RU2814349C1 - Device for creating gas-liquid flow, method and system for dissolving gas in liquid - Google Patents

Abstract

FIELD: various technological processes.

SUBSTANCE: group of inventions relates to methods and devices for dissolving gases in liquids and can be used, in particular, for dissolving air oxygen in water during treatment of domestic and industrial waste water. System for dissolving gas in a liquid comprises in-series connected a liquid supply unit, at least one device for creating a gas-liquid flow, located above the surface of the volume of liquid in which the gas is dissolved, and at least one turbine located in the bottom area of the liquid volume. Device for creating a gas-liquid flow comprises nozzle, working chamber, ejector chamber and diffuser, all being connected in series to make a single cylindrical housing. Nozzle consists of confuser and cavitator. At the beginning of the ejector chamber there are support posts with openings for gas supply along the external surface of the liquid flow. In cavitator there are channels for suction of gas flow from external medium and its supply inside liquid flow. Nozzle is made with possibility to create gas-liquid flow and is characterized by a flow coefficient of not less than 0.9.

EFFECT: increased energy efficiency of gas dissolution in liquid.

23 cl, 1 tbl, 40 dwg

Description

TECHNICAL FIELD

The invention relates to methods and devices for dissolving gases in liquids and can be used, in particular, for dissolving oxygen in water in the process of treating domestic and industrial wastewater.

BACKGROUND OF THE ART

The phenomenon of hydrodynamic cavitation, first described by Rayleigh in [Rayleigh L. On the pressure developed in a liquid during the collapse of a spherical cavity // Philos. Mag. - 1917 - V. 34. - P. 94-98.], characterized by the appearance in a liquid medium of vapor-gas bubbles growing from cavitation nuclei as a result of a local decrease in pressure in the flow to a level at which evaporation of the liquid and diffusion of dissolved gases into the bubbles occurs. Cavitation that occurs through this mechanism is called natural. For hydrodynamic cavitation to occur, the necessary reduction in pressure in the liquid is achieved by accelerating the flow while reducing its open cross-section.

If gas is supplied to a rarefied region of a liquid flow, a phenomenon called artificial (ventilated) cavitation occurs, in which there is no evaporation of the liquid. Artificial cavitation is widely used in the technique of experimental studies of cavitation flows, as it allows the creation of cavities at significantly lower fluid velocities compared to natural cavitation.

In experimental studies, hydrodynamic cavitation tubes are widely used - devices, the structural elements of which have become the basic prototypes of the vast majority of cavitation technological devices [Gorshkov A.S., Rusetsky A.A. Cavitation pipes. Leningrad: Shipbuilding, 1972], [Borusevich V.O. Hydrodynamic aspects of designing cavitation pipes. Dissertation for the job application uch. Art. Ph.D. tech. Sciences, St. Petersburg, 2005, 185 pp.]. For example, what these devices have in common is that cavitation is created by locally accelerating the flow using a confuser and diffuser.

The threshold values of flow velocity and pressure at which cavitation occurs are related by the formula for the cavitation number. At low cavitation numbers, which correspond to high flow velocities and low pressures, a long cavity or supercavity is formed, the length of which is many times greater than the transverse size of the body behind which it is formed. It should be noted here that at the same flow rates, artificial cavitation leads to the formation of longer cavities. In other words, the process of forming an artificial supercavity is energetically more efficient. But the dynamics of a natural cavity are more intense, since it develops under conditions of large velocity and pressure gradients.

In practice, in the processes of dissolution of gases in liquids, high-speed hydrodynamic regimes of liquid flow, corresponding to natural cavitation, are often used with simultaneous supply of gas to the cavity region. It is assumed that the intense collapse of cavitation bubbles causes dispersion of the gas phase and intensified dissolution of gas in liquid. However, the intensity of the collapse of cavitation bubbles significantly depends on the presence of steam in it, the condensation of which causes high-speed collapse of the bubble. But the supply of gas to the cavity is accompanied by an increase in pressure in the cavity, which leads to the cessation of the process of evaporation of the liquid. Therefore, the target effect of gas dispersion due to cavitation effects with intense bubble collapse is not achieved, but a lot of energy is spent to ensure high flow rates.

A method and device for treating water using hydrodynamic cavitation is known from the prior art, disclosed in US 7247244 B2, published on April 20, 2006. The method involves supplying additional gas components to the flow section in which the cavitator is installed to carry out oxidation processes.

From US 7338551 B2, published 02/09/2006, a method and device for generating microbubbles in a liquid using hydrodynamic cavitation are known. The method involves gassing a liquid by supplying gas to the flow section in which the cavitator is installed to obtain a dispersed gas-liquid mixture.

US 6,012,492 A, published January 11, 2000, discloses a method and apparatus for carrying out sonochemical reactions using hydrodynamic cavitation. The method involves carbonating the liquid to control the progress of sonochemical reactions.

In the above patent sources, liquid flows with velocities of at least 12÷16 m/s are used in the compressed section of the flow in which the cavitator is installed. In addition, multi-stage cavitators and additional structural elements are used to compress the flow before or after the cavitator. Such solutions increase energy costs for the work process and cannot be used in technologies with more stringent requirements for their energy intensity.

From RU 2194024, published on December 10, 2000, an aerator is known. The aerator supplies gas to the region of liquid flow, in which the flow speed increases as it flows around a body installed in it to a level at which steam cavitation occurs. Dispersion of gas in liquid for carrying out oxidative processes is carried out using the energy of collapse of cavitation bubbles. In the aerator, the streamlined nozzle is made in the form of a combination of a cone 11, streamlined in the steam cavitation mode, and an impeller 12, which serves to enhance the turbulization of the flow. Gas enters the liquid flow in two of its sections, distant from each other along the flow. In this case, the first gas inlet along the flow is made through pipe 2 of the air injection line connected to a source of compressed air. Gas is supplied through pipe 2 not into the cavern, but into the liquid flow in a section located upstream to the low pressure zone 18. The second gas inlet along the flow path is made through pipe 6, which introduces gas not into the cavern, but into the low-pressure zone 18 around the cavern. The liquid flow regime assumes its cavitation boiling in zone 18 and the subsequent collapse of cavitation bubbles in zone 19. The vapor-gas cavitation thus created serves to disperse the gas flow in the liquid flow.

The use of additional sources of compressed air, carrying out the gasification process in the steam cavitation mode, requiring high flow velocities in the compressed section of the cavitator installation of more than 15 m/s, forced turbulization of the flow in the high-speed zone using specially installed difficult-to-flow bodies require increased energy consumption.

SU 865847 A1, published 09/23/1981, discloses a device for aerating water. The device, mounted on a pipe below the water level, uses local acceleration of the water flow in confuser 2. The resulting dynamic pressure reduction ensures air suction in two stages - between confusers 2 and 3 and between confusers 3 and 6 through the gaps between pipes 1 and 5 and the upper cylindrical part of the confuser 3. The device operates in non-cavitation mode and is used for aeration of wastewater.

The location of the device for water aeration under the water level is characterized by an increase in hydrostatic pressure, depending on the depth of its immersion, in those sections of the flow inside the device in which air is sucked. Increasing the specified pressure reduces the amount of air drawn in compared to options for installing the device above the water surface. Therefore, to maintain the amount of intake air at the required level in this device, an increase in the water flow rate is required, which causes additional energy losses.

The operating principle of this device for water aeration involves the release of a stream of aerated water into the surrounding volume. In this case, rapid separation of gas from water occurs with a concentration of floating bubbles around the device in close proximity to it. A wider volumetric distribution of air bubbles is possible by increasing the flow rate at the outlet of the device, which also leads to an increase in energy costs.

From RU 2248331 C1, published on March 20, 2005, a device for water aeration is known. The device contains a water supply pipe 1 with a conical nozzle 2, an air supply pipe 3 with a conical tip, which is a confuser, a mixing chamber 4 and a diffuser 5, coaxially located to the air supply pipe 3. The water supply pipe 1 is connected to the water supply pipeline 6 through a cylindrical distribution device 7 installed outside and coaxially relative to the air supply pipe 3. The distribution device 7 is equipped with pipes 8. The device operates in a non-cavitation mode and is used for aeration of wastewater. The device uses the effect of swirling the water flow entering through pipeline 6 into the distribution device 7 and then through pipes 8 into the water supply pipe 1, in which the water flow is tangentially swirled. Then the swirling flow is further accelerated in conical nozzle 2, at the output of which the rotating accelerated flow creates a vacuum in chamber 4 and sucks in air entering through pipe 3.

The acceleration and swirling of the flow ensures that air is sucked in and interacts with the rotating flow of water, as a result of which the air moves downstream. However, this method of organizing the process is not optimal from the point of view of energy consumption, since the water flow goes through several stages of intense vortex formation, flow collision and acceleration: at the inlet to the distribution device 7, at the inlet and outlet of the nozzles 8, in the water supply pipe 1, in the nozzle 2, in mixing chamber 4. The operating principle of this device involves the release of a stream of aerated water into the surrounding volume. In this case, rapid separation of gas from water occurs with a concentration of floating bubbles around the device in close proximity to it. A wider volumetric distribution of air bubbles is possible by increasing the flow rate at the outlet of the device, which also leads to an increase in energy costs.

The closest in technical essence to the proposed invention is a hydrodynamic cavitation mixer, disclosed in SU 1456206 A/1, published 02/07/1989.

The device consists of an ejector 1 with inlet pipes for components 2 and 3 and a mixture outlet 4, made in the form of a conical chamber 5 with a conical nozzle 6. Ejector 1 is equipped with a cavitator 7, made in the form of a confuser. The device contains a rotating divider 8 with radially arranged blades. The device operates in cavitation mode and is used, among other things, for mixing liquid and gas. The device provides water supply to pipe 2, from which water passes through nozzle 6, cavity 5 and cavitator 7 and then flows into the cavity of glass 10. In the compressed section of cavitator 7, a pressure drop occurs, which is accompanied by gas suction through pipes 3 and boiling of water as a result of cavitation flow.

The resulting stream of water and gas flows onto the rotating divider 8 at the bottom of the glass 10, resulting in additional dispersion of the gas in the water. The mixture of gas and liquid is removed from the device through pipes 4.

In this device, the operating process is carried out in steam cavitation mode to use the pulsed cavitation effects that occur when water evaporates and steam condenses to disperse the gas. To obtain such regimes, the water flow is accelerated in the cavitator channel to speeds of at least 32 m/s. After this, a high-speed jet flow flows onto a rotating divider 8, which serves to intensively mix the components of the flow in the volume of the glass 10. All these stages together cause large energy costs.

Technological processes of liquid gasification require the dissolution of a certain amount of gas and mainly contain two stages - gas absorption and its dissolution. Gas dissolution is effectively solved by dispersing it in a liquid flow, since an increase in the contact area of the gas and liquid phases intensifies mass transfer. But with an increase in the required amount of dissolved gas, it becomes necessary to increase the volume of sucked gas, and this complicates the process of its dispersion and worsens mass transfer. Intensification of gas dispersion by increasing the speed of liquid flow or its turbulization as a result of complicating the design of flow channels leads to an increase in energy costs. The solution lies in the optimal combination of hydrodynamic parameters (flow speed and pressure) in the gas suction and dispersion areas.

DISCLOSURE OF INVENTION

The technical problem that the proposed method solves is to increase the energy efficiency of dissolving gas in liquid, which is determined by the ratio of the amount of dissolved gas to the energy spent on this process.

The technical result achieved by implementing the proposed method coincides with the stated technical task.

The specified technical result is achieved due to the fact that the device for creating a gas-liquid flow contains a nozzle consisting of a confuser and a cavitator, a working chamber and a diffuser, connected in series and forming a single cylindrical body, while the cavitator has channels for sucking in the gas flow from the external environment and feeding it into the liquid flow, while the nozzle is characterized by a flow coefficient of at least 0.9.

Between the diffuser and the working chamber there is an ejector chamber, at the beginning of which there are support posts with windows for supplying gas along the outer surface of the liquid flow.

The cavitator is made in the form of a cylindrical body, inside of which there is an axisymmetric cavitating body and at least two struts connecting the axisymmetric cavitating body and the inner surface of the cavitator body, while inside each strut there is a channel for sucking a gas flow from the external environment and supplying it into the liquid flow , connected to a corresponding gas flow suction hole located in the cylindrical body.

The cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two parallel plates installed at a distance from each other in the cross-sectional plane of the cylindrical body, while at the entrance to the cavitator the plates are made pointed, and a channel is made in each plate for sucking a gas flow from the external environment and supplying it into the liquid flow, connected to a corresponding gas flow suction hole located in the cylindrical body.

The cavitating body has at least one additional channel located between the channels for sucking up a gas flow from the external environment and supplying it into the liquid flow, and at least one additional channel located in front of said channels for sucking up a gas flow, wherein said additional channels connected to each other and configured to supply technological additives into the liquid flow.

The cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two diametrically intersecting plates, while at the entrance to the cavitator the plates are made pointed, and in each plate there is a channel for sucking the gas flow from the external environment and supplying it into the flow liquid connected to a corresponding gas flow suction hole located in a cylindrical body.

The cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two diametrically non-intersecting fairings, while flexible tubes with channels are installed inside the fairings for sucking the gas flow from the external environment and supplying it into the liquid flow, one end of which is brought out into a liquid stream, and the other is fixed in a corresponding suction hole for a gas stream located in a cylindrical body.

The cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two parallel fairings, while flexible tubes with channels are installed inside the fairings for sucking the gas flow from the external environment and supplying it inside the liquid flow, one end of which is brought into the flow liquid, and the other is fixed in the corresponding hole for suction of the gas flow, located in the cylindrical body.

The method of dissolving gas in liquid includes the following steps:

a) forming a gas-liquid flow above the surface of the liquid, consisting of at least two gas flows and at least one liquid flow located between the gas flows, using a device for creating a gas-liquid flow;

b) supplying a gas-liquid flow to the bottom region of the liquid in the vertical direction;

c) dispersion of gas as part of a two-phase flow and distribution of gas in the volume of liquid;

d) dissolution of gas in a volume of liquid.

Gas dissolution is carried out in a stationary volume of liquid or a moving volume of liquid.

Additionally, when forming a gas-liquid flow, technological additives are introduced into the liquid flow.

A system for dissolving a gas in a liquid contains a series-connected liquid supply unit, at least one device for creating a gas-liquid flow located above the surface of the liquid volume in which the gas is dissolved, and at least one turbine located in the bottom region of the liquid and containing a diffuser, a guide base configured to change the direction of the gas-liquid flow, and perforated nozzles located in a plane perpendicular to the axis of the turbine diffuser, wherein the liquid supply unit and the device for creating a gas-liquid flow are connected to each other using a first pipeline, and the device for creating a gas-liquid flow and the turbine are connected to each other via a second pipeline.

Gas dissolution is carried out in a stationary volume of liquid or in a moving volume of liquid.

The guide base comprises a centrally located turbine fairing and guide vanes arranged radially around the turbine fairing.

The perforated nozzles are made in the form of a rectangular tube.

The perforated nozzles are made in the form of a round tube.

At least one perforated nozzle contains a guide tip bent in a vertical plane.

At least one perforated nozzle contains a guide tip bent in a horizontal plane.

Perforation - made in the form of a slot or in the form of holes of round, triangular, square, rectangular and polygonal shapes.

For a perforated nozzle in the form of a rectangular tube, the perforation is made on the vertical or horizontal surface of the perforated nozzle.

For a perforated nozzle in the form of a rectangular tube, the perforation is made on the vertical surface of the perforated nozzle in the form of a slot with an inclination from the lower horizontal surface at the entrance to the perforated nozzle to the upper horizontal surface at the exit of the perforated nozzle.

The liquid supply unit is made in the form of a pump mounted outside or inside a stationary volume of liquid.

The liquid supply unit is made in the form of a pump fixed outside or inside the moving volume of liquid.

The liquid supply unit is made in the form of a pump installed on a float platform.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention will be more clear from the description, which is not restrictive and is given with reference to the accompanying drawings, which show:

Fig. 1 is a longitudinal section through the claimed device according to the first embodiment of the invention.

Fig. 2 is a longitudinal section through the nozzle of the claimed device according to the first embodiment of the invention.

Fig. 3 - longitudinal section of the confuser of the claimed device.

Fig. 4 - cavitator of the claimed device according to the first embodiment of the invention.

Fig. 5 is a view of the cavitator of the claimed device according to the first embodiment of the invention (from the entrance side).

Fig. 6 is a local cross-section of the cavitator of the claimed device according to the first embodiment of the invention.

Fig. 7a is a view of the cavitator of the claimed device according to the first embodiment of the invention (from the outlet side).

Fig. 7b - distribution of gas and liquid flows in the cross section of the cavitator of the claimed device according to the first embodiment of the invention.

Fig. 8 - change in the profile of gas and liquid flows when using the cavitator of the claimed device according to the first embodiment of the invention.

Fig. 9 is a longitudinal section through a cavitation device known from the prior art.

Fig. 10 is a longitudinal section through the claimed device without an ejector chamber according to the first embodiment of the invention.

Fig. 11 - graphs of the dependence of the ejection coefficient on the liquid flow rate depending on the cavitator design: a - cavitator design according to FIG. 9; b - cavitator design according to Fig. 10; c - cavitator design according to Fig. 1; d - cavitator design according to Fig. 12; e - cavitator design according to Fig. 16; f - cavitator design according to Fig. 20.

Fig. 12 - cavitator of the claimed device according to the second embodiment of the invention.

Fig. 13 is a longitudinal section through the cavitator of the claimed device according to the second embodiment of the invention.

Fig. 14a is a cross-section of the cavitator of the claimed device according to the second embodiment of the invention.

Fig. 14b - distribution of gas and liquid flows in the cross section of the cavitator of the claimed device according to the second embodiment of the invention.

Fig. 15 is a longitudinal section through the cavitator of the claimed device according to the third embodiment of the invention.

Fig. 16 - cavitator of the claimed device according to the fourth embodiment of the invention.

Fig. 17 is a longitudinal section of the cavitator of the claimed device according to the fourth embodiment of the invention (section).

Fig. 18 is a longitudinal section of the cavitator of the claimed device according to the fourth embodiment of the invention (section).

Fig. 19 - distribution of gas and liquid flows in the cross section of the cavitator of the claimed device according to the fourth embodiment of the invention.

Fig. 20 is a longitudinal section through the cavitator of the claimed device according to the fifth embodiment of the invention.

Fig. 21 is a view of the cavitator of the claimed device according to the fifth embodiment of the invention in the transverse plane (from the entrance side).

Fig. 22 is a view of the cavitator of the claimed device according to the fifth embodiment of the invention in the transverse plane (from the outlet side).

Fig. 23 - distribution of gas and liquid flows in the cross section of the cavitator of the claimed device according to the fifth embodiment of the invention in the transverse plane.

Fig. 24 is a longitudinal section through the cavitator of the claimed device according to the sixth embodiment of the invention.

Fig. 25 - distribution of gas and liquid flows in the cross section of the cavitator of the claimed device according to the sixth embodiment of the invention.

Fig. 26 is a general view of a turbine according to the first embodiment of the invention.

Fig. 27 is a longitudinal section through a turbine according to a first embodiment of the invention.

Fig. 28 - longitudinal section of the turbine diffuser.

Fig. 29 is a general view of the turbine guide base.

Fig. 30 is a perspective view of a perforated nozzle according to the first embodiment of the invention.

Fig. 31 is a perspective view of a perforated nozzle according to a second embodiment of the invention.

Fig. 32 is a perspective view of a perforated nozzle according to a third embodiment of the invention.

Fig. 33 is a perspective view of a perforated nozzle according to a fourth embodiment of the invention.

Fig. 34 is a perspective view of a perforated nozzle according to a fifth embodiment of the invention.

Fig. 35 is a general view of a turbine according to a second embodiment of the invention.

Fig. 36 is a general view of a turbine according to a third embodiment of the invention.

Fig. 37 is a general view of the inventive system for dissolving gas in liquid according to the first embodiment of the invention.

Fig. 38 is a general view of the inventive system for dissolving gas in liquid according to the first embodiment of the invention.

Fig. 39 is a general view of the claimed system for dissolving gas in liquid according to the second embodiment of the invention

Fig. 40 is a general view of the claimed system for dissolving gas in liquid according to the third embodiment of the invention

1 - confuser; 2 - cavitator; 3 - working chamber; 4 - ejector chamber; 5 - support posts; 6 - diffuser; 7 - channel for sucking a gas flow from the external environment and supplying it into the liquid flow; 8 - direction of gas flow when flowing into the liquid flow from the cavitator; 9 - direction of gas flow through the windows between the support posts; 10 - direction of fluid flow in the confuser; 11 - direction of gas-liquid flow; 12 - convex arc; 13 - concave arc; 14 - cavitator body; 15 - stand; 16 - cavitating body; 17 - hole for suction of gas flow; 18 - common outlet of channels for sucking gas flow from the external environment and supplying it into the liquid flow; 19 - entrance edge of the rack; 20 - outer surface of the cavitating body; 21 - edge of the cavitating body; 22 - gas flow inside the annular liquid flow; 23 - annular fluid flow; 24 - external annular gas flow; 25 - inlet water flow; 26 - air flow inside the water flow; 27 - supercavity; 28 - annular flow of water; 29 - external air flow; 30 - tail region of the gas-liquid flow; 31 - external annular air flow; 32 - deflection of the annular water flow; 33 - receiving chamber; 34 - direction of liquid flow in the receiving chamber; 35 - gondola, 36 - tube; 37 - pointed edges; 38 - flat liquid flow; 39 - flat gas flow; 40 - channel for supplying technological additives, located in front of the channels for sucking a gas flow from the external environment and supplying it into the liquid flow; 41 - channel for supplying technological additives, located between the channels for sucking a gas flow from the external environment and supplying it inside the liquid flow; 42 - first feed stream of technological additives; 43 - second feed stream of technological additives; 44 - direction of supply of technological additives into the liquid flow; 45 - output edge of the rack; 46 - sector fluid flow; 47 - star-shaped gas flow; 48 - cavitator fairing; 49 - flexible tube; 50 - direction of gas suction through a flexible tube; 51 - end of a flexible tube brought into the liquid stream; 52 - direction of fluid flow at the entrance to the cavitator; 53 - fluid flow; 54 - gas flow in flexible tubes; 55 - turbine diffuser; 56 - turbine guide base; 57 - perforated turbine nozzle; 58 - turbine fairing; 59 - guide blades; 60 - holes of the perforated turbine nozzle; 61 - end exit of the perforated turbine nozzle; 62 - gas-liquid flow; 63 - trajectory of change in direction of gas-liquid flow in the turbine; 64 - turbine diffuser inlet; 65 - rounded concave profile of the turbine diffuser; 66 - diameter of the turbine diffuser outlet; 67 - concave profile of the turbine fairing; 68 - interblade channel; 69 - side surface of the guide blade; 70 - leading edge of the guide blade; 71 - cylindrical surface of the guide blade; 72 - entrance to the perforated turbine nozzle; 73 - slot of the perforated nozzle; 74 - guide tip; 75 - container with liquid; 76 - pump; 77 - first pipeline; 78 - device for creating a gas-liquid flow; 79 - second pipeline; 80 - turbine; 81 - volume of liquid; 82 - submersible box; 83 - suction pipeline; 84 - float platform.

IMPLEMENTATION OF THE INVENTION

Energy consumption in a device for creating a gas-liquid flow is determined by the fluid flow rate in it and the hydraulic resistance of the device, which is characterized by the device nozzle flow rate.

The claimed device for creating a gas-liquid flow does not operate in the steam cavitation mode, but in the gas supercavitation mode, which is carried out at lower liquid flow rates in the device. At the same time, the device nozzle flow coefficient is at least 0.9.

An increase in the amount of sucked gas in a device for creating a gas-liquid flow is achieved by improving the contact interaction between the liquid and gas flows.

The claimed device for creating a gas-liquid flow increases the amount of gas sucked into the liquid flow by improving the contact interaction of gas and liquid flows as a result of changing the shape of the contact surface between several gas and liquid flows in the direction of flow.

In fig. 9 shows a device for creating a gas-liquid flow, typical for the use of a liquid flow regime corresponding to steam cavitation. A device for creating a gas-liquid flow (for steam cavitation) contains a receiving chamber (33), which includes a liquid flow in direction (34), a confuser (1), a working chamber (3), a diffuser (6), a nacelle (35), and a tube (36), cavitator (2). The receiving chamber (33), nacelle (35), tube (36) and cavitator (2) have a channel (7) for sucking a gas flow from the external environment and supplying it into the liquid flow in direction (8).

Cavitator (2) in Fig. 9 is made in the form of a disk. As a rule, in such devices the cavitator is made in the form of a poorly streamlined body with sharp bends of the profile in the longitudinal section, which contributes to the formation of liquid vortices as it flows around it. A sharp drop in pressure in the vortices leads to boiling of the liquid and the formation of a cavity, an area of low pressure, located behind the cavitator along the flow. The suction of gas into the specified cavity occurs due to the pressure difference between the cavity and an external source of gas, from which gas flows into the internal channels of the apparatus.

The cavitation apparatus shown in FIG. 9 demonstrates a common approach to the design of devices of this type - the cavitator is installed in the flow by means of a support nacelle 38 located in the pipeline in front of the confuser 35, which leads to turbulence of the flow inside the confuser 35 and causes additional energy losses. The sucked gas passes through channels of greater length, the transverse dimensions of which are limited by the need to reduce the external dimensions of the nacelle 38 and tube 36 to reduce the hydraulic resistance of the entire structure. This increases the resistance to gas flow. These circumstances worsen the energy efficiency of the device.

The claimed device for creating a gas-liquid flow contains a nozzle connected in series and forming a single cylindrical body, consisting of a confuser (1) and a cavitator (2), a working chamber (3) and a diffuser (6), while the cavitator (2) has channels ( 7) to suck in a gas flow from the external environment and supply it into the liquid flow, while the nozzle is characterized by a flow coefficient of at least 0.9.

The main element of the device for creating a gas-liquid flow is its nozzle, installed at the entrance to the device and consisting of a confuser 1 and a cavitator 2. The design of the nozzle determines the energy intensity of the supercavitation apparatus. Its main characteristic is the flow coefficient u, the value of which depends on the hydraulic resistance of the nozzle flow channels. The proposed method of dissolving gas in liquid is implemented at values of μ≥0.9. To achieve such a value of the nozzle flow coefficient, the geometry of the confuser and cavitator must provide minimal resistance to fluid flow.

The confuser (1) serves to accelerate the flow of liquid, since its cross-sectional area decreases along the flow from the cross-sectional area at the entrance to the confuser (1) to the cross-sectional area of the cavitator flow part (2). Accelerating the flow of liquid leads to a decrease in pressure in it, which creates conditions for gas absorption. The longitudinal section profile of the inner surface of the confuser (1) is formed by a convex arc (12), the tangent to which at the entrance to the confuser (1) is parallel to the axis of the confuser (1), and a concave arc (13), the tangent to which at the exit of the confuser (1) is parallel confuser axis (1). Both arcs (12, 13) at the intersection point have a common tangent.

In the device for creating a gas-liquid flow, an ejector chamber (4) is additionally located between the diffuser (6) and the working chamber (3), at the beginning of which there are support posts (5) with windows for supplying gas along the outer surface of the liquid flow.

In accordance with the first embodiment of the invention, the cavitator (2) is made in the form of a cylindrical body (14), inside of which there is an axisymmetric cavitating body (16) and at least two posts (15) connecting the axisymmetric cavitating body (16) and the inner surface of the body (14) of the cavitator, while inside each rack (15) there is a channel (7) for sucking the gas flow from the external environment and supplying it inside the liquid flow, connected to the corresponding hole (17) for sucking the gas flow, located in the cylindrical body (14 ). The channels (7) on one side have holes (17) connecting the channels (7) with the external gas environment, for example, the atmosphere, and on the other side the channels (7) are united by a common outlet (18), through which the sucked gas enters the flow liquid in direction (8). The number of racks (15) can be more than two, provided that the cross-sectional area of the racks (15) in the plane of their greatest width is no more than 30% of the cross-sectional area of the body (14), calculated by its internal diameter. The inlet (19) and outlet edges (45) of the racks (15) are made pointed with a full angle of convergence of the edges of no more than 20°. The outer surface (20) of the axisymmetric cavitating body (16) has the shape of half an ellipsoid of revolution formed by rotating the ellipse around its long axis coinciding with the longitudinal axis of the cavitator (2), and the long axis of the ellipse is 2-2.5 times larger than its minor axis, which represents is the diameter of the axisymmetric cavitating body (16) in the plane of the edge of the cavitating body (21), the value of which is 0.5-0.7 of the internal diameter of the cavitator body (14) (2), and the ratio of the gas flow area (22) to the sum of the gas flow areas ( 22) and liquid (23) does not exceed 50% of the cross-sectional area of the working chamber (3). Thus, the design of the flow channels of the supercavitation apparatus creates conditions for the formation of a multilayer spatial flow, consisting of an internal gas flow 22 in the form of a supercavity, a surrounding ring-shaped liquid flow 23 and an external gas flow 24. A device for creating a gas-liquid flow, containing series-connected and forming a single cylindrical body nozzle consisting of a confuser (1) and a cavitator (2), containing an axisymmetric cavitating body (16), a working chamber (3), an ejector chamber (4) and a diffuser (6) creates conditions for the formation of a multilayer spatial flow - gas-liquid flow containing a gas flow (22) in the form of a supercavity inside an annular liquid flow (23), surrounding an annular liquid flow (23) and an outer annular gas flow (24), while the annular liquid flow (23) is located between the gas flows (22 , 24). The combined flow of these flows (22, 23, 24) is accompanied by wave-like deformations of the annular liquid flow (23), which improves the contact interaction between the liquid and gas flows (22, 23, 24) and increases the amount of sucked gas.

Improvement of the contact interaction of gas and liquid flows in the device according to the first embodiment is ensured by creating two coaxial gas flows inside and outside the annular liquid flow located between the gas flows, and the internal gas flow is a gas supercavity. At the same time, the movement of the annular liquid flow is accompanied by wave-like deformations of its shape in the direction of the flow, which improve the contact interaction of the flows and lead to an increase in the amount of sucked gas.

In accordance with the second embodiment of the invention, the cavitator (2) is made in the form of a cylindrical body (14), inside of which there is a cavitating body (16) in the form of at least two parallel plates installed at a distance from each other in the cross-sectional plane of the cylindrical body ( 14), while at the entrance to the cavitator (2) the plates are made pointed, and in each plate there is a channel (7) for sucking the gas flow from the external environment and supplying it into the liquid flow, connected to the corresponding hole (17) for sucking the gas flow , located in a cylindrical housing (14). A device for creating a gas-liquid flow (without an ejector chamber) contains a nozzle connected in series and forming a single cylindrical body, consisting of a confuser (1) and a cavitator (2), containing a cavitating body (16) in the form of at least two parallel plates mounted on distance from each other in the cross-sectional plane of the cylindrical body (14), the working chamber (3) and the diffuser (6) forms a multilayer gas-liquid flow consisting of flat liquid flows (38) and flat gas flows (39). More than two parallel plates of the cavitating body (16) can be installed in the cavitator (2). The width and number of parallel plates of the cavitating body (16) are selected so that the total area of flat gas flows (39) is no more than 50% of the total area of liquid (38) and gas flows (39). A multilayer gas-liquid flow is created using a cavitating body (16) in the form of the specified parallel plates when a liquid flow flows around them and gas is sucked through channels (7), while the specified parallel plates of the cavitating body (16) have a well-streamlined shape, and the inlet edges of the specified parallel The plates of the cavitating body (16), facing towards the fluid flow, are made with pointed edges (37) with a full angle of convergence of the edges (37) of no more than 20°. A device for creating a gas-liquid flow without an ejector chamber (4) has a length of the working chamber (3) that is 2-4 times greater than the diameter of the working chamber (2).

Improvement of the contact interaction of gas and liquid flows in the device according to the second embodiment is ensured by creating several plane-parallel flows of gas and liquid, the movement of which is accompanied by an inversion change in the shape of the contact surface of the gas and liquid in the direction of the flow.

In accordance with the third embodiment of the invention, in the plates of the acquitting body (16) of the cavitator (2) there is at least one additional channel (41) located between the channels (7) for sucking the gas flow from the external environment and supplying it into the liquid flow, and at least one additional channel (40) located in front of the specified channels (7) for suction of the gas flow, while the specified additional channels (40, 41) are connected to each other and are configured to supply technological additives into the liquid flow. Through the indicated channels (40, 41) the first (42) and second (43) flows of technological additives are supplied into the liquid flow, and the direction of supply of technological additives into the liquid flow coincides with the direction of the gas flow when flowing into the liquid flow from the cavitator (2).

In accordance with the fourth embodiment of the invention, the cavitator (2) is made in the form of a cylindrical body (14), inside of which there is a handshake body (16) in the form of at least two diametrically intersecting plates, while at the entrance to the cavitator (2) the plates are made pointed , and in each plate there is a channel (7) for sucking the gas flow from the external environment and supplying it inside the liquid flow, connected to the corresponding hole (17) for sucking the gas flow, located in the cylindrical body (14). A device for creating a gas-liquid flow (without an ejector chamber) with a cavitator (2) containing a handshake body (16) in the form of at least two diametrically intersecting plates forms a multilayer gas-liquid flow consisting of sector liquid flows (46) and a star-shaped gas flow ( 47). More than two diametrically intersecting plates can be installed in the cavitator (2). The width and number of diametrically intersecting plates are selected so that the area of the gas flow (47) is no more than 50% of the total area of the liquid (46) and gas flows (47). A multilayer gas-liquid flow is created using a cavitating body (16) in the form of the specified diametrically intersecting plates when they flow around them with a liquid flow and gas suction through the channels (7), while the specified diametrically intersecting plates of the cavitating body (16) have a well-streamlined shape, and the inlet edge the indicated parallel plates of the cavitating body (16), facing the liquid flow, are made with pointed edges (37) with a full angle of convergence of the edges (37) of no more than 20°.

Improving the contact interaction of gas and liquid flows in the device according to the fourth embodiment is ensured by creating several sectoral liquid flows separated by a star-shaped gas flow, the movement of which is accompanied by an inversion change in the shape of the gas-liquid contact surface in the direction of the flow.

In accordance with the fifth embodiment of the invention, the cavitator (2) is made in the form of a cylindrical body (14), inside of which there is a cavitating body (16) in the form of at least two diametrically non-intersecting fairings (48), made with a pointed leading edge facing the flow , with a full angle of convergence of the faces (37) no more than 20°. In this case, flexible tubes (49) with channels (7) are installed inside the fairings (48) for sucking the gas flow from the external environment and supplying it inside the liquid flow, one end of which is brought out into the liquid flow, and the other is fixed in the corresponding hole (17) for suction gas flow located in a cylindrical housing (14). The liquid flow enters the cavitator in the direction (52); when flowing in the area of the fairings (48) and flexible tubes (49), a decrease in pressure occurs due to a local decrease in the open cross-section of the liquid flow and a corresponding increase in its speed. As a result of the formation of a pressure difference between the external environment and the liquid flow inside the cavitator (2), gas is suctioned through flexible tubes (49) in the direction (50) of gas suction, which enters the liquid flow in the form of separate gas jets. Under the influence of a turbulent flow, the flexible tubes (49) begin to move relative to their axis and their outlet section (51) performs unsteady oscillatory movements, as a result of which the gas jets flowing from the tubes acquire a trajectory of motion that is different from a straight line, resulting in a change in the shape of the contact surface gas and liquid flows. Thus, the use of flexible tubes (49) supplying gas to the liquid flow increases the amount of gas drawn in. More than two fairings (48) can be installed in the cavitator (2). The diameter of the flexible tubes (49) should not exceed the transverse size of the fairings (48), so as not to increase the hydraulic resistance of the cavitator (2). The width and number of fairings (48) are selected based on the fact that the total area of gas flows (54) in flexible tubes should not exceed 50% of the total area of liquid (53) and gas flows (54). Flexible tubes (49) of different diameters can be used as part of one cavitator (2).

In accordance with the sixth embodiment of the invention, the cavitator (2) is made in the form of a cylindrical body (14), inside of which there is a cavitating body (16) in the form of at least two parallel fairings (48), with flexible tubes installed inside the fairings (48). (49) with channels (7) for sucking a gas flow from the external environment and supplying it inside the liquid flow, one end of which is brought into the liquid flow, and the other is fixed in the corresponding hole (17) for sucking the gas flow, located in a cylindrical body (14 ). A device for creating a gas-liquid flow (without an ejector chamber) with a cavitator (2) containing a handshaking body (16) in the form of three parallel fairings (48) forms a gas-liquid flow in the form of gas flows (54), between which there is a liquid flow (53).

Improving the contact interaction of gas and liquid flows in the device according to the fifth and sixth embodiments is ensured by creating several gas flows flowing into the liquid through flexible tubes, and the area of inflow of gas flows into the liquid flow changes its position under the action of the liquid flow, which is accompanied by a change shapes of the contact surface of gas and liquid flows in the direction of flow.

In fig. Figure 11 presents data on the efficiency of gas suction using various designs of the claimed cavitator, disclosed on graphs of the dependence of air ejection coefficients on water flow rate, obtained on an experimental stand: a - design of the cavitator according to Fig. 9; b - cavitator design according to Fig. 10; c - cavitator design according to Fig. 1; d - cavitator design according to Fig. 12; e - cavitator design according to Fig. 16; f - cavitator design according to Fig. 20. As can be seen from FIG. 11, the claimed device for creating a gas-liquid flow in all its embodiments has a higher ejection coefficient than a cavitation device known from the prior art.

A system for dissolving a gas in a liquid contains a series-connected liquid supply unit in the form of a pump (76), at least one device (78) for creating a gas-liquid flow located above the surface of the liquid volume (81) in which the gas is dissolved, and at least one turbine (80) located in the bottom region of the liquid volume (81) and containing a turbine diffuser (55), a guide base (56) configured to change the direction of the gas-liquid flow along the trajectory (63) and perforated nozzles (57) located in plane perpendicular to the axis of the diffuser (55) of the turbine, wherein the liquid supply unit (76) and the device (78) for creating a gas-liquid flow are connected to each other using a first pipeline (77), and the device (78) for creating a gas-liquid flow and the turbine (80) are connected to each other using a second pipeline (79).

Dissolution of the gas is carried out in a stationary volume of liquid (81), for example, in a container (75), or in a moving volume of liquid (81), for example, in a river.

The guide base (56) contains a centrally located turbine fairing (58) and guide vanes (59) arranged radially around the turbine fairing (58).

The perforated nozzles (57) are made in the form of a rectangular tube.

The perforated nozzles (57) are made in the form of a round tube.

At least one perforated nozzle (57) contains a guide tip (74) bent in a vertical plane.

At least one perforated nozzle (57) contains a guide tip (74) bent in a horizontal plane.

The perforation is made in the form of a slot (73) or in the form of round, triangular, square, rectangular and polygonal holes.

For a perforated nozzle (57) in the form of a rectangular tube, the perforation is made on the vertical or horizontal surface of the nozzle (57).

For a perforated nozzle (57) in the form of a rectangular tube, perforation is made on the vertical surface of the perforated nozzle (57) in the form of a slot (73) with an inclination from the lower horizontal surface at the entrance to the perforated nozzle (57) to the upper horizontal surface at the exit of the perforated nozzle ( 57).

The liquid supply unit is made in the form of a pump (76) fixed outside or inside a stationary volume of liquid (81).

The liquid supply unit is made in the form of a pump (76) fixed outside or inside the moving volume of liquid (81).

The fluid supply unit is made in the form of a pump (76) installed on a float platform (84).

The claimed method for dissolving a gas in a liquid using a claimed system for dissolving a gas (air) in a liquid (water) containing a device for creating a gas-liquid flow in accordance with the first embodiment of the invention, containing a cavitator (2) according to the first embodiment of the invention, is carried out as follows .

At the first stage, water located in the container (75), using a pump (76), is supplied through the first pipeline (77) to the device (78) to create a gas-liquid flow located above the liquid level (81) in the container (75). Water through the confuser (1) in direction (10) enters the cavitator (2). The water flow (25) flows around the cavitating body 16 shown in FIG. 4, and as a result of a local decrease in pressure in the water flow (25), air is sucked in and an air flow (26) is formed inside the annular water flow (28) in the form of a supercavity (27) filled with air. The supercavity (27) is surrounded by an annular flow of water (28). Next, the air flow (26), surrounded by an annular flow of water (28), enters the space between the working chamber (3) and the ejector chamber (4), where air is sucked through the windows of the support column (5) and an external air flow (29) is formed. . When the gas-liquid flow exits from the supercavity (27) from the ejector chamber (3) in the direction (11) of the gas-liquid flow, the supercavity decreases in transverse size in the tail region (30) of the gas-liquid flow, and the outer annular air flow (31) increases in area, as a result a deflection (32) of the annular water flow (28) is formed, which moves in the direction of the flow, resulting in periodic wave-like deformations of the water flow (28). These deformations enhance the contact interaction of water and air flows. The generated gas-liquid flow from the diffuser (6) of the device (78) for creating a gas-liquid flow in the vertical direction through the second pipeline (79) enters the turbine (80) located in the bottom region of the liquid volume (81). The gas-liquid flow (62) from the second pipeline (79) enters the turbine diffuser (55) in a vertical direction, containing an inlet (64) and a rounded concave profile (65). In the diffuser (55) of the turbine, the speed of the gas-liquid flow (62) decreases, which enters the guide base (56) of the turbine and changes the flow direction by 90° along the trajectory (63), the smoothness of this change in direction is ensured by the fairing (58) of the turbine. The guide vanes (59) distribute the gas-liquid flow (62) through the perforated nozzles (57). Next, the gas-liquid flow (62) exits from the perforated nozzles (57) into the surrounding volume of liquid (81) through rectangular perforated holes (60) made on the perforated nozzles (57) and through the end outlet 61. When the gas-liquid flow flows out of the perforated nozzles ( 57) the gas is dispersed and distributed in the plane of the bottom of the volume of liquid in which the gas is dissolved.

The energy consumption in the device for creating a gas-liquid flow depends on the value of the back pressure at the outlet of the device. The higher the back pressure, the higher the fluid flow rate must be to transfer gas from the suction zone to the high pressure area downstream at the outlet of the device, and the higher the energy required to operate the device.

In the claimed method of dissolving a gas in a liquid, reducing the back pressure at the outlet of the device for creating a gas-liquid flow is achieved by installing it vertically above the surface of the liquid. In this case, in the pipeline section between the device for creating a gas-liquid flow and the turbine located above the surface of the liquid, negative hydrostatic pressure is created, which reduces the back pressure at the outlet of the device for creating a gas-liquid flow.

To increase the amount of gas dissolved in a liquid, it is necessary to disperse the gas and distribute it throughout the volume of the liquid so as to avoid the merging of small gas bubbles into large ones, as a result of which the mass transfer surface decreases.

In the claimed method of dissolving gas in a liquid, an increase in the amount of gas dissolved in the liquid is provided by perforated turbine nozzles by dispersing the gas as part of the gas-liquid flows flowing into the volume of the liquid and the spatial distribution of the gas in the plane of its bottom.

The system was tested using the following method:

when the aeration system is turned off, a sodium bisulfite-based reagent is added to the water in the aeration tank (a container filled with water), which binds oxygen dissolved in the water;

during the process of mixing water, the concentration of dissolved oxygen is measured using instruments whose sensors are installed in the aeration tank at different depths;

when the dissolved oxygen concentration reaches low values (≤1-2 mg/l), the hydraulic pump of the aeration system is switched on to a water flow rate of 100 m ³ /h and air suction into the supercavitation apparatus begins;

the water in the aeration tank is continuously aerated and the concentration of dissolved oxygen in the water is simultaneously measured until an oxygen concentration close to saturated at a given water temperature is achieved;

Using the results of measurements of oxygen concentrations in water, standard (calculated to a water temperature of 20°C) indicators of the efficiency of oxygen dissolution during aeration are determined: standard oxygen transfer efficiency SOTE, standard oxygen transfer rate SOTR, standard aeration energy efficiency SAE.

The system used a device for creating a gas-liquid flow (without an ejector chamber) with a cavitator, disclosed in Fig. 12, in which the cavitator creates plane-parallel flows of liquid and gas. The nozzle consumption coefficient of the supercavitation apparatus is μ=0.96.

The tests were carried out in an aeration tank with a water volume of 54.8 m ³ at a water depth H _WT = 4.5 m. At a water flow rate Q _W = 100 m ³ / h, the air ejection coefficients were η = 0.5 and η = 0.6 at the installation height of the device for creating a gas-liquid flow above the water surface H _WTA =0.5 m and H _WTA =1.0 m, respectively. The outside air temperature during the tests was in the range T _A = 18.6-20.2 ° C, the water temperature was in the range T _W = 16.5-17.0 ° C.

Determination of the kinetics of oxygen dissolution in water is carried out using the volumetric mass transfer coefficient k _L a.

The change in oxygen concentration in water depending on time is described by the equation:

where C is the concentration of oxygen in water, mg/l; C _∞ - steady-state oxygen concentration in water, mg/l; t - time, s; k _L a - mass transfer coefficient, s ^-1 .

By integrating the equation within C=C ₀ at time t=0 and C=C _t at time t=t _t , k _L a can be determined from the slope of a semi-logarithmic graph of the concentration difference (C _∞ -C) versus water aeration time t. Thus, the mass transfer coefficient k _L a will be determined as:

The dependence graph (C _∞ -C)=f(t) is approximated by the exponential regression equation y=A⋅exp(-B⋅x), in which A=C _∞ , B=k _L a. These data are used to calculate the OTR oxygen transfer rate:

OTR=k _L a⋅C _∞ ⋅V _w

where V _w is the volume of water in the aeration tank.

Aeration efficiency AE is determined by the formula:

AE=OTR/N _P

where N _P is the power consumption of the hydraulic pump.

OTE oxygen transfer efficiency is calculated using the formula:

OTE=OTR/M _O2

where M _O2 is the mass flow of oxygen during aeration.

To determine aeration efficiency indicators under standard conditions (T=20°C, P=101325 Pa), the mass transfer coefficient k _L a and the steady-state oxygen concentration C _∞ are recalculated to standard conditions.

k _L a ₂₀ =k _L a⋅Θ ^(20-T)

where Θ is the temperature correction coefficient (=1.024); T - water temperature.

where t is the temperature correction coefficient; Ω - pressure correction coefficient.

where C _ST and C _S20 are the saturated oxygen concentrations in water at actual P _b and standard P _s barometric pressure.

The rate of oxygen transfer under standard conditions is calculated by the formula:

SOTR=k _L a ₂₀ ⋅C _∞20 ⋅V _w

The efficiency of aeration under standard conditions is determined by the formula:

SAE=SOTR/N _P

The efficiency of oxygen transfer under standard conditions is calculated by the formula:

SOTE=SOTR/M _SO2

where M _SO2 is the mass flow rate of oxygen during aeration, calculated from the properties of air and oxygen under standard conditions.

For the option of installing a device for creating a gas-liquid flow above the water surface at a height of 0.5 m, the aeration indicators were OTE = 55% (SOTE = 57%), OTR = 7.7 kgO ₂ / h (SOTR = 8.0 kgO ₂ / h), AE = 4.3 kgO ₂ /kWh (SAE=4.5 kgO ₂ /kWh).

For the option of installing a device for creating a gas-liquid flow above the water surface at a height of 1.0 m, the aeration indicators were OTE = 59% (SOTE = 62%), OTR = 9.9 kgO ₂ / h (SOTR = 10.3 kgO ₂ / h), AE = 5.0 kgO ₂ /kWh (SAE=5.3 kgO ₂ /kWh).

Based on the test results, a computational model of the process of dissolving oxygen in water using the proposed method has been developed. The calculation results are presented in Table 1.

The invention has been described above with reference to a specific embodiment thereof. Other embodiments of the invention may be obvious to those skilled in the art but do not change its essence as disclosed in the present description. Accordingly, the invention should be considered limited in scope only by the following claims.

Claims (27)

1. A device for creating a gas-liquid flow, containing a nozzle connected in series and forming a single cylindrical body, consisting of a confuser and a cavitator, a working chamber, an ejector chamber, at the beginning of which there are support posts with windows for supplying gas along the outer surface of the liquid flow, and a diffuser , while in the cavitator there are channels for sucking a gas flow from the external environment and supplying it into the liquid flow, and the nozzle is designed to create a gas-liquid flow and is characterized by a flow coefficient of at least 0.9. 2. The device according to any one of paragraphs. 1 or 2, characterized in that the cavitator is made in the form of a cylindrical body, inside of which there is an axisymmetric cavitating body and at least two racks connecting the axisymmetric cavitating body and the inner surface of the cavitator body, while inside each rack there is a channel for suction of the gas flow from external environment and feeding it into the liquid flow, connected to a corresponding suction hole for the gas flow, located in the cylindrical body. 3. Device according to any one of paragraphs. 1 or 2, characterized in that the cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two parallel plates installed at a distance from each other in the cross-sectional plane of the cylindrical body, while at the entrance to the cavitator the plates are made pointed, and in each plate there is a channel for sucking a gas flow from the external environment and supplying it into the liquid flow, connected to a corresponding hole for sucking the gas flow located in the cylindrical body. 4. The device according to claim 3, characterized in that the cavitating body has at least one additional channel located between the channels for sucking a gas flow from the external environment and supplying it inside the liquid flow, and at least one additional channel located in front of the specified channels for suction of the gas flow, while the specified additional channels are connected to each other and are configured to supply technological additives into the liquid stream. 5. Device according to any one of paragraphs. 1 or 2, characterized in that the cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two diametrically intersecting plates, while at the entrance to the cavitator the plates are made pointed, and in each plate there is a channel for suction of the gas flow from the external environment and feeding it into the liquid flow, connected to a corresponding suction hole for the gas flow, located in the cylindrical body. 6. Device according to any one of paragraphs. 1 or 2, characterized in that the cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two diametrically non-intersecting fairings, while flexible tubes with channels are installed inside the fairings for sucking the gas flow from the external environment and supplying it inside liquid flow, one end of which is discharged into the liquid flow, and the other is fixed in the corresponding hole for suction of the gas flow, located in the cylindrical body. 7. Device according to any one of paragraphs. 1 or 2, characterized in that the cavitator is made in the form of a cylindrical body, inside of which there is a cavitating body in the form of at least two parallel fairings, while flexible tubes with channels are installed inside the fairings for sucking the gas flow from the external environment and supplying it inside the flow , one end of which is brought out into the liquid flow, and the other is fixed in the corresponding hole for suction of the gas flow, located in the cylindrical body. 8. A method for dissolving a gas in a liquid using a device according to any one of claims. 1-7, including the following steps: a) forming a gas-liquid flow above the surface of the liquid, consisting of at least two gas flows and at least one liquid flow located between the gas flows, using a device for creating a gas-liquid flow; b) supplying a gas-liquid flow to the bottom region of the liquid in the vertical direction; c) dispersion of gas as part of a two-phase flow and distribution of gas in the volume of liquid; d) dissolution of gas in a volume of liquid. 9. The method according to claim 8, characterized in that the gas is dissolved in a stationary volume of liquid or in a moving volume of liquid. 10. The method according to claim 8, characterized in that additionally, when forming a gas-liquid flow, technological additives are introduced into the liquid flow. 11. A system for dissolving gas in liquid, containing a liquid supply unit connected in series, at least one device for creating a gas-liquid flow according to any one of claims. 1-7, located above the surface of the liquid volume in which the gas is dissolved, and at least one turbine located in the bottom region of the liquid volume and containing a diffuser, a guide base configured to change the direction of the gas-liquid flow, and perforated nozzles located in the plane , perpendicular to the axis of the turbine diffuser, wherein the liquid supply unit and the device for creating a gas-liquid flow are connected to each other using a first pipeline, and the device for creating a gas-liquid flow and the turbine are connected to each other using a second pipeline. 12. The system according to claim 11, characterized in that the gas is dissolved in a stationary volume of liquid or in a moving volume of liquid. 13. The system according to claim 11, wherein the guide base comprises a centrally located turbine fairing and guide vanes arranged radially around the turbine fairing. 14. The system according to claim 11, characterized in that the perforated nozzles are made in the form of a rectangular tube. 15. The system according to claim 11, characterized in that the perforated nozzles are made in the form of a round tube. 16. The system according to claim 11, characterized in that at least one perforated nozzle contains a guide tip bent in a vertical plane. 17. The system according to claim 11, characterized in that at least one perforated nozzle contains a guide tip bent in a horizontal plane. 18. The system according to any one of paragraphs. 14 or 15, characterized in that the perforation is made in the form of a slot or in the form of round, triangular, square, rectangular and polygonal holes. 19. The system according to claim 14, characterized in that the perforation is made on a vertical or horizontal surface of the perforated nozzle. 20. The system according to claim 14, characterized in that the perforation is made on the vertical surface of the perforated nozzle in the form of a slot with an inclination from the lower horizontal surface at the entrance to the perforated nozzle to the upper horizontal surface at the exit of the perforated nozzle. 21. The system according to claim 11, characterized in that the liquid supply unit is made in the form of a pump mounted outside or inside a stationary volume of liquid. 22. The system according to claim 11, characterized in that the liquid supply unit is made in the form of a pump mounted outside or inside the moving volume of liquid. 23. The system according to claim 11, characterized in that the liquid supply unit is made in the form of a pump installed on a float platform.