RU2785705C2 - Method and device for injection mixing of fluids with twisted jets - Google Patents

Abstract

FIELD: oil industry.

SUBSTANCE: inventions relate to technological processes of continuous mixing in static mixers of liquid, gaseous, and other fluids in different industries; they can be used at oil-producing, refining, and petrochemical enterprises in oil preparation for recycling, namely for injection of demulsifier and flushing water into an oil flow and their mixing at desalination stages, as well as in other industries for mixing of the main flow of liquid or gas with smaller amounts of additional liquid or gaseous components. The mixing method consisting in organization of injection of an additional component into separate jets of the processed flow is implemented in a device for injection mixing of fluids with twisted jets, containing a case with a flow chamber for the processed flow and a branch pipe for input of the additional component, connected to the chamber. In the device, there are separate mixing channels located in the flow chamber, formed by tubes evenly distributed along the entire cross-section of the mixer case, providing a calm mode of flowing of the processed flow, while the branch pipe for input of the additional component is connected to an inter-tube space formed by an outer surface of tubes and an inner surface of a cylindrical part of the case, while tubes of the flow chamber have holes with a tangential input direction, a diameter, shape, angle of inclination, number, and mutual location of which in tubes are determined based on condition of achievement of required mixing parameters, providing injection of the additional component with semi-limited submerged jets forming twisted turbulent flows in mixing channels, mixing with separate jets of the processed flow.

EFFECT: increase in the efficiency of desalination of oil.

2 cl, 4 dwg, 2 tbl

Description

The inventions relate to technological processes of continuous mixing in static mixers of liquid, gaseous and other fluids in various industries, and can be used at oil producing, oil refining and petrochemical enterprises in the preparation of oil for processing, namely for introducing a demulsifier and wash water into the oil flow and their mixing before the desalting stage, as well as in other industries for mixing the main liquid or gas stream with smaller amounts of additional liquid or gaseous components. The efficiency of oil desalination, which is characterized by the specific consumption of the demulsifier and washing water with a satisfactory oil quality, depends on their optimal use, which is achieved by devices for intensifying their distribution in the treated stream. Another indicator of efficiency is the energy component of the preparation process - the pressure of the processed flow to overcome the hydraulic resistance in the production line. Local hydraulic resistances are used in static mixers for intensive mixing of liquids due to flow disturbance and turbulence, a side effect of which is a high dispersion of the oil emulsion and an increase in its stability, which entails an increase in oil treatment costs. Therefore, achieving optimal mixing parameters of the demulsifier and wash water is a key factor affecting the efficiency of oil desalination.

The prior art method of mixing in a diaphragm mixer (Yu.K. Molokanov "Processes and apparatus for oil and gas processing." - M.: Chemistry, 1980, 408 pages), in which the device is a system of partitions (diaphragms) installed in the pipeline, through which mixed liquids are pumped. When the liquid flow passes through the holes in the partitions, it becomes turbulent, leading to intensive mixing of the pumped liquids.

The disadvantage of the known method of mixing is a significant hydrodynamic resistance to flow, which leads to blocking (squeezing) of the liquid with a lower flow rate and pumping pressure, which, in turn, leads to a violation of the volume ratio of the mixed liquids.

A liquid mixer is also known (RF patent 2230882, IPC E21V 33/13, V28C 5/02, publ. 06/20/2006), including nozzles, one of which is made for mixing liquid with a lower flow rate, and a pipeline with an installed partition. The branch pipe for liquid with a lower flow rate is placed coaxially in the pipeline and is perforated along a helical line along the entire length with a total area of the perforation holes equal to or greater than the sectional area of the branch pipe. The partition of the pipeline is made in the form of a tape wound on a perforated branch pipe to form a spiral channel for the main liquid flow and with the possibility of preventing this liquid flow from blocking the liquid flow with a lower flow rate in the branch pipe.

The disadvantages of the mixing method using the known device are the low intensity of mixing of the liquid phases in the spiral channel due to the high speed of movement of the main fluid flow and the impossibility of regulating the supply of the mixed liquid with a lower flow rate when changing the supply of the main liquid.

A mixer is also known (see RF patent 126623, IPC B01F5/02, publ. 04/10/2013), containing a housing with a flow chamber for the main liquid flow and an additional liquid input channel connected to it, the latter is made in the form of coaxially mounted external and internal nozzles . The nozzles of the specified nozzles are located mutually overlapping with the possibility of changing the area of the passage section. A grate is installed in front of the nozzles in the direction of the main flow, and a dispersant is installed behind the nozzles.

The disadvantage of the mixing method using the known device is incomplete, partial coverage of the cross-sectional area of the processed flow at the stage of input and distribution of the liquid component, as a result of which the intensity of mixing of liquids is achieved due to hydrodynamic perturbation and turbulence of the flow using a grate and a dispersant, creating a pressure drop across the device.

In addition, a jet injection mixer is known (see RF patent 2643967, IPC B01F5 / 04, B01F5 / 06, publ. 02/06/2018), containing a housing with a flow chamber for the processed liquid flow and an additional component input pipe connected to it. separate flow channels are made located in the flow chamber, made of tubes evenly distributed over the entire cross section of the mixer body, providing a calm flow of the main flow, and the inlet pipe of the additional component is connected to the annular space formed by the outer surface of the tubes and the inner surface of the cylindrical part of the body, at the same time, inlet holes are uniformly distributed over the surface of the tubes, the diameter, shape, number and relative position of which is determined from the condition for achieving optimal mixing characteristics, and through which the additional component in the form of free flooded jets with a turbulent flow regime enters from the duct space of the body into the pipe space, distributing through separate channels and mixing with separate jets of the processed flow.

The disadvantage of the mixing method using the known device is incomplete, partial coverage of the cross-sectional area of the processed flow at the stage of input and distribution of the component due to the use of the radial direction of input with the formation of free direct-flow jets, as evidenced by the indication in the formula and description of the invention of the type of jets created - “free ... jets”, in contrast to the tangential direction of injection, known as more efficient for mixing, with the formation of semi-limited swirling jets (from sources: Lyakhovsky D.N. Turbulence in direct-flow and swirling jets // Theory and Practice of Gas Burning. L. : Nedra, 1964. v. II. - pp. 18-48; Gupta A. et al. Swirling flows: Translated from English / Gupta A., Lilly D., Saired N. - M .: Mir, 1987. - 588 p.).

Known technical solution and accepted as a prototype for the claimed inventions.

The technical result achieved by the proposed inventions is to increase the efficiency of oil desalination, which is expressed in improving the quality of oil treatment, reducing the cost of thermal, chemical and electrical effects due to a decrease in the stability of the oil emulsion, reducing the cost of washing water supply while ensuring optimal mixing quality through optimal distribution of the demulsifier and wash water over the entire cross-sectional area of the processed oil flow, not due to high-intensity large-scale mixing in a single volume, but due to injection mixing with swirling jets in separate mixing channels uniformly distributed over the entire cross-section of the processed flow.

The technical challenge facing the author is to create an effective method and easy-to-execute device for mixing fluids with low hydraulic resistance, which allows for optimal input - distribution of the demulsifier and wash water in the treated oil stream in order to further desalt the latter.

The problem underlying the present inventions is solved by organizing the injection of swirling jets of an additional component into separate jets of the processed stream using an injection mixer containing a body, the flow chamber of which has mixing channels made of separate tubes having tangentially directed inlet holes through which In swirling jets, an additional component enters the processed flow.

In addition, on the outer cylindrical surface of the housing there is a branch pipe for introducing an additional component into the annulus.

In addition, the body is sealed from the ends with covers having through holes, the number and diameter of which corresponds to the number and diameter of the tubes, and having annular grooves for centering both the body itself and all tubes, and to make the entire structure tight, the grooves are sealed with gasket material; the covers are pulled together with pins installed in the holes located on the periphery of the covers.

In addition, adapter pipes with flanges or for welding are mounted to the covers for connection with the pipeline in the form of a diffuser at the inlet and a confuser at the outlet of the processed stream, which contributes to additional mixing of the mixture components and makes it possible to assemble and disassemble the device during maintenance.

The transition of the separation chamber to separate channels with a total cross-sectional area equal to or greater than the cross-sectional area of the supply pipeline allows the processed flow to be divided into separate small flows, thereby ensuring a calm flow regime and equalization of velocities in the internal space of the mixing channels with the almost complete absence of pressure drop across the device .

The characteristics necessary for the technological process: the efficiency and intensity of mixing, are provided by the device parameters determined by the calculation: the number, diameter, mutual arrangement of tubes and inlet holes that form jets of the additional component dispersed in individual channels of the processed flow.

The shape of the inlet holes from the proposed options, as well as the angle of inclination of their axis relative to the flow direction, is selected based on the required dispersion of the additional component, determined empirically, for example, by a microscopic method.

Uniform placement of the tubes over the entire cross-sectional area of the mixer body ensures maximum coverage of the processed flow, and the distance between the tubes of the channels is determined from the condition of the flow of the introduced additional component without the formation of a pressure drop.

Adjustment of the device is not required, the design is initially calculated for the specified technological parameters of the process, but if it is necessary to change the flow rate of the processed or additional flows, the recalculation is made for new technological parameters of the geometric dimensions according to the formulas below and the replacement of tubes with modified characteristics of the inlet holes (number, diameter, shape and location ).

The simplicity and compactness of the design, which does not require additional alignment and adjustment of the device, makes it easy to assemble - disassemble, install - dismantle and maintain the mixer.

The combination of design features of the proposed mixer significantly reduces energy costs while achieving optimal parameters for the process of mixing the demulsifier and water with oil and, as a result, the effective desalination of the latter.

The listed features are essential and interconnected with the formation of a stable set of essential features sufficient to obtain the specified technical result.

The comparative analysis of the proposed technical solution with the identified analogues of the prior art showed that it differs from the known analogues, therefore the claimed inventions are new. The claimed distinguishing features of the inventions do not explicitly follow from the prior art, are not obvious to the average specialist in the field of mixing gas-liquid media, and therefore, we believe that the claimed inventions have an inventive step. Taking into account the possibility of industrial batch production of the mixer and the use of the method in production, the inventions can be considered industrially applicable, and as a result, it can be concluded that they meet the patentability criteria.

The present inventions are illustrated by specific examples of calculation and execution of an injection mixer and application of the method of injection mixing of fluids with swirling jets, which clearly demonstrates the possibility of obtaining the specified technical result. Various modifications and improvements are allowed that do not go beyond the scope of the inventions defined by the attached claims.

The presented embodiment and use of the inventions is described below on the basis of the presented drawings, where:

- in Fig. 1 shows a general view of the mixer;

- in Fig. 2 shows a cross section A of the mixer body;

- in Fig. 3 shows the remote elements B and C with a tangential input;

- in Fig. 4 shows a schematic diagram of the desalination stage.

The design of the injection mixer is prefabricated, it consists of a cylindrical body 1 made of a section of a pipe of a standard assortment, on the outside of which a branch pipe 2 is mounted for introducing an additional component into the annular space of the body 3, ending in a fitting 4 with a mounting thread. The body 1 is sealed at the ends with covers 5, which have through holes 6, the number and diameter of which corresponds to the number and inner diameter of the tubes 7, which, on the one hand, serve as channels for mixing, and on the other hand, the function of devices for injecting an additional component under pressure. Between the tubes 7 there is a space 3 sufficient for the unhindered introduction of the additional component, and the tubes 7 themselves have inlet holes 8 to form the required shape and length of the jet. The number, diameter, shape and relative position of the inlet holes may vary depending on the required mixing characteristics (intensity and efficiency). Covers 5 on the inside have annular grooves 9 and 10 for centering both the body 1 and individual tubes 7. To make the whole structure tight, the grooves are sealed with ring gaskets 11 and 12, and the covers 5 are tightened with studs 13 with nuts 14 installed in the holes 15, located on the peripheral circumference of the covers 5. The transition pipes 16 of the distribution and collection chambers with mounting flanges 17 for connection with the pipeline are mounted to the covers 5.

The treated flow enters the injection mixer through the inlet mounting flange 17, enters the diffuser of the distribution chamber formed by the inner surface of the transition pipe 16 and the perforated surface of the outer side of the cover 5, is distributed through separate mixing channels made of tubes 7 with calculated dimensions (length, diameter and wall thickness). The flow regime in the tubes changes to a quieter one, which creates conditions for a layer-by-layer, unperturbed flow, which provides a low shear rate when the processed flow is mixed with an additional component. The additive component is fed into the mixer through the nozzle 2, enters the annular space 3 of the housing 1 and, washing the outer surface of the tubes 7, is injected through the inlet holes 8 and mixes with the processed flow in the tube space. Separate flows from the mixing channels formed by tubes 7 enter the confuser of the collection chamber, formed similarly to the distribution chamber - the inner surface of the transition pipe 16 and the perforated surface of the outer side of the cover 5, where the introduced additional component is additionally mixed due to the vortices formed by the narrowing of the confuser, after which the finished the mixture leaves the mixer through the outlet mounting flange 17.

The number, diameter, wall thickness and length of tubes 7 are calculated based on the condition of ensuring the total cross-sectional area of the tubes is equal to or greater than the cross-sectional area of the inlet oil pipeline without changing the flow rate in the tubes and with reducing the turbulence of the processed flow and transferring it to the laminar regime. The distance between the tubes 7 is determined from the conditions of uniform coverage of the entire area of the inner surface of the caps 5 and the annulus 3, sufficient for the unimpeded movement of the introduced component.

The number, diameter, shape and relative position of the inlet holes 8 in the tubes 7 are calculated based on the conditions for the formation of free flooded jets with a turbulent regime, and the shape and angle of inclination of the inlet holes 8 relative to the axis of the tubes 7 are selected depending on the required mixing efficiency, in order to provide the necessary the degree of dispersion of the mixture, determined empirically, for example, using a microscopic research method.

The supply pressure of the additional component is created more than the pressure of the processed stream, while the specific value of the pressure difference is calculated depending on the physical characteristics of the mixed media and the geometry of the inlet holes, which is determined empirically.

The calculation of the main structural dimensions is quite simple, does not require special programs, as it is based on geometric and hydrodynamic dependencies, subject to the above conditions.

Table 1 presents the algorithm for calculating the main parameters of the device using the example of mixing fresh water with dehydrated oil at the desalination stage.

Table 1 - Calculation of the main parameters of the injection mixer

No. Parameters Unit rev. Notation and formulas Values one 2 3 4 five one Processed stream - dry oil 1.1 Kinematic viscosity m ² /s Νp 0.000221 1.2 Consumption m ³ / s Qp 0.1319 1.3 Operating pressure kgf / cm ² Pp 3.0 2 Process flow supply line 2.1 Outside diameter mm Dnp 273 2.2 Wall thickness mm Tp 11.5 2.3 Inner diameter mm Dvp \u003d Dnp-2 * tp 250 2.4 Cross-sectional area m ²

0.04906 2.5 Oil flow rate m/s Vp=qp/Sp 2.7 2.6 Reynolds number -

3046 2.7 flow regime - Rep > 2100 turbulence 3 Process flow tubes 3.1 Tube outer diameter mm Dnt 22.0 3.2 Tube wall thickness mm Tt 3.0 3.3 Tube inner diameter mm Dvt \u003d Dnt - 2 * t 16.0 3.4 Cross-sectional area of the tube m ²

0.000201 3.5 The number of tubes from the condition of equal patency PC Nt = Sp / St 244 3.6 Process flow through one tube m ³ / s qt = qp / Nt 0.000541 3.7 Reynolds number for tube flow -

268 3.8 Flow regime in the tube - Ret << 2300 laminar 4 Mixer body 4.1 Cover area occupied by tubes m ²

0.09271 4.2 Excess of the entire area of the inner part of the cover relative to the area occupied by the tubes once k 2.0 4.3 Int. area cover parts m ² Skr = k * Skrt 0.18541 4.4 Internal minimum body diameter mm

496 4.5 Shell wall thickness (GOST 8732-78) mm Tk 6.0 4.6 The nearest larger outer diameter (GOST 8732-78) mm Dnk 530 4.7 Body inner diameter mm Dvk \u003d Dnk - 2 * tk 518 4.8 Case cross-sectional area m ²

0.21063 4.9 Minimum distance between tubes and housing mm Ht 5.0

Table 1 continued - Calculation of the main parameters of the injection mixer

one 2 3 4 five 4.10 Seal thickness mm Hp 1.5 4.11 The length of the tubes from the condition of equal patency of the additional component between the tubes mm Lt \u003d (Sk / 2 * ht) + hp 120 4.12 Body cylinder length mm Lc \u003d Lt 120 4.13 The thickness of the covers of the mixer body for blind flanges Ru-16 mm Hk thirty 4.14 Number of studs for DN and PN-16 PC Nsh twenty 4.15 Stud diameter for DN and PN-16 mm Dsh thirty 4.16 Nut height mm Hg 24 4.17 Stud length mm Lsh \u003d Lc + 2 * hk + 2 * hg + 2 * 10 276 4.18 The length of the threaded part of the studs mm Lshr \u003d (Lsh-Lc) / 2 78 4.19 Reducer length mm L lane 615 4.20 Flange thickness Ru-16 mm Hf 28 4.21 Mounting length of the device mm Lu=Lc+2*hk+2*Lper+2*hf 1486 five Introduced component - fresh water 5.1 Density kg / m ³ Ρk 1000 5.2 Kinematic viscosity m ² /s NK 0.000478 5.3 Consumption m ³ / s Qk 0.007917 5.4 Operating pressure kgf / cm ² Pk = Pp + ΔPk 3.5 6 Inlet pipeline of the input component 6.1 Outside diameter mm Dnk 45 6.2 Wall thickness mm Tk 3.2 6.3 Inner diameter mm Dvk \u003d Dnk-2 * tk 38.6 6.4 Cross-sectional area m ² Sk \u003d π / Dvk ² 0.00117 7 Tubing inlets for additional component 7.1 Inlet diameter mm Do 1.3 7.2 Hole area m ² So = π/4Do ² 0.00000133 7.3 Consumption of a component introduced into one tube m ³ / s qkt = qk/Nt 0.0000324 7.4 Reynolds number for turbulence of a free submerged jet (Rets > 10) - Rets 23 7.5 Flow rate through the hole from the jet turbulence condition m/s

0.0000127 7.6 Component injection rate through holes in the tube m/s Vo = qo / So 8.375 7.7 Estimated number of holes PC No = qkt/qo 3 7.8 Pressure drop across the hole for forming a jet of the additional component kgf / cm ²

0.5 7.9 Distance between inlets mm Lo = Lt / (No + 1) thirty 7.10 Distance from the end of the tube to the inlet mm L1o = Lo thirty 7.11 Angle of rotation of the axis of the holes on the tube cylinder º α = 360º / No 120

- according to the known parameters of the processed flow (clauses 1.1-1.3) and the dimensions of the supply pipeline (clauses 2.1, 2.2), the geometric characteristics (clauses 2.3, 2.4), the flow rate and the flow regime in the pipeline (clauses 2.5-2.7) are determined;

- from the standard range of GOST 8734 - 75, the diameters and thickness of the tubes are selected (clauses 3.1, 3.2) for pipes in the range of outer diameters from 10 to 25 mm, after which one option is selected from them based on considerations of expediency and ease of manufacture of the device, geometric characteristics of the tubes (clauses 3.3, 3.4), as well as the number of tubes themselves (clause 3.5) from the condition of ensuring equal cross-section of the supply pipeline and the sum of the sections of all tubes of the device;

- according to the data obtained, the flow rate of the processed flow through one tube (section 3.6.) and the flow regime in the tube (sections 3.7, 3.8) are calculated taking into account the transfer from turbulent to laminar regime.

- based on a 4-fold excess of the entire area of the cover (clause 4.3) to the area of the part occupied by tubes (clause 4.1), taking into account the thickness of the body (clause 4.5) and the minimum distance between the tubes and the inner surface of the body (clause 4.10) , the minimum outer diameter of the cylindrical part of the mixer body is determined (clause 4.6), then the nearest larger outer diameter of the casing (clause 4.7) is selected from the standard series GOST 8732 - 78, the inner diameter (clause 4.8) and the cross-sectional area of the pipeline (clause 4.8) are found. 4.9);

- according to the known geometric characteristics of the supply pipeline of the additional component (clauses 6.1, 6.2) and the specified distance between the tubes (clause 4.10), the length of the tubes and the length of the cylindrical part of the body (clauses 4.12, 4.13) are determined from the condition of ensuring equal cross-section of the component's supply pipeline and the space formed by the distance between the tubes and covers of the device;

- based on the dimensions of the cylindrical part of the body, the dimensions of all parts are calculated and selected from the standard series (clauses 4.14 - 4.23);

- according to the known characteristics of the additional component (clauses 5.1, 5.2) and the parameters of the pipeline (clauses 6.1, 6.2), based on the consideration of the feasibility, the value of the diameter of the inlet is selected and the required flow rate of the component through one inlet is determined (clause 7.3) for conditions for guaranteed excess of the Reynolds number for the flow in the inlet (section 7.4) to the critical value of the transition of the flow regime from laminar to turbulent, corresponding to 10 units (according to the source: Experimental study of submerged jets at low Reynolds numbers / V.V. Lemanov, V. I. Terekhov, K. A. Sharov, A. A. Shumeiko / Letters to ZhTF, 2013, volume 39, issue 9, pp. 34-40);

- according to the data obtained, the number of holes is determined (clause 7.7) and their location on the tube (clauses 7.9 - 7.11), taking into account their uniform placement on the cylindrical surface of the tube;

- according to the obtained values of the cross-sectional area of the inlet (clause 7.2) and the component flow required through it (clause 7.5.), the flow rate (clause 7.6) and the pressure loss (clause 7.8) of the component in the inlet are determined, and based on the known the value of the pressure of the processed stream (clause 1.3), the pressure of the additional component is determined (clause 5.4).

Most of the parts of the injection mixer are standardized and produced by the industry, and the design of the device is simple and can be manufactured by means of mechanical repair services of manufacturing enterprises and is characterized by compactness and ease of operation.

The proposed technical solution for injection mixing of components in the treated stream increases the efficiency of introducing and distributing the demulsifier and wash water in the crude oil stream and subsequently significantly improves the desalting process.

An example of the application of the method using the device. In FIG. 4 is a schematic diagram of an oil desalting stage used to treat oil in oil fields and refineries. Unprepared crude oil is fed to the inlet of the desalter 18, where a demulsifier and fresh water are alternately added to the crude oil stream through injection mixers 19 and 20. The desalinated oil is removed from the desalter 18 and sent to the stabilization stage or the final separation unit. Mineralized water is discharged from the desalter 18 and removed from the desalination stage, after transferring heat to fresh water in the heat exchanger 21.

To confirm the theoretical conclusions about the greater efficiency of the tangential injection, which ensures the swirling of the jets of the injected component in the processed stream, full-scale tests and a comparison of the performance of the oil desalination stage according to the one shown in Fig. 4 scheme using the proposed method and design of the injection mixer and technical solutions for the prototype.

According to the test results, the degree of oil desalination was determined as the ratio of water salinity in desalted oil to its mineralization in the original (crude) oil:

δ _c \ _u003d 1 - (M out / M _in ), (1)

where Ms _in , Ms _out - mineralization of water at the inlet and outlet, mg / dm ³ .

The mineralization of water in crude and desalted oil was determined based on the results of analyzes of oil samples for water content in accordance with GOST R54284-2010 and chloride salts in accordance with GOST 33703-2015, selected in accordance with GOST 2517-2012 at the inlet and outlet of the first stage of desalination, respectively:

M _in = S _in × 100 / W _in , (2)

M out \ _u003d S _out × 100 / W _out , (3)

where S _in , S _out - the salt content in the oil at the inlet and outlet, mg / dm ³ ;

W _in , W _out - the water content in oil at the inlet and outlet, mg / dm ³ .

According to the content of water and chloride salts in oil before and after desalting, the mineralization of water droplets contained in oil before and after desalting was calculated using formulas (2) and (3), and then the degree of desalting was calculated using formula (1) for the proposed design of the mixer and for the prototype.

In accordance with the data of table 2, the use of the proposed mixer, ceteris paribus, increases the degree of desalting of oil by 15% in absolute and 20% in relative terms compared to the prototype, which confirms the higher efficiency of the claimed method and device for injection mixing of fluids swirling streams.

Table 2 - Test results and efficiency of mixers

No. pp Operating parameters of the desalination stage when working with mixers Prototype Suggested mixer one Types of created jets according to characteristic features: Media Properties flooded Limitation Free Semi-restricted Flow Direct-flow twisted 2 Jet entry direction, R / T Radial tangential 3 Water content in oil at the inlet, % 0.50 4 Water content in oil at the outlet, % 0.50 0.50 five The content of salts in oil at the inlet, mg / dm ³ 1000 6 The content of salts in the oil at the outlet, mg / dm ³ 250 100 7 Mineralization of water in oil at the inlet, mg / dm ³ 200000 eight Mineralization of water in oil at the outlet, mg / dm ³ 50000 20000 nine Degree of oil desalination, % 75.0 90.0

Claims (2)

1. The method of injection mixing of fluids with swirling jets, characterized in that the mixing is carried out by injecting an additional component in the form of semi-restricted submerged jets that form swirling turbulent flows in the mixing channels of the processed flow, and the additional component enters from the annular space into the mixing channels due to pressure supply through the inlet holes of the tubes at an angle and at a speed determined by the achievement of the required mixing parameters. 2. Device for injection mixing of fluids by swirling jets, containing a body with a flow chamber for the processed flow and an additional component input pipe connected to it, characterized in that the flow chamber consists of separate mixing channels made of tubes evenly distributed over the entire cross section of the mixer body , and the branch pipe for introducing the additional component is connected to the annular space formed by the outer surface of the tubes and the inner surface of the cylindrical part of the body, while the tubes of the flow chamber have holes with a tangential input direction and ensure the injection of the additional component by semi-limited submerged jets that form swirling turbulent flows in the mixing channels, and the diameter, shape, angle of inclination, number and relative position of the inlet holes in the tubes is determined from the condition of achieving the required mixing parameters.

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