage. 2 cl, 3 dwg, 3 tbl, 2 ex
The invention relates to a method of washing cationite filters from the products of regeneration and iron compounds to reduce costs of water, reagents, to increase the working exchange capacity of the cation and is intended for use in the system of ion-exchange water of thermal power plants (TPP, TPP), boiler and utilities, as well as in industries that use softened water in technological processes. The well-known "Method of simultaneous softening and iron removal water"described in the patent of Russia №2176988, publ. 20.12.2001, In the known method applies processing of cation exchange resin KU-2-8 in the Na-form solution of the trylon B at the stage of softening the water and at the stage of regeneration of the cation exchanger, the basic reagent is sodium chloride by washing with water. High water softening and iron removal in this way is achieved by the known ability of the trylon B (accurate chemical name of which ethylenediaminetetraacetate sodium) to form complex compounds with ions of iron, calcium, magnesium. Known widespread use of the trylon B in the analysis of ion stiffness. The disadvantage of this method is that it is almost impossible to apply on an industrial scale because of the high cost and toxicity of the trylon B. In the described method, the expert is ment conducted only on a laboratory column with a volume of cation exchange resin 15 cm 3. The impossibility of using the method on an industrial scale is caused, first of all, its expensiveness, as heavy consumption of reagent trylon B value of 225 thousand rubles per ton way economically viscosimeter, secondly, environmental reasons, since the implementation of the method described above Trilon B passes into the waste water in the form of complex compounds with calcium, iron, and, in addition, and in free form. It is known that Trilon B on the status of the standard MAC when discharged into water bodies refers to high-risk substances. Known "Method of use of chelating agents in the process of regeneration-Na-cationite filters described in article Clarabow, Avibhasha and others, published in the journal "Energy and water", No. 1, 2001, p.73-76. In the known method in the main regeneration solution of sodium chloride was added to the solution complexone NTF (nitrilotriethanol acid) with a concentration of 30-120 mg/l for the regeneration of the cation exchanger not only from ions of hardness, but also from iron oxide compounds. The result of the application of this method is the increase in the operating exchange capacity of the cation exchanger for subsequent regeneration cycle. The disadvantage of this method is that the combined company not only binds the iron compounds to remove them from the cation exchanger, but Sora is associated by the cation exchanger and, as noted by the authors, passivates the active, i.e. ion-exchange surface of the resin, which causes the complexity and instability of the technological method in General. Also the disadvantage of this method is the high toxicity of the applied NTF, which, as noted by the authors relates to organophosphorus compounds. It is known, for example, organophosphorus compounds included in the composition of some chemical warfare agents, and therefore represent a danger not only for the discharge of waste waters into water bodies (MPC NTF 1 mg/l), but also for staff. Known "Method of regeneration of ion exchange resins described in the patent of Russia №2144848 published 27.01.2000, In the known method before serving the main filter regenerating solution of sodium chloride used washing of the cation exchanger air / water mixture at a volume ratio air:water (2-10):1, which is supplied to the filter in pulse mode, with the system during washing is served from 1 to 1000 pulses. The result of this method is flotation of suspended particles, rust and other contaminants due to the supply when the filter washing water-air mixture and a 10% increase in the working capacity of the cation exchanger. The disadvantage of this method is the difficulty of controlling the volumetric air flow in the air / water mixture, which can lead to vanoucek floating inert layer (if used), and the cation exchange resin, moreover, the disadvantage is the large uncertainty of the mode of air supply and pulses (volumetric ratio of air: water (2-10):1, the supply of pulses from 1 to 1000). Known "Method of water treatment in the water treatment system described in the patent of Russia №2116260 published 27.07.1998, In a known way water is supplied to heat exchanger boiler installation, pre-treated in a tapered magnetic turbolister to reduce scale deposits on the walls of the equipment. The disadvantage of magnetic water treatment is that unlike ion-exchange method of water treatment this way softens water, and only partially prevents deposition on the walls of the apparatus scale of hardness salts, which are removed from the system continuous directional reset parietal stream of water. This disadvantage is due to the inability to use this method in water treatment systems before high pressure boilers in thermal power plants (TPP, TPP), as these systems require a high degree of softening water to 10 μg-EQ/L. The closest analogue, selected as a prototype, is a method of washing cationite filters from the products of regeneration described in the "guidelines for start-up, adjustment and EAC is ugiwaniu installations H-Na-zeolite softening", publishing house "Southampton", niitekhim, 1982, P.73-77, 127. In the described method, the cation exchange resin KU-2-8 after regeneration salt solution of sodium chloride washed with source water with hardness of not less than 2.5 mEq/l with a linear speed of the cleaning 6-8 m/h, with a specific consumption of wash water 6 m3/m3the cation exchanger to a residual hardness in wash water of 0.03 mEq/l (str in the copy of the prototype). Of the brands in the prototype of the cation exchanger was selected cation marks KU-2-8, as it is compared with cations other brands have the most complete and working exchange capacity and, consequently, for its cleaning required maximum specific consumption of wash water, which is reflected in the prototype. The result is described in the prototype method, regeneration and washing the cation exchange resin KU-2-8 achieved its working exchange capacity of not less than 950 g-EQ/m3when the total capacity 1650-1700 g-EQ/ m3(p.75 prototype). The disadvantages of the method of washing cationite filters as described in the prototype, is, first, a large share of the consumption of wash water (6 m3/m3cation exchanger for KU-2-8). In this specific discharge wash water total water consumption when washing the filter with the volume of the cation exchanger 17 m3amount of 102 m3(17 m3×6 m3/m3cation exchanger). If you consider that enterprises Teploenergo the key simultaneously work two or three filters, and their regeneration and washing are carried out in 2-3 days, the cost of a wash water in these enterprises are tens of thousands of m3per month. At high contents in the washing waters of the salt sodium chloride, and salts of hardness (hardness total at the beginning of cleaning up to 350 mEq/l) discharge of a large amount of water in the reservoirs through the sewers causes environmental damage, in this regard, enterprises have problems building and increasing the volume of liquid sludge ponds, enterprises impose penalties for the discharge of these waters into water bodies, and secondly, not enough high operating exchange capacity of the cation exchanger by ions of hardness in comparison with its full operating capacity. One of the reasons for the reduction of the working exchange capacity is insufficient washing of the cation from iron compounds, occupying vacancies hardness ions. The decrease in operating exchange capacity reduces the performance of the filter on softened water reduces the duration time of the working cycle to the regeneration of the cation salt solution of sodium chloride and subsequent cleaning, which increases the annual amount of regeneration and cleaning, increases the costs of reagents and water. The technical result of the claimed method of washing cationite filters from the products of regeneration and connect the developments of iron is to increase the economic efficiency of the method and reduce environmental damage when it is used by reducing the specific consumption of wash water (in m 3/m3cation exchanger), increasing the working exchange capacity of the cation exchanger by increasing the rate and degree of washing of the cation from the products of regeneration and iron compounds. The technical result of the claimed invention is achieved in that in the method of washing cationite filters from the products of regeneration and iron compounds, including passage through the cation exchanger from top to bottom of the source water with a total hardness of not less than 2.5 mEq/l speeds of 6-8 m/h and the flow of water to a residual hardness in wash water of 0.03 mEq/l, according to the invention, the washing is carried out with a specific water consumption of not more than 3 m3/m3the cation exchange resin in two stages, the first of which through the cation exchanger is passed the source water treated by the magnetic field, to a residual hardness in wash water of 0.7 mEq/l, then stop passing water, washing the cation exchange resin is carried out in stagnant minichannel water for 1-2 hours, in the second stage of washing through the cation exchanger miss the original, without magnetic treatment of water, while the magnetic treatment of water is produced by passing the source water at a rate of 0.5-1.5 m/s through a magnetic device, the tubular form is based on permanent magnets with magnetic induction 0,2-0,35 Tesla (2000-3500 Gauss). Due to the fact that in the method of washing cationite filters products from regenerate and iron compounds washing is carried out with a specific water consumption of not more than 3 m 3/m3the cation exchange resin in two stages, the first of which through the cation exchanger is passed the source water treated by the magnetic field, to a residual hardness in wash water of 0.7 mEq/l, then stop passing water, washing the cation exchange resin is carried out in stagnant minichannel water for 1-2 hours, in the second stage of washing through the cation exchanger miss the original, without magnetic treatment of water, while the magnetic treatment of water is produced by passing the source water at a rate of 0.5-1.5 m/s through a magnetic device, the tubular form is based on permanent magnets with magnetic induction 0,2-0,35 Tesla (2000-3500 Gauss), increases the economic efficiency of the method and reduces environmental damage by using this method by reducing the specific consumption of wash water (in m3/m3cation exchanger), increasing the working exchange capacity of the cation exchanger by increasing the rate and degree of washing of the cation from the products of regeneration and iron compounds. The inventive method of washing cationite filters from the products of regeneration and iron compounds has a "novelty", differing from the prototype of the above symptoms, and achieving perceived by the applicant of the result. The popularity of the influence of the above mentioned distinguishing features on the specified technical result is e confirmed by the known technical solutions therefore, the applicant believes that the claimed method of washing cationite filters from the products of regeneration and iron compounds meets the criterion of "inventive step". The inventive method of washing cationite filters from the products of regeneration and iron compounds can be widely used in ion-exchange water of thermal power plants (TPP, TPP), boiler and utilities, as well as in industries that use softened water in technological processes, and therefore meets the criterion of "industrial applicability". The essence of the proposed method of cleaning cationite filters from the products of regeneration and iron compounds is illustrated by drawings, where: figure 1 - diagram of water consumption for washing the cation exchange resin KU-2-8 depending on the method of washing (the amount of cation exchanger 17 m3); figure 2 - chart showing the flow of water for washing the cation exchange resin KU-2-8 (m3/m3cation exchanger) depending on the method of washing; figure 3 - graphs washing the cation exchange resin KU-2-8 from iron (Fetotaldepending on the method of washing. The method of washing cationite filters from the products of regeneration and iron compounds is that when passing through the cation exchanger from top to bottom of the source water with hardness of not less than 2.5 mEq/l / min net with the calling 6-8 m/h and the flow of water to a residual hardness in wash water 0, 03 mEq/l, washing is carried out with a specific water consumption of not more than 3 m3/m3the cation exchange resin in two stages, the first of which through the cation exchanger is passed the source water treated by the magnetic field, to a residual hardness in wash water of 0.7 mEq/l, then stop passing water, washing the cation exchange resin is carried out in stagnant minichannel water for 1-2 hours, in the second stage of washing through the cation exchanger miss the original, without magnetic treatment of water, while the magnetic treatment of water is produced by passing the source water at a rate of 0.5-1.5 m/s through a magnetic device, the tubular form is based on permanent magnets with magnetic induction 0,2-0,35 Tesla (2000-3500 Gauss). During the development of the proposed method conducted research on the influence of magnetic treatment of water and salt solutions of NaCl on all major stages of ion exchange technology: magnetised source of water on stage chemisorption (absorption) cation exchange resin rigidity and iron ions, the magnetization that of the NaCl solution used in the regeneration of the cation exchanger, and the magnetised water used for washing the cation exchange resin from the products of regeneration and iron compounds. It was found that at the stage of chemisorption (absorption) rigidity and iron ions application minichannel water affects this process, the magnetization that salt solutions aCl at the stage of regeneration of the cation exchanger has almost no influence on this process and only use minichannel water at the stage of washing the cation exchange resin from the products of regeneration and iron compounds is highly effective. Based on these studies when developing a method of washing was developed in the second stage of washing, in which, along with intensive wash from the hardness ions and iron ions is provided by the displacement minichannel water the source water for subsequent to the washing step of ion sorption stiffness. The mechanism of the effect of magnetic treatment of water is as follows. Conducted by the authors claimed methods laboratory studies have shown that the implementation of this method when the magnetization that changes the physico-chemical properties of the source water, in particular, the kinematic viscosity of water when the magnetization that is reduced from 1,002 to 0,950 mm2/s It is known that the viscosity of the water indicates the change in the structure of liquids, in particular, when magnetised water according to some researchers is the destruction hydrate and solvate shells compounds of calcium and magnesium in the source water, the water molecules become more mobile, increasing the rate of their diffusion in globule of the cation increases the rate of desorption (washing) of the cation from the rigidity and iron ions and, consequently, reduces the specific consumption of water for washing. It should be noted that softened water, i.e. water containing hardness salts, according to various ASCS is adavani not magnetivity. Laboratory and pilot tests of the method of washing cationite filters from the products of regeneration and iron compounds described in the examples, experience 1 experience 2. Experience 1 At power plant of the city of Chelyabinsk on the filter is loaded cation exchange resin KU-2-8 with a capacity of 17 m3, conducted pilot testing in two ways cleaning cationite filters from the products of regeneration and iron compounds, according to the first method described in the prototype, and on the second way of washing cationite filters from the products of regeneration and iron compounds claimed in the invention. Water consumption for washing was determined by the flow meter. When this magnetic processing wash water held in the prescribed recovery line-washing near the magnetic filter device. To determine the relative speed of the process of washing the cation exchange resin according to the present method and by the method described in the prototype, the analysis determined the residual concentration of hardness ions in the wash waters after a certain period of time. On the basis of these data determined the effective order of the process of washing and hoped kt - effective rate constants of the process of washing for each point according to the formula: kt=1/tlnCo/Stwhere: t is the time from the beginning of the washing; Withabout- the initial concentration of the ones hardness in wash water; Ctthe concentration of hardness ions in wash water at time t, which is presented in table 1.
As follows from the presented data in table 1, the rate constant of the process of washing the cation exchange resin by SPO is trained, the claimed invention by 40.9% above the rate constant washing of the prototype. It should be noted that during the experiment for that and other ways to a residual concentration of hardness in wash water of 0.03 mEq/l is the rate constant does not change in a physical sense the rate constants. Water consumption for washing the cation exchange resin KU-2-8 depending on the method of washing (the amount of cation exchanger 17 m3) is presented in figure 1. The three-dimensional chart 1 shows the water flow for a method on the prototype of three-dimensional chart 2 - water consumption for the method according to the present invention (with two stages). As follows from the data presented in figure 1, the water consumption for washing the cation exchange resin KU-2-8 for a method claimed according to the invention, in 2 times smaller than the prototype. The specific consumption of water for washing the cation exchange resin KU-2-8 (m3/m3cation exchanger) depending on the method of washing are presented in figure 2. On a volume chart 3 presents the specific consumption of water for washing the cation exchange resin for a method on the prototype, on a volume chart 4 - the specific consumption of water for washing the cation exchange resin for the method according to the present invention (with two stages). As follows from the data presented in figure 2, the specific consumption of wash water is 6 m3/m3the cation exchanger according to the method described in the prototype, and 2,87 m /m3the cation exchanger according to the method claimed in the invention (2,47 m3/m3the first stage, 0.4 m3/m3the second stage). In addition, it should be noted that industrial filter (load volume 17 m3also there was an experiment conducted by the washing of the cation with the use of the original without magnetic treatment of water, but with the introduction of the two-stage cleaning up residual hardness in wash water of 0.7 mEq/l, the termination of the transmission of water and washing the cation exchange resin in stagnant water for 1-2 hours, followed by passing water until the end of the washing. It was found that water consumption for washing has not changed. Performance cationite filter on softened water (filtrate) for one filter cycle, the working exchange capacity of the cation exchanger, depending on the method of washing are presented in table 2.
As can be seen from table 2, the working exchange capacity when washing the cation exchange resin according to the present method of the invention is increased by 19%. Experience 2 To assess the degree of washing cationite filter from iron compounds claimed in the invention method, it is necessary to have data on the number of sorbed on the cation exchanger iron (Fetotaland the amount of iron desorbed (washed) with a cation exchanger. As industrial filter was contaminated with iron compounds to conduct experimental tests, which were not considered quantitatively, the balance iron with the hillshade was possible to spend only on laboratory column. Comparative tests on two ways of washing the cation exchange resin from iron compounds was carried out on two columns with capacity of 0.2 m3·10-3each and with an iron content of 0.3 mg in each column. As follows from figure 3 presents the data, in the cleaning method of the prototype (figure 5) washed 0,147 mg of iron, or 49% of the original iron, according to the method claimed (graph 6) washed 0,228 mg Fetotalor 85% of the initial content on the cation exchanger. Table 3 presents comparative data of how the prototype and the proposed method in terms of washing and obtain a technical result.
The inventive method of washing cationite filters from the products of regeneration and iron compounds increases the economic efficiency of the method and reduces environmental damage by using this method by reducing the specific consumption of wash water (in m3/m3cation exchanger), increasing the working exchange capacity of the cation exchanger by increasing the rate and degree of washing of the cation from the products of regeneration and iron compounds, due to the fact that in the method of washing cationite filters from the products of regeneration and iron compounds washing is carried out with the specific water consumption of not more than 3 m 3/m3the cation exchange resin in two stages, the first of which through the cation exchanger is passed the source water treated by the magnetic field, to a residual hardness in wash water of 0.7 mEq/l, then stop passing water, washing the cation exchange resin is carried out in stagnant minichannel water for 1-2 hours, in the second stage of washing through the cation exchanger miss the original, without magnetic treatment of water, while the magnetic treatment of water is produced by passing the source water at a rate of 0.5-1.5 m/s through a magnetic device, the tubular form is based on permanent magnets with magnetic induction 0,2-0,35 Tesla (2000-3500 Gauss). 1. The method of washing cationite filters from the products of regeneration and iron compounds, including passage through the cation exchanger from top to bottom of the source water with a total hardness of not less than 2.5 mEq/l speeds of 6-8 m/h and the flow of water to a residual hardness in wash water of 0.03 mEq/l, characterized in that the washing is carried out with a specific water consumption of not more than 3 m3/m3the cation exchange resin in two stages, the first of which through the cation exchanger is passed the source water treated by the magnetic field, to a residual hardness in wash water of 0.7 mEq/l, then stop passing water, washing the cation exchange resin is carried out in stagnant minichannel water for 1-2 hours, in the second stage of washing through the cation exchanger will roboscout source, without magnetic treatment of water. 2. The method of washing cationite filters from the products of regeneration and iron compounds according to claim 1, characterized in that the magnetic treatment of water is produced by passing the source water at a rate of 0.5-1.5 m/s through a magnetic device, the tubular form is based on permanent magnets with magnetic induction of 0.2-0.35 T (2000-3500 HS).
|
||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||||