KR20090081320A - Gas-liquid separator and refrigerating apparatus equipped therewith - Google Patents

Abstract

A gas-liquid separator and a freezing apparatus including the same are provided to capture the liquid carried with the vapor. A freezing apparatus comprises a groove formation body(4), a gas-liquid separation room(1) and a gas-liquid separator. The groove formation body has a groove, facing a liquid outlet pipe, at one side of the gas-liquid separation room. An outer block body and an opening dividing body make a small place at the upper stream of the gas-liquid separation. Gas-liquid two phases flowing through the outer block body is induced to the gas-liquid separation room after passes through the small place from the groove formation body. The liquid phase is introduced to a liquid outlet pipe(7) through the groove formation body. The gas is introduced to a gas outlet pipe from the gas-liquid separation room.

Description

Refrigeration apparatus with gas-liquid separator and gas-liquid separator {GAS-LIQUID SEPARATOR AND REFRIGERATING APPARATUS EQUIPPED THEREWITH}

TECHNICAL FIELD This invention relates to the gas-liquid separator and oil separator of heat engines, such as a refrigeration cycle and a steam cycle, for example. Specifically, It is related with the technique which further aims at high performance and a miniaturization.

For example, as the gas-liquid separator and oil separator used in the refrigeration cycle, a tank for storing the liquid or oil by gravity is used, or the liquid or oil is attached to the outer wall by the centrifugal force of the swirling flow, Or gas-liquid separation apparatus etc. which collect | recover oil are used.

In the gas-liquid separator and the oil separator having such a configuration, the liquid-liquid having a high density is separated basically by volume force such as gravity or centrifugal force. For this reason, since it uses a tank and a swirl flow generating apparatus, it is a large apparatus, and there is little freedom in the installation position and direction of a gas-liquid separation apparatus. Moreover, the means which isolate | separated gas liquid efficiently was not provided.

Therefore, firstly, the inventors have applied for a patent of the invention for the purpose of making the gas-liquid separation device more efficient and downsizing by allowing the liquid phase to adhere to the grooves by the action of surface tension in the grooves in order to solve the above problems. It was.

[Patent Document 1] International Patent Application No .: PCT / JP2006 / 322682

In the conventional gas-liquid separator and the oil separator, since the liquid (oil) having a high density is separated by volume force such as gravity or centrifugal force, it is necessary to set the radius of curvature and the flow rate so that the volume force is dominant. The necessity of matching the installation direction with the gravity direction was necessary.

These require a tank having a height secured in the direction of gravity, or increase the flow velocity when using centrifugal force. In addition, in order to generate a curved flow, it is necessary to change the direction of the flow by a partition plate or the like. For this reason, pressure loss tends to be large, and in order to prevent it, the apparatus becomes large and it was difficult to miniaturize.

In order to reduce the size of the gas-liquid separator, it is necessary to increase the flow velocity and decrease the radius of curvature. However, as the size of the gas-liquid separator is reduced, the effects of viscous force and surface tension on the volume force such as centrifugal force and gravity cannot be ignored. There existed a problem that the refrigerating cycle performance fell because the characteristic of the apparatus itself fell, or a pressure loss became large.

The present invention further develops PCT / JP2006 / 322682, which has been filed previously, and utilizes the surface tension effect to carry out the gas-liquid separation device and the oil separator, which are aimed at making the gas-liquid separation device more efficient and smaller. Provides high performance and compact gas-liquid separators and oil separators capable of capturing droplets, and the gas-liquid separators also include refrigeration units such as air conditioners, refrigerators, freezers, dehumidifiers, shokes, vending machines, and car air conditioners. It is proposed to employ a back.

There are two ways to consider the maximum amount of droplets transported in the weather, the first being the means of capturing the maximum droplets in the grooves, and the second is the flow of water from the meteorological exit pipe even if the droplets exit from the grooves in the weather. It is a means to make a difficult structure. These means will be described below.

In the invention according to claim 1, the liquid phase outlet pipe is formed on the upper portion of the gas-liquid separation device so that the droplet is hardly leaked from the gas phase outlet pipe even if the liquid droplet is discharged from the groove in the gas phase after the maximum trapping of the droplet in the groove. The lower portion of the gas phase outlet pipe is connected to the upper portion of the inlet partition in fluid communication, and the entire gas-liquid separation chamber cross-sectional area is used as the axial gas phase rise passage.

The invention as set forth in claim 2 provides a gas-liquid separator and an oil separator of a suitable specification for trapping droplets in a groove for required operating conditions and refrigerant flow rates. In order to capture the droplet, an inclined substantially wave shape is formed in the groove forming body.

According to the invention of claim 3, in order to generate a strong secondary flow to trap the droplets in the grooves, and to drop the trapped droplets by the effect of the centrifugal force by using the shear force and gravity of the flow, the surface of the groove forming body The substantially wave shape inclined in the flow direction formed in the groove is formed so as to widen radially outward in the direction of the flow.

According to the invention of claim 4, the surface of the groove forming body is generated so as to generate a strong secondary flow in order to trap the droplet in the groove, and to cause the droplet captured by the effect of the centrifugal force to flow down using the shear force and gravity of the flow. An approximately wave shape inclined in the flow direction formed in the groove is formed to have a wide end portion in the flow direction.

Invention of Claim 5 is the gas-liquid separation apparatus of Claim 2, Comprising: The division cylinder was provided also in the inside of the groove formation body so that the two phase flow which flows inside the groove formation body may not escape to radial inside. do.

The invention according to claim 6 is the gas-liquid separation device according to claim 2, and in order to capture the droplets in the grooves, the length L of the groove forming body, the pitch p of the groove forming body, the mainstream velocity u flowing through the groove forming body, and the droplet diameter d , gas phase viscosity coefficient μ _G , gas phase density ρ _G , liquid phase density ρ _L ,

Characterized in that.

The invention according to claim 7 has an angle with respect to the centerline of the outer periphery in order to capture the droplet as much as possible in the groove and to make it difficult for the droplet to flow out of the gas phase outlet pipe even if the droplet flows out of the groove in the gas phase. It is characterized by forming the inclined α.

The invention as set forth in claim 8 provides a gas-liquid separator and an oil separator of a suitable specification for trapping droplets in a groove for a required operating condition and a refrigerant flow rate. In order to capture a droplet, the inclined substantially wave shape was formed in the groove formation body. It is characterized by the above-mentioned.

The invention as set forth in claim 9 provides a gas-liquid separator and an oil separator of a suitable specification for trapping droplets in a groove for a required operating condition and a refrigerant flow rate. In order to capture the droplet, an inclined substantially wave shape is formed in the groove forming body.

The invention as set forth in claim 10 is configured to angle the groove with respect to the centerline of the outer periphery in order to capture the droplet as much as possible within the groove and to make it difficult for the droplet to flow out of the gas phase outlet pipe even if the droplet flows out of the groove in the gas phase. It is characterized by forming the inclined α.

Invention of Claim 11 built-in the gas-liquid separator of any one of Claims 1-10 in refrigeration cycles, such as an air conditioner, The refrigeration apparatus provided with the gas-liquid separator.

Invention of Claim 12 connects the outlet pipe of the pressure reducer in a refrigerating cycle, to the two-phase inlet pipe of the gas-liquid separator of any one of Claims 1-10, and connects the liquid outlet pipe of a gas-liquid separator to an evaporator. And a gaseous outlet pipe of the gas-liquid separator is connected to the suction pipe of the compressor via a bypass and a resistance regulator.

According to the invention described in claim 13, the compressor discharge pipe in the refrigerating cycle is connected to the two-phase inlet pipe of the gas-liquid separator according to any one of claims 1 to 10, and the flow-through adjustment of the liquid outlet pipe of the gas-liquid separator is performed. It is a refrigeration apparatus characterized by connecting to the compressor suction pipe via the shaft part, and connecting the gas-phase outlet pipe of the gas-liquid separator to the conduit which leads to the condenser of a refrigeration cycle.

According to the gas-liquid separation apparatus of Claim 1, a gaseous-phase outlet tube is installed in the upper part of a gas-liquid separator, and the lower part of a gas-phase outlet tube is connected to the upper part of an inlet compartment in fluid communication, and a gas-phase outlet tube is a gas-liquid separation chamber. Since the whole inside diameter Dt of a groove top point virtual circle becomes an axial gas phase rise flow path in a gas-liquid separation chamber, the gas phase rise rate u _a falls and a droplet falls easily downward. Therefore, the droplets are less likely to flow out of the gas phase outlet pipe, thereby providing a high performance gas-liquid separation device.

According to the gas-liquid separation device according to Claims 2, 8, and 9, by forming a substantially wave shape having an inclination angle on the surface of the groove forming body, a strong secondary flow can be generated in the space fitted into the groove forming body. Moreover, since this secondary flow becomes a flow in the very narrow space which fits in the groove formation body, the curvature radius of the streamline can be made very small. Thereby, very strong centrifugal force can be exerted on a droplet. In addition, by compactly mounting the surface area of the groove-forming body per volume of the gas-liquid separation device, the droplet trapping area per volume can be increased, thereby making it possible to constitute a very compact gas-liquid separation device.

According to the gas-liquid separator according to claim 3, by forming a substantially wave shape inclined in the flow direction formed on the surface of the groove forming body so as to widen radially outward in the direction of flow, a strong secondary flow is generated, The droplet captured by the effect can be effectively lowered on the wall by using the shear force and gravity of the flow without scattering again as the droplet.

According to the gas-liquid separation device according to claim 4, by forming an approximately wave shape inclined in the flow direction formed on the surface of the groove forming body at the end in the direction of the flow, a strong secondary flow is generated and the effect of the centrifugal force is increased. The captured droplets can be effectively lowered on the wall by using the shear force and gravity of the flow without scattering them again as droplets.

According to the gas-liquid separation device according to claim 5, the partition cylinder is also provided inside the groove forming body so that the droplets collide effectively with the groove forming wall without causing the two-phase flow flowing inside the groove forming body to exit radially inward. Can be captured.

According to the gas-liquid separator according to claim 6, the length L of the groove forming body, the pitch p of the groove forming body, the mainstream velocity u flowing through the groove forming body, the droplet diameter d , the gas phase viscosity coefficient μ _G , the gas phase density ρ _G , the liquid phase density When ρ _L

By doing so, it is possible to secure a secondary flow and a capture distance of sufficient strength to capture the droplets.

According to the gas-liquid separation device according to claim 7, the following three effects are obtained by forming the groove at an angle α inclined with respect to the centerline of the outer body. The first effect is smaller than the groove width b when the groove width b 'is not inclined by tilting the groove. When the gaseous phase flows in the grooves, droplets carried in the gaseous phase easily collide with the surface of the grooves to become liquid films as the width of the grooves decreases, so that the gas-liquid separation performance can be improved by tilting the grooves to reduce the actual groove width. The second effect is that the flow direction of the gaseous phase coming out of the grooves flows into the gas-liquid separation chamber at an angle α by tilting the grooves at angle α. Therefore, since the gaseous phase flows into the gas-liquid separation chamber from all the grooves opened in the gas-liquid separation chamber, swirl flow occurs in the gas-liquid separation chamber. The microdroplets discharged from the groove by the gaseous phase are easily collected in the space in the gas-liquid separation chamber close to the opening of the groove by the action of the centrifugal force due to the swirl flow, and the probability of the microdroplets being combined with each other to be larger is increased. . If the droplet diameter d becomes large, it will fall easily. Therefore, the droplets are less likely to flow out of the gas phase outlet pipe 6, thereby providing a high-performance gas-liquid separation device. The third effect is that the groove depth h 'in the vertical direction with respect to the groove bottom is smaller than the groove depth h when the groove is not inclined by tilting the groove while the substantial length h of the groove is constant. Therefore, by tilting the groove, the diameter Dt of the groove peak virtual circle becomes substantially large. Therefore, the axial gas phase ascending velocity u _a in the gas-liquid separation chamber decreases, and the droplets easily fall downward. Therefore, the droplets are less likely to flow out of the gas phase outlet pipe, thereby providing a high performance gas-liquid separation device.

According to the refrigeration apparatus of Claim 11, 12, in addition to the effect of Claim 1 thru | or 10, the pressure loss in an evaporator can be suppressed, it is possible to reduce compression power and enable high efficiency operation. It can provide a refrigeration apparatus that can be.

According to the refrigeration apparatus of Claim 13, since the effect of Claims 1-10 is acquired and the outflow of the refrigeration oil to a refrigeration cycle can be prevented, the refrigeration apparatus which can enable high efficiency and high reliability operation is provided. can do.

EMBODIMENT OF THE INVENTION Hereinafter, the specific embodiment which applied this invention is described in detail, referring drawings.

"First embodiment"

1 is a cross-sectional view showing the gas-liquid separation device of the first embodiment. FIG. 2 is a sectional view taken along the line A-A of the gas-liquid separator shown in FIG. FIG. 3 is an exploded perspective view of the groove forming body 4 formed by bending the thin plate, and FIG. 4 is an enlarged view when one pitch of the groove forming body 4 of FIG. 3 is taken out. As shown in Fig. 1, a groove forming body 4 having a groove 2 facing the liquid outlet tube 7 is provided in the outer casing 10, and an inlet partition body is located upstream of the groove forming body 4. (16) is provided and constitutes the gas-liquid separation chamber (1). As shown in FIG. 3, the groove forming body 4 is bent into a thin plate to form the groove 2, and is rounded and inserted into the outer body 10 as shown in FIG. Downstream of the groove forming body 4, the gas phase outlet pipe 6 is surrounded by an outlet partition 8 joined to the gas phase outlet pipe 6 so as to define a lower position in the height direction of the groove forming body 4. (10) It is joined to the lower shaft pipe part 13.

The gas-liquid two-phase flows in from the inlet pipe 5 and into the narrow space 12 made up with the inlet partition 16 and the outer shell B 11. The gas-liquid two-phase flows into the groove along the groove because the gas-liquid two-phase flows along the groove 2 in the narrow space 12 formed with the inlet partition 16. The two-phase liquid phase introduced into the groove-forming body 4 basically adheres to the surface of the groove 2 to form a liquid film. In addition, the droplets carried in the gas phase collide with the surface of the groove 2 to form a liquid film. The liquid film flows downward and flows out from the liquid outlet pipe 7. The gaseous phase from which the droplets have been removed flows out of the gas phase outlet pipe 6.

Here, an approximately wave shape inclined in the mainstream direction as shown in FIG. 4 is formed on the surface of the groove forming body 4. This substantially wave shape is formed so that it may spread radially outward in the direction of a flow. Due to this inclined substantially wave-shaped effect, the secondary flow 20 in the cross section as shown in FIG. 10 is generated inside the groove 2. When the droplets 14 conveyed in the gas phase flow therebetween, the droplets rotate in the cross section by the secondary flow 20 and collide with the groove forming body 4 by the effect of the centrifugal force acting at that time. . The collided droplet 14 becomes a liquid film on the surface of the groove forming body, and falls downward along the substantially wave shape by the shear force and gravity of the mainstream. In this way, the liquid droplets in the gas phase can be gas-liquid separated.

In addition, since the generated secondary flow becomes a flow in a very narrow space in the groove of the groove forming body, the curvature radius of the streamline is also very small. Thereby, very strong centrifugal force can be exerted on a droplet. In addition, since the surface area of the groove-formed body per volume of the gas-liquid separator can be compactly mounted, the droplet trapping area per volume can be increased, and a very compact gas-liquid separator can be constituted.

"2nd embodiment"

5 is a cross-sectional view showing the gas-liquid separation device of the second embodiment. FIG. 6 is an exploded perspective view of the groove forming body 4 formed by bending the thin plate, and FIG. 7 is an enlarged view when one pitch of the groove forming body 4 of FIG. 3 is taken out. This substantially wave shape is wide in the end in the direction of flow.

Here, an approximately wave shape inclined in the mainstream direction is formed on the surface of the groove of the groove forming body 4 as shown in FIG. This substantially wave shape is wide in the end in the direction of flow. Due to this inclined substantially wave-shaped effect, the secondary flow 20 in the cross section as shown in FIG. 10 is generated inside the groove 2. When the droplets 14 conveyed in the gas phase flow therebetween, the droplets rotate in the cross section by the secondary flow 20 and collide with the groove forming body 4 by the effect of the centrifugal force acting at that time. The collided droplet 14 becomes a liquid film on the surface of the groove forming body, and falls downward along the substantially wave shape by the shear force and gravity of the mainstream. In this way, the liquid droplets in the gas phase can be gas-liquid separated.

"Third embodiment"

8 is a cross-sectional view showing the gas-liquid separation device of the third embodiment. In the third embodiment, as shown in Fig. 9, a partition cylinder 37 is provided between the groove forming body 4 and the gas-liquid separation chamber 1. The gas-liquid two-phase flow which flows in the groove formation body 4 by the partition cylinder 37 can flow until it reaches below the groove formation body 4, without escaping to the gas-liquid separation chamber 1. Thereby, the distance required in order for a droplet to collide with the wall surface of a groove formation body can be ensured enough. The gaseous phase which reaches below the groove formation body 4 flows into the gas-liquid separation chamber 1 from the communication hole 22 formed in the outlet partition 8, and flows out from the gaseous-phase outlet pipe 6.

Hereinafter, the phenomenon until a droplet collides with a wall surface is considered. As the first approximation, a model as shown in FIG. 11 is considered. Consider the balance between the centrifugal force acting on the droplet 14 of diameter d rotating at the radius r ₀ and the radial drag from the gas phase acting on the droplet. If the radial velocity of the droplet is u _r and the peripheral velocity is u _l , the balance between centrifugal force and drag is expressed by the following equation.

Here, since the droplet is small, the drag coefficient is left as follows.

The radial velocity u _r is obtained from the equations (1) and (2) as follows.

Consider the following integration here. Note that u _r = dr / dt ,

It becomes Where T is the time the droplet travels from r ₀ to r ₀ + h , ie the flight time required for the droplet to hit the wall. Integrating Equation 4,

Is obtained. Therefore, the flight time T until the droplets hit the wall is

Becomes

The mainstream speed u × flight time T is the flow direction flight distance of the droplets required until the droplets collide with the wall surface, and this becomes the required length L of the groove forming body of the gas-liquid separation device.

Let's apply this model to the groove forming body of FIG. As the secondary flow, a pair of vortex pairs are formed between the groove pitches, and the radius r ₀ of the vortex is a times the groove forming pitch p,

Suppose Further, suppose that the distance between the streamline of the vortex and the wall of the groove-former is h , and this can be described as follows using the above-described vortex radius r ₀ and the groove-former pitch p.

This is based on the assumption that a pair of vortex pairs of radius r ₀ are formed between the groove forming body pitch p as shown in FIG.

Also assume that the radial velocity u _l of the vortex is b times the mainstream velocity u . In other words,

Substituting Equations 7-9 into Equation 6 yields a flight time T until the droplets collide with the wall surface and multiplies it by the mainstream velocity u to capture the droplet's flight distance, i.e. The length L of the groove | channel formation required in order is calculated | required as follows.

By modifying equation (10), the following equation is obtained.

Fig. 12 shows changes in the value on the right side of the equation (11) when the values of the coefficients a and b are changed. The intensity of the secondary flow induced by the inclined substantially wave shape of the present invention can be considered to be about 0.05 ≦ b ≦ 0.3. Moreover, since a pair of vortex pairs per pitch of groove-forms is comprised, it is a <= 0.25 about the radius of a vortex. Assuming such conditions, the equation (11) becomes maximum when a = 0 and b = 0.05, and the value is 900. therefore,

In this case, droplets at any position can be captured under this condition.

"4th embodiment"

Fig. 13 is a sectional view showing the gas-liquid separation device of the fourth embodiment. FIG. 14 is a sectional view taken along line A-A of the gas-liquid separation device shown in FIG. Fig. 15 is an exploded perspective view of the groove forming body 4 formed by bending a thin plate. Fig. 16 is a principle model diagram showing the effect formed by tilting the groove 2. As shown in Fig. 13, a groove forming body 4 having a groove 2 facing the liquid outlet tube 7 is provided in the outer casing 10, and an inlet section upstream of the groove forming body 4 is provided. The sieve 16 is provided and comprises the gas-liquid separation chamber 1. The groove forming body 4 is bent into a thin plate to form a groove 2 as shown in FIG. 15, and is rounded and inserted into the outer body 10 as shown in FIG. Downstream of the groove forming body 4, the gas phase outlet pipe 6 is surrounded by an outlet partition 8 joined to the gas phase outlet pipe 6 so as to define a lower position in the height direction of the groove forming body 4. It is joined to the lower shaft pipe part 13 of (10).

The gas-liquid two-phase flows in from the inlet pipe 5 and into the narrow space 12 made up with the inlet partition 16 and the outer shell B 11. Since the gas-liquid two-phase upstream is supplied along the groove 2 in the narrow space 12, the gas-liquid two-phase flows into a groove along the groove. The two-phase liquid phase introduced into the groove-forming body 4 basically adheres to the surface of the groove 2 to form a liquid film. In addition, the droplets carried in the gas phase collide with the surface of the groove 2 to form a liquid film. The liquid film flows downward and flows out from the liquid outlet pipe 7. The gaseous phase from which the droplets have been removed flows out of the gas phase outlet pipe 6.

Here, the groove 2 of the groove forming body 4 is formed with the angle α inclined with respect to the center line 15 of the outer body 10 as shown in FIG. The effect of tilting the groove at the angle α will be described using the principle model diagram shown in FIG. Fig. 16 is a principle model diagram in which one groove of the groove forming body 4 is taken out, and Fig. 16 (a) is a model diagram when the groove is not inclined, and Fig. 16 (b) is inclined the groove at an angle α. A model diagram of the case.

The first effect by tilting the groove will be described. By tilting the groove, the groove width b 'becomes smaller than the groove width b when not tilting. When the gaseous phase flows through the groove, droplets carried in the gaseous phase easily collide with the surface of the groove 2 as the groove width is smaller, thereby forming a liquid film. Thus, the gas-liquid separation performance can be improved by tilting the groove to reduce the actual groove width. have. In addition, in Fig. 16 (a), it is also considered to simply reduce the groove pitch p. However, if the groove pitch p is simply reduced while the diameter of the outer body 10 is constant, it means that the number of grooves increases. There is a problem that the price of the gas-liquid separator increases due to the increase in the amount of the material forming the groove forming body. Therefore, the groove width can be reduced by making the groove smaller, thereby providing a high performance and inexpensive gas-liquid separation device.

A second effect by tilting the groove will be described with reference to FIG. As shown in Fig. 14, by inclining the groove α, the flow direction 23 of the gaseous phase flowing out of the groove flows into the gas-liquid separation chamber 1 at an angle α. Therefore, the swirl flow 24 is generated in the gas-liquid separation chamber 1 by introducing a gaseous phase at an angle α from all the grooves opened in the gas-liquid separation chamber 1.

When the droplets carried in the gaseous phase in the grooves 2 are very small, the fine droplets sometimes flow from the grooves 2 into the gas-liquid separation chamber 1 without colliding with the groove surface. At this time, as shown in Fig. 20, when the groove is not inclined, the fine droplets spilled into the gas-liquid separation chamber 1 are uniformly distributed toward the center of the gas-liquid separation chamber 1, and the shaft in the gas-liquid separation chamber is It flows out from the gaseous-phase outlet pipe 6 according to the direction gaseous-phase rising speed u _a (25). By turning the groove, the swirl flow 24 is generated in the gas-liquid separation chamber 1, and the fine droplets collect in the space in the gas-liquid separation chamber close to the opening of the groove 2 by the action of the centrifugal force by the swirl flow. It becomes easy, and the probability that fine droplets combine with each other and becomes larger droplet increases. When the droplets are large, the gravity Fg acting on the droplets exceeds the drag force F _D which raises the droplets by the axial gas phase rising speed u _a (25), so that the droplets easily fall downward and thus the gas phase outlet pipe (6). It is difficult to escape from the. In other words,

When it satisfy | fills, a droplet will fall easily below. Here, by the droplet diameter d, the drag coefficient C _D, vapor density ρ _G, a liquid density ρ _L, weather such a viscosity coefficient ν _G, the droplets projected area ^{A = π d 2/4,} Fg and F _D becomes Equations 14 and 15, respectively.

Given a drag coefficient defined in Equation 2,

When the droplet diameter d becomes large, the droplets easily fall downward. Therefore, by tilting the groove, swirl flow 24 is generated in the gas-liquid separation chamber 1, and droplets are less likely to flow out of the gas phase outlet pipe 6, thereby providing a high-performance gas-liquid separation device.

The third effect by tilting the groove will be described with reference to FIGS. 13, 14 and 16. FIG. As shown in Fig. 16, by inclining the groove in a state where the substantial length h of the groove is constant, the vertical groove depth h 'with respect to the bottom of the groove becomes smaller than the groove depth h when not inclined. Therefore, by tilting the groove, the diameter Dt of the groove peak virtual circle 9 shown in Fig. 14 becomes substantially large. Accordingly, the gas-liquid separation chamber within the axial vapor rising velocity u _a (25) is lowered, it is easy to fall into F _D <Fg a stronger tendency of the droplets downward, as indicated by equation (16). Therefore, by tilting the groove, the liquid droplets are less likely to flow out of the gas phase outlet pipe 6, thereby providing a high-performance gas-liquid separation device. In addition, although the example using the groove formation body 4 which bent the thin plate was described in 4th Embodiment mentioned above, as shown in FIG. 17, the groove formation body is another groove | channel produced by some means, such as a machining process. It is a matter of course that the above-described effects are the same even in the formed body.

"Fifth Embodiment"

18 is a sectional view showing the gas-liquid separation device of the fifth embodiment. 19 is a cross-sectional view taken along the line C-C in FIG. 20 is a cross-sectional view taken along the line A-A of FIG. As shown in FIG. 19, the inlet pipe 5 is provided so that it may flow in the tangential direction from the horizontal direction of the outer periphery B11 to the inflow chamber 19. As shown in FIG. As shown in Fig. 18, the gas-liquid separator is provided with a gas phase outlet tube 6 on the upper portion of the gas-liquid separator, and the lower portion of the gas phase outlet tube 6 is in fluid communication with the upper portion of the inlet compartment 16. The gas phase outlet pipe 6 is joined to the upper shaft pipe part 17 of the outer shell B11. In the outer casing 10, a groove forming body 4 having a groove 2 facing the liquid outlet tube 7 is provided, and an inlet partition 16 is provided upstream of the groove forming body 4. The gas-liquid separation chamber 1 is configured. The groove forming body 4 is bent into a thin plate to form the groove 2, as shown in FIG. 21, and is rounded and inserted into the outer body 10 as shown in FIG. The downstream of the groove formation body 4 defines the lower position of the height direction of the groove formation body 4 by the bead 26 provided in the exterior body 10, and the lower shaft pipe part 13 of the exterior body 10 The liquid outlet pipe 7 is joined to the.

The gas-liquid two-phase flows in from the inlet pipe 5 and into the narrow space 12 made up with the inlet partition 16 and the outer shell B 11. Since the gas-liquid two-phase upstream is supplied along the groove 2 in the narrow space 12, the gas-liquid two-phase flows into a groove along the groove. The two-phase liquid phase introduced into the groove-forming body 4 basically adheres to the surface of the groove 2 to form a liquid film. In addition, the droplets carried in the gas phase collide with the surface of the groove 2 to form a liquid film. The liquid film flows downward and flows out from the liquid outlet pipe 7. The gaseous phase from which the droplets have been removed rises in the gas-liquid separation chamber 1, passes through the inlet compartment 16, and flows out of the gas phase outlet pipe 6.

According to the gas-liquid separator of 5th Embodiment shown in FIG. 18, since the gaseous-phase outlet tube 6 is provided in the upper part of a gas-liquid separator, a gaseous-phase outlet tube does not penetrate the gas-liquid separation chamber 1, and FIG. since the entire inner diameter Dt of the groove top point a virtual source (9) as shown in 20 to a gas-liquid separation chamber within the axial vapor rising flow path, vapor rising velocity u _a is decreased, as indicated by equation (16) F _D The tendency of < Fg becomes strong, and droplets fall easily below. Therefore, by installing the gas phase outlet tube 6 in the upper part of the gas-liquid separator and connecting the lower part of the gas phase outlet tube 6 to the upper part of the inlet partition 16 in fluid communication, the droplets may form the gas phase outlet tube ( It is hard to flow out from 6) and can provide a high performance gas-liquid separation device. In particular, in the case of an oil separator having a large amount of gas phase flow rate relative to the liquid phase flow rate, it is necessary to increase the diameter dp of the gas phase outlet pipe 6 shown in Fig. 14, and the gas phase occupies the axial gas phase rising passage in the gas-liquid separation chamber. The cross-sectional area of the outlet pipe 6 cannot be ignored, and the configuration in which the gas phase outlet pipe 6 does not penetrate the gas-liquid separation chamber 1 has a great effect.

"The sixth embodiment"

22 is a diagram illustrating the first refrigeration cycle when the above-mentioned gas-liquid separator is used for a refrigeration cycle. The refrigeration cycle block diagram shown in FIG. 22 shows the basic components necessary for explaining the present embodiment. That is, the compressor 27 has a first cylinder 28 and a second cylinder 29, the low-temperature low-pressure gaseous refrigerant sucked by the compressor in two stages in the first cylinder 28 and the second cylinder 29. It is compressed and becomes a high temperature high pressure gaseous refrigerant, passes through the refrigerant discharge pipe 30, and is radiated by air sent from the condenser 31 to the condenser blower 32 to become a high pressure liquid refrigerant. The liquid refrigerant is depressurized by the first pressure reducer 33 to become two-phase flow, flows into the gas-liquid separator 43 from the inlet pipe 5, and the liquid refrigerant flows out of the liquid outlet pipe 7 and then the second It is further depressurized in the pressure reducer 34, takes heat from the air that enters the evaporator 35 and is sent to the blower 36 for the evaporator, and becomes a low-temperature, low-pressure gaseous phase refrigerant which is sucked into the compressor 27. On the other hand, since the gaseous phase refrigerant separated by the gas-liquid separator 43 is sucked into the second cylinder 29 from the gaseous-phase outlet pipe 6, the gaseous phase refrigerant which does not contribute to the evaporation separated by the gas-liquid separator 43 is the first. There is no need to compress in the cylinder 28, which can reduce the compression power and enable high efficiency operation.

"Seventh embodiment"

FIG. 23 is a diagram of a second refrigeration cycle when the above-described gas-liquid separator is used in a refrigeration cycle. The refrigeration cycle block diagram shown in FIG. 23 shows the basic components necessary for explaining this embodiment. That is, the compressor 27 has only the first cylinder 28, the low-temperature low-pressure gaseous refrigerant sucked by the compressor is compressed in the first cylinder 28 and becomes a high-temperature high-pressure gaseous refrigerant through the refrigerant discharge pipe 30, The heat is radiated by the air sent from the condenser 31 to the condenser blower 32 to form a high pressure liquid refrigerant. The liquid refrigerant is depressurized in the first pressure reducer 33 to be in two phase flow, is introduced into the gas-liquid separator 43 from the inlet pipe 5, and the liquid refrigerant is transferred from the liquid outlet pipe 7 to the evaporator 35. The heat is taken from the air sent to the blower blower 36 for evaporator, and it becomes a low-temperature, low-pressure gaseous phase refrigerant, and is sucked into the compressor 27. On the other hand, the gaseous phase refrigerant separated by the gas-liquid separator is sucked into the compressor 27 from the gas phase outlet pipe 6 via the evaporator bypass pipe 38.

When the gas-liquid separator 43 is not used, the two-phase gaseous phase refrigerant depressurized by the pressure reducer 33 also flows into the evaporator, and in particular, when the air temperature sent by the evaporator blower 36 is low, the evaporation pressure is reduced. This decreases and the density of the gaseous refrigerant decreases, so that the volume flow rate increases, so that the pressure loss in the evaporator 35 is large, so that the outlet pressure of the evaporator 35, that is, the compressor suction pressure, decreases, so that the compression power is increased, resulting in high efficiency operation. You won't be able to.

On the other hand, as shown in the present embodiment, a gas-liquid separator 43 is provided, and the separated gaseous refrigerant is sucked from the gas phase outlet pipe 6 through the evaporator bypass pipe 38 to the compressor 27 to prevent evaporation. Since the gaseous refrigerant that does not contribute does not flow into the evaporator 35, the pressure loss in the evaporator 35 can be suppressed, and the compression power can be reduced, thereby enabling high efficiency operation.

Conventionally, as a gas-liquid separator used in a refrigeration cycle, a tank for storing a liquid by gravity or a gas-liquid separator for attaching a liquid to the outer wall by centrifugal force of swirling flow and recovering the liquid by gravity is used. Although the gas-liquid separator of such a structure basically has a structure which separates a liquid density with a high density by volume force, such as gravity and centrifugal force, in addition to having less freedom in the installation position and direction of a gas-liquid separator, In the sixth and seventh embodiments of the present invention, a large-sized device is used because the swirl flow generating device is used. As described above, high efficiency operation can be enabled.

"Eighth Embodiment"

Fig. 24 is a third refrigeration cycle diagram when the above-mentioned gas-liquid separator is used for a refrigeration cycle. Fig. 24 is an example of a separate type air conditioner, which is composed of an outdoor unit 39 and an indoor unit 40, and shows a cycle during cooling operation. Refrigerator oil is mixed in the high temperature and high pressure gaseous refrigerant compressed by the compressor 27, and when the amount of the refrigerant oil mixed into the gaseous refrigerant discharged from the compressor increases, the pressure loss of the refrigeration cycle refrigerant path increases, and the evaporative heat transfer rate of the refrigerant is increased. And condensation heat transfer rate is lowered, which causes a decrease in refrigeration cycle efficiency. In addition, when the compressor is started, the refrigeration oil encapsulated in the compressor is formed, and a large amount of the refrigeration oil is mixed with the gaseous refrigerant, discharged from the compressor, and discharged into the refrigeration cycle. In particular, in the case of a separate type air conditioner, a connecting pipe connecting an indoor unit and an outdoor unit is provided. When the connecting pipe 48 is long, the refrigeration oil flowing out of the refrigeration cycle does not return to the compressor for a long time, Therefore, there is a problem that the lack of refrigeration oil in the compressor causes a problem in the reliability of the compressor.

Thus, in order to solve the above problems, FIG. 24 is provided with a compact gas-liquid separator 43 in the refrigerant discharge pipe of the compressor 27 to secure the refrigeration cycle efficiency and the reliability of the compressor. That is, the low-temperature, low-pressure gaseous phase refrigerant sucked by the compressor 27 is compressed by the compressor 27 and becomes a high-temperature, high-pressure gaseous phase refrigerant through the refrigerant discharge pipe 41 from the inlet pipe 5 of the gas-liquid separator 43. Flows into the gas-liquid separator. In the high-temperature, high-pressure gas phase refrigerant compressed by the compressor 27, refrigeration oil is mixed, and in the gas-liquid separator 43, the refrigeration oil is separated into a liquid phase and the gaseous refrigerant is separated into a gaseous phase, respectively. It is taken out from the gas phase outlet pipe 6. The refrigeration oil exiting the liquid outlet pipe 7 is sucked into the compressor suction pipe 46 via the liquid receiver 42 and the flow adjusting throttle 45, and the freezer oil is returned to the compressor. The reason why the flow rate adjusting throttle 45 is provided is that the refrigeration oil mixed in the high temperature and high pressure gaseous refrigerant discharged from the compressor 27 is less than the gaseous refrigerant in normal operating conditions, and thus the gas-liquid separator 43 This is to return the refrigeration oil from the flow rate adjusting shaft 45 to the compressor 27 gradually from the freezing oil separated from the flow path. Further, the reason why the liquid receiver 42 is provided is that the refrigerant oil enclosed in the compressor is foamed at the time of starting the compressor and a large amount of the refrigerant oil is mixed into the gaseous refrigerant and discharged from the compressor. The refrigeration oil separated in (43) is temporarily stored in the liquid receiver 42 to gradually return the refrigeration oil to the compressor 27 from the flow rate adjusting shaft 45. In addition, when the volume of the liquid storage part 18 of a gas-liquid separator is large, a liquid receiver is not necessarily required.

On the other hand, the gaseous phase refrigerant separated in the gas-liquid separator 43 passes through the four-way valve 47 from the gas phase outlet pipe 6, and radiates heat with the air sent from the condenser blower 32 in the condenser 31 to generate a high-pressure liquid. It is a refrigerant. The liquid refrigerant is depressurized by the first pressure reducer 33 to become a low-temperature, low-pressure two-phase stream, and enters the evaporator 35 to extract heat from the air sent to the evaporator blower 36 to become a low-temperature low-pressure gaseous refrigerant. Inhaled by 27. Therefore, in the gas-liquid separator 43, the refrigeration oil is separated as a liquid phase, and is sucked into the compressor suction pipe 46 from the liquid outlet pipe 7 via the liquid receiver 42 and the flow adjustment throttle 45, and the freezer Since oil is returned to the compressor, it is possible to prevent the freezer oil from leaking into the freezing cycle, thereby enabling high efficiency refrigeration cycle operation, and preventing the freezer oil from leaking into the refrigeration cycle at start-up, thus enabling highly reliable operation. .

The present invention is a gas-liquid separation device that separates the gaseous phase and the liquid phase through a narrow groove through the gas-liquid two-phase flow, using a secondary flow in order to capture the droplets carried in the gaseous phase to the maximum, tilting the grooves, gas-liquid separation It is possible to efficiently capture the droplets conveyed in the gas phase by using the entire cross-sectional area as the axial gas phase rising passage, thereby enabling the provision of a gas-liquid separation device that can follow the miniaturization of the refrigeration apparatus, as well as the freezing. It can greatly contribute to improving the cooling performance of the device.

1 is a cross-sectional view of the gas-liquid separation device of the first embodiment.

FIG. 2 is a cross-sectional view taken along the line A-A of the gas-liquid separator shown in FIG.

3 is an exploded perspective view of the groove forming body shown in FIG. 2;

FIG. 4 is a perspective view showing one pitch of the groove-formed body in which a substantially wave shape inclined with respect to the mainstream shown in FIG. 3 is formed; FIG.

Fig. 5 is a sectional view of the gas-liquid separation device of the second embodiment.

Fig. 6 is an exploded perspective view of a groove forming body in which a substantially wave shape with a wide end is formed with respect to the mainstream shown in Fig. 5;

FIG. 7 is a perspective view showing one pitch of the groove-formed body in which an approximately wide end shape is formed with respect to the mainstream shown in FIG. 6; FIG.

Fig. 8 is a sectional view of the gas-liquid separation device of the third embodiment.

FIG. 9 is a sectional view taken along the line B-B of the gas-liquid separation device shown in FIG. 8; FIG.

Fig. 10 is a sectional view of the groove forming body shown in Figs. 4 and 7;

FIG. 11 shows a model of attachment of droplets to the wall surface; FIG.

Fig. 12 is a diagram showing the dimensionless length of the grooved body obtained from the calculation.

Fig. 13 is a sectional view showing the gas-liquid separation device of the fourth embodiment.

Fig. 14 is a sectional view taken along the line A-A of the gas-liquid separation device shown in Fig. 13;

FIG. 15 is an exploded perspective view of the groove forming body shown in FIG. 13; FIG.

Fig. 16 is a principle model diagram showing the effect formed by tilting the groove 2;

Figure 17 is an enlarged cross sectional view of a portion of another groove formation.

Fig. 18 is a sectional view showing the gas-liquid separation device of the fifth embodiment.

Fig. 19 is a sectional view taken along the line C-C in Fig. 18;

20 is a cross-sectional view taken along line A-A of FIG.

FIG. 21 is an exploded perspective view of the groove forming body shown in FIG. 18; FIG.

Fig. 22 is a sixth embodiment of the first refrigeration cycle configuration diagram when the above-mentioned gas-liquid separator is used for a refrigeration cycle.

FIG. 23 is a diagram of a second refrigeration cycle when the above-mentioned gas-liquid separator is used for a refrigeration cycle.

Fig. 24 is a third refrigeration cycle diagram when the above-mentioned gas-liquid separator is used for a refrigeration cycle.

<Explanation of symbols for the main parts of the drawings>

1: gas-liquid separation chamber

2: home

3: rapid expansion unit

4: groove forming body

5: entrance tube

6: weather outlet pipe

7: liquid outlet pipe

8: outlet compartment

9: home top point virtual circle

10: outline

11: outline B

12: narrow space

13: lower shaft pipe part

14: Droplet

15: centerline

16: inlet compartment

17: upper shaft pipe

18: liquid storage part

19: inflow chamber

20: secondary flow

21: weather inlet end

22: communication hole

23: flow direction of the weather from the groove

24: swirl flow

25: axial meteorological ascent rate Ua

26: Bead

27: compressor

28: first cylinder

29: second cylinder

30: discharge tube

31: condenser

32: blower for condenser

33: first pressure reducer

34: second pressure reducer

35: evaporator

36 blower for evaporator

37: compartment cylinder

38: evaporator bypass pipe

39: outdoor unit

40: indoor unit

41: refrigerant discharge tube

42: liquid receiver

43: gas-liquid separator

45: flow adjustment throttle

46: compressor suction pipe

47: four-way valve

48: connection piping

Claims (13)

Part of the gas-liquid separation chamber is provided with a groove forming body having a groove facing the liquid outlet tube, and has a narrow space having an outer body and an inlet partition upstream of the gas-liquid separation chamber, and at the same time, a gas-liquid two-phase flow introduced from the inlet tube. After passing through the narrow space to guide the gas-liquid separation chamber from the groove forming body, the gas-liquid two-phase flow is introduced into the liquid-phase outlet pipe through the groove forming body, the gas phase is introduced into the gas phase outlet pipe from the gas-liquid separation chamber A gas-liquid separation device comprising a gas-liquid separation mechanism, wherein the gas-phase outlet tube is provided above the gas-liquid separator, and the lower portion of the gas-phase outlet tube is connected to the upper portion of the inlet compartment in fluid communication. A gas-liquid separation device characterized by the above-mentioned. The gas-liquid separation device according to claim 1, wherein the surface of the groove forming body has an approximately wave shape inclined in the flow direction. The gas-liquid separation device according to claim 2, wherein a substantially wave shape inclined in the flow direction formed on the surface of the groove-forming body is formed to widen radially outward in the flow direction. The gas-liquid separation device according to claim 2, wherein an approximately wave shape inclined in the flow direction formed on the surface of the groove forming body is formed to have a wide end in the flow direction. The gas-liquid separation device according to claim 2, wherein a partition cylinder is provided inside the groove forming body. 3. The length L of the groove forming body, the pitch p of the groove forming body, the mainstream velocity u flowing through the groove forming body, the droplet diameter d , the gas phase viscosity coefficient μ _G , the gas phase density ρ _G , and the liquid phase density ρ _L. time,

Gas-liquid separation apparatus characterized in that. The gas-liquid separation device according to claim 1, wherein the groove is formed at an angle α inclined with respect to the centerline of the outer body. 8. The gas-liquid separation device according to claim 7, wherein the surface of the groove forming body has an approximately wave shape inclined in the flow direction. Part of the gas-liquid separation chamber is provided with a groove forming body having a groove facing the liquid outlet tube, and a narrow space is formed with the outer body and the inlet partition upstream of the gas-liquid separation chamber, and the gas-liquid two-phase flow introduced from the inlet tube. After passing through the narrow space is introduced into the gas-liquid separation chamber from the groove forming body, the gas-liquid two-phase flow is introduced into the liquid-phase outlet pipe through the groove forming body, the gaseous phase is introduced into the gas phase outlet pipe from the gas-liquid separation chamber A gas-liquid separation device comprising: a gas-liquid separation device, wherein the gas-liquid separation device has a substantially wave shape inclined in the flow direction of the groove-forming body. Part of the gas-liquid separation chamber is provided with a groove forming body having a groove facing the liquid outlet tube, and a narrow space is formed with the outer body and the inlet partition upstream of the gas-liquid separation chamber, and the gas-liquid two-phase flow introduced from the inlet tube. After passing through the narrow space is introduced into the gas-liquid separation chamber from the groove forming body, the gas-liquid two-phase flow is introduced into the liquid-phase outlet pipe through the groove forming body, the gaseous phase is introduced into the gas phase outlet pipe from the gas-liquid separation chamber A gas-liquid separation device comprising a gas-liquid separation mechanism, wherein the groove is formed by inclining the angle α with respect to the centerline of the outer body. The gas-liquid separation apparatus in any one of Claims 1-10 was built in refrigeration cycles, such as an air conditioner, The refrigeration apparatus provided with the gas-liquid separation apparatus characterized by the above-mentioned. The outlet pipe of the pressure reducer in a refrigerating cycle is connected to the two-phase inlet pipe of the gas-liquid separator of any one of Claims 1-10, and the liquid-phase outlet pipe of a gas-liquid separator is connected to the pipeline which leads to an evaporator. And a gas phase outlet tube of the gas-liquid separator is connected to the suction tube of the compressor via a bypass and a resistance regulator. The compressor discharge pipe in the refrigeration cycle is connected to the two-phase inlet pipe of the gas-liquid separator according to any one of claims 1 to 10, and the liquid outlet pipe of the gas-liquid separator is connected to the compressor suction pipe through the flow adjusting throttle. And a gas phase outlet pipe of the gas-liquid separator is connected to a conduit leading to the condenser of the refrigeration cycle.

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