JP2018155485A - Gas-liquid separation device and refrigeration device including gas-liquid separation device - Google Patents

Abstract

PROBLEM TO BE SOLVED: To solve the problem in which various types of means are adopted regarding improvement in separation performance in a conventional gas-liquid separation device, however, there has been no proposal about how to prevent a gas phase from being mixed with a liquid phase and leaking from a liquid phase outlet pipe, by paying attention to a behavior of a gas phase swirl.SOLUTION: In a gas-liquid separation device, a swirling force is added to a two-phase flow introduced in a cylindrical container from a two-phase flow inlet pipe, a gas and a liquid are separated by a centrifugal force, and a gas phase is flowed out from a gas phase outlet pipe and a liquid phase is flowed out from a liquid phase outlet pipe. A downward conical inclined surface part is formed in which an apex angle is 120 degrees or less in a cross section including a central axis of a cylindrical part, and the liquid outlet pipe is provided at a position of the inclined surface part excluding a connection curved surface provided between the inclined surface part and the cylindrical part of the cylindrical container. Also, in the cross section including the central axis of the cylindrical part, when a ridge line between a cylindrical part inner wall 2b and a connection curved surface inner wall 13a is defined as X, a distance between the ridge line X and the central axis of the cylindrical part is defined as L, and a distance between the ridge line X and a central axis of the liquid phase outlet pipe is defined as L, L/L<0.6 is satisfied.SELECTED DRAWING: Figure 5

Description

  The present invention relates to a gas-liquid separation device for separating a gas phase and a liquid phase used in a mechanical system that handles a refrigeration cycle, a vapor cycle, and a gas-liquid two-phase flow, and a refrigeration device, a vapor cycle device, and a gas-liquid two-phase using the same. More particularly, the present invention relates to a technique for further improving performance, downsizing, and reducing the price.

  Gas-liquid separator for separating gas-phase refrigerant and liquid-phase refrigerant, gas-liquid separator for separating water vapor and water or air and water, oil separator for separating oil and gas, and mechanical system for handling gas-liquid two-phase flow A gas-liquid separator that separates gases and liquids (hereinafter collectively referred to as a gas-liquid separator) rotates a two-phase flow and attaches the liquid to the wall surface by the centrifugal force of the swirling flow. Gas-liquid separation devices that separate liquids by gravity are mainly used.

  For example, in a gas-liquid separator for a refrigeration cycle that separates a gas phase refrigerant and a liquid phase refrigerant, a gas phase outlet pipe is provided at the upper end of the container, a liquid phase outlet pipe is provided at the lower part of the container, and a two-phase inlet pipe is provided. Provided above the container, the two-phase flow that has flowed into the container from the inlet pipe is swung along the inner wall surface of the container, separated into a gas phase and a liquid phase by the action of centrifugal force, and the gas phase is caused to flow out from the gas phase outlet pipe, After the liquid phase is attached to the inner wall surface of the container, the liquid phase is temporarily stored under the container by the action of gravity, and is taken out from the liquid phase outlet pipe.

JP 2005-265387 A JP 2002-061993 JP 2007-107861 A JP 2001-99527 A

  The gas-liquid separators described in Patent Documents 1 to 4 described above have also taken various measures for improving the gas-liquid separation performance, but determined the inlet position of the liquid-phase outlet pipe in relation to the gas-phase vortex, There were few references that prevented the gas phase from being sucked into the phase and coming out of the liquid phase outlet tube.

That is, the gas-liquid separation device 51 disclosed in the cited references 1 (FIG. 16) and 2 (FIG. 17) is provided with a conical slope portion on the bottom wall and the inlet position of the liquid phase outlet pipe at the lowermost end. The liquid level is increased by improving the performance by providing a conical slope portion on the bottom wall.
However, in this type of gas-liquid separator, the swirling flow of the liquid phase that flows while swirling along the conical slope portion develops as it goes downward as the centrifugal force increases.
When the swirl flow develops, the liquid phase stored on the bottom wall is pushed up along the side surface of the cylindrical container peripheral wall as shown by the broken line in FIG. Along with this, the lowermost end of the gas phase vortex is lowered, approaches the liquid phase outlet pipe inlet 55a, and the gas phase flows out of the liquid phase outlet pipe 55, which deteriorates the gas-liquid separation performance.
In Patent Documents 1 and 2, there is no description to improve the gas-liquid separation performance by paying attention to the relationship between the swirling flow and the liquid phase outlet pipe 55.

  In Patent Document 3 (FIG. 18), a protrusion is provided at the center of the bottom wall, and a liquid phase outlet pipe 55 is provided below the upper end position of the protrusion. The protrusion 57 has a large function in the sense of raising the liquid level 56 of the liquid reservoir accumulated in the bottom wall 52a and preventing the gas phase from flowing out from the liquid phase outlet pipe 55 together with the liquid phase. There is a problem that attaching 57 to the bottom wall 52a is expensive and increases the number of processing steps. In addition, this patent document 3 does not describe the swirling flow, and does not describe how the protrusion 57 contributes to the swirling flow.

In Patent Document 4 (FIG. 19), the liquid phase outlet pipe 55 is provided not near the center of the substantially flat bottom wall 52a but near the cylindrical side wall. In this case as well, since the bottom wall 52a is substantially flat, the gas phase vortex is likely to fluctuate from the central axis of the container due to speed and pressure fluctuations, and the gas phase vortex is likely to approach the liquid phase outlet tube inlet 55a. The gas phase easily flows out together with the liquid phase. Further, since the liquid phase outlet pipe 55 has to be provided on a curved surface having a complicated curved surface shape, there are problems such as difficult drilling work and difficult welding work.
Further, as in Patent Documents 1 and 3, there is no description about the swirling flow, and no consideration is given to the behavior of the swirling flow.
The inventor clarified the phenomenon in which the gas phase is sucked into the liquid phase outlet pipe by performing verification with reference to the examples of the above patent documents. That is, the two-phase flow that flows in from the inlet pipe is separated into a liquid phase and a gas phase by centrifugal force, and the gas phase becomes a gas phase vortex by centrifugal force and is finally discharged to the gas phase outlet pipe. If there are fluctuations in the speed, pressure, etc. of the two-phase flow due to the operating conditions, the gas-phase vortex approaches the liquid-phase outlet pipe inlet due to the difference in the shape of the gas-phase vortex and the degree of instability. It will be sucked into the phase outlet pipe. As a result, it became clear that the gas-liquid separation performance deteriorated. It has also been found that the shape and stability of the gas phase vortex varies depending on the shape of the container bottom and the position of the liquid phase outlet pipe inlet.

  The present invention has been made to solve the above-mentioned problems, and the object of the present invention is to improve the performance and further reduce the size of a small gas-liquid separator that separates gas and liquid by centrifugal force by swirling flow. In addition, the gas-liquid separation device can be incorporated into various devices such as a refrigeration device, a steam cycle device, and a fluid mechanical device that handles a gas-liquid two-phase flow, and can improve the efficiency and reliability of the device. Is to provide.

Means to solve the problem

The present invention provides a gas-liquid separation device that can improve performance while remaining compact.
That is, a swirling force is applied to the two-phase flow introduced into the cylindrical container from the two-phase inlet pipe, and gas and liquid are separated by centrifugal force. The gas phase is from the gas-phase outlet pipe, and the liquid phase is the liquid-phase outlet pipe. Further, in the gas-liquid separation device that is allowed to flow out, the apex angle is 120 degrees or less (preferably 90 to 120 degrees) in a cross section including the central axis of the cylindrical portion at the lower end of the cylindrical portion of the cylindrical container, and The inclined surface portion formed with a downwardly conical inclined surface portion having an inclined surface portion outermost lowermost point h on the substantially central axis of the cylindrical portion, and the connecting curved surface provided between the inclined surface portion and the cylindrical portion of the cylindrical container is removed. In the cross section including the central axis of the cylindrical portion, the ridgeline between the cylindrical portion inner wall 2b and the connection curved inner wall 13a is X, and the ridgeline X and the central axis of the cylindrical portion The distance is L ₀ and includes the intersection of the ridgeline X, the central axis of the liquid-phase outlet pipe 6 and the inclined portion inner side 10b. The gas-liquid separator is L ₁ / L ₀ <0.6, where L ₁ is the distance from the line segment parallel to the central axis of the cylindrical portion.

Further, a swirling force is applied to the two-phase flow introduced into the cylindrical container from the two-phase inlet pipe, and gas and liquid are separated by centrifugal force. The gas phase is from the gas-phase outlet pipe, and the liquid phase is the liquid-phase outlet pipe. Further, in the gas-liquid separation device that is allowed to flow out, the apex angle is 120 degrees or less (preferably 90 to 120 degrees) in a cross section including the central axis of the cylindrical portion at the lower end of the cylindrical portion of the cylindrical container, and In addition to the substantially central axis of the cylindrical portion, the inclined surface is formed with a downward cone-shaped inclined surface portion having an outermost lowermost point h, and the connecting curved surface provided between the inclined surface portion and the cylindrical portion of the cylindrical container is removed. A liquid phase outlet pipe is provided at the position of the slope portion on the opposite side of the slope portion outer lowest point h with respect to the central axis of the cylindrical portion, and the cross section includes the central axis of the cylindrical portion. In this case, the ridge line between the inner wall 2b of the cylindrical portion and the inner wall 13a of the connecting curved surface is defined as X, and the distance between the ridge line X and the central axis of the cylindrical portion. It was a L _0, the distance L ₂ between the center axis of the parallel line segments and the cylindrical portion to the central axis of the cylindrical part including the inclined surface portion outer lowermost point _h, the ridge line X, the central axis and the liquid phase outlet pipe Gas liquid with L ₁ / (L ₀ + L ₂ ) <0.6, where L ₁ is the short side of the distance from the line segment parallel to the central axis of the cylindrical portion including the intersection with the slope portion inner side 10b. Separation device.

  Further, a swirling force is applied to the two-phase flow introduced into the cylindrical container from the two-phase inlet pipe, and gas and liquid are separated by centrifugal force. The gas phase is from the gas-phase outlet pipe, and the liquid phase is the liquid-phase outlet pipe. Further, in the gas-liquid separation device that is allowed to flow out, a downward conical shape having a vertical angle of 120 degrees or less (preferably 90 to 120 degrees) in a cross section including the central axis of the cylindrical portion at the lower end of the cylindrical portion of the cylindrical container. A cross section that includes a liquid phase outlet pipe at the position of the lower end of the cylindrical portion that forms the inclined portion and removes the connecting curved surface provided between the inclined portion and the cylindrical portion of the cylindrical container, and includes the central axis of the cylindrical portion Where X is the ridgeline between the inner wall 2b of the cylindrical portion and the connecting curved inner wall 13a, and L is the distance between the ridgeline X and the lower end of the outer diameter of the liquid phase outlet pipe provided at the lower end of the cylindrical portion where the connecting curved surface is removed. The gas-liquid separator is L / d <2.5, where d is the inner diameter of the liquid phase outlet pipe.

  Further, the gas-liquid separation device described above is provided with a protrusion on the inner side of the lowermost end of the slope portion at the lower end of the cylindrical portion of the cylindrical container.

  Further, the protrusion formed at the innermost lower end of the slope portion is the above-described gas-liquid separation device formed integrally with the cylindrical container.

  Further, the projection formed on the inner side of the lower end of the slope portion is the gas-liquid separator described above formed by raising a brazing material that seals the tip of the slope portion of the cylindrical container to the inner side of the lower end of the slope portion.

Further, the projection formed on the innermost lower end of the slope portion is a cylinder including the ridgeline X, where X is the ridgeline between the cylindrical portion inner wall 2b and the connection curved inner wall 13a in the cross section including the central axis of the cylindrical portion of the cylindrical container. part of the distance between the inclined surface portion inside the lowest point h _in the cylindrical portion the lower end of the vertical plane and the cylindrical container to the central axis and h ₁ of the vertical plane and the cylindrical container the central axis of the cylindrical part including the apex of the protrusion when the distance between the inclined surface portion inside the lowest point _{h in} the cylindrical portion the lower end to the _{h 0,} a gas-liquid separator described above in which the h ₀ / h 1> 0.06.

  In addition, the gas-liquid separator is disposed between the compressor discharge pipe and the condenser of the refrigeration cycle, the compressor discharge pipe is connected to the two-phase inlet pipe of the gas-liquid separator, and the liquid phase of the gas-liquid separator is This is a refrigeration system in which the outlet pipe is connected to the compressor suction pipe via a flow rate adjusting throttle, while the gas-phase outlet pipe of the gas-liquid separator is connected to a conduit leading to the condenser.

  In addition, the gas-liquid separator is disposed between the decompressor and evaporator of the refrigeration cycle, the two-phase inlet pipe of the gas-liquid separator is connected to the decompressor outlet pipe, and the liquid-phase outlet pipe is connected to the evaporator inlet. It is a refrigeration apparatus which is connected and connected to a compressor suction pipe after the vapor phase outlet pipe bypasses the evaporator.

  Further, the fluid mechanical device is provided with the gas-liquid separation device and separates the gas-liquid two-phase flow into a gas phase and a liquid phase.

  Since the gas-liquid separator of the present invention has a slope portion and the liquid-phase outlet pipe is defined at an optimum position, it can be a small-sized gas-liquid separator having good gas-liquid separation performance. Furthermore, the gas-liquid separation device of the present invention can be a gas-liquid separation device that has good mass productivity and is inexpensive. Furthermore, by adopting the gas-liquid separation device, various devices such as a refrigeration device, a steam cycle device, and a mechanical device that handles a gas-liquid two-phase flow can be obtained with improved efficiency and reliability of the device.

It is sectional drawing which shows the gas-liquid separation apparatus of Embodiment 1 provided with this invention. It is sectional drawing which shows the gas-liquid separation apparatus of Embodiment 1 provided with this invention different from FIG. It is an expanded AA sectional view of the gas-liquid separation device shown in FIG. It is principal part expansion explanatory drawing of FIGS. 1-1. FIG. 4 is an example of the relationship between the mounting position (L / d) of the liquid phase outlet pipe and the liquid phase outlet side vapor phase mixing ratio shown in FIG. 3 and the relationship between L / d and distance L. It is sectional drawing explaining the attachment position of the liquid phase exit pipe | tube different from FIG. FIG. 5 is an enlarged explanatory view of a main part of FIG. 4. FIG. 5 is an enlarged explanatory view of a main part of a cross-sectional view for explaining a mounting position of a liquid phase outlet pipe different from FIGS. 1 and 4. It is explanatory drawing which compared and examined the liquid phase exit side gaseous-phase mixing ratio of the centrifugal gas-liquid separation apparatus from which a cylindrical container lower part throttle shape differs. Among the verification results shown in FIG. 6, the relationship between the liquid phase outlet-side gas phase mixing ratio and the gas phase outlet-side liquid phase mixing ratio for the gas-liquid separation apparatus equipped with the present invention and the gas-liquid separation apparatus having the conventional structure is shown. It is explanatory drawing verified. It is explanatory drawing which verified the magnitude | size of the upward protrusion and the liquid-phase exit side gaseous-phase mixing ratio among the verification results in FIG. Is a diagram of the liquid phase outlet vapor contamination ratio was verified when the mounting position of the liquid outlet pipe _(L 1 _/ L ₀₎ was variable shown in FIG. 5 It is a figure which shows the relationship between a cone-shaped apex angle and a liquid phase exit side vapor phase mixing ratio. It is the figure explaining the movement of the liquid phase and gas phase of the liquid phase exit pipe | tube part of the gas-liquid separator provided with this invention with the photograph. It is the figure explaining the movement of the liquid phase and gas phase of the liquid phase exit pipe | tube part of the gas-liquid separator which is not equipped with this invention with the photograph. It is sectional drawing explaining the principal part of the structure of the gas-liquid separator different from FIG. It is sectional drawing explaining the attachment position of the liquid phase exit pipe | tube different from FIG. It is sectional drawing explaining the upward protrusion different from FIG. The embodiment provided with this invention is shown and it is a refrigeration cycle block diagram at the time of using a gas-liquid separator for a refrigeration cycle. FIG. 14 is an example of another refrigeration cycle configuration diagram when the gas-liquid separation device of the present invention is used in a refrigeration cycle, which is different from FIG. 13. FIG. 9 is a system diagram showing another embodiment including the present invention, in which a gas-liquid separation device is applied to a fluid mechanical device that handles a gas-liquid two-phase flow. It is a figure explaining the structure and gas-liquid separation state of the conventional gas-liquid separation apparatus. It is a figure explaining the structure and gas-liquid separation state of the conventional gas-liquid separator of the structure different from FIG. It is a figure explaining the structure and gas-liquid separation state of the conventional gas-liquid separation apparatus of the structure different from FIG. 16, FIG. It is a figure explaining the structure and gas-liquid separation state of the conventional gas-liquid separation apparatus of the structure different from FIGS.

  Embodiments of the present invention will be described below with reference to the drawings. In addition, this invention is not limited by this embodiment. Further, in each embodiment, the description already given in one embodiment may be omitted in another embodiment. Therefore, the configurations described in the embodiments can be freely combined within a range that does not impair the effects of the invention.

Embodiment 1

The first embodiment of the present invention will be described with reference to FIG. 1, FIG. 1-1, FIG. 2, and FIG. Here, FIG. 1 is a cross-sectional view for explaining the structure of the gas-liquid separation device 1 equipped with the present invention and the relationship between the swirling flow and the liquid phase outlet pipe 6, and FIG. FIG. 2 is a cross-sectional view of a structure in which an upward projection is added to the inside of the lower end of the inclined portion, FIG. 2 is a cross-sectional view taken along line AA in FIGS. 1 and 1-1, and FIG. It is explanatory drawing.
1 and 2, a gas-liquid separation device 1 of the present invention has a cylindrical portion 2 a constituting a cylindrical container 2, a connecting curved surface 13, and an inclined surface portion 10. Is formed. The cylindrical container 2 has a two-phase inlet pipe 7 provided with the center line shifted from the side of the upper wall surface as shown in FIG. The cylindrical container 2 has a gas phase outlet pipe 9 penetrating the cylindrical container 2 in the central axis direction, and a liquid phase outlet pipe 6 beside the lower wall surface of the cylindrical container 2. The inner diameter of the liquid phase outlet pipe 6 is set so that d / D ≦ 0.3, where D is the inner diameter of the cylindrical container 2 and d is the inner diameter of the liquid phase outlet pipe 6. D / D may be 0.29 or less, 0.28 or less, 0.27 or less, 0.26 or less, and the like. Further, d / D may be 0.10 or more, 0.13 or more, 0.16 or more, 0.19 or more, and the like.
3 is a gas-liquid separation chamber formed in the cylindrical container 2, 4 is a liquid reservoir, and 5 and 5 a are liquid levels of the liquid reservoir 4. Reference numeral 10 denotes a slope part forming the lower part of the cylindrical part, which has a downward conical shape, and its apex angle is 90 to 120 degrees in a cross section including the central axis of the cylindrical part. The lower limit value of the apex angle may be 50 degrees, 55 degrees, 60 degrees, 65 degrees, 70 degrees, 75 degrees, 80 degrees, 85 degrees, or the like.
Below, the effect is described about the cone-shaped slope part 10. FIG.
The liquid surface 5a is a liquid surface in the present invention when the lower portion of the cylindrical portion is the conical slope portion 10. The liquid level 5 is the liquid level when the bottom of the cylindrical portion is flat, for example, and is displayed to explain the difference from the liquid level 5a.
The liquid surfaces 5 and 5a are designed and managed so that they are always above the inlet 6a of the liquid phase outlet pipe 6, and the gas phase flows out of the liquid phase outlet pipe 6 together with the liquid phase, thereby separating performance. Is prevented from falling.
Since the lower part of the cylindrical part is the conical slope part 10, the centrifugal force increases, so that the swirling flow of the liquid phase (liquid phase vortex) is, for example, compared with the case where the bottom part of the cylindrical part is flat, From the liquid level 5, the central portion is further recessed, and the outer peripheral portion further rises along the cylindrical portion inner wall 2b.
In the case where the lower portion of the cylindrical portion is the conical slope portion 10, the liquid phase outlet pipe 6 is equivalent to the height difference between the liquid surface 5 and the liquid surface 5a on the inner wall 2b of the cylindrical portion, as compared with the case where the bottom surface of the cylindrical portion is flat. Since the liquid level is separated from the inlet 6a, the inlet 6a is easily blocked by the liquid level even if the liquid level fluctuates depending on operating conditions, for example, and the gas phase mixing ratio to the liquid phase outlet pipe 6 can be suppressed. In order to raise the liquid level, the cylindrical container can be lengthened and the liquid level 5 can be designed and managed higher. In this case, however, the size of the cylindrical container is reversed. If the conical slope part 10 is provided in the lower part of the cylindrical part as in the present invention, the separation performance can be maintained high without lengthening the cylindrical container, that is, without enlarging the gas-liquid separator. Further, the inclined surface portion 10 has a function of guiding and collecting a swirling flow (gas phase vortex) in a gas phase flowing into the gas-liquid separation chamber 3 to the center of the conical shape along the inclined surface portion. This is to suppress the mixing ratio of the gas phase into the pipe 6.

Next, the mounting structure of the liquid phase outlet pipe 6 to the cylindrical container 2 will be described with reference to FIG. In FIG. 3, the liquid level is omitted.
In FIG. 3, 1 is a gas-liquid separator, 2 is a cylindrical container, 6 is a liquid phase outlet pipe, 7 is a two-phase inlet pipe, 9 is a gas phase outlet pipe, and 10 is a slope portion. The portion 10 is a slope portion that forms a downward conical shape with an apex angle of 90 to 120 degrees in a cross section including the central axis of the cylindrical portion. Reference numeral 11 denotes an upward projection. In FIG. 3, L ₁ / L ₀ described later in the second embodiment can be defined in the same manner as in the second embodiment, L ₁ / L ₀ is zero, and L ₁ / L ₀ <0. 6 is satisfied. That is, according to the same concept as in the second embodiment, in the cross section including the central axis of the cylindrical portion of the cylindrical container, L ₀ is a ridge line when the ridge line between the cylindrical portion inner wall 2b and the connection curved inner wall 13a is X. It is defined as the distance between X and the central axis of the cylindrical portion. Further, L ₁ is a ridge line X, (corresponding to Embodiment 2, the inclined surface portion inside 10b) central axis of the liquid outlet pipe 6 parallel to the central axis of the cylindrical part including the intersection of the cylindrical inner wall 2b The parallel line segment is the cylindrical inner wall 2b, and therefore L ₁ = 0. Thus, L ₁ / L ₀ = 0. Note that L ₁ / L ₀ may be less than 0.5, less than 0.4, less than 0.3, less than 0.2, or the like.

  In the present invention, a downward conical shape is formed in the lower part of the cylindrical portion, and the position where the liquid phase outlet pipe 6 is attached to the cylindrical container 2 is regulated, thereby suppressing the gas phase mixing ratio into the liquid phase outlet pipe 6. , Downsizing, and improving the workability of mounting the liquid phase outlet pipe 6. In addition, the ideal liquid phase outlet-side gas phase mixing ratio is zero, but the practically acceptable liquid phase outlet-side gas phase mixing ratio is 0.03.

  In FIG. 3, the liquid phase outlet pipe 6 is provided on the lower end side of the cylindrical portion from which the connection curved inner wall 13a is removed. In FIG. 3, the liquid phase outlet pipe 6 is provided above the ridgeline X.

  Here, the position of the liquid-phase outlet pipe 6 provided on the lower end side of the cylindrical portion from which the connection curved inner wall 13a is removed is set to the cylindrical inner wall 2b and the connection curved inner wall 13a in the cross section including the central axis of the cylindrical portion of the cylindrical container. By managing L / d <2.5, where X is the ridge line with L, L is the distance between the ridge line X and the lower end of the liquid phase outlet pipe outer diameter, and d is the liquid phase outlet pipe inner diameter, The exit-side gas-phase mixture ratio becomes smaller and the size can be reduced. On the other hand, the processability of the cylindrical container for mounting the liquid-phase outlet pipe is excellent. Further, since L is shortened and the amount of stored liquid can be reduced, the amount of staying liquid can be reduced, and a gas-liquid separator that can contribute to resource saving of the refrigeration cycle can be obtained. In addition, the liquid phase exit pipe outer diameter lower end shown here shows the outer diameter lower end part of the liquid phase exit pipe at the connecting portion between the cylindrical container and the liquid phase exit pipe 6.

For example, when the inner diameter D of the cylindrical container is 35 mm, the inner diameter d of the liquid phase outlet pipe is 6 mm, and the distance L between the outer diameter lower end of the liquid phase outlet pipe and the ridge line X is 15 mm, L / d = 2.5. .
FIG. 3A shows an example of the relationship between the mounting position (L / d) of the liquid phase outlet pipe shown in FIG.
As is clear from FIG. 3-1, in order for the liquid phase outlet side gas phase mixing ratio to be 0.03 or less which is practically acceptable, L / d <19 may be satisfied. The overall length of the cylindrical container becomes long. When L is further shortened and L / d <6.5, a high-performance of 0.02 or less, which is less than 0.03, which is practically acceptable, is ensured. Not optimal in terms of sex and liquid storage. When L / d <2.5, that is, L = 15 mm or less, the liquid phase outlet side gas phase mixing ratio is maintained at 0.02, and the miniaturization, workability, and liquid storage properties are optimal.
In addition, by setting L / d <2.5, as will be described later with reference to FIG. 7, it is possible to significantly improve the liquid phase outlet side gas phase mixing ratio while maintaining the gas phase outlet side liquid phase mixing ratio small. it can.
Note that L / d may be less than 2.0, less than 1.5, less than 1.0, less than 0.5, or the like.
The reason for removing the liquid phase outlet pipe from the connection curved surface 13 is as follows.
That is, the connecting curved inner wall 13a is a complicated curved surface in which the cylindrical inner wall 2b and the conical sloped inner surface 10b are smoothly connected, so that a mounting hole for the liquid phase outlet pipe 6 is formed on the curved surface. It is difficult to braze with high accuracy. Therefore, the drilling operation and the welding operation are facilitated by attaching the liquid phase outlet pipe 6 while avoiding the connecting curved inner wall 13a.

Next, in FIG. 1 and FIG. 9, the reason why the apex angle of the downward cone shape is set to 90 to 120 degrees in the cross section including the central axis of the cylindrical portion of the cylindrical container will be described. FIG. 9 shows the liquid phase outlet side vapor phase mixing ratio when the apex angle is changed from 90 to 180 degrees in the shape of FIG. 1, the horizontal axis is the apex angle of the downward cone shape, and the vertical axis is the liquid phase. It is the exit side vapor phase mixing ratio. Further, the bold line is the actual measurement value of the liquid phase outlet side vapor phase mixing ratio, and the upper and lower thin lines indicate the variation with respect to the actual measurement value of the liquid phase outlet side gas phase mixing ratio. Here, the vertex angle corresponding to the practically acceptable liquid phase outlet side gas phase mixing ratio 0.03 including variations is 120 degrees. That is, the apex angle of 90 to 120 degrees is an angle at which the liquid phase outlet side gas phase mixing ratio can be maintained at 0.03 or less as shown in FIG.
The liquid phase outlet side gas phase mixing ratio 0.03 is a practically acceptable liquid phase outlet side gas phase mixing ratio, but corresponds to L ₁ / L ₀ <0.6 in FIG. 8 described later. Since the liquid phase outlet side vapor phase mixing ratio 0.03 is also the starting point of curvature change, the upper limit of the apex angle is set to 120 degrees corresponding to 0.03. Regarding the lower limit of the apex angle, the smaller the apex angle, the better the liquid phase outlet side vapor phase mixing ratio. When estimated by an approximate expression from experimental values, for example, 0.019 at an apex angle of 90 degrees, 0.011 at an apex angle of 60 degrees, and when L = 0 at which the liquid phase outlet pipe is the lowest end in FIG. The apex angle is 0.009 at about 50 degrees. On the other hand, when the apex angle becomes small, the total length of the gas-liquid separator becomes long. For example, when the apex angle is about 50 degrees, the length of the conical portion becomes 37 mm, and the processing cost and material cost also increase. The apex angle can be selected depending on whether the emphasis is on gas-liquid separation performance or the total length, but the lower limit of the apex angle is about 50 degrees in terms of structure. Considering the balance between the separation performance and the total length, the lower limit of the apex angle is preferably 60 degrees, more preferably the lower limit of the apex angle is 90 degrees, and the conical part length is about 18 mm.

Next, referring to FIG. 3, an embodiment of a gas-liquid separation device in which an upward projection is provided in the vicinity of the central axis of the cylindrical portion inside the lowermost end of the slope portion of the cylindrical portion of the cylindrical container will be described.
That is, if there is an upward protrusion at the lower end of the conical slope, the liquid phase swirl (liquid vortex) tends to rotate around the upward protrusion, so the liquid vortex is held at the center of the conical slope. Is done.
Therefore, the gas phase vortex is also more stably held at the center of the conical shape with the movement of the liquid phase vortex.

In addition, the inflow speed of the two-phase flow may be high and the lower end of the gas phase vortex may reach an upward projection. In this case, since the gas phase vortex tends to swivel around the upward protrusion, the gas phase vortex is held more stably at the conical center.
That is, with the above-described configuration, the liquid-phase vortex and the gas-phase vortex are more concentrated in the central portion of the cone due to the operational effects of the conical slope portion and the upward projection described in detail later. It is held more stably.

Next, referring to FIG. 3, an embodiment of a gas-liquid separation device will be described in which a brazing material that seals the tip of the slope portion of the cylindrical container is raised inside the bottom end of the slope portion to form an upward projection.
The upward projection 11 of the present invention is not formed by using a special separate part in the production stage of the gas-liquid separator 1 as in the prior art, but is formed by using a member necessary for the structure. Therefore, compared with the protrusion provided by using another component on the bottom of the container of the conventional gas-liquid separator, the number of components and processes is reduced, and the structure is suitable for mass production. For example, in a gas-liquid separation device manufactured by spinning or spatula drawing, a brazing material is filled so as to rise inside the lowermost end of the slope portion when brazing is part of the process.
The details of the above-described projection formation by brazing are as follows. That is, when the slope portion 10 is formed by spinning or spatula drawing, a hole is formed at the tip of the slope portion 10 at the final stage of drawing. Normally, this hole is closed by brazing. The projection 11 of the present invention is a brazing material 11a used in the brazing, and forms the upward projection 11. When brazing, the brazing material closes the hole with the end of the inclined portion 10 as the upper surface. 11a is poured and the brazing material 11a is suspended by its own weight to form an upward projection 11.
As described above, it is a matter of course that the effect of the protrusion described above can be obtained by using the brazing material for the protrusion.

In summary of the first embodiment, the movement of the swirling flow entering the gas-liquid separation chamber 3 from the two-phase inlet pipe 7 provided with the present invention, and the swirling of the cone-shaped slope portion 10 and the upward projection described above. The relationship with the flow, and further the relationship with the improvement of the gas-liquid separation performance by these will be described.
That is, when the two-phase flow swirls in the gas-liquid separation chamber 3 of the cylindrical container 2, the liquid phase component with high density swirls along the outer periphery of the cylinder by the action of centrifugal force, and the gas phase component with low density becomes The inside of the swirling liquid phase component, that is, the vicinity of the central portion in the cylinder is swirled. At this time, the liquid surface vortex liquid surface, which is the boundary surface between the liquid phase and the gas phase by the action of centrifugal force, is centered on the center of the cylindrical portion of the cylindrical container, as shown by the solid line liquid surface 5 (shown in FIG. 1). It becomes a rotating parabolic shape. That is, the swivel center of the liquid level enters into the liquid reservoir, and the center is recessed.

If the lower part of the cylinder has a conical slope, the turning radius decreases along the conical slope 10 and the centrifugal force increases. Therefore, as the centrifugal force increases, the liquid phase vortex develops further downward as shown by the broken liquid surface 5a (shown in FIG. 1), and more stably at the lower center of the conical shape. Retained.
On the other hand, the gas phase vortex is also guided to the lower center portion of the conical shape along with the movement of the liquid phase vortex, so that the lower end of the gas phase vortex is stably held at the central portion of the conical shape.
Furthermore, as described above, if the conical slope portion 10 has an upward protrusion 11 at the lower end, the liquid phase vortex tends to rotate around the protrusion, so the center of the liquid phase vortex is the center of the protrusion 11, that is, , Held at the center of the conical slope 10. Therefore, the gas phase vortex is also more stably held at the center of the conical shape with the movement of the liquid phase vortex.

  The fluctuation of the gas phase vortex is suppressed by both the effect of the cone-shaped slope portion and the effect of the upward projection described above, and the gas phase can be prevented from being mixed with the liquid phase and flowing out from the liquid phase outlet pipe. Therefore, a gas-liquid separation device with greatly improved gas-liquid separation performance can be obtained.

  On the other hand, the speed of two-phase flow flowing into the gas-liquid separator, the pressure, the ratio of the gas-phase liquid phase, and the like may vary depending on the operating conditions of the equipment. At this time, if the shape of the gas phase vortex is not the shape of the present invention, the lower end swirling center position of the gas phase vortex may deviate from the center portion of the conical shape. Since the distance between the liquid phase outlet pipe 6 and the liquid phase outlet pipe 6 is always kept at a certain value or more, fluctuation of the gas phase vortex can be suppressed and the gas phase can be prevented from flowing out of the liquid phase outlet pipe 6. .

Hereinafter, the effects of the present invention that have been frequently described will be described using FIG. 6, FIG. 7, and FIG.
First, as the gas-liquid separation performance, the liquid phase outlet side gas phase mixture ratio and the gas phase outlet side liquid phase mixture ratio are defined as follows.
That is, of the two-phase flow flowing from the inlet pipe, the liquid phase total flow rate is W _L , the gas phase total flow rate is W _g ,
Of the two-phase flow discharged from the liquid phase outlet pipe, the liquid phase flow rate is WL _{(liquid phase outlet pipe)} , the gas phase flow rate is W _{g (liquid phase outlet pipe) ,}
Of the two-phase flow discharged from the gas phase outlet pipe, the liquid phase flow rate is W _{L (gas phase outlet pipe)} , the gas phase flow rate is W _{g (gas phase outlet pipe) ,}
The liquid phase outlet side gas phase mixing ratio is defined as W _{g (liquid phase outlet pipe)} / W _g ,
The vapor outlet liquid phase mixture ratio, W L _{(vapor outlet pipe)} / W _L and defined.
According to this definition, the smaller the value of the liquid phase outlet side gas phase mixing ratio and the gas phase outlet side liquid phase mixing ratio, the better the gas-liquid separation performance.
In addition, as an ideal function of the gas-liquid separator, the liquid phase outlet side gas phase mixing ratio is preferably 0, but in practice, in many cases, the liquid phase outlet side gas phase mixing ratio is allowed to about 0.03. The

FIG. 6 is a diagram showing a result of comparison and verification of the liquid phase outlet side vapor phase mixing ratio when the cylindrical container lower part shape is changed. The test conditions at this time are as follows.
1. The inflowing two-phase flow rate is constant.
2. The ratio of the inflowing gas phase and liquid phase is constant.
3. The gas phase outlet side liquid phase mixture ratio is constant.
As is clear from this test result, the liquid phase outlet side gas phase mixing ratio that achieves the target of 0.03 or less is “C cone shape of the present invention” and “D cone shape of the present invention + low protrusion shape”. "E" Conical shape of the present invention + projection shape height "," A Conventional conical shape (the liquid phase outlet pipe is concentric with the cylindrical portion of the cylindrical container) "," B End plate shape "of the conventional shape The target of 0.03 cannot be achieved.
This is because “C-cone shape of the present invention”, “D-cone shape of the present invention + low projection shape” and “E-cone shape of the present invention + protrusion shape high” have a slope, and the liquid phase outlet pipe 6 This is because the mounting position is set to L ₁ / L ₀ = 0, that is, L ₁ / L ₀ <0.6, and the fluctuation of the gas phase vortex is suppressed so that the fluctuation does not reach the liquid phase outlet pipe 6.
In addition, “D Conical shape of the present invention + low protrusion shape” and “E Conical shape of the present invention + high protrusion shape” are better than “C Conical shape of the present invention”. This is because the fluctuation of the vortex is further suppressed and the gas phase is prevented from flowing out from the liquid phase outlet pipe.

Next, FIG. 7 shows a gas-liquid separator equipped with the present invention (FIG. 1 or “C-conical shape of the present invention” in FIG. 6) and a conventional gas-liquid separator (FIG. 17 or “A conventional” in FIG. 6). In a conical shape (the liquid phase outlet pipe is concentric with the cylindrical portion of the cylindrical container))), the relationship between the liquid phase outlet side vapor phase mixing ratio and the gas phase outlet side liquid phase mixing ratio is shown. It is a graph which made the vertical axis | shaft the gas-phase exit side liquid phase mixing rate in the phase-outlet side gas-phase mixing rate. The test conditions at this time are as follows.
1. The inflowing two-phase flow rate is constant.
2. The ratio of the inflowing gas phase and liquid phase is constant.
As can be seen from FIG. 7, in the conventional structure (FIG. 17 or “A Conventional conical shape (the liquid phase outlet pipe is concentric with the cylindrical portion of the cylindrical container)” in FIG. If the gas phase is reduced (that is, the gas-liquid separation performance on the liquid-phase outlet side is improved), the gas-phase outlet-side liquid-phase mixing ratio increases and the gas-phase gas-liquid separation performance deteriorates. However, in the gas-liquid separation apparatus (FIG. 1 or “C-cone shape of the present invention” in FIG. 6) provided with the present invention, the gas-liquid separation performance on the liquid phase side is reduced by reducing the liquid phase outlet side vapor phase mixing ratio. Even if it improves, the gaseous-phase exit side liquid phase mixing ratio can be maintained with small, and the gas-liquid separation performance of the gaseous-phase side can be maintained well.
In other words, the gas-liquid separation device equipped with the present invention ("C-cone shape of the present invention" in FIG. 6) greatly reduces the liquid phase outlet side gas phase mixing ratio while keeping the gas phase outlet side liquid phase mixing ratio small. It was verified that small improvements could be made.

Next, the “C cone shape of the present invention”, “D cone shape of the present invention + low projection shape”, and “E cone shape of the present invention + projection shape height” described above, that is, the height of the upward projection 11 and the liquid phase The relationship of the outlet side gas phase mixing ratio will be described with reference to FIGS.
First, in FIG. 3, the height of the upward projection 11 is defined as follows. That is, in the cross section including the central axis of the cylindrical portion of the cylindrical container, the ridgeline between the cylindrical inner wall 2b and the connecting curved inner wall 13a is X, and the plane perpendicular to the cylindrical container central axis including X and the cylindrical portion of the cylindrical container the distance between the inclined surface portion inside the lowest point h _in the bottom h _1, of the cylindrical portion the lower end of the vertical plane and the cylindrical container in a cylindrical container the central axis including the apex of the upward projection inclined surface portion of the inner lowest point h _in distance to _{h 0.} At this time, when h ₀ / h ₁ is taken on the horizontal axis and the liquid phase outlet side vapor phase mixing ratio is taken on the vertical axis, as shown in FIG. 7A, by setting h ₀ / h ₁ > 0.06, It is possible to further suppress the outflow of the gas phase from the liquid phase outlet pipe. Even if there is no upward projection, a practically acceptable liquid phase outlet side gas phase mixing ratio of 0.03 can be ensured, but by setting h ₀ / h ₁ > 0.06, the gas phase can be removed from the liquid phase outlet pipe. Can be further suppressed.
Note that h ₀ / h ₁ may be greater than 0.07, greater than 0.08, greater than 0.09, greater than 0.1, or the like. Further, h ₀ / h ₁ may be less than 1, less than 0.8, less than 0.6, less than 0.5, less than 0.4, less than 0.35, or the like. In the case of 0.35> h ₀ / h _1, the liquid phase outlet side vapor phase mixing ratio can be suppressed to about ½ compared to the case without protrusions.

For example, in order to satisfy h ₀ / h ₁ > 0.06, the height h ₁ of the slope is 14.5 mm, and the upward projection height h ₀ is 0.88 mm (that is, h ₀ / h ₁ > 0.06) or 5 mm (that is, h ₀ / h ₁ <0.35), the above-described upward projection effect can be obtained.
In other words, as described above, due to the upward protrusion (for example, 0.88 mm or 5 mm), the liquid phase vortex swirls around the upward protrusion. As a result, the gas phase vortex is also stably held in the center of the conical shape following the liquid phase vortex. Accordingly, the gas phase vortex does not fluctuate, does not approach the liquid phase outlet pipe inlet 6a, and does not flow out together with the liquid phase, so that the gas-liquid separation performance is not deteriorated.

Embodiment 2

Next, a second embodiment of the present invention will be described with reference to FIGS. 4, 5, 5-1, 8, 10 a, 10 b, 11, and 11-1. The second embodiment has a structure in which the liquid phase outlet pipe 6 is provided on the conical slope part 10 at the lower part of the cylindrical part.
4 is a cross-sectional view when the liquid phase outlet pipe 6 is provided on the conical slope portion 10 at the bottom of the cylindrical portion in FIG. 1-1, and the central axis of the conical shape is concentric with the central axis of the cylindrical portion 2a. 5 is an enlarged explanatory view of the main part of FIG. 4, FIG. 5-1 is a sectional view in which the liquid phase outlet pipe 6 is attached to the slope part 10 at a substantially right angle, and FIG. 8 shows the position of the liquid phase outlet pipe 6 and the liquid It is a figure which shows the relationship of the phase-outlet side gaseous-phase mixing ratio, FIG. 10a is the photograph which showed the movement of the liquid phase and gaseous phase of the liquid phase exit pipe | tube part provided with this invention, FIG. 10b is equipped with this invention. FIG. 11 is a cross-sectional view when the central axis of the conical shape is not concentric with and parallel to the central axis of the cylindrical portion 2a. FIG. 11A is a cross-sectional view in which the liquid phase outlet pipe 6 is attached to the inclined surface portion 10 at a substantially right angle. In addition, the liquid level is abbreviate | omitted similarly to FIG.
First, in FIGS. 4 and 5, the liquid phase outlet pipe 6 is provided on the slope portion 10 from which the connecting curved surface 13 is removed, and the central axis of the cylindrical portion 2a of the cylindrical container 2 and the conical center axis are concentric. In other words, an example in which the outermost lowermost point h of the slope portion 10 is provided on the substantially central axis of the cylindrical portion will be described. In the cross section including the central axis of the cylindrical portion 2a of the cylindrical container 2, the liquid phase outlet pipe 6 is provided on the slope portion 10 from which the connecting curved inner wall 13a is removed, substantially parallel to the central axis of the cylindrical portion 2a, and the previous ridgeline When the distance between X and the central axis of the conical shape, that is, the central axis of the cylindrical portion 12 is L _0, and the distance between _the previous ridge line X and the central axis of the liquid phase outlet pipe 6 is L ₁ , L ₁ / L ₀ < By managing the position of the liquid phase outlet pipe 6 from the center of the gas phase vortex, and managing the gas phase outlet side liquid phase mixing ratio as small as 0.02 or less, as shown in FIG. The liquid phase outlet side vapor phase mixing ratio can be reduced.
In the above description, the central axis of the cylindrical portion and the central axis of the conical shape are concentric. However, the same effect can be obtained if the outermost lowermost point h of the conical slope portion is on the substantially central axis of the cylindrical portion. It is done. The operational effect of the conical slope is the same as in the first embodiment.
Further, in FIG. 5, the liquid phase outlet pipe 6 is provided substantially parallel to the central axis of the cylindrical portion. However, the liquid phase outlet pipe 6 is located on the inclined surface and L ₁ / L ₀ <0.6. And may not be substantially parallel to the central axis of the cylindrical portion. That is, the same effect as in FIG. 5 can be obtained even if the angle θ formed between the slope portion inner side 10b and the central axis of the liquid phase outlet pipe 6 is an arbitrary angle. Here, when the liquid phase outlet pipe 6 is not substantially parallel to the central axis of the cylindrical portion, L _1, the center of the cylindrical part including the intersection of the central axis and the swash surface portion inside 10b of the ridgeline X and the liquid phase outlet pipe 6 This is the distance from the line parallel to the axis.
FIG. 5A is a case where the liquid phase outlet pipe 6 is provided at a substantially right angle to the inclined surface portion 10, but the same effect as in FIG. 5 can be obtained.
FIG. 8 is a diagram showing a change in the liquid phase outlet side vapor phase mixing ratio when L ₁ / L ₀ is changed in the same structure as FIG. 5 and without an upward protrusion. The test conditions in FIG. 8 are as follows.
1. The ratio of the inflowing gas phase and liquid phase is constant.
2. The gas phase side liquid phase mixing ratio is constant.
In the present invention, the liquid phase outlet side gas phase mixing ratio is set to 0.03 or less as a target value, but as is clear from FIG. 8, it is set to L ₁ / L ₀ <0.6. By this, the liquid phase outlet side vapor phase mixing ratio can be made 0.03 or less.
In addition, if L ₁ / L ₀ <0.6, the liquid phase outlet pipe can keep the gas phase outlet side liquid phase mixture ratio small in both horizontal extraction (FIG. 3) and lower extraction (FIG. 5). It was confirmed that the liquid phase outlet side vapor phase mixing ratio can be reduced.
As described above, by setting L ₁ / L ₀ <0.6, the performance of the conventional gas-liquid separator alone can be greatly improved, and of course, it is possible to reduce the size and weight. Incorporation is also improved.

FIG. 10a shows a liquid reservoir in the gas-liquid separator having the structure shown in FIG. 5 when the present invention is provided (L ₁ / L ₀ ≈0.3, ie, L ₁ / L ₀ <0.6). The state of the flow in the vicinity of 4 is shown in the photograph, and the lower end of the gas phase vortex is held near the center of the conical shape, and it can be confirmed that only the liquid phase flows out from the liquid phase outlet pipe 6.
FIG. 10b shows a liquid reservoir in the gas-liquid separator having the structure shown in FIG. 5 when the present invention is not provided (L ₁ / L ₀ ≈0.7, that is, L ₁ / L ₀ ≧ 0.6). The state of the flow around 4 is shown in the photograph, and it is confirmed that the lower end of the gas phase vortex is close to the liquid phase outlet pipe 6, is mixed with the liquid phase, and the gas phase flows out of the liquid phase outlet pipe 6. it can.

Next, in FIG. 11, when the central axis of the conical shape is not concentric and parallel to the central axis of the cylindrical portion, the liquid phase outlet pipe 6 is connected to the connection curved surface 13 as shown in FIG. An embodiment in the case where the inclined surface portion 10 is provided in parallel with the central axis of the cylindrical portion will be described.
The present embodiment is a means for easily obtaining the value of L ₁ / L ₀ <0.6 shown in FIG. 5 even when the diameter of the cylindrical container 2 becomes small, and the liquid phase outlet side vapor phase mixing ratio Is a means that can be further reduced.
Hereinafter, the present invention will be described in detail with reference to FIG. That is, when the diameter of the cylindrical container 2 is reduced in FIG. 5, it is naturally difficult to obtain L ₁ / L ₀ <0.6. At this time, for example, eccentric drawing or pressing, by using a forging, as shown in FIG. 11, if L ₂ moves away the slant portion 10 outside the lowermost point h from the liquid phase outlet pipe 6, is evident from FIG. as described above, even if the diameter of the cylindrical container 2 is small _{L 0} small _dimensions, L ₁ / L 0 <0.6 is facilitated. That, in FIG. _11, L ₁ / L 0 if defined as for <0.6, the distance between the center axis of the previous ridge X and the cylindrical portion 2a _{L 0,} the previous ridge X and the liquid phase outlet L _{1 is} the short side of the distance from the central axis of the tube 6, and L ₂ is the distance between the line segment parallel to the central axis of the cylindrical portion including the outermost lowermost point h of the conical slope and the central axis of the cylindrical portion 2 a. , L ₁ / (L ₀ + L ₂ ) <0.6, and in the same way as L ₁ / L ₀ <0.6, the position of the liquid phase outlet pipe 6 is further increased from the center of the gas phase vortex. It can be further separated, the liquid phase outlet side gas phase mixing ratio can be further reduced, and the outflow of the gas phase to the liquid phase outlet pipe can be suppressed.
Even if the diameter of the cylindrical container 2 is not necessarily small, it is clear that the above-described effect can be obtained if L ₁ / (L ₀ + L ₂ ) <0.6. _{L 1 / (L 0 + L} 2) may be less than 0 to 0.6, such as less than 0.55, less than 0.5, less than 0.45, may be such as less than 0.4.
Further, in the above description, _{L 2} is, for example, a 1/4 to 1/2 of 1/5 to 1/2, _{L 0} of _{L 0,} practically, 1 / 3-1 of the _{L 0} / 2 is preferable.
In the above description, the conical central axis is not concentric with and parallel to the central axis of the cylindrical portion. Naturally, the conical central axis may be parallel to the central axis of the cylindrical portion. Good.
FIG. 11 shows an embodiment in which the liquid phase outlet pipe 6 is substantially parallel to the central axis of the cylindrical portion, but the liquid phase outlet pipe 6 is substantially perpendicular to the inclined surface portion 10 as shown in FIG. It may be provided. Furthermore, the liquid phase outlet pipe 6 may be on the inclined surface and L ₁ / (L ₀ + L ₂ ) <0.6, and may not be substantially parallel to the central axis of the cylindrical part. That is, the same effect as in FIG. 11 can be obtained even if the angle θ formed between the slope portion inner side 10b and the central axis of the liquid phase outlet pipe 6 is an arbitrary angle.
11 and 11-1, the central axis of the cylindrical portion and the conical shape of the cylindrical portion described above (FIGS. 5 and 5-1) except that the central axis of the cylindrical portion and the central axis of the conical shape are not concentric. This is the same structure as the case where the central axis of the cylindrical portion is concentric, and the operational effect is also the same as the case where the central axis of the cylindrical portion and the central axis of the conical shape are concentric.

Embodiment 3

Next, the shape of the protrusion produced by a different formation method from that of Embodiment 1 (FIGS. 1-1 and 3) will be described with reference to FIG.
This embodiment is a gas-liquid separation device in which upward protrusions are formed integrally with a cylindrical container. For example, when forming the slope portion 10 by forging or pressing, the upward protrusions 11 are formed integrally at the same time. is there. According to this example, there is no need for brazing as in the first embodiment (FIG. 3), so it is possible to reduce the number of components and processing steps, and the dimensional accuracy is good, so that mass production is excellent. It becomes.
The above configuration is the same as that of the first embodiment (FIG. 3) except that the processing method is different, and the shape and function and effect on the liquid reservoir 4 side are the same as those in FIG. Therefore, the same effect as in the first embodiment can be obtained.
The protrusion shape may be a mountain-shaped protrusion shape or a hook-shaped protrusion shape in addition to D, E, and FIG. 12 in FIGS.

Embodiment 4

  FIG. 13 is a configuration diagram of a refrigeration cycle when the gas-liquid separator described above is used in a refrigeration cycle. The refrigeration cycle configuration diagram shown in FIG. 13 shows basic components necessary for explaining the present embodiment. That is, the compressor 18 has only the first cylinder 19, and the low-temperature and low-pressure gas-phase refrigerant sucked in by the compressor is compressed by the first cylinder 19 to become a high-temperature and high-pressure gas-phase refrigerant and is condensed through the refrigerant discharge pipe 20. The heat is dissipated to the air sent by the condenser blower 22 in the condenser 21 to become a high-pressure liquid refrigerant. The liquid refrigerant is decompressed by the first decompressor 23 to become a two-phase flow and flows into the gas-liquid separator 1 from the two-phase inlet pipe 7, and the liquid refrigerant enters the evaporator 24 from the liquid-phase outlet pipe 6 and evaporates. Heat is taken from the air sent by the blower 25 for equipment and becomes a low-temperature and low-pressure gas-phase refrigerant, which is sucked into the compressor 18. On the other hand, the gas-phase refrigerant separated by the gas-liquid separator is sucked into the compressor 18 from the gas-phase outlet pipe 9 through the evaporator bypass pipe 26.

When the gas-liquid separation device 1 is not used, the two-phase gas-phase refrigerant decompressed by the decompressor 23 also flows into the evaporator. Therefore, when the air temperature sent by the evaporator blower 25 is low, the evaporation pressure Since the density of the gas-phase refrigerant decreases and the volume flow rate increases, the pressure loss in the evaporator 24 increases and the outlet pressure of the evaporator 24, that is, the compressor suction pressure decreases, and the compression power increases. However, highly efficient operation cannot be performed.
On the other hand, the gas-liquid separation device 1 is provided as shown in the present embodiment, and the separated gas-phase refrigerant is sucked into the compressor 18 from the gas-phase outlet pipe 9 through the evaporator bypass pipe 26, thereby cooling. Since the gas-phase refrigerant that contributes very little to the evaporator 24 does not flow into the evaporator 24, pressure loss in the evaporator 24 can be suppressed, compression power can be reduced, and highly efficient operation can be achieved.

Embodiment 5

  FIG. 14 is a refrigeration cycle configuration diagram different from FIG. 13 when the gas-liquid separator is used in the refrigeration cycle. FIG. 14 shows an example of a separate type air conditioner, which includes an outdoor unit 27 and an indoor unit 28, and shows a cycle during cooling operation. Refrigerating machine oil is mixed in the high-temperature and high-pressure gas-phase refrigerant compressed by the compressor 18, and when the amount of refrigerating machine oil mixed in the gas-phase refrigerant discharged from the compressor increases, the pressure loss of the refrigeration cycle refrigerant flow path increases. In addition, the evaporative heat transfer coefficient and the condensation heat transfer coefficient are decreased, causing a decrease in the efficiency of the refrigeration cycle. Furthermore, when the compressor is started, the refrigerating machine oil enclosed in the compressor forms, and a large amount of the refrigerating machine oil is mixed into the gas phase refrigerant and discharged from the compressor, and flows out to the refrigerating cycle. In particular, in the case of a separate type air conditioner, a connecting pipe for connecting the indoor unit and the outdoor unit is provided. When this connecting pipe 34 is long, the refrigerating machine oil that has flowed into the refrigeration cycle does not return to the compressor for a long time. Depending on the operating conditions, there is a problem that the compressor oil in the compressor is insufficient and the reliability of the compressor is hindered.

  Therefore, in order to solve the above problems, FIG. 14 provides a compact gas-liquid separation device 1 in the refrigerant discharge pipe of the compressor 18 to improve the refrigeration cycle efficiency and ensure the reliability of the compressor. That is, the low-temperature and low-pressure gas-phase refrigerant sucked in by the compressor 18 is compressed by the compressor 18 to become a high-temperature and high-pressure gas-phase refrigerant, passes through the compressor discharge pipe, and is separated from the two-phase inlet pipe 7 of the gas-liquid separator 1. Flows into the device. The high-temperature and high-pressure gas-phase refrigerant compressed by the compressor 18 is mixed with refrigerating machine oil, and the refrigerating machine oil is separated as a liquid phase and the gas-phase refrigerant is separated as a gas phase in the gas-liquid separation device 1. It is taken out from the pipe 6 and the gas phase outlet pipe 9. The refrigerating machine oil that has exited the liquid phase outlet pipe 6 passes through the liquid receiver 30 and the flow rate adjusting throttle 31, and is sucked into the compressor suction pipe 32, and the refrigerating machine oil returns to the compressor. The reason why the flow rate adjusting throttle 31 is provided is that, under normal operating conditions, the amount of refrigerating machine oil mixed in the high-temperature and high-pressure gas-phase refrigerant discharged from the compressor 18 is smaller than that in the gas-phase refrigerant. This is because the refrigeration oil separated in step (3) is gradually returned to the compressor 18 by the flow rate adjusting throttle 31. The reason why the liquid receiver 30 is provided is that the refrigerating machine oil enclosed in the compressor is formed at the time of starting the compressor, and a large amount of refrigerating machine oil is mixed in the gas phase refrigerant and discharged from the compressor. This is a temporary phenomenon, so that the refrigerating machine oil separated by the gas-liquid separator 1 is temporarily stored, and the refrigerating machine oil is gradually returned to the compressor 18 by the flow rate adjusting throttle 31.

  On the other hand, the gas-phase refrigerant separated in the gas-liquid separation device 1 radiates heat to the air sent from the condenser blower 22 through the four-way valve 33 from the gas-phase outlet pipe 9, and becomes high-pressure liquid refrigerant. The liquid refrigerant is decompressed by the first decompressor 23 to become a low-temperature and low-pressure two-phase flow, takes heat from the air that enters the evaporator 24 and is sent by the evaporator blower 25, and becomes a low-temperature and low-pressure gas-phase refrigerant. Inhaled. Therefore, the refrigerating machine oil is separated as a liquid phase in the gas-liquid separation device 1 and is sucked into the compressor suction pipe 32 through the liquid receiver 30 and the flow rate adjusting throttle 31 from the liquid phase outlet pipe 6, and the refrigerating machine oil enters the compressor. Because it returns, it is possible to prevent refrigeration oil from flowing into the refrigeration cycle, enabling highly efficient refrigeration cycle operation, and also preventing refrigeration oil from flowing into the refrigeration cycle even at start-up, so that reliable operation is possible. Is possible.

Embodiment 6

FIG. 15 is a system diagram showing an example in which the gas-liquid separator is applied to a mechanical device that handles a gas-liquid two-phase flow.
Specifically, FIG. 15 shows an air purifier, which removes dirt components such as odor components and fine particle components mixed in the air to obtain clean air. Dirty air 35 containing odorous components and fine particle components is sent to a dirt adsorption chamber 37 by a blower 36. On the other hand, adsorbed water 39 is sent from the pump 38 to the nozzle 40, and fine water droplets 41 are sprayed from the nozzle 40 into the dirt adsorbing chamber 37. The fine water droplet 41 adsorbs the odor component and fine particle component of the dirty air sent to the dirt adsorption chamber 37, falls downward and is taken out from the drain pipe 42. On the other hand, the purified air is taken out from the air take-out unit 43, and the air contains a large number of fine water droplets 41. Therefore, purified air containing a large number of fine water droplets is introduced into the gas-liquid separation device 1 from the two-phase inlet pipe 7 of the gas-liquid separation device 1 to separate the fine water droplets 41, and the fine water droplets are liquid. Take out from the phase outlet pipe 6. On the other hand, the purified air excluding the fine water droplets is taken out from the gas phase outlet pipe 9. Therefore, the gas phase component can be efficiently extracted by using the gas-liquid separation device of the present invention.

  The gas-liquid separators of the fourth embodiment and the fifth embodiment described above are devised based on findings from experiments using refrigerant HFC-32 and refrigeration oil. It can also be applied to HFC refrigerants, HFO refrigerants, and natural refrigerants. Further, the gas-liquid separation device of the sixth embodiment is an example of a two-phase air-water flow, but can also be applied to a general two-phase flow consisting of a gas phase and a liquid phase.

By incorporating the gas-liquid separation device of the present invention into a refrigeration device such as an air conditioner, a refrigeration device equipped with gas injection, a steam cycle device, or a mechanical device that handles gas-liquid two-phase flow, it is efficient and reliable. An improved low-cost refrigeration apparatus, steam cycle apparatus, and mechanical apparatus that handles a gas-liquid two-phase flow can be obtained.
In addition to the air purification device of the sixth embodiment, the mechanical device that handles the two-phase flow includes a device that separates water mixed in exhaust gas (such as nitrogen), such as a fuel cell, and waste by supercritical water. A device that separates product gas from oil and water, such as a plastic oil refiner, a device that separates product gas (such as methane) and water, such as a biogas production device that uses supercritical water, and an ozone water generator that uses electrochemistry. Thus, an apparatus for separating hydrogen and water produced at the cathode is included.

1 Gas-liquid separator
2 cylindrical container 2a cylindrical part 2b cylindrical part inner wall
3 Gas-liquid separation chamber 4 Liquid reservoir
5 Solid line liquid surface 5a Broken line liquid surface 6 Liquid phase outlet pipe 6a inlet 7 Two-phase inlet pipe 8 Gas phase vortex tip 9 Gas phase outlet pipe 10 Slope portion 10b Slope portion inner side 11 Upward projection 11a Brazing material 12 Cylindrical lower end 13 Connection curved surface 13a Connection curved inner wall 18 Compressor 19 First cylinder 20 Refrigerant discharge pipe 21 Condenser 22 Condenser blower 23 First decompressor 24 Evaporator 25 Evaporator blower 26 Evaporator bypass pipe 27 Outdoor unit 28 Indoor unit 29 Refrigerant discharge pipe 30 Liquid receiver 31 Flow rate adjusting throttle 33 Four-way valve 34 Connection pipe 35 Dirty air 36 Blower 37 Dirty adsorption chamber 38 Pump 39 Adsorbed water 40 Nozzle 41 Fine water droplet 42 Drain pipe 43 Air outlet 51 Gas-liquid separator 51a Inner peripheral wall 52 container 52a bottom wall 53 two-phase flow inlet 54 gas-phase outlet pipe 55 liquid-phase outlet pipe 55a inlet 56 liquid level 57 Cause

Claims (10)

A swirl force is applied to the two-phase flow introduced into the cylindrical vessel from the two-phase flow inlet pipe, the gas and liquid are separated by centrifugal force, the gas phase is from the gas phase outlet pipe, and the liquid phase is from the liquid phase outlet pipe. In the gas-liquid separator designed to flow out,
A downward cone-shaped slope portion having an apex angle of 120 degrees or less in the cross section including the central axis of the cylindrical portion at the lower end of the cylindrical portion of the cylindrical container and having the slope portion outermost lowermost point h on the substantially central axis of the cylindrical portion is formed. And a liquid phase outlet pipe is provided at the position of the slope portion from which the connection curved surface provided between the slope portion and the cylindrical portion of the cylindrical container is removed, and
In the cross section including the central axis of the cylindrical portion, the ridge line between the inner wall of the cylindrical portion and the inner wall of the connecting curved surface is X, the distance between the ridge line X and the central axis of the cylindrical portion is L ₀ , the ridge line X and the liquid phase outlet pipe L ₁ / L ₀ <0.6, where L ₁ is the distance between the central axis of the cylindrical portion and the line segment parallel to the central axis of the cylindrical portion including the intersection of the slope portion inside Gas-liquid separator. A swirl force is applied to the two-phase flow introduced into the cylindrical vessel from the two-phase flow inlet pipe, the gas and liquid are separated by centrifugal force, the gas phase is from the gas phase outlet pipe, and the liquid phase is from the liquid phase outlet pipe. In the gas-liquid separator designed to flow out,
A downward-cone-shaped inclined surface portion having a vertical angle of 120 degrees or less in a cross section including the central axis of the cylindrical portion at the lower end of the cylindrical portion of the cylindrical container and having an outermost lowermost point h on the inclined surface portion in addition to the substantially central axis of the cylindrical portion. At the position of the inclined surface portion formed by removing the connecting curved surface provided between the inclined surface portion and the cylindrical portion of the cylindrical container, and opposite to the lowermost point h outside the inclined surface portion with respect to the central axis of the cylindrical portion A liquid phase outlet pipe is provided at the position of the slope portion on the side, and
In the section including the center axis of the cylindrical portion, the ridge line of the cylindrical inner wall and the connecting curved inner wall and X, the distance between the center axis of the ridge line X and the cylindrical portion and L _0, the slope portion outer lowermost point h center of the cylindrical part including the distance between the center axis of the parallel line segments and the cylindrical portion to the central axis of the cylindrical portion and L _2, and the ridge line X, the intersection between the central axis and the swash surface inside the liquid outlet pipe comprising A gas-liquid separation device characterized in that L ₁ / (L ₀ + L ₂ ) <0.6, where L ₁ is the short side of the line parallel to the axis. A swirl force is applied to the two-phase flow introduced into the cylindrical vessel from the two-phase flow inlet pipe, the gas and liquid are separated by centrifugal force, the gas phase is from the gas phase outlet pipe, and the liquid phase is from the liquid phase outlet pipe. In the gas-liquid separator designed to flow out,
A curved surface provided between the inclined surface portion and the cylindrical portion of the cylindrical container is formed at the lower end of the cylindrical portion of the cylindrical container with a downward conical inclined surface portion having an apex angle of 120 degrees or less in a cross section including the central axis of the cylindrical portion. A liquid phase outlet pipe is provided at the lower end of the cylindrical portion, and
In the cross section including the central axis of the cylindrical portion, the ridgeline between the inner wall of the cylindrical portion and the inner wall of the connecting curved surface is X, and the lower end of the outer diameter of the liquid phase outlet pipe provided at the lower end of the cylindrical portion excluding the ridgeline X and the connecting curved surface L / d <2.5, where L is the distance between the liquid phase outlet tube and d is the inner diameter of the liquid phase outlet pipe.   The gas-liquid separation device according to claim 1, wherein a protrusion is provided on the inside of the lowermost end of the slope portion at the lower end of the cylindrical portion of the cylindrical container.   5. The gas-liquid separator according to claim 4, wherein the protrusion formed on the innermost lower end of the slope portion is formed integrally with the cylindrical container.   5. The gas-liquid separation device according to claim 4, wherein the protrusion formed on the inner side of the lower end of the slope portion is formed by raising a brazing material sealing the tip of the slope portion of the cylindrical container on the inner side of the lower end of the slope portion. . In the cross section including the central axis of the cylindrical portion of the cylindrical container, the ridgeline between the cylindrical portion inner wall and the connecting curved inner wall is X, and the plane perpendicular to the central axis of the cylindrical portion including the ridgeline X and the lower end of the cylindrical portion of the cylindrical container The distance from the slope innermost point h _in is h _1, and the plane perpendicular to the central axis of the cylindrical portion including the apex of the upward projection and the slope inner lower point h _in at the lower end of the cylindrical portion of the cylindrical container The gas-liquid separation device according to claim 4, wherein h ₀ / h ₁ > 0.06 when the distance is h ₀ .   The gas-liquid separator according to any one of claims 1 to 7 is disposed between a compressor discharge pipe and a condenser of a refrigeration cycle, and the compressor discharges into a two-phase inlet pipe of the gas-liquid separator. Connect the pipe, connect the liquid-phase outlet pipe of the gas-liquid separator to the compressor suction pipe through the flow rate adjusting throttle, and connect the gas-phase outlet pipe of the gas-liquid separator to the pipe leading to the condenser. Refrigeration equipment characterized.   The gas-liquid separator according to any one of claims 1 to 7 is arranged between a decompressor and an evaporator of a refrigeration cycle, and the decompressor outlet pipe is a two-phase inlet pipe of the gas-liquid separator. A refrigeration apparatus comprising: a liquid phase outlet pipe connected to an evaporator inlet; and a gas phase outlet pipe bypassed the evaporator and then connected to a compressor suction pipe.   A fluid machine device comprising the gas-liquid separation device according to any one of claims 1 to 7 and separating a gas-liquid two-phase flow into a gas phase and a liquid phase.