阅读说明：本技术 一种管道式高流速气液分离装置和方法 (Pipeline type high-flow-rate gas-liquid separation device and method ) 是由 卫鹏凯 王栋 于 2019-10-21 设计创作，主要内容包括：本发明公开了一种管道式高流速气液分离装置和方法,气液两相流体在主路管流经旋流装置后,液相受到离心力作用在管壁形成均匀厚度的旋流液膜,气芯在管道中心流动；当旋流液膜流经管壁上的切向窄流道时,由于切向窄流道布置方向和液膜运动的方向一致,阻力极小,大部分的旋流液膜通过自身的动能和惯性从切向窄流道中流出,在管道内即可完成气液分离；同时,在分离液膜的过程中,管壁切向窄流道对气芯的流动几乎没有任何影响；本发明管壁切向窄流道对液膜流动的阻力小,并对气芯的流动影响很小,降低了因为高气速造成气路的液相夹带,可以很好地提高分离器的入口气速范围,尤其适合入口高流速的情况,整个气液分离在管道内便可完成,缩小了分离器的体积。(The invention discloses a pipeline type high-flow-speed gas-liquid separation device and a method, wherein after a gas-liquid two-phase fluid flows through a cyclone device in a main pipeline, a liquid phase is acted on a pipe wall by centrifugal force to form a cyclone liquid film with uniform thickness, and a gas core flows in the center of a pipeline; when the cyclone liquid film flows through the tangential narrow flow channel on the pipe wall, as the arrangement direction of the tangential narrow flow channel is consistent with the moving direction of the liquid film, the resistance is extremely small, most of the cyclone liquid film flows out of the tangential narrow flow channel through the self kinetic energy and inertia, and the gas-liquid separation can be completed in the pipe; meanwhile, in the process of separating the liquid film, the tangential narrow flow channel of the pipe wall hardly has any influence on the flow of the gas core; the tangential narrow flow channel of the pipe wall has small resistance to the flow of the liquid film and small influence on the flow of the gas core, reduces the liquid phase entrainment of the gas circuit caused by high gas velocity, can well improve the inlet gas velocity range of the separator, is particularly suitable for the condition of high inlet flow velocity, can complete the whole gas-liquid separation in the pipeline, and reduces the volume of the separator.)

1. The utility model provides a pipeline formula high flow rate gas-liquid separation device which characterized in that: the device comprises a main pipeline (1), wherein a liquid phase collecting pipe (4) is coated outside the middle part of the main pipeline (1), a rotational flow device (2) is coaxially arranged in the main pipeline (1), and at least one tangential narrow flow channel (3) is arranged on the pipe wall of the main pipeline (1) positioned in the liquid phase collecting pipe (4) at the downstream of the rotational flow device (2); the lower part or the bottom of the liquid phase collecting pipe (4) is communicated with a liquid phase discharge pipe (5), the liquid phase collecting pipe (4) is communicated with the main path pipe (1) through a tangential narrow channel (3) and is connected with an outlet of the liquid phase discharge pipe (5), and the liquid phase collecting pipe (4) forms a closed space;

the tangential narrow flow passage (3) is always tangent to the inner pipe wall of the main pipeline (1) on any cross section of the main pipeline (1), and the arrangement direction is consistent with the rotation direction of the liquid film after flowing through the cyclone device (2).

2. The ducted high flow rate gas-liquid separation device according to claim 1, wherein: the tangential narrow flow passages (3) are uniformly or non-uniformly distributed on the pipe wall of the main branch pipe (1) in the circumferential direction of the pipe wall.

3. The ducted high flow rate gas-liquid separation device according to claim 1, wherein: the tangential narrow flow passages (3) are vertically arranged on the pipe wall of the main road pipe (1), namely, along the flowing direction of the fluid, or are arranged on the pipe wall of the main road pipe (1) according to a spiral line.

4. The ducted high flow rate gas-liquid separation device according to claim 1, wherein: and the liquid phase discharge pipe (5) is provided with a regulating valve (6).

5. The method for gas-liquid separation in a tubular high-flow-rate gas-liquid separation device according to any one of claims 1 to 4, wherein: after the gas-liquid two-phase fluid flows through the cyclone device (2) in the main pipeline (1), the gas-liquid two-phase fluid generates cyclone in the main pipeline (1) through the cyclone device (2), the liquid phase moves to the pipe wall of the main pipeline (1) under the action of centrifugal force and forms a cyclone liquid film with uniform thickness to flow closely to the pipe wall, and the gas is forced to move to the center of the main pipeline (1) to form a gas core; when the rotational flow liquid film and the gas core flow through the tangential narrow flow passage (3) on the pipe wall of the main pipeline pipe (1), the arrangement direction of the tangential narrow flow passage (3) is consistent with the movement direction of the liquid film, the outflow resistance of the liquid film is extremely low, almost all the liquid film directly enters the tangential narrow flow passage (3) and enters the liquid phase collecting pipe (4) through the tangential narrow flow passage (3) by means of the kinetic energy and inertia of the liquid film, the liquid phase is discharged from a liquid phase discharge pipe (5) at the bottom of the liquid phase collecting pipe (4) under the action of gravity and centrifugal force, and an adjusting valve (6) is arranged on the liquid phase discharge pipe (5) and used for controlling the liquid level height of the; gas and residual liquid in the pipe are discharged from an outlet of the main branch pipe (1); at this point, the gas-liquid separation process is complete.

Technical Field

The invention relates to the technical field of gas-liquid two-phase fluid separation, in particular to a pipeline type high-flow-rate gas-liquid separation device and method.

Background

The gas-liquid two-phase flow separation technology has wide application in the fields of electric power, petroleum, chemical engineering, nuclear engineering and the like. Conventional gas-liquid separators rely primarily on gravity and centrifugal forces for separation, such as the most widely used cyclone separator in the industry, where a two-phase gas-liquid fluid enters the cyclone separator through a tangential inlet, where the fluid forms a cyclonic flow. Under the action of gravity and centrifugal force, the liquid phase is pushed to the wall surface and flows downwards, and is discharged from a liquid outlet at the bottom; the gas phase is concentrated in the center and discharged from the top gas outlet. To prevent the liquid film from being torn by the rising high velocity gas stream and causing severe entrainment, the axial updraft velocity of the separator is significantly limited by design rules, typically less than 0.4 m/s at high pressure and less than 1.1 m/s at low pressure, so the cyclone diameter is several times the inlet tube diameter. Therefore, the conventional gas-liquid separator is often large in size, heavy in weight, and high in cost. In recent years, many compact gas-liquid separators, such as GLCC and rotary vane steam-water separator, have been introduced for cost reduction. However, the high velocity updraft is still prone to entrain liquid phase into the gas path outlet of the GLCC and the inlet gas velocity has a very limited operating range, typically less than 9.2 m/s. Wang et al (2003) (Wang S., Gomez L.E., Mohan R.S., et al.gas-Liquid cyclical (GLCC) reactors for well gaps technologies [ J ]. Journal of Energy Resources Technology,2003,125 (1)) proposed an improved GLCC having an increased inlet gas phase conversion rate to 18m/s by adding AFE to the upper portion of the GLCC to separate Liquid entrainment in the gas path outlet by swirling action. The rotary vane steam-water separator separates a liquid film through a central pipe arranged at the downstream of the rotary vane, the liquid film is discharged through an annular space between the outer wall of the central pipe and the inner wall of the separation cylinder, and the gas core flows into the downstream from the central pipe. However, in the process of separating the gas core from the liquid membrane, the gas core suddenly shrinks when flowing into the central tube, the flow rate increases, the liquid phase is easily entrained to enter the gas path, and generally, the conversion speed of the gas phase at the inlet is less than 24m/s under normal temperature and normal pressure.

US patents 3884660 and US4180391 propose a tubular gas-liquid separator. A settling chamber contains a main conduit in which a swirl device is mounted, the main conduit being provided with one or two annular jets downstream of the swirl device. After the gas-liquid two-phase fluid flows through the cyclone device, because a part of the liquid phase does not have enough kinetic energy to overcome the resistance of the annular nozzle, in order to discharge all the liquid film through the annular nozzle, a part of the gas has to be sprayed into the settling chamber together with the liquid film through the annular nozzle, and finally the gas is separated in the settling chamber by gravity. However, this makes it still a vessel separator, which is bulky.

US patent nos. US4909067 and US patent No. US4856461 propose a gas-liquid separation device, which mainly comprises a cylindrical shell and a central tube, wherein the cylindrical shell is wrapped inside the cylindrical shell, a spiral turbolator is coaxially installed inside the central tube, and a small hole is formed in the wall of the central tube. When the gas-liquid two-phase fluid flows through the spiral turbolator, the fluid rotates, and the liquid drops move to the pipe wall under the action of centrifugal force and fall into the liquid collecting box in the cylindrical shell through the small holes in the pipe wall to complete gas-liquid separation. However, when the gas flow rate exceeds 4.9m/s, the liquid droplets cannot be completely removed. Temperature reaches thousand (2009) (document: temperature reaches thousand. porous pipe gas-liquid separator experimental study [ D ]. Saian: the university of Sian traffic, 2009) on the basis of which an improved gas-liquid separator is provided, wherein a straight pipe section is replaced by a conical pipe with a hole on the pipe wall, and a rotational flow device is arranged in the center of the inlet of the conical pipe. The experimental result shows that the gas phase conversion flow velocity can reach 30 m/s. Similarly, US7381235, which is incorporated herein by reference, proposes a cyclone separator with a grooved wall, in which a cyclone device is installed in a pipe, and a plurality of vertical grooves (or a spiral groove) are formed in the downstream wall of the cyclone blade and uniformly arranged in the circumferential direction of the pipe wall.

Through the analysis, the liquid phase in the two-phase flow can form a rotational flow liquid film on the pipe wall by using a centrifugal method, but the liquid film is difficult to be directly and independently separated because the strong coupling effect (particularly on a gas-liquid interface) still exists between the liquid film and the gas core. For a rotary vane steam-water separator, significant disturbance will be introduced to the flow of the air core during the separation process. In US4909067, US4856461, US7381235, the holes or slots formed in the tube wall are all perpendicular to the tube wall, i.e. along the radial direction of the tube, and these methods are all intended to separate the liquid phase in the radial direction (i.e. in the direction of the centrifugal force), but after leaving the tube wall, the rotating liquid phase will continue to move in the tangential direction when leaving the wall surface due to the inertia, so that the resistance of the liquid phase passing through the radial holes or slots of the tube wall is greatly increased, and at the same time, due to the thickness of the tube wall, the liquid film will easily hit the hole wall when flowing out of the tube through the radial holes or slots, and thus the liquid drops cannot flow out smoothly.

Disclosure of Invention

In view of the above problems in the prior art, an object of the present invention is to provide a pipeline type high flow rate gas-liquid separation apparatus and method, in which after a gas-liquid two-phase fluid flows through a cyclone apparatus in a main pipeline, a liquid phase in the gas-liquid two-phase fluid is subjected to a centrifugal force to act on a pipe wall to form a cyclone liquid film with uniform thickness, and a gas core flows in the center of the pipeline. Aiming at the flowing characteristics of the cyclone liquid film on the pipe wall, the direction of the tangential narrow flow channel arranged on the pipe wall is consistent with the moving direction of the cyclone liquid film, so that the resistance of the cyclone liquid film flowing out is extremely small, almost all the liquid film can directly enter the tangential narrow flow channel and can be completely discharged from the pipeline by means of the kinetic energy and inertia of the liquid film. Because the liquid film is removed from the side surface of the pipe wall, the gas core flowing in the center of the pipe is hardly influenced in the separation process.

In order to achieve the purpose, the invention adopts the following technical scheme:

a pipeline type high-flow-rate gas-liquid separation device comprises a main pipeline 1, wherein a liquid-phase collecting pipe 4 is coated outside the middle part of the main pipeline 1, a rotational flow device 2 is coaxially arranged in the main pipeline 1, and at least one tangential narrow flow passage 3 is arranged on the pipe wall of the main pipeline 1, which is positioned in the liquid-phase collecting pipe 4, at the downstream of the rotational flow device 2; the lower part or the bottom of the liquid phase collecting pipe 4 is communicated with a liquid phase discharge pipe 5, the liquid phase collecting pipe 4 is communicated with the main path pipe 1 through a tangential narrow channel 3 and is connected with the outlet of the liquid phase discharge pipe 5, and the liquid phase collecting pipe 4 forms a closed space.

The tangential narrow flow channel 3 is always tangent to the inner pipe wall of the main branch pipe 1 on any cross section of the main branch pipe 1, and the arrangement direction is consistent with the rotation direction of the liquid film after flowing through the cyclone device 2.

The tangential narrow flow passages 3 are uniformly or non-uniformly distributed on the tube wall of the main bypass tube 1 in the circumferential direction of the tube wall.

The tangential narrow flow channels 3 can be arranged vertically, i.e. in the direction of fluid flow, on the pipe wall, or can be arranged according to a spiral line on the pipe wall.

And the liquid phase discharge pipe 5 is provided with a regulating valve 6.

According to the gas-liquid separation method of the pipeline type high-flow-rate gas-liquid separation device, after a gas-liquid two-phase fluid flows through the cyclone device 2 in the main pipeline 1, the gas-liquid two-phase fluid generates cyclone flow in the main pipeline 1 through the cyclone device 2, the liquid phase moves to the pipeline wall of the main pipeline 1 under the action of centrifugal force and forms a cyclone liquid film with uniform thickness to flow tightly attached to the pipeline wall, and the gas is forced to move to the center of the main pipeline 1 to form a gas core; when the rotational flow liquid film and the gas core flow through the tangential narrow flow passage 3 on the pipe wall of the main pipeline 1, the arrangement direction of the tangential narrow flow passage 3 is consistent with the movement direction of the liquid film, the outflow resistance of the liquid film is extremely small, almost all the liquid film can directly enter the tangential narrow flow passage 3 and enter the liquid phase collecting pipe 4 through the tangential narrow flow passage 3 by means of the kinetic energy and inertia of the liquid film, the liquid phase is discharged from a liquid phase discharge pipe 5 at the bottom of the liquid phase collecting pipe 4 under the action of gravity and centrifugal force, and an adjusting valve 6 is arranged on the liquid phase discharge pipe 5 and used for controlling the liquid level height of the liquid; gas and residual liquid in the tube are discharged from an outlet of the main branch tube 1; at this point, the gas-liquid separation process is complete.

Compared with the prior art at home and abroad, the invention has the following characteristics:

(1) the arrangement direction of the tangential narrow flow channel on the pipe wall is consistent with the movement direction of the liquid film, so that the resistance to the flow of the liquid film is very small, and almost all the liquid film can flow out of the tangential narrow flow channel through the kinetic energy and inertia of the liquid film.

(2) Because the tangential narrow flow passage separates the cyclone liquid film from the outer side of the circumference of the pipeline, in the process of separating the cyclone liquid film, the disturbance introduced to the flow of the central gas core of the main pipeline is very small, the flow of the gas core is hardly influenced, the gas speed and the liquid speed of the separation device can be effectively increased, and the phenomenon that liquid drops are entrained at the gas path outlet caused by overhigh rising gas speed in the traditional separator is avoided.

(3) The whole separation process can be completed in the pipeline, the structure is compact, the whole separator is small similar to a common pipeline, the size is small, no moving part is needed, the maintenance is convenient, and the separator can be widely applied to the fields of petrochemical industry, natural gas and the like.

Drawings

Fig. 1 is a schematic sectional structure of the present invention.

Fig. 2 is a schematic view of a tangential narrow channel structure in embodiment 1 of the present invention, wherein: fig. 2(a) is a schematic view of the tangential narrow flow channels vertically arranged on the main road pipe wall, and fig. 2(b), fig. 2(c) and fig. 2(d) are respectively sectional views of fig. 2(a) along the direction a-a and the tangential narrow flow channels distributed on the circumference of the main road pipe, and the number of the tangential narrow flow channels is two, three and five.

Fig. 3 is a schematic view of a tangential narrow channel structure in embodiment 2 of the present invention, wherein: fig. 3(a) is a schematic diagram of a tangential narrow flow passage arranged on the wall of the main branch pipe in a spiral line, and fig. 3(B) is a cross-sectional view of fig. 3(a) along the direction B-B.

Detailed Description

The invention is described in further detail below with reference to the figures and specific embodiments.