CN107557087A - A kind of spiral-flow type gas-liquid separation device and method - Google Patents
A kind of spiral-flow type gas-liquid separation device and method Download PDFInfo
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Abstract
The invention discloses a kind of spiral-flow type gas-liquid separation device and method.Spiral-flow type gas-liquid separation device is provided with cylinder (3), the gas-liquid inlet tube (1) of vertical and cylindrical, and the inner cylinder (5) of vertical and cylindrical is provided with cylinder.Spiral plate (7) is provided with the annular space formed between cylinder and inner cylinder, helical duct (6) is formed between cylinder madial wall, inner cylinder lateral wall and neighbouring two circles spiral plate.Gas-liquid inlet tube is set diagonally downward, the helical duct entrance at the top of the outlet insertion helical duct of gas-liquid inlet tube.Inner cylinder is provided with aperture area, and aperture area is provided with steam vent (8).There is gas phase cushion space (12) and cyclonic separation section (13) in cylinder.The invention discloses the method that spiral-flow type gas-liquid separation is carried out using above-mentioned spiral-flow type gas-liquid separation device.Present invention is mainly used for carry out gas-liquid separation to the higher low gas liquid rate gas-liquid mixture of liquid phase viscosity.
Description
Technical field
The present invention relates to a kind of spiral-flow type gas-liquid separation dress for gas-liquid separation of oil gas field oil vapor treatment technical field
Put and spiral-flow type gas-liquid separating method.
Background technology
In oil gas field oil vapor treatment technical field, often gas-liquid separation is carried out using column spiral-flow type gas-liquid separation device.Post
Shape spiral-flow type gas-liquid separation device is provided with cylinder, the gas-liquid inlet tube of vertical and cylindrical, and gas is respectively equipped with the top and bottom of cylinder
Phase outlet and liquid-phase outlet pipe, gas-liquid inlet tube are connected along the tangential of cylinder with cylinder.Column spiral-flow type gas-liquid separation device
Interior centrifugal force field is the ideal place that gas-liquid is separated, and the difference of gas-liquid density can cause centrifugal force suffered by gas-liquid number to be present
The difference of magnitude.But the effect of above-mentioned gas-liquid separation is had a great influence by gas liquid ratio.Moved in the gas-liquid polyphase flow of high gas-liquid ratio
During, gas phase velocity is higher, and gas phase drives liquid phase to form the more violent flow pattern such as slug flow, mist flow.This feature
There is inherent advantage for gas-liquid cyclonic separation, gas-liquid separation can be promoted.Gas liquid ratio is the volume ratio of gas phase and liquid phase；Gas
Liquor ratio is referred to as high gas-liquid ratio when being higher than 8, is referred to as low gas liquid rate during less than 8.Different from the gas-liquid mixture of high gas-liquid ratio, low gas-liquid
Ratio in the gas-liquid mixture of ratio shared by liquid phase is higher, more representational flow pattern such as bubble flow.Relatively low energy density
It is unfavorable for forming the larger eddy flow field of tangential velocity, has influence on gas-liquid separation effect.Especially in the higher situation of liquid phase viscosity
Under (such as furol viscosity is more than 300 mpas, and viscosity measures within the temperature range of 20~50 DEG C), use column spiral-flow type gas
Liquid separating apparatus carries out the less effective of gas-liquid separation, and gas of the diameter more than 200 microns can be still carried in the liquid phase isolated
Bubble.
The content of the invention
It is an object of the invention to provide a kind of spiral-flow type gas-liquid separation device and method, to solve existing spiral-flow type gas-liquid
The low gas liquid rate gas-liquid mixture higher to liquid phase viscosity present in isolation technics carries out asking for the less effective of gas-liquid separation
Topic.
To solve the above problems, the technical solution adopted by the present invention is：A kind of spiral-flow type gas-liquid separation device, provided with vertical
Columnar cylinder, gas-liquid inlet tube, the top of cylinder are provided with cylinder top plate, gaseous phase outlet pipe, and the bottom of cylinder is provided with cylinder
Bottom plate, liquid-phase outlet pipe, it is characterised in that：The inner cylinder of vertical and cylindrical, the ring formed between cylinder and inner cylinder are provided with cylinder
Spiral plate is provided with shape space, helical duct is formed between cylinder madial wall, inner cylinder lateral wall and neighbouring two circles spiral plate,
Gas-liquid inlet tube is set diagonally downward, the helical duct entrance at the top of the outlet insertion helical duct of gas-liquid inlet tube, on inner cylinder
Provided with aperture area, aperture area is provided with steam vent, and the top of spiral plate is provided with cover plate, and the space between cover plate and cylinder top plate is gas
Phase cushion space, the lower section of inner cylinder are provided with spin-ended part, and the space between inner cylinder bottom and spin-ended part top is cyclonic separation
Section.
The method that spiral-flow type gas-liquid separation is carried out using above-mentioned spiral-flow type gas-liquid separation device, it is characterised in that：Gas-liquid
Mixture enters helical duct by the outlet of gas-liquid inlet tube, along the downward helical flow of helical duct, carries out first time gas-liquid
Cyclonic separation, the gas phase isolated in helical duct enter the inner chamber of inner cylinder through steam vent and flow up, buffered into gas phase
Space, flowed out after buffering through gaseous phase outlet pipe, the liquid phase isolated in helical duct is led to from the spiral of helical duct bottom
Road outlet flows into cyclonic separation section and carries out second of gas-liquid cyclonic separation, the gas phase isolated in cyclonic separation section flows up,
Into the inner chamber of inner cylinder, gas phase cushion space is entered after merging with the gas phase isolated in helical duct, is most gone out afterwards through gas phase
Mouth pipe flows out, and the liquid phase isolated in cyclonic separation section flows downwardly through spin-ended part, is most flowed out afterwards through liquid-phase outlet pipe.
Using the present invention, there is following beneficial effect：During gas-liquid separation, gas-liquid mixture is first in helical duct
Interior progress first time gas-liquid cyclonic separation, the liquid phase isolated flow into cyclonic separation section and carry out second of gas-liquid cyclonic separation again.
Bubble of the diameter more than 200 microns is there is no by separating twice, in liquid phase.Present invention is mainly used for liquid phase viscosity
Higher low gas liquid rate gas-liquid mixture carries out gas-liquid separation, can obtain preferable separating effect.
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description.Accompanying drawing and specific embodiment party
Formula is not intended to limit the scope of protection of present invention.
Brief description of the drawings
Fig. 1 is the structural representation of spiral-flow type gas-liquid separation device of the present invention.
Fig. 2 is the A-A sectional views (amplification) in Fig. 1.
Fig. 3 is the dimensional structure diagram (amplification) of spin-ended part shown in Fig. 1.
For Fig. 1 into Fig. 3, same reference numerals represent identical technical characteristic.
Embodiment
Referring to Fig. 1, Fig. 2 and Fig. 3, spiral-flow type gas-liquid separation device of the invention is provided with the cylinder 3 of vertical and cylindrical, gas-liquid
Inlet tube 1.The top of cylinder 3 is provided with cylinder top plate, gaseous phase outlet pipe 11, and the bottom of cylinder 3 is provided with cylinder bottom plate, liquid-phase outlet
Pipe 10.The inner cylinder 5 of vertical and cylindrical is coaxially arranged with cylinder 3 with cylinder 3, inner cylinder 5 is located in cylinder 3 in the height direction
Top.Spiral plate 7, the inward flange of spiral plate 7 and the outside of inner cylinder 5 are provided with the annular space formed between cylinder 3 and inner cylinder 5
Wall is connected, and the outward flange of spiral plate 7 is connected with the madial wall of cylinder 3.The madial wall of cylinder 3, the lateral wall of inner cylinder 5 and neighbouring two
Helical duct 6 is formed between circle spiral plate 7.Gas-liquid inlet tube 1 is set diagonally downward, and the outlet of gas-liquid inlet tube 1 is through one piece
The helical duct entrance at the top of plugging plate insertion helical duct 6, plugging plate are located at helical duct porch.It is of the present invention to incline
Obliquely, it is depending on the flow direction by gas-liquid mixture.In helical duct porch, gas-liquid inlet tube 1 and the phase of helical duct 6
Cut, direction of the gas-liquid inlet tube 1 with helical duct 6 diagonally downward is consistent.The cross-sectional area of helical duct 6 typically enters with gas-liquid
The cross-sectional area of mouth pipe 1 is identical.The cross-sectional area of helical duct 6 should be able to ensure the gas-liquid of the flowing in helical duct 6
Liquid phase in mixture can produce the centrifugal force with 5~10 acceleration of gravity, so both can guarantee that gas-liquid separation effect,
And can prevent gas-liquid flow velocity exceed erosion rate and to gas-liquid contact to part cause to denude strongly.
Gas-liquid inlet tube 1 should typically set negative throat noz(zle) in the pipeline section close to its outlet, so that gas-liquid mixture accelerates
Spray.Negative throat noz(zle) shown in Fig. 1 and Fig. 2 is existing, is made up of the madial wall of plug 2 and gas-liquid inlet tube 1, and plug 2 is solid
Due on the madial wall of gas-liquid inlet tube 1.The system of plug 2 falls a part from side beveling with a cylinder and is made, scarf
Tapered channels are formed between the madial wall of gas-liquid inlet tube 1, the outlet of tapered channels is the spout 20 of negative throat noz(zle).
Inner cylinder 5 is provided with aperture area, and aperture area is provided with steam vent 8.Steam vent 8 is used to make to isolate in helical duct 6
Gas phase through steam vent 8 enter inner cylinder 5 inner chamber.
The top of spiral plate 7 is provided with cover plate 4, and cover plate 4 is annular.The outward flange of cover plate 4 and the madial wall phase of cylinder 3
Even, the edge of the centre bore of cover plate 4 is connected with the top of inner cylinder 5.Space between cover plate 4 and cylinder top plate is gas phase cushion space
12, the height a of gas phase cushion space 12 are generally 1~3 times of the interior diameter of cylinder 3.The interior diameter of cylinder 3 and inner cylinder 5, mainly
Determined according to conditions such as the gas liquid ratio of gas-liquid mixture and flows.The lower section of inner cylinder 5 is provided with spin-ended part, and spin-ended part is located at liquid
The top of phase outlet 10.Space between the bottom of inner cylinder 5 and spin-ended part top is cyclonic separation section 13, cyclonic separation section 13
Height b be generally 5~10 times of the interior diameter of cylinder 3.
Spiral plate 7 is generally right helicoid shape, and the lift angle of the circular helix that spiral plate 7 intersects with inner cylinder 5 is generally 5~
10 degree.The angle (angle between gas-liquid inlet tube 1 and horizontal plane) of gas-liquid inlet tube 1 diagonally downward and the liter of circular helix
Angle is essentially identical.Spiral plate 7 and helical duct 6 can be left-handed (as shown in Figure 1), or dextrorotation (figure omits).Gas-liquid
The setting of inlet tube 1 will be in consideration of it, the gas-liquid mixture from its outlet outflow should be along 6 downward spiral flow of helical duct
It is dynamic.
Helical duct 6 typically sets 10~15 circles.Generally, to the circle of inverse the 2nd or fallen in the 2nd circle or the 3rd circle helical duct 6
The aperture area that number the 3rd is enclosed on the region setting inner cylinder 5 of helical duct 6.The number of turns of above-mentioned helical duct 6 counts from top to bottom, falls
A few are several, are to count from bottom to top.
The generally circular or rectangle of steam vent 8, or other shapes.The area one of single steam vent 8
As be 400~1600 square millimeters, the percent opening of aperture area is generally 60%~70% on inner cylinder 5.Circular steam vent 8 is typically adopted
With square or equilateral triangle arrangement.Above-mentioned shape and parameter, measured in the expansion plane of inner cylinder 5.
A kind of spin-ended part used in the present invention is by a cylindrical column 91 on the axial line of cylinder 3 and around column
91 4~6 pieces of rectangle risers 9 being uniformly arranged form and (6 pieces of rectangle risers 9 are provided that shown in Fig. 1, Fig. 2 and Fig. 3).Each piece of square
One end of shape riser 9 is fixed in the side wall of column 91, and the other end is connected with the madial wall of cylinder 3.The height c of rectangle riser 9
Generally 0.5~0.8 times of the interior diameter of cylinder 3.
The shape of cross section of gas-liquid inlet tube 1, gaseous phase outlet pipe 11 and liquid-phase outlet pipe 10 is typically circle.The present invention
The material of each part is generally stainless steel (such as 304 stainless steels), the connection or fixed typically using welding between part.
Explanation carries out the side of spiral-flow type gas-liquid separation using the spiral-flow type gas-liquid separation device of the present invention below in conjunction with the accompanying drawings
Method.Gas-liquid mixture in gas-liquid inlet tube 1 is after negative throat noz(zle) accelerates by the outlet of gas-liquid inlet tube 1 along helical duct 6
Tangentially enter helical duct 6, along 6 downward helical flow of helical duct, the is carried out using the spontaneous centrifugal force field of helical flow
Gas-liquid cyclonic separation.The gas phase isolated in helical duct 6 enters the inner chamber of inner cylinder 5 through steam vent 8, and at rear, gas phase pushes away
Flowed up in the presence of dynamic and buoyancy, enter gas phase cushion space 12 by the centre bore of cover plate 4, through gas after buffering
Phase outlet 11 flows to the gas phase treatment equipment in downstream.Con trolling index of the liquid holdup of above-mentioned gas phase not as the present invention.
The liquid phase isolated in helical duct 6 flows into cyclonic separation section 13 from the helical duct outlet of the bottom of helical duct 6
Carry out second of gas-liquid cyclonic separation.The gas phase isolated in cyclonic separation section 13 flows up, the inner chamber into inner cylinder 5, with
The gas phase isolated in helical duct 6 enters gas phase cushion space 12 after merging, and most flows to downstream through gaseous phase outlet pipe 11 afterwards
Gas phase treatment equipment.The liquid phase isolated in cyclonic separation section 13 flows downward in the presence of pressure and gravity, flows through only
By spin-ended (flowing of stopping the rotation) when revolving part.Liquid phase flows out from the bottom of spin-ended part, is most flowed afterwards through liquid-phase outlet pipe 10
Liquid phase processing equipment downstream.In Fig. 1 and Fig. 2 of the present invention, do not note reference arrow represent gas-liquid mixture, gas phase or
The flow direction of liquid phase.
During helical flow separation in above-mentioned helical duct 6 and the cyclonic separation in cyclonic separation section 13,
The region flowing that liquid phase tends near the madial wall of cylinder 3, gas phase tend to the axial line region flowing to cylinder 3.
Gas phase in above-mentioned gas-liquid mixture is usually natural gas, and liquid phase is usually the heavy oil that viscosity is more than 300 mpas
(viscosity measures within the temperature range of 20~50 DEG C).The gas liquid ratio of gas-liquid mixture is less than 8, usually 3~6.Entered by gas-liquid
The flow velocity of the gas-liquid mixture of the outlet outflow of mouth pipe 1 is generally 4~6 meter per seconds, and gas-liquid mixture stops in helical duct 6
The time is stayed to be generally 10~20 seconds.Residence time of the gas phase in gas phase cushion space 12 into gas phase cushion space 12 is general
For 5~10 seconds, the liquid phase into cyclonic separation section 13 stayed the time to be generally 15~20 seconds in cyclonic separation section 13.
The liquid phase flowed out from helical duct 6, comprises only bubble of a small amount of diameter more than 200 microns.These liquid phases are being revolved
Flow separation section 13 carries out second of gas-liquid cyclonic separation, can go out bubble separation of the contained a small amount of diameter more than 200 microns
Go.
Claims (7)
1. a kind of spiral-flow type gas-liquid separation device, cylinder (3), gas-liquid inlet tube (1) provided with vertical and cylindrical, cylinder (3)
Top is provided with cylinder top plate, gaseous phase outlet pipe (11), and the bottom of cylinder (3) is provided with cylinder bottom plate, liquid-phase outlet pipe (10), and it is special
Sign is：The inner cylinder (5) of vertical and cylindrical is provided with cylinder (3), in the annular space formed between cylinder (3) and inner cylinder (5)
Provided with spiral plate (7), spiral is formed between cylinder (3) madial wall, inner cylinder (5) lateral wall and neighbouring two circle spiral plate (7)
Passage (6), gas-liquid inlet tube (1) are set diagonally downward, the spiral shell at the top of the outlet insertion helical duct (6) of gas-liquid inlet tube (1)
Feeder connection is revolved, inner cylinder (5) is provided with aperture area, and aperture area is provided with steam vent (8), and the top of spiral plate (7) is provided with cover plate
(4), the space between cover plate (4) and cylinder top plate is gas phase cushion space (12), and the lower section of inner cylinder (5) is provided with spin-ended part,
Space between inner cylinder (5) bottom and spin-ended part top is cyclonic separation section (13).
2. spiral-flow type gas-liquid separation device according to claim 1, it is characterised in that：Spiral plate (7) is right helicoid shape,
The lift angle for the circular helix that spiral plate (7) intersects with inner cylinder (5) is 5~10 degree.
3. spiral-flow type gas-liquid separation device according to claim 1 or 2, it is characterised in that：Helical duct (6) setting 10~
15 circles.
4. spiral-flow type gas-liquid separation device according to claim 1 or 2, it is characterised in that：In the 2nd circle or the 3rd circle spiral
The region of passage (6) to the circle of inverse the 2nd or the circle helical duct of inverse the 3rd (6) sets the aperture area on inner cylinder (5).
5. spiral-flow type gas-liquid separation device according to claim 1 or 2, it is characterised in that：Steam vent (8) is shaped as justifying
Shape or rectangle, the area of single steam vent (8) is 400~1600 square millimeters, and the percent opening of aperture area is on inner cylinder (5)
60%~70%.
6. spiral-flow type gas-liquid separation device according to claim 1 or 2, it is characterised in that：Spin-ended part is by a root post
(91) 4~6 pieces of rectangle risers (9) composition and around column (91) being uniformly arranged, one end of each piece of rectangle riser (9) are fixed on vertical
In the side wall of post (91), the other end is connected with the madial wall of cylinder (3).
7. a kind of method that spiral-flow type gas-liquid separation is carried out using spiral-flow type gas-liquid separation device described in claim 1, its feature
It is：Gas-liquid mixture enters helical duct (6) by the outlet of gas-liquid inlet tube (1), along helical duct (6) downward spiral flow
It is dynamic, first time gas-liquid cyclonic separation is carried out, the gas phase isolated in helical duct (6) enters the interior of inner cylinder (5) through steam vent (8)
Chamber simultaneously flows up, into gas phase cushion space (12), is flowed out after buffering through gaseous phase outlet pipe (11), helical duct (6)
The liquid phase inside isolated flows into cyclonic separation section (13) from the helical duct outlet of helical duct (6) bottom and carries out second of gas-liquid
Cyclonic separation, the gas phase isolated in cyclonic separation section (13) flows up, the inner chamber into inner cylinder (5), and in helical duct
(6) gas phase isolated in enters gas phase cushion space (12) after merging, and is most flowed out afterwards through gaseous phase outlet pipe (11), cyclonic separation
The liquid phase isolated in section (13) flows downwardly through spin-ended part, is most flowed out afterwards through liquid-phase outlet pipe 10.
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| CN108654147A (en) * | 2018-08-28 | 2018-10-16 | 湖南大三湘茶油股份有限公司 | Edible oil froth breaker |
| CN110090470A (en) * | 2019-04-11 | 2019-08-06 | 北京康得利智能科技有限公司 | Centrifugal degasser |
| CN111299741A (en) * | 2020-03-24 | 2020-06-19 | 大连理工大学 | Device and method for removing bubbles in vacuum brazing filler metal |
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| CN118564227A (en) * | 2024-07-31 | 2024-08-30 | 东北石油大学三亚海洋油气研究院 | Downhole multiphase separation device for same-well injection and production |
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| CN115382339B (en) * | 2022-07-26 | 2024-05-07 | 中国石油大学(华东) | Ultrasonic carbon capture energy recovery device and system for industrial hydrogen production |
| CN115487669A (en) * | 2022-10-19 | 2022-12-20 | 厚成科技（南通）有限公司 | A absorb scrubbing tower for lithium hexafluorophosphate tail gas |
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| CN118564227A (en) * | 2024-07-31 | 2024-08-30 | 东北石油大学三亚海洋油气研究院 | Downhole multiphase separation device for same-well injection and production |
| CN118564227B (en) * | 2024-07-31 | 2024-10-08 | 东北石油大学三亚海洋油气研究院 | Downhole multiphase separation device for same-well injection and production |
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