JPH0538408A - Gas-liquid separation apparatus - Google Patents

Abstract

PURPOSE:To prevent liquid drops in gas-liquid two-phase flow which flows in a tangent line direction from rising while following the gas flow in the center part and coming in to the inside of a pipe from the upper open part of an inner cylinder (gas discharging pipe) and being discharged to the outside of a vertical-type centrifugal gas-liquid separation apparatus. CONSTITUTION:A flowing-in nozzle 12 is extended to the inside of a cylinder body 11 and its bottom face is made declining backward and at the same time the exit width B12a of the flowing-in nozzle 12 is made narrower than the width B16 of a circular cross section whirling flow route 16 formed between the cylinder body 11 and an inner cylinder 14.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas-liquid two-phase flow gas-liquid separator in various plants, and more particularly to a gas-liquid separator suitable for improving the purity of geothermal power generation steam.

[0002]

2. Description of the Related Art FIG. 10 is a horizontal cross-sectional view showing an example of a conventional gas-liquid separator (X-X section in FIG. 11), and FIG.
0 is a vertical sectional side view of XI-XI, and FIG. 12 is a vertical sectional front view of XII-XII in FIG.

In these figures, (01) is a vertical cylindrical cylinder, (02) is an inflow nozzle having a circular cross section tangentially attached to the side surface of the cylinder (01), and (03) is the same. An inlet pipe connected to the inflow nozzle. Reference numeral (04) is a gas discharge pipe, which is coaxially arranged in the cylindrical body (01) and has an upper end opened to an upper part in the cylindrical body (01). (0
Reference numeral 5) is a liquid discharge pipe that opens at the bottom of the cylindrical body (01). The cross section of the inflow nozzle (02) is a circular cross section of the same size obtained by directly extending the inlet pipe (03) (diameter D ₀₃ ). The nozzle width B ₀₂ (= nozzle diameter D ₀₂ ) is almost equal to the width B ₀₆ of the swirling flow passage (06) having an annular cross section formed between the cylindrical body (01) and the gas discharge pipe (04). Is.

In such a gas-liquid separator, when a gas-liquid two-phase flow flows from the inlet pipe (03) through the inflow nozzle (02) into the annular swirl flow path (06) of the cylindrical body (01), In the swirl flow path (06), the droplets collide with and adhere to the inner peripheral wall of the cylindrical body (01) due to inertial force and centrifugal force, and then flow down by the action of gravity along the wall surface and collect at the bottom. This is discharged out of the system through the liquid discharge pipe (05). On the other hand, the gas swirls and rises in the annular swirl flow path (06), and the gas exhaust pipe (0
4) It is introduced inside and discharged outside the system. The rising speed of the gas flow in the annular swirling flow path (06) has a remarkable characteristic that the central part is fast and the peripheral part is slow due to the gas discharge pipe (04) installed in the central part of the tubular body (01). ..

[0005]

The flow ejected from the inflow nozzle (02) of the gas-liquid separation device into the inside of the cylinder (01) becomes a free jet according to the cross-sectional shape of the nozzle, and the inside of the cylinder is solved. After jetting out, the flow spreads and slows down. The divergence angle of the jet flow is such that the one-sided divergence angle α ₀ is about 12 degrees in the jet flow from the circular nozzle (02) as illustrated in FIGS. 10 to 12, and the jet flow from the rectangular nozzle (two-dimensional jet flow). Then, the one-sided spread angle is about 16 degrees.

When a gas-liquid two-phase flow flows into the annular swirl flow path (06) as a fluid flowing in from the inflow nozzle (02) having a circular cross section, the flow outside the inflow nozzle (02) (see FIG. 10).
W ₀₁₁ ) therein smoothly flows into the annular swirl flow path (06) along the inner peripheral wall of the cylindrical body (01). Further, the liquid droplets in the flow in the central portion (W _{012 in} FIG. 10) also travel straight in the annular swirl flow path (06) and collide with the inner peripheral wall of the cylindrical body (01),
Most of them adhere to the wall surface and are separated. Then, after a very small part of the droplet collides with the peripheral wall of the cylinder, it re-scatters in the annular swirl flow path (06) (for example, in the direction of W _{022 in} the figure). However, when the droplet in the flow inside the nozzle jets into the annular swirl flow path (06), it goes straight in the direction of W ₀₁₃ through the central portion of the tubular body where the gas rising velocity is fast, or spreads further and becomes a tubular tube. _Scatter toward the center of the body (in the W ₀₁₄ direction). Then, it collides with the inner peripheral wall of the cylindrical body (01) or the outer peripheral wall of the gas discharge pipe (04), and some droplets adhere to these wall surfaces, but the remaining droplets collide again with the annular swirling flow path (06). Re-scatter inside.

As described above, the droplets in the jet flow inside the nozzle, after being jetted, pass through the central portion of the cylinder having a high gas rising speed, or spread and scatter toward the central portion of the cylinder. Even if it collides with the inner wall of the cylinder or the outer wall of the gas discharge pipe, the wall surface collision angle β ₀ is relatively large, so a considerable amount of droplets do not adhere to these wall surfaces, and a large number of small droplets after strong wall collision. And then scatter again. (For example, W ₀₁₃ and W in FIGS.
_Scatter in the directions of ₀₁₄ , W ₀₁₈ , and W ₀₂₃ , W ₀₂₄ , W ₀₂₈
Re-scatter in the direction of. ) These numerous scattered and re-scattered droplets with a minute diameter float in the annular swirl flow path (06),
It is carried by the air flow rising toward the upper end opening of the gas discharge pipe (04) and goes out of the apparatus. Therefore, the gas-liquid separation efficiency is significantly reduced.

[0008]

In order to solve the above-mentioned conventional problems, the present invention provides a vertical cylindrical tube body, an inflow nozzle tangentially attached to the side surface of the tube body, and the tube. In a gas-liquid separation device, which is coaxially arranged in the body and has a gas discharge pipe having an upper end opened to an upper part in the cylinder body, and a liquid discharge pipe opened to a lower part of the cylinder body, wherein the inflow nozzle is the cylinder body. The in-cylinder extension is inclined so that the cross-sectional area does not decrease toward the downstream side and the bottom surface decreases toward the downstream side, and its width is constant or tapered along the flow. The present invention proposes a gas-liquid separation device characterized in that the width at the nozzle outlet is narrower than the width of an annular swirl flow path formed between the cylindrical body and the gas discharge pipe.

[0009]

By installing the inflow nozzle extended in the cylinder as described above, the gas-liquid two-phase flow flowing into the annular swirl flow path is directed to the cylinder peripheral wall side and the cylinder bottom, and the gas discharge pipe. And the swirling flow in the annular swirling flow passage smoothly flows without being disturbed by the inflowing jet flow. Further, since the angle at which the droplets collide with the peripheral wall is kept small, almost all the droplets collide and adhere to the peripheral wall of the cylindrical body, and re-scattering after the collision is almost prevented. and again,
The drop is allowed to flow to the bottom. In this way, the gas-liquid separation efficiency of the gas-liquid separator is significantly improved.

[0010]

First Embodiment FIG. 1 shows a first embodiment of the present invention.
A horizontal cross-sectional view (II cross section of FIG. 2) showing a case where a rectangular cross-section nozzle is provided, FIG. 2 is a II-II vertical side view of FIG. 1, and FIG. 3 is a III-III vertical front view of FIG. is there.

In these figures, (11) is a vertical cylindrical separator main body (cylindrical body), (12) is an inflow nozzle tangentially attached to the side surface of the cylindrical body (11), and (13). Is an inlet pipe connected to the inflow nozzle. Reference numeral (14) is a gas discharge pipe, which is coaxially arranged in the cylindrical body (11) and has an upper end opened to an upper part in the cylindrical body (11).
Reference numeral (15) is a liquid discharge pipe that opens at the bottom of the cylindrical body (11).

The inflow nozzle (12) of this embodiment comprises a connecting nozzle (12a) and a rectangular nozzle (12b). The connecting nozzle (12a) is a deformed joint that connects the inlet pipe (13) having a circular cross section and the rectangular nozzle (12b) having a rectangular cross section. The rectangular nozzle (12b) has a cylindrical body (1
It extends to the inside of 1) and forms an inlet for the gas-liquid two-phase flow to the gas-liquid separator.

The connecting nozzle (12a) has an outlet width B
_The inner wall surface is inclined outward so that _12a is about half the width B ₁₆ of the annular swirl flow path (16) formed between the tubular body (11) and the gas discharge pipe (14). Further, the bottom surface is inclined at an angle θ _1a so as to decrease toward the downstream side, and the outlet height is from the inlet height (inlet pipe diameter) D ₁₃ to H _1a.
Until the outlet cross-sectional area of the connecting nozzle (12a) becomes smaller than the inlet cross-sectional area (cross-sectional area of the inlet pipe (13)). The bottom surface of the rectangular nozzle (12b) is also inclined at an angle θ _1b (= θ _1a ) so that it becomes lower toward the downstream like the connection nozzle (12a), and its outlet height is the inlet height H _1a. To H _1b . The width B _12b of the rectangular nozzle (12b) is constant in the flow direction (that is, the same as the outlet width B _12a of the connecting nozzle (12a)). Therefore, the cross-sectional area of the rectangular nozzle (12b) is enlarged downstream.

In such a gas-liquid separation device, the tubular body (11) is passed from the inlet pipe (13) through the inflow nozzle (12), that is, the connecting nozzle (12a) and the rectangular nozzle (12b).
The gas-liquid two-phase flow flowing into the annular swirl flow path (16) in the inside has a flow direction toward the outer peripheral wall and the lower part of the cylindrical body and collides with the gas outflow pipe (14) at the center of the cylindrical body or close thereto. There is no flow. Further, the swirling flow in the annular swirling flow path (16) is rectified by the inward-cylinder extending duct wall of the rectangular nozzle (12b) provided extending in the cylindrical body, and a smooth swirling flow without turbulence is maintained. Further, since the angle at which the desired swirling flow and the jet flow collide with the inner peripheral wall of the cylindrical body (11) becomes small, re-scattering of water drops after the jet flow collides with the peripheral wall is almost eliminated. In this way, in the conventional gas-liquid separation device, almost no floating droplets, which are scattered or re-scattered in the annular swirl flow path, floated up by the ascending air current, and are conveyed and discharged from the gas outflow pipe, are almost eliminated. Since all the droplets collide with and adhere to the peripheral wall of the cylinder, the gas-liquid separation efficiency is significantly improved. In this embodiment, the outlet width B _12b of the rectangular nozzle (12b) is also used.
_Is equal to the outlet width B _12a of the connection nozzle (12a), and the bottom surface inclination angle θ _1b of the rectangular nozzle (12b) is maintained at the same angle as the bottom surface inclination angle θ _1a of the connection nozzle (12a),
Connect the outlet area of the rectangular nozzle (12b) to the connecting nozzle (12
larger than the exit area of (a) (and therefore the inlet pipe (1
By making it larger than the cross-sectional area of 3), the static pressure loss of the inflow nozzle (12) can be reduced. That is, in this embodiment, the dual effects of improving the separation efficiency and recovering the static pressure loss are exhibited.

In FIGS. 1 and 2, W ₁₁₂ ,
W ₁₁₃ , W ₁₁₅ , and W ₁₁₆ are the main flow directions of the liquid droplets in the two-phase jet flowing into the cylindrical body (11) from the illustrated positions of the inflow nozzle (12), and W ₁₁₄ is the spread of the liquid droplets. The flow directions, W ₁₂₂ to W _126, represent the main rebounding and scattering directions of the liquid droplets when it is assumed that the liquid droplets that have collided with the peripheral wall of the cylinder re-scatter. W ₁₁₀ and W ₁₂₀ are the flow directions of the spreading liquid droplets in the two-phase flow jet when the inflow nozzle is not extended into the cylinder, and the main components of the liquid droplets re-scattered when they collide with the peripheral wall of the cylinder. The bounce direction, which is shown for comparison with the flow direction W ₁₁₄ and the re-scattering direction W ₁₂₄ in the above embodiment, respectively.

As described above, in this embodiment, since the bottom surface of the inflow nozzle (12) is inclined so as to become lower toward the downstream side, it flows into the cylindrical body (11) and collides with the peripheral wall of the cylindrical body. The gas-liquid two-phase flow is suppressed from rising along the wall surface, and in particular it is effective in reducing the rising height of the scattered mist, and the entrainment and outflow of liquid particles due to the rising gas flow is reduced, improving the separation efficiency. To be done. The effect of the tilt angles θ _1a and θ _{1b on} this improvement will be improved as the tilt angle increases, but the best angle is about 10 to 15 °,
When the angle is further increased, the effect gradually decreases, and when it exceeds 30 °, the opposite effect is obtained. In the region where the inclination exceeds 30 °, a part of the two-phase flow that has flowed into the cylindrical body from the inflow nozzle (12) extended in the cylindrical body (11) is accumulated in the bottom surface region of the cylindrical body (11). This is because the liquid droplets collide with the generated liquid surface and are triggered by the liquid surface to scatter the liquid droplets from the liquid surface. Therefore, it is desirable that the bottom surface inclination angles θ _1a and θ _1b of the inflow nozzle (12) (that is, the connection nozzle (12a) and the rectangular nozzle (12b)) with respect to the horizontal plane be 30 ° or less. It should be noted that the effects of the inclination angles θ _1a and θ _1b are significant even if the inclination angles θ _1a and θ _1b are slightly increased from 0 °. This is because the liquid film flow that is flowing largely on the bottom surface side of the inflow nozzle tends to flow due to the inclination of the surface, and the entrainment due to the gas flow from the surface of the liquid film flow is sharply reduced.

Next, the length of the inflow nozzle (12) (that is, the length from the inlet of the connecting nozzle (12a) to the outlet of the rectangular nozzle (12b) provided in the tubular body (11)) L ₁ Is preferably about 3 times or more of the inner diameter D _{13 of} the inlet pipe (13) (that is, the inlet diameter of the inflow nozzle (12)). This is because when the inflow nozzle (12) is bent from the horizontal plane (average angle θ / 2), the internal flow is directed toward the bending angle (θ / 2) at the inflow nozzle outlet (cylindrical inflow end). Corresponding to the required approach distance. That is, when the conduit bends, the flow generally drifts to the outside of the bend,
As it flows down, it is gradually corrected to a uniform distribution, and the distance that the liquid film flow returns to the inside of the bend (in this case, the bottom surface side of the inflow nozzle) is about 3 times the pipe diameter, especially in the gas-liquid two-phase flow. Because it will be.

The in-cylinder extension of the inflow nozzle (12) may have a trapezoidal cross section as well as a rectangular cross section.

[0019]

[Second Embodiment] FIG. 4 shows a second embodiment of the present invention.
A horizontal cross-sectional view (IV- in FIG. 5) showing a case where a rectangular cross-section nozzle having a shape slightly different from that of the first embodiment is provided.
IV cross section), FIG. 5 is a vertical cross-sectional side view of VV in FIG. 4, and FIG.
FIG. 6 is a vertical sectional view of VI-VI in FIG. In these figures, the parts similar to those of the first embodiment described with reference to FIGS. 1 to 3 are indicated by the reference numerals (including suffixes) in FIGS. 1 to 3 in order to avoid redundancy. A reference numeral in which 1 is replaced with 2 is given, and detailed description is omitted.

Also in this embodiment, the inflow nozzle (22)
Width B of the connecting nozzle (22a) forming the first half of the
_The side wall surface is narrowed so that _22a is about half the width B ₂₆ of the annular swirl flow path (26), and the outlet area of the connecting nozzle (22a) is not smaller than the cross-sectional area of the inlet pipe (23). The point that the bottom surface is inclined downward while maintaining the height is the same as in the first embodiment. In this embodiment, both the inner and outer wall surfaces are narrowed to narrow the width of the connecting nozzle (22a). That is, the shape of the connection nozzle (22a) is symmetrical. In addition, the cylinder (2
The rectangular nozzle (22b) extended in 1) is
The same bottom inclination θ _2a as the bottom inclination θ _2a of the connecting nozzle (22a)
_2b (= θ _2a ) and the outlet cross-sectional area of the rectangular nozzle (22b) is made equal to the outlet cross-sectional area of the connecting nozzle (22a), the outlet width B _22b of the rectangular nozzle (22b) is equal to the connecting nozzle (22a). ) The exit width B _22a is further narrowed. Inflow nozzle (22) (ie connecting nozzle (22
The length L ₂ of (a) and the rectangular nozzle (22b)) is about 3 times the inlet pipe diameter D ₂₃ or more, as in the first embodiment.

The present embodiment is different from the first embodiment in the shape and size of the rectangular nozzle. That is, in this embodiment, the cross-sectional area of the rectangular nozzle (22b) is equal to the cross-sectional area of the inlet pipe (23) and the cross-sectional area of the connecting nozzle (22a) in order to obtain a higher separation efficiency than in the first embodiment. The width B _22b of the outlet is further narrowed while being extended to the inside of the tubular body (21) while being held at. As an effect thereof, the scattering and re-scattering of the liquid droplets and the floating of the liquid droplets caused thereby are almost completely eliminated, and the separation efficiency is remarkably improved. Instead, the static pressure loss reduction, which is one of the effects of the first embodiment, is not expected.

[0022]

[Third Embodiment] FIG. 7 shows a third embodiment of the present invention.
A horizontal cross-sectional view (VII-VII cross section of FIG. 8) showing a case where a nozzle having a circular cross section is provided, FIG. 8 is a vertical side view of VIII-VIII of FIG. 7, and FIG. 9 is a front view of IX-IX of FIG. 7. Is. Also in these drawings, the same parts as those of the first and second embodiments are denoted by reference numerals in which the heads 1 or 2 of the reference numerals (including suffixes) in FIGS. 1 to 6 are replaced with 3. Omit detailed explanation.

In the third embodiment, the cylindrical body (31)
The inflow nozzle (32) extending in the cylinder along the tangential plane of the side surface of the is a circular nozzle having a diameter D ₃₂ smaller than the width B _{36 of the} annular swirl flow path (36), and has a cylindrical body ( The center line (37) of (31) is extended into the cylindrical body (31) to a position close to the center line (37), and a straight portion having a total length L ₃ including the outside and the inside of the barrel is provided, and the straight portion extends in the flow direction. To get lower
It is provided at an angle of θ _{3 with} respect to the horizontal. Here, the arrow W in FIGS. 7 and 8 indicates the direction of the jet flow, and W _{311 to} W ₃₁₃ and W _{315 to} W ₃₁₇ respectively indicate the directions of the main jets ejected from the illustrated ejection positions,
W ₃₁₄ and W ₃₁₈ are the divergent jet direction (divergent angle α
₃₁ and α ₃₂ ). Also, arrows W _{322 to} W ₃₂₄ and W
_{325 to} W ₃₂₈ typically exemplify the main direction of bounce when the droplet bounces and re-spatters after colliding with the peripheral wall.

In such a cylindrical vertical steam separator,
The main stream of liquid droplets in the gas-liquid two-phase jet introduced into the cylindrical body (31) by the inflow nozzle (32) is shown in the flow lines W _{311 to} W 3.
_As indicated by ₃₁₃ and W _{315 to} W ₃₁₇ , the straight line advances in the axial direction of the inflow nozzle toward the inner peripheral wall of the cylindrical body (31), even if the illustrated streamline W
_{As indicated by 314,} the angle α ₃₁ (divergence angle 12
Even if it spreads and flows in at about (°), it does not collide with the gas discharge pipe (34). Further, since the main stream of droplets drops along the bottom surface of the nozzle in the axial direction of the inflow nozzle, the droplets spread at an angle α ₃₂ (divergence angle of about 12) from the vicinity of the upper surface of the rear end of the nozzle, as shown by the streamline W _318. Even if there is a flow and it collides with the inner peripheral wall of the tubular body (31) and jumps upward, the height of the jump is small and the amount is small, and it goes toward the gas discharge pipe (34). The floating droplets entrained in the rising gas flow are almost eliminated, and the gas-liquid separation efficiency is improved. Furthermore, the downward flow (bottom surface inclination angle θ ₃ ) at the time of inflow promotes that the droplets carried to the inner wall of the cylinder descend (fall down) on the wall surface. As described above, the lowering of the inflow nozzle (32) toward the downstream side not only prevents re-scattering of droplets but also effectively acts on the flow of the liquid and contributes to the improvement of gas-liquid separation efficiency.

Also in this embodiment, the downward mounting angle θ ₃ of the inflow nozzle (32) with respect to the horizontal plane is preferably 30 ° or less, and the best setting is about 10 to 15 °. Further, the length L ₃ of the inclined straight portion of the inflow nozzle (32) is also the inner diameter D ₃₃ of the inlet pipe (33) (that is, the inflow nozzle (32) for the reason described in the description of the first embodiment. It is desirable that the inner diameter D ₃₂ ) is about 3 times or more. The cross-sectional shape of the inflow nozzle (32) may be oval.

[0026]

According to the present invention, almost all of the liquid droplets in the gas-liquid two-phase flow that has flowed into the cylinder from the inflow nozzle collide with and adhere to the inner peripheral wall of the cylinder, causing scattering / re-scattering and the resulting droplets. Almost no floating. In addition, the swirling flow in the annular swirling flow path is not disturbed and flows smoothly. In this way, the gas-liquid separation efficiency is significantly improved.

[Brief description of drawings]

FIG. 1 is a horizontal cross-sectional view (cross section I-I in FIG. 2) showing a first embodiment of the present invention.

FIG. 2 is a vertical sectional side view taken along the line II-II of FIG.

FIG. 3 is a vertical sectional front view taken along line III-III in FIG.

FIG. 4 is a horizontal cross-sectional view (IV-IV cross section in FIG. 5) showing a second embodiment of the present invention.

5 is a vertical cross-sectional side view taken along line VV of FIG.

6 is a vertical sectional front view of VI-VI in FIG. 4.

FIG. 7 is a horizontal cross-sectional view (cross section VII-VII of FIG. 8) showing a third embodiment of the present invention.

FIG. 8 is a vertical cross-sectional side view of VIII-VIII of FIG. 7.

9 is a vertical cross-sectional front view taken along line IX-IX of FIG. 7.

FIG. 10 is a horizontal cross-sectional view (X-X cross section of FIG. 11) showing an example of a conventional gas-liquid separator.

11 is a vertical sectional side view taken along line XI-XI of FIG.

12 is a vertical cross-sectional front view taken along the line XII-XII of FIG.

[Explanation of symbols]

(01), (11), (21), (31) Cylindrical body (02), (12), (22), (32) Inflow nozzle (12a), (22a) Connection nozzle (12b), (22b) Rectangular nozzles (03), (13), (23), (33) Inlet pipes (04), (14), (24), (34) Gas discharge pipes (05), (15), (25), ( 35) Liquid discharge pipe (06), (16), (26), (36) Circular swirl flow path (37) Cylindrical center line

Claims (1)

[Claims] 1. A vertical cylindrical tubular body, an inflow nozzle tangentially attached to a side surface of the tubular body, a gas coaxially arranged in the tubular body, and an upper end of which is opened to an upper portion of the tubular body. In a gas-liquid separation device including a discharge pipe and a liquid discharge pipe that opens at the bottom of the cylinder, the inflow nozzle is extended into the cylinder, and the extension in the cylinder has a cross-sectional area toward the downstream. It does not become smaller, the bottom surface is inclined so that it becomes lower toward the downstream side, and its width is constant or tapered along the flow, and it is formed between the cylinder body and the gas discharge pipe at the nozzle outlet. A gas-liquid separation device characterized in that it is narrower than the width of the annular swirling flow path.