WO2006098660A1 - Method for reducing the corrosive activity of aqueous chlorine-containing solutions and disinfecting agent - Google Patents

Abstract

The invention relates to applied electrochemistry and can be used for technical areas in which disinfecting agents are used for disinfecting and sterilising different objects in the industry and public health. The disinfecting agents are embodied in the form of oxidant aqueous chlorine-containing solutions whose pH is equal to 7.5, total salt content ranges from 0.2 to 2.0 g/l and oxidant content ranges from 80 to 1000 mg/l. The inventive method for producing said agents consists in treating an initial aqueous alkali metal chloride solution in the anode chamber of a diaphragm electrochemical reactor, in introducing a corrosion inhibitor embodied in the form of a low-molecular mono- or a diatomic alcohol or the mixture thereof, wherein a corrosion inhibitor is introducible into the oxidant solution in the quantity of equal to or less than 10 % by volume after the treatment in said anode chamber or prior to the use. The quantity of the introducible ethanol is determined by formula Cal= (18.4x CNaCl)x Cox, wherein Cal is the ethanol concentration, in mmol/l, CNaCl is the concentration of initial sodium chloride solution, in g/l, Cox is the oxidant concentration, in mmol/l. Methods for producing the oxidant aqueous solutions and the inventive disinfecting agent are also disclosed.

Description

 A method of reducing the corrosion activity of aqueous chlorine-containing solutions and a disinfectant

Application area

The invention relates to the field of applied electrochemistry and can be used in those areas of technology in which disinfectants are used to disinfect and sterilize various objects, both manufacturing and in the healthcare sector, including in hospitals, microbiological laboratories, and at sanitary and epidemiological stations, in veterinary institutions, in pharmaceutical enterprises, etc.

State of the art

In medical institutions, for the disinfection treatment and sterilization of various objects, both physical methods are used, for example, thermal sterilization methods, ionizing radiation, and chemical methods intended primarily for low-temperature treatment using liquid chemicals (see, for example, V.I.Vashkov, Means and methods of sterilization used in medicine, M, Medicine, 1973, p. 5-15).

In practice, chemical disinfectants and sterilizing agents containing galloids, including chlorine and its derivatives, in particular sodium hypochlorite, are widely used (see ibid., Pp. 176-182).

The disadvantage of liquid chemical disinfectants used today is the requirement for their concentration restrictions, which is related to their toxicity to medical personnel and patients; in addition, their use does not exclude the development of microbial strains resistant to these agents.

Such disadvantages are deprived of biocidal solutions obtained at the place of consumption by the methods of electrochemical treatment of water-salt solutions of alkali metal chlorides with the possibility of obtaining them with predetermined properties from environmentally friendly starting components: water, salt and electricity.

However, a common drawback of aqueous solutions of disinfectants obtained both chemically and electrochemically is their high corrosivity, which dramatically reduces their scope and the possibility of achieving a high degree of disinfection and sterilization.

The most common way to reduce this drawback is to introduce a corrosion inhibitor into the disinfectant.

So, it is known a powdered disinfectant containing a corrosion inhibitor (see, for example, RF patent Ns 2234218, A61 N 25/12, publ. 08.20.2004). Also known is an antimicrobial agent for disinfecting dental instruments containing hydrogen peroxide, an organic acid and a corrosion inhibitor — zinc salt, complexones and a nonionic surfactant (see, for example, RF patent Ne 2216335, A61 KZ3 / 40, publ. 2003).

The closest in technical essence and the achieved result is a method of reducing the corrosive activity of water-salt chlorine-hydrogen-containing solutions by introducing a corrosion inhibitor based on polyamines and benzyl chloride (see RF patent NQ 2237110, C23 F 11/04, publ. September 27, 2004). This technical solution is selected as a prototype.

A disadvantage of the known solution is that both the inhibitor used in the proposed solution and other known inhibitors cannot be used to reduce the corrosive activity of aqueous oxidant solutions, the method of preparation of which involves treating the initial solution in the anode chamber of a diaphragm electrochemical reactor, since they sharply reduce biocidal activity of solutions. Known use for disinfection, pre-sterilization cleaning and sterilization of electrochemically activated biocidal solutions with optimal pH values, the method of preparation of which includes processing the initial solution of alkali metal chloride, for example, sodium chloride in the anode chamber of a diaphragm electrochemical reactor (see Electrochemical activation: history, state and prospects, under the editorship of prof. V.M. Bakhir, M., printing house VNIIIMT, 1999, pp. 36 - 105). Depending on the conditions and requirements for the disinfection and sterilization of certain objects of medical equipment, the requirements for a biocidal agent are changed, on the basis of which the method for its preparation is modified; however, upon receipt of all types of disinfectants, the final step in obtaining the target product is to process the solution in the anode chamber of the diaphragm electrochemical reactor.

A disinfectant can be obtained by treating the initial aqueous solution of chloride with a single flow through the anode chamber. The initial solution can also be subjected to additional physico-chemical and / or electrochemical treatment using the same or additional electrochemical reactors before processing in the anode chamber.

According to the known solution, disinfectants are non-toxic and can be obtained directly at the place of use using compact and easy-to-use devices. However, the known solution is limited in applications due to the fact that in order to increase the biocidal activity of the products obtained, operating under increased organic load, characterized by the ability to deactivate chlorine-oxygen biocidal agents, it is necessary to increase the concentration of oxidants by increasing the salinity of the initial water-salt solution while increasing the amount of electricity passed through electrochemical reactors. Moreover, an increase in the concentration of oxidants in the solutions used can adversely affect the compatibility of the biocidal agent with the materials of the treated objects. When creating new medical devices and devices, as well as other objects used both in the healthcare system and in other areas of technology, polymer materials are widely used, for example, coatings based on Teflon or other hydrophobic materials, which leads to a limited wetting and penetrating ability of disinfectants based on aqueous solutions and requires special techniques for their use.

Disclosure of invention

The technical result of the application of the present invention is the ability to reduce the corrosive activity of electrochemically activated aqueous solutions used as disinfectants without increasing the concentration of active substances while maintaining their biocidal activity and expanding the functionality of disinfectants by providing the possibility of effective processing of products and surfaces from various including hydrophobic materials of protein and non-protein pro convergence. This result is achieved in that in order to reduce the corrosive activity of aqueous chlorine-containing solutions of oxidants with a pH of 6.5 - 7.5, a total salt content of 0.2 - 2.0 g / l and an oxidant content of 80 - 1000 mg / l, the production method of which includes treatment of the initial aqueous solution of alkali metal chloride in the anode chamber of the diaphragm electrochemical reactor, a corrosion inhibitor is introduced, which is used as a low molecular weight mono- or dihydric alcohol or a mixture of such alcohols, and the corrosion inhibitor is introduced into the oxide solution nt in an amount of up to 10% volume after processing in the anode chamber before use. In the practice of corrosion protection in weakly acidic environments, the use of low molecular weight monohydric alcohols is known (see, for example, RF patents Ne 797265, C23F 11/04, 1999, and Ns 1809992, C23F 11/08, 1999). However, in known solutions, corrosion inhibitors are complex organic compounds, such as the condensation product of higher pyridic acids and synthetic fatty acids (patent Ns 797265) or the products of the interaction of ethoxylated monoalkylphenol with dimethylphosphite or monomethylphosphite or phosphorus trichloride when heated, followed by reaction with ethanolamine. In known solutions, alcohols are introduced to solve another technical problem - to increase the effectiveness of these inhibitors. In the known solutions, the alcohols are not directly inhibitors, and, in addition, in these solutions, the alcohols are introduced in amounts exceeding 20% by weight.

In the proposed solution, the introduction of an additive - a low molecular weight mono- or dihydric alcohol or a mixture of such alcohols - ensures the achievement of a different technical result — a decrease in the corrosion activity of aqueous chlorine-containing solutions of oxidants with a pH of 6.5 - 7.5 and a total salt content of 0.2 - 2.0 g / l and an oxidant content of 80-1000 mg / l, the production method of which includes processing the initial aqueous solution of alkali metal chloride in the anode chamber of a diaphragm electrochemical reactor, for which this problem has not been previously solved.

The introduction of alcohol in an amount of more than 10% vol. Leads to a disproportionate increase in the consumption of reagents and narrowing the area of use of solutions due to a more rapid decrease in the concentration of oxidants in time. The lower limit is determined by the conditions of the problem being solved, and depends on the characteristics of the resulting solution. Optimum is a lower limit of 0.1% by volume. In the case of using a solution of sodium chloride as the source, and as a corrosion inhibitor - ethyl alcohol, the amount of introduced alcohol can be determined by the formula

C _a i = (0.012 χ C _Na cι) χC _O χ, where

C _3I - ethanol concentration, g / l

CN ₃ CI - concentration of the initial solution of sodium chloride, g / l

C _0x is the concentration of oxidants, mg / L.

Aqueous chlorine-containing solutions of oxidants with a pH of 6.5 - 7.5, a total salt content of 0.2 - 2.0 g / l and an oxidant content of 80 - 1000 mg / l, the method of preparation of which involves processing the initial aqueous solution of alkali metal chloride in the anode chamber aperture an electrochemical reactor can be obtained using various processing schemes.

Obtaining aqueous solutions of oxidants, referred to by the authors as "anolyte AN", can be carried out by processing the initial solution in the anode chamber of a diaphragm electrochemical reactor. In this case, the initial solution is prepared by mixing a low-mineralized aqueous solution or drinking water with a highly-mineralized aqueous electrolyte solution, and the treatment is carried out when the pressure in the anode chamber is 0.2-0.4 kgf / cm 2 while maintaining the pH of the solution in the cathode chamber at 12- 14 by circulating a solution in a cathode circulation circuit containing a container with an inlet at the top and an outlet at the bottom, the inlet and outlet of the cathode chamber being connected respectively to the outlet and the inlet of the vessel to form a circulation about the contour. This organization of the process allows you to get anolyte, the main active component of which is hypochlorous acid, which ensures its effective use at neutral and slightly acidic pH values.

An aqueous solution of oxidants, referred to by the authors as "anolyte neutral AHK", can be obtained by treating the initial solution by exceeding the pressure in the anode chamber by 0.2 - 0.4 kgf / cm ² while maintaining the pH of the solution in the cathode chamber at a level of 12-14 by circulation of the solution in the cathode circulation loop containing a flotation reactor with an inlet in the middle and an outlet in the lower parts, while the inlet and outlet of the cathode chamber are connected respectively to the outlet and the inlet of the vessel to form a circulation loop, and after processing in the anode chamber An aqueous solution of oxidants is mixed with a solution taken from the cathode circulation loop in the ratio (1, 1 - 2.0): 1.

This operating mode ensures the economical operation of the reactor due to the presence of catholyte in the cathode chamber with high conductivity due to the increased concentration of sodium hydroxide. In addition, this scheme gives a high degree of conversion of the salt contained in the initial solution, low catholyte consumption, the ability to automate the process of operation and washing, and also a minimum amount of shut-off regulatory devices. The most important advantage achieved with this scheme is its high efficiency when working on highly diluted stock solutions. This is due to the fact that during operation in the cathode chamber a concentrated sodium hydroxide solution is formed, which has a very high electrical conductivity and thereby reduces the electrical resistance of the reactor, which, accordingly, provides energy savings in the synthesis of anolyte AHK. The increased pressure in the anode chamber also creates the best conditions for the isolation and dissolution of the products of the anodic oxidation of the sodium chloride solution with a reduced (due to increased pressure) gas filling of the electrolyte.

Obtaining a solution of oxidants, referred to by the authors "AHK-P", may include preparing the initial solution by mixing a low saline aqueous solution or drinking water with a highly saline aqueous electrolyte solution and processing the resulting stock solution in the anode chamber of the diaphragm electrochemical reactor. Before mixing, a highly mineralized electrolyte solution is treated in the cathode chamber of the same reactor. Processing is carried out in a circulation mode using a circulation circuit with an additional capacity, while maintaining the pH value of the electrolyte in the circulation circuit at a level of 12.5 - 13.5. Part of the highly mineralized electrolyte is taken from the circuit and fed to the mixing. Mixing a low-mineralized solution (or drinking water) with a highly-mineralized solution processed in the cathode chamber is carried out until the concentration of the resulting starting solution reaches 0.2 - 2.0 g / L.

The preparation of the initial solution by mixing a low mineralized aqueous solution or drinking water with a highly mineralized aqueous electrolyte solution allows you to adjust the salt content of the initial solution, which extends the functionality of the invention.

The mixing mixture of a highly saline electrolyte treated in the cathode chamber of the same cell allows reduce energy costs for the process. Processing highly mineralized electrolyte solution in the cathode chamber is carried out in a circulating mode, which ensures maximum use of the electrolyte. The pH of the electrolyte in the circulation circuit is maintained at a level of - 12.5 - 13.5. Lowering the pH below 12.5 does not allow to obtain a disinfectant solution with the desired characteristics. The set pH values are adjusted by changing the concentration of highly mineralized electrolyte solution, as well as by removing part of the treated electrolyte from the circuit for mixing and / or discharge and replenishing the circuit with a fresh solution.

Processing highly mineralized electrolyte in the cathode chamber in the circulation mode can significantly reduce the energy consumption for the process by increasing the conductivity of the electrolyte in the cathode chamber. The salt content of the obtained disinfectant solution is comparable to the salt content of the initial solution and is maintained at the level of 0.3 - 2.0 g / l. With a decrease in salt content, the stability of the disinfecting properties of the solution decreases, with an increase in the corrosivity of the solutions, the need arises for the use of special methods for treating wastewater after using such solutions.

The electrochemical reactor operates in a mode in which the volumetric flow rate of the feed solution through the anode chamber is 100 to 500 times greater than the volumetric flow rate of supplying highly mineralized electrolyte to the cathode chamber.

The fact that the treatment is carried out while maintaining the volumetric flow rate through the anode chamber at a level 100 to 500 times higher than the volumetric flow rate of the highly mineralized electrolyte into the cathode chamber provides optimal conditions for processing the initial solution in the anode chamber. With less than a hundred-fold excess of the flow rate of the initial solution through the anode chamber of the volumetric supply of highly mineralized electrolyte to the cathode chamber, the biocidal and washing properties of the anolyte decrease, with more than five-hundred-fold excess of the flow rate of the initial solution through the anode chamber of the volumetric supply of highly mineralized electrolyte into the cathode chamber sharply increases the sensitivity of the anolyte to external influences, which leads to its deactivation, and also increases the energy consumption for the process. The initial solution is treated in the anode chamber of the reactor until the pH of the anolyte reaches 6.5 - 7.5 and the value of the redox potential is from plus 250 to plus 800 mV relative to the silver chloride reference electrode.

The pH and redox potential are determined based on the conditions of the problem being solved. But in the general case, it should be noted that a decrease in pH below 6.5 and an increase in the redox potential above plus 800 mV increases the corrosivity of the solution. Increasing the pH above 7.5 and reducing the redox potential below plus 250 mV reduces the disinfecting ability of the solution.

At the same time, the pressure difference in the anode and cathode chambers is maintained in the reactor at a level that ensures filling the pores of the diaphragm with anolyte in the range from 70 to 99% of the thickness of the diaphragm.

Anolyte filling from 70 to 99% of the diaphragm thickness helps prevent the deposition of hydroxides in its pores. This effect becomes noticeable when filling 70% of the thickness of the diaphragm and above. The pushing of the anolyte into the cathode chamber leads to a deterioration in the properties of the resulting solutions and an increase in energy consumption.

The required pressure difference can be maintained both by maintaining a pressure in the anode chamber of the reactor exceeding atmospheric pressure in the cathode chamber and by maintaining vacuum in the cathode chamber at a pressure close to atmospheric (evacuation of the cathode circulation loop). While maintaining high pressure in the anode chamber due to the evacuation of the circulation circuit, it is fed by supplying a highly mineralized electrolyte solution to the lower point of the circulation circuit before entering the cathode chamber, and selection processed highly mineralized electrolyte for mixing - from the upper part of the capacity of the circulation circuit. Preparation of the stock solution is carried out in an airtight mixer. The pH values in the circulation circuit are maintained at a predetermined level due to the selection of part of the initial solution in the form of a gas-liquid mixture (see FIG. 3).

With this embodiment of the method, it is possible to reduce the total mineralization of the anolyte AHK-P without deteriorating its biocidal properties with a reduced content of biocidal substances (using the effect of increasing metastability and, therefore, biocidal with decreasing total mineralization). In addition, the discharge of catholyte is reduced (by 5 - 10%) and thus the volume of fluid removed into the drainage is reduced.

While maintaining the pressure in the anode chamber of the reactor exceeding the pressure in its cathode chamber due to the evacuation of the cathode circuit, it can also be replenished by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the cathode circulation circuit. The selection of the processed highly mineralized electrolyte for mixing is carried out from the upper part of the additional capacity of the circulation circuit, and the initial solution is prepared in a separator with the simultaneous separation of electrolysis gases. The pH regulation in the circulation circuit is carried out by withdrawing part of the treated highly mineralized electrolyte solution from the lower part of the additional tank (see Fig. 4). This achieves an additional significant reduction in the discharge of catholyte discharged by 90 - 95% due to the dosed selection (with control of the pH of the anolyte at the outlet) of concentrated catholyte from the circulation tank.

The process can be carried out by creating excess pressure in the anode chamber compared to the cathode circulation loop. Excessive pressure is created, for example, by means of a booster pump installed in front of the entrance to the anode chamber (see Fig. 5). In this case, the circulation circuit is fed by feeding highly mineralized electrolyte solution in the lower part of the additional capacity of the circulation circuit, the selection of the processed highly mineralized electrolyte for mixing is carried out from the upper part of the additional capacity of the circulation circuit, and the initial solution is prepared in an airtight mixer. The pH regulation in the circulation loop is carried out by taking part of the initial solution in the form of a gas-liquid mixture from a sealed flotation reactor installed in front of the entrance to the anode chamber. Due to the fact that the pressure in the anode chamber is increased compared to the cathode, the neutral anolyte AHK - P is removed from the anode chamber through a pressure regulator.

It is advisable to use such an organization of the process in conditions of insufficient pressure of the source water, i.e. in the presence of difficulties in creating a vacuum. Also, when the process is carried out with a pressure in the anode chamber of the reactor greater than the pressure in its cathode chamber due to maintaining excessive pressure in the anode chamber, the circulation circuit is fed by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the circulation circuit, and selection of the processed highly mineralized electrolyte for mixing carried out from the bottom of the additional capacity of the circulation circuit. To prepare the initial solution using a mixer. A pressure pump is installed in front of the mixer (see Fig. 6), with which the pressure in the anode chamber and the mixer is maintained. The ratios of the flows through the chambers are controlled by the dosed selection of catholyte from the cathode circulation circuit. The obtained neutral anolyte AHK-P is withdrawn from the anode chamber through a pressure regulator. Maintaining pH values in the circulation circuit is carried out by draining part of the treated highly mineralized electrolyte solution from the upper part of the additional tank.

It is also possible to carry out the process while maintaining excess pressure in the anode chamber of the reactor and feeding circulation circuit by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the circulation circuit, selecting the processed highly mineralized electrolyte for mixing from the lower part of the additional capacity of the circulation circuit and preparing the initial solution in the mixer, in front of which there is a booster pump that creates excess pressure in the mixer and the anode chamber ( see Fig. 7). The neutral anolyte AHK-P is removed from the anode chamber through a pressure regulator, and the pH values in the circulation circuit are maintained by removing part of the treated highly mineralized electrolyte solution from the lower part of the additional tank with the simultaneous removal of hydrogen from the upper part of the additional tank.

These options allow you to automate the process as much as possible due to the possibility of tying a single system of automatic control of all pumps used in the implementation of the method. The system is configured to maintain the optimal (predetermined) pH value of the anolyte AHK - P.

In all cases, the regulation of the flow ratios through the anode and cathode chambers of the reactor is carried out by controlling the mixing process and the process of maintaining the pH in the circulation circuit. Obtaining a solution of oxidants, called by the authors the neutral anolyte AHK (Fig. 8, 9), may include processing the initial aqueous solution of sodium chloride in the cathode chamber of the main diaphragm electrochemical reactor with subsequent separation of the processed solution stream into two parts, one of which is removed from the treatment cycle in drainage, and the other is fed to the anode chamber of the same reactor for processing, after treatment in the cathode chamber of the main reactor and before separation, the stream is sequentially processed in the cathode and ano hydrochloric chambers diafragmennøgo additional electrochemical reactor.

When processing an additional reactor in the cathode chamber by increasing the pH by 13-17%, the depth of extraction of heavy and alkaline earth metal ions from the initial solution increases, which are separated at the stage of separation of the solution into two streams. The decrease in pH and the synthesis of oxidants occurs in the anode chambers of the additional and the main reactor, and in the anode chamber of the additional reactor, the entire stream of the initial solution received for processing is processed, and part of this stream is processed in the anode chamber of the main reactor. This stepwise treatment allows you to intensify the process of synthesis of oxidants and reduces the amount of solution sent to the drain. The intensification of the synthesis of oxidants is achieved due to the fact that the main reactor (when reactors are running in parallel flows) flows into the electrode chambers that have a lower difference in pH values than by the known method. This effect can be enhanced when the flows in the primary and secondary reactors are countercurrent, which further reduces the difference in pH values and allows both to intensify the process and to reduce the amount of solution sent to the drain.

When carrying out processing in the primary and secondary reactors with a direct-flow solution in the electrode chambers, the concentration of sodium chloride in the initial solution can be 0.2-2.0 g / l, while part of the flow removed from the treatment cycle is 2-5%. When processing in the primary and secondary reactors with countercurrent flow of the solution in the electrode chambers, the concentration of sodium chloride in the initial solution can be 0.2-2.0 g / l, while the part of the stream withdrawn from the treatment cycle is 0.5-3.0 %

With a lower concentration of chloride and a smaller proportion of the excreted portion of the solution, the necessary degree of disinfecting ability of the solutions is not provided, and at high values, the concentration of active chlorine in the solution increases, which leads to an increase in corrosion activity and narrows the scope.

AHK neutral anolyte can be obtained according to the schemes shown in FIG. 10-16. In this case, the initial solution is treated in the cathode chamber of the diaphragm electrochemical reactor, followed by the removal of part of the solution processed in the cathode chamber and the main flow of the solution in the anode chamber of the diaphragm electrochemical reactor, the treatment being carried out using an electrochemical reactor block containing 2, 3 or 4 a reactor with a single parallel flow of a solution through the cathode chambers of all reactors; The part of the solution processed in the cathode chambers is removed by treatment in a sealed flotation reactor with the discharge of sludge and the main stream is sequentially processed in the anode chambers of the reactors, and the flow rate of the treated solution through the anode chambers of the reactors is 2 to 4 times higher than the speed of its flow through the cathode chambers. Processing the initial solution with a single flow through the cathode chambers and a sequential flow through more than one anode chamber of the diaphragm electrochemical reactor allows the process to be carried out in such a way as to avoid destruction of the biocidal substances formed due to electromigration through the diaphragm between the electrode chambers.

Processing in a flotation reactor makes it possible to control the flow replenishment by removing part of the hydrogen, to remove part of the treated solution in the form of a gas-liquid mixture, and also to regulate the composition of the solution by removing insoluble impurities that are formed during processing in the cathode chamber.

After processing in the cathode chamber of the main reactor, the solution is sequentially processed in at least two anode chambers (depending on the design of the method).

The flow rate of the treated solution in the anode chamber, exceeding the flow rate of the treated solution in the cathode chamber by 2 to 4 times, can reduce the energy consumption for processing, especially when processing low saline solutions, since at a low flow rate through the cathode chamber, hydroxyl ions accumulate in the latter with significant mobility and providing high conductivity of the solution. An increase in the flow rate in the anode chambers makes it possible to increase the yield of oxidants, since intensive mixing creates the conditions for the formation of smaller electrolysis gas bubbles and helps to intensify the process of their dissolution in the treated solution, and, as a result, the intensification of redox reactions in the solution. As the initial solution of alkali metal chloride, a solution of sodium chloride with a concentration of 0.2 - 2.0 g / L is used. When using a more concentrated solution, the salt content of the resulting disinfectant solution increases, which limits the scope of application of the latter. In addition, the corrosive activity of disinfecting solutions increases sharply, and there is a need to use special methods for cleaning waste solutions after use. When using less concentrated solutions, the required degree of oxidant concentration is not achieved. Using the initial solution with a concentration of 0.2-2.0 g / l allows you to get a disinfectant solution with optimal salinity (on average 1, 5 - 2.0 g / l or less, which is significantly lower than in the installation of the prototype - 0, 3 - 5.0 g / l) and expand the scope of solutions. This salt content of the disinfecting solution allows you to expand the scope of its application, to avoid the possible salting of the resulting wastewater while ensuring the necessary degree of disinfectant properties of the solution.

In the process, stock solutions of a different, higher concentration can also be used, however, the salt content of the resulting disinfectant solution is maintained at a constant level.

So, for example, an initial solution of sodium chloride with a concentration of 50-100 g / l can be used, and before processing in the cathode chamber, the initial solution is mixed with fresh water to a concentration of 0.2-2.0 g / l. Or, an initial solution with a concentration of 50 - 250 g / l can be used, and after treatment in the cathode chamber, the treated solution is mixed with fresh water to a concentration of 0.2 - 2.0 g / l.

The same initial solution with a concentration of 50 - 250 g / l is treated in a cathode chamber, a flotation reactor and an anode chamber, and before treatment in each of the additional anode chambers, the treated solution is mixed with fresh water until a concentration of 0.2 is reached at the outlet from the last additional anode chamber - 2.0 g / l. Upon receipt of the disinfectant solution, treatment is carried out when the pressure in the anode chambers of the reactor or reactors is higher than in the cathode.

Processing when the pressure in the anode chamber is higher than that of the cathode (in this case, the disinfectant solution - neutral anolyte AHK is removed from the anode chamber of the electrochemical reactor or reactors through a pressure regulator) or when the pressure in the cathode chamber is higher than the anode allows directing the process electromigration of ions through the diaphragm and, therefore, change the properties of the resulting neutral anolyte.

On average, it is advisable to maintain the pressure difference in the electrode chambers at the level of 0.1-0.4 kgf / cm ² .

Before being fed into the anode chamber, the treated solution can be passed through a catalyst bed, for example, aluminosilicate, zirconium oxide, niobium oxide. This treatment allows you to extract the smallest particles of heavy metal hydroxides from the solution, which shorten the life of oxidants in the AHK anolyte. A reactor with a similar loading from granules of a mineral catalyst is called electrokinetic, since its operation is based on the use of electrokinetic phenomena, i.e. the whole complex of processes (electroosmosis, electrophoresis, electrostatic filtration), which takes place in a double electric layer at the “solid - liquid” interface.

Obtaining a solution of oxidants, called the authors of the ANDA, may include the following stages. Preparation of the initial solution by mixing drinking water or a low-mineralized aqueous solution with a highly mineralized aqueous electrolyte solution and processing the obtained initial solution in the anode chamber of the main diaphragm electrochemical reactor at a specific electricity consumption of 400-4000 C / l. After processing in the anode chamber of the main reactor, the solution is fed into the anode chamber of the additional electrochemical reactor, while processing in the anode chamber of the additional reactor is carried out until a pH of 6.5 - 7.5 is reached and 5

17 oxidation-reduction potential plus 700 - plus 1100 mV relative to the silver chloride reference electrode.

The cathode chambers of the primary and secondary electrochemical reactors are connected by circulation circuits to a vessel with a highly mineralized aqueous electrolyte solution. The initial solution is prepared by mixing drinking water or a low saline solution with a highly mineralized electrolyte solution taken from the circulation circuit, and the pH of the auxiliary electrolyte circulating in the cathode chamber is maintained at least 10 or by removing part of the initial solution before feeding it into the anode chamber of the main reactor , or by withdrawing part of the highly mineralized electrolyte solution from the tank, and processing in an additional electrochemical reactor is carried out when exceeding d in the anode chamber phenomenon compared with the cathode by 0.1 - 0 4 kgf / cm ² (Fig 17, 18.). As a highly mineralized electrolyte solution, a sodium chloride solution with a total salinity of 50 to 300 g / l is used.

The preparation of the initial solution by mixing a low mineralized aqueous solution or drinking water with a highly mineralized aqueous electrolyte solution allows you to adjust the salt content of the initial solution, which extends the functionality of the invention.

The mixing of a highly mineralized electrolyte solution from the circulation circuit, in which it is processed in the cathode chambers of the primary and secondary reactors, reduces energy costs for the process. The treatment of a highly mineralized electrolyte solution in the cathode chambers is carried out in a circulating mode, which ensures maximum use of the electrolyte. The pH of the electrolyte in the circulation circuit is maintained at a level of at least 10. Lowering the pH to less than 10 does not allow to obtain a disinfectant solution with the desired characteristics. The set pH values are adjusted by changing the concentration of highly mineralized electrolyte solution, as well as due to the removal of part of the treated electrolyte from the circuit to mix and / or discharge and recharge the circuit with a fresh solution.

Processing the resulting stock solution in the anode chamber of the main diaphragm electrochemical reactor with a specific electricity consumption of 400 - 4000 C / l allows the process to be carried out in such a way as to avoid destruction of the formed biocidal substances due to electromigration between the electrode chambers. When the amount of electricity is less than 400 C / l, the amount of reagents formed is not enough, and when the amount of electricity exceeds 4,000 C / l, the phenomena of electric transport become noticeable. In addition, when the solution is processed in the specified range of the specific amount of electricity, the solution is formed in the electrode chambers and the solution is saturated with hydrogen and oxygen, which are both in the dissolved and in the gaseous state. These gases take part in the subsequent electrochemical transformation of the solution and the synthesis of its biocidal components. With a small specific amount of electricity consumed during the processing of the solution in the main reactor (less than 400 C / l), the concentration of dissolved gases is low and, accordingly, biocidal substances with their participation are not formed in the additional reactor to significantly increase the biocidality of the anolyte solution of AND. With a specific amount of electricity of more than 4000 C / l, the gas filling of the solution increases, which leads to increased energy consumption.

After processing in the anode chamber of the main reactor, the solution is fed into the anode chamber of the additional electrochemical reactor, and processing in the anode chamber of the additional reactor is carried out until the pH value is 6.5 - 7.5 and the redox potential is plus 700 - plus 1100 mV relative to the silver chloride reference electrode .

The pH and redox potential are determined based on the conditions of the problem being solved. But, in the general case, it should be noted that a decrease in pH below 6.5 and an increase in the redox potential above plus 1100 mV increases the corrosivity of the solution and requires the observance of safety measures when working with a solution. Increasing the pH above 7.8 and lowering the redox potential below plus 700 mV reduces the disinfecting ability of the solution.

The salt content of the obtained disinfecting solution is comparable to the salt content of the initial solution and is maintained at a level of 0.2 - 2.0 g / l. With a decrease in salt content, the stability of the disinfecting properties of the solution decreases, with an increase in the corrosivity of the solutions, the need arises for the use of special methods for treating wastewater after using such solutions.

The cathode chambers of the primary and secondary electrochemical reactors are connected to the vessel, forming circulating circuits of a highly mineralized electrolyte. The pH value of the highly mineralized electrolyte circulating in the cathode chambers is maintained at a level of at least 10.

Processing highly mineralized electrolyte in a circulating mode provides the opportunity to reduce the discharge of electrolyte into the drainage and stabilize the operation of the primary and secondary reactors by maintaining the constant characteristics of the auxiliary electrolyte. During processing, before the treated solution is fed into the anode chamber of the main electrochemical reactor, a part of the solution that does not contain gas bubbles can be removed from the solution. In this case, the regulation of the pH of the finished solution occurs by changing the flow rate of the removed solution. It is advisable to use such a scheme to simplify the regulation of the parameters of the finished anolyte, however, this is associated with a loss of approximately 2 - 5% of the total consumption of the initial solution. Adjustment of the parameters of the finished solution of ANDA can be carried out by taking part of the catholyte from the circulation circuit. At the same time, the catholyte discharge into the drain is 0.01 - 0.02% of the total flow rate of the initial solution, however, such a control system requires the use of metering pumps of high accuracy with the ability to automatically control their operation by feedback from the sensors of the anolyte parameters AND at the device output . Processing in an additional electrochemical reactor is carried out when the pressure in the anode chamber is 0.1-0.4 kgf / cm ² higher than the cathode one (and the neutral anolyte AED is withdrawn from the anode chamber of the additional electrochemical reactor through a pressure regulator). Carrying out the process at this pressure makes it possible to negate the negative effects of ion electromigration in an additional reactor and to purposefully change the properties of the resulting neutral anolyte. At a pressure of less than 0.1 kgf / cm ² , the migration of ions from the cathode chamber to the anode cannot be suppressed, and excess pressure above 0.4 kgf / cm ² does not lead to a new result, but increases the cost of the process.

Obtaining a solution of oxidants - a neutral anolyte AND can be carried out in another way.

In this case, in the method for producing a disinfecting solution — an AND neutral anolyte, comprising preparing a stock solution by mixing a low saline aqueous solution or drinking water with a highly saline aqueous electrolyte solution and treating the resulting stock solution sequentially in the cathode and anode chambers of the main diaphragm electrochemical reactor, treating the stock solution mainly the reactor is conducted at a specific electricity consumption of 400 - 4000 C / l and after processing the solution is supplied the anode chamber of the additional electrochemical reactor, and the processing in the anode chamber of the additional reactor are carried out until the pH value is 6.5 - 7.5 and the redox potential is plus 700 - plus 1100 mV relative to the silver chloride reference electrode, and the cathode chamber of the additional electrochemical reactor is equipped with a circulation loop auxiliary electrolyte with a capacity, moreover, the pH of the auxiliary electrolyte circulating in the cathode chamber is maintained at a level of not less than 10, and processing in addition Yelnia electrochemical reactor is carried out at the pressure in the anode chamber as compared with the cathode at 0.1 - 0.4 kgf / cm ² (Fig.19).

Preparation of a stock solution by mixing a low saline aqueous solution or drinking water with highly mineralized aqueous electrolyte solution allows you to adjust the salt content of the initial solution, which extends the functionality of the invention.

Processing the resulting stock solution sequentially in the cathode and anode chambers of the main diaphragm electrochemical reactor with a specific electricity consumption of 400-4000 C / l allows the process to be carried out in such a way as to avoid destruction of the formed biocidal substances due to electromigration between the electrode chambers. When the amount of electricity is less than 400 kL / l, the amount of reagents formed is not enough, and when the amount of electricity exceeds 4,000 kL / l, the phenomena of electric transport become noticeable. In addition, when the solution is processed in the specified range of the specific amount of electricity, the solution is formed in the electrode chambers and the solution is saturated with hydrogen and oxygen, which are both in the dissolved and in the gaseous state. These gases take part in the subsequent electrochemical transformation of the solution and the synthesis of its biocidal components. With a small specific amount of electricity consumed during the processing of the solution in the main reactor (less than 400 C / l), the concentration of dissolved gases is low and, accordingly, biocidal substances with their participation are not formed in the additional reactor to significantly increase the biocidality of the anolyte solution of AND. With a specific amount of electricity of more than 4000 C / l, the gas filling of the solution increases, which leads to increased energy consumption. After processing in the anode chamber of the main reactor, the solution is fed into the anode chamber of the additional electrochemical reactor, and processing in the anode chamber of the additional reactor is carried out until the pH value is 6.5 - 7.5 and the redox potential is plus 700 - plus 1100 mV relative to the silver chloride reference electrode ,

The salt content of the obtained disinfecting solution is comparable to the salt content of the initial solution and is maintained at a level of 0.2 - 2.0 g / l. With a decrease in salinity decreases stability of the disinfecting properties of the solution, with an increase - the corrosivity of the solutions sharply increases, and there is a need to use special methods of wastewater treatment after using such solutions. The solution is treated in the anode chamber of the additional reactor until the anolyte pH is 6.5 - 7.5 and the redox potential is from plus 700 to plus 1100 mV relative to the silver chloride reference electrode.

The pH and redox potential are determined based on the conditions of the problem being solved. But in the general case, it should be noted that a decrease in pH below 6.5 and an increase in the redox potential above plus 1100 mV increases the corrosivity of the solution and requires the observance of increased safety measures when working with the solution. Increasing the pH above 7.5 and reducing the redox potential below plus 700 mV reduces the disinfecting ability of the solution.

The cathode chamber of the additional electrochemical reactor is equipped with a secondary auxiliary electrolyte circulation circuit with a capacity, the pH of the auxiliary electrolyte circulating in the cathode chamber being maintained at a level of at least 10.

Processing the auxiliary electrolyte in the cathode chamber in a circulating mode provides the opportunity to reduce the discharge of electrolyte into the drainage and stabilize the operation of the additional reactor by maintaining the constant characteristics of the auxiliary electrolyte. The pH value of the electrolyte in the circulation circuit is maintained at a level of at least 10. Lowering the pH below 10 does not allow to obtain a disinfectant solution with the desired characteristics. The set pH values are adjusted by changing the concentration of the electrolyte solution by removing part of the treated electrolyte from the circuit to discharge and replenishing the circuit with fresh electrolyte.

As an auxiliary electrolyte in the circulation circuit of the cathode chamber of the additional reactor can be used the initial solution (Fig. 19), which allows the process to be carried out at a lower energy consumption, but with a small consumption of the initial chloride solution.

As an auxiliary electrolyte, drinking water can also be used, which is a low-mineralized solution of electrolytes (Figs. 20 and 21). In this case, during processing, at least a part of the gaseous and dissolved hydrogen is removed from the solution before the treated solution is fed into the anode chamber of the main electrochemical reactor or before the treated solution is fed into the anode chamber of the additional electrochemical reactor, and the neutral anolyte Ande is removed from the anode chamber of the additional electrochemical reactor through the pressure regulator. It is advisable to use such a scheme to save salt solution, but at the same time, the energy consumed increases somewhat. Processing in an additional electrochemical reactor is carried out when the pressure in the anode chamber is 0.1 - 0, 4 kgf / cm ² higher than the cathode one (and the neutral anolyte AED is withdrawn from the anode chamber of the additional electrochemical reactor through a pressure regulator). Carrying out the process at this pressure makes it possible to negate the negative effects of ion electromigration in an additional reactor and to purposefully change the properties of the resulting neutral anolyte. At a pressure of less than 0.1 kgf / cm ^{2, the} migration of ions from the cathode chamber to the anode cannot be suppressed, and an excess of pressure above 0.4 kgf / cm ² does not lead to a new result, but increases the cost of the process.

When preparing the initial solution according to all the above schemes, a sodium chloride solution with a total salinity of 50-300 g / l is used as a highly mineralized electrolyte solution.

Such a solution is not scarce and does not require special safety measures. The total mineralization of the solution is 50 - 300 g / l. With a decrease in concentration below 50 g / l, energy costs and volumes of processed solutions increase. Concentration increase above 300 g / l does not gives a new result, but requires special conditions for the preparation of such solutions, which unreasonably increases the cost of the process.

It is also advisable to use an ultrafiltration or nanofiltration diaphragm made of ceramics in the cells of electrochemical reactors when obtaining solutions of oxidants according to all the above schemes. Ceramic diaphragms do not change their characteristics during differential pressure and during processing, which ensures the stability of processing parameters.

The composition of ceramics is selected based on the conditions of the problem being solved; it is preferable to use ceramics based on zirconium oxide or ceramics based on zirconium oxide with the addition of aluminas and yttrium, which have an optimal combination of characteristics.

It is advisable to use flow-through electrochemical reactors described in RF patent Ne 2078737 or in US patent Ns 5, 635, 040. These reactors are compact diaphragm electrolyzers made of vertical cylindrical and rod electrodes, coaxially mounted in dielectric bushings, ceramic diaphragms, also coaxially installed in the bushings between the electrodes and dividing the interelectrode space into the electrode chambers, the chambers having an entrance to the bottom and an exit at the top of the cell. The electrolyzers are made on a modular basis, which allows the method to be achieved with a given performance and, in addition, they provide the ability to disconnect part of the reactor cells without stopping its operation, as well as connecting new cells to the reactor during its operation to increase its productivity.

According to the schemes presented above, aqueous solutions of oxidants can be obtained with a wide range of characteristics (with pH = 6.0 - 7.8 and an oxidant content in the range of 80 - 1000 mg / l). To obtain them, initial solutions with a concentration of 0.2 - 5.0 g / l can be used. However, for the purposes of the present invention, it is advisable to use aqueous solutions of oxidants obtained according to the above schemes, which impart certain characteristics - pH 6.5 - 7.5 and an oxidant content of 80 - 1000 mg / l with a total salt content of 0.2 - 2.0 g / l, since it is these parameters that make it possible to most widely use such solutions as disinfectants. However, they have a significant drawback - relatively high corrosion properties.

The introduction of additives, low molecular weight monohydroxy or dihydric alcohol, or a mixture of such alcohols, allows to obtain a disinfectant with reduced corrosion activity while maintaining and increasing biocidal activity in relation to all types of processed objects, including hydrophobic. It has been established that the biocidal activity of disinfectants with an alcohol supplement obtained according to the proposed solution increases with the treatment of surfaces infected with B. subtilus spores, which are highly resistant to all types of biocidal agents. The use of such disinfectants can expand the range of their application, including the treatment of hydrophobic objects contaminated with especially resistant microorganisms, and / or reduce the consumption of a disinfectant, and / or the concentration of oxidants, and / or processing time.

When an additive is added in an amount of less than 0.1% by volume, there is no noticeable decrease in anticorrosive activity while maintaining the concentration of oxidants, and when an additive is added more than 10% by volume, the reagent consumption disproportionately increases due to a significant decrease in the concentration of oxidants.

The introduction of the additive is preferably carried out after processing the solution in the anode chamber immediately before use.

In the practice of medical institutions, it is known to use a solution of low molecular weight alcohol, in particular ethyl alcohol, as an antiseptic or disinfectant (see, for example, the Practical Guide for the Use of Disinfectants and Sterilization in Healthcare Facilities, n / a A. V. Avchinnikova, Smolensk, SGMA, 2002). However, well-known recommendations suggest the use of alcohol solutions with a concentration of 70 - 80% with a treatment time of 1 minute - treatment of the skin of the injection field - up to 30 minutes - disinfection of certain species, tools, such as root needles, etc. Alcohol solutions with a concentration of up to 5% by volume are not used either for disinfection or for antiseptic treatment, because such low concentrations of alcohols do not have a pronounced biocidal activity, do not cause protein denaturation, which is the main mechanism of their antimicrobial effect.

The introduction of a monohydric organic alcohol in an amount of 0.1-10.0% in May is known. in a disinfectant based on carbamide didecylmethylammonium bromide clathrate (see RF patent Ns 2187337, A 61 L 2/18, 2002) or monohydroxy alcohol in an amount of 0.5 - 10.0% in May. in a disinfectant based on alkyldimethylbenzylammonium chloride (see RF patent Ns 2190426, A 61L2 / 16, 2002)

However, the known solutions are a kind of concentrates that are not used in their pure form, but for solving tasks - namely, for disinfection - they are used in the form of diluted working solutions by diluting the product with drinking water. So, according to patent 2187337 use working solutions containing 0.2 - 5.0% of a patented agent, and according to patent 2190426 - solutions containing 0.012 - 3.0% of a patented agent. Therefore, when using known solutions for disinfection, solutions are used containing other amounts of monohydric alcohol than in the proposed solution.

The disinfectant according to the invention is a ready-to-use disinfectant solution that does not require additional dilution operations and is used for disinfection purposes precisely when the content of the additive, low molecular weight alcohol, is within the limits indicated in the formula.

At the same time, a new positive result is achieved, which cannot be achieved in known solutions, namely, a decrease in corrosion activity in the pH range of the use of a disinfectant. In addition, the tool can be obtained directly at the place of use, and in those quantities that are necessary for each specific case, while simplifying the process of applying the tool, since there is no operation of dilution of the concentrate. Compared with known means, the proposed solution has a higher activity - according to known solutions, the exposure time is 1-3 hours, while according to the proposed solution, the exposure time is no more than 30 minutes.

As an additive of low molecular weight alcohol, it is preferable to use ethyl or isopropyl alcohol or a mixture thereof. These reagents are affordable, relatively cheap, approved in medical practice and are almost always available in medical institutions.

As the initial water-salt solution, a solution of sodium chloride with a concentration of 0.2-2.0 g / l is mainly used. However, the concentration of the initial solution of sodium chloride and the concentration of chlorine-acid oxidizing agents can vary depending on the type of object being treated, the level of danger and resistance of the disinfected microorganism, and the method of using the disinfectant. For example, during the decontamination of objects infected with especially dangerous infections, the concentration of sodium chloride is 2 g / l, the concentration of oxidants is up to 1000 mg / l to ensure speed with minimal consumption of a disinfecting agent, including in the form of an aerosol. At the same time, when processing irrigation systems of medical devices, electrochemically synthesized solutions with an initial concentration of sodium chloride of less than 1 g / l and an oxidizing agent concentration of 80 mg / l are effective.

Brief Description of the Drawings

In FIG. 1 shows a diagram for the preparation of an aqueous solution of oxidants - a disinfectant - with reduced corrosion properties. In FIG. 2 to 21 show the schemes for preparing aqueous solutions of oxidants, which make it possible to obtain disinfectants according to the invention. A device for producing an aqueous solution of oxidants (Fig. 1) contains an electrochemical diaphragm reactor made according to the modular principle of electrochemical cells. In all figures, the reactor is depicted in the form of one electrochemical cell 1, the interelectrode space of which is divided by the diaphragm into anode 2 and cathode 3 of the chamber. The output of the anode chamber 2 is connected to the line 4 of the drain of an aqueous solution of oxidants. On line 4, a mixer 5 can be installed (Fig. 1) for introducing an additive, an alcohol or a mixture of alcohols, into an aqueous solution of oxidizing agents. Also on line 4, a pressure regulator can be installed up to 6 (Fig.2, 5-7.17 - 21).

The installation contains a feed line for the initial solution 7, which can be connected to the input of the anode chamber 2 (Fig. 1), or with other nodes of the installation. The initial solution can be prepared by mixing a low-saline solution (drinking water), which is supplied via line 8, with a highly-mineralized solution, for example, a concentrated solution of sodium chloride, which is supplied to the plants from the tank 9 to the mixer 10, which is connected to lines 7 and 8.

The installation may include a flotation reactor 11 with an entrance at the top and an exit at the bottom, a capacity of the cathode circulation loop 12, also with an entrance at the top and an exit at the bottom, an output line of catholyte 13 and a mixture of gaseous products of the cathode circuit 14, or an output line of a gas-liquid mixture from the cathode loop 15, and these lines can be connected both to the flotation reactor 11 and to the capacity of the cathode circulation loop 12. The installation may include an electrokinetic reactor 16, with an entrance to the top and exit to parts, additional electrochemical diaphragm reactors 17 - 35, adjustable hydraulic resistance 36, additional pressure regulator 37, filter for removing mechanical impurities 38, mixers 39 - 44, made, for example, in the form of water-jet pumps, as well as overflow lines and control valves 45 - 62.

The invention using installations for obtaining an aqueous solution of oxidants is as follows. The source water, for example, drinking water from the tap along line 8 (Fig. 1), is mixed in a mixer 10 (made, for example, as a water-jet pump) with a concentrated (more than 100 g / l) sodium chloride solution, the supply of which from the tank 9 through line 7 enters the anode 2 chamber of the electrochemical reactor 1, the pressure in which during operation should be higher than the pressure in the cathode chamber 3 by 0.2 - 0.4 kgf / cm ^{2 "} . The cathode chamber 3 of the reactor 1 is connected to the circulation tank 12, forming a closed circulation circuit of the auxiliary electrolyte. The main source of replenishment of the catholyte circulation loop is the anode chamber 2 of reactor 1, from which sodium ions penetrate through the diaphragm into the cathode chamber 3. The excess catholyte is removed from the tank 12 at the drain outlet 15. Hydraulic resistance 36 to the feed line with the lower part of the cathode circulation circuit is designed to fill the circulation tank 12 at the time of starting the electrochemical system and the drip feed of the initial solution into the circuit lation circuit during operation. At the outlet of the anode chamber of the reactor, the obtained aqueous solution of oxidants, anolyte AN, is withdrawn via line 4. On line 4, a mixer 5 is installed, in which an additive - alcohol - is mixed with an aqueous solution of oxidants, and the resulting disinfectant is sent to the consumer.

An aqueous solution of oxidizing agents called AHK anolyte and a disinfectant based on it can be obtained according to the scheme depicted in FIG. 2. Water, for example, tap water, is supplied through line 8 to the installation.

Having passed the filter 38 and the pressure regulator 37, the water enters the mixer 10, in which it is mixed with a saturated solution of sodium chloride from the tank 9. Next, the resulting stock solution is supplied via line 7 to the anode chamber 2 of reactor 1. The cathode chamber 3 of reactor 1 is connected to the flotation reactor 11 with the formation of a circulation circuit. Hydrogen is discharged through line 14 from the flotation reactor, and excess catholyte is discharged through line 13 to the drainage. Part of the catholyte from the flotation reactor 11 through the flow line enters the mixer 39. The main The principle of obtaining an AHK anolyte in this setup is the anodic treatment of a dilute sodium chloride solution under pressure, which ensures the migration of sodium ions and water molecules from the anode chamber to the cathode and metered electrodiffusion selection of hydroxyl ions from the cathode chamber, followed by the introduction of part of the volume of catholyte saturated with dissolved hydrogen into the freshly prepared anolyte . This operating mode ensures the economical operation of the reactor, which is achieved by the presence in the cathode chamber 3 of catholyte with high conductivity due to the increased concentration of sodium hydroxide. Through line 4, the resulting aqueous solution of oxidants - anolyte AHK - enters mixer 5, in which it is mixed with an additive - alcohol, and the resulting disinfectant is supplied to the consumer.

An aqueous solution of oxidants, referred to by the authors as the neutral anolyte AHK-R _1, can be obtained using plants whose circuits are depicted in FIG. 3-7.

The highly mineralized solution from the reservoir 9 (FIG. 3) is supplied through the control valve to the cathode chamber 3 of the reactor 1 and fills the circulation circuit and tank 12. The low-mineralized solution or drinking water from the source (not shown in the diagram) along line 8 through the water-jet pump 40 and flotation the reactor 11 enters the anode chamber 2. After filling the anode and cathode loops, a voltage is applied to the electrodes of the reactor 1 and processing of the solution in the circulation loop begins. A low-mineralized solution is pumped through the anode chamber 2, which is then temporarily discharged into the drainage through line 4. After the solution has reached the required characteristics in the circulation circuit, the treated solution is fed through a vacuum line through the pump 40 to the flotation reactor 11, where the mixing of the low-mineralized solution with the highly mineralized, completed in the circulation circuit of the cathode chamber. From the flotation reactor 11, by means of an adjustable valve, hydrogen gas is removed from the mixture, as well as part of the initial solution is removed in the form of a gas-liquid mixture along line 15. The solution processed in the anode chamber is sent through line 4 to the tank (not shown in the diagram) or directly to the consumer. During operation, the circulation circuit is replenished with fresh highly mineralized solution, and a vacuum is maintained in the circuit itself, which ensures that the anolyte fills from 70 to 99% of the thickness of the diaphragm. Hydrogen separation can be carried out in the separator 45, while part of the treated highly mineralized solution is removed from the tank 12 by means of an adjustable pump 46 from the circulation circuit along line 47 to the drain (Fig. 4).

When maintaining an overpressure in the anode chamber that exceeds the pressure in the cathode chamber, the initial solution is obtained in mixer 48, and a pressure regulator “set up” 6 is installed on line 4 (Fig. 5-7).

The pressure drop across the diaphragm is maintained at a level of 0.4 - 0.6 atm. The preparation of an aqueous solution of oxidants, referred to by the authors as neutral anolyte AHK, can be carried out using an additional electrochemical diaphragm reactor, as shown in FIG. 8 and 9.

The initial solution of the desired concentration through line 7 enters the input of the cathode chamber 3 of the reactor 1 (see Fig. 8). After a single passage through the cathode chamber 3 (Fig. 8), the solution is alkalinized to pH 9.5-9.8, which leads to the release of 78-80% dissolved metals in the form of insoluble hydroxides. The solution processed in the cathode chamber 3 of the reactor 1 together with electrolysis gases and insoluble impurities enters through the overflow line 49 to the input of the cathode chamber of the additional reactor 17. After processing in the cathode chamber of the additional reactor 17; the pH of the solution rises to 10.9 - 11, 0, which allows you to allocate another 13-15% of soluble metals. Further, along line 50, the stream enters the anode chamber of the reactor 17 for processing, in which the pH values are partially neutralized, by an amount that does not lead to the reverse dissolution of metal impurities released into the insoluble form. From the anode chamber of the reactor 17 through line 52, the treated solution enters the flotation reactor 11, in which the suspended particles of metal hydroxide are separated and electrolysis gases. The reactor 11 can be made, for example, in the form of a sealed cylindrical flotation reactor with a tangential inlet, moreover, from the upper part of the reactor fleet sludge with part of the solution flow is removed and sent through line 15 to the drainage. A clarified stream is discharged from the bottom of the flotation reactor via line 53. Thus, in the reactor 11, the flow of the medium to be treated is divided into two parts, one of which, in an amount of 2-5%, is withdrawn from the treatment cycle, and the other is fed through line 53 to the input of the anode chamber 2 of reactor 1. When processing in the anode chamber 2 pH values are reduced to neutral (about 7), and the resulting solution through line 4 is supplied to the consumer.

Depending on the conditions of the problem being solved, both a straight-through duct of the medium to be treated in the electrode chambers (Fig. 8) and countercurrent (Fig. 9) can be used. The switching of hydraulic circuits is carried out by a special connection of the electrode chambers of reactors 1 and 17 with hydraulic lines 49.50 and 53.

So, for example, with the vertical execution of electrochemical cells connected to the reactor, the entrance to both the anode and cathode chambers is located at the bottom of the reactors, and the exit from the anode and cathode chambers is at the top. The connection diagram of such reactors according to the forward flow principle is shown in FIG. 8.

If the arrangement of the input and output of the electrode chambers of the reactors is different, then the circuit of their connection according to the counterflow principle is shown in FIG. 9. In counterflow mode, the device operates as follows. The initial solution of the desired concentration through line 7 enters the inlet of the cathode chamber 3 of the reactor i (see Fig. 9). After a single passage through the cathode chamber 3, the solution is alkalinized to pH values of more than 10, which leads to the release of 80 - 82% dissolved heavy and alkaline earth metal ions in the form of insoluble hydroxides. Treated in the cathode chamber 3 of the reactor 1, the solution, along with electrolysis gases and insoluble impurities, enters the inlet of the cathode chamber of the reactor 17 through the overflow line 49. After processing in the cathode chamber of the reactor 17, the pH of the solution rises to values more than 11.0, which allows us to allocate another 15 - 17% of soluble metals. Then, along line 50, the stream enters the anode chamber of the reactor 17 for processing, in which the pH values are partially neutralized by a value that does not lead to the reverse dissolution of metal impurities released into the insoluble form. From the anode chamber of the reactor 17 through line 53, the treated solution enters the flotation reactor 11, in which the suspended particles of metal hydroxide and electrolysis gases are separated. The sludge with a part of the solution flow is removed from the upper part of the reactor 11 and is sent to the drainage line 15. A clarified stream is discharged from the bottom of the flotation reactor 11. Thus, in the flotation reactor 11, the flow of the medium to be treated is divided into two parts, one of which is removed from the treatment cycle in an amount of 0.5-3.0%, and the other is fed through line 53 to the input of the anode chamber 2 of reactor 1. During processing in the anode chamber 2, the pH values are reduced to neutral (about 7), and the resulting solution through line 4 is supplied to the consumer.

Upon receipt of an aqueous solution of oxidants - the neutral anolyte AHK - schemes using a block of electrochemical reactors containing 2, 3 or 4 reactors with a single parallel flow of the solution through the cathode chambers of all reactors can be used (see Fig. 10-16).

The apparatus for producing an oxidant solution (Fig. 10) contains a reactor block, which includes two flow diaphragm electrochemical reactors (the drawings show the execution of each of the reactors from one flow electrochemical module element - hereinafter TEM elements) 1 and 18, in which the interelectrode space is divided by diaphragms into cathode and anode chambers, a flotation reactor 11 and a control valve 54 for dosing the flush sludge from the top of the flotation reactor 11. The installation can also keep the electrokinetic reactor 16.

The cathode chambers of the FEM elements 1 and 18 are connected hydraulically in parallel, and the anode chambers are connected in series. The feed line 7 of the initial aqueous solution is connected to the entrance to the cathode chambers reactors 1 and 18, and the conclusions of the cathode chambers are connected to the flotation reactor 11 and the electrokinetic reactor 16. The output of the electrokinetic reactor is connected to the input to the anode chamber of the reactor 18, and the output of the anode chamber of the reactor 18 is connected to the input to the anode chamber of the reactor 1. Output of the anode chamber of the reactor 1 is connected to the drain line of the oxidant solution 4.

In FIG. 11 is a diagram of an installation containing one unit, consisting of three diaphragm electrochemical reactors 1, 19, and 20. The cathode chambers of the reactors 1, 19, and 20 are connected hydraulically in parallel, and the anode chambers are connected in series.

On Fig. Presents a diagram of the installation containing two blocks, each of which is made of two reactors 1, 21 and 22, 23, respectively, while the cathode chambers of all reactors are hydraulically connected to the feed line of the initial solution 7 in parallel, and the anode chambers of the reactors 1 and 21 of the first block, and the anode chambers of the reactors 22 and 23 of the second block are connected in series inside each block, and the blocks themselves are connected in parallel, while the output line of the disinfectant solution 4 is connected to the conclusions of the anode chambers of the rector 1 of the first block and the reactor 23 of the second block. On Fig presents a diagram of an installation containing three units, each of which is made of three reactors 24, 25 and 26 - the first unit, 27, 28 and 29 - the second, and 30, 31 and 1 - the third. The installation contains a supply line of tap (drinking) water 8, a container with a concentrated solution of chloride 9 and a pump 10. The cathode chambers of all reactors are hydraulically connected in parallel, and the anode chambers are in series inside each block, and the blocks themselves are hydraulically in parallel.

On Fig presents a diagram of the installation, in accordance with one aspect of the present invention, in which support overpressure in the anode chambers. The installation contains one unit made of two diaphragm electrochemical reactors 1 and 32, as well as a flotation reactor 11, an electrokinetic reactor 16, a feed line for the initial solution 7, a feed line for fresh water 8 and a water-jet pump 10. On Fig presents according to another aspect of the present invention, the installation diagram, which maintain the excess pressure in the cathode chambers. The installation contains one unit made of two diaphragm electrochemical reactors 1 and 32, as well as a flotation reactor 11, an electrokinetic reactor 16, a feed line for the initial solution 7, a feed line for fresh water 8 and a mixer 55.

In FIG. 16 shows, according to yet another aspect of the present invention, a plant arrangement in which overpressure in the anode chambers is maintained. The installation contains one unit made of three diaphragm electrochemical reactors 1, 33 and 34, as well as a flotation reactor 11, an electrokinetic reactor 16, a feed line for a feed solution 7, a feed line for fresh water 8, water-jet pumps 56, 57, 58 and a pressure regulator 37 .

Installation works as follows. The initial solution of a concentration of 0.2 - 2.0 g / l via line 7 is fed into the reactor block of the installation containing two reactors 1 and 18 (Fig. 10). The solution enters the cathode chambers of reactors 1 and 18 in parallel.

The streams processed in the cathode chambers of reactors 1 and 18 are connected and fed into a sealed flotation reactor 11. In the flotation reactor 11, mainly, the process of separation of liquid and gas occurs. The solution after the previous cathodic treatment in an electrochemical reactor is saturated with electrically active microbubbles of hydrogen. The sizes of microbubbles of hydrogen are in the range of 0.2 - 10 microns. The electrical activity of hydrogen bubbles is due to the fact that electrochemically active unstable products of cathodic reactions, such as H ₂ O ₂ ^" , HO ₂ ^" , O ₂ ^" , e _aq , are concentrated at the gas-liquid interface. At the same interface, insoluble metal hydroxides and other colloidal particles. Removing all microbubbles of gas in a conventional flotation reactor requires a lot of time due to the low speed of their floating. Therefore, in the most advanced electroflotation reactors it is possible to separate no more than 70% of all ex floatable particles. As a result, the solution is fed into the anode chamber only with dissolved gas (hydrogen), but without gas bubbles, which allows you to change the chemical composition of the resulting disinfectant solution - neutral anolyte AHK (increase the yield of ozone and peroxide compounds). A portion of the overflow from the flotation reactor 11 is diverted from the system via line 15 through the valve 54, and the remaining part of the stream is sequentially processed in the anode chamber of the reactor 18, and after exiting it is fed into the anode chamber of the reactor 1 and, after processing in this chamber, line 4 received disinfectant solution - neutral anolyte AHK - is supplied to the consumer.

In the process of processing the initial solution after the flotation reactor 11, an electrokinetic reactor 16 can be installed with an entrance at the top and an exit at the bottom. In the electrokinetic reactor, the remaining part of the hydroxides of heavy metals, including iron and other colloidal suspensions, is removed. In an electrokinetic reactor, conditions are created for the electrostatic confinement of colloidal particles in the zone of diffusion layers of electrochemically activated surfaces of mineral crystals (for example, large quartz crystals with a size of 1, 5 - 2.0 mm). The operation of the reactor is based on the use of electrokinetic phenomena — electroosmosis, electrophoresis, electro-filtration — known from colloid chemistry. Due to the thick diffuse layers (Gui-Chapman ionic layers) surrounding the mineral particles of the reactor’s active mass, water with a low redox potential flows freely through its charge, leaving colloidal particles and other colloidal suspensions in the diffusion layers of the reactor’s active mass. The active mass of the reactor is regenerated by removing charges from the surfaces of mineral crystals and removing colloidal suspensions by washing with water. For efficient operation of the reactor, an electrokinetic reactor is fed with a solution after cathodic treatment with a high reduction potential, which induces the appearance of electrically active ion-hydrated shells around the mineral crystalline particles of the active mass of the reactor. Depending on the performance requirements and characteristics of the resulting disinfectant solution, the reactor unit of the installation may contain three reactors (Fig. 11) or four reactors. The installation may also contain two blocks (Fig. 12) or three blocks (Fig. 13). The initial solution of the desired concentration is fed to processing through line 7. For the preparation of the initial solution, concentrated chloride solutions can be used, for example, a solution with a concentration of 50-100 g / l. In this case, the installation provides a container for concentrated solution 9 (Fig. 13) and a fresh water supply line 8. The concentrated solution is mixed with fresh water, for example, using pump 10, in which the flows are mixed to a concentration of 0.2 - 2, 0 g / l and are fed to the cathode chambers of the reactor units for processing.

During operation of the installation, an initial solution of a concentration of 50 - 250 g / l can be used (see Figs. 14.15 and 16).

In the installation shown in Fig. 14, the concentrated solution from the container for the concentrated solution (not shown in the figure) enters through the line 7 for processing into the cathode chambers of the reactors 1 and 32. After processing, the streams from the chambers are connected and fed to the pump 10, to which a fresh water supply line 8 is connected. The solution processed in the cathode chamber is diluted to a concentration of 0.2 - 2.0 g / l and is supplied for further processing. Due to the use of a pump, the pressure in the anode chambers of the reactors exceeds the pressure in the cathode chambers.

The concentrated solution after processing in the cathode chambers can enter the mixer 55 (Fig. 15), to which the fresh water supply line is connected 8. By using the mixer, it is possible to increase the pressure in the cathode chambers compared to the anode chambers.

A scheme can be used in which the initial solution with a concentration of 50 - 250 g / l is supplied in parallel flows to the cathode chambers of reactors 1, 33 and 34 (Fig. 16), and after processing in the cathode chambers of reactors 1, 33 and 34 through a peristaltic pump 56, creating excess pressure in the anode chambers of the reactors 1, 33 and 34, the flotation reactor 11 and the tank with the catalyst 16, the original the concentrated solution enters the anode chamber of the reactor 33, and then through the peristaltic pump 57 to the anode chamber of the reactor 34 and then through the peristaltic pump 58 to the anode chamber of the reactor 1. Fresh water supply line 8 is connected to the pumps 57 and 58 through the pressure regulator 37, and Before processing in the anode chambers of the reactors 34 and 1, a partial dilution of the initial solution occurs, until a concentration of 0.2 - 2.0 g / l is reached at the outlet of the anode chamber of the reactor 1.

An aqueous solution of oxidants in the implementation of the present invention, referred to by the authors as "neutral anolyte AED", can also be obtained in plants, the schemes of which are shown in FIG. 17 and 18. Installations work as follows.

Highly mineralized solution from tank 9 with open ventel

59 enters the tank 12, filling the cathode chambers and circulation circuits. Drinking water (low saline solution) flows through line 8 and, using a pump 10, mixes with the highly saline solution from tank 12, fills the anode chamber of reactor 35 and fills the anode chamber of reactor 1 through flow 60 (Fig. 17). After filling the installation, voltage is applied to the electrodes of reactors 1 and 35.

The initial solution obtained in the pump 10, before being fed into the anode chamber of the reactor 35, enters the separator 61, in which precipitated hardness salts can be separated and part of the solution is removed. The solution is processed in the anode chamber of the reactor 35, and after exiting from it through line 60, it is supplied to the anode chamber 2 of reactor 1, and after processing in this chamber through line 4 through the pressure regulator 6, an aqueous solution of oxidants - neutral anolyte AND - is supplied to the consumer.

From the anode chamber of the reactor 35, the entire fluid flow with dissolved oxygen and hydrogen, as well as hydrogen gas and oxygen, enters the anode chamber 2 of the reactor 1, the pressure of which is greater than 0 in the cathode chamber 3 (circulation loop) of the reactor 1, 1 to 0.4 kgf / cm ² .

The solution in the cathode chamber 3 is processed in a circulating mode due to gas lift, therefore, its pH exceeds 10. With increasing pH 00115

39 over 12 part of the solution from the circuit is discharged through line 10 to the drainage, and a fresh stock solution is supplied to the circuit.

In the process of processing the initial solution in the reactor 35 during flow from the cathode chamber to the anode on line 12, a separator 14 can be installed to remove part of the solution without gas bubbles (Fig. 2). As a result, a solution is supplied to the anode chamber only with dissolved and undissolved gases, which participate in electrochemical reactions at the anode and can increase the yield of highly active biocidal compounds. An aqueous solution of oxidants — the neutral anolyte AND — can also be obtained in plants, the scheme of which is shown in FIG. 19-21. Installations work as follows. The highly mineralized solution along the line from the tank 9 through the pump enters the mixer 61, in which it is mixed with drinking water (low mineralized solution), coming in line 8 (Fig.19).

The working solution obtained in the mixer is fed into the cathode chamber of the reactor 35, and also through the control valve fills the circulation circuit and the tank 12 of the reactor 1.

From the cathode chamber of the reactor 35, the solution through the overflow line 62 enters the anode chamber of the reactor 35, and after exiting from it through line 63 it is supplied to the anode chamber 2 of reactor 1, and after processing in this chamber through line 4 through the pressure regulator 6, the neutral anolyte AND is fed to the consumer.

The main biocidal compound formed in the anode chamber of the reactor 35 when the entire stream of liquid and gaseous products from the cathode chamber is supplied under conditions of almost the same pressure in the electrode chambers of the reactor is hypochlorite ion.

From the anode chamber of the reactor 35, the entire fluid flow with dissolved oxygen and hydrogen, as well as hydrogen gas and oxygen, enters the anode chamber 2 of the reactor 1, the pressure of which is greater than 0.1 in the cathode chamber (circulation loop) of the reactor 1 up to 0.4 kgf / cm ² . The solution in the cathode chamber is processed in a circulating mode due to gas lift, therefore, its pH exceeds 10. With an increase in pH above 12, part of the solution from the circuit is discharged via line 15 to the drain, and a fresh initial solution is supplied to the circuit. In the process of processing the initial solution in the main reactor during the flow from the cathode chamber to the anode on line 62, a separator 64 can be installed to separate the liquid and gas (Fig. 20). As a result, a solution with only dissolved gases, but without gas bubbles, is fed into the anode chamber of reactor 35, which allows changing the chemical composition of the obtained anolyte AND (increasing the yield of ozone and peroxide compounds).

If the separator 64 is located on line 63 (Fig. 21), then the biocidal substances of the obtained anolyte AND are mainly represented by oxygen compounds of chlorine.

Case Studies

The invention is illustrated by the following examples, which, however, do not exhaust all possible embodiments of the invention.

The disinfectants according to the invention for the disinfection, pre-sterilization cleaning and sterilization of medical devices are synthesized in plants, the schemes of which are shown in Figures 1 - 21. In all examples, the electrochemical reactor according to US Pat. No. 5, 635, 040 with coaxially mounted cylindrical and rod electrodes and coaxially the ceramic ultrafiltration ceramic diaphragm installed between them, based on a mixture of zirconium, aluminum, and yttrium oxides (60, 37, and 3%, respectively cc) and 0.7 mm thick. The electrodes used were titanium coated from a mixture of ruthenium and iridium oxides (anode) and titanium with a pyrocarbon coating (cathode).

The efficiency of the aqueous solution of oxidants obtained in the anode chamber was evaluated by the following parameters: - hydrogen indicator (pH), the redox potential (ORP), measured relative to the silver chloride reference electrode, mV,

- oxidizing ability equivalent to the content of active chlorine (C _O χ), m g / l,

- total salt content (C ₀ ), g / l,

The specific energy consumption for the solution was also measured.

Example 1. A disinfectant was obtained on the installation, a diagram of which is shown in figure 1.

Tap water through line 8 is mixed in a mixer 10 (made in the form of a water-jet pump) with a solution of sodium chloride concentration of 150 g / l, the supply of which is carried out from the tank 9; along line 7, the resulting initial solution with a concentration of 2.0 g / l enters the anode chamber 2 of the electrochemical reactor 1, the pressure in which during operation should be higher than the pressure in the cathode chamber 3 by 0.3 kgf / cm ² . The cathode chamber 3 of the reactor 1 is connected to the circulation tank 12, forming a closed circulation loop of the auxiliary electrolyte. The main source of replenishment of the catholyte circulation loop is the anode chamber 2 of reactor 1, from which sodium ions penetrate through the diaphragm into the cathode chamber 3 together with the water surrounding them and making up the hydration shells. The excess catholyte is removed from the tank 12 at the drain outlet 15. The hydraulic resistance 36 on the feed line of the lower part of the cathode circulation circuit is designed to fill the circulation tank 12 at the time of starting the electrochemical system and drip feed of the initial solution into the circulation circuit during operation. At the outlet of the anode chamber of the reactor, the obtained aqueous solution of oxidants, anolyte AN, having a pH value of 6.5, a salt content of 2.0 g / l and an oxidant content of 1000 mg / l, is withdrawn through line 4.

On line 4, a mixer 5 is installed, into which an additive, ethyl alcohol, is supplied in an amount determined by the calculation formula, 24 g / l. After mixing with an aqueous solution of oxidants, the resulting disinfectant is sent to the consumer.

The obtained disinfectant has the following advantages compared to the means obtained according to the prototype: high activity in the processing of hydrophobic objects, including increased wetting ability of hydrophobic surfaces with dry organic load. Example 2. The disinfectant was obtained on the installation, a diagram of which is shown in figure 2.

Tap water through line 8 passes through a filter 38 and is mixed after a gearbox 37 in a mixer 10 with a saturated solution of sodium chloride, the supply of which is from tank 9; along line 7, the resulting initial solution with a concentration of 1.0 g / l enters the anode chamber 2 of the electrochemical reactor 1, the pressure in which during operation should be higher than the pressure in the cathode chamber 3, by 0.7 - 0.8 kgf / cm ² . This pressure is provided by a pressure reducer 6 installed on the drain line 4 of the finished disinfectant solution.

The cathode chamber 3 of the reactor 1 is connected to the separator 11, forming a closed circulation loop of the auxiliary electrolyte. The main source of replenishment of the catholyte circulation loop is the anode chamber 2 of reactor 1, from which sodium ions and water molecules surrounding them and constituting hydration shells penetrate through the diaphragm into the cathode chamber 3. The excess catholyte is removed from the separator 11 at the drain outlet 13. At the outlet of the anode chamber of the reactor, line 4 is discharged to the obtained aqueous solution of oxidants - anolyte AHK, having a pH value of 7.0, a salinity of 1.0 g / l and an oxidant content of 700 mg / l . Dosed electrodiffusion selection of hydroxyl ions from the cathode chamber, followed by the introduction of part of the volume of catholyte saturated with dissolved hydrogen into freshly prepared anolyte to the desired pH value, takes place using mixer 39, which is a water-jet pump. On line 4, a mixer 5 is installed, in which an additive - ethyl alcohol - is supplied in an amount determined by the calculation formula - 8.4 g / l. After mixing with an aqueous solution of oxidants, the resulting disinfectant is sent to the consumer.

The obtained disinfectant has the following advantages compared to the means obtained according to the prototype: high activity in the processing of hydrophobic objects, including increased wetting ability of hydrophobic surfaces with dry organic load.

The following examples show the preparation of aqueous oxidant solutions that can be used in the practice of the present invention.

Example 3. To obtain an aqueous solution of oxidants, the schemes shown in FIG. 3-5

The data are shown in table 1.

Table 1

Пример 4. Для получения водного раствора оксидантов использовали установки, схемы которых приведены на фиг 8 и 9. Каждая из электрохимических систем содержала по 2 элемента ПЭМ.

Example 4. To obtain an aqueous solution of oxidants, we used plants, the schemes of which are shown in Figs. 8 and 9. Each of the electrochemical systems contained 2 TEM elements.

The results of comparative tests of electrochemical systems of the prototype and the present invention are shown in the following table 2.

table 2

Comparative characteristics of the operation of electrochemical systems

Example 5. The initial solution of sodium chloride with a salinity of 2.0 g / l was processed in the installation, the scheme of which is shown in Fig.10.

The initial solution was simultaneously fed into the cathode chambers of reactors 1 and

18. After a single passage of the chambers, the stream was combined and entered the flotation reactor 11, from which the sludge was removed, and part of the solution was taken through the control valve 54. The main stream was fed to the electrokinetic tank 16, filled with a granular aluminosilicate catalyst, and left the tank , sequentially processed in the anode chamber of the reactor 18 and the anode chamber 2 of the reactor 1, after which through line 4 entered the collection of finished product. The flow rate of the solution in the anode chambers was 2.3 times higher than the flow rate in the cathode chambers.

Example 6. A concentrated solution of sodium chloride with a salinity of 200 g / l was processed in the installation, a diagram of which is shown in Fig. 14. Using a dosing pump, the initial solution was supplied via line 7 to the cathode chambers of reactors 1 and 32. The streams leaving the cathode chambers were combined and fed to a mixer 10, which also received fresh water through line 8. A solution diluted to a concentration of 1, 8 g / l, was processed in flotation reactor 11. Flotation sludge was removed from flotation reactor 11, and part of the solution was taken, after which the main stream was sequentially processed in the anode chambers of reactors 1 and 32. From the anode chamber 2 of reactor 1, the flow was directed along line 4 c finished product booster. The flow rate in the anode chambers was 3 times higher than the flow rate of the initial solution in the cathode chambers.

Example 7. A concentrated solution of sodium chloride with a salinity of 200 g / l was processed in the installation, the scheme of which is shown in Fig.16. The initial concentrated solution was simultaneously supplied to the cathode chambers of reactors 1, 33, and 34. The streams leaving the cathode chambers were combined and entered the pump 56 and then to the flotation reactor 11. Flotation sludge was removed from the flotation reactor and a part of the solution was taken, after which the main stream was processed in the electrocatalytic reactor 16, and then in the anode chamber of the reactor 33. The stream processed in the anode chamber of the reactor 1 was fed to a mixer 57, into which fresh water was supplied, and was diluted to a concentration of 8 g / l and fed to brabotku the anode reactor chamber 34, from which the flow is fed to a mixer 58 which was diluted to a concentration of 1, 6 g / l and treated in the anode chamber of the reactor 1, from which the fed via line 4 to the collection of the finished product. The flow velocity through the cathode chambers was 2 times lower than the flow velocity through the anode chamber of the reactor 33, and accordingly 3 and 4 times lower than the flow velocity in the anode chambers of the reactors 34 and 1. Table 3

Example 8. The preparation of an aqueous solution of oxidants was carried out according to the schemes depicted in FIG. 17-18. The data are shown in table 4.

Table 4

Example 9. Obtaining aqueous solutions of oxidants was carried out in plants, the schemes of which are shown in FIG. 19-21. The data are shown in table 5.

Table 5

При введении в растворы оксидантов, полученных в примерах 3-9, добавки этилового спирта в количестве до 10 % об. коррозионная активность снижалась в среднем на 90%, а при введении изопропилового спирта или смеси спиртов - соответственно на 80 и 85 %.

When introducing into the solutions of the oxidants obtained in examples 3-9, additives of ethyl alcohol in an amount of up to 10% vol. corrosion activity decreased on average by 90%, and with the introduction of isopropyl alcohol or a mixture of alcohols - by 80 and 85%, respectively.

Applicability

As follows from the above, the use of the invention allows to reduce the corrosion activity of aqueous chlorine-containing solutions of oxidants with a pH of 6.5 - 7.5, a total salt content of 0.2 - 2.0 g / l and an oxidant content of 80 - 1000 mg / l, the method of preparation of which includes the processing of the initial aqueous solution of alkali metal chloride in the anode chamber of the diaphragm electrochemical reactor, and to obtain disinfectants with reduced corrosion activity, which have wide functional capabilities due to the possibility of efficient processing of products and surfaces from various, including hydrophobic, materials of protein and non-protein origin.

Claims

Claim 1. A method of reducing the corrosion activity of aqueous chlorine-containing solutions by introducing a corrosion inhibitor, characterized in that the aqueous chlorine-containing solutions of oxidants with a pH of 6.5 - 7.5, a total salt content of 0.2 - 2.0 g / l and an oxidant content of 80 - 1000 mg / l, the production method of which includes processing the initial aqueous solution of alkali metal chloride in the anode chamber of the diaphragm electrochemical reactor, a low molecular weight mono- or dihydric alcohol or a mixture of such alcohols is introduced as a corrosion inhibitor, wherein Ozias introduced into the oxidant solution in an amount of up to 10% by volume after treatment in the anode chamber before use. 2. A method of reducing the corrosion activity of aqueous chlorine-containing solutions according to claim 1, characterized in that ethanol is used as a corrosion inhibitor, a sodium chloride solution is used as a metal chloride initial solution, and a corrosion inhibitor is introduced in an amount determined by the formula C _a ι = (0.012 χ C _NaC i) χC _o χ, where C _a i - ethanol concentration, g / l Sy _a cι - concentration of the initial solution of sodium chloride, g / l C _0x - concentration of oxidants, mg / l. 3. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that when preparing aqueous solutions of oxidizing agents by treating the initial solution in the anode chamber of a diaphragm electrochemical reactor, the initial solution is prepared by mixing a low-mineralized aqueous solution or drinking water with a highly mineralized aqueous electrolyte solution, and processing lead when the pressure in the anode chamber is exceeded by 0.2 - 0.4 kgf / cm 2 while maintaining the pH of the solution in the cathode chamber at a level of 12-14 by circulation solution into the cathode circulation circuit, comprising a container with inlet at the top and an outlet at the bottom, wherein the input and the output of the cathode chamber is connected respectively to the output and to the input of the capacitance with the formation of a circulation loop. 4. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that when preparing aqueous solutions of oxidants by treating the initial solution in the anode chamber of a diaphragm electrochemical reactor, the initial solution is prepared by mixing a low-mineralized aqueous solution or drinking water with a highly mineralized aqueous electrolyte solution, processing Overpressure in the anode chamber by 0.2 - 0.4 kgf / cm ² while maintaining the pH of the solution in the cathode chamber at a level of 12-14 by circulating a solution in the cathode circulation loop containing a flotation reactor with an inlet in the middle and an outlet in the lower parts, the inlet and outlet of the cathode chamber being connected respectively to the outlet and the inlet of the vessel to form a circulation loop, and after processing in the anode chamber, an aqueous solution of oxidants is mixed with a solution selected from the cathode circulation circuit in the ratio (1, 1-2.0): 1. 5. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that when preparing aqueous solutions of oxidizing agents by treating the initial solution in the anode chamber of a diaphragm electrochemical reactor, the initial solution is prepared by mixing a low-mineralized aqueous solution or drinking water with a highly mineralized aqueous electrolyte solution and before mixing a highly mineralized electrolyte solution is treated in the cathode chamber of the same reactor, and the treatment is carried out in the mode of cir rations using a circulation circuit with an additional capacity while maintaining the pH value of the electrolyte in the circulation circuit at a level of 13-14, part of the highly mineralized electrolyte taken from the circuit is mixed and the mixture is mixed until the initial solution concentration reaches 0.2 - 2.0 g / l while maintaining the volumetric flow rate of the stream of the initial solution through the anode chamber at a level of 100 - 500 from the volumetric flow rate of the duct of highly mineralized electrolyte through the cathode chamber to achieving anolyte pH values of 6.5 - 7.5 and a redox potential of plus 250 to plus 800 mV relative to the silver chloride reference electrode while maintaining the pressure difference in the anode and cathode chambers of the reactor at a level that ensures filling the pores of the diaphragm with anolyte within from 70 to 100% of the thickness of the diaphragm. 6. The method according to claim 5, characterized in that the process of obtaining an aqueous solution of oxidants is carried out while maintaining the pressure in the anode chamber of the reactor exceeding the pressure in its cathode chamber, feeding the circulation circuit by supplying a highly mineralized electrolyte solution to the lower point of the circuit before entering the cathode chamber the selection of the processed highly mineralized electrolyte for mixing is carried out from the upper part of the additional capacity of the circulation circuit and the preparation of the initial solution is a sealed mixer, and adjusting the pH in the circulation circuit of the reactor cathode chamber is effected by selecting part of the original solution as a gas-liquid mixture from the sealed mixer. 7. The method according to claim 5, characterized in that the process of obtaining an aqueous solution of oxidants is carried out when the pressure in the anode chamber of the reactor is higher than the pressure in its cathode chamber, the circulation circuit is fed by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the circulation circuit, the selection of the processed highly mineralized electrolyte for mixing is carried out from the upper part of the additional capacity of the circulation circuit, the preparation of the initial solution and lead in a separator with the simultaneous separation of electrolysis gases, and pH regulation in the circulation circuit of the cathode chamber of the reactor is carried out by removing part of the treated highly mineralized electrolyte solution from the lower part of the additional tank. 8. The method according to claim 5, characterized in that the process of obtaining an aqueous solution of oxidants is carried out while maintaining the pressure in the anode chamber of the reactor less than the pressure in its cathode chamber, recharge the circulation circuit is carried out by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the circulation circuit, the processed highly mineralized electrolyte is selected for mixing from the upper part of the additional capacity of the circulation circuit, and the initial solution is prepared in a sealed mixer, and the pH is maintained in the circulation circuit of the cathode chamber of the reactor due to the selection of part of the initial solution in the form of a gas-liquid mixture from hermetic th flotation reactor installed in front of the anode chamber and an aqueous solution of oxidant discharge from the anode chamber is performed through a pressure regulator. 9. The method according to claim 5, characterized in that the process of obtaining an aqueous solution of oxidants is carried out while maintaining the pressure in the anode chamber of the reactor lower than the pressure in its cathode chamber, feeding the circulation circuit by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the circulation circuit , the selection of the processed highly mineralized electrolyte for mixing is carried out from the lower part of the additional capacity of the circulation circuit, and the preparation of the initial solution the solution is kept in the mixer, neutral anolyte AHK is removed from the anode chamber through a pressure regulator, and pH values are maintained in the circulation circuit of the reactor cathode chamber by removing part of the treated highly mineralized electrolyte solution from the upper part of the additional tank 10. The method according to claim 5, characterized in that the process of obtaining an aqueous solution of oxidants is carried out while maintaining the pressure in the anode chamber of the reactor lower than the pressure in its cathode chamber, feeding the circulation circuit by supplying a highly mineralized electrolyte solution to the lower part of the additional capacity of the circulation circuit the selection of the processed highly mineralized electrolyte for mixing is carried out from the lower part of the additional capacity of the circulation circuit and The initial solution is prepared in a mixer, the neutral anolyte AHK is removed from the anode chamber through a pressure regulator, and the pH values are maintained in the circulation circuit of the reactor cathode chamber by removing part of the treated highly mineralized electrolyte solution from the lower part of the additional tank while hydrogen is removed from the upper part additional capacity. 11. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that when receiving aqueous solutions of oxidants by treating the initial solution in the anode chamber of the diaphragm electrochemical reactor, before processing in the anode chamber, the initial solution is processed in the cathode chamber of the same diaphragm electrochemical reactor with the subsequent separation of the flow of the treated solution into two parts, one of which is removed from the treatment cycle, and the other is fed to the anode chamber for processing of the reactor, the stream before separation sequentially processed in the cathode and anode chambers further diaphragm electrochemical reactor, and the processing in the primary and secondary reactors being processed in the cathode chamber solution move cocurrent or countercurrent to the direction of movement of the solution in the anode compartments. 12. The method according to p. 11, characterized in that, when processing the main and additional reactors, the solution to be treated in the cathode chambers moves in direct flow with respect to the direction of the solution in the anode chambers, the concentration of sodium chloride in the initial solution is 0.2-2.0 g / l, while part of the flow output from the treatment cycle is 2-5%. 13. The method according to p. 11, characterized in that when processing the primary and secondary reactors, the treated solution in the cathode chambers moves countercurrently with respect to the direction of the solution in the anode chambers, the concentration of sodium chloride in the initial solution is 0.2-2.0 g / l, while part of the flow output from the processing cycle is 0.5-3.0%. 14. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that upon receipt of aqueous solutions of oxidants by treating the initial solution in the anode chamber of the diaphragm electrochemical reactor, the initial solution is treated in the cathode chamber of the diaphragm electrochemical reactor with subsequent removal of part of the solution processed in the cathode chamber and processing the main flow of the solution in the anode chamber of the diaphragm electrochemical reactor, and processing is carried out using by a unit of electrochemical reactors containing 2, 3 or 4 reactors with a single parallel flow of the solution through the cathode chambers of all reactors, part of the solution processed in the cathode chambers is removed by treatment in a sealed flotation reactor with the output of sludge, and the main stream is sequentially processed in the anode chambers of the reactors moreover, the flow rate of the treated solution through the anode chambers of the reactors is 2 to 4 times higher than the speed of its flow through the cathode chambers. 15 The method according to p. 14, characterized in that when receiving an aqueous solution of oxidants, an initial solution of sodium chloride with a concentration of 50-100 g / l is used and before treatment in the cathode chambers of the reactors, the initial solution is mixed with fresh water to a concentration of 0.2-2.0 g / l 16. The method according to p. 14, characterized in that when receiving an aqueous solution of oxidants, an initial solution of a concentration of 50-250 g / l is used, and after processing in the cathode chambers of the reactors, the treated solution is mixed with fresh water to a concentration of 0.2-2.0 g / l 17. The method according to p. 14, characterized in that when receiving an aqueous solution of oxidizing agents, an initial solution of a concentration of 50-250 g / l is used, and after processing in the cathode chambers of the reactors, flotation reactor and the first anode chamber in the course of flow before processing in each of subsequent anode chambers of the reactors, the treated solution is mixed with fresh water, lowering its concentration, and at the entrance to the last in the course of the treated solution, the concentration of the treated solution is 0.2 - 2.0 g / L. 18. The method according to one of paragraphs.14 to 17, characterized in that the processing is carried out when the pressure in the anode chambers of the reactors is higher than the cathode chambers or when the pressure in the cathode chambers is higher than the anode chambers, the pressure drop in the electrode chambers of the reactors is not less than 0.3 atm. 19. The method according to one of paragraphs. 14 to 18, characterized in that after treatment in a flotation reactor, before being fed into the anode chambers, the solution is passed through a catalyst bed, for example, aluminosilicate, oxide-zirconium, oxide-niobium. 20. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that when receiving aqueous solutions of oxidants by treating the initial solution in the anode chamber of a diaphragm electrochemical reactor, the initial solution is prepared by mixing drinking water or a low saline aqueous solution with a highly saline aqueous electrolyte solution and processing an electrochemical reactor is conducted at a specific electricity consumption of 400-4000 C / l, and after processing in the anode chamber of the reactor, the solution under is fed into the anode chamber of the additional electrochemical reactor, and the processing in the anode chamber of the additional reactor is carried out until the pH value is 6.5 - 7.5 and the redox potential plus 700 - plus 1100 mV relative to the silver chloride reference electrode, the cathode chambers of the main and additional electrochemical reactors connected by circulating circuits with a tank with a highly mineralized aqueous electrolyte solution, drinking water or a low-mineralized solution and high-minerals are mixed A fixed electrolyte solution taken from the circulation circuit, and the pH of the auxiliary electrolyte circulating in the cathode chamber is maintained at least 10 or by removing part of the initial solution before feeding it into the anode chamber of the main reactor, or by draining part of the highly mineralized electrolyte solution from the tank, and processing in an additional electrochemical reactor is carried out at excess pressure in the anode chamber compared with the cathode by 0.1 - 0, 4 kgf / cm ² . 21. The method according to claim 20, characterized in that when receiving an aqueous solution of oxidizing agents, as a highly mineralized electrolyte solution, a solution of sodium chloride with a total salinity of 50-300 g / l is used. 22. A method of reducing the corrosive activity of aqueous chlorine-containing solutions according to claim 1, characterized in that when preparing aqueous solutions of oxidants, the initial solution is prepared by mixing drinking water or a low saline aqueous solution with a highly saline aqueous electrolyte solution, followed by processing the resulting stock solution sequentially in the cathode and anode chambers diaphragm electrochemical reactor with a specific electricity consumption of 400 - 4000 C / l, with subsequent supply of the treated solution to the anode chamber of the additional electrochemical reactor and the processing in the anode chamber of the additional reactor are carried out until the pH value is 6.5 - 7.5 and the redox potential is plus 700 - plus 1100 mV relative to the silver chloride reference electrode, the cathode chamber of the additional electrochemical reactor is equipped with a secondary electrolyte circulation circuit with a capacity, moreover, the pH of the auxiliary electrolyte circulating in the cathode chamber is maintained at a level of not less than 10, and processing in addition An electrochemical reactor is conducted when the pressure in the anode chamber is higher than the cathode by 0.1-0.4 kgf / cm ² . 23. The method according to p. 22, characterized in that upon receipt of an aqueous solution of oxidants, an initial solution is used as an auxiliary electrolyte, and the output of an aqueous solution of oxidants from the anode chamber of the additional electrochemical reactor is carried out through a pressure regulator. 24. The method according to p. 22, characterized in that upon receipt of an aqueous solution of oxidizing agents, a low-saline solution or drinking water is used as an auxiliary electrolyte, before serving the treated solution into the anode chamber of the first electrochemical reactor, at least part of the gaseous and dissolved hydrogen is removed from it, and the aqueous solution of oxidants is removed from the anode chamber of the additional electrochemical reactor through a pressure regulator. 25. The method according to p. 22, characterized in that when receiving an aqueous solution of oxidants as an auxiliary electrolyte, a low-mineralized solution or drinking water is used, at least part of the free and dissolved electrolysis gases are removed from it before it is fed to the anode chamber of an additional electrochemical reactor and the conclusion of an aqueous solution of oxidants from the anode chamber of the additional reactor is carried out through a pressure regulator. 26. A disinfectant containing an aqueous solution of oxidants, with a pH of 6.5 - 7.5, a total salt content of 0.2 - 2.0 g / l and an oxidant content of 80 - 1000 mg / l, characterized in that it additionally contains an additive - low molecular weight alcohol, with the following ratio of components in volume%: low molecular weight - 0, 1 - 10.0 aqueous solution of oxidants - the rest, and the additive is introduced into the solution of oxidants after treatment in the anode chamber before use. 27. The disinfectant according to claim 26, characterized in that ethanol or isopropyl alcohol or a mixture thereof is used as a low molecular weight alcohol.