CN114425184B - CO (carbon monoxide) 2 Device and method for gas-liquid separation of drive produced liquid pipeline - Google Patents
CO (carbon monoxide) 2 Device and method for gas-liquid separation of drive produced liquid pipeline Download PDFInfo
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- CN114425184B CN114425184B CN202011005758.6A CN202011005758A CN114425184B CN 114425184 B CN114425184 B CN 114425184B CN 202011005758 A CN202011005758 A CN 202011005758A CN 114425184 B CN114425184 B CN 114425184B
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- 239000007788 liquid Substances 0.000 title claims abstract description 430
- 238000000926 separation method Methods 0.000 title claims abstract description 138
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 title claims description 4
- 238000000034 method Methods 0.000 title abstract description 11
- 238000003860 storage Methods 0.000 claims abstract description 35
- 239000012071 phase Substances 0.000 claims abstract description 25
- 238000004519 manufacturing process Methods 0.000 claims abstract description 22
- 238000000605 extraction Methods 0.000 claims abstract description 19
- 239000007791 liquid phase Substances 0.000 claims abstract description 13
- 239000012530 fluid Substances 0.000 claims abstract description 7
- 230000005484 gravity Effects 0.000 claims description 12
- 238000011144 upstream manufacturing Methods 0.000 claims description 10
- 230000009471 action Effects 0.000 claims description 9
- 230000000694 effects Effects 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000009826 distribution Methods 0.000 claims description 3
- 238000006073 displacement reaction Methods 0.000 abstract description 2
- 230000005514 two-phase flow Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000000853 adhesive Substances 0.000 description 4
- 230000001070 adhesive effect Effects 0.000 description 4
- 239000010779 crude oil Substances 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000002734 clay mineral Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 208000036460 primary closed-angle glaucoma Diseases 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0063—Regulation, control including valves and floats
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/24—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by centrifugal force
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/164—Injecting CO2 or carbonated water
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
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- Chemical & Material Sciences (AREA)
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- Fluid Mechanics (AREA)
- Environmental & Geological Engineering (AREA)
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- General Life Sciences & Earth Sciences (AREA)
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Abstract
The invention belongs to oil field ground CO 2 The technical field of gas-liquid separation of oil displacement and extraction processes, in particular to a CO 2 A device and a method for gas-liquid separation of a drive produced liquid pipeline. The device comprises a horizontal inlet pipe, a gas-liquid pre-separation device, a cyclone device, a liquid film guiding device, a gas fine separation device, a liquid storage device, an S-shaped pipe, a dry gas outlet pipe and a liquid production discharge pipe. The device adopts the cyclone to separate the gas phase and the liquid phase in the pipe, and the liquid outlet tangential to the spiral flow direction of the liquid film is arranged, so that the flow resistance of the liquid film is obviously reduced, and the thin liquid film can be directly separated from the pipeline; the applicable gas-liquid range of the device is enlarged through the pre-separation structure, the separation efficiency is improved by the tangential liquid extraction method, the high-efficiency separation of the gas-liquid two-phase flow fluid in the pipeline is realized, and the CO is satisfied 2 And (3) driving the operation requirement of the oil extraction process system.
Description
Technical Field
The invention belongs to oil field ground CO 2 The technical field of gas-liquid separation of oil displacement and extraction processes, in particular to a CO 2 A device and a method for gas-liquid separation of a drive produced liquid pipeline.
Technical Field
Because the permeability of the low-permeability oil reservoir is too low, more clay minerals in the reservoir are present, and the reservoir swells to block pores after meeting water, so that the water absorption capacity is poor during water injection. As the oil field is developed for a certain period, the contradiction of 'no injection and no production' is gradually highlighted, the characteristic of 'three low' (low liquid amount, low productivity and low recovery ratio) is more obvious, the difficulty of stable production is increased, and the oil yield of oil extraction in a water injection mode is continuously reduced. And CO 2 Is a strong steaming agent capable of extracting C 5 ～C 30 Hydrocarbon components in the range expand the crude oil, reduce the viscosity of the crude oil and improve the fluidity of the crude oil. And, CO 2 The method has the characteristics of acidizing the rock, reducing interfacial tension and the like, and becomes an effective technology for improving the development level of low permeability oil fields at home and abroad. However, CO is adopted 2 The driving technology is used for oil extraction, and the produced gas contains a large amount of gas, but the produced gas is not allowed to be directly discharged into the atmosphere, and the produced gas needs to be recycled after separation.
Conventional separation techniques rely primarily on gravity and centrifugal force for separation. The three-phase separator commonly used in industry is a conventional separator for separating liquid produced by gravity, and the separation technology is relatively mature, but has the defects of overlarge occupied area, high investment efficiency, low safety cost and the like. Another type of separator that is more common in the industry is a hydrocyclone separator, in which two-phase fluid is caused to flow vertically downward by gravity through a tangential inlet, and gas in the middle flows upward from a downward cyclone, and flows out of a gas pipe. Meanwhile, an overflow ring is added at the outlet of the separator to carry out water film separation, so that the separation efficiency of the separator is improved. However, when the flow direction of the liquid is opposite to that of the gas, and the flow rate of the gas is high, the liquid film layer can be damaged by discharging the gas from the gas outlet at the top, and a large number of liquid drops are carried at the same time, so that the separation efficiency of the device is affected. The separator has the defects of large volume, high manufacturing cost, safety cost, small application range and the like. For GAS carrying, university of talsa students in the united states have proposed an improved GAS-liquid separation device (GAS-LIQUID CYLINDRICAL CYCLONE), abbreviated as improved GLCC (Journal of Energy Resources Technology,2008,130 (4): 042701.Doi: 10.1115/1.3000101). The improved device reduces the volume, and meanwhile, a liquid film extraction ring is added at the gas outlet, so that the gas-liquid separation efficiency is improved, but the flow rate of the mixed gas-liquid inlet still cannot be too high, and the applicable gas speed range is small.
U.S. patent No. GAS PIPELINE DRIP (US 5525133) discloses a pipe-type gas-liquid separation apparatus. According to the invention, the layering of the gas phase and the liquid phase is realized in the flowing process under the action of gravity by utilizing the gas-liquid density difference of the mixture in the pipeline, the flowing direction of the layered gas phase and liquid phase is changed by utilizing the T-shaped structure, the liquid freely subsides into the liquid collecting tank, and the gas flows into the downstream along the main pipeline, so that the separation of the gas phase and the liquid phase is realized. The invention only uses the gravity action, so that the flow rate of the mixed gas-liquid cannot be too high, otherwise, a large number of carried liquid drops are generated, and the separation efficiency is drastically reduced. The invention is separated by a pipeline, but the liquid collecting tank has larger volume, belongs to a pressure container, and has higher safety requirement, site cost and safety monitoring cost.
The Chinese patent "gas-liquid separator" (CN 106178786A) discloses a gas-liquid separation device which utilizes the actions of a silk screen, a partition plate and tangential rotational flow to efficiently separate liquid drops in gas. The device can realize the high-efficient separation of gas-liquid under the low gas velocity condition, but, whole device is bulky, belongs to pressure vessel, and area is big, therefore the cost in place is higher. Because of the internal silk screen structure, the resistance in the container is increased, the container is easy to be blocked, and the pressure loss is also large.
U.S. Pat. No. 4,182, (U.S. Pat. No. 3,62) proposes a tubular GAS-LIQUID separation device in which the separation conduit is enclosed in a large tank vessel. A swirling device is located in the inlet conduit forcing the liquid against the wall and two annular jet ports in series are formed in the separator conduit to remove the liquid film and a portion of the gas to the liquid reservoir. However, from the tube wall to the gas core, the liquid film is divided into three regions: adhesive sublayers, base films and waves. The adhesive sub-layer near the pipe wall has small kinetic energy and large speed gradient due to the adhesive shearing stress action of the pipe wall. Although most of the gas in the mixture may enter the separation conduit outlet directly, a portion of the gas must be ejected from the annular port together with the liquid film, since the liquid film itself does not have sufficient kinetic energy to overcome the resistance. This portion of the gas is separated from the liquid in the reservoir by gravity and inertia, and therefore the reservoir must be a large container. Furthermore, the annular jet orifice is similar to a pickup ring, but it does not address the problem of high velocity gas entrainment.
Japanese Hironobu KATAOKA published an article in Journal ofPower and Energy Systems, named Two-Phase Swirling Flow in a Gas-Liquid Separator. The article describes an analytical separator for separating a swirling gas-liquid by means of a pickup ring. The gas-liquid flows in the vertical pipe from bottom to top, the mixed gas-liquid forms an annular flow after being swirled by the swirler, and a liquid film is separated after passing through a Pick-up Ring (Pick-Off-Ring) in the pipe. This document compares the separation efficiency of the separator with the different spacing between the POR and the conduit and the presence or absence of a cyclone. It was demonstrated that cyclones and certain intervals of POR can improve the efficiency of gas-liquid separation in the pipeline. However, the separator in this article is affected by the POR interval size factor, the amount of separation liquid is small, and the applicable gas velocity is low.
Disclosure of Invention
The invention aims to solve the problems existing in the prior art and provides a CO 2 A device and a method for gas-liquid separation of a drive produced liquid pipeline. The device can be applied to the CO2 flooding oil extraction process of an oil field, realizes on-line tubular separation of gas and liquid with wide gas-liquid ratio range, small occupied area and high efficiency separation, and the separated gas can be treated and recycled, so that the device is more economical and environment-friendly, and reduces the gas production to the atmosphereThe safety is improved and the pollution is reduced by the medium emission.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
CO (carbon monoxide) 2 The device for driving the output liquid pipeline type gas-liquid separation comprises a horizontal inlet pipe (1), a gas-liquid pre-separation device (2), a cyclone device (3), a liquid film guiding device (4), a gas fine separation device (5), a liquid storage device (6), an S-shaped pipe (7), a dry gas outlet pipe (8) and a output liquid discharge pipe (9).
The horizontal inlet pipe (1), the gas-liquid pre-separation device (2) and the second Y-shaped tee joint (11) are connected through a first Y-shaped tee joint (10), and a first valve (13) is arranged between the first Y-shaped tee joint (10) and the second Y-shaped tee joint (11).
The second Y-shaped tee joint (11) is respectively connected with the first Y-shaped tee joint (10), the straight pipe (12) and the gas-liquid pre-separation device (2), and a liquid level meter (15) is arranged in the gas-liquid pre-separation device (2).
One end of the S-shaped pipe (7) is connected with the gas-liquid pre-separation device (2), the other end of the S-shaped pipe is connected with the liquid storage device (6), and a second valve (14) is arranged in the S-shaped pipe.
A rotational flow device (3) is arranged between the straight pipe (12) and the gradually-expanding pipe (16), and an outlet of the gradually-expanding pipe (16) is connected with a liquid film guiding device (4).
The liquid film guiding device (4) is provided with a first liquid taking port (17) and a second liquid taking port (18) along the tangential direction of a gas-liquid rotation streamline, the first liquid taking port and the second liquid taking port are respectively positioned at the left side and the right side of the device, and the tail end of a pipeline is provided with a semicircular annular gap; wherein the opening of the second liquid taking port (18) is inclined upwards, the inclination angle is 50-53 degrees, and a semicircular arc guide baffle (21) is arranged in the tangential direction of the side opening; the first liquid taking port (17) is downward in opening, a vertical flow guide baffle (23) is arranged in the tangential direction of the side opening, and the inclination angle of the axial directions of the two liquid taking ports is 42-45 degrees; a first element shrinkage tube (19) is arranged above the semicircular notch at the tail end of the pipeline of the liquid film guiding device (4).
The upstream of the gas fine separation device (5) is connected with a first element shrinkage tube (19) at the tail end of the liquid film guiding device (4), and the inner diameters of the two are the same; the bottom of the pipeline of the gas fine separation device (5) is a square notch, the edge of the notch is tangent to the semicircular cross section of the pipeline, the length is 100mm, and the width is 26mm; the tail end of the gas fine separation device (5) is provided with a second shrinkage tube (26) which is communicated with a dry gas outlet tube (8).
The liquid film collecting device is characterized in that the first liquid storage device (6 a) and the second liquid storage device (6 b) are respectively communicated with an upstream liquid film leading-out device (4) and a gas fine separation device (5) through a first gradually-reducing deformation pipe (20) and a second gradually-reducing pipe (22), an interface is arranged on the side face of a pipeline of the first liquid storage device (6 a) and is connected with an S-shaped pipe (7), a liquid level meter (24) is arranged in the second liquid storage device (6 b), and the other ends of the first liquid storage device (6 a) and the second liquid storage device (6 b) are respectively connected into a liquid production discharge pipe (9) through a first gradually-reducing pipe (27) and a second gradually-reducing pipe (28). The third valve (25) is arranged at the outlet of the liquid production discharge pipe (9).
The horizontal inlet pipe (1), the first valve (13), the straight pipe (12) and the cyclone device (3) are coaxially arranged and are all positioned at the same horizontal height.
The liquid level value in the gas-liquid pre-separation device (2) is controlled by a liquid level meter (15) and a second valve (14).
The cyclone device (3) is formed by rotating four semi-elliptic sheets with the thickness of 1 millimeter around the axis of the circular tube, the included angle between the semi-elliptic sheets and the section of the pipeline is 45 degrees, and the semi-elliptic sheets and the inner wall of the circular tube are of an integral structure.
The included angle between the inclined section and the horizontal section of the first Y-shaped tee joint (10) is 15-30 degrees, and the included angle between the inclined section and the horizontal section of the second Y-shaped tee joint (10) is 70-75 degrees.
The outer wall of the pipeline of the first pixel shrinkage pipe (19) and the outer wall of the pipeline of the second pixel shrinkage pipe (26) are conical, the gap between the outer wall surface of the first pixel shrinkage pipe (19) and the inner wall surface of the liquid film guiding-out device (4) is 4-6 mm, and the difference between the inner diameter of the first pixel shrinkage pipe and the inner diameter of the pipeline of the liquid film guiding-out device (4) is less than 10mm; the gap between the outer wall surface of the second pixel shrinkage tube (26) and the inner wall surface of the gas fine separation device (5) is 4-7 mm, and the difference between the inner diameter of the second pixel shrinkage tube (26) and the inner diameter of a pipeline of the gas fine separation device (5) is smaller than 14mm; the lengths of the first and second pixel shrinking pipes (19, 26) are 15-20 mm.
The invention further discloses a gas-liquid separation method of the separation device, which specifically comprises the following steps:
(1) The device is arranged on CO 2 In a liquid production conveying pipeline of the oil extraction system, the flow pattern of the produced gas and liquid in the pipeline is stratified flow or annular flow, and the thickness distribution of a liquid film in a horizontal pipe is thin at the upper part and thick at the lower part; the first valve (13) is properly regulated, so that the produced mixed gas-liquid enters the gas-liquid pre-separation device (2), and the gas and the liquid are separated in the gas-liquid pre-separation device (2).
(2) The separated liquid is discharged into the liquid storage device (6) through the S-shaped pipe (7), and a liquid level meter (15) with the liquid level of the liquid passing through the liquid level meter and a second valve (14) in the S-shaped pipe (7) are regulated together, so that the impact of the liquid due to overlarge flow rate is well buffered.
(3) The separated gas enters the main pipeline through the second Y-shaped tee joint, and after being mixed with the gas and liquid at the upstream of the main pipeline through the first valve (13), the gas and liquid in the straight pipe (12) enters the cyclone device (3) through the straight pipe (12), the gas and liquid in the straight pipe (12) are thrown to the vicinity of the pipe wall due to the high density under the centrifugal force effect generated by the cyclone in the cyclone device (3), the gas and liquid are converged to form a liquid film near the pipe wall, the gas phase with the low density is converged at the center of the pipeline, the cyclone device (3) converts the gas-liquid two-phase fluid into a gas core-liquid film annular flow, and the liquid film and the gas both flow forwards with the rotational kinetic energy.
(4) After passing through the gradual expanding pipe (16), the circulating cross-sectional area of the liquid film in the annular flow type is increased, the flow velocity of the liquid film and liquid drops is reduced, and the liquid film still presents annular flow. When passing through the downstream liquid film guiding device, the liquid film and liquid drops are guided downwards along the tangential liquid taking opening under the action of centrifugal force and gravity on the right side in the flowing direction; on the left side of the flowing direction, the liquid film flows upwards obliquely along the rotating flow line and is guided out by the semicircular arc guide plate, and finally flows downwards; the residual liquid drops enter the gas fine separation device (5) through the first pixel shrinkage tube (19) along with the swirling flow carried by the gas, the liquid drops are carried to the pipe wall by the gas due to the centrifugal effect, flow downwards along the pipe wall, the gas spirals forwards, the gas and the liquid drops are finally separated by the second pixel shrinkage tube (26), and the dry gas enters and flows out of the separation device through the dry gas outlet pipe (8).
(5) Liquid film guiding-out deviceThe product liquid separated in the device (4) and the gas fine separation device (5) flows downwards along with the pipe wall of the liquid storage device (6), and flows out of the separation device through the product liquid outlet pipe (9) after being collected with the product liquid discharged from the bottom of the gas liquid pre-separation device (2), thereby realizing CO 2 And (3) separating gas phase and liquid phase of the flooding produced liquid.
The method is divided into three steps to finish the CO 2 The gas-liquid two-phase of the drive produced liquid in the pipeline is completely separated. The first step, the produced gas and liquid by the bypass enters a mixed gas-liquid pre-separation device, so that the large liquid amount and liquid-bullet and gas-bullet impact which occur at the beginning of production are reduced, the stability of the flow of the produced gas and liquid in the pipeline at the upstream of the cyclone is increased, the cyclone can better perform two lines of cyclone gas and liquid, and a stable gas-liquid annular flow pattern is obtained; secondly, the liquid film is led out by a liquid film leading-out device in a homeotropic manner, and the influence on the resistance of the liquid film is minimized; and thirdly, carrying out secondary separation on the gas containing residual liquid drops through a gas fine separation device to complete separation of the produced liquid and the produced gas, thereby realizing high-efficiency gas-liquid separation.
Compared with the prior art, the invention has the following advantages:
(1) The device adopts a tubular structure, has small volume and can be applied to being arranged on CO 2 In the oil extraction system pipeline, CO is realized 2 The gas and liquid produced by the flooding are efficiently separated in an on-line pipe type; meanwhile, the device has the advantages of wide applicable gas-liquid flow range, large gas-speed variation range, safe operation, low manufacturing cost and the like.
(2) The invention adopts the in-tube phase separation technology, combines the centrifugal and gravity separation functions, and completes CO through rectification, liquid film export and fine separation structure 2 The in-pipe high-efficiency separation of the liquid phase and the gas phase is driven to be produced, thereby greatly reducing the volume of a device for separating the liquid phase and the gas phase, improving the gas-liquid ratio and the gas speed range of the separation device, obviously reducing the manufacturing cost and facilitating the separation of CO 2 The method is widely applied to the oil-extraction process.
(3) The invention adopts the downward gas-liquid pre-separation device to ensure that the produced gas-liquid two-phase fluid reduces the impact of gas and liquid bullets due to gravity, the expansion effect of a pipeline and the liquid level buffer effect in the U-shaped pipe; the 4 swirl blades with the 45-degree inclination angle can increase the swirl strength of the gas and the liquid while meeting certain pipeline resistance, and strengthen the centrifugal force born by liquid drops; the liquid taking port along the tangential direction of the liquid level rotation streamline reduces the flow resistance of the liquid film, so that the thin liquid film flows out of the liquid storage device along the liquid taking port more easily; the shrinkage pipe structure separates the central rotational flow gas and the wall liquid film, reduces the carrying effect of the gas on liquid drops, and increases the gas-liquid separation efficiency; the T-shaped straight tee structure of the gas fine separation device can strengthen the collection of liquid drops separated for the second time; the liquid has a rotating speed, the thin liquid film close to the wall surface has small kinetic energy, the liquid flows downwards in the liquid storage device in a rotational flow way from the main pipeline, the flow guiding effect can be achieved through the flow guiding plate and the T-shaped straight tee structure in the tangential direction of the liquid taking port, the resistance of the liquid film flowing out is reduced, and the thin liquid film close to the wall surface can smoothly flow out. Finally, the liquid level meter and the valve which are arranged inside the device form a liquid level regulating device together, so that the liquid production discharge flow in the device is regulated, the gas-liquid flow in the device is stabilized, and the efficient separation of the gas and the liquid in the device is ensured.
Description of the drawings:
FIG. 1 is a CO of the present invention 2 The overall structure of the driving output liquid pipe type gas-liquid separation device is schematically shown.
FIG. 2 is a schematic view of a liquid film leading-out device according to the present invention.
FIG. 3 is an enlarged view of a portion of the first pixel shrink tube and the surrounding joint in the liquid film guiding device according to the present invention.
FIG. 4 is a schematic cross-sectional view of a liquid film leading-out device according to the present invention.
FIG. 5 is a schematic cross-sectional structure of a gas fine separation device of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples.
As shown in fig. 1-5, a CO 2 The device for driving the output liquid pipeline type gas-liquid separation comprises a horizontal inlet pipe (1), a gas-liquid pre-separation device (2), a cyclone device (3), a liquid film guiding-out device (4), a gas fine separation device (5) and a liquid storage device (6)) An S-shaped pipe (7), a dry gas outlet pipe (8) and a liquid production discharge pipe (9).
The horizontal inlet pipe (1), the gas-liquid pre-separation device (2) and the second Y-shaped tee joint (11) are connected through a first Y-shaped tee joint (10), and a first valve (13) is arranged between the first Y-shaped tee joint (10) and the second Y-shaped tee joint (11).
The second Y-shaped tee joint (11) is respectively connected with the first Y-shaped tee joint (10), the straight pipe (12) and the gas-liquid pre-separation device (2), and a liquid level meter (15) is arranged in the gas-liquid pre-separation device (2).
One end of the S-shaped pipe (7) is connected with the gas-liquid pre-separation device (2), the other end of the S-shaped pipe is connected with the liquid storage device (6), and a second valve (14) is arranged in the S-shaped pipe.
A rotational flow device (3) is arranged between the straight pipe (12) and the gradually-expanding pipe (16), and an outlet of the gradually-expanding pipe (16) is connected with a liquid film guiding device (4).
The liquid film guiding device (4) is provided with a first liquid taking port (17) and a second liquid taking port (18) along the tangential direction of a gas-liquid rotation streamline, the first liquid taking port and the second liquid taking port are respectively positioned at the left side and the right side of the device, and the tail end of a pipeline is provided with a semicircular annular gap; wherein the opening of the second liquid taking port (18) is inclined upwards, the inclination angle is 50-53 degrees, and a semicircular arc guide baffle (21) is arranged in the tangential direction of the side opening; the first liquid taking port (17) is downward in opening, a vertical flow guide baffle (23) is arranged in the tangential direction of the side opening, and the inclination angle of the axial directions of the two liquid taking ports is 42-45 degrees; a first element shrinkage tube (19) is arranged above the semicircular notch at the tail end of the pipeline of the liquid film guiding device (4).
The upstream of the gas fine separation device (5) is connected with a first element shrinkage tube (19) at the tail end of the liquid film guiding device (4), and the inner diameters of the two are the same; the bottom of the pipeline of the gas fine separation device (5) is a square notch, the edge of the notch is tangent to the semicircular cross section of the pipeline, the length is 100mm, and the width is 26mm; the tail end of the gas fine separation device (5) is provided with a second shrinkage tube (26) which is communicated with a dry gas outlet tube (8).
The liquid film collecting device is characterized in that the first liquid storage device (6 a) and the second liquid storage device (6 b) are respectively communicated with an upstream liquid film leading-out device (4) and a gas fine separation device (5) through a first gradually-reducing deformation pipe (20) and a second gradually-reducing pipe (22), an interface is arranged on the side face of a pipeline of the first liquid storage device (6 a) and is connected with an S-shaped pipe (7), a liquid level meter (24) is arranged in the second liquid storage device (6 b), and the other ends of the first liquid storage device (6 a) and the second liquid storage device (6 b) are respectively connected into a liquid production discharge pipe (9) through a first gradually-reducing pipe (27) and a second gradually-reducing pipe (28). The third valve (25) is arranged at the outlet of the liquid production discharge pipe (9).
The horizontal inlet pipe (1), the first valve (13), the straight pipe (12) and the cyclone device (3) are coaxially arranged and are all positioned at the same horizontal height.
The liquid level value in the gas-liquid pre-separation device (2) is controlled by a liquid level meter (15) and a second valve (14).
The cyclone device (3) is formed by rotating four semi-elliptic sheets with the thickness of 1 millimeter around the axis of the circular tube, the included angle between the semi-elliptic sheets and the section of the pipeline is 45 degrees, and the semi-elliptic sheets and the inner wall of the circular tube are of an integral structure.
The included angle between the inclined section and the horizontal section of the first Y-shaped tee joint (10) is 15-30 degrees, and the included angle between the inclined section and the horizontal section of the second Y-shaped tee joint (10) is 70-75 degrees.
The outer wall of the pipeline of the first pixel shrinkage pipe (19) and the outer wall of the pipeline of the second pixel shrinkage pipe (26) are conical, the gap between the outer wall surface of the first pixel shrinkage pipe (19) and the inner wall surface of the liquid film guiding-out device (4) is 4-6 mm, and the difference between the inner diameter of the first pixel shrinkage pipe and the inner diameter of the pipeline of the liquid film guiding-out device (4) is less than 10mm; the gap between the outer wall surface of the second pixel shrinkage tube (26) and the inner wall surface of the gas fine separation device (5) is 4-7 mm, and the difference between the inner diameter of the second pixel shrinkage tube (26) and the inner diameter of a pipeline of the gas fine separation device (5) is smaller than 14mm; the lengths of the first and second pixel shrinking pipes (19, 26) are 15-20 mm.
The invention further discloses a gas-liquid separation method of the separation device, which specifically comprises the following steps:
(1) The device is arranged on CO 2 In a liquid production conveying pipeline of the oil extraction system, the flow pattern of the produced gas and liquid in the pipeline is stratified flow or annular flow, and the thickness distribution of a liquid film in a horizontal pipe is thin at the upper part and thick at the lower part; the first valve (13) is properly regulated, so that the produced mixed gas-liquid enters the gas-liquid pre-separation device (2), and the gas and the liquid are separated in the gas-liquid pre-separation device (2).
(2) The separated liquid is discharged into the liquid storage device (6) through the S-shaped pipe (7), and a liquid level meter (15) with the liquid level of the liquid passing through the liquid level meter and a second valve (14) in the S-shaped pipe (7) are regulated together, so that the impact of the liquid due to overlarge flow rate is well buffered.
(3) The separated gas enters the main pipeline through the second Y-shaped tee joint, and after being mixed with the gas and liquid at the upstream of the main pipeline through the first valve (13), the gas and liquid in the straight pipe (12) enters the cyclone device (3) through the straight pipe (12), the gas and liquid in the straight pipe (12) are thrown to the vicinity of the pipe wall due to the high density under the centrifugal force effect generated by the cyclone in the cyclone device (3), the gas and liquid are converged to form a liquid film near the pipe wall, the gas phase with the low density is converged at the center of the pipeline, the cyclone device (3) converts the gas-liquid two-phase fluid into a gas core-liquid film annular flow, and the liquid film and the gas both flow forwards with the rotational kinetic energy.
(4) After passing through the gradual expanding pipe (16), the circulating cross-sectional area of the liquid film in the annular flow type is increased, the flow velocity of the liquid film and liquid drops is reduced, and the liquid film still presents annular flow. When passing through the downstream liquid film guiding device, the liquid film and liquid drops are guided downwards along the tangential liquid taking opening under the action of centrifugal force and gravity on the right side in the flowing direction; on the left side of the flowing direction, the liquid film flows upwards obliquely along the rotating flow line and is guided out by the semicircular arc guide plate, and finally flows downwards; the residual liquid drops enter the gas fine separation device (5) through the first pixel shrinkage tube (19) along with the swirling flow carried by the gas, the liquid drops are carried to the pipe wall by the gas due to the centrifugal effect, flow downwards along the pipe wall, the gas spirals forwards, the gas and the liquid drops are finally separated by the second pixel shrinkage tube (26), and the dry gas enters and flows out of the separation device through the dry gas outlet pipe (8).
(5) The liquid film guiding device (4) and the liquid produced by the gas fine separation device (5) flow downwards along with the pipe wall of the liquid storage device (6), and flow out of the separation device through the liquid produced outlet pipe (9) after being collected with the liquid produced discharged from the bottom of the gas liquid pre-separation device (2), thereby realizing CO 2 And (3) separating gas phase and liquid phase of the flooding produced liquid.
When the oil extraction starts, the gas speed is low, and under the condition of high liquid yield (small gas-liquid ratio), most of the liquid yield flows into the gas-liquid pre-separation device due to the closing of the first valve. The liquid level control system formed by the liquid level gauge and the second valve adjusts the liquid level height in the gas-liquid pre-separation device, so that the gas and the liquid are buffered and then separated. After the gas is stabilized, the gas flows into the main pipeline and a part of liquid enters the cyclone device for cyclone through the side outlet and the Y-shaped tee joint. Because the gas speed is low, stable annular flow cannot be formed, a liquid film can be gathered at the bottom of a pipeline along with the flow, after entering a liquid film guiding device, a part of gathered liquid is separated by a shrinkage pipe and flows out from a notch at the bottom of the annular chamber to enter a liquid storage device; residual gas and liquid enter a gas fine separation device, liquid gathers and flows downwards through a straight tee structure, gas is separated from liquid drops through a shrinkage tube, and finally obtained dry gas is discharged through a pipeline.
After oil extraction is performed for a period of time, after the produced gas and liquid quantity reaches a stable state, the gas speed is higher, and under the condition of less produced liquid quantity (large gas-liquid ratio), the gas-liquid two phases in the pipeline flow in a ring shape, only a small part of liquid separated in the gas-liquid pre-separation device is separated, the first valve is opened, and most of produced gas and liquid enters the downstream cyclone device through the horizontal pipeline. The gas phase and the liquid phase after rotational flow form gas core-liquid film annular flow which has tangential velocity and flows in a spiral forward form. The liquid film on the wall of the annular flowing pipe is divided into three layers: an adhesive sub-layer (near wall), a base film (intermediate to the liquid film) and waves (gas-liquid interface). The viscous sub-layer is close to the pipe wall, has large velocity gradient and smaller kinetic energy; the base film is positioned in the middle of the liquid film, has proper kinetic energy and is less affected; the wave layer is a gas-liquid interface, the kinetic energy of the wave layer is large, but the wave layer is easily absorbed by gas, and small liquid drops in the wave layer can be carried by the gas for the second time. Because the liquid yield is less, the thickness of the formed liquid film is smaller, and therefore, the proportion of the viscous sub-layer close to the wall surface to the whole liquid film is larger. The integral kinetic energy of the liquid film is reduced, the gradual expansion pipe reduces the axial pressure drop loss in the pipeline, and meanwhile, liquid is taken through the tangential liquid taking port mode with minimum resistance, so that the thin liquid film can have sufficient kinetic energy to flow out into the liquid storage device along the liquid taking port under the action of gravity. Meanwhile, the shrinkage pipe separates the high-gas-speed rotational flow gas core from the liquid film, the inner diameter change is smaller, the liquid drop carrying caused by the gas negative pressure shrinkage condition is reduced, and the gas phase and the liquid phase can be separated to the greatest extent. And finally, carrying out secondary cyclone separation on the liquid drops with very few residues through a gas fine separation device. When the liquid amount is large (the gas-liquid ratio is moderate), the gas-liquid pre-separation device divides the flow through the liquid level and the inclined pipeline, so that the impact of the gas bomb and the liquid bomb on the cyclone is reduced, the cyclone device can normally operate, and stable cyclone gas-liquid is obtained. Two relative liquid taking openings in the liquid film guiding device can just meet the requirement of completely taking out the rotational flow liquid film because the length of the two relative liquid taking openings is larger than one half of the screw pitch. The guide plates at the corresponding sides of the liquid inlet can guide liquid film fluid, so that liquid can be guided out rapidly, and liquid collecting port effusion is prevented. The gas fine separation device adopts a tangential liquid taking mode, so that the influence on the gas rotational flow in the main pipeline is small, and residual liquid drops can be accumulated on the pipe wall and are isolated by the separation shrinkage pipe. The liquid level adjusting device in the whole device adjusts the liquid level height in each structure, so that gas phase and liquid phase in the pipeline flow out of the pipeline through which the gas phase and the liquid phase should pass, and the gas-liquid separating device can operate efficiently and normally.
The device structure designed by the invention is applied to CO 2 The high-efficiency separation of gas and liquid in the on-line pipeline can be realized under the working conditions of different gas speeds and different gas-liquid ratio ranges in the field of oil-driving and oil-extraction processes. The invention greatly reduces CO 2 The volume of the gas-liquid separation device in the driving process reduces the manufacturing cost of the separation device and completes CO 2 On-line tubular gas-liquid efficient separation for flooding extraction, and is convenient for CO 2 The method is widely applied to the oil-extraction process.
Claims (6)
1. CO (carbon monoxide) 2 Drive output liquid pipeline formula gas-liquid separation's device, its characterized in that installs at CO 2 In the oil extraction system pipeline, the device comprises a horizontal inlet pipe (1), a gas-liquid pre-separation device (2), a cyclone device (3), a liquid film guiding-out device (4), a gas fine separation device (5), a liquid storage device (6), an S-shaped pipe (7), a dry gas outlet pipe (8) and a liquid production discharge pipe (9);
the horizontal inlet pipe (1), the gas-liquid pre-separation device (2) and the second Y-shaped tee joint (11) are connected through a first Y-shaped tee joint (10), and a first valve (13) is arranged between the first Y-shaped tee joint (10) and the second Y-shaped tee joint (11); the horizontal inlet pipe (1), the first valve (13), the straight pipe (12) and the cyclone device (3) are coaxially arranged and are all positioned at the same horizontal height; the included angle between the inclined section and the horizontal section of the first Y-shaped tee joint (10) is 15-30 degrees, and the included angle between the inclined section and the horizontal section of the second Y-shaped tee joint (11) is 70-75 degrees;
the gas-liquid pre-separation device (2) is obliquely arranged downwards, and the liquid level value in the gas-liquid pre-separation device is controlled by a liquid level meter (15) and a second valve (14);
the second Y-shaped tee joint (11) is respectively connected with the first Y-shaped tee joint (10), the straight pipe (12) and the gas-liquid pre-separation device (2), and a liquid level meter (15) is arranged in the gas-liquid pre-separation device (2);
one end of the S-shaped pipe (7) is connected with the gas-liquid pre-separation device (2), the other end of the S-shaped pipe is connected with the liquid storage device (6), and a second valve (14) is arranged in the S-shaped pipe;
a rotational flow device (3) is arranged between the straight pipe (12) and the gradually-expanding pipe (16), and the outlet of the gradually-expanding pipe (16) is connected with a liquid film guiding device (4);
the cyclone device (3) is formed by rotating four semi-elliptic sheets with the thickness of 1 millimeter around the axis of the circular tube, the included angle between the semi-elliptic sheets and the section of the pipeline is 45 degrees, and the semi-elliptic sheets and the inner wall of the circular tube are of an integral structure;
the liquid film guiding device (4) is provided with a first liquid taking port (17) and a second liquid taking port (18) along the tangential direction of a gas-liquid rotation streamline, the first liquid taking port and the second liquid taking port are respectively positioned at the left side and the right side of the device, and the tail end of a pipeline is provided with a semicircular annular gap; wherein the opening of the second liquid taking port (18) is inclined upwards, the inclination angle is 50-53 degrees, and a semicircular arc guide baffle (21) is arranged in the tangential direction of the side opening; the first liquid taking port (17) is downward in opening, a vertical flow guide baffle (23) is arranged in the tangential direction of the side opening, and the inclination angle of the axial directions of the two liquid taking ports is 42-45 degrees; a first shrinkage pipe (19) is arranged above the semicircular notch at the tail end of the pipeline of the liquid film guiding device (4);
the upstream of the gas fine separation device (5) is connected with a first shrinkage tube (19) at the tail end of the liquid film guiding device (4), and the inner diameters of the two shrinkage tubes are the same; the tail end of the gas fine separation device (5) is provided with a second shrinkage tube (26) which is communicated with a dry gas outlet tube (8);
the first liquid storage device (6 a) and the second liquid storage device (6 b) are respectively communicated with an upstream liquid film guiding-out device (4) and a gas fine separation device (5) through a first tapered deformation pipe (20) and a second tapered deformation pipe (22), an interface is arranged on the side surface of a pipeline of the first liquid storage device (6 a) and is connected with an S-shaped pipe (7), a liquid level meter (24) is arranged in the second liquid storage device (6 b), and the other ends of the first liquid storage device (6 a) and the second liquid storage device (6 b) are respectively connected into a liquid production discharge pipe (9) through a first reducing pipe (27) and a second reducing pipe (28); the third valve (25) is arranged at the outlet of the liquid production discharge pipe (9).
2. The CO according to claim 1 2 The device for driving the gas-liquid separation of the produced liquid pipeline is characterized in that the bottom of the pipeline of the gas fine separation device (5) is a square notch, and the edge of the notch is tangent to the semicircular cross section of the pipeline, and the length is 100mm and the width is 26mm.
3. The CO according to claim 1 2 The device for separating gas from liquid by driving the produced liquid pipeline is characterized in that the lengths of the first shrinkage pipe (19) and the second shrinkage pipe (26) are 15-20 mm.
4. The CO according to claim 1 2 Drive output liquid pipeline formula gas-liquid separation's device, its characterized in that, the pipeline outer wall of first draw (19) and second draw (26) is the toper, and clearance between first draw (19) outer wall and the liquid film guiding device (4) inner wall is 4~6mm, and first draw internal diameter and liquid film guiding device (4) pipeline internal diameter differ by less than 10mm.
5. The CO according to claim 1 2 Device for driving produced liquid pipeline type gas-liquid separation, and special device thereofThe gas fine separation device is characterized in that a gap between the outer wall surface of the second shrinkage tube (26) and the inner wall surface of the gas fine separation device (5) is 4-7 mm, and the difference between the inner diameter of the second shrinkage tube (26) and the inner diameter of a pipeline of the gas fine separation device (5) is smaller than 14mm.
6. A CO according to any one of claims 1 to 5 2 The separation method of the drive produced liquid pipeline type gas-liquid separation device is characterized by comprising the following steps of:
(1) The device is arranged on CO 2 In a liquid production conveying pipeline of the oil extraction system, the flow pattern of the produced gas and liquid in the pipeline is stratified flow or annular flow, and the thickness distribution of a liquid film in a horizontal pipe is thin at the upper part and thick at the lower part; the first valve (13) is properly regulated, so that the produced mixed gas-liquid enters the gas-liquid pre-separation device (2), and the gas and the liquid are separated in the gas-liquid pre-separation device (2);
(2) The separated liquid is discharged into a liquid storage device (6) through an S-shaped pipe (7), and a liquid level meter (15) with the liquid level of the liquid passing through is regulated together with a second valve (14) in the S-shaped pipe (7), so that the impact of the liquid due to overlarge flow rate is well buffered;
(3) The separated gas enters the main pipeline through a second Y-shaped tee joint, and is mixed with gas and liquid at the upstream of the main pipeline through a first valve (13), and then enters the cyclone device (3) through a straight pipe (12), the gas and the liquid in the straight pipe (12) are thrown to the vicinity of the pipeline wall due to higher density under the centrifugal force effect generated by a cyclone in the cyclone device (3), and are converged to form a liquid film at the vicinity of the pipeline wall, the gas phase with lower density is converged at the center of the pipeline, the cyclone device (3) converts the gas-liquid two-phase fluid into a gas core-liquid film annular flow, and the liquid film and the gas both flow forward with rotational kinetic energy;
(4) After passing through the gradual expanding pipe (16), the circulating cross-sectional area of the liquid film of the annular flow pattern is increased, the flow velocity of the liquid film and the liquid drops is reduced, but the liquid film still presents annular flow, and when passing through the downstream liquid film guiding device, the liquid film and the liquid drops are guided downwards along the tangential liquid taking opening under the action of centrifugal force and gravity on the right side in the flowing direction; on the left side of the flowing direction, the liquid film flows upwards obliquely along the rotating flow line and is guided out by the semicircular arc guide plate, and finally flows downwards; residual liquid drops enter a gas fine separation device (5) through a first shrinkage pipe (19) along with the swirling flow carried by the gas, the liquid drops are carried to the pipe wall by the gas under the centrifugal action, flow downwards along the pipe wall, the gas spirals forwards, the gas and the liquid drops are finally separated by a second shrinkage pipe (26), and dry gas enters the gas fine separation device and flows out of the separation device through a dry gas outlet pipe (8);
(5) The liquid film guiding device (4) and the liquid produced by the gas fine separation device (5) flow downwards along with the pipe wall of the liquid storage device (6), and flow out of the separation device through the liquid production discharge pipe (9) after being collected with the liquid produced discharged from the bottom of the gas liquid pre-separation device (2), thereby realizing CO 2 And (3) separating gas phase and liquid phase of the flooding produced liquid.
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| CN107882546A (en) * | 2016-09-29 | 2018-04-06 | 中国石油化工股份有限公司 | High water cut low yield gas oil well liquid-producing three-phase metering mechanism and method |
| CN111306063A (en) * | 2020-02-29 | 2020-06-19 | 罗辉 | Gas-liquid cooling separation system for liquid ring pump |
| CN111569627A (en) * | 2020-04-30 | 2020-08-25 | 浙江省天正设计工程有限公司 | Efficient recovery device and process for continuous double-suction treatment of tail gas |
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| JP5439026B2 (en) * | 2009-05-11 | 2014-03-12 | 株式会社神戸製鋼所 | Gas-liquid separator |
| CN106964200A (en) * | 2017-05-09 | 2017-07-21 | 中国海洋石油总公司 | A kind of separator under water and method with pre-separation pipeline |
| CN109141563B (en) * | 2018-09-30 | 2024-05-28 | 长江大学 | Z-type natural gas moisture real-time measurement device and method based on in-pipe phase separation |
| CN111495040B (en) * | 2020-04-30 | 2021-03-16 | 西安交通大学 | Horizontal pipeline type gas-liquid separation device and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107882546A (en) * | 2016-09-29 | 2018-04-06 | 中国石油化工股份有限公司 | High water cut low yield gas oil well liquid-producing three-phase metering mechanism and method |
| CN111306063A (en) * | 2020-02-29 | 2020-06-19 | 罗辉 | Gas-liquid cooling separation system for liquid ring pump |
| CN111569627A (en) * | 2020-04-30 | 2020-08-25 | 浙江省天正设计工程有限公司 | Efficient recovery device and process for continuous double-suction treatment of tail gas |
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