Downhole forced derotation particle size reforming and separating device

Abstract

The invention relates to a multiphase medium separation technology in the fields of petroleum, chemical engineering, environmental protection and the like, in particular to an underground forced derotation particle size reforming separation device. The underground forced reverse rotation particle size reforming separation device comprises a first barrel, a second barrel and a third barrel, wherein the first barrel is provided with a cyclone separation cavity, a first inlet and an outlet; the second barrel is arranged on the first barrel in a sleeving mode, a coalescence reforming cavity is defined by the second barrel and the first barrel, the coalescence reforming cavity is communicated with the first inlet, and the second barrel is provided with a second inlet communicated with the coalescence reforming cavity; the first inlet extends in the tangential direction of the circumferential side wall of the first barrel, the extending direction of the first inlet is a first deflection direction relative to the circumferential direction of the first barrel, the second inlet extends in the tangential direction of the circumferential side wall of the second barrel, and the extending direction of the second inlet is a second deflection direction relative to the circumferential direction of the second barrel. The first deflection direction and the second deflection direction are arranged oppositely and are used for adjusting the rotational flow direction of the multiphase medium mixed liquid entering the coalescence reforming cavity, so that the separation efficiency and precision are improved.

Description

Technical Field

[0001] This application relates to multiphase media separation technology in the fields of petroleum, chemical industry, and environmental protection, and in particular to a downhole forced reverse swirl particle reforming separation device. Background Technology

[0002] Achieving economical and efficient oilfield exploitation during the high water-cut phase is a crucial foundation for ensuring national energy security. In-situ injection-production technology, through downhole oil-water separation, plays a key role in stabilizing oil production, controlling water levels, and reducing energy consumption. However, with continuous oilfield development, most of my country's oilfields have entered the mid-to-late stages, with many achieving water cuts exceeding 98%. In high water-cut environments, the oil phase typically disperses in the aqueous phase as tiny oil droplets, forming a stable oil-in-water emulsion. The oil droplet dispersion significantly alters the viscosity of the mixed phase, severely impacting the oil-water separation efficiency of downhole hydrocyclones.

[0003] While current downhole separation devices offer advantages such as small size and fast processing speed, the high-speed rotating flow field inside the hydrocyclone generates strong shear forces and eddies, making oil droplets easily broken up. Furthermore, they are less effective at removing small-diameter particles or oil droplets, limiting their applicability in ultra-high water-cut oil wells. Simultaneously, as reservoir pressure decreases, continuous water injection is necessary to maintain formation pressure. However, for high water-cut oil wells, a large amount of aqueous phase in the produced fluid is lifted to the surface, increasing unnecessary extraction costs and significantly raising the burden on surface wastewater treatment.

[0004] Therefore, in response to the problems of low downhole oil-water separation efficiency and poor separation accuracy in the application of existing same-well injection and production technologies, there is an urgent need for a new downhole separation device. Summary of the Invention

[0005] This application provides a downhole forced counter-rotation particle size reforming separation device, which can perform efficient in-situ separation of multiphase media mixtures downhole. By counter-rotating coalescence and particle size reforming of the discrete phase, it improves the separation efficiency and accuracy of small-diameter discrete phases, thereby optimizing the stability of separation performance. In particular, it enhances the separation capability of small-diameter oil droplets, reduces the decrease in separation efficiency caused by emulsification of fine oil droplets, and improves the purity of oil phase production and reduces the lift of water phase, thereby improving production efficiency from the source and significantly reducing unnecessary economic losses.

[0006] To achieve the above objectives, the technical solution of this application is as follows: This application provides a downhole forced reverse swirl particle reforming and separation device, comprising: a first cylinder having a first end and a second end disposed opposite to each other along its own axial direction; the first cylinder having a swirl separation chamber and a first inlet and an outlet communicating with the swirl separation chamber, one of the first inlet and the outlet being disposed at the first end and the other at the second end; and a second cylinder sleeved on the first cylinder and enclosing the first cylinder to form a coalescing reforming chamber, the coalescing reforming chamber communicating with the first inlet, and the second cylinder having a second inlet communicating with the coalescing reforming chamber, the second inlet being axially opposite to the first inlet of the second cylinder. An overflow pipe is located near the outlet; an overflow pipe is located at one of the first and second ends and is located away from the outlet relative to the first inlet, and the overflow pipe is connected to the swirl separation chamber; wherein, the first inlet extends along the tangential direction of the circumferential sidewall of the first cylinder, and the extension direction of the first inlet is deflected in a first direction relative to the circumference of the first cylinder; the second inlet extends along the tangential direction of the circumferential sidewall of the second cylinder, and the extension direction of the second inlet is deflected in a second direction relative to the circumference of the second cylinder; the first deflection direction and the second deflection direction are set opposite to each other to adjust the swirl direction of the multiphase medium mixture entering the coalescence reforming chamber.

[0007] In one possible implementation, the downhole forced reverse rotation particle reforming separation device provided in this application can have a first deflection direction consistent with a second deflection direction when the first cylinder rotates n ° around its own axis and is mirrored relative to a plane perpendicular to the axial direction, wherein 0 ≤ n < 360.

[0008] In one possible implementation, the downhole forced reverse-swirl particle reforming separation device provided in this application has a coalescing reforming chamber having a first sub-region, a transition region, and a second sub-region arranged sequentially along the axial direction. A first inlet is opened on the outer wall of the first cylinder and is arranged corresponding to the first sub-region, so that the multiphase medium mixture in the first sub-region can form a swirling flow in a first swirling direction. A second inlet is opened on the outer wall of the second cylinder and is arranged corresponding to the second sub-region, so that the multiphase medium mixture in the second sub-region can form a swirling flow in a second swirling direction. The transition region is located between the first sub-region and the second sub-region, and the transition region can include a swirling flow in the first swirling direction and a swirling flow in the second swirling direction, wherein the first swirling direction and the second swirling direction are opposite.

[0009] In one possible implementation, the downhole forced reverse-rotation particle reforming and separation device provided in this application has at least two of the first cylinder, the second cylinder, and the overflow pipe arranged coaxially.

[0010] In one possible implementation, the downhole forced reverse-rotation particle reforming separation device provided in this application has a first end of the first cylinder flush with one end of the second cylinder along the axial direction, a second end of the first cylinder protruding from the other end of the second cylinder along the axial direction, and an outlet disposed close to the second end relative to the first end, so that the outlet is exposed to the outside of the second cylinder.

[0011] In one possible implementation, the downhole forced reverse-rotation particle reforming separation device provided in this application has the following features: the inner diameter of the second cylinder is D1; ​​the axial height of the first cylinder is H1, where D1≤H1≤200×D1; the axial length of the first cylinder protruding beyond the second cylinder is H2, where 0.05×H1≤H2≤0.7×H1; and / or, the maximum inner diameter of the first cylinder is D2, where 0.5×D1≤D2≤0.75×D1.

[0012] In one possible implementation, the downhole forced reverse-rotation particle reforming separation device provided in this application has a portion of the overflow pipe extending axially into the interior of the first cylinder; the axial height of the overflow pipe is H3, where 0.1×H1≤H3≤0.9×H1; and / or, the axial extension length of the overflow pipe within the first cylinder is H4, where 0<H4≤3D1; and / or, the inner diameter of the overflow pipe is D3, where 0.1×D1≤D3≤0.7×D1.

[0013] In one possible implementation, the downhole forced reverse-rotation particle reforming separation device provided in this application has a rectangular cross-sectional shape for the first inlet, the second inlet, and the outlet; the axial height of the second inlet is H5, where 0.05×D1≤H5≤D1; the axial height of the outlet is H6, where 0.5×H5≤H6≤2×H5; the port width of the outlet is L2, where 0.05×D2≤L2≤0.8×D2; the axial height of the first inlet is H7, where 0.05×D1≤H7<D1; and the port width of the first inlet is L3, where 0.05×D1≤L3≤0.8×D1.

[0014] In one possible implementation, the downhole forced reverse-rotation particle reforming separation device provided in this application includes a first cylinder comprising one of a cylinder, a cone, and a cylindrical cone; and / or, the outlet is a tangential outlet arranged circumferentially along the first cylinder, or an axial outlet arranged axially and away from the overflow pipe opening.

[0015] In one possible implementation, the downhole forced reverse swirl particle reforming and separation device provided in this application further includes end caps, which are disposed on both ends of the first cylinder and the second cylinder in the axial direction to seal the first cylinder and the second cylinder.

[0016] The downhole forced reverse swirl particle size reforming and separation device provided in this application includes a first cylinder, a second cylinder, and an overflow pipe. The first cylinder has a first end and a second end disposed opposite to each other along its axial direction. The first cylinder has a swirl separation chamber, a first inlet communicating with the swirl separation chamber, and an outlet. One of the first inlet and the outlet is located at the first end, and the other at the second end. The overflow pipe communicates with the swirl separation chamber and is located away from the outlet relative to the first inlet. Thus, the swirl separation chamber provides a swirl separation space for the multiphase medium mixture, the overflow pipe is used to discharge the separated discrete phase, and the outlet is used to discharge the separated continuous phase. The second cylinder is sleeved on the first cylinder and encloses it to form a coalescing reforming chamber. The coalescing reforming chamber communicates with the first inlet. The second cylinder has a second inlet communicating with the coalescing reforming chamber, and the second inlet is located axially closer to the outlet relative to the first inlet in the second cylinder. The coalescing reforming chamber provides a pre-coalescing space for the multiphase medium mixture before it enters the swirl separation chamber, for preliminary agglomeration treatment of the small-particle-size discrete phase. The first inlet extends tangentially to the circumferential sidewall of the first cylinder, with its extension direction deflected by a first direction relative to the circumference of the first cylinder. The second inlet extends tangentially to the circumferential sidewall of the second cylinder, with its extension direction deflected by a second direction relative to the circumference of the second cylinder. By setting the first and second deflection directions opposite to each other, the turbulent disturbance within the coalescing reforming chamber can be enhanced through the anti-swirl effect, thereby adjusting the swirling direction of the multiphase medium mixture entering the coalescing reforming chamber. This allows the multiphase medium mixture entering the coalescing reforming chamber via the second inlet to form a reverse swirling flow within the chamber before entering the first inlet. This guides the small-diameter discrete phase, originally distributed in the large-radius region of the swirling flow field within the coalescing reforming chamber, to the small-radius region, increasing the probability of collisional coalescence of the small-diameter discrete phase and achieving anti-swirl coalescence and particle size reforming of the discrete phase. This, in turn, increases the radial migration force of the coalesced discrete phase and reduces the probability of the small-diameter discrete phase being discharged from the outlet with the continuous phase. In the coalescence reforming chamber, the coalesced multiphase medium mixture enters the cyclone separation chamber through the first inlet. It can achieve rapid separation of discrete and continuous phases by means of the centrifugal force of the cyclone field, thereby improving separation efficiency and separation accuracy.

[0017] In summary, this application proposes a downhole forced counter-rotating particle size reforming separation device suitable for high water-cut oilfields, which can achieve efficient separation of small-diameter oil droplets in the downhole environment. Compared with conventional separation devices, the downhole forced counter-rotating particle size reforming separation device provided in this application can effectively converge small-diameter oil droplets in the large radius region of the swirling field to the central region and promote the coalescence and growth of small-diameter oil droplets. Simultaneously, this application innovatively utilizes the counter-rotating effect to achieve coalescence and particle size reforming of discrete phase particles. By organically combining the coalescence reforming chamber and the swirling separation chamber with a sleeve-type structure, the coalesced oil droplets can be separated quickly, accurately, and efficiently. This separation device significantly improves the separation accuracy of downhole multiphase media, reduces the energy consumption of unnecessarily lifting large amounts of water phase to the surface, thereby effectively reducing oil production operation costs and significantly improving economic benefits. Attached Figure Description

[0018] To more clearly illustrate the technical solutions in the embodiments of this application or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0019] Figure 1 A schematic diagram of the structure of the downhole forced anti-spin particle size reforming and separation device provided in the embodiments of this application; Figure 2 for Figure 1 Partial sectional view Figure 1 ; Figure 3 for Figure 1 Partial sectional view Figure 2 ; Figure 4 This is a schematic diagram of the structure of the first cylinder provided in an embodiment of this application; Figure 5 This is a schematic diagram of the structure of the second cylinder provided in an embodiment of this application; Figure 6 A schematic diagram of the axial principle of the downhole forced anti-spin particle reforming and separation device provided in the embodiments of this application; Figure 7 for Figure 1 Internal structure diagram; Figure 8 for Figure 7 Sectional view at point AA; Figure 9 for Figure 7 Sectional view at point BB; Figure 10 for Figure 7 Sectional view at CC; Figure 11 This is a schematic diagram showing the dimensions of the downhole forced anti-spin particle reforming and separation device provided in the embodiments of this application; Figure 12 This is a schematic diagram of the internal structure of a downhole forced anti-rotation particle reforming and separation device provided in another embodiment of this application.

[0020] Explanation of reference numerals in the attached figures: 10-Downhole forced reverse-spinning particle size reforming and separation device; 100 - First cylinder; 100a - First end; 100b - Second end; 110 - Swirl separation chamber; 120 - First inlet; 130 - Outlet; 200 - Second cylinder; 210 - Coalescence reforming chamber; 211 - First sub-region; 212 - Transition zone; 213 - Second sub-region; 220 - Second inlet; 300-Overflow pipe; 400-End Cap; X - Axial direction; Y - Circumferential direction; Y1 - First deflection direction; Y2 - Second deflection direction.

[0021] The accompanying drawings illustrate specific embodiments of this application, which will be described in more detail below. These drawings and descriptions are not intended to limit the scope of the concept in any way, but rather to illustrate the concept of this application to those skilled in the art through reference to particular embodiments. Detailed Implementation

[0022] To make the objectives, technical solutions, and advantages of this application clearer, the technical solutions in the preferred embodiments of this application will be described in more detail below with reference to the accompanying drawings. Obviously, the described embodiments are merely some embodiments of this application, not all embodiments. All other embodiments obtained by those skilled in the art based on the embodiments of this application without creative effort are within the scope of protection of this application.

[0023] It should be noted that in the description of the embodiments of this application, the terms "upper", "lower", "inner", "outer" and other terms indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of description, and do not indicate or imply that the device or component must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation on the embodiments of this application.

[0024] Furthermore, it should be noted that the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this application, "multiple" means two or more, unless otherwise explicitly specified.

[0025] In this application, unless otherwise expressly specified and limited, the terms "installation," "connection," "fixation," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a connection that allows communication between them; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication between two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0026] Downhole cyclone separators in related technologies typically include a cavity, an overflow port, an underflow port, and an inlet. After entering the cavity through the inlet, the multiphase medium rotates at high speed within the cavity, generating a centrifugal force field. The denser phase moves towards the cavity wall under the influence of centrifugal force and is discharged through the underflow port; the less dense phase converges towards the central region of the cavity and is discharged through the overflow pipe, thus achieving the separation of the multiphase medium. However, the aforementioned downhole cyclone separators, which are currently the main types used, suffer from low separation efficiency and poor separation accuracy for small-particle-size discrete phases.

[0027] In view of this, this application provides a downhole forced reverse swirl particle size reforming and separation device, comprising a first cylinder, a second cylinder, and an overflow pipe. The first cylinder has a first end and a second end disposed opposite to each other along its own axial direction. The first cylinder has a swirling separation chamber, a first inlet communicating with the swirling separation chamber, and an outlet. One of the first inlet and the outlet is disposed at the first end, and the other is disposed at the second end. The overflow pipe communicates with the swirling separation chamber and is located away from the outlet relative to the first inlet. Thus, the swirling separation chamber provides a swirling separation space for the multiphase medium, the overflow pipe is used to discharge the separated discrete phase, and the outlet is used to discharge the separated continuous phase. The second cylinder is sleeved on the first cylinder and encloses the first cylinder to form a coalescing reforming chamber. The coalescing reforming chamber communicates with the first inlet, and the second cylinder is provided with a second inlet communicating with the coalescing reforming chamber. The second inlet is disposed axially in the second cylinder closer to the outlet relative to the first inlet. The coalescing reforming chamber is used to provide a pre-coalescing space for the multiphase medium before entering the swirling separation chamber, so as to perform preliminary agglomeration treatment on the small-particle-size discrete phase. The first inlet extends tangentially along the circumferential sidewall of the first cylinder, with its extension direction deflected by a first deflection relative to the circumference of the first cylinder. The second inlet extends tangentially along the circumferential sidewall of the second cylinder, with its extension direction deflected by a second deflection relative to the circumference of the second cylinder. By setting the first and second deflection directions opposite to each other, the turbulent disturbance within the coalescing reforming chamber can be enhanced through the anti-swirl effect, thereby adjusting the swirling direction of the multiphase medium entering the coalescing reforming chamber. As a result, the multiphase medium entering the coalescing reforming chamber through the second inlet can form a reverse swirling flow within the coalescing reforming chamber before entering the first inlet, thereby increasing the collisional coalescence probability of the small-particle-size discrete phase, realizing anti-swirl coalescence and particle size reforming of the discrete phase, thereby increasing the radial migration force of the coalesced discrete phase and reducing the probability of the small-particle-size discrete phase being discharged from the outlet along with the continuous phase. After coalescence and reforming, the multiphase medium enters the cyclone separation chamber through the first inlet. It can achieve rapid separation of discrete and continuous phases by means of the centrifugal force of the cyclone field, thereby improving separation efficiency and separation accuracy.

[0028] The present application will now be described in detail with reference to the accompanying drawings and specific embodiments.

[0029] See Figures 1 to 3 This application provides a downhole forced reverse-spinning particle reforming and separation device 10, which consists of... Figures 1 to 3As can be seen, the overall shape is cylindrical, which is convenient for downhole use. The downhole forced reverse swirl particle reforming and separation device 10 includes a first cylinder 100, a second cylinder 200, and an overflow pipe 300. The first cylinder 100 has a first end 100a and a second end 100b arranged opposite to each other along its own axial direction X. The first cylinder 100 has a swirl separation chamber 110 and a first inlet 120 and an outlet 130 communicating with the swirl separation chamber 110. One of the first inlet 120 and the outlet 130 is located at the first end 100a, and the other is located at the second end 100b. The second cylinder 200 is sleeved on the first cylinder 100 and encloses the first cylinder 100 to form a coalescing and reforming chamber 210. The coalescing and reforming chamber 210 communicates with the first inlet 120. The second cylinder 200 is provided with a second inlet 220 communicating with the coalescing and reforming chamber 210, and the second inlet 220 is positioned in the axial direction X of the second cylinder 200 relative to the first inlet 120 and closer to the outlet 130. An overflow pipe 300 is provided at one of the first end 100a and the second end 100b and is located away from the outlet 130 relative to the first inlet 120. The overflow pipe 300 communicates with the vortex separation chamber 110. The first inlet 120 extends along the tangent direction of the circumferential Y-side wall of the first cylinder 100, and the extension direction of the first inlet 120 is deflected in a first deflection direction Y1 relative to the circumferential Y of the first cylinder 100. The second inlet 220 extends along the tangent direction of the circumferential Y-side wall of the second cylinder 200, and the extension direction of the second inlet 220 is deflected in a second deflection direction Y2 relative to the circumferential Y of the second cylinder 200. The first deflection direction Y1 and the second deflection direction Y2 are set opposite to each other to adjust the swirling direction of the multiphase medium mixture entering the coalescence reforming chamber 210.

[0030] The first cylindrical body 100 has a first end 100a and a second end 100b arranged opposite each other along the axial direction X. The first cylindrical body 100 may have a hollow structure to form a swirling separation chamber 110 inside. The swirling separation chamber 110 can provide swirling motion space for the multiphase medium, ensuring that the multiphase medium mixture can achieve separation of the discrete phase and the continuous phase through centrifugal force within the swirling separation chamber 110. See also Figure 4 The first cylinder 100 is further provided with a first inlet 120 and an outlet 130 communicating with the cyclone separation chamber 110. Specifically, the first inlet 120 can be located at the first end 100a and the outlet 130 at the second end 100b; or, the first inlet 120 can be located at the second end 100b and the outlet 130 at the first end 100a. For example, the first inlet 120 is located at the first end 100a and the outlet 130 is located at the second end 100b, thereby extending the movement path of the multiphase medium mixture within the cyclone separation chamber 110 to ensure more thorough separation of the discrete phase and the continuous phase.

[0031] It should be noted that a multiphase medium mixture can be a gas-liquid mixture, a liquid-liquid mixture, or a solid-liquid mixture. The discrete phase can be understood as a substance existing in a dispersed form within the continuous phase in a multiphase medium, while the continuous phase can be understood as a substance that can continuously fill the entire space in a multiphase medium.

[0032] The overflow pipe 300 is used to discharge the discrete phase. Optionally, the overflow pipe 300 can be positioned away from the outlet 130 relative to the first inlet 120. When the multiphase medium mixture is in the cyclone separation chamber 110, the multiphase medium will form a cyclone motion under the action of centrifugal force: the continuous phase with a higher density will move towards the inner wall of the first cylinder 100 due to the greater centrifugal force, and flow along the inner wall to the outlet 130 for discharge; while the discrete phase with a lower density will gather towards the center of the cyclone field due to the relatively smaller centrifugal force. As the continuous phase is continuously discharged from the outlet 130, an axial X-flow will be formed in the center of the cyclone field, which is opposite to the discharge direction of the continuous phase. The driving force generated by the upward flow can overcome the gravity of the discrete phase itself, and drive the discrete phase gathered in the center of the cyclone field to continuously move towards the overflow pipe 300. Thus, the discrete phase can be discharged through the overflow pipe 300.

[0033] It should be noted that, in order to reduce the probability of small-particle-size discrete phase being discharged from outlet 130 along with the continuous phase, see [reference needed]. Figure 2 and Figure 5 A second cylinder 200 can be fitted over the outer side of the first cylinder 100. A coalescing and reforming chamber 210 is formed between the first cylinder 100 and the second cylinder 200. The coalescing and reforming chamber 210 can be an annular chamber. By setting the coalescing and reforming chamber 210, anti-swirl coalescing treatment can be provided for the multiphase medium mixture before it enters the swirling separation chamber 110. By guiding the small-diameter light discrete phase, which was originally distributed in the large radius region of the swirling flow field of the coalescing and reforming chamber 210, to the small radius region of the swirling flow field of the coalescing and reforming chamber 210, the collision probability of the small-diameter discrete phase is enhanced, and the small-diameter discrete phase is agglomerated into a larger-diameter discrete phase, so that it can be more easily separated in the swirling separation chamber 110. In a specific implementation, the second cylinder 200 may be provided with a second inlet 220 that communicates with the coalescing reforming chamber 210. The second inlet 220 is located closer to the outlet 130 than the first inlet 120. The extension direction of the first inlet 120 is deflected by a first deflection direction Y1 relative to the circumferential Y of the first cylinder 100, and the extension direction of the second inlet 220 is deflected by a second deflection direction Y2 relative to the circumferential Y of the second cylinder 200. The first deflection direction Y1 and the second deflection direction Y2 are set opposite to each other.

[0034] Among them, see Figure 10The first deflection direction Y1 can be understood as the direction in which the first inlet 120 is inclined in a certain direction (such as counterclockwise) along the tangent of the outer wall of the first cylinder 100. The second deflection direction Y2 can be understood as the direction in which the second inlet 220 is inclined in a circumferential direction (such as clockwise) opposite to the first deflection direction Y1 along the tangent of the outer wall of the second cylinder 200.

[0035] Optionally, the positions of the first inlet 120 and the second inlet 220 in the circumferential Y direction can be adjusted according to the actual working conditions, as long as the deflection directions of the first inlet 120 and the second inlet 220 are opposite.

[0036] See Figures 6 to 10 The following explanation uses water as the continuous phase and oil as the discrete phase. When the oil-water mixture enters the coalescence reforming chamber 210 through the second inlet 220, guided by the second deflection direction Y2, the mixture forms a swirling flow with a second rotation direction and moves along a spiral path towards the first inlet 120. Because oil droplets of different sizes experience different centrifugal forces, their rotational speeds differ, increasing the probability of collisions between droplets. During collisions, the oil droplets rupture the interfacial film through mutual compression, subsequently coalescing to form larger droplets. Through coalescence, some small oil droplets are transformed into larger droplets, thereby improving the separation efficiency. Furthermore, since the first inlet 120 and the second inlet 220 have opposite deflection directions, they will guide the swirling flow field in the coalescing reforming chamber 210, and can adjust the direction of the swirling flow field in the coalescing reforming chamber 210. For example, the counterclockwise direction of the swirling flow field can be forcibly changed to clockwise, thereby generating a counter-swirl effect. This guides the small-diameter oil droplets that were originally distributed in the large radius region of the swirling flow field in the coalescing reforming chamber 210 to the small radius region of the swirling flow field in the coalescing reforming chamber 210. This causes the small-diameter oil droplets that are entrained in the water to break away from their original motion state with the water flow, resulting in turbulence and deflection of their motion trajectory, and increasing the probability of collision between small-diameter oil droplets. Small-diameter oil droplets will gradually agglomerate through collisions to form larger-diameter oil droplets. When the larger-diameter oil droplets enter the cyclone separation chamber 110, they will be subjected to stronger centrifugal force (or radial migration force) due to their greater mass, making them more likely to aggregate towards the center of the cyclone. This avoids being carried away by the continuous phase and effectively reduces the probability of small-diameter oil droplets being discharged from the outlet 130 with the aqueous phase.

[0037] For example, the principle that the first deflection direction Y1 and the second deflection direction Y2 are set in opposite directions, which can adjust the swirling direction of the multiphase medium entering the coalescing reforming chamber 210, can be understood as follows: When the multiphase medium entering the coalescing reforming chamber 210 through the second inlet 220 forms a counterclockwise swirling flow under the guidance of the second deflection direction Y2, since the first deflection direction Y1 of the first inlet 120 corresponds to the guiding requirement of the clockwise swirling flow, when the counterclockwise swirling flow guided by the second inlet 220 moves towards the first inlet 120, it will be subjected to a continuous reverse guiding force from the first inlet 120. The reverse guiding force will gradually change the stable motion state of the counterclockwise swirling flow. As the multiphase medium continues to approach the first inlet 120, the effect of the reverse guiding force gradually increases, causing the rotation direction of the multiphase medium mixture to slowly change from counterclockwise to clockwise, and finally enter the first inlet 120 in a clockwise direction.

[0038] It should also be noted that, in the embodiments of this application, the path of the oil droplet's reverse rotation can be described by a segmented helix. Taking the initial swirling field as a counterclockwise rotation as an example, the oil droplet rotates from counterclockwise to clockwise along the helical path towards the first inlet 120 within the coalescence reforming chamber 210. Its path at the lower end of the coalescence reforming chamber 210 is as follows:

[0039] At the upper end of the coalescence reforming chamber 210, the oil droplet's counter-rotation is clockwise, and its path is as follows:

[0040] After passing through the coalescence reforming chamber 210, the oil droplets continue to rotate clockwise and enter the cyclone separation chamber 110 through the first inlet 120. The path is as follows:

[0041] in, This is a polar angle variable, representing the angle by which the oil droplet rotates around the central axis; r 11 , r 12 These are the counterclockwise rotation radius at the lower end and the clockwise rotation radius at the upper end of the coalescing reforming chamber 210, respectively. r 2 The radius of rotation of the cyclone separation chamber 110; β 11 , β 12 These represent the counterclockwise helix angle at the lower end and the clockwise helix angle at the upper end of the coalescing reforming chamber 210, respectively. β 2 The helix angle of the cyclone separation chamber 110; 1The reverse rotation switching point pole angle represents the ending angle of the first reverse rotation. Preferably, the reverse rotation switching point pole angle... 1 The value is π to 2π, meaning that the oil droplet particles complete half to one rotation in the last rotation path before flowing out of the coalescing reforming chamber 210. The upper end of the coalescing reforming chamber 210 can be understood as the end of the second cylinder 200 near the overflow pipe 300, and the lower end of the coalescing reforming chamber 210 can be understood as the end of the second cylinder 200 near the outlet 130.

[0042] During cyclone separation, oil droplets in the aqueous phase are affected by multiple forces, including flow field shear force, centrifugal force, and radial migration force. Particularly within the coalescence reforming chamber 210, the flow trajectories of the oil droplets intersect due to the anti-cyclone effect, creating a high probability of collision. Assume the diameters of the two oil droplets are... d 1 and d 2 Its relative velocity in the shear flow field is v rel According to Smoluchowski's theory of coalescence, the number of collisions occurring per unit volume per unit time can be expressed as:

[0043] in, C1 , C2 The number concentrations of oil droplets of the two different sizes that collided are respectively. K The collision kernel function reflects the frequency of collisions between oil droplets of different sizes in a given flow field. The calculation formula is as follows:

[0044] Furthermore, the actual number of collisions that can successfully coalesce depends on the coalescing efficiency. Ec The number of aggregations per unit time is:

[0045] coalescence efficiency Ec The following factors influence the flow: relative velocity between oil droplets; relative contact area between oil droplets; intensity and duration of flow field disturbance.

[0046] In the coalescing reforming cavity 210 of this application embodiment, the flow field fluctuations caused by the reversal of the rotation direction can improve... v rel This also increases the relative contact area between droplets, thereby increasing the collision frequency. K Within a certain range of shear rates, it also helps to improve Ec This causes small-diameter oil droplets to rapidly coalesce into larger droplets. Furthermore, due to particle size reconstruction, the coalesced oil droplets are guided to the central region of the swirling field, and their radial migration velocity...v r The increase allows oil droplets to enter the cyclone separation chamber 110 and be discharged through the overflow pipe 300, thereby completing the efficient oil-water separation process.

[0047] It should be noted that the anti-swirl effect refers to the interaction between the reverse swirling flows guided by the opposite deflection directions of the first inlet 120 and the second inlet 220 within the coalescence reforming chamber 210, which forces the swirling flow initially flowing in a certain direction (such as counterclockwise) to change to flowing in the opposite direction (such as clockwise). During this process, the swirling flow field forms a turning direction and disturbance.

[0048] It should also be noted that the device described in this application is a highly efficient separation device for small-diameter oil droplets in downhole mixtures by combining multiple technologies such as anti-swirl coalescence, particle size reforming, and swirling flow. Because the first inlet 120 and the second inlet 220 are arranged with opposite swirl directions, the swirl direction is reversed within the coalescence reforming chamber. Under the effect of the anti-swirl, small-diameter oil droplets originally distributed in the large-radius region of the swirling flow field in the coalescence reforming chamber 210 are forcibly guided to the small-radius region of the swirling flow field in the coalescence reforming chamber 210. Simultaneously, anti-swirl coalescence and particle size reforming are achieved through collisions between the small-diameter oil droplets. The reformed oil-water mixture enters the swirling flow field of the swirling flow separation chamber 110 through the first inlet 120. After coalescence reforming, the rotation radius of the small-diameter oil droplets is relatively smaller compared to small-diameter oil droplets in existing downhole separation technologies, and their radial migration ability is enhanced, thus making it easier for them to gather in the central region of the swirling flow field in the swirling flow separation chamber 110 and separate rapidly. Meanwhile, larger-diameter oil droplets, upon entering the coalescing reforming chamber 210, are distributed in the small-radius region of the swirling field due to the centrifugal force difference with the aqueous phase. During the reverse swirling process, these larger-diameter oil droplets are forcibly guided to the large-radius region of the swirling field. After the reverse swirling, due to the greater centrifugal force difference between the larger-diameter oil droplets and the aqueous phase, they migrate back from the large-radius region of the swirling field to the small-radius region. Then, after entering the swirling separation chamber 110 from the small-radius region, they concentrate at the center of the swirling field. At this point, the large-radius region of the swirling field within the separation chamber is the aqueous phase, which moves upwards to the first outlet 130 for discharge and simultaneous reinjection into the well. The oil droplets in the central region are discharged through the overflow pipe 300, achieving efficient separation of small-diameter oil droplets downhole.

[0049] In summary, by having the extension direction of the first inlet 120 deflected by a first deflection direction Y1 relative to the circumferential Y of the first cylinder 100, and the extension direction of the second inlet 220 deflected by a second deflection direction Y2 relative to the circumferential Y of the second cylinder 200, with the first deflection direction Y1 and the second deflection direction Y2 being set oppositely, the oil-water mixture can be guided to form opposite swirling flows at both ends of the coalescing reforming chamber 210 along the axial X direction. The intersection of these two opposing swirling flows in the coalescing reforming chamber 210 will break the original stable flow state of the oil-water mixture, forming a local vortex. The local vortex will cause the medium in different regions of the chamber to form a velocity gradient. Small-diameter oil droplets, due to their light weight and low inertia, are prone to turbulent and intersecting motion trajectories with changes in velocity, and no longer flow stably with the water phase, thereby increasing the probability of contact and collision between oil droplets of different diameters, and thus promoting the coalescence of small-diameter oil droplets into large-diameter oil droplets. In the counter-rotation effect, large-diameter oil droplets migrate from the small-radius region of the swirling field in the coalescing and reforming chamber 210 to the large-radius region of the swirling field in the coalescing and reforming chamber 210. However, due to the large centrifugal force difference between the larger-diameter oil droplets and water, after the counter-rotation is completed, the large-diameter oil droplets will migrate back to the small-radius region of the swirling field in the coalescing and reforming chamber 210 and concentrate at the center of the swirling field in the swirling separation chamber 110 through the first inlet 120, ensuring high separation efficiency. Thus, the coalesced and reformed oil droplets entering the swirling separation chamber 110 can increase the radial migration force of the coalesced oil droplets and reduce the probability of small-diameter oil droplets being discharged from the outlet 130 with the water phase. The coalesced and reformed oil-water mixture enters the swirling separation chamber 110 through the first inlet 120, where the centrifugal force of the swirling field enables rapid separation of the oil and water phases, thereby improving separation efficiency and accuracy.

[0050] It should also be noted that small-diameter oil droplets can cause them to form oil-in-water emulsions with water, and separation devices in related technologies are not very effective at separating such oil-water mixtures. However, the downhole forced reverse-spinning particle size reforming separation device 10 provided in this application can improve the separation effect of small-diameter oil droplets and water through the reverse-spinning effect. That is, the same oil-water mixture can be separated into more oil using the separation device 10 provided in this application, thereby reducing the amount of oil-in-water emulsions and effectively improving separation efficiency.

[0051] Meanwhile, the downhole forced reverse-spinning particle size reforming separation device 10 provided in this application performs oil-water separation of the produced fluid downhole, lifting the low-water-cut product to the surface and reinjecting the high-water-cut product back into the injection layer, achieving simultaneous injection and production within the same wellbore. In contrast, the oil-water mixture lifted by separation devices in related technologies cannot effectively separate small-diameter oil droplets, resulting in a high water content in the lifted oil-water mixture and thus increasing lifting costs.

[0052] In some embodiments, when the first cylinder 100 rotates n° about its own axis and is mirrored relative to a plane perpendicular to the axial direction X, the first deflection direction Y1 can be consistent with the second deflection direction Y2, wherein 0≤n<360.

[0053] The mention of rotation and mirror reversal of the first cylinder 100 here does not refer to the need for dynamic adjustment of the first cylinder 100 in actual use, but rather to clearly illustrate the flexibility in setting the first deflection direction Y1 and the second deflection direction Y2. That is, the first inlet 120 can be set at any position on the circumferential Y-axis of the first cylinder 100, and the extension direction of the first inlet 120 can exhibit different first deflection directions Y1 depending on the circumferential Y-axis position of the first cylinder 100; similarly, the second inlet 220 can be set at any position on the circumferential Y-axis of the second cylinder 200, and similarly, the extension direction of the second inlet 220 can also exhibit different second deflection directions Y2 depending on the circumferential Y-axis position of the second cylinder 200. In other words, the first deflection direction Y1 is the deflection trend of the first inlet 120 towards the outer wall of the first cylinder 100 relative to the deflection trend of the first cylinder 100 towards the Y direction, and the second deflection direction Y2 is the deflection trend of the second inlet 220 towards the outer wall of the second cylinder 200 relative to the deflection trend of the second cylinder 200 towards the Y direction.

[0054] Therefore, by extending the first inlet 120 and the second inlet 220 in opposite deflection directions, the multiphase medium can be guided to form a reverse vortex, creating eddies and velocity gradients within the coalescing reforming chamber 210. This guides small-diameter oil droplets, originally distributed in the large-radius region of the vortex field of the coalescing reforming chamber 210, to the small-radius region of the vortex field, altering the stable motion trajectory of the small-diameter oil droplets and thus increasing the probability of oil droplet collision, thereby ensuring improved separation efficiency.

[0055] See Figure 6 In some embodiments, the coalescing reforming chamber 210 has a first sub-region 211, a transition region 212, and a second sub-region 213 arranged sequentially along the axial direction X. A first inlet 120 is opened on the outer wall of the first cylinder 100 and is arranged corresponding to the first sub-region 211, so that the multiphase medium in the first sub-region 211 can form a swirling flow in a first direction. A second inlet 220 is opened on the outer wall of the second cylinder 200 and is arranged corresponding to the second sub-region 213, so that the multiphase medium in the second sub-region 213 can form a swirling flow in a second direction. The transition region 212 is located between the first sub-region 211 and the second sub-region 213, and the transition region 212 can include a swirling flow in the first direction and a swirling flow in the second direction, wherein the first direction and the second direction are opposite.

[0056] It should be noted that, see Figure 8The direction of its arrow rotation can be understood as the second swirling flow formed when the multiphase medium enters the second sub-region 213 through the second inlet 220. Figure 9 The direction of the rotation of the middle arrow can be understood as the first swirling flow formed when the multiphase medium enters the first sub-region 211.

[0057] The first sub-region 211, the transition region 212, and the second sub-region 213 are interconnected and form a continuous medium flow channel. The flow path of the multiphase medium in the coalescence reforming chamber 210 can be that it first enters the second sub-region 213 through the second inlet 220, then flows to the first sub-region 211 through the transition region 212, and then enters the cyclone separation chamber 110 through the first inlet 120 from the first sub-region 211, thereby completing the transport of the coalescence reformed medium.

[0058] The first inlet 120 can be opened on the outer wall of the first cylinder 100, and the position of the first inlet 120 in the axial direction X can correspond to the first sub-region 211. The extension direction of the first inlet 120 is deflected by a first deflection direction Y1 relative to the circumferential direction Y of the first cylinder 100. The first deflection direction Y1 can directionally guide the multiphase medium flowing through the first sub-region 211, so that the multiphase medium in the first sub-region 211 can stably form a swirling flow with a first vortex direction. The second inlet 220 is opened on the outer wall of the second cylinder 200, and its position in the axial direction X corresponds to the second sub-region 213. The extension direction of the second inlet 220 is deflected by a second deflection direction Y2 relative to the circumferential direction Y of the second cylinder 200, which is opposite to the first deflection direction Y1. When the multiphase medium enters the second sub-region 213 from the second inlet 220, it will form a swirling flow with a second vortex direction under the guidance of the second deflection direction Y2. The transition zone 212 is located between the first sub-zone 211 and the second sub-zone 213. As the connecting region of the swirling flow field between the first sub-zone 211 and the second sub-zone 213, it is simultaneously subjected to the swirling effect from both the first sub-zone 211 and the second sub-zone 213. In specific implementation, the multiphase medium flowing in from the second sub-zone 213 enters the transition zone 212 along the second swirling direction. Within the transition zone 212, the multiphase medium gradually changes its rotation direction through the reverse guiding force brought by the first inlet 120, that is, it gradually transitions from the initial second swirling direction to the first swirling direction. After the transition is completed, the multiphase medium enters the first sub-zone 211 along the first swirling direction, and then enters the swirling separation chamber 110 through the first sub-zone 211 and the first inlet 120. As a result, local eddies and velocity gradients are generated within the transition zone 212. Small-diameter oil droplets, due to their light weight and low inertia, are easily driven off their original paths by flow fields with different swirling directions. Through the anti-swirling effect, small-diameter oil droplets originally distributed in the large-radius region of the coalescing reforming chamber 210 are guided to the small-radius region of the swirling flow field within the coalescing reforming chamber 210, thereby increasing the probability of mutual contact and collision. This causes the small-diameter oil droplets to break the interfacial film through compression and coalesce into larger-diameter oil droplets. The larger-diameter oil droplets, upon entering the swirling separation chamber 110, experience stronger centrifugal force (or radial migration force) due to their greater mass, making them more likely to aggregate towards the swirling center. This avoids being entrained by the water phase, effectively reducing the probability of small-diameter oil droplets being discharged from the outlet 130 with the water phase. Therefore, the purity of the oil phase is ensured, the lifting cost of the water phase is reduced, efficiency is improved from the root, and economic waste is greatly reduced. This significantly improves the efficiency of small-diameter oil droplet separation in downhole.

[0059] See Figure 7 In some embodiments, at least two of the first cylinder 100, the second cylinder 200, and the overflow pipe 300 are coaxially arranged.

[0060] For example, the first cylinder 100, the second cylinder 200, and the overflow pipe 300 are arranged coaxially.

[0061] This effectively avoids problems such as flow field imbalance, abnormal local flow velocity, or media stagnation in the coalescence reforming chamber 210 caused by axial misalignment. It ensures that the counter-currents guided by the first inlet 120 and the second inlet 220 act uniformly in the coalescence reforming chamber 210, smoothly driving the transition zone 212 to achieve a swirling transition from the second swirling direction to the first swirling direction, providing a stable flow field environment for the collision and coalescence of small-diameter oil droplets. At the same time, the coaxial arrangement allows the overflow pipe 300 to be aligned with the swirling center region of the swirling separation chamber 110, ensuring efficient export of the separated oil phase and improving the operational stability and separation efficiency of the downhole forced counter-swirling particle size reforming separation device 10.

[0062] See Figure 7 In some embodiments, the first end 100a of the first cylinder 100 is flush with one end of the second cylinder 200 along the axial direction X, the second end 100b of the first cylinder 100 protrudes from the other end of the second cylinder 200 along the axial direction X, and the outlet 130 is disposed close to the second end 100b relative to the first end 100a so that the outlet 130 is exposed to the outside of the second cylinder 200.

[0063] The first cylinder 100 has a first end 100a and a second end 100b arranged opposite each other along the axial direction X. The first end 100a of the first cylinder 100 and one end of the second cylinder 200 along the axial direction X are flush. This flush arrangement allows the first cylinder 100 and the second cylinder 200 to form a flat mating surface at that end, effectively reducing assembly gaps and preventing leakage or retention of multiphase media at the end of the coalescence reforming chamber 210. It also ensures the structural stability of the first cylinder 100 and the second cylinder 200 after docking. Optionally, the first cylinder 100 and the second cylinder 200 can be integrally formed; or the first cylinder 100 and the second cylinder 200 can be separate structures, which are then docked through welding, sealing, or other methods.

[0064] The second end 100b of the first cylinder 100 protrudes from the other end of the second cylinder 200 along the axial direction X. The outlet 130 is opened on the side wall of the first cylinder 100, and the position of the outlet 130 in the axial direction X is closer to the second end 100b than the first end 100a, so that the outlet 130 is exposed to the external space of the second cylinder 200. This arrangement can avoid the second cylinder 200 from blocking or interfering with the outlet 130, ensuring that the separated aqueous phase can flow out smoothly, reducing the flow resistance caused by obstruction, and helping to improve the separation efficiency.

[0065] See Figure 11 In some embodiments, the inner diameter of the second cylinder 200 is D1, and the height of the first cylinder 100 in the axial direction X is H1, wherein D1≤H1≤200×D1.

[0066] It should be noted that the inner diameter of the second cylinder 200 can be understood as the maximum radial distance inside the second cylinder 200. The inner diameter of the second cylinder 200 can be determined based on the physical property parameters of the multiphase medium and the flow rate of the second inlet 220. The physical property parameters may include density, mass, particle size of the discrete phase, etc.

[0067] It is understandable that H1 can be any value between D1 and 200×D1. Thus, the first cylinder 100 can provide sufficient residence time for the multiphase medium to ensure the separation efficiency and accuracy of the discrete and continuous phases, while also taking into account the energy consumption of the multiphase medium in the swirling separation process.

[0068] If H1 is too low, for example, less than D1, the residence time of the multiphase medium in the first cylinder 100 will be too short, resulting in decreased separation efficiency and accuracy, thus affecting the separation effect. If H1 is too high, for example, greater than 200×D1, it will lead to increased energy loss and pressure drop during the cyclone separation process, which is not conducive to improving energy utilization efficiency and long-term stable operation. It will also result in an excessively large volume of the first cylinder 100, increasing manufacturing costs.

[0069] The first cylinder 100 protrudes from the second cylinder 200 by a length of H2 in the axial direction X, where 0.05×H1≤H2≤0.7×H1.

[0070] For example, H2 = 0.15 × H1, H2 = 0.24 × H1, H2 = 0.36 × H1, H2 = 0.57 × H1, etc. It should be noted that if the length of the first cylinder 100 protruding beyond the second cylinder 200 in the axial X direction is too long, it will lead to increased resistance and energy consumption of the continuous phase when passing through the outlet 130. If the length of the first cylinder 100 protruding beyond the second cylinder 200 in the axial X direction is too short, it will lead to a decrease in the stability of the swirling flow field within the swirling separation chamber 110.

[0071] See Figure 11 In some alternative embodiments, the maximum inner diameter of the first cylinder 100 is D2, wherein 0.5×D1≤D2≤0.75×D1.

[0072] In other words, D2 can be any value between 0.5×D1 and 0.75×D1, including the two extreme values ​​of 0.5×D1 and 0.75×D1. This allows for a balance between the processing capacity, separation accuracy, operational stability, and economic benefits of the first cylinder 100. Optionally, D2 = 0.53×D1, D2 = 0.62×D1, D2 = 0.71×D1, etc.

[0073] See Figure 11In some embodiments, a portion of the overflow pipe 300 extends along the axial direction X into the interior of the first cylinder 100; the height of the overflow pipe 300 along the axial direction X is H3, wherein 0.1×H1≤H3≤0.9×H1.

[0074] It should be noted that if the height of the overflow pipe 300 in the X-axis direction is too high, it will lead to high energy consumption and poor economic efficiency. If the height of the overflow pipe 300 in the X-axis direction is too low, outside air will be easily drawn into the overflow pipe 300, resulting in a decrease in the stability of the swirling flow field within the swirling separation chamber 110, thereby reducing the separation efficiency. Therefore, H3 can be made to satisfy: 0.1×H1≤H3≤0.9×H1.

[0075] The overflow pipe 300 extends along the axial direction X within the first cylinder 100 for a length of H4, where 0 < H4 ≤ 3D1.

[0076] Optionally, H4 = 1.2 × D1, H4 = 1.6 × D1, H4 = 2.1 × D1, H4 = 2.3 × D1, etc. This ensures that the overflow pipe 300 is located in the discrete phase aggregation region of the swirling flow field within the first cylinder 100, guaranteeing efficient capture and removal of the discrete phase, improving separation accuracy, and enhancing separation performance. If the extension length of the overflow pipe 300 along the axial direction X within the first cylinder 100 is too small, it can easily lead to the failure of the downhole forced reverse swirling particle reforming separation device 10, resulting in poor separation performance; if the extension length of the overflow pipe 300 along the axial direction X within the first cylinder 100 is too large, it will reduce separation accuracy and increase energy consumption.

[0077] In some alternative embodiments, the inner diameter of the overflow pipe 300 is D3, wherein 0.1×D1≤D3≤0.7×D1.

[0078] It should be noted that if the inner diameter of the overflow pipe 300 is too large, for example, D3 > 0.7 × D1, it will lead to an increase in the overflow volume of the overflow pipe 300 and a decrease in the separation accuracy. If the inner diameter of the overflow pipe 300 is too small, for example, D3 < 0.1 × D1, it will lead to an increase in the resistance of the discrete phase when passing through the overflow pipe 300, resulting in a decrease in the processing capacity of the overflow pipe 300 and an increase in the energy consumption of the discrete phase.

[0079] In some embodiments, the cross-sectional shapes of the first inlet 120, the second inlet 220, and the outlet 130 can be circular, rectangular, or the like. For example, the cross-sectional shapes of the first inlet 120, the second inlet 220, and the outlet 130 are rectangular. This ensures that the flow areas of the first inlet 120, the second inlet 220, and the outlet 130 remain regular, guaranteeing the uniformity of the multiphase medium's flow during inflow or outflow, and reducing localized eddies or sudden velocity changes caused by irregular cross-sectional shapes.

[0080] The height of the second inlet 220 in the axial direction X is H5, where 0.05×D1≤H5≤D1.

[0081] If the height of the second inlet 220 in the X-axis is too high, insufficient centrifugal force will result in decreased stability of the swirling flow field within the coalescing reforming chamber 210. Conversely, if the height of the second inlet 220 in the X-axis is too low, the stability of the swirling flow field within the coalescing reforming chamber 210 will also decrease, leading to reduced separation efficiency. Therefore, H5 can be any value between 0.05×D1 and D1 to ensure the stability of the swirling flow field.

[0082] In some embodiments, the port width of the second inlet 220 is L1, where 0.05×D1≤L1≤0.8×D1. That is, L1 can be any value between 0.05×D1 and 0.8×D1, including the two endpoints of 0.05×D1 and 0.8×D1, which helps to improve separation efficiency and separation effect.

[0083] In some embodiments, the height of the outlet 130 in the axial direction X is H6, wherein 0.5×H5≤H6≤2×H5.

[0084] If the height of outlet 130 in the X-axis direction is too high, the flow rate at outlet 130 will be too large, which will easily lead to a decrease in the separation effect. If the height of outlet 130 in the X-axis direction is too low, it will not be conducive to the orderly discharge of the multiphase media that have completed the cyclone separation. Therefore, H6 can be any value between 0.5×H5 and 2×H5, including the two extreme values ​​of 0.5×H5 and 2×H5.

[0085] In some embodiments, the port width of outlet 130 is L2, 0.05×D2≤L2≤0.8×D2. That is, L2 can be any value between 0.05×D2 and 0.8×D2, including the two end values ​​of 0.05×D2 and 0.8×D2, which helps to improve separation efficiency and separation effect.

[0086] In some embodiments, the height of the first inlet 120 in the axial direction X is H7, wherein 0.05×D1≤H7<D1.

[0087] If the height of the first inlet 120 in the X-axis is too high, the collision efficiency will be reduced, making it easier for unreversed discrete phases to enter the first cylinder 100, resulting in poor separation. If the height of the first inlet 120 in the X-axis is too low, the first swirling driving force guided by the first inlet 120 will be insufficient, making it difficult to form an effective swirling change in the transition zone 212, leading to an unstable swirling state of the multiphase medium. Therefore, H7 can be any value between 0.05×D1 and D1, including the extreme value of 0.05×D1.

[0088] In some embodiments, the port width of the first inlet 120 is L3, 0.05×D1≤L3≤0.8×D1. L3 can be any value between 0.05×D1 and 0.8×D1, including the two end values ​​of 0.05×D1 and 0.8×D1, which helps to improve separation efficiency and separation effect.

[0089] See Figure 2 and Figure 12 In some embodiments, the first cylinder 100 includes one of a cylinder, a cone, and a cylindrical cone. In some alternative embodiments, the outlet 130 is a tangential outlet 130 disposed along the circumferential Y direction of the first cylinder 100, or the outlet 130 is an axial X outlet 130 disposed along the axial direction X and opposite to the opening of the overflow pipe 300.

[0090] When the first cylinder 100 adopts a cylindrical structure, its inner wall maintains a uniform cross-section along the axial direction X, providing a stable flow space for the multiphase medium. When the first cylinder 100 adopts a conical structure, its cross-section gradually changes along the axial direction X. When the first cylinder 100 adopts a cylindrical-conical structure, the cylindrical-conical structure can be understood as having a portion that is cylindrical and a portion that is conical along its axial direction X. This allows for flexible adaptation to flow field requirements under different operating conditions. Optionally, liquid-liquid mixture separation can employ a four-segment cylindrical-conical or a three-segment cylindrical-conical structure, while gas-liquid mixture separation and solid-liquid mixture separation can employ a two-segment cylindrical-conical structure. Of course, gas-liquid mixture separation can also use either a cylinder or a cone; this embodiment does not impose limitations, and the specific implementation can be tailored to the actual operating conditions.

[0091] Furthermore, the outlet 130 on the first cylinder 100 can have various structural forms to adapt to discharge requirements. If the outlet 130 is a tangential outlet 130 arranged along the circumferential Y direction of the first cylinder 100, the extension direction of the outlet 130 is tangential to the circumferential Y direction of the first cylinder 100, which can guide the separated water phase to flow out tangentially along the circumferential Y direction of the first cylinder 100. If the outlet 130 is an axial X outlet 130 arranged along the axial direction X and facing away from the opening of the overflow pipe 300, its opening direction is consistent with the axial X direction of the first cylinder 100. Optionally, when the first cylinder 100 is a cylindrical structure, the outlet 130 can be a tangential outlet 130; when the first cylinder 100 is a conical structure or a cylindrical cone structure, the outlet 130 can be an axial X outlet 130, thereby better adapting to the gradually changing cross section of the cone or cylindrical cone along the axial X direction, conforming to the axial X flow trend of the water phase, reducing energy loss caused by the friction between the water phase turning and the cylinder wall, enabling the water phase to pass through the outlet 130 at a more stable flow rate, reducing the pressure drop caused by local resistance, and reducing the momentum loss of the water phase.

[0092] In some alternative embodiments, the first inlet 120 may be configured as multiple inlets, for example, two first inlets 120 may be configured, and the two first inlets 120 may be spaced apart on the circumferential Y-axis of the first cylinder 100. Optionally, the first inlet 120 may be configured as a straight inlet, a vortex inlet, etc.

[0093] See Figure 7 In some embodiments, an end cap 400 is also included, which is disposed on both ends of the first cylinder 100 and the second cylinder 200 in the axial direction X to seal the first cylinder 100 and the second cylinder 200.

[0094] Thus, the end caps 400 cover the ends of the first cylinder 100 and the second cylinder 200, achieving a seal between them. This configuration effectively prevents leakage of the multiphase medium within the coalescing reforming chamber 210, avoiding impact on separation efficiency due to multiphase medium loss, and also prevents external air, dust, moisture, and other impurities from entering the first cylinder 100 and the second cylinder 200. Furthermore, the excellent sealing performance maintains stable pressure within the coalescing reforming chamber 210, providing a stable pressure base for the reverse swirling flow guided by the first inlet 120 and the second inlet 220, thereby ensuring the smoothness of the swirling direction change in the transition zone 212, providing a reliable guarantee for subsequent swirling separation, and improving the operational stability and reliability of the downhole forced reverse swirling particle size reforming separation device 10.

[0095] The downhole forced reverse-swirl particle size reforming separation device 10 proposed in this application has a simple structure, small size, and reliable and stable operation. It can be applied downhole to efficiently separate small-diameter oil droplets in produced fluids. The oil-water mixture first passes through a coalescence reforming chamber to achieve reverse-swirl coalescence and particle size reforming of small-diameter oil droplets. This transforms small-diameter oil droplets into larger droplets through coalescence, causing them to gather from the outside of the swirling field to the central region of the swirling field, greatly improving separation accuracy and effect. Subsequently, it enters the swirling separation chamber for oil-water phase separation, and the water phase is directly reinjected into the well, saving water phase lift consumption. This application utilizes reverse-swirl coalescence, particle size reforming, and swirling separation technologies to achieve efficient downhole separation of small-diameter oil droplets. The separation efficiency is high, the separation effect is good, and it is conducive to the sustainable development of oilfields, possessing high practicality. Furthermore, the downhole forced reverse-swirl particle size reforming separation device 10 provided in this application is also applicable to surface water treatment.

[0096] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this application.

Claims

1. A downhole forced reverse-spinning particle size reforming and separation device, characterized in that, include: A first cylindrical body (100) has a first end (100a) and a second end (100b) disposed opposite to each other along its own axial direction (X). The first cylindrical body (100) has a swirling separation chamber (110) and a first inlet (120) and an outlet (130) communicating with the swirling separation chamber (110). One of the first inlet (120) and the outlet (130) is disposed at the first end (100a) and the other is disposed at the second end (100b). The second cylinder (200) is sleeved on the first cylinder (100) and surrounds the first cylinder (100) to form a coalescing reforming cavity (210). The coalescing reforming cavity (210) is connected to the first inlet (120). The second cylinder (200) is provided with a second inlet (220) connected to the coalescing reforming cavity (210). The second inlet (220) is located in the axial direction (X) of the second cylinder (200) relative to the first inlet (120) and close to the outlet (130). An overflow pipe (300) is disposed at one of the first end (100a) and the second end (100b) and is located away from the outlet (130) relative to the first inlet (120); the overflow pipe (300) is in communication with the vortex separation chamber (110); The first inlet (120) extends along the tangential direction of the circumferential (Y) sidewall of the first cylinder (100), and the extension direction of the first inlet (120) is in a first deflection direction (Y1) relative to the circumferential (Y) of the first cylinder (100). The second inlet (220) extends along the tangential direction of the circumferential (Y) sidewall of the second cylinder (200), and the extension direction of the second inlet (220) is in a second deflection direction (Y2) relative to the circumferential (Y) of the second cylinder (200). The first deflection direction (Y1) and the second deflection direction (Y2) are set opposite to each other to adjust the swirling direction of the multiphase medium mixture entering the coalescing reforming chamber (210).

2. The downhole forced reverse-spinning particle size reforming and separation device according to claim 1, characterized in that, When the first cylinder (100) rotates n° around its own axis and is mirrored relative to a plane perpendicular to the axis (X), the first deflection direction (Y1) can be consistent with the second deflection direction (Y2), where 0≤n<360.

3. The downhole forced reverse-spinning particle size reforming and separation device according to claim 1, characterized in that, The coalescing reforming chamber (210) has a first sub-region (211), a transition region (212), and a second sub-region (213) arranged sequentially along the axial direction (X). The first inlet (120) is opened on the outer wall of the first cylinder (100) and is arranged corresponding to the first sub-region (211) so that the multiphase medium mixture in the first sub-region (211) can form a swirling flow in the first direction. The second inlet (220) is opened on the outer side wall of the second cylinder (200) and is provided corresponding to the second sub-region (213) so that the multiphase medium mixture in the second sub-region (213) can form a swirling flow in the second direction; The transition region (212) is located between the first sub-region (211) and the second sub-region (213). The transition region (212) can include a swirling flow in the first direction and a swirling flow in the second direction, wherein the first direction and the second direction are opposite.

4. The downhole forced reverse-spinning particle size reforming and separation device according to claim 1, characterized in that, At least two of the first cylinder (100), the second cylinder (200), and the overflow pipe (300) are coaxially arranged.

5. The downhole forced reverse-spinning particle size reforming and separation device according to claim 1, characterized in that, The first end (100a) of the first cylinder (100) is flush with one end of the second cylinder (200) along the axial direction (X), the second end (100b) of the first cylinder (100) protrudes from the other end of the second cylinder (200) along the axial direction (X), and the outlet (130) is disposed close to the second end (100b) relative to the first end (100a) so that the outlet (130) is exposed to the outside of the second cylinder (200).

6. The downhole forced reverse-spinning particle size reforming and separation device according to claim 5, characterized in that, The inner diameter of the second cylindrical body (200) is D1; The height of the first cylinder (100) in the axial direction (X) is H1, where D1≤H1≤200×D1; The first cylinder (100) protrudes from the second cylinder (200) in the axial direction (X) by a length of H2, wherein 0.05×H1≤H2≤0.7×H1; And / or, the maximum inner diameter of the first cylinder (100) is D2, wherein 0.5×D1≤D2≤0.75×D1.

7. The downhole forced reverse-spinning particle size reforming and separation device according to claim 6, characterized in that, Part of the overflow pipe (300) extends along the axial direction (X) into the interior of the first cylinder (100); The height of the overflow pipe (300) in the axial direction (X) is H3, wherein 0.1×H1≤H3≤0.9×H1; And / or, the overflow pipe (300) extends for a length of H4 along the axial direction (X) within the first cylinder (100), where 0 < H4 ≤ 3D1; And / or, the inner diameter of the overflow pipe (300) is D3, wherein 0.1×D1≤D3≤0.7×D1.

8. The downhole forced reverse-spinning particle size reforming and separation device according to claim 6, characterized in that, The cross-sectional shape of the first inlet (120), the second inlet (220), and the outlet (130) is rectangular; The height of the second inlet (220) in the axial direction (X) is H5, where 0.05×D1≤H5≤D1; The port width of the second entry (220) is L1, where 0.05×D1≤L1≤0.8×D1; The height of the outlet (130) in the axial direction (X) is H6, wherein 0.5×H5≤H6≤2×H5; The port width of the outlet (130) is L2, where 0.05×D2≤L2≤0.8×D2; The height of the first inlet (120) in the axial direction (X) is H7, where 0.05×D1≤H7<D1; The port width of the first entry (120) is L3, 0.05×D1≤L3≤0.8×D1.

9. The downhole forced reverse-spinning particle size reforming and separation device according to any one of claims 1 to 8, characterized in that, The first cylindrical body (100) includes one of a cylinder, a cone, and a cylindrical-conical body; And / or, the outlet (130) is a tangential outlet (130) disposed along the circumferential (Y) direction of the first cylinder (100), or the outlet (130) is an axial (X) outlet (130) disposed along the axial direction (X) and opposite to the opening of the overflow pipe (300).

10. The downhole forced reverse-spinning particle size reforming and separation device according to any one of claims 1 to 8, characterized in that, It also includes end caps (400) which cover the first cylinder (100) and the second cylinder (200) at both ends in the axial direction (X) to seal the first cylinder (100) and the second cylinder (200).

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