CN110075619B - Wide-flow multi-flow high-efficiency gas-liquid separator - Google Patents
Wide-flow multi-flow high-efficiency gas-liquid separator Download PDFInfo
- Publication number
- CN110075619B CN110075619B CN201910396092.2A CN201910396092A CN110075619B CN 110075619 B CN110075619 B CN 110075619B CN 201910396092 A CN201910396092 A CN 201910396092A CN 110075619 B CN110075619 B CN 110075619B
- Authority
- CN
- China
- Prior art keywords
- inner cylinder
- separator
- liquid
- gas
- impeller
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/02—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising gravity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
- B01D45/08—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
- B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Centrifugal Separators (AREA)
- Cyclones (AREA)
Abstract
The invention aims to provide a wide-flow multi-flow type high-efficiency gas-liquid separator which comprises an outer cylinder and an inner cylinder, wherein the inner cylinder extends into the outer cylinder, the lower end part of the inner cylinder is left outside the outer cylinder, a primary impeller is arranged in the middle of the inner cylinder, a secondary impeller is arranged at the top of the inner cylinder, a liquid drainage section is arranged on the inner cylinder between the primary impeller and the secondary impeller, a liquid drainage hole for communicating the inner space of the inner cylinder with the inner space of the outer cylinder is formed in the liquid drainage section, a separator liquid phase lead-out opening is formed at the lower end part of the outer cylinder, a separator gas phase lead-out opening is formed at the top of the outer cylinder, and a separation chamber for enabling a liquid phase to fall back is formed between the secondary impeller and the separator gas phase lead-out opening. The invention comprehensively utilizes the centrifugal separation principle, the gravity separation principle and the inertia separation principle, has simple and compact structure and can realize high-efficiency gas-liquid separation in a wide flow range and under a multi-flow mode.
Description
Technical Field
The invention relates to a gas-liquid separator, in particular to a gas-liquid separator in the field of nuclear energy.
Background
Nuclear power is gaining more and more attention as a clean energy source today where energy problems are becoming more and more prominent. Gas-liquid separation technology has also received increasing attention as a key technology in nuclear power development. Before a gas-liquid mixture to be separated enters a separator, the flow characteristics of the gas-liquid two-phase mixture are changed due to the flow pattern change caused by the change of the converted flow rate of a gas phase and a liquid phase, and particularly the gas-liquid two-phase mixture is violently oscillated under an unstable flow pattern, which brings a new challenge to the current gas-liquid separation technology.
Present gas-liquid separation can divide into according to the theory of operation at present: gravity type gas-liquid separator, centrifugal gas-liquid separator, inertial gas-liquid separator, and of course, there are some gas-liquid separators that combine various principles. Limited by the space of use, the operating environment, the state of the gas-liquid mixture to be separated, centrifugal gas-liquid separators and multi-principle separators based on the principle of centrifugal separation have drawn attention because of their advantages of small size, light weight, high efficiency, high speed, etc. The principle of generating centrifugal force can be generally divided into: tangential injection centrifugal separators and axial flow centrifugal separators. The tangential injection type centrifugal separator generates centrifugal force by means of injecting gas-liquid mixture tangentially, has the advantages of simple structural form, no moving part, high reliability and the like, is the most widely used centrifugal separator at present (a novel double-cone-angle hydrocyclone, CN205887222U, an adjustable flow division ratio hydrocyclone device, N206425106U), and has the problems of poor stability of a gas core, large pressure drop, high turbulence, low separation efficiency and the like. Unlike tangential injection centrifugal separators, axial flow centrifugal separators utilize impellers to generate centrifugal force, and have the advantages of low turbulence, small pressure drop and the like (a rotary vane type multi-stage micro-bubble screening device, CN107684983A, lu Mingchao, li Yazhou and Xiong Zhenqin. Steam-water separator performance test research [ J ] in the dynamic engineering report, 2013.33 (1): 77-80). However, in the existing combined gas-liquid separator, although various separation principles are integrated and the separation effect is improved to a certain extent, the problem caused by the change of the flow pattern of the gas-liquid mixture before entering the separator is not considered in the design process, and when the flow pattern of the gas-liquid mixture before entering the separator is changed, particularly when the gas-liquid mixture is in an unstable flow pattern, the separation performance of the separator cannot be ensured ("a cyclone type combined gas-liquid high-efficiency separation device", CN106492544 a).
Most of the existing gas-liquid separators are separators based on a single principle, and although a few separators based on a plurality of principles exist, the existing gas-liquid separators are designed for a single and stable flow pattern basically and lack separators capable of efficiently operating under a plurality of flow patterns, particularly under an unstable flow pattern. However, in the practical application process of nuclear energy development, the flow pattern of the gas-liquid mixture is often changed due to the change of the gas-liquid ratio and the conversion speed in the gas-liquid mixture, and the performance of the separator is further affected. And due to the characteristics of the nuclear power device, the problems of narrow use space, high maintenance cost and the like exist.
Disclosure of Invention
The invention aims to provide a wide-flow multi-flow type high-efficiency gas-liquid separator which solves the problems that the separator in the technical field of gas-liquid separation is single in applicable flow type and can not efficiently operate under a multi-flow type.
The purpose of the invention is realized as follows:
the invention relates to a wide-flow multi-flow high-efficiency gas-liquid separator, which is characterized in that: including outer barrel, interior barrel stretches into to outer barrel inside, the lower tip of interior barrel is stayed outer barrel outside, the mid-mounting one-level impeller of interior barrel, the top installation secondary impeller of interior barrel, set up the flowing back district section on the interior barrel between one-level impeller and the secondary impeller, set up the outage that communicates interior barrel inner space and outer barrel inner space on the flowing back district section, the tip sets up the separator liquid phase and draws forth the mouth under the outer barrel, outer barrel top sets up the separator gaseous phase and draws forth the mouth, for the separation cavity that makes the liquid phase fall back between secondary impeller and the separator gaseous phase draw forth the mouth.
The present invention may further comprise:
1. the hub of the first-stage impeller is of a solid structure, and the hub of the second-stage impeller is of a hollow structure.
2. The upper edge of the blade of the secondary impeller is flush with the upper edge of the inner cylinder.
3. The separator gas phase outlet is a pipe extending towards the inside of the outer barrel, a separation baffle is arranged in the outer barrel below the separator gas phase outlet, and the separation baffle is connected with the outer barrel above the separation baffle through a separation baffle lacing wire.
4. The tangential direction of the inlet end of the first-stage impeller blade is parallel to the central axis of the inner cylinder, the included angle between the tangential direction of the outlet end of the first-stage impeller blade and the central axis of the inner cylinder is 55 degrees +/-5 degrees, the included angle between the tangential direction of the inlet end of the second-stage impeller blade and the central axis of the inner cylinder is 15 degrees +/-1 degrees, and the included angle between the tangential direction of the outlet end and the central axis of the inner cylinder is 55 degrees +/-5 degrees.
The invention has the advantages that: the invention realizes the high-efficiency separation of gas-liquid mixture under multi-flow type, wide flow, especially unstable flow type by the organic combination of three separation methods of centrifugal separation, gravity separation and inertia separation. The device can realize that:
(1) The wide-flow multi-flow high-efficiency gas-liquid separator provided by the invention utilizes the mutually sleeved double-layer cylinder structures, and comprehensively utilizes three separation principles of centrifugal separation, gravity separation and inertia separation by matching the two-stage impeller, the liquid discharge section, the outer cylinder separation chamber and the separation baffle in the separator, thereby realizing high-efficiency separation under a multi-flow mode, particularly an unstable flow mode.
(2) The first-stage impeller is of a solid structure, the second-stage impeller is of a hollow structure, and a gas-phase flow channel is independently established. After the gas-liquid mixture passes through the first-stage impeller, the gas phase is polymerized towards the center under the action of centrifugal force to form a gas core, and the liquid phase is gathered on the wall surface of the outer cylinder to form an annular liquid film. The gas phase and a small part of liquid directly enter the separation chamber of the outer cylinder body through the hollow channel of the hub of the secondary impeller, the annular liquid film firstly enters the flow channel between the blades of the secondary impeller after passing through the liquid discharge section, and the rotation strength is further increased, so that the gas phase and the liquid phase on the wall surface are mixed again, and the carrying effect of the gas phase is greatly reduced.
(3) The upper edges of the blades of the secondary impeller are flush with the upper edge of the inner cylinder, so that the liquid phase between different flow channels of the blades of the secondary impeller is directly thrown to the outer cylinder separation cavity after leaving the blades, the liquid phase is prevented from being recombined to form a complete annular liquid film, and the impact height of the liquid phase in the outer cylinder separation cavity is further too high.
(4) After the annular liquid film is formed by the first-stage impeller and the liquid phase, the gas-liquid mixture can be separated into partial liquid in advance when passing through a liquid discharge section between the second-stage impeller, so that the primary separation of the gas-liquid two-phase mixture is realized, and the separation pressure of a subsequent separation structure is reduced.
(5) The separation baffle and the inward extending design of the gas phase lead-out opening can perform inertia separation on liquid drops carried in the liquid phase at the liquid phase lead-out opening of the separator, so that the separation efficiency is further improved.
(6) The tangential direction of the inlet end of the first-stage impeller blade is parallel to the central axis, and the tangential direction of the inlet end of the second-stage impeller blade has a certain included angle with the central axis, so that the pressure loss of the two-phase fluid is ensured to be as small as possible when the two-phase fluid enters the separator.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2a is a front view of a primary impeller structure, and FIG. 2b is a top view of the primary impeller structure;
fig. 3a is a front view of the two-stage impeller structure, and fig. 3b is a top view of the two-stage impeller structure.
Detailed Description
The invention will now be described in more detail by way of example with reference to the accompanying drawings in which:
referring to fig. 1-3b, the combined multi-flow type high-efficiency gas-liquid separator provided by the invention comprises an inner cylinder 1, an inlet flange 2, a primary impeller 3, a secondary impeller 4, a liquid discharge section 5, a shockproof strip 6, a separation baffle lacing wire 7, a separation baffle 8, a separator gas phase outlet 9, an outlet flange 10, an outer cylinder 11, a separator liquid phase outlet 12 and a separator outer cylinder separation chamber 13. The main structure comprises two layers of cylinder structures which are sleeved with each other, the outer layer is an outer cylinder 11, the inner layer is an inner cylinder 1, a shockproof strip 6 is arranged between the inner cylinder 1 and the outer cylinder 11, a separator gas-phase lead-out opening 9 is arranged at the top of the separator, and a separator liquid-phase lead-out opening 12 is arranged at the bottom end of the outer cylinder 11, symmetrically arranged and mutually standby; a primary impeller 3 and a secondary impeller 4 are arranged in the inner cylinder 1 along the flowing direction of the gas-liquid mixture, the primary impeller 3 is arranged in the middle of the inner cylinder 1, and the secondary impeller 4 is arranged at the top of the inner cylinder 1; a liquid discharge section 5 is arranged on the inner wall of the inner cylinder body 1 between the first-stage impeller 3 and the second-stage impeller 4, and a certain number of liquid discharge holes are arranged in the liquid discharge section; an inertial separation baffle 8 is arranged at the inlet end of a gas phase outlet 9 of the separator; the separation chamber 13 of the outer cylinder of the separator between the secondary impeller 4 and the separation baffle 8 has sufficient space to ensure that gravity has sufficient vertical distance to allow most of the liquid phase to fall back.
The hub of the first-stage impeller 3 is of a solid structure, the hub of the second-stage impeller 4 is of a hollow structure, so that an independent gas phase circulation channel is established, and the inner diameter of the channel is larger than the outer diameter of the hub of the first-stage impeller 3.
The upper edge of the blade of the secondary impeller 4 is flush with the upper edge of the inner cylinder 1, so that the impact height of liquid under the high-flow-rate working condition is effectively reduced.
The liquid discharge section 5 may be provided with one or more sections, and the number of the openings, the form of the openings, and the arrangement of the openings may be set according to actual use conditions.
The separator gas phase outlet 9 extends a part towards the inside of the outer cylinder 11 to limit the carrying effect of the gas at the separator gas phase outlet 9 under high flow rate; and the separation baffle 8 can also be replaced by other inertia separation structures, such as: corrugated board, wire mesh.
The tangential direction of the blade inlet end of the first-stage impeller 3 is parallel to the central axis of the inner cylinder body 1, the included angle between the tangential direction of the outlet end and the central axis of the inner cylinder body 1 is 55 degrees, the included angle between the tangential direction of the blade inlet end of the second-stage impeller 4 and the central axis of the inner cylinder body 1 is 15 degrees, the included angle between the tangential direction of the outlet end and the central axis of the inner cylinder body 1 is 55 degrees, the number of the blades of the two impellers is 5, and the two-phase fluid can be guaranteed to fully rotate in a flow channel between the blades.
In the gas-liquid separation process, the technical scheme of the gas-liquid separator device is as follows: the separator is first fixedly mounted by means of the inlet flange 2 and the outlet flange 10. In the operation process of the separator, a gas-liquid mixture firstly enters the gas-liquid separator device through the inlet of the inner cylinder 1, and flows through the first-stage impeller 3 to change the normal linear motion into the rotary motion, so that the centrifugal force is generated while the rotary motion is generated. Under the action of centrifugal force, the gas phase with lower density is gathered at the center of the inner cylinder body 1 to form a gas core; the liquid phase with higher density is accumulated on the wall surface of the inner cylinder body 1 and forms an annular liquid film, so that the interphase separation is realized. After passing through the first-stage impeller 3, the gas-liquid mixture continues to move upwards in the inner cylinder body 1, when flowing through the liquid discharge section 5, part of liquid phase in the annular liquid film enters the inner cylinder body 1 through the opening of the liquid discharge section 5, enters the annular cavity between the outer cylinder bodies 11, and flows out of the separator through the liquid phase lead-out opening of the separator, so that primary centrifugal separation is realized. Due to the effects of friction dissipation and the like, the rotating strength of the gas phase and the liquid phase is attenuated to a certain degree, namely the centrifugal force is weakened to a certain degree. After passing through the liquid discharge section 5, the gas-liquid two phases continue to move upward, and the following phenomena are different between the high gas content condition and the low gas content condition, which will be described separately below.
Under the condition of low gas content, the gas flow rate is low, and the flow pattern is stable. The gas phase and a small amount of liquid phase move upwards through a middle hole channel established by a hub of the secondary impeller 4, enter the outer barrel separation chamber 13, continuously move upwards after entering the outer barrel separation chamber 13 of the separator, and leave the separator through a gas phase lead-out port 10 of the separator, and the liquid phase falls back into an annular cavity between the inner barrel 1 and the outer barrel 11 under the action of gravity to realize secondary gravity separation and then leaves the separator through a liquid phase lead-out port of the separator. After the liquid phase and a small amount of gas phase pass through the channel between the impellers, the rotating strength is increased, and the centrifugal force is further enhanced. After leaving the secondary impeller blades 4, under the action of centrifugal force, the liquid phase with high density is thrown to the inner wall surface of the outer cylinder body 11, falls back into an annular cavity between the inner cylinder body 1 and the outer cylinder body 11 under the action of gravity, leaves the separator, moves upwards, and leaves the separator through the upper cavity 13 of the outer cylinder body and the gas phase lead-out port 9 of the separator respectively, and finally, gas-liquid separation is completely realized.
Under the condition of high gas content, the gas flow rate is high, and the gas-liquid two-phase mixture can be in an unstable flow pattern such as stirring flow or annular flow. The annular liquid film formed after passing through the first-stage impeller 3 and a small amount of gas enter the channel between the blades of the second-stage impeller 4, the rotating strength is increased, and the centrifugal force is further enhanced. After leaving the blades of the secondary impeller 4, the liquid phase is thrown to the inner wall of the outer cylinder 11 of the separator under the action of centrifugal force and is influenced by gas carrying and flow pattern oscillation, the liquid phase continues to move upwards along the inner wall of the outer cylinder 11, part of the liquid phase can move to a gas phase lead-out opening 9 of the separator, and part of the liquid phase can fall back on the way to enter an annular cavity between the outer cylinder 11 and the inner cylinder 1. The liquid reaching the separator gas phase outlet 9 cannot enter the separator gas phase outlet 9 under the influence of gas carrying due to the blocking effect of the inward extending part of the separator gas phase outlet 9, so that the separation efficiency is influenced, and the liquid finally falls back and finally leaves the separator after passing through the outer cylinder separation chamber 13 and the annular cavity between the outer cylinder 11 and the inner cylinder 1. The gas core and a small amount of liquid phase formed after passing through the first-stage impeller 3 enter a flow passage established by a hollow hub of the second-stage impeller 4 and then enter the outer cylinder separation chamber 13, and the impact height of the liquid phase in the outer cylinder separation chamber 13 is higher under the carrying effect of high-flow-rate gas. Wherein, the liquid drops with larger diameter fall back into the annular cavity between the outer cylinder body 11 and the inner cylinder body 1 under the action of gravity and leave the separator, thereby realizing secondary gravity separation; the liquid drops with smaller diameter move upwards under the carrying effect of the gas phase, the small liquid drops carried in the gas phase are separated under the effect of the separation baffle 8, and the gas phase leaves the separator through a gas phase outlet 9 of the separator, so that three times of inertial separation is realized, and finally the whole separation process is realized.
Claims (2)
1. A wide-flow multi-flow high-efficiency gas-liquid separator is characterized in that: the separator comprises an outer cylinder and an inner cylinder, wherein the inner cylinder extends into the outer cylinder, the lower end part of the inner cylinder is left outside the outer cylinder, a primary impeller is arranged in the middle of the inner cylinder, a secondary impeller is arranged at the top of the inner cylinder, a liquid discharge section is arranged on the inner cylinder between the primary impeller and the secondary impeller, a liquid discharge hole for communicating the inner space of the inner cylinder with the inner space of the outer cylinder is arranged on the liquid discharge section, a separator liquid phase lead-out port is arranged at the lower end part of the outer cylinder, a separator gas phase lead-out port is arranged at the top of the outer cylinder, and a separation chamber for enabling a liquid phase to fall back is arranged between the secondary impeller and the separator gas phase lead-out port;
the hub of the first-stage impeller is of a solid structure, and the hub of the second-stage impeller is of a hollow structure;
the upper edge of the blade of the secondary impeller is flush with the upper edge of the inner cylinder;
the tangential direction of the inlet end of the first-stage impeller blade is parallel to the central axis of the inner cylinder, the included angle between the tangential direction of the outlet end of the first-stage impeller blade and the central axis of the inner cylinder is 55 degrees +/-5 degrees, the included angle between the tangential direction of the inlet end of the second-stage impeller blade and the central axis of the inner cylinder is 15 degrees +/-1 degrees, and the included angle between the tangential direction of the outlet end and the central axis of the inner cylinder is 55 degrees +/-5 degrees.
2. The wide flow path multi-flow type high efficiency gas-liquid separator as claimed in claim 1, wherein: the separator gas phase outlet is a pipe extending towards the inside of the outer barrel, a separation baffle is arranged in the outer barrel below the separator gas phase outlet, and the separation baffle is connected with the outer barrel above the separation baffle through a separation baffle lacing wire.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910396092.2A CN110075619B (en) | 2019-05-14 | 2019-05-14 | Wide-flow multi-flow high-efficiency gas-liquid separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910396092.2A CN110075619B (en) | 2019-05-14 | 2019-05-14 | Wide-flow multi-flow high-efficiency gas-liquid separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110075619A CN110075619A (en) | 2019-08-02 |
| CN110075619B true CN110075619B (en) | 2023-03-21 |
Family
ID=67419945
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910396092.2A Active CN110075619B (en) | 2019-05-14 | 2019-05-14 | Wide-flow multi-flow high-efficiency gas-liquid separator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110075619B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110926638B (en) * | 2019-12-05 | 2021-07-16 | 中国航发四川燃气涡轮研究院 | Gas temperature measuring probe in gas-liquid two-phase flow and use method thereof |
| CN110886601A (en) * | 2019-12-09 | 2020-03-17 | 哈尔滨工程大学 | Spring type liquid level self-adaptive gas-liquid separator |
| CN110898535A (en) * | 2019-12-09 | 2020-03-24 | 哈尔滨工程大学 | Axial-flow type multi-flow-channel gas-liquid separator |
| CN110898534A (en) * | 2019-12-09 | 2020-03-24 | 哈尔滨工程大学 | Intubation type gas-liquid separator based on differential pressure balance |
| CN111974027B (en) * | 2020-08-03 | 2022-03-18 | 哈尔滨工程大学 | Pipeline type multistage oil-water separator utilizing angular momentum conservation |
| CN117618989B (en) * | 2023-10-23 | 2024-06-25 | 山东铭锋新能源有限公司 | Oil-gas-water three-phase separator |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL1026268C2 (en) * | 2004-05-26 | 2005-11-30 | Flash Technologies N V | In-line cyclone separator. |
| CN2787662Y (en) * | 2005-05-09 | 2006-06-14 | 陈然 | Mixed diversion mechanism of urea-synthesizing tower |
| DE102008005574B4 (en) * | 2008-01-22 | 2013-11-28 | Areva Gmbh | centrifugal |
| CN107684983B (en) * | 2017-07-04 | 2020-08-04 | 上海交通大学 | Rotary vane type multi-stage microbubble screening device |
| CN107261654B (en) * | 2017-07-05 | 2019-07-05 | 中国石油大学(华东) | A kind of two-stage duct type gas-liquid cyclone separator |
| CN108815927B (en) * | 2018-06-12 | 2021-05-14 | 哈尔滨工程大学 | Multifunctional wide-flow-path efficient gas-liquid separation device combining gravity and centrifugal technology |
-
2019
- 2019-05-14 CN CN201910396092.2A patent/CN110075619B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN110075619A (en) | 2019-08-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110075619B (en) | Wide-flow multi-flow high-efficiency gas-liquid separator | |
| CN108815927B (en) | Multifunctional wide-flow-path efficient gas-liquid separation device combining gravity and centrifugal technology | |
| US11369906B2 (en) | Vortex separation device | |
| JP5550318B2 (en) | Multistage air-water separator and air-water separator | |
| CN100589883C (en) | Conical core type supersonic condensing cyclone separator | |
| CN106958439B (en) | Double-cone liquid-discharging type gas-liquid separator for oil-gas well test open-flow | |
| CN100385190C (en) | Cyclonic fluid separator with vortex generator in inlet section | |
| CN202224255U (en) | Symmetrical double-rotation type whirlcone | |
| CN110173254B (en) | Underground double-cylinder single-stage adjustable gas-liquid separator | |
| CN106861296A (en) | A kind of duct type NGL cyclone separator | |
| CN204933069U (en) | A kind of vortex tube gas-liquid separator | |
| WO2013016952A1 (en) | Tubular oil-water separator and spiral flow generator therefor | |
| CN110075622A (en) | A kind of twin-tub gas-liquid separator | |
| JPH06507693A (en) | Method and apparatus for generating useful energy from cocurrent flow | |
| CN105148625A (en) | Vortex tubular gas-liquid separator | |
| JP2014522717A (en) | Improved centrifuge | |
| CN205435993U (en) | Spiral entry is cone type hydraulic cyclone | |
| CN201088892Y (en) | Gas-liquid condenser | |
| CN204767854U (en) | Gas -liquid separator | |
| CN201214074Y (en) | Conic core type supersonic speed condensation cyclonic separating apparatus | |
| CN110075618A (en) | A kind of combination high-efficiency gas-liquid separator | |
| CN110075623A (en) | A kind of fining gas-liquid separator | |
| CN210186616U (en) | Gas-liquid separator | |
| CN102600995A (en) | Double-introduction-layer tower expanding cavity type separator | |
| US3507099A (en) | Centrifugal liquid-vapor separator |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |