CN110835565A - Natural gas-liquid separation device - Google Patents
Natural gas-liquid separation device Download PDFInfo
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- CN110835565A CN110835565A CN201911136162.7A CN201911136162A CN110835565A CN 110835565 A CN110835565 A CN 110835565A CN 201911136162 A CN201911136162 A CN 201911136162A CN 110835565 A CN110835565 A CN 110835565A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
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Abstract
The invention provides a natural gas-liquid separation device. The invention comprises a first cyclone separator, a Laval nozzle and a separation tank which are connected in sequence, wherein the separation tank comprises a tank body, an air inlet, an air outlet and a liquid outlet are arranged on the tank body, a liquid baffle is arranged on one side of the air inlet inside the tank body, and a second cyclone separator is arranged above the liquid baffle inside the tank body. According to the invention, natural gas firstly forms a cyclone effect in the first cyclone separator, and liquid is thrown onto the side wall and moves along the side wall under the action of centrifugal force; then, the gas lubricating oil in the natural gas is cooled into liquid drops through the Laval nozzle for speed increasing, pressure reducing and temperature reducing; the liquid drops directly impact a liquid baffle inside the separation tank to carry out primary separation; when the natural gas passes through the second cyclone separator, the secondary separation of gas phase and liquid phase is realized by the centrifugal force again, and the effect of gas-liquid separation of the natural gas is finally achieved; the gas-liquid separation efficiency is high, the separation effect is good, the phenomena of liquid phase crushing and entrainment can not occur, and the structure is simple.
Description
Technical Field
The invention relates to the technical field of natural gas processing, in particular to a natural gas-liquid separation device.
Background
Nowadays, with the shortage of energy sources, natural gas resources are more and more important. The natural gas consumption of China is huge and is in a steep stateAnd (4) a growing stage. In the long distance pipeline transportation of natural gas, compressors are used for pressurization, lubricating oil is needed for the operation of the compressors, and therefore, some lubricating oil used for pressurization of the compressors is entrained in the natural gas. Along with the change of the temperature and the pressure in the long-distance pipeline transportation process, lubricating oil is likely to be separated out from natural gas to form liquid, so that the pipeline is blocked. Meanwhile, acid gases such as H in natural gas2S and the like also dissolve in the lubricating oil, causing corrosion of the pipe. Therefore, the natural gas is treated and developed, the natural gas treatment cost in China is reduced, the energy conservation and emission reduction in the field of natural gas processing are realized, and the significance is great.
Currently, natural gas processing technology focuses mainly on dehydration and dealkylation of natural gas, for example: chinese patent CN204122261U discloses a natural gas tornado type supersonic cyclone separation device, which mainly comprises two major systems, namely a throttling acceleration system and a tornado type cyclone system, wherein the throttling acceleration system adopts a Laval nozzle, the tornado type cyclone system comprises a jacket, a rectangular nozzle, a cyclone cavity, an overflow section, a large cone section, a small cone section, an underflow section and a liquid collection tank, the outer wall of the jacket is connected with the Laval nozzle, a cylindrical cyclone cavity is fixed inside the jacket, a plurality of groups of rectangular nozzles are arranged on the outer wall of the cyclone cavity, the top of the cyclone cavity is communicated with the overflow section, the bottom of the cyclone cavity is connected with the small cone section through the large cone section, and the lower end of the small cone section is connected with the liquid collection tank through the underflow section; after the mixed natural gas is subjected to adiabatic expansion by the Laval nozzle, the speed reaches supersonic speed, and the mixed natural gas enters a tornado type cyclone system for gas-liquid separation. The cyclone separation device has the advantages of more compact structure, small volume, high separation efficiency, large treatment capacity and better purification effect; the cyclone separation device aims at the treatment of natural gas produced from offshore oil and gas fields, and the natural gas produced from offshore oil and gas fields has high content of water vapor and heavy hydrocarbon. The cyclone separation device reduces the temperature of natural gas to about minus 35 ℃ through throttling expansion. At this temperature, the condensed water and hydrocarbons contained in the natural gas liquefy and the liquid phase is separated off by means of a cyclone. However, the cyclone separation device is unreasonable in structural design, is suitable for high-liquid-content separation, and has the problems of low separation efficiency under the condition that liquid phases are less, and the problems of liquid phase crushing, entrainment and the like often exist under the condition that liquid phases are more, so that the separation efficiency is low, and the gas-liquid separation requirement of natural gas in long-distance pipeline transportation cannot be met.
Disclosure of Invention
The invention aims to provide a natural gas-liquid separation device, and aims to solve the problem that the separation efficiency of the natural gas-liquid separation device in the prior art is low due to unreasonable structural design.
In order to solve the technical problem, the technical scheme of the invention is realized as follows: comprises a first cyclone separator, a Laval nozzle and a separation tank; the first cyclone separator comprises a first air inlet end and a first air outlet end; the Laval nozzle comprises a second air inlet end and a second air outlet end, and the second air inlet end is connected with the first air outlet end; the separating tank comprises a tank body, wherein an air inlet, an air outlet and a liquid outlet are formed in the tank body, the air inlet is connected with the air outlet end of the second, a liquid baffle is arranged on one side of the air inlet in the tank body, and a second cyclone separator is arranged above the liquid baffle in the tank body.
According to the natural gas treatment device, natural gas to be treated sequentially passes through the first cyclone separator, the Laval nozzle and the separation tank, and sequentially passes through the liquid baffle and the second cyclone separator in the separation tank, so that gas-liquid separation in the natural gas is realized, the separated gas is discharged from the gas outlet, and the separated liquid is discharged from the liquid outlet. Firstly, forming a cyclone effect in the natural gas to be treated in the first cyclone separator, and throwing liquid onto the side wall and flowing along the side wall under the action of centrifugal force; then, the speed is increased, the pressure is reduced and the temperature is reduced through a Laval nozzle, so that the gaseous lubricating oil in the natural gas is cooled into liquid drops; after the liquid drops enter the separation tank, the liquid drops directly impact a liquid baffle inside the separation tank, and primary separation is carried out under the action of the liquid baffle; the liquid after the primary separation flows downwards, the gas after the primary separation flows upwards and passes through the second cyclone separator, the gas-liquid two-phase secondary separation is realized under the action of centrifugal force again, the separated gas continues to flow upwards and is discharged from the gas outlet, and the separated liquid flows downwards and is discharged from the liquid outlet, so that the effect of gas-liquid separation of natural gas is finally achieved. The gas-liquid separation device has the advantages of simple structure and scientific and reasonable design, is suitable for separation of high-liquid content liquid and separation under the condition of less liquid content, has high gas-liquid separation efficiency, does not generate the phenomena of liquid phase crushing and entrainment, has good separation effect, and is particularly suitable for gas-liquid separation of natural gas after long-distance pipeline transportation.
As a preferred embodiment, the second cyclone separator comprises a second pipe and a cyclone blade arranged in the second pipe, and a second gap is arranged between the edge of the cyclone blade and the inner surface of the second pipe; the equation of the swirl vane is as follows:in the formula: r is the inner diameter of the second conduit, δ is the length of the second gap, ω is the angular velocity, v is the velocity in the axial direction, and t is the time of movement. After the natural gas to be processed enters the second cyclone separator in the separation tank, spiral rotary motion is carried out under the action of the cyclone blades, gas-liquid separation is realized in the ascending process of the natural gas under the action of centrifugal force, liquid is thrown onto the inner wall of the second pipeline under the action of the centrifugal force and flows downwards along the inner wall, and the gas continues to flow upwards. Under the action of centrifugal force, liquid drops gathered on the outer side of the swirl vane can flow out along the second gap delta, the curved surface of the swirl vane is smooth and continuous, disturbance to natural gas is reduced, rising resistance is small, and the separation effect is good; in addition, the separated liquid flows along the edge of the cyclone blade and the inner surface of the second pipeline, namely, the second gap of the design can be adjusted according to the flow, namely, the second cyclone separators with different structures can be replaced according to the gas treatment capacity and the gas phase components, so that the production requirements can be met, the use is convenient, and the separation effect is good.
As a preferred embodiment, the second cyclone separators are a plurality of and are uniformly distributed in the tank body, and a fixing frame for mounting the second cyclone separators is arranged in the tank body. The second cyclone separators which are uniformly distributed in the tank body have the function of shunting, so that fluid entering the second cyclone separators is uniformly distributed, the cyclone area is increased, the distance of centrifugal movement of liquid drops is shortened, and efficient separation of small liquid drops is realized.
As a preferred embodiment, the second cyclone separator comprises an air inlet section and a cyclone section, the cyclone section is arranged at the top of the air inlet section, the fixing frame comprises an upper supporting plate and a lower supporting plate, an upper mounting hole matched with the cyclone section is formed in the upper supporting plate, and a lower mounting hole matched with the air inlet section is formed in the lower supporting plate. The setting of mount has made things convenient for second cyclone's fixed and installation, simultaneously, has also made things convenient for the reposition of redundant personnel of the natural gas of treating the separation in the jar body, makes it evenly get into second cyclone smoothly.
As a preferred embodiment, the liquid baffle is arranged inside an air inlet cylinder, the air inlet cylinder is horizontally arranged, the liquid baffle comprises a plurality of front baffles and a plurality of rear baffles, and the front baffles and the rear baffles are opposite and arranged at intervals; preceding baffle with the backplate is all towards keeping away from the slope of air inlet direction sets up, along keeping away from the direction of air inlet, the length of preceding baffle is and increases gradually the setting, the length of backplate also is and increases gradually the setting. The front baffle and the rear baffle are respectively fixed in the tank body from front to back, one end of the air inlet cylinder is directly connected with the air inlet, and the other end of the air inlet cylinder is a free end; the air flow entering the separation tank directly impacts the liquid baffle plate to block liquid drops; the air inlet cylinder and the liquid baffle fully ensure that all liquid drops are impacted from the front direction and the rear direction, and the liquid drops which slide down along the front baffle and the rear baffle continuously flow outwards along the air inlet cylinder and flow out from the free end of the air inlet cylinder, so that the liquid drops are separated from air and flow downwards; moreover, the liquid baffle does not hinder the ascending movement of the gas, and the gas continuously collides with the front baffle and the rear baffle, flows out from the free end of the gas inlet cylinder and smoothly enters the second cyclone separator.
As a preferred embodiment, the liquid baffle is disposed inside an air inlet pipe, the air inlet pipe is connected to the air inlet through a turning pipe, the turning pipe is horizontally disposed, the air inlet pipe is vertically disposed, the liquid baffle includes a plurality of first baffles and a plurality of second baffles, and the first baffles and the second baffles are opposite and spaced; first baffle with the second baffle is all towards keeping away from the slope of air inlet direction sets up, along keeping away from the direction of air inlet, the length of first baffle is and increases gradually the setting, the length of second baffle also is and increases gradually the setting. After entering the separation tank, the airflow flows in the bend pipe along the horizontal direction, then vertically downwards enters the air inlet pipe, continuously impacts the first baffle and the second baffle, so that liquid drops are blocked, the air continuously flows downwards and flows out from an outlet of the air inlet pipe, and then does ascending motion to enter the second cyclone separator; the air inlet pipe and the liquid baffle plate enable the air flow to move in a zigzag mode, so that the air flow is fully guaranteed to impact the first baffle plate and the second baffle plate to separate liquid drops, the air flow is guaranteed to flow in a circuitous mode, and the air flow is fully dispersed before entering the second cyclone separator; the separated liquid drops flow down from the outlet of the air inlet pipe along the tail ends of the first baffle and the second baffle under the action of gravity. The first baffle and the second baffle which are obliquely arranged further reduce the resistance of the gas in the flowing process, and meanwhile, liquid drops doped with the gas can be fully blocked, so that the gas-liquid separation effect is good. The length of the baffle plate which is far away from the air inlet in the liquid baffle plate is longer, and the baffle plate is lengthened gradually, so that liquid drops can be blocked step by step, namely the longer baffle plate can block the liquid drops which cannot be blocked by the baffle plate in front, and the gas-liquid separation efficiency is improved.
As a preferred embodiment, the liquid baffle is arranged inside an air inlet channel, the air inlet channel is horizontally arranged, the liquid baffle comprises a plurality of upper baffles and a plurality of lower baffles, and the upper baffles and the lower baffles are opposite and arranged at intervals; liquid outlets are formed in the lower baffle plates, liquid outlets in the Nth lower baffle plate are located on two sides of the lower baffle plate, liquid outlets in the (N + 1) th lower baffle plate are located in the middle of the lower baffle plate, and N is a natural number; the overhead gage with down the baffle is all towards keeping away from the slope of air inlet direction sets up, along keeping away from the direction of air inlet, the length of overhead gage is and increases gradually the setting, the length of baffle also is and increases gradually the setting down. Generally, the air inlet channel comprises an upper fixed plate, a lower fixed plate, a front fixed plate and a rear fixed plate, wherein the upper baffle plate is arranged on the upper fixed plate, the lower baffle plate is arranged on the lower fixed plate, liquid outlets are arranged on two sides of the lower baffle plate, namely, a gap, namely a liquid outlet, is reserved between the lower baffle plate and the front fixed plate and between the lower baffle plate and the rear fixed plate, and liquid after primary separation flows out; the gas flow which impacts the lower baffle plate also has part of gas flowing out of the liquid outlet; then, the gas-liquid separation is carried out again after the gas-liquid separation is carried out again; finally, the lower baffle plate is impacted again, and at the moment, the middle part of the lower baffle plate is provided with a liquid outlet for liquid to flow out and air flow to pass through. The liquid outlets arranged in a staggered mode are beneficial to smooth flowing of liquid, and meanwhile, the flowing direction of air flow is disturbed continuously, so that the air flow continuously collides the lower baffle and the upper baffle, and the efficiency of primary gas-liquid separation is improved.
As a preferred embodiment, the laval nozzle includes a first straight line segment, a tapered segment, a throat portion, a diverging segment and a third straight line segment connected in sequence from the second gas inlet end to the second gas outlet end, and the laval nozzle is symmetrically arranged with the throat portion as a center. In the Laval nozzle, a second gas inlet end is connected with a first straight line section at first, the first straight line section is connected with a reducing section, the reducing section is connected with a throat part, the throat part is connected with a diverging section, the diverging section is connected with a third straight line section, the third straight line section is connected with a second gas outlet end, the whole Laval nozzle (Laval nozzle) is a reducing-diverging nozzle with a thin middle and thick two ends, the junction of the reducing section and the diverging section of the reducing-diverging nozzle is the throat part of the nozzle, the cross section area of the pipeline is minimum, and the cross section of the Laval nozzle is generally circular.
As a preferred embodiment, the boundary line equation of the tapered section is:in the formula (I); h is1Is half the height of the first straight line segment, h2Half the throat height, l is the horizontal length of the tapered section. The converging section and the diverging section of the Laval nozzle are of symmetrical structures along the throat position, the flow field airflow acceleration uniformity is good, the boundary line equation of the converging section is high-order and can be guided, the curve is smooth, the generation of turbulence or disturbance in a pipeline can be reduced or avoided, and the energy loss is reduced; in addition, the Laval nozzles with different structures can be replaced according to the gas treatment capacity and the gas phase components, so that the Laval nozzles can meet the production requirements.
As a preferred embodiment, the first cyclonic fluid separator comprises a first conduit and a helical blade disposed within the first conduit; the equation for the helical blade is:
in the formula (I); ω is the angular velocity, v is the velocity along the axis, r is the inner diameter of the first pipe, and t is the movement time. The helical blade provided by the invention has smooth and continuous curved surface, and can reduce disturbance; the fluid forms a rotational flow under the action of the helical blade in the first cyclone separator, the liquid is gathered at the outer side of the helical blade through centrifugal force and moves forwards continuously along the outer side of the helical blade, so that the liquid phase in the fluid entering the Laval nozzle flows along the inner surface of the Laval nozzle and is gathered, and the separation efficiency is improved. In the first cyclonic separator, the edges of the helical blades are directly connected to the inner surface of the first conduit, thereby facilitating cyclonic flow. In addition, in the helical blade equation of the invention, r and v are variables and can be adjusted according to parameters such as flow and the like, namely, the first cyclone separators with different structures can be replaced according to the gas treatment capacity and the gas phase components, so that the production requirements can be met, and the helical blade equation is convenient to use.
Compared with the prior art, the invention has the beneficial effects that: according to the natural gas treatment device, natural gas to be treated sequentially passes through the first cyclone separator, the Laval nozzle and the separation tank, and sequentially passes through the liquid baffle and the second cyclone separator in the separation tank, so that gas-liquid separation in the natural gas is realized, the separated gas is discharged from the gas outlet, and the separated liquid is discharged from the liquid outlet. Firstly, forming a cyclone effect in the natural gas to be treated in the first cyclone separator, and throwing liquid onto the side wall and flowing along the side wall under the action of centrifugal force; then, the speed is increased, the pressure is reduced and the temperature is reduced through a Laval nozzle, so that the gaseous lubricating oil in the natural gas is cooled into liquid drops; after the liquid drops enter the separation tank, the liquid drops directly impact a liquid baffle inside the separation tank, and primary separation is carried out under the action of the liquid baffle; the liquid after the primary separation flows downwards, the gas after the primary separation flows upwards and passes through the second cyclone separator, the gas-liquid two-phase secondary separation is realized under the action of centrifugal force again, the separated gas continues to flow upwards and is discharged from the gas outlet, and the separated liquid flows downwards and is discharged from the liquid outlet, so that the effect of gas-liquid separation of natural gas is finally achieved. The gas-liquid separation device has the advantages of simple structure and scientific and reasonable design, is suitable for separation of high-liquid content liquid and separation under the condition of less liquid content, has high gas-liquid separation efficiency, does not generate the phenomena of liquid phase crushing and entrainment, has good separation effect, and is particularly suitable for gas-liquid separation of natural gas after long-distance pipeline transportation.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic cross-sectional structural view of a natural gas-liquid separation device according to a first embodiment of the present invention;
FIG. 2 is an enlarged view of the structure of the separation tank of FIG. 1;
FIG. 3 is an enlarged view of the first cyclonic separator of FIG. 1;
FIG. 4 is a schematic perspective cross-sectional view of FIG. 3;
FIG. 5 is an enlarged view of the structure of the Laval nozzle of FIG. 1;
FIG. 6 is a perspective view of the liquid baffle of FIG. 1;
FIG. 7 is a schematic top view of the structure of FIG. 6;
FIG. 8 is an enlarged view of the cyclone separator of FIG. 1;
FIG. 9 is a schematic perspective view of FIG. 8;
fig. 10 is a schematic cross-sectional structural view of a natural gas-liquid separation apparatus according to a second embodiment of the present invention;
FIG. 11 is a schematic perspective view of the liquid baffle of FIG. 10;
fig. 12 is a schematic sectional structural view of a natural gas-liquid separation apparatus according to a third embodiment of the present invention;
FIG. 13 is a schematic perspective view of the liquid baffle of FIG. 12;
in the figure: 1-a first cyclonic separator; 2-a laval nozzle; 3-a separation tank; 4-a liquid barrier; 5-a second cyclone separator; 6-an air inlet cylinder; 7-an air inlet pipe; 8-a breakover tube; 9-an air inlet channel; 11-a first air intake end; 12-a helical blade; 13-a first fixed shaft; 14-a first outlet end; 21-a second air inlet end; 22-a first straight line segment; 23-a tapered section; 24-throat; 25-divergent section; 26-a third straight line segment; 27-a second outlet end; 31-an air inlet; 32-air outlet; 33-a first liquid outlet; 34-a second liquid outlet; 41-front baffle; 42-a tailgate; 43-a first baffle; 44-a second baffle; 45-upper baffle plate; 46-a lower baffle; 47-a liquid outlet; 51-an air inlet section; 52-a cyclone section; 53-swirl vanes; 54-a second gap; 55-a second fixed shaft; 61-an upper support plate; 62-a lower support plate; 63-groove.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example one
Referring to the attached drawings 1, 2, 3, 4, 5, 6, 7, 8 and 9, the natural gas-liquid separation device comprises a first cyclone separator 1, a laval nozzle 2 and a separation tank 3, wherein the first cyclone separator 1 is connected with the laval nozzle 2, and the other end of the laval nozzle 2 is connected with the separation tank 3; the first cyclone separator 1 comprises a first gas inlet end 11 and a first gas outlet end 14, wherein the first gas inlet end 11 is used for feeding natural gas to be treated; the laval nozzle 2 comprises a second gas inlet end 21 and a second gas outlet end 27, the second gas inlet end 21 is connected with the first gas outlet end 14, and therefore the connection of the first cyclone separator 1 and the laval nozzle 2 is achieved; the separating tank 3 comprises a tank body, wherein a gas inlet 31, a gas outlet 32 and a liquid outlet are formed in the tank body, the gas inlet 31 is connected with a second gas outlet end 27, so that the Laval nozzle 2 is connected with the separating tank 3, a liquid baffle 4 is arranged in the tank body on one side of the gas inlet 31, and a second cyclone separator 5 is arranged in the tank body above the liquid baffle 4. The gas inlet 31 is positioned at the middle lower part of the tank body, the liquid baffle 4 is directly connected with the gas inlet 31, the second cyclone separator 5 is positioned below the gas outlet 32, the two liquid outlets are a first liquid outlet 33 and a second liquid outlet 34, the second liquid outlet 34 is positioned at the bottom of the tank body, namely below the gas inlet 31, and the first liquid outlet 33 is positioned at the bottom of the second cyclone separator 5. The natural gas to be treated sequentially passes through the first cyclone separator 1, the laval nozzle 2 and the separation tank 3 and sequentially passes through the liquid baffle 4 and the second cyclone separator 5 in the separation tank 3, so that gas-liquid separation in the natural gas is realized, the separated gas is discharged from the gas outlet 32, and the separated liquid is discharged from the liquid outlets, namely the first liquid outlet 33 and the second liquid outlet 34.
Referring to fig. 1, 3 and 4, in general, the first cyclone separator 1 comprises a first pipe and a helical blade 12 arranged in the first pipe, the helical blade 12 is arranged on a first fixed shaft 13 in the first pipe, the helical blade 12 provides centrifugal force, liquid in natural gas is thrown to the outer side or edge of the helical blade 12 under the action of the centrifugal force and is gathered to form liquid drops, and the liquid drops flow along the inner wall of the first pipe. The equation for the helical blade 12 is preferably:
in the formula (I); ω is the angular velocity, v is the velocity along the axis, r is the inner diameter of the first pipe, and t is the movement time. The helical blade 12 with the arrangement has smooth and continuous curved surface, and can reduce disturbance; the fluid forms a rotational flow in the first cyclone separator 1, and liquid is gathered outside the helical blade 12 through centrifugal force, so that liquid phase in the fluid entering the laval nozzle 2 flows along the inner surface of the first pipeline, and the liquid phase is gathered, thereby improving the separation efficiency. In addition, in the equation of the helical blade 12, r and v are variables, and can be adjusted according to parameters such as flow and the like, namely the first cyclone separator 1 with different structures can be replaced according to the gas treatment capacity and different gas-phase components, so that the production requirements can be met, and the use is convenient.
Referring to fig. 1 and 5, fluid enters a laval nozzle 2 from a first cyclone separator 1 at a certain speed, and is subjected to speed increasing, temperature reducing and pressure reducing in the laval nozzle 2, and gaseous lubricating oil is condensed into liquid. Generally, the laval nozzle 2 includes a first straight line section 22, a tapered section 23, a throat section 24, a diverging section 25 and a third straight line section 26 connected in sequence from the second gas inlet end 21 to the second gas outlet end 27, and the laval nozzle 2 is symmetrically disposed with the throat section 24 as a center. In the Laval nozzle 2, the second gas inlet 21 is first connected to the first straight line segment 22, the first straight line segment 22 is then connected to the tapered segment 23, the tapered segment 23 is connected to the throat 24, the throat 24 is then connected to the diverging segment 25, the diverging segment 25 is connected to the third straight line segment 26, the third straight line segment 26 is connected to the second gas outlet 27, the whole Laval nozzle 2(Laval nozzle) is a tapered-diverging nozzle with a thin middle and thick two ends, the junction of the tapered segment 23 and the diverging segment 25 of the tapered-diverging nozzle is the throat 24 of the nozzle, the cross-sectional area of the pipe is the minimum, and the cross-section of the Laval nozzle 2 is generally circular. The borderline equation for the tapered section 23 is:
in the formula (I); h is1Is half the height, h, of the first straight line segment 222Half the height of the throat 24, l is the horizontal length of the tapered section 23. The convergent section 23 and the divergent section 25 of the Laval nozzle 2 are of a symmetrical structure along the position of the throat part 24, the Laval nozzle 2 is composed of a closed curved surface, the cross-sectional area is firstly reduced and then enlarged, the throat part 24 is formed at the minimum position, and the convergent section 23 and the divergent section 25 of the Laval nozzle 2 are respectively arranged on the left side and the right side of the throat part 24. The flow field airflow acceleration uniformity of the Laval nozzle 2 is good, the boundary line equation of the tapered section 23 is high-order and can be guided, the curve is smooth, the generation of turbulence or disturbance in the pipeline can be reduced or avoided, and the energy loss is reduced; in addition, the Laval nozzle 2 with different structures can be replaced according to the gas treatment capacity and the gas phase components, so that the production requirements can be met.
Referring to fig. 1, 6 and 7, the lubricating oil liquid entrained in the natural gas directly impacts the liquid baffle 4 to remove the liquid droplets with larger volume by the action of inertia force. The liquid baffle 4 is arranged inside an air inlet cylinder 6, the air inlet cylinder 6 is horizontally arranged, the liquid baffle 4 comprises a plurality of front baffles 41 and a plurality of rear baffles 42, the front baffles 41 and the rear baffles 42 are opposite and arranged at intervals, and the front baffles 41 and the rear baffles 42 of the liquid baffle 4 are arranged in the front-back direction; preceding baffle 41 and backplate 42 all set up towards keeping away from air inlet 31 direction slope, along the direction of keeping away from air inlet 31, and the length of preceding baffle 41 is the gradual increase setting, and the length of backplate 42 also is the gradual increase setting. The front baffle plate 41 and the rear baffle plate 42 are respectively fixed in the tank body from the front to the rear direction, and the air inlet cylinder 6 can be cylindrical, cuboid or other shapes; one end of the air inlet cylinder 6 is directly connected with the air inlet 31, and the other end is a free end; the air flow entering the separation tank 3 directly impacts the liquid baffle 4, so that liquid drops are blocked; the air inlet cylinder 6 and the liquid baffle 4 are arranged in such a way that all liquid drops are fully ensured to be impacted from the front direction to the rear direction, and the liquid drops sliding down along the front baffle 41 and the rear baffle 42 continuously flow outwards along the air inlet cylinder 6 and flow out from the free end of the air inlet cylinder 6, so that the liquid drops are separated from air and flow downwards; moreover, the liquid baffle 4 does not hinder the gas from rising, and the gas, after continuously striking the front baffle 41 and the rear baffle 42, also flows out of the free end of the inlet pipe 6 and smoothly enters the second cyclone 5. The liquid baffle 4 ensures that all liquid drops are impacted sufficiently, so that all liquid drops are blocked, separated from the gas and flow downwards, and finally discharged from a second liquid outlet 34 at the bottom of the tank body; moreover, the liquid baffle 4 does not interfere with the upward movement of the gas, and the gas can smoothly enter the second cyclone 5. The inclined front baffle plate 41 and the inclined rear baffle plate 42 further reduce the resistance of the gas in the flowing process, and can fully block liquid drops doped with the gas, so that the gas-liquid separation effect is good. The length of the front baffle 41 is gradually increased and the length of the rear baffle 42 is gradually increased in a direction away from the air inlet 31. The longer the baffle length of the liquid baffle 4 away from the air inlet 31 is, the longer the baffle is, the liquid droplets can be blocked step by step, namely, the longer baffle can block the liquid droplets which cannot be blocked by the front baffle, and the gas-liquid separation efficiency is improved.
Referring to fig. 1, 8 and 9, after passing through the liquid baffle 4, the fluid enters the second cyclone separator 5, the fluid forms a cyclone again in the second cyclone separator 5, small liquid drops are thrown to the side wall due to the action of centrifugal force, and fine liquid is separated out through the centrifugal force, so that the separation efficiency is improved. The second cyclone separator 5 includes a second duct and a cyclone blade 53 disposed in the second duct, a second gap 54 is provided between an edge of the cyclone blade 53 and an inner surface of the second duct, and the cyclone blade 53 is mounted on a second fixed shaft 55 in the second duct; the equation for swirl vanes 53 is:
in the formula: r is the inner diameter of the second conduit, δ is the length of the second gap 54, ω is the angular velocity, v is the velocity in the axial direction, and t is the time of movement. After the natural gas to be processed enters the second cyclone separator 5 in the separation tank 3, the natural gas performs spiral rotary motion under the action of the cyclone blades 53, gas-liquid separation is realized in the ascending process of the natural gas under the action of centrifugal force, liquid is thrown onto the inner wall of the second pipeline under the action of the centrifugal force and flows downwards along the inner wall, and the gas continues to flow upwards. Under the action of centrifugal force, liquid drops gathered at the outer side of the cyclone blade 53 can flow out along the second gap 54 delta, the curved surface of the cyclone blade 53 is smooth and continuous, disturbance to natural gas is reduced, rising resistance is small, and the separation effect is good; in addition, the separated liquid flows along the second gap 54 between the edge of the cyclone blade 53 and the inner surface of the second pipeline, and the second gap 54 with the design can be adjusted according to the flow rate, namely, the second cyclone separator 5 with different structures can be replaced according to the gas treatment capacity and the gas phase components, so that the production requirements can be met, the use is convenient, and the separation effect is good. Usually, the second cyclone separators 5 are a plurality of and are uniformly distributed in the tank body, and the tank body is internally provided with a fixing frame for mounting the second cyclone separators 5. The second cyclone separators 5 which are uniformly distributed in the tank body have the function of shunting, so that fluid entering the second cyclone separators 5 is uniformly distributed, the cyclone area is increased, the distance of centrifugal movement of liquid drops is shortened, and efficient separation of small liquid drops is realized. The second cyclone separator 5 comprises an air inlet section 51 and a cyclone section 52, the cyclone section 52 is arranged at the top of the air inlet section 51, the fixing frame comprises an upper supporting plate 61 and a lower supporting plate 62, the upper supporting plate 61 is provided with an upper mounting hole matched with the cyclone section 52, and the lower supporting plate 62 is provided with a lower mounting hole matched with the air inlet section 51. The setting of mount has made things convenient for second cyclone 5's fixed and installation, simultaneously, has also made things convenient for the reposition of redundant personnel of the natural gas of treating the separation in the jar body, makes it evenly get into second cyclone 5 smoothly. Finally, the small liquid drops separated by the second cyclone separator 5 flow down through the second gap 54 and are discharged out of the tank body from the first liquid outlet 33 at the bottom of the second cyclone separator 5, and the dried gas is discharged from the gas outlet 32. In general, the circumferential direction of the upper support plate 61 is provided with grooves 63 which are circumferentially and symmetrically distributed, and the number of the grooves 63 can be 6 or other numbers; due to the part of the small droplets that the drying gas may carry along during the rising, these droplets will sink under gravity settling after rising into the head space of the separator tank 3; the groove 63 is arranged to enable the settled droplets to flow downwards along the inner wall of the separation tank 3, enter between the upper support plate 61 and the lower support plate 62 through the upper support plate 61, and finally be discharged out of the separation tank 3 through the first liquid outlet 33 beside the lower support plate 62, so that the circulation is smooth, and the occurrence of fluid dead angles is avoided.
Example two
Referring to fig. 10 and 11, different from the first embodiment, in the present embodiment, the liquid baffle 4 is vertically installed inside the separation tank 3, specifically, the liquid baffle 4 is installed inside an air inlet pipe 7, the air inlet pipe 7 is connected to the air inlet 31 through a turning pipe 8, the turning pipe 8 is horizontally installed, the air inlet pipe 7 is vertically installed, the liquid baffle 4 includes a plurality of first baffles 43 and a plurality of second baffles 44, and the first baffles 43 and the second baffles 44 are opposite and spaced; first baffle 43 and second baffle 44 all set up towards keeping away from the slope of air inlet 31 direction, along the direction of keeping away from air inlet 31, and the length of first baffle 43 is the gradual increase setting, and the length of second baffle 44 also is the gradual increase setting. The first shutter 43 and the second shutter 44 may be installed in the left-right direction or the front-back direction; the intake pipe 7 may be cylindrical, rectangular parallelepiped, or other shapes. After entering the separation tank 3, the airflow flows in the bend pipe 8 along the horizontal direction, then vertically and downwardly enters the air inlet pipe 7, continuously collides with the first baffle 43 and the second baffle 44, so that liquid drops are blocked, the air continuously flows downwardly, flows out from an outlet of the air inlet pipe 7, then does ascending movement, and enters the second cyclone separator 5; the air inlet pipe 7 and the liquid baffle 4 are arranged in such a way that the air flow moves in a zigzag way, so that the air flow is fully ensured to impact the first baffle 43 and the second baffle 44 to separate liquid drops, the air flow is ensured to flow in a circuitous way, and the air flow is fully dispersed before entering the second cyclone separator 5; the separated droplets flow down from the outlet of the inlet pipe 7 along the ends of the first baffle 43 and the second baffle 44 by gravity. The first baffle 43 and the second baffle 44 which are arranged in an inclined manner further reduce the resistance of the gas in the flowing process, and simultaneously can fully block liquid drops doped with the gas, so that the gas-liquid separation effect is good. The longer the baffle length of the liquid baffle 4 away from the air inlet 31 is, the longer the baffle is, the liquid droplets can be blocked step by step, namely, the longer baffle can block the liquid droplets which cannot be blocked by the front baffle, and the gas-liquid separation efficiency is improved.
EXAMPLE III
Referring to fig. 12 and 13, the same as the first embodiment, the liquid baffle 4 in this embodiment is also horizontally installed inside the separation tank 3, and different from the first embodiment, the upper baffle 45 and the lower baffle 46 of the liquid baffle 4 in this embodiment are installed in the up-down direction, specifically, the liquid baffle 4 is installed inside an air inlet channel 9, the air inlet channel 9 is horizontally installed, the liquid baffle 4 includes a plurality of upper baffles 45 and a plurality of lower baffles 46, and the upper baffles 45 and the lower baffles 46 are opposite and spaced; liquid outlets 47 are formed in the lower baffle plates 46, the liquid outlets 47 in the Nth lower baffle plate 46 are located on two sides of the lower baffle plate, the liquid outlets 47 in the (N + 1) th lower baffle plate 46 are located in the middle of the lower baffle plate, and N is a natural number; the top board 45 and the lower board 46 are all towards keeping away from the slope setting of air inlet 31 direction, along the direction of keeping away from air inlet 31, the length of top board 45 is and increases gradually the setting, and the length of lower board 46 also is and increases gradually the setting. The air inlet channel 9 can be cylindrical, cuboid or other shapes; in general, the air intake channel 9 includes an upper fixing plate, a lower fixing plate, a front fixing plate and a rear fixing plate, the upper baffle 45 is disposed on the upper fixing plate, the lower baffle 46 is disposed on the lower fixing plate, two sides of the lower baffle 46 are provided with liquid outlets 47, i.e., a gap, i.e., the liquid outlet 47, is left between the lower baffle 46 and the front fixing plate and between the lower baffle 46 and the rear fixing plate, for the liquid after the preliminary separation to flow out; the gas flow impinging on the lower baffle 46, and also a portion of the gas, exits the liquid outlet 47; then, the gas and the liquid are again separated by impacting the upper baffle 45; and finally strikes the lower baffle 46 again, at which time the middle of the lower baffle 46 is provided with a liquid outlet 47 for the liquid to flow out and the air to pass through. The staggered liquid outlets 47 are beneficial to smooth outflow of liquid, and simultaneously, the flowing direction of the airflow is also disturbed continuously, so that the airflow continuously impacts the lower baffle 46 and the upper baffle 45, and the efficiency of primary gas-liquid separation is improved.
Compared with the prior art, the invention has the beneficial effects that: in the invention, natural gas to be treated sequentially passes through the first cyclone separator 1, the Laval nozzle 2 and the separation tank 3 and sequentially passes through the liquid baffle 4 and the second cyclone separator 5 in the separation tank 3, so that gas-liquid separation in the natural gas is realized, the separated gas is discharged from the gas outlet 32, and the separated liquid is discharged from the liquid outlets, namely the first liquid outlet 33 and the second liquid outlet 34. Firstly, forming a cyclone effect in the natural gas to be treated in the first cyclone separator 1, and throwing liquid onto the side wall and flowing along the side wall under the action of centrifugal force; then, the speed is increased, the pressure is reduced and the temperature is reduced through the Laval nozzle 2, so that the gaseous lubricating oil in the natural gas is cooled into liquid drops; after the liquid drops enter the separation tank 3, the liquid drops directly impact a liquid baffle 4 in the separation tank 3, and primary separation is carried out under the action of the liquid baffle 4; the liquid after the primary separation flows downwards, the gas after the primary separation flows upwards and passes through the second cyclone separator 5, the gas-liquid two-phase secondary separation is realized under the action of centrifugal force again, the separated gas continues to flow upwards and is discharged from the gas outlet 32, the separated liquid flows downwards and is discharged from the liquid outlets, namely the first liquid outlet 33 and the second liquid outlet 34, and finally the effect of gas-liquid separation of natural gas is achieved. The gas-liquid separation device has the advantages of simple structure and scientific and reasonable design, is suitable for separation of high-liquid content liquid and separation under the condition of less liquid content, has high gas-liquid separation efficiency, does not generate the phenomena of liquid phase crushing and entrainment, has good separation effect, and is particularly suitable for gas-liquid separation of natural gas after long-distance pipeline transportation.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. A natural gas-liquid separation device, comprising:
the first cyclone separator comprises a first air inlet end and a first air outlet end;
the Laval nozzle comprises a second air inlet end and a second air outlet end, and the second air inlet end is connected with the first air outlet end;
the separating tank comprises a tank body, wherein the tank body is provided with an air inlet, an air outlet and a liquid outlet, the air inlet is connected with the air outlet end of the second tank, one side of the air inlet is provided with a liquid baffle plate inside the tank body, and a second cyclone separator is arranged above the liquid baffle plate inside the tank body.
2. The natural gas-liquid separation device according to claim 1, characterized in that:
the second cyclone separator comprises a second pipeline and a cyclone blade arranged in the second pipeline, and a second gap is formed between the edge of the cyclone blade and the inner surface of the second pipeline;
the equation of the swirl vane is as follows:
in the formula: r is the inner diameter of the second conduit, δ is the length of the second gap, ω is the angular velocity, v is the velocity in the axial direction, and t is the time of movement.
3. The natural gas-liquid separation device according to claim 1 or 2, characterized in that:
the second cyclone separator is a plurality of and be in the internal evenly distributed that is of jar, jar internal being equipped with is used for installing the mount of second cyclone separator.
4. The natural gas-liquid separation device according to claim 3, characterized in that:
the second cyclone separator comprises an air inlet section and a cyclone section, the top of the air inlet section is provided with the cyclone section, the fixing frame comprises an upper supporting plate and a lower supporting plate, the upper supporting plate is provided with an upper mounting hole matched with the cyclone section, and the lower supporting plate is provided with a lower mounting hole matched with the air inlet section.
5. The natural gas-liquid separation device according to claim 1, characterized in that:
the liquid baffle is arranged in an air inlet cylinder, the air inlet cylinder is horizontally arranged, the liquid baffle comprises a plurality of front baffles and a plurality of rear baffles, and the front baffles and the rear baffles are opposite and arranged at intervals;
preceding baffle with the backplate is all towards keeping away from the slope of air inlet direction sets up, along keeping away from the direction of air inlet, the length of preceding baffle is and increases gradually the setting, the length of backplate also is and increases gradually the setting.
6. The natural gas-liquid separation device according to claim 1, characterized in that:
the liquid baffle is arranged in an air inlet pipe, the air inlet pipe is connected with the air inlet through a turning pipe, the turning pipe is horizontally arranged, the air inlet pipe is vertically arranged, the liquid baffle comprises a plurality of first baffles and a plurality of second baffles, and the first baffles and the second baffles are opposite and arranged at intervals;
first baffle with the second baffle is all towards keeping away from the slope of air inlet direction sets up, along keeping away from the direction of air inlet, the length of first baffle is and increases gradually the setting, the length of second baffle also is and increases gradually the setting.
7. The natural gas-liquid separation device according to claim 1, characterized in that:
the liquid baffle is arranged in an air inlet channel, the air inlet channel is horizontally arranged, the liquid baffle comprises a plurality of upper baffles and a plurality of lower baffles, and the upper baffles and the lower baffles are opposite and arranged at intervals;
liquid outlets are formed in the lower baffle plates, liquid outlets in the Nth lower baffle plate are located on two sides of the lower baffle plate, liquid outlets in the (N + 1) th lower baffle plate are located in the middle of the lower baffle plate, and N is a natural number;
the overhead gage with down the baffle is all towards keeping away from the slope of air inlet direction sets up, along keeping away from the direction of air inlet, the length of overhead gage is and increases gradually the setting, the length of baffle also is and increases gradually the setting down.
8. The natural gas-liquid separation device according to claim 1, characterized in that:
the laval nozzle comprises a first straight line section, a reducing section, a throat part, a gradually expanding section and a third straight line section which are sequentially connected from a second air inlet end to a second air outlet end, and the laval nozzle is symmetrically arranged by taking the throat part as a center.
9. The natural gas-liquid separation device according to claim 8, characterized in that:
the boundary equation of the reducing section is as follows:
in the formula (I); h is1Is half the height of the first straight line segment, h2Half the throat height, l is the horizontal length of the tapered section.
10. The natural gas-liquid separation device according to claim 1, characterized in that:
the first cyclonic separator includes a first conduit and a helical blade disposed within the first conduit;
the equation for the helical blade is:
in the formula (I); ω is the angular velocity, v is the velocity along the axis, r is the inner diameter of the first pipe, and t is the movement time.
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| CN114470977A (en) * | 2022-04-18 | 2022-05-13 | 天津大学 | Gas-water separator applied to hydrogen fuel cell |
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| CN117965217A (en) * | 2024-04-02 | 2024-05-03 | 内蒙古万瑞天然气有限责任公司 | Separation type natural gas low-temperature separator |
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| CN110835565B (en) | 2021-05-11 |
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