Method and plant for producing water vapor and distillate

Abstract

The inventions relate to the field of thermal power engineering. A plant and method for producing water vapour and distillate from cavitated aqueous solutions and suspensions is characterized in that a stream of a cavitated liquid is injected into the plant using a hydraulic feed pump, and a pneumohydraulic disperser is used to generate in said stream a dispersion of gas bubbles which absorb cavitational vapour-gas microbubbles. The resulting gas-filled liquid mixture is fed fountain fashion into an air space of a hyperbaric fountain chamber, where the dispersed bubbles separating from the fountain flow form a vapour-gas phase. The accumulated liquid phase is subjected to sparging, increasing the pressure in the air space of the hyperbaric fountain chamber to a level sufficient to suppress excessive foaming, as well as to force the vapour-gas phase out of the hyperbaric fountain chamber into a condensation zone and to force the spent cavitated liquid mixture into an external pipeline. Liquid is fed into the hydraulic feed pump from a pipeline mounted in the lower part of the fountain chamber, downstream of a flow regulator, or from a source of liquid. The result of the invention is the extraction of high-temperature cavitational microbubbles from the cavitated liquid.

Description

[0001] METHOD AND DEVICE FOR PRODUCING WATER VAPOR AND DISTILLATE

[0002] Field of technology

[0003] The invention relates to the field of cavitation technology and engineering and is intended for the production of water vapor and distillate from polluted waters, using cavitation as the main source of energy, for obtaining drinking water and concentrating impurities, as well as for reducing the destructive effect of cavitation on elements of production equipment when using cavitation modules as anti-cavitation valves.

[0004] State of the art

[0005] At present, practically everywhere, the consumption of water from natural sources, even artesian, without additional treatment and controlled quality is dangerous to human health. In emergency situations of natural and man-made nature, the problem is aggravated by the fact that the most common technologies do not allow producing drinking water due to the high pollution of nearby water sources.

[0006] To obtain high-quality drinking water, the most common technologies are based on distillation of the original liquid, which is then mineralized and disinfected to give the water beneficial properties and a familiar taste.

[0007] In particular, the reverse osmosis method is, in fact, distillation using reverse osmosis membranes. But to purify water using membranes, it is necessary to ensure that strict requirements are met for the composition, concentration and chemical activity of dissolved substances, with the indispensable condition of preliminary purification of the initial liquid from coarse impurities and microparticles. This circumstance makes it practically impossible to use membrane methods to obtain drinking water directly from polluted waters.

[0008] The thermal method is the production of distillate by evaporation of the initial water, brought to a boiling state in various evaporation units by various methods. In this case, more than 15% (about 415 kJ / kg) of energy is spent on heating the main mass of water, and about 85% (about 2260 kJ / kg) directly on evaporation. The disadvantage of the thermal method is that heating water to boiling can cause physical and chemical changes in the properties of impurities, including the formation of scale, as well as chemical action of the components of the separated liquid on the elements of the evaporation unit equipment. This necessitates the use of corrosion-resistant materials.

[0009] In addition to the high requirements for the quality of preliminary water treatment, the disadvantage of reverse osmosis and thermal technologies for obtaining high-quality drinking water is the high requirements for personnel ensuring the operation and maintenance of expensive and complex production equipment.

[0010] One of the promising methods of obtaining drinking water, which allows to significantly reduce the requirements for the quality of preliminary water treatment, is based on the use of cavitation energy for evaporation of water. The term cavitation refers to the process of formation of microvoids in a liquid, filled with molecules of dissolved and dispersed gases, forming gas-filled microbubbles, which explosively collapse with the release of energy, which is accompanied by heating of the liquid. The results of numerous studies, among the primary sources of which are [1, 2, 3], indicate that under the influence of various natural and man-made factors, local tensile stresses arise in the volume of a liquid medium and microvoids are formed.Molecules of dissolved foreign gases, chaotically moving in the volume of liquid, can fill a nearby microcavity, preventing it from closing, and, forming a surface of separation between the gas phase and liquid, form cavitation nuclei, the enlargement of which causes cavitation microbubbles. Molecules in a gas microbubble and in nearby liquid layers continuously migrate in both directions through the boundary of separation between the gas and liquid phases, overcoming surface tension, and perform work against uncompensated intermolecular forces. This is repeated many times by many molecules, which leads to the release of thermal energy, an increase in temperature and pressure inside the microbubble and in nearby liquid layers, causing oscillations of the surface and center of gravity, due to which the microbubble increases in size, and then acquires an elliptical shape and bursts.The sizes of cavitation microbubbles reach 100 microns, and during explosive collapse, cumulative jets with speeds of 400-800 m / s are formed in them, local pressure up to 100 MPa develops and the temperature increases from several tens to 1000°C and more. The heat released during the collapse of bubbles increases the temperature of the liquid, activates vaporization and causes boiling, during which the concentration of dissolved gases decreases and, accordingly, the efficiency of cavitation heating decreases. At high concentrations, cavitation microbubbles have a destructive effect on the surfaces of materials with which they come into contact.

[0011] Non-patent documents:

[0012] [1] - I. Metter, “The Physical Nature of Cavitation and the Mechanism of Cavitation Damage,” journal “Advances in Physical Sciences,” 1948, v. XXXV, issue I.

[0013] [2] - Suslick, K. S., ed., Ultrasound, Its Chemical, Physical, and Biological Effects, VCH, NY, 1988.

[0014] - Kenneth S. Suslik, "Chemical effects of ultrasound". J. "In the World of Science", No. 4, 1989, pp. 54-61.

[0015] [3] - Katoh, New Edition Cavitation: Basics and Recent Advance, Written and Edited by Yoji Katoh, Published by Makishoten, 1999.

[0016] Prior art known from patent documentation.

[0017] Known is patent RU 2633725 C1 "Method and device for producing steam" from a two-phase steam-water superheated rotating hydrodynamic medium of low density by feeding liquid without preliminary heating with a metered flow rate under excess pressure, providing superheating of the medium above 100°C, into the peripheral part of the working cavity of a hydrodynamic steam generator in the cavitation zone. The resulting steam is taken from the low-pressure zone in the central part of the working cavity when the medium is heated to a temperature at which the steam pressure exceeds the centrifugal force acting on the rotating liquid flow. Steam is taken at a specified pressure depending on the required parameters of the steam output and the liquid supply is resumed when the pressure in the steam generator cavity decreases below the liquid supply pressure.

[0018] Known patent RU 52976 U1, utility model "Rotary cavitation steam generator" for generating steam in one pass of water from any initial temperature without its preliminary heating and chemical water treatment while improving the quality of the resulting steam due to the guaranteed separation of the coolant into a liquid and vapor phase. The difference of the proposed solution is that water is supplied under pressure directly to the working area of ​​the device, which is formed due to the guaranteed radial and axial gap between the disk and the stator. Water entering the rotating disk, by analogy with a centrifugal pump, is thrown towards the peripheral part of the disk and balances the pressure of the incoming water flow. Thus, the water is "locked" in a narrow gap between the rotor and the stator. Due to the effect of friction forces, cavitation, etc. on the water, it begins to heat up intensively and boils.The resulting steam under pressure enters the outlet cone of the device, located in the central part of the disk. In this case, even the smallest drops of moisture or condensate present in the steam are thrown by the rotating disk to the periphery into the gap between the rotor and the stator for subsequent heating. This ensures a stable boundary between the liquid and vapor phases, internal separation of moisture and the production of "dry steam". The task of increasing efficiency is solved by ensuring a stable, unregulated cavitation process in the device in all operating modes.

[0019] The technical parameters of steam and the productivity of the device are determined in wide limits by the pressure and dosage of water at the device inlet and the power of the drive motor. The patent RU 2759460 Cl "Method of steam production" is known, which includes feeding a magnetized liquid into the working cavity of a cavitation steam generator, forming a high-speed flow of rotating liquid, heating the liquid in the working cavity of the steam generator, creating a two-phase steam-water medium in the working cavity of the steam generator and steam extraction. The pressure of the steam-water mixture at the outlet of the steam generator is regulated by reducing or increasing the supply of liquid to the inlet of the steam generator. In this case, the steam output unit contains a steam control valve installed directly near the lance, while the lance is equipped with a heat-insulated flexible steam pipe and a flexible nozzle.

[0020] The common features of the listed and similar technical solutions are:

[0021] - increasing the temperature of the main mass of the liquid phase to values ​​exceeding the boiling point of water;

[0022] - creation of a two-phase steam-water environment in the working cavity of the steam generator;

[0023] - steam extraction directly from the steam generator body;

[0024] - the need to use heat-resistant and corrosion-resistant structural materials.

[0025] The common disadvantages of the listed and similar technical solutions are:

[0026] 1. High level of requirements for the composition, concentration and chemical activity of dissolved substances, as well as for the content of coarse impurities and microparticles in the source liquid, which cause fouling and blockage of the internal surfaces of water-conducting channels as a result of:

[0027] - small cross-section of the structural elements required to initiate cavitation, which are clogged with insoluble components of the contaminated liquid; - high risks of destruction of individual structural elements of the equipment under the influence of high temperatures due to the combination of the stages of formation, growth and collapse of cavitation microbubbles in the volume of the cavitating device.

[0028] 2. A decrease in the energy efficiency of the cavitation device due to the suppression of the cavitation process when the temperature of the main mass of the liquid phase increases to values ​​close to the boiling point of water.

[0029] 3. Reduction in the service life of device elements that come into contact with cavitation gas microbubbles.

[0030] Known patent RU 2530106 C2 "Device for wastewater treatment" consists of a first preliminary treatment unit containing a settling tank and a filter; a second coagulation-flotation unit containing a high-pressure centrifugal pump, a hydrodynamic cavitator, a coagulant supply tank, a flotation coagulator; and a third unit for post-treatment and disinfection using cavitation and several chemical components, containing a filter, an ultraviolet irradiation unit with an ultrasonic emitter, and an ejector with a throttle washer for collecting a water flow. As follows from the description, the hydrodynamic cavitators in the second and third units of the device act as homogenizers for mixing additional components with the flow of the liquid being purified. The device is intended for wastewater treatment and obtaining clean water by separating impurities during liquid circulation in a closed circuit.

[0031] The disadvantages of the device include:

[0032] - use of chemicals for coagulation of impurities;

[0033] - discharge of sludge containing coagulants into the environment;

[0034] - there are no devices for separating water vapor and distillate formed in cavitators from the initial liquid and removing it. The patent RU No. 64200 U1, utility model "Distiller" was selected as a prototype, as the closest in technical essence and achievable technical result to the claimed technical solution, in which a rotary pulse unit supplies and cavitational heats the initial cold liquid entering for desalination into an evaporator with a heat exchanger, a separator for separating steam and a distillate collection system. In this case, the residual (absolute) pressure in the distillate collection system is no more than 0.04 MPa, the temperature of the liquid entering the inlet pipes of the evaporator heat exchanger is not less than the boiling point of the liquid at a given pressure (for water, not less than 76 °C).

[0035] The disadvantages of the prototype's technical solution are:

[0036] - the cost of cavitation energy for heating the initial liquid to the boiling point and above;

[0037] - additional energy consumption of the drive device of the rotary pulse unit for heating the liquid due to an increase in the heating duration, as a result of the suppression of the intensity of the formation of cavitation microbubbles when the temperature of the main mass of the liquid phase increases to values ​​close to the boiling point of water;

[0038] - the need to use heat-resistant and corrosion-resistant structural materials with which cavitation microbubbles come into contact in order to reduce the level of destructive effects of cavitation.

[0039] Disclosure of invention

[0040] The technical problems that the claimed invention is aimed at solving are:

[0041] - reduction of cavitation energy losses for heating the main mass of liquid during the separation of the vapor-gas phase; - reduction of the level of requirements for the content of coarse impurities and microparticles in the initial liquid, for the composition, concentration and chemical activity of dissolved substances; prevention of the destructive effect of the increased temperature of cavitation microbubbles on the elements of the device with which the cavitation gas microbubbles come into contact.

[0042] The technical result of the claimed solution is the extraction of high-temperature cavitation microbubbles from cavitated liquid, due to the dispersion of gas from the external environment under excess pressure into the flow of pre-cavitated liquid phase and the merging and absorption of dispersed gas bubbles with cavitation vapor-gas microbubbles, before their collapse occurs and the released thermal energy causes heating of the main mass of contaminated water, and the resulting flow of gas-filled liquid is subjected to degassing by fountaining and bubbling methods.

[0043] The technical result of the claimed technical solution is achieved by the fact that a method is proposed for obtaining water vapor and distillate from cavitated aqueous solutions and suspensions, including the creation of a dispersion of gas bubbles in a flow of cavitated liquid pumped into the installation by means of a feed hydraulic pump, using a pneumohydraulic disperser, feeding the resulting gas-filled liquid mixture by a fountain, with a jet length of at least 0.1 m, into the air space of a hyperbaric fountain chamber, where the dispersed bubbles released from the fountaining jet form a vapor-gas phase, and the accumulating liquid phase is subjected to bubbling, removing the residual amount of dispersed bubbles from the liquid, increasing the pressure in the air space of the hyperbaric fountain chamber to a level sufficient to suppress excess foaming, squeezing out the vapor-gas phase from the hyperbaric fountain chamber into the condensation zone,and squeezing out the spent cavitated liquid mixture into an external pipeline, while the supply of liquid to the feed hydraulic pump is carried out from a pipeline installed in the lower part of the hyperbaric fountain chamber after the flow regulator, or from a liquid source.

[0044] Also proposed is a plant for producing water vapor and distillate from cavitated aqueous solutions and suspensions, consisting of a feed hydraulic pump with a tubular distribution manifold connected by a pipeline to a cavitation unit including a hydrodynamic pump combined with a cavitator, connected to a feed manifold, which is connected to an evaporation unit including a hyperbaric fountain chamber with a bubbling device, a unit for condensing a vapor-gas mixture, a gas compression unit and a pneumohydraulic disperser connected to the feed manifold, wherein the hyperbaric fountain chamber contains an inclined upper part and a vertical lower part, in which a liquid flow regulator is installed, a bubbling device connected to a gas compression unit connected to a pneumohydraulic disperser, a pressure valve is located in the upper part of the fountain chamber,connected to a unit for condensing a steam-gas mixture, equipped with a pipeline for removing distillate, the gas compression unit is designed with the possibility of feeding gas into a pneumohydraulic disperser.

[0045] In preferred embodiments, it is possible that: the lower part of the fountain chamber contains a hydro turbine of the power plant installed on the pipeline after the liquid flow regulator; the feed hydraulic pump is designed and installed with the possibility of taking liquid from the source; the pipeline after the liquid flow regulator is connected to the intake of the feed hydraulic pump; a hatch is located in the upper part of the fountain chamber; the installation contains 2 or more parallel-installed cavitation units;the installation contains several sequentially connected installations, wherein the first feed hydraulic pump is designed with the possibility of drawing liquid from a source, the installations are connected by means of a pipeline connecting the second and more hydraulic pumps with the lower part of the fountain chamber of the previous installation, the pressure valves of the installations are sequentially connected to a common manifold of the steam-gas mixture, at least one unit for condensing the steam-gas mixture, a gas compression unit.

[0046] The combination of the above essential features results in the following opportunities being provided:

[0047] - to obtain a steam-gas mixture and distillate for the production of drinking water from contaminated water in foundationless, mobile, easily assembled non-membrane type devices, the operation of which does not require expensive material resources and highly qualified service personnel;

[0048] - use serial high-performance pumping equipment, stamped structures and plastic tubular products for the production of cavitation evaporation units;

[0049] - reduce the cost of manufacturing, operation and maintenance of equipment for obtaining distillate from polluted water;

[0050] - obtain a steam-gas mixture and distillate from contaminated water not only in a periodic cyclic process, but also in a continuous flow mode without preliminary heating of the initial liquid, preventing the formation of sediments requiring disposal; reduce the risks of disruption of the normal operation of equipment, including the destruction of individual structural elements under the influence of cavitation microbubbles, and as a result of contamination of the initial and waste liquid mixture with components.

[0051] - obtain the required amount of the final product - steam-gas mixture, distillate, thermal energy, concentrated solutions and suspensions, using modules with different numbers of cavitators operating in parallel or sequentially.

[0052] Brief description of the drawings

[0053] The proposed designs of the devices are shown in Fig. 1-5, with the following positions indicated:

[0054] 1. Feed hydraulic pump (with distribution manifold).

[0055] 2, 3. Cavitation unit: hydrodynamic pump combined with a cavitator.

[0056] 4. Feed manifold.

[0057] 5. Pneumatic hydraulic disperser.

[0058] 6. Hyperbaric fountain chamber.

[0059] 7. Bubbling device.

[0060] 8. Gas compression unit.

[0061] 9. Unit for condensing steam-gas mixture.

[0062] 10. Automatic pressure valve.

[0063] 11. Liquid flow regulator.

[0064] 12. Steam-gas mixture collector.

[0065] 13. Hydro turbine of a power plant.

[0066] 14. Maintenance hatch. Implementation and examples of implementation

[0067] The claimed technical and technological solutions are as follows:

[0068] 1. Creation of a flow of pre-cavitated liquid containing cavitation gas microbubbles, inside which the temperature exceeds one hundred degrees and the pressure increases, and outside which a shell of water vapor is formed, using a device that combines a hydrodynamic pump and a cavitator of any known design.

[0069] 2. Creation of a flow of gas-filled liquid mixture by dispersing gas and / or gas-emitting substance supplied from the external environment by a pneumatic disperser under excess pressure into the flow of cavitated liquid, creating a dispersion of gas bubbles that increase in size, absorbing cavitation vapor-gas microbubbles before they collapse, and the released thermal energy causes heating of the main mass of contaminated water.

[0070] 3. The release of vapor-gas bubbles from a stream of gas-filled liquid mixture, at a pressure exceeding atmospheric pressure, gushing into the air space of a hyperbaric fountain chamber.

[0071] 4. Release of residual vapor-gas bubbles during bubbling of a partially degassed gas-filled liquid mixture into the air space of a hyperbaric fountain chamber.

[0072] 5. Formation of a vapor-gas phase in the air space of a hyperbaric fountain chamber from released dispersed and bubbling gases.

[0073] 6. Increasing the pressure in the air space of the hyperbaric fountain chamber by regulating the gas supply through the pneumatic disperser and the bubbling device to a level sufficient to displace the vapor-gas phase and waste liquid from the hyperbaric fountain chamber. 7. Reducing the level of destructive impact of cavitation microbubbles on elements of production equipment when using cavitation modules as anti-cavitation valves.

[0074] To implement the proposed method, a device based on the modular structures of Figs. 1-5 is used, in which:

[0075] - a cavitator of any known design, combined with a pump that generates a flow of cavitated liquid;

[0076] - a pneumohydraulic disperser fills the flow of cavitated liquid with gas bubbles that absorb cavitation vapor-gas microbubbles, preventing the destructive effect of cavitation on the elements of the device;

[0077] - a hyperbaric fountain chamber ensures the rupture of the flow coming from the pneumohydraulic disperser when a jet of gas-filled liquid is fountained into the air space, where the gas bubbles burst and form a vapor-gas phase;

[0078] - the bubbling device additionally saturates the partially degassed liquid with gas bubbles, which absorb the residual amount of cavitation vapor-gas microbubbles and burst in the air space of the hyperbaric fountain chamber;

[0079] - the gas compression unit provides increased pressure for feeding gas into the pneumatic disperser and into the bubbling device, and also allows for an additional increase in pressure in the air space to the level required for squeezing out the vapor-gas mixture and the outflow of degassed liquid from the hyperbaric fountain chamber;

[0080] - a unit for condensing the steam-gas mixture and recovering thermal energy separates moisture from the gas, which, cooling to a specified temperature, returns to the gas compression unit. Preferred options, the general purpose and specified parameters of the main elements of which are given in Table 1.

[0081]

[0082]

[0083]

[0084]

[0085] Table 1.

[0086] All structural elements are connected by pipelines with threaded or flanged connections in the sequence indicated in the figures; the elements themselves can be located either on a common base - a platform, foundation, or on individual elements, the ground surface, trusses, etc.

[0087] Figures 1 and 2 show a view of a device without continuous fluid intake from outside. The device includes a feed hydraulic pump 1 with a tubular distribution manifold installed either separately on a truss or foundation, or at the location of the entire installation and connected by means of pipes to a hydrodynamic pump 2 combined with a cavitator 3, on the other side from the connection to the hydraulic pump 1, the hydrodynamic pump 2 combined with a cavitator 3 through a feed manifold 4, are connected to a pneumohydraulic disperser 5, which in turn is connected through a pipeline to a hyperbaric fountain chamber 6 in its upper part, which can be represented in the form of a cone placed with a narrow part towards the bottom (Fig. 1), or an angular tubular chamber (Fig.2-5, the diameter of the pipe of which is at least 5 times greater than the diameter of the pipelines of the installation, wherein in the lower part of the chamber 6 or, preferably, in the pipeline, branched off from the lower part, a liquid flow regulator 11 is installed. In the lower part of the fountain chamber 6, in the section from the installed flow regulator 11 to the middle of the chamber 6, a bubbling device 7 is installed, which is connected by means of a pipeline to a gas compression unit 8, carried out beyond the boundaries of the chamber 6 and made with the possibility of supplying gas (air) from the outside. In the upper part of the fountain chamber 6, in the cover of the chamber 6, a pressure valve is located, connected by means of a pipeline to a unit for condensing a steam-gas mixture 9, which is equipped with a pipeline for removing the distillate. The gas compression unit 8 is connected by a pipeline to a pneumohydraulic disperser 5 for supplying gas to it at an increased pressure.

[0088] The lower part of the fountain chamber 6 can also contain a hydro turbine of the power plant 13, installed on the pipeline after the liquid flow regulator 11. The installation can be made for the possibility of using liquid from outside, for example, from tanks, reservoirs, puddles and other water sources. In such cases, Figs. 3-5, the liquid is taken by the feed hydraulic pump 1 from a liquid source, respectively, while the feed hydraulic pump 1 is made and installed with the possibility of implementing such a withdrawal (installation, outlet of the feed pipeline or hose, etc.). The installation can also use liquid after cavitation treatment and passed through the fountain chamber 6, and the liquid flow regulator 11. In such embodiments, the pipeline after the liquid flow regulator 11 is connected to the intake of the feed hydraulic pump 1, as shown in Figs. 1 and 2.In the upper part (in the cover or the upper part of one of the walls) of the fountain chamber, a hatch 14 may be located to enable maintenance of the elements of the fountain chamber 6 and the inlet and outlet parts of the pipeline.

[0089] Figure 4 shows a variant of the installation with several parallel-connected cavitation units (table 1). With this implementation of the installation, the initial liquid is taken from the source by the feed hydraulic pump 1, the flow is supplied to the tubular distribution manifold (table 1), in which the total flow of the initial liquid is distributed to each parallel-connected cavitation unit, consisting of a hydrodynamic pump 2, combined with a cavitator 3 (table).1, at the outlet of which the cavitated liquid enters through the supply pipes into the main pipe of the feed manifold 4, connected to the pneumohydraulic disperser 5, from which the gas-filled flow, forming a fountain jet, enters directly into the air space of the upper-inclined part of the tubular hyperbaric fountain chamber 6, where the main volume of the dispersed gas phase is released, forming a vapor-gas mixture; the liquid phase drains into the lower part of the chamber 6 and, in order to remove the remains of the dispersed gas, is subjected to bubbling by a bubbling device 7 installed in the lower part of the chamber 6 and connected by means of a pipeline to a gas compression unit 8 located outside the boundaries of the chamber 6, allowing the required amount of gas (air) to be supplied from outside and, incl. to supply gas through a pipeline to the pneumohydraulic disperser 5.The vapor-gas phase accumulates in the air space in the upper part of the fountain chamber 6 at an increased pressure, the value of which is set and regulated by the gas compression unit 8 through the pneumohydraulic disperser 5 and the bubbler 7, so that the total pressure of the vapor-gas phase in the air space of the chamber 6 does not exceed the pressure of the gas coming from the disperser into the flow of cavitated liquid, and is higher than the operating limit of the pressure valve 10 located in the upper part of the fountain chamber 6, which is connected by means of a pipeline to the unit for condensing the vapor-gas mixture 9, and is also connected in the upper part by a pipeline to the gas compression unit 8 and is equipped with an external pipeline for removing the distillate.

[0090] The draining of the de-aerated liquid, regulated by the liquid flow regulator 11, is carried out through a pipeline from the lower part of the fountain chamber 6. The lower part of the fountain chamber 6 in figure 4 contains a hydro turbine of the power plant 13, mounted in the pipeline after the liquid flow regulator 11.

[0091] Figure 5 shows a variant of the installation, the process chain of which contains several sequentially connected cavitation units of Table 1, each of which consists of a hydrodynamic pump 2 combined with a cavitator 3, after each of which a connection is sequentially made through a feed manifold 4 with a pneumohydraulic disperser 5, which, in turn, is connected through a pipeline to a fountain chamber 6 in its upper part, while a liquid flow regulator 11 is installed in the lower part of the chamber 6. In the lower part of the fountain chamber 6, in the section from the installed flow regulator 11 to the middle of the chamber 6, a bubbling device 7 is installed, which is connected by means of a pipeline to a gas compression unit 8 located outside the boundaries of the chamber 6 and designed with the possibility of feeding gas (air) from the outside, both to the bubbling device 7 and to the pneumohydraulic disperser 5.In the upper part of each fountain chamber 6, in the cover of the chamber 6, there is a pressure valve 10, connected by means of a pipeline to the unit for condensing the steam-gas mixture 9 (one or more), which in the upper part is connected by a pipeline to the gas compression unit 8 (one or more) and is equipped with at least one device for removing distillate, while, unlike the above-described installation options, the pipelines installed after the automatic pressure valves 10 are connected by a common pipeline that connects to the unit for condensing the steam-gas mixture 9.With such implementation of the installation, the initial liquid is taken from the source by the feed hydraulic pump 1 and the flow is supplied through the distribution manifold to the first cavitation unit 2, 3, from which the cavitated liquid enters the feed manifold 4, into the pneumohydraulic disperser 5 and the gas-filled flow forms a fountain jet in the air space of the upper-inclined part of the tubular hyperbaric fountain chamber 6, releasing the main volume of the dispersed gas phase and forming a vapor-gas mixture; the liquid phase drains into the lower part of the chamber 6, where the remains of the dispersed gas are released from the liquid during bubbling by means of a bubbling device 7 installed in the lower part of the chamber 6 and connected by means of a pipeline to a gas compression unit 8 located outside the boundaries of the chamber 6, allowing the required amount of gas (air) to be supplied from outside and, incl., to supply gas through a pipeline to the pneumohydraulic disperser 5.The vapor-gas phase accumulates in the air space in the upper part of the fountain chamber 6 at an elevated pressure, the value of which is set and regulated by the gas compression unit 8 through the pneumohydraulic disperser 5 and the bubbler 7 so that the total pressure of the vapor-gas phase in the air space of the chamber 6 does not exceed the pressure of the gas coming from the disperser 5 and the bubbler 7 into the flow of cavitated liquid, and is higher than the actuation limit of the pressure valve 10 located in the upper part of the fountain chamber 6, which is connected by means of a pipeline to the unit for condensing the vapor-gas mixture and recovering thermal energy 9, and is also connected in the upper part by a pipeline to the gas compression unit 8 and is equipped with a pipeline for removing the distillate. The deaerated liquid from the lower part of the fountain chamber 6 is subjected to repeated processing, i.e.enters the next cavitation block, from which the cavitated liquid enters the pneumohydraulic disperser via the feed manifold, is poured as a jet into the fountain chamber, bubbles and is again fed for re-processing in the next link of the process chain. At the end of the process chain, a liquid flow regulator 11 is installed, which ensures an adjustable mode of outflow of deaerated liquid from the last fountain chamber, in accordance with the specified parameters of pressure and volume.

[0092] Unlike the above-described variants of Figs. 1-4, in the installation of Fig. 5 the steam-gas mixture from the upper part of each fountain chamber enters a single pipeline of the collector 12 of Table 1, connected to the unit for condensing the steam-gas mixture 9, from which a pipeline for collecting the distillate is led out; also each disperser 5 and each bubbling device 7, installed along the entire process chain, are connected by pipelines to the gas compression unit 8 (one or more), ensuring their operation in accordance with the specified parameters of pressure and gas flow.

[0093] Preferred options:

[0094] The initial data for the evaluation and subsequent extrapolation of the technical and technological parameters were obtained on a device that is a single-circuit cavitation evaporation module (KIM-1), the basic diagram of which is shown in Fig. 1.

[0095] Extrapolation of experimental data obtained on KIM-1 allows optimizing the scheme, composition, functions of the equipment and production and technological characteristics. In this case, the preferred option for implementing the method is a multi-loop cavitation evaporation module (KIM-8), on the basis of which multi-module high-performance production units can be created, including a hydroturbine and a power plant (Fig. 3-5).

[0096] The method for producing water vapor and distillate from cavitated aqueous solutions and suspensions consists of the effect of cavitation on aqueous solutions and suspensions of various substances due to the formation of cavitation gas microbubbles, inside which the temperature exceeds one hundred degrees and the pressure increases, and outside which a shell of water vapor is formed, in a device combining a hydrodynamic pump and a cavitator; the creation of a vapor-gas mixture and condensation of vapors with the formation of distillate due to the dispersion of gas (gas-emitting substance) in the flow of pre-cavitated liquid and the formation of a dispersion of gas bubbles, which increase in size, absorbing cavitation vapor-gas microbubbles before they collapse, and the released thermal energy causes heating of the main mass of contaminated water;wherein the flow of cavitated and gas-filled liquid mixture is fed by a fountain, with a jet length of at least 0.1 m, into the air space of the hyperbaric fountain chamber, where dispersed gas bubbles released from the fountaining jet form a vapor-gas phase, and the accumulating liquid phase is subjected to bubbling, removing the residual amount of dispersed bubbles from the liquid, increasing the pressure in the air space of the hyperbaric fountain chamber to a level sufficient to suppress excess foaming and squeeze the vapor-gas phase out of the hyperbaric fountain chamber into the condensation zone, and to squeeze the spent cavitated liquid mixture into an external pipeline. Example of implementation;

[0097] The example below illustrates a variant of the claimed invention, but does not limit it.

[0098] The feed hydraulic pump 1 performs the suction of liquid with its subsequent entry through the pipeline into the cavitation unit consisting of the hydrodynamic pump 2 and the cavitator 3, connected to the feed manifold 4, from which the flow of cavitated liquid enters under pressure into the pneumohydraulic disperser 5 and mixes with the gas under pressure from the gas compression unit 8, forming a flow of gas-filled liquid mixture entering the hyperbaric fountain chamber 6, the body of which contains two zones - an inclined one, with an air space that ensures the rupture and fountaining of the flow of gas-filled liquid mixture and a vertical one, for bubbling and accumulation of the degassed liquid phase, wherein the vapor-gas phase, being released from the stream of the fountaining gas-liquid mixture and from the bubbling gas, fills the air space and at a pressure exceeding a specified limit,through the automatic pressure relief valve 10, it enters the condensation unit 9 via a pipeline, where distillate and dried gas are formed, which can be used to feed the gas compression unit 8.

[0099] The method is illustrated by experimental results of separation of the vapor-gas phase and distillate, using a single-loop cavitation evaporation module of Fig. 1 during multiple cavitation treatment of a limited amount of water or liquid mass artificially contaminated with organic and inorganic impurities.

[0100] During preliminary experiments, the conditions for excitation of cavitation, characteristic of the device of this design, were determined, and the optimal ratios of the operating modes of each of the design elements were established (Table 2). The technical and technological parameters of the experiments, using a single-circuit cavitation evaporation module (Fig. 1), are given in Table 2.

[0101] Table 2.

[0102] * The temperature of the liquid in the feed manifold was measured by a thermocouple (not shown in the diagrams in Figs. 1-5) at the inlet to the disperser. - The pressure of the vapor-gas phase in the air space of the hyperbaric fountain chamber was limited to 0.15 MPa using an automatic pressure relief valve 10.

[0103] - The temperature of the degassed liquid was measured by a thermocouple (not shown in the diagrams in Figs. 1-5) at the outlet of the hyperbaric fountain chamber after the liquid flow regulator 11.

[0104] The technological and design parameters of the installation, a variant of which is shown in Figure 1, are given in Table 2. With this implementation of the installation, the initial liquid is taken by a hydrodynamic pump 1, through a drain branch and a liquid flow regulator 11 directly from a hyperbaric fountain chamber 6, into which 30 liters of water and artificial pollutants in the quantities indicated in Table 3 were preliminarily loaded through a hatch 14. From the hydrodynamic pump 1, the flow of the initial liquid entered the cavitation unit, consisting of a hydrodynamic pump 2 combined with a cavitator 3 (Table 1), from which the cavitated liquid entered the feed manifold 4, with a volumetric velocity of about 5 cubic meters.m per hour under a pressure of 0.3 MPa, then into the pneumohydraulic disperser 5, where it was mixed with a gas flow supplied under a pressure of 0.35 MPa, and the gas-filled flow created a fountain jet of liquid, 0.1 m long, in the air space of the upper part of the hyperbaric fountain chamber 6, releasing a dispersed vapor-gas phase; the liquid phase merged into the lower part of the chamber 6, forming a liquid layer of 0.25-0.3 m, and in order to separate the remains of the dispersed gas from the liquid, it was subjected to bubbling, by means of a bubbling device 7 installed in the lower part of the chamber 6, and connected by means of a pipeline to a gas compression unit 8 located outside the boundaries of the chamber 6, from which the required amount of air was supplied from outside to the bubbling device 7 and to the pneumohydraulic disperser 5.When the pressure of the steam-gas mixture in the air space of the hyperbaric fountain chamber 6 exceeded 0.25 MPa, the automatic pressure valve 11 was activated, and the steam-gas mixture entered a metal tube washed with cold water, condensed, and the resulting distillate was collected in a measuring container.

[0105] The generalized experimental data and technological parameters of the process of obtaining distillate during repeated cavitation treatment of a limited amount of water or liquid mass artificially contaminated with organic and inorganic impurities are given in Table 3.

[0106] Table 3.

[0107] The data presented in Table 3 indicate that forced dispersion of gas in a liquid flow previously subjected to cavitation action, causing the formation of cavitation gas microbubbles, allows: - to increase the efficiency of using cavitation energy to obtain distillate from aqueous suspensions, compared to a similar process (water without carbonation) during cavitation heating of water; to prevent cavitation heating, and, consequently, the destructive effect of cavitation on the contact surface of the cavitated liquid with equipment elements in devices using cavitation for liquid evaporation, as well as as an anti-cavitation pneumatic seal in pipeline systems for pumping liquids.

[0108] From the above it follows that in a number of processes, cavitation can become an unconventional source of renewable energy, which can be used to implement environmentally friendly technologies - technological processes of physical and chemical transformation of substances, including the production of steam, thermal energy and distillate, as well as for concentrating the components of liquid mixtures.

[0109] Example 2.

[0110] Table 4 shows the results of extrapolation of experimental data using a single-loop cavitation evaporation module (example 1) to obtain a steam-gas mixture and distillate from contaminated water in cavitation evaporators with a different number of cavitation units (Fig. 5, KIM-...), when operating for 24 hours a day to provide people in emergency situations with the daily consumption rate of drinking water.

[0111] Table 4.

[0112] * The daily norm for drinking water consumption is 2 liters per day per person.

[0113] The objectives of the invention of Fig. 1, 2 and Table 1 are achieved by the fact that:

[0114] 1. The flow of the initial liquid mixture is fed by the feed hydraulic pump with the distribution manifold 1 to the hydrodynamic pump 2, combined with the cavitator 3, of any known design that allows for the excitation of cavitation in the flow of liquid containing dissolved components and / or particle suspensions. In this case, cavitation gas microbubbles should arise in the liquid mixture, but not burst, inside which the temperature reaches one hundred degrees or more, and the pressure increases, and a shell of water vapor is formed outside. For example, a rotary pulsation unit, serially produced, in which the impeller and centrifugal pumps are combined with a rotary pulse pump.

[0115] 2. The flow of cavitated liquid mixture from cavitator 3 enters the feed manifold 4 - a branch pipe connecting the cavitator and the pneumohydraulic disperser 5, preferably of serial production. The pressure in the feed manifold 4 is set automatically depending on the ratio of the diameter, length and volumetric flow rate of the cavitated liquid mixture.

[0116] 3. Gas is introduced into the flow of cavitated liquid mixture through pneumohydraulic disperser 5. Gas enters pneumohydraulic disperser 5, of serial production, from gas compression unit 8, of serial production. Volume of dispersed gas and sizes of bubbles are determined experimentally, based on volumetric velocity and pressure of cavitated liquid flow. Flow of cavitated gas-filled liquid mixture from pneumohydraulic disperser 5 enters air space of hyperbaric fountain chamber 6, pressure in which is regulated mainly by pressure and volume of bubbling gas entering bubbling device 7, of arbitrary design, from gas compression unit 8. Tubular body of hyperbaric fountain chamber 6 contains two zones - vertical, for accumulation of liquid phase, and inclined (air space) for vapor-gas mixture;

[0117] The volume and dimensions of the housing zones are determined based on the pump capacity, flow rate and length of the gas-filled liquid jet, which must be no shorter than 0.1 m.

[0118] 4. A bubbling gas is introduced into the flow of liquid accumulating in the vertical zone of the hyperbaric fountain chamber, increasing the pressure in the air space to a level not exceeding the pressure in the feed manifold 4.

[0119] 5. The resulting vapor-gas phase is removed from the air space of the hyperbaric fountain chamber through an automatic pressure relief valve - not specified in the description of the design of systems, serial production, through a pipeline into unit 9 for condensation of the vapor-gas mixture and recovery of thermal energy.

[0120] 6. Under the action of the pressure created in the air space of the hyperbaric fountain chamber 6 by the steam-gas mixture, the liquid accumulating in the vertical zone of the hyperbaric fountain chamber is forced out into the pipeline and sent to the drain or for reprocessing.

[0121] 7. In multi-module high-performance production units, the energy of the flow displaced from the hyperbaric fountain chamber is preferably used to produce electrical energy by directing the flow of waste liquid to the blades of the hydroturbine 10 of the mini power plant Fig. 2 of serial production.

[0122] The novelty of the proposed solution is that in the process of obtaining distillate, energy losses for heating the main mass of the liquid phase and equipment are minimized, increasing the efficiency of using the energy contained in cavitation vapor-gas microbubbles during vaporization, for which:

[0123] 1. Cavitation vapor-gas microbubbles are separated from a flow of contaminated liquid, previously subjected to cavitation treatment, before they collapse, and the released thermal energy causes heating of the main mass of contaminated water by absorption by gas bubbles formed during dispersion of gas from the external environment at elevated pressure in the flow of cavitated liquid.

[0124] 2. They release gas bubbles, enlarged as a result of merging with cavitation vapor-gas microbubbles, releasing a fountain of gas-filled liquid into the air space of the hyperbaric fountain chamber, where the pressure exceeds atmospheric pressure, but does not exceed the pressure in the flow of gas-filled liquid.

[0125] 3. The layer of partially degassed gas-filled liquid formed in front of the drain hole of the hyperbaric fountain chamber is subjected to bubbling to release the residual amount of gas bubbles.

[0126] 4. The pressure of the vapor-gas phase formed in the air space of the hyperbaric fountain chamber is set by adjusting the volume and pressure of the gas supplied to the disperser and bubbler to a level sufficient to displace the vapor-gas mixture from the air space into the condensation zone and the waste liquid accumulating in the hyperbaric fountain chamber into the external pipeline. 5. The energy efficiency of the cavitation evaporator is additionally increased by installing a hydroturbine 13 of Fig. 4 of the power plant, using the force of the flow of the waste cavitated liquid mixture sent to the drain or for reprocessing.

Claims

Invention formula 1. A method for producing water vapor and distillate from cavitated aqueous solutions and suspensions, characterized in that in a flow of cavitated liquid pumped into the unit by means of a feed hydraulic pump, using a pneumohydraulic disperser, a dispersion of gas bubbles is created that absorb cavitation vapor-gas microbubbles, the resulting gas-filled liquid mixture is fed by a fountain, with a jet length of at least 0.1 m, into the air space of a hyperbaric fountain chamber, where the dispersed bubbles released from the fountaining jet form a vapor-gas phase, and the accumulating liquid phase is subjected to bubbling, removing the residual amount of dispersed bubbles from the liquid, increasing the pressure in the air space of the hyperbaric fountain chamber to a level sufficient to suppress excess foaming, squeezing out the vapor-gas phase from the hyperbaric fountain chamber into the condensation zone,and squeezing out the spent cavitated liquid mixture into an external pipeline, while the supply of liquid to the feed hydraulic pump is carried out from a pipeline installed in the lower part of the hyperbaric fountain chamber after the flow regulator or from a liquid source.

2. An installation for producing water vapor and distillate from cavitated aqueous solutions and suspensions, characterized in that it consists of a feed hydraulic pump with a tubular distribution manifold connected by a pipeline to a cavitation unit, including a hydrodynamic pump combined with a cavitator, connected to a feed manifold, which is connected to an evaporation unit, including a hyperbaric fountain chamber with a bubbling device, a unit for condensing a steam-gas mixture, a gas a compression unit and a pneumohydraulic disperser connected to a feed manifold, wherein the hyperbaric fountain chamber comprises an inclined upper part and a vertical lower part in which a liquid flow regulator is installed, the bubbling device is connected to a gas compression unit connected to the pneumohydraulic disperser, in the upper part of the fountain chamber a pressure valve is located, connected to a unit for condensing a steam-gas mixture, equipped with a pipeline for removing distillate, the gas compression unit is designed with the possibility of feeding gas to the pneumohydraulic disperser.

3. The installation according to item 2, characterized in that the lower part of the fountain chamber contains a hydroturbine of the power plant, installed on the pipeline after the liquid flow regulator.

4. The installation according to paragraph 2, characterized in that the feed hydraulic pump is designed and installed with the ability to draw liquid from the source.

5. The installation according to paragraph 2, characterized in that the pipeline after the liquid flow regulator is connected to the intake of the feed hydraulic pump.

6. The installation according to item 2, characterized in that a hatch is located in the upper part of the fountain chamber.

7. The installation according to paragraph 2, characterized in that the installation contains 2 or more cavitation blocks installed in parallel.

8. The installation according to item 2, characterized in that the installation contains several sequentially connected installations, wherein the first feed hydraulic pump is designed with the possibility of drawing liquid from a source, the installations are connected by means of a pipeline connecting the second and more hydraulic pumps with the lower part of the fountain chamber of the previous installation, the pressure valves of the installations are sequentially connected to a common collector of the steam-gas mixture, at least one a unit for condensing a steam-gas mixture, a gas compression unit.

Images