RU2297267C2 - Method of separation of multi-phase media and device for realization of this method - Google Patents

Abstract

FIELD: cleaning of liquid mixtures containing suspended agents, mechanical impurities, petroleum products, gases; purification of waste water; aeronautical engineering; rocketry; chemical and oil industries; separation of byproduct gas and water from oil.

SUBSTANCE: proposed method includes repeated forming of vortex flow of medium, centrifugal separation of media at removal of light fractions and straight-flow separation of heavy fractions. Device proposed for realization of this method has housing, vortex flow forming unit made in form of immovable hollow body with twisting blades rigidly connected with housing walls. Cavity of housing whose open end is directed towards delivery of mixture is connected with light fraction discharge pipe line. Housing is connected with separation chamber made in form of tube.

EFFECT: enhanced efficiency of media separation.

10 cl, 8 dwg, 6 ex

Description

The invention relates to methods and devices for cleaning liquid mixtures containing suspended equal and different density substances, mechanical impurities, oil products and other organic compounds, gaseous inclusions, and can be used for the treatment of domestic wastewater and wastewater in various industries, as well as in aviation, rocket, chemical, oil industry and other fields of technology. The invention can also be used to separate associated gas from oil during production at the stage of preparing oil for transportation through the main pipeline, for purifying associated water from oil, or oil from water and solids.

The issues of water purification and its return to natural circulation in recent years have acquired great importance. The growth of production volumes associated with the consumption and pollution of water, technological disasters leading to the pollution of water basins with oil and other substances harmful to nature, put forward the task of cleaning liquid media from harmful impurities.

Known methods and devices for separating mixtures using gas flotation, chemicals, electrolytic processes, etc., do not provide high-quality purification.

The known Vortoil method and device for its implementation, using the centrifugal effect, developed by CONOCO Specialty Products Inc. (see brochure, 1990).

In accordance with the method, a stream of contaminated water with an oil concentration of 0 to 10,000 ppm is fed into the involute channels and spun into a vortex stream rotating at a speed of 30,000 rpm. At the same time, due to centrifugal forces - more than 1000 g - flow separation is ensured. Lighter oil is drawn into the vortex flow into the low pressure zone. As you move away from the swirling zone, the pressure along the axis increases and conditions are created for the reverse flow of the separated oil to occur by blocking the direct-flow main flow, i.e., an internal directional flow opposite to the main flow is formed. Heavier water moves along the outer wall and is discharged through a side outlet.

The device for implementing the method is a hydrocyclone with an involute inlet, providing a swirl of the flow of contaminated liquid supplied to the cyclone through the pipeline. The cyclone body is equipped with a radial channel for oil output from the central zone to the discharge pipe and a channel for the removal of purified water.

The indicated method and device use a single physical principle of operation - centrifugal separation of different fractions, ensure the implementation of a continuous process in a stable mode. The Vortoil system can contain many devices connected in parallel, which makes it possible to handle any amount of contaminated media. However, the Vortoil system can only be used to clean two-phase fluid flows of oil-water type.

Thus, the disadvantage of this method is the low cleaning efficiency of multiphase liquid mixtures.

The disadvantage of this device is the large energy loss during separation associated with the need to feed the liquid mixture into the involute channel under high pressure equal to 40 kg / cm ² , large dimensions, weight and installation cost. To ensure a capacity of about 700 m ³ / h, a block of 37 separator sections will be required.

In addition, the Vortoil system provides purification with a residual concentration of at least 40 mg / l, while the national regulations of many countries provide for the discharge of treated water into the sea with a residual concentration of not more than 5 mg / l. Even more stringent requirements for water discharged into inland fisheries (up to 0.05 mg / l).

The specified system does not provide such a degree of purification.

A known method of separating multiphase oil-containing systems in the chemical, oil refining and oil industries, selected as a prototype, involves the creation of a tangential vortex flow of a cleaned medium supplied under pressure, subsequent centrifugal separation of the media with removal by creating a negative pressure gradient of light fractions along the axis of the hydrocyclone in the direction reverse translational movement of the cleaned medium, and the removal of more severe in relation to the carrier medium s in the opposite direction (See. Patent №2211095, priority of 08.11.2001, published 27.08.2003).

As a prototype of the device, a hydrocyclone is selected, which ensures the implementation of the above method. The specified hydrocyclone contains a housing, a unit for creating a vortex flow supplied to the housing from the pipeline of contaminated liquid, made in the form of a tangentially located inlet pipe, a pipeline for removing contaminants and a pipeline of purified liquid mounted coaxially to the housing from opposite sides. At the output end of the casing, a straightening (spinning) device is installed, made in the form of an impeller, the outer diameter of which is less than or equal to the inner diameter of the casing, and the slope of the input edges of the blades coincides with the slope of the trajectory of the heavy phase, while the output edges of the blades are directed along the axial planes of the casing ( see patent No. 2211095, priority of 11/08/2001, published on 08/27/2003).

The disadvantages of the method and device are the large energy losses during separation associated with the need to supply the liquid mixture to the involute channel 4 under high pressure equal to 40 kg / cm ² , large dimensions, weight and installation cost.

In addition, they, like the analogues described above, are characterized by an insufficient level of purification.

The presence of a spinning device in the form of an impeller, blocking the axial flow and installed at a distance equal to several body diameters, provides the possibility of separating the liquid-gas medium. But in the separation of the liquid – liquid mixture, the presence of such an obstacle in the path of the vortex flow leads to the destruction of this flow and entrainment of contaminants together with the cleaned medium leaving the hydrocyclone, which does not allow ensuring high-quality separation of the media.

The objective of the proposed method and device is to enable highly efficient cleaning of multiphase liquid mixtures while reducing energy costs, dimensions, weight and cost.

To solve this problem in the method of separation of multiphase media, mainly “liquid + liquid + gas + suspended solids and / or mechanical impurities”, including the creation of a vortex flow supplied under pressure of the cleaned medium, the subsequent centrifugal separation of the media with the removal of light fractions due to the creation of a negative gradient the pressure of light fractions along the axis of the centrifugal separator in the direction opposite to the translational movement of the medium to be cleaned, and the direct-flow removal of heavier relative to the bearing medium de fractions according to the invention, initially form a mixture flow with Reynolds number (Re) is not lower than 10 ⁵ and the carrier medium and produce a multi-stage separation of a mixture with the creation in each step of the vortex flow in cocurrent linear conduit and consistent centrifugal separation media, preferably in the order of the density of the separated media decreases, while in the first stage of the liquid + gas separation of the media, the vortex flow forms a length of 2-10 diameters of the separation chamber and the gas fraction is removed countercurrently, then carry out forced rectification and braking of the vortex flow with the formation of a free channel in the axial part of the flow; at the stage of liquid-liquid separation, the vortex stream forms a length of 80-100 diameters of the separation chamber and light fractions are removed by countercurrent flow, then the flow is decelerated, while at the stage of separation of the liquid + liquid mixture 3 ... 5 seconds before creation a vortex flow at an oil fraction concentration in water of more than 50 mg / l, an appropriate demulsifier is introduced, and at a concentration of less than 50 mg / l, an electrolyte is introduced; at the stage of separation of equal-density media, 3-5 seconds before the creation of the vortex flow, a sorbent is introduced, with a density higher than the medium to be removed, and at the stage of separation of different-density media, suspended solids (mechanical impurities) are removed directly through the annular slit of the separation chamber, while the multiplicity of multi-stage separation of the mixture carry out to the required values of the parameters of each environment.

At the stage of separation of the mixture "liquid + mechanical impurities" with the content of surface-active substances (surfactants) 3 ... 5 seconds before the creation of the vortex flow can be introduced electrolyte.

As an electrolyte, a 5-7% solution of iron sulfate or a 5-7% solution of aluminum sulfate or a 5-7% solution of zinc sulfate can be used.

As a sorbent, you can enter a solution of lime in a concentration of up to 5% wt, while the dose of the solution should be 50-300 mg / L.

To solve this problem, in a device for separating multiphase media, comprising a housing, a unit for creating a vortex flow supplied to the housing from a contaminated liquid pipeline, a pipeline for removing a lighter phase and a pipeline for purified liquid, according to the invention, the unit for creating a vortex flow is made in the form of a stationary mounted in the housing hollow central body with twisting blades rigidly connected to the walls of the body, and the cavity of the central body, directed by the open end towards the supply of the mixture, It is connected with a pipeline for removing the lighter phase, while the housing is connected to a separation chamber made in the form of a pipe.

The projection of the swirling blades on a plane perpendicular to the axis of the flow can overlap at least the cross-section of the channel in the area of the eddy flow generating unit.

The cavity of the Central body of the node creating a vortex flow may be associated with the pipeline to remove contaminants through radial channels.

The cavity of the Central body of the node creating a vortex flow may be associated with the pipeline to remove contaminants through an axial tubular channel.

In the case of separation of a compressible medium (liquid - gas), a node for the forced rectification of the purified liquid flow is arranged in front of the diffuser to create a vortex flow at a distance of 2-10 diameters of the separation chamber, made in the form of fixed blades connected to the walls of the pipeline, the direction of bending of which is opposite to the blades node creating a vortex flow, while in the axial zone between the blades a free channel is formed.

In the case of separation of different-density media (liquid - suspended solids or mechanical impurities), a unit for removing a heavier phase, made in the form of a collector with an annular gap formed between the flow channel, is placed behind the vortex flow creating unit at a distance of 0.5-5.0 of the separation chamber diameter separation chamber and piping of purified liquid.

In the case of separation of incompressible media (liquid - liquid), the length of the separation chamber is 80-100 of its diameters.

In the case of multi-stage separation, a diffuser can be placed behind the separation chamber.

Conducted patent studies have shown that the claimed objects meet the eligibility criteria of inventions "novelty" and "inventive step".

The inventive methods and devices for their implementation can be implemented industrially, therefore, meet the criterion of "industrial applicability".

The essence of the claimed technical solutions is illustrated by drawings and diagrams, which show:

figure 1 - a device for the separation of multiphase media, mainly gas-liquid mixtures;

figure 2 - flow diagram in a device for the separation of multiphase media, mainly gas-liquid mixture;

figure 3 is an embodiment of a device for the separation of multiphase media, mainly a mixture of "liquid - liquid";

figure 4 is a graph of the dependence of the efficiency of gas extraction from a gas-liquid mixture from the volumetric gas content with the length of the separation chamber equal to two diameters of the separation chamber;

figure 5 is a graph of the dependence of the efficiency of gas extraction from a gas-liquid mixture from the volumetric gas content with a length of the separation chamber equal to 3.8 diameters of the separation chamber;

figure 6 is a graph of the dependence of the efficiency of gas extraction from a gas-liquid mixture from the volumetric gas content with a length of the separation chamber equal to 6.8 diameters of the separation chamber;

7 is a graph of the dependence of the efficiency of gas extraction from a gas-liquid mixture from the volumetric gas content with a separation chamber length equal to 8.6 diameters of the separation chamber;

on Fig - an embodiment of a device for the separation of different-density media, mainly "liquid - suspended solids or mechanical impurities".

For a more accurate understanding of the essence of the claimed methods, we first consider the proposed device designs for the separation of multiphase media.

The device (figure 1), made in the form of a straight-through linear pipeline, includes a housing 1, inside which a unit for creating a vortex flow supplied to the housing from the pipeline of contaminated liquid is fixedly installed. The specified node is made in the form of a hollow central body 2, on the outer surface of which hollow twisting blades 3 are fixed, rigidly connected with the walls of the housing 1. The projection of the twisting blades on a plane perpendicular to the axis of the flow can close at least the channel section in the zone of the creation node swirl flow.

The inner cavity of the Central body 2, directed by the open end towards the supply of the mixture, is connected with the pipe 4 removal of the lighter phase. Communication can be carried out by means of radial channels (Figs. 1, 2) or by means of an axial tubular channel (Fig. 3). The housing 1 is connected with the separation chamber 5, made in the form of a pipe of appropriate length. The output of the separation chamber may be provided with a diffuser 6.

In the case of separation of a compressible medium (liquid - gas), a node for creating a straightened flow of purified liquid in the form of stationary blades connected with the walls of the pipeline 7 is placed in front of the diffuser 6 at a distance of 2-10 diameters of the separation chamber 5, the bending direction which is opposite to the blades 3 of the node creating a vortex flow. Moreover, in the axial zone between the blades formed a free channel "A" (Fig.1).

In the case of separation of different-density media (liquid - suspended solids or mechanical impurities), a node for removing a heavier phase, made in the form of a collector 8 with an annular gap 9 formed between the flow channel of the separation chamber 5 and the pipeline of the purified liquid 10 (see Fig. 8).

In the case of separation of the liquid-liquid medium, the length of the separation chamber is 80-100 of its diameters.

The device may include one of the separation units described above (chamber 1, central hollow body 2 with blades 3, separation chamber and pipelines), and may contain two or more consecutively placed blocks, for example, the block shown in FIG. 1, providing for separation of the mixture liquid - gas ", then the block shown in Fig. 8, providing separation of the mixture" liquid - suspended solids or mechanical impurities ", and then the block presented on Fig. 3, providing separation of the mixture" liquid - liquid ", that is, in order P on a decrease in the densities of shared media.

The inventive method is as follows.

Shared medium is supplied to housing 1 under pressure. Direct-flow medium flow. Flowing around the central body 2 with the blades 3, the medium flow swirls, and centrifugal separation of the media occurs. The heavier phase is discarded to the periphery of the separation chamber 5, and the lighter phase is collected in the axial flow zone. This ensures the creation of a negative pressure gradient of light fractions along the axis of the centrifugal separator.

The heavier phase flows directly through the separation chamber, while the lighter phase is countercurrently removed into the pipeline. 4. This separation stage is effective in the liquid-gas and liquid-liquid environments.

To increase the pressure gradient, the cleaned medium can be forcedly "braked", for example, through the use of a diffuser. When separating the liquid-gas medium, it is possible to straighten the flow exiting the separation chamber 5, for example, by using fixed blades 7, which also provides an increase in the pressure gradient.

The method is also characterized by the fact that at the stage of separation of the mixture "liquid + liquid" for 3 ... 5 seconds before creating a vortex flow when the concentration in the water of the oil fraction of more than 50 mg / l, the corresponding demulsifier is introduced. This ensures the destruction of the shell surfactant drops of oil.

If the concentration in the water of the oil fractions is less than 50 mg / l, an electrolyte is introduced. The electrolyte provides increased mobility of particles, which leads to collision and coagulation.

At the stage of separation of equal-density media, 3-5 seconds before the creation of the vortex flow, a sorbent is introduced with a density higher than the medium to be removed

Thus, these method and device can effectively carry out the separation of a variety of multiphase media.

When separating a compressible medium, for example a gas-liquid mixture, the separation is carried out in a centrifugal separator, a schematic diagram of which is shown in figure 1.

The most important feature of this separator is the formation along the axis of the zone of the return flow of the separated lighter phase (gas), while the liquid will be removed from the hollow body 2 with blades 3, only along the periphery of the separation chamber 3, see figure 2, where for simplicity are shown streamlines of the constituent phases of the mixture without regard to peripheral speed.

In a separator without a forced flow straightening unit (straightener) used to separate an incompressible mixture, the cause of the return flow is the gradual, as the distance from the hollow body with the blades, damping of the rotational motion due to friction of the rotating medium on the pipe wall. The pressure gradient along the radius decreases with distance, both due to viscous friction and due to deceleration of the flow as the density of the mixture increases. Therefore, in the near-axial zone of the separation chamber, an axial pressure gradient is created, directed from the twisting blades, and the movement of the separated less dense medium, determined by the magnitude of this gradient, is directed to the eddy flow creating unit (hollow body with blades), through which the separated phase is removed through the outlet channels. The zone of secondary currents can have a considerable extent. So, the test results of the claimed object, in which the node creating the vortex flow was located in a transparent cylindrical pipe, showed that the separated lighter phase of the liquid-liquid mixture extends to a length of 80-100 diameters of the separation chamber (d _c.s. ) at Re≥10 ⁵ .

The reduction of the return flow zone (separation chamber length) of the separated compressible phase (gas) in the gas-liquid mixture is achieved by artificially increasing the pressure using the forced flow straightening unit. This assembly consists of profiled blades, the generators of which are radial in sections perpendicular to the axis of the separation chamber. An annular passage “A” is formed between the blades along the pipe axis. The installation of such a unit makes it possible to reduce the length of the separation chamber (l _c.s. ) to several pipe diameters with full gas extraction (100% efficiency), see FIG. 4, 5, 6, 7.

In order to reduce hydraulic resistance, increase the reliability and efficiency of the separator, the outlet channel of the removed less dense phase is performed in the form of a tube laid through the central body and brought out of the input (supply) pipe body (see figure 3).

The liquid stream is cleaned from the particles of different density and equal density located in it using the heavy phase removal unit (see Fig. 8).

The separated heavier phase (suspended particles and mechanical impurities), displaced to the periphery of the pipe, moves forward flow. On her way at a distance of 0.5-5.0 d _c.c. an annular gap is formed from a cut of the vortex flow creation unit, through which the heavier phase enters the collector 8 and then is removed to the sewer or to the collection tank, etc. The collector 8 is connected to pipes of different diameters, due to which a gap is formed.

To separate equal-dense suspended solids, for example, domestic wastewater, the suspended particles are weighted by introducing a CaO solution (milk of lime) into the main stream, which is sorbed onto the particles, makes them heavier and thereby allows them to be effectively separated from the main stream in a centrifugal field and removed from the main flow in the site of removal of the heavy phase.

In a model of a system consisting of two individual substances and one surfactant, a surfactant is always an emulsification factor. In practice, the system includes complex phases:

- oil, produced water, surfactants, mechanical impurities;

- domestic wastewater - water, surfactants, petroleum products, suspended solids, mechanical impurities, nitrogen-containing impurities, phosphorus, etc.

Chemical demulsification is the displacement from the surface of particles of substances of another type with a small structural and mechanical strength. Particles with weakened surface shells in a collision easily coalesce or compact in a centrifugal field.

This treatment is used to purify produced water with an input concentration of oil in water of tens to hundreds of milligrams per liter.

The best results of world practice in water purification from petroleum products when used including chemical demulsification and other centrifugal separation reagents are up to 20 mg / l.

The results of industrial tests for the treatment of produced water for the inventive facility amounted to 2-5 mg / l at a rate of 15 mg / l.

Deep purification of oily wastewater with a low input concentration of oil in water (from units to several tens of mg / l) to discharge them into fishery reservoirs (norm 0.05 mg / l) requires significant costs - filtering, biological treatment, etc.

The traditional technology of wastewater treatment from oil products using coagulants can reduce their concentration from 2.0 mg / l to 1.5 mg / l, which may not be an acceptable solution.

When an electrolyte (iron sulfate, aluminum sulfate, zinc sulfate) is fed into the emulsion stream, surfactants are neutralized, the presence of which determines the forces of mutual repulsion of oil globules (water, suspended particles), which are of an electrical nature.

Example No. 1

Bench tests of the separator for the separation of gas from a gas-liquid mixture were carried out. The test method consisted in determining the efficiency of gas extraction from the stream

,

,

where V _St. - volumetric flow of free gas at the inlet to the separator;

V _from - volumetric flow rate of the sampled gas.

The experimental points were plotted on the plane of parameters Ψ and β (here β is the volumetric flow rate of the mixture at different lengths of the separation chamber lc.c. (see Figs. 4-7), where in Fig. 4 l.c. = 2d.c .; in Fig. 5 lk.s. = 3.8 dk.s.; in Fig.6 lk.s. = 6.8 dk.s .; in Fig. 7 lk.s. = 8.6 dk.s.

As follows from the test results (see Fig.4-7), with increasing length of the separation chamber, the β zone increases with 100% removal of gas from the liquid, while the hydraulic resistance of the separator does not exceed 0.1 kg / cm ² .

Example No. 2

Pilot tests of the inventive method and device for purifying water from oil pollution were carried out.

When the water flow rate of 25-35 m ³ / h, supplied to the separation system from the settling pond with the addition of coagulating agents before the second separation stage, the following results were obtained:

The concentration of contaminants at the inlet to the separator, mg / l The concentration of pollution at the exit, mg / l The pressure drop across the separator, kg / cm ² I stage II stage I stage II stage 215 16,0 0.05 0.1 0.1 300 10.0 0.05 285 2,56 Lack of

Example No. 3

Pilot tests of a centrifugal separator for the treatment of associated water have been carried out. Associated water (water-oil emulsion) was treated with a demulsifier (introduced into the pipeline at the inlet of the station) with a dose determined for this mixture in laboratory conditions, as is usually used in practice.

The oil concentration at the inlet to the separator ranged from 98.8 mg / L to 526.3 mg / L.

Using the inventive facility, the concentration of oil in water at the outlet of the separator averaged from 2 mg / l to 5 mg / l with a norm of 15 mg / l. Moreover, the training scheme is greatly simplified.

Example No. 4

a) The crude oil emulsion of the Shaim field of the Tyumen region at a temperature of 8 ° C, treated with the Separol MF-41 demulsifier with a dosage of 400 g / t, followed by stirring and settling for 3.5 hours showed that the oil content in the separated water C was

C = 237 mg / L

b) The same as in paragraph a) with an exposure of 20 hours

C = 24 mg / L

c) The same as in paragraph b), followed by treatment with a 7% solution of aluminum sulfate in an amount of 3 ml per 0.5 l

C = 6 mg / L

Example No. 5

a) The crude oil emulsion of the Shaim field of the Tyumen region at a temperature of 28 ° C, treated with the demulsifier Akvanoks ML3230 with a dosage of 8.0 g / t, followed by stirring and settling for 1 hour showed that

C = 356.0 ml

b) The same as in paragraph a) with an exposure of 20 hours

C = 36.0 mg / L

c) The same as in paragraph b) with treatment with 7% aluminum sulfate solution in the amount of 3 ml per 0.5 l of sample

C = 5.2 mg / L

d) The same as in item c) with repeated treatment with an electrolyte solution in an amount of 3 ml per 0.5 l of sample, which showed

C = 0.05 mg / L

Example No. 5

Pilot tests of the claimed facility for the treatment of domestic wastewater were carried out.

The purpose of these tests was to assess the optimal operational characteristics of the separation system with the establishment of the efficiency of wastewater treatment from oil products and suspended particles.

The results of pilot tests of new technological methods have shown the high efficiency of the separation plant for wastewater treatment until there is no oil content (input concentration of oil products varied from 1.5 to 6.0 mg / l) for suspended solids - at an input concentration of 40 mg / l to 66.5 mg / l, the output concentration was 3.2-11.4 mg / l with a norm of 31.0 mg / l. Such a reagent treatment using the inventive multiphase mixture purification system made it possible to ensure 100% removal of oil products, humic substances, phosphorus and significantly reduce the amount of nitrogen-containing impurities.

As reagents, we used an electrolyte - aluminum sulfate and milk of lime, designed to weight suspended particles (initial particle density 1.002 g / cm ³ ) and efficient separation in a centrifugal field and removal from the stream.

The concentration of the initial solutions, respectively, 5% -7% for Al ₂ SO ₄ and 4.8% for CaO. The dose of aluminum sulfate was 15 mg / l, the dose of milk of lime was 50 mg / l.

Doses of reagents for a specific water are determined in practice in laboratory conditions and are specified in an industrial environment.

The time of water treatment with electrolyte and milk of lime or the residence time of the reagent in the fluid stream τ, defined as

where l is the length of the pipeline from the inlet of the reagent to the exit of pollution;

w is the fluid flow rate,

amounted to 3 seconds and up to 3 seconds, respectively.

The discharge rate of water with oil products and suspended solids was not more than 3% in relation to the total consumption of purified water.

Example No. 6

An emulsion of produced water with suspended particles with a dispersion of 5-10 microns and their concentration in water of 300 mg / l at a temperature of 18 ° C is treated with a 7% solution of iron sulfate with a dose of 25 mg / l of Fe ₂ O ₃ , followed by stirring and settling for 1 hours. As a result, water clarification was obtained.

Claims (10)

1. The method of separation of multiphase media, mainly "liquid + liquid + gas + suspended solids + solids", including the creation of a vortex flow supplied under pressure of a multiphase medium, the subsequent centrifugal separation of the media with the removal of light fractions due to the creation of a negative pressure gradient along the axis of the centrifugal separator in the direction opposite to the translational movement of the multiphase medium, and direct-flow removal of the heavier fractions relative to the carrier medium, characterized in that the initial о form a mixture stream with a Reynolds number value of at least 10 ⁵ in the carrier medium and produce a multi-stage separation of the mixture with the creation of a vortex stream at each stage in a straight-through linear pipeline and sequential centrifugal separation of the media, mainly in the order of decreasing density of the separated media, while on the first stages of liquid + gas separation of the vortex flow form a length of 2-10 diameters of the separation chamber and remove the gas fraction in countercurrent flow, then force straightening and braking ix to form the vortex flow in the axial part of the free-flow channel; at the stage of liquid-liquid separation, the vortex stream forms a length of 80-100 diameters of the separation chamber and light fractions are removed by countercurrent, then the flow is decelerated, while at the stage of separation of the liquid + liquid mixture, 3-5 s before the creation of the vortex stream at a concentration of an oil fraction of more than 50 mg / l in water, an appropriate demulsifier is introduced, and at a concentration of less than 50 mg / l, an electrolyte is introduced; at the stage of separation of equal-density media 3-5 s before the creation of the vortex flow, a sorbent with a density higher than the medium to be removed is introduced, and at the stage of separation of different-density media, suspended solids or mechanical impurities are removed directly through the annular slit of the separation chamber, while the multiplicity of multi-stage separation of the mixture is the required parameter values of each environment. 2. The method according to claim 1, characterized in that at the stage of separation of the mixture "liquid + suspended solids and / or solids" with the content of surface-active substances 3-5 seconds before the creation of the vortex stream, an electrolyte is introduced. 3. The method according to claim 1, characterized in that a 5-7% solution of iron sulfate, or a 5-7% solution of aluminum sulfate, or a 7% solution of zinc sulfate is introduced as an electrolyte. 4. The method according to claim 1, characterized in that the lime solution is added as a sorbent in a concentration of up to 5 wt.%, While the dose of the solution is 50-300 mg / L. 5. A device for separating multiphase media, including a housing, a unit for creating a vortex flow supplied to the housing from a multiphase medium pipeline, made in the form of a hollow central body fixedly installed in the housing with twisting blades rigidly connected to the walls of the housing, and the cavity of the central body is connected to the pipeline removal of a lighter phase, characterized in that the twisting blades are designed to project onto a plane perpendicular to the axis of the flow, overlapping the cross section of the channel in e node creation of the vortex flow, the body is connected with the separation chamber formed as a tube. 6. The device according to claim 5, characterized in that the cavity of the Central body of the node creating the vortex flow is connected to the pipeline for removing the lighter phase through the axial tubular channel. 7. The device according to claim 5, characterized in that in the case of separation of the compressible medium "liquid + gas" behind the node creating a vortex flow at a distance of 2-10 diameters of the separation chamber is placed node forced rectification of the fluid flow, made in the form of fixed, connected with the walls a pipeline of blades, the direction of bending of which is opposite to the direction of bending of the blades of the vortex flow assembly, while a free channel is formed in the axial region between the blades of the flow straightening assembly. 8. The device according to claim 5, characterized in that in the case of separation of different density media "liquid + suspended solids and / or mechanical impurities" behind the site of the creation of the vortex flow at a distance of 0.5-5.0 diameter of the separation chamber is placed node removal heavier phase, made in the form of a collector with an annular gap formed between the flow channel of the separation chamber and the liquid pipe. 9. The device according to claim 5, characterized in that in the case of separation of incompressible media "liquid + liquid" the length of the separation chamber is 80-100 of its diameters. 10. The device according to claim 5, characterized in that in the case of multi-stage separation, a diffuser is placed behind the separation chamber.

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