A device and method for realizing rapid separation of large-phase oil-water mixture

Abstract

The present invention discloses a device and method for realizing rapid separation of large-scale oil-water mixtures. The separation device includes one or more cyclone core tubes, which are cyclone sections, tapered sections and flow-stabilizing tubes from bottom to top. The cyclone section is a cylinder with upper and lower openings, and the lower end opening of the cyclone section is an axial inlet, and a spiral blade is provided on the upper part of the axial inlet; the tapered section includes an inner cone section with a certain taper and upper and lower openings, and a sleeve outside the inner cone section, and a plurality of water phase outlets are evenly distributed on the sleeve in an annular direction, and two rows of water holes are axially symmetrically provided on the inner cone section; the flow-stabilizing tube is a cylinder with upper and lower openings, and the lower end of the flow-stabilizing tube penetrates into the inner cone section from the upper opening of the inner cone section and is fixed to the upper part of the cyclone section, and the upper opening of the flow-stabilizing tube is an oil phase outlet. The separation device of the present invention introduces a flow-stabilizing tube to collect large oil droplets near the axial direction of the cyclone section, and has a compact structure, high separation efficiency and stable separation effect.

Description

Technical Field

[0001] The invention relates to the technical field of oil-water separation equipment, and in particular to a device and method for realizing rapid separation of a large-phase oil-water mixture. Background Art

[0002] In current production, the pollutants in oilfield produced fluids are mainly petroleum pollutants. The traditional treatment process for oil-water separation of produced fluids is a combination of three-phase separators, inclined plates, flotation and filtration. The space on offshore platforms is small, and the equipment for the above treatment process occupies a large area. Therefore, cyclone separators with small size, low maintenance cost and high separation efficiency have good application prospects on offshore platforms.

[0003] At present, the more typical cyclone separator is the conical cyclone. The oil-water mixture enters from the tangential inlet of the conical cyclone and forms a cyclone. The oil-water mixture is separated under the action of the cyclone. In order to ensure a high degree of turbulence in the cyclone field, a higher inlet flow rate is required. However, a higher inlet flow rate is likely to cause the droplets formed after the oil-water separation to break up, thereby affecting the separation effect. In addition, the presence of the cone section in the conical cyclone makes it difficult to improve its processing capacity. When multi-stage cyclones are used to increase the processing capacity, the supporting column process is also very complicated.

[0004] In order to solve the above problems, an axial flow cyclone was further proposed. Compared with the conical cyclone, the axial flow cyclone has a higher processing capacity, a lower degree of turbulence, and a lower probability of droplet breakage. For example, the axial flow downhole cyclone oil-water separator (VTPS) proposed by the Institute of Mechanics of the Chinese Academy of Sciences in the "Study on the Influence of Separation Performance of Axial Flow Cyclone Separators" has a compact structure and a large processing capacity, but there are defects such as the attenuation of the intensity of the cyclone in the later stage causing the droplets to diverge, the oil core to be unstable, and the separation effect to be unstable. In addition, patent CN104815768A proposes an axial flow reverse inlet flow channel cyclone, which collects small oil droplets through an enrichment tube to achieve efficient separation. However, the spiral flow channel and reverse inlet of the upper half of the cyclone are the main separation areas, and the cyclone chamber and cone section of the lower half are to further promote the aggregation of small oil droplets and large oil droplets that have been separated, that is, the oil-water mixture has been initially separated when entering the cyclone chamber, and the enrichment tube of the cyclone does not play a role in stabilizing the oil core and flow field.

[0005] Therefore, there is a need to improve the structure of the axial flow cyclone separation device to meet the requirements of compact structure, large processing capacity and stable cyclone field, so as to improve the separation effect of large-scale oil-water mixture and achieve the purpose of rapid separation in a short process. Summary of the invention

[0006] In order to solve the above problems existing in the prior art, the present invention provides a device and method for realizing rapid separation of a large-phase oil-water mixture.

[0007] The technical solution adopted by the present invention is as follows:

[0008] A device for realizing rapid separation of a large-scale oil-water mixture, the device comprising one or more cyclone core tubes, the cyclone core tubes being composed of a cyclone section, a tapered section and a steady flow tube from bottom to top, and the axes of the cyclone section, the tapered section and the steady flow tube coincide, wherein:

[0009] The swirl section is a cylinder with upper and lower openings, the lower end opening of the swirl section is an axial inlet, a spiral blade is provided on the upper part of the axial inlet, and the lower end of the swirl section is fixedly connected to the liquid inlet pipe through a third flange;

[0010] The tapered section includes an inner cone section with a certain taper and upper and lower openings, and a sleeve outside the inner cone section, the inner cone section is of the same height as the sleeve, a plurality of water phase outlets are evenly distributed annularly on the sleeve, two rows of water discharge holes are axially symmetrically provided on the inner cone section, the diameters of the upper opening and the lower opening of the inner cone section are respectively the same as the diameters of the flow stabilizing tube and the swirl section, and the upper end and the lower end of the inner cone section are respectively fixedly connected to the flow stabilizing tube and the swirl section through a first flange and a second flange;

[0011] The flow stabilizing tube is a cylinder with upper and lower openings. The lower end of the flow stabilizing tube passes through the first flange, penetrates into the inner cone section from the upper opening of the inner cone section, and is fixed to the upper part of the swirl section. The upper opening of the flow stabilizing tube is an oil phase outlet.

[0012] Furthermore, when the device is configured with two or more swirl core tubes according to actual use requirements, the swirl core tubes are connected in parallel and connected to the distribution pipe through a third flange for positioning, and the swirl core tubes are arranged in parallel, wherein the distribution pipe is the liquid inlet pipe.

[0013] Furthermore, the portion of the flow stabilizing tube above the first flange is the outlet section, and the portion below the first flange is the flow stabilizing section.

[0014] Further, the diameter of the swirl section is set to D1 and the length is L1; the diameter of the sleeve of the tapered section is set to D2 and the length is L2, the diameter of the water phase outlet on the sleeve is D6, the distance from the center of the water phase outlet on the sleeve to the upper end of the sleeve is L4, the diameter of the upper opening of the inner cone section is D4, the diameter of the lower opening is D7, the diameter of the water outlet on the inner cone section is D5, and the spacing between the water outlets is L5; the diameter of the steady flow tube is set to D3, the length of the steady flow section of the steady flow tube is L3, and the outlet The length of the segment is L6; the relationship between the above dimensions is: D1 is 40-80mm, L1 / D1=5-8, L1 / L2=1-1.43, D2 / D1=1.5-2.5, D1 / D5=5-5.25, D1 / D6=2.5-2.86, D3=D4, L1 / L3=2-3.33, D1 / D4=2.5-2.86, L4 / D6=2.6-2.8, L5 / D5=1.4-1.6, D1=D7, L6 / D1=0.8-1.2.

[0015] Furthermore, four water phase outlets are evenly distributed in an annular direction on the outer sleeve of the tapered section, and a total of 12-20 water outlet holes are arranged on the inner cone section. The inclination angle α of the inner cone section is 80-85°.

[0016] Furthermore, a deflection section is provided at the upper end of the spiral blade, and a guide section is provided at the lower end thereof. The number of blades of the spiral blade is 4-6, the length of the blade is 110-140 mm, and the inclination angle β of the blade is 30-60°.

[0017] A method for realizing rapid separation of oil-water mixture with a large phase ratio, using the above-mentioned device for realizing rapid separation of oil-water mixture with a large phase ratio to separate oil and water from the oil-water mixture.

[0018] Furthermore, the process includes the following: the oil-water mixture enters from the axial inlet at the lower end of the swirl section of the swirl core tube, and under the action of the spiral blades, the axial movement of the oil-water mixture is converted into swirl movement. Under the action of the swirl, the oil phase and the water phase in the oil-water mixture are separated, and the oil phase enters from the lower end opening of the steady flow tube and is discharged from the oil phase outlet at the upper end of the steady flow tube. After the water phase rises to the tapered section, it is discharged from the water outlet on the inner cone section to the external sleeve, and finally discharged from the water phase outlet on the sleeve.

[0019] Furthermore, the volume fraction of the oil-water mixture is 2-10%, preferably 6-10%.

[0020] The beneficial effects of the present invention are as follows:

[0021] 1. The present invention introduces a flow stabilizing tube structure, which collects large oil droplets near the axis of the swirl section, weakens the divergence of oil droplets caused by the attenuation of the intensity of the swirl in the later stage, solves the problem of unstable separation effect caused by further divergence of oil droplets, stabilizes the oil droplets and the flow field, and breaks through the limitations of traditional methods.

[0022] 2. The cyclone core tube of the present invention has a simple structure, a large inlet area, a large processing capacity, and multiple cyclone core tubes can be arranged in parallel through distribution pipes, so that the processing capacity has a higher operational flexibility.

[0023] 3. The separation device of the present invention can reduce the oil content of the water phase outlet of an oil-water mixture with an oil content of 10% to below 0.08% after cyclone separation, which greatly reduces the processing difficulty and energy consumption required for subsequent processes and has good economic benefits.

[0024] 4. The separation device of the present invention has the characteristics of compact structure, high separation efficiency, stable separation effect, etc. It can realize rapid pretreatment of oil-water mixture in a short process compared with that of the conventional method, and is suitable for the petroleum and petrochemical industry. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 It is a schematic diagram of the three-dimensional structure of the cyclone core tube in the present invention.

[0026] Figure 2 It is a cross-sectional view of the cyclone core tube in the present invention.

[0027] Figure 3 It is a schematic diagram of the three-dimensional structure of the tapered section of the swirl core tube in the present invention.

[0028] Figure 4 It is a top view of the tapered section of the swirl core tube in the present invention.

[0029] Figure 5 for Figure 4 Cross-sectional view along the BB direction.

[0030] Figure 6 It is a schematic diagram of the three-dimensional structure of the flow stabilizing tube of the swirl core tube in the present invention.

[0031] Figure 7 It is a side view of the flow stabilizing tube of the swirl core tube in the present invention.

[0032] Figure 8 It is a schematic diagram of the structure of the spiral blade in the present invention.

[0033] Among them: 10-swirl core tube; 20-swirl section; 30-tapered section; 40-steady flow tube; 21-axial inlet; 22-spiral blade; 23-guide section; 24-baffle section; 31-inner cone section; 32-sleeve; 33-water outlet; 34-water phase outlet; 35-upper opening; 36-lower opening; 41-oil phase outlet, 50-first flange; 51-second flange; 52-third flange. DETAILED DESCRIPTION

[0034] The technical solutions in the embodiments of the present invention are described clearly and completely below. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0035] Example 1: A device for realizing rapid separation of oil-water mixture with large phase ratio

[0036] like Figure 1 and Figure 2 As shown, the separation device includes one or more cyclone core tubes 10, and the cyclone core tube 10 is composed of a cyclone section 20, a tapered section 30 and a flow stabilizing tube 40 from bottom to top, and the axes of the cyclone section 20, the tapered section 30 and the flow stabilizing tube 40 coincide, wherein:

[0037] The swirl section 20 is a cylinder with upper and lower openings. The lower end opening of the swirl section 20 is an axial inlet 21. A spiral blade 22 is provided on the upper part of the axial inlet 21. The lower end of the swirl section 20 is fixedly connected to a liquid inlet pipe (not shown in the figure) through a third flange 52.

[0038] Combination Figure 3-5 As shown, the tapered section 30 includes an inner cone section 31 with a certain taper and upper and lower openings, and a sleeve 32 outside the inner cone section 31, the inner cone section 31 and the sleeve 32 are of the same height, a plurality of water phase outlets 34 are evenly distributed annularly on the sleeve 32, two rows of water discharge holes 33 are axially symmetrically provided on the inner cone section 31, the diameters of the upper opening 35 and the lower opening 36 of the inner cone section 31 are respectively the same as the diameters of the flow stabilizing tube 40 and the swirl section 20, and the upper end and the lower end of the inner cone section 31 are fixedly connected to the flow stabilizing tube 40 and the swirl section 20 through the first flange 50 and the second flange 51, respectively;

[0039] Combination Figure 6 and Figure 7 As shown, the flow stabilizing tube 40 is a cylinder with upper and lower openings. The lower end of the flow stabilizing tube 40 passes through the first flange 50, penetrates into the inner cone section 31 from the upper opening 35 of the inner cone section 31, and is fixed to the upper part of the swirl section 20. The upper opening of the flow stabilizing tube 40 is the oil phase outlet 41.

[0040] Furthermore, when the device is configured with two or more cyclone core tubes 10 according to actual usage requirements, the cyclone core tubes 10 are connected in parallel and connected to the distribution pipe through a third flange 52 for positioning. The cyclone core tubes 10 are arranged in parallel, wherein the distribution pipe is the liquid inlet pipe. For the specific installation method, refer to the assembly diagram of multiple integrated separation core tubes in CN112387013A.

[0041] Furthermore, the portion of the flow stabilizing tube 40 above the first flange 50 is an outlet section, and the portion below the first flange 50 is a flow stabilizing section.

[0042] Further, the diameter of the swirl section 20 is set to D1 and the length is L1; the diameter of the sleeve 32 of the tapered section 30 is set to D2 and the length is L2, the diameter of the water phase outlet 34 on the sleeve 32 is D6, the distance from the center of the water phase outlet 34 on the sleeve 32 to the upper end of the sleeve 32 is L4, the diameter of the upper opening 35 of the inner cone section 31 is D4, the diameter of the lower opening 36 is D7, the diameter of the water outlet 33 on the inner cone section 31 is D5, and the spacing between the water outlets 33 is L5; the diameter of the steady flow tube 40 is set to D3, and the steady flow The length of the steady flow section of the tube 40 is L3, and the length of the outlet section is L6; the relationship between the above dimensions is: D1 is 40-80 mm, L1 / D1=5-8, L1 / L2=1-1.43, D2 / D1=1.5-2.5, D1 / D5=5-5.25, D1 / D6=2.5-2.86, D3=D4, D1=D7, L1 / L3=2-3.33, D1 / D4=2.5-2.86, L4 / D6=2.6-2.8, L5 / D5=1.4-1.6, L6 / D1=0.8-1.2.

[0043] Furthermore, four water phase outlets 34 are evenly distributed in an annular direction on the outer sleeve 32 of the tapered section 30, and a total of 12-20 water outlet holes 33 are arranged on the inner cone section 31. The inclination angle α of the inner cone section 31 is 80-85°.

[0044] Furthermore, if Figure 8 As shown, the upper end of the spiral blade 22 is provided with a deflection section 24, and the lower end thereof is provided with a guide section 23. The number of blades of the spiral blade 22 is 4-6, the length of the blade is 110-140 mm, and the inclination angle β of the blade is 30-60°.

[0045] A separation method for treating a large-scale oil-water mixture using the above-mentioned separation device, the specific process is: the oil-water mixture enters from the axial inlet 21 at the lower end of the swirl section 20 of the swirl core tube 10, and under the action of the spiral blades 22, the axial movement of the oil-water mixture is converted into swirl movement. Under the action of the swirl, the oil phase in the oil-water mixture migrates toward the center of the tube diameter and rises to the vicinity of the lower end opening of the steady flow tube 40. The steady flow tube 40 collects the oil phase and discharges the oil phase from the oil phase outlet 41 at the upper end of the steady flow tube 40. The water phase in the oil-water mixture migrates toward the side wall of the pipe under the action of the swirl, rises to the tapered section 30, and is discharged from the water outlet 33 on the inner cone section 31 to the outer sleeve 32, and finally is discharged from the water phase outlet 34 on the sleeve 32.

[0046] Furthermore, the oil-water mixture is a large-phase oil-water mixture, wherein the volume fraction of the oil phase is 2-10%, preferably 6-10%.

[0047] Example 2: Experimental device for separation of oil-water mixture

[0048] The experimental device used in this embodiment includes a water tank, a water pump, an oil tank, an oil pump, a cyclone core tube, a purified water tank, a purified oil tank, two flow meters, and a number of pipes and valves.

[0049] Among them, the cyclone core tube adopts the cyclone core tube provided in Example 1, and its specific dimensions are: the diameter of the cyclone section is 50mm, the length of the cyclone section is 500mm, the length of the steady flow section is 210mm, the length of the tapering section is 160mm, the outer sleeve diameter is 80mm, the diameter of the water phase outlet is 18mm, the diameter of the water outlet is 10mm, the spacing of the water outlet holes is 15mm, the diameter of the oil phase outlet is 20mm, and 16 water outlet holes are provided on the inner cone section. The length of the spiral blade is 120mm, the number of blades is 6, and the blade inclination angle β is 40°.

[0050] The tap water in the water tank is transported to the cyclone core tube by a water pump, and the water phase flow rate is adjusted and measured by a flow meter. The oil in the oil tank is transported to the cyclone core tube by an oil pump, and the flow rate is adjusted and measured by another flow meter, thereby controlling the inlet oil content and inlet flow rate of the oil-water mixture. The oil-water mixture passes through the cyclone core tube from bottom to top, and most of the water flows from the water phase outlet to the purified water tank, and most of the oil flows out from the oil phase outlet to the purified oil tank.

[0051] The purified water phase and purified oil phase flowing out of the water phase outlet and the oil phase outlet of the cyclone core tube were tested for oil content and oil droplet size distribution, and the separation efficiency η of the cyclone core tube was calculated by the following formula:

[0052]

[0053] In formula (1), c inand c out They represent the oil content of the oil-water mixture at the axial inlet and the oil content in the purified water phase, respectively.

[0054] Example 3: Effect of the flow stabilizing tube on the separation efficiency of the cyclone core tube

[0055] This example uses the experimental device of Example 2 to conduct experiments to study the influence of the flow stabilizing tube on the separation efficiency of the cyclone core tube. First, the oil content of the inlet oil-water mixture is controlled to be 10%. The oil content described in this example and the following examples is calculated by volume fraction. The inlet flow rate is adjusted to 0.3m / s, 0.5m / s, 0.7m / s, and 0.9m / s in sequence. The oil content of the purified water phase at the water phase outlet is measured, and the separation efficiency is calculated. The specific results are shown in Table 1.

[0056] Table 1 Separation efficiency of cyclone core tube with and without flow stabilizing tube at different inlet flow rates

[0057]

[0058] When the inlet flow rate is 0.5m / s, compared with the case without adding a steady flow tube, the separation efficiency of the cyclone core tube after adding a steady flow tube increases from 96.2% to 99.2%, and the oil content of the purified water phase at the water phase outlet decreases from 0.38% to 0.08%, which is a decrease of 3.75 times, and the oil content in the purified water phase is significantly reduced. In addition, the inventors found in the results of experimental research and numerical simulation that in the oil-water separation process, the cyclone core tube without a steady flow tube is difficult to reduce the oil content in the purified water phase to 0.1% or less, and it will also cause the oil droplets at the end of the cyclone section to diverge. It can be seen that the steady flow tube plays a role in enriching the oil phase and improving the separation performance of the cyclone core tube.

[0059] Example 4: Effect of Fluctuation of Oil Content of Inlet Oil-Water Mixture on Separation Efficiency

[0060] This example uses the experimental device of Example 2 to conduct experiments to study the influence of the fluctuation of the inlet oil content on the separation efficiency. Under the condition of an inlet flow rate of 0.5 m / s, the oil content of the oil-water mixture at the inlet is adjusted to 2%, 4%, 6%, 8%, 10%, 12%, and 14% in sequence, the oil content of the purified water phase at the water phase outlet is measured, and the separation efficiency is calculated. The specific results are shown in Table 2.

[0061] Table 2 Effect of inlet oil content fluctuation on separation efficiency

[0062]

[0063] It can be seen from Table 2 that with the increase of the inlet oil content, the separation efficiency of the cyclone core tube first increases and then decreases, but the overall difference is not large, especially when the inlet oil phase volume fraction is 6-10%, the separation efficiency is above 99%, and the oil content at the water phase outlet is below 0.08%. The separation device of the present invention shows good applicability.

[0064] The above shows and describes the basic principles, main features and advantages of the present invention. It should be understood by those skilled in the art that the present invention is not limited to the above embodiments, and the above embodiments and descriptions are only for explaining the principles of the invention. The present invention may be subject to various changes and improvements without departing from the spirit and scope of the present invention, and these changes and improvements fall within the scope of the present invention to be protected. The scope of protection of the present invention is defined by the attached claims and their equivalents.

Claims

1. A device for achieving rapid separation of large-phase oil-water mixture, characterized in that: The device comprises one or more swirl core tubes, which are composed of a swirl section, a tapered section and a steady flow tube from bottom to top, and the axes of the swirl section, the tapered section and the steady flow tube coincide, wherein: The swirl section is a cylinder with upper and lower openings, the lower end opening of the swirl section is an axial inlet, a spiral blade is provided on the upper part of the axial inlet, and the lower end of the swirl section is fixedly connected to the liquid inlet pipe through a third flange; The tapered section includes an inner cone section with a certain taper and upper and lower openings, and a sleeve outside the inner cone section, the inner cone section is of the same height as the sleeve, a plurality of water phase outlets are evenly distributed in an annular direction on the sleeve, two rows of water discharge holes are axially symmetrically provided on the inner cone section, the diameters of the upper opening and the lower opening of the inner cone section are respectively the same as the diameters of the flow stabilizing tube and the swirl section, the upper end and the lower end of the inner cone section are respectively fixedly connected to the flow stabilizing tube and the swirl section through a first flange and a second flange; the taper direction of the inner cone section is inwardly inclined, that is, it is small at the top and large at the bottom; The flow stabilizing tube is a cylinder with upper and lower openings. The lower end of the flow stabilizing tube passes through the first flange, penetrates into the inner cone section from the upper opening of the inner cone section, and is fixed to the upper part of the swirl section. The upper opening of the flow stabilizing tube is an oil phase outlet.

2. The device for realizing rapid separation of oil-water mixture with large ratio according to claim 1, characterized in that: When the device is configured with two or more cyclone core tubes according to actual use requirements, the cyclone core tubes are connected in parallel and connected to the distribution pipe through a third flange for positioning. The cyclone core tubes are arranged in parallel, wherein the distribution pipe is the liquid inlet pipe.

3. The device for realizing rapid separation of oil-water mixture with large ratio according to claim 1, characterized in that: The portion of the flow stabilizing tube above the first flange is the outlet section, and the portion below the first flange is the flow stabilizing section.

4. The device for realizing rapid separation of oil-water mixture with large ratio according to claim 3, characterized in that: The diameter of the swirl section is set to D1 and the length is L1; the diameter of the sleeve of the tapered section is set to D2 and the length is L2, the diameter of the water phase outlet on the sleeve is D6, the distance from the center of the water phase outlet on the sleeve to the upper end of the sleeve is L4, the diameter of the upper opening of the inner cone section is D4, the diameter of the lower opening is D7, the diameter of the water outlet hole on the inner cone section is D5, and the spacing between the water outlet holes is L5; the diameter of the flow stabilizing tube is set to D3, the length of the flow stabilizing section of the flow stabilizing tube is L3, and the length of the outlet section is L4. The degree is L6; the relationship between the above dimensions is: D1 is 40-80mm, L1 / D1=5-8, L1 / L2=1-1.43, D2 / D1=1.5-2.5, D1 / D5=5-5.25, D3=D4, D1=D7, D1 / D6=2.5-2.86, L1 / L3=2-3.33, D1 / D4=2.5-2.86, L4 / D6=2.6-2.8, L5 / D5=1.4-1.6, L6 / D1=0.8-1.

2.

5. The device for realizing rapid separation of large-phase oil-water mixture according to claim 1, characterized in that: Four water phase outlets are evenly distributed in an annular direction on the outer sleeve of the tapered section, and a total of 12-20 water outlet holes are arranged on the inner cone section. The inclination angle α of the inner cone section is 80-85°.

6. The device for realizing rapid separation of oil-water mixture with large ratio according to claim 1, characterized in that: The upper end of the spiral blade is provided with a deflection section, and the lower end thereof is provided with a guide section. The number of blades of the spiral blade is 4-6, the length of the blade is 110-140 mm, and the inclination angle β of the blade is 30-60°.

7. A method for achieving rapid separation of a large-phase oil-water mixture, characterized in that: The oil-water mixture is separated into oil and water using the device for achieving rapid separation of oil-water mixture at a large ratio as described in any one of claims 1 to 6.

8. The method for realizing rapid separation of oil-water mixture with large phase ratio according to claim 7, characterized in that: The process includes the following: the oil-water mixture enters from the axial inlet at the lower end of the swirl section of the swirl core tube; under the action of the spiral blades, the axial movement of the oil-water mixture is converted into swirl movement; under the action of the swirl, the oil phase and the water phase in the oil-water mixture are separated; the oil phase enters from the lower end opening of the steady flow tube and is discharged from the oil phase outlet at the upper end of the steady flow tube; after the water phase rises to the tapered section, it is discharged from the water outlet on the inner cone section to the external sleeve and finally discharged from the water phase outlet on the sleeve.

9. The method for realizing rapid separation of oil-water mixture with large phase ratio according to claim 7, characterized in that: The volume fraction of the oil-water mixture is 2-10%.

10. The method for realizing rapid separation of large-phase oil-water mixture according to claim 7, wherein the volume fraction of the oil-water mixture is 6-10%.

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