Two-phase separation device

Abstract

The invention relates to the technical field of two-phase separation, in particular to two-phase separation equipment which comprises an inner barrel, an inner rotational flow cavity and an inner rotational flow component are arranged in the inner barrel, and the inner rotational flow component is used for forming rotational flow from top to bottom in the inner rotational flow cavity to achieve primary separation of a two-phase mixture to obtain primary separation inner rotational flow and primary separation outer rotational flow; an auxiliary rotational flow pipe is arranged in the inner rotational flow cavity, the upper end of the auxiliary rotational flow pipe is covered with a collecting pipe in a spaced mode to form a secondary separation section, and an auxiliary rotational flow starting component is installed in the secondary separation section and used for leading primary separation inner rotational flow into the secondary separation section from an annular gap between the auxiliary rotational flow pipe and the collecting pipe and forming rotational flow for secondary separation. According to the invention, quenching or waste heat recovery can be completed while material separation is realized.

Description

Technical Field

[0001] The present invention relates to the technical field of two-phase separation, and particularly relates to a two-phase separation device. Background Art

[0002] In the chemical process industry, gas-liquid, gas-solid or liquid-solid separation is a common and important separation step, which widely exists in various process flow processes. Taking gas-liquid separation as an example, gas-liquid bubbling or spraying reactors are common gas-liquid reactors. Usually, the gas after reaction leaves the reaction system from the top of the reactor and enters the next unit. In this process, the gas usually entrains a considerable amount of liquid droplets. Therefore, a wire mesh demister is usually installed at the top of the reactor to separate the liquid droplets, and further series of pressure reduction - temperature reduction flash evaporation and other methods are used to enhance the liquid droplet condensation. However, it is often difficult to achieve a high separation efficiency in such separation processes. In order to improve the separation efficiency, the corresponding pressure drop and energy consumption cost will be significantly increased. At the same time, such multi-stage series processes will also significantly increase the equipment floor area and increase the investment cost. Summary of the Invention

[0003] The purpose of the present invention is to overcome the problems of insufficient separation performance, high energy consumption and high equipment cost existing in the prior art, and provide a two-phase separation device, which has the advantage of being able to complete quenching or waste heat recovery while realizing material separation.

[0004] In order to achieve the above purpose, the present invention discloses a two-phase separation device, which includes a two-phase separator, and the two-phase separator includes: An inner cylinder body, which is provided with an inner swirl chamber and an inner swirl member. The inner swirl member is used to form a downward swirl in the inner swirl chamber to realize the primary separation of the two-phase mixture, and obtain a primary separation inner swirl and a primary separation outer swirl; A secondary swirl tube is arranged in the inner swirl chamber. The upper end of the secondary swirl tube is spaced from and covered with a manifold to form a secondary separation section. A secondary swirl generating member is installed in the secondary separation section. The secondary swirl generating member is used to introduce the primary separation inner swirl from the annular gap between the secondary swirl tube and the manifold into the secondary separation section and form a swirl for secondary separation.

[0005] In some embodiments of the present invention, the bottom end of the inner swirl chamber is provided with a tapered body that tapers upward. The annular gap between the tapered body and the wall of the inner swirl chamber forms a first outlet for the heavy components.

[0006] In some embodiments of the present invention, the top end of the tapered body extends upward to form a secondary swirl tube, and the end face opening at the bottom end of the tapered body forms a second outlet for the heavy components.

[0007] In some embodiments of the present invention, one end of the auxiliary overflow pipe penetrates through the header pipe and extends into the auxiliary cyclone tube, and the other end extends out of the inner cyclone cavity to form the second outlet for light components.

[0008] In some embodiments of the present invention, an overflow pipe is provided through the top wall of the inner cyclone cavity, the overflow pipe is sleeved outside the auxiliary overflow pipe, and the annular gap between the auxiliary overflow pipe and the overflow pipe forms the first outlet for light components.

[0009] In some embodiments of the present invention, the inner cyclone member includes a first inner cyclone member and a second inner cyclone member along the material flow direction, wherein the two-phase material is initially swirled by the first inner cyclone member and then swirled again by the second inner cyclone member.

[0010] In some embodiments of the present invention, preferably, the first inner cyclone member includes Form A or Form B, wherein: Form A: The first inner cyclone member is provided as a tangential mixture inlet opened on the tangent of the inner cylinder. Form B: The first inner cyclone member is provided as a first impeller sleeved on the overflow pipe, and the gap between the overflow pipe and the inner cylinder forms an axial mixture inlet for feeding the two-phase mixture.

[0011] In some embodiments of the present invention, the two-phase separator includes an outer cylinder, the outer cylinder is sleeved outside the inner cylinder and an annular cavity is formed therebetween, and the annular cavity is used for circulating a heat exchange medium to perform a wall-type heat exchange with the inner cyclone cavity.

[0012] In some embodiments of the present invention, heat exchange fins are provided on the outer wall of the inner cylinder, and preferably, the heat exchange fins are provided as spiral heat exchange fins extending along the axis of the inner cylinder.

[0013] In some embodiments of the present invention, an outer cyclone member is provided in the annular cavity, and the outer cyclone member causes the heat exchange medium to form an axial swirl in the annular cavity.

[0014] In some embodiments of the present invention, the outer cyclone member includes Form C or Form D, wherein: Form C: The outer cyclone member is provided as a tangential heat exchange medium inlet opened on the side wall of the outer cylinder, and the tangential heat exchange medium inlet is provided at the upper or lower part of the outer cylinder. Form D: The outer cyclone member is provided as a second impeller sleeved on the inner cylinder, and the two open ends of the outer cylinder form a working medium axial through port for passing the heat exchange medium.

[0015] Through the above technical solution, the two-phase separation device of the present invention can achieve secondary separation, shorten the process flow, reduce the floor area of the equipment, and increase the production intensity. Further, the two-phase separation device of the present invention has an inner and outer two-layer flow space, integrating cyclone separation and material cooling heat exchange, and can complete the quenching or waste heat recovery process while achieving efficient separation of materials. The present invention has the advantages of shortening the process flow, reducing the floor area of the equipment, and increasing the production intensity. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 FIG. is a schematic structural diagram of a two-phase separation device according to an embodiment of the present invention; Figure 2 FIG. is a schematic structural diagram of a two-phase separation device according to another embodiment of the present invention; Figure 3 FIG. is a schematic structural diagram of a two-phase separation device according to another embodiment of the present invention; Figure 4 FIG. is a schematic structural diagram of a two-phase separation device according to another embodiment of the present invention; Figure 5 FIG. is a schematic structural diagram of a two-phase separation device according to another embodiment of the present invention; Figure 6 FIG. is a three-dimensional structural diagram of a spiral heat exchange fin according to an embodiment of the present invention; Figure 7 FIG. is a three-dimensional structural diagram of a conical body according to an embodiment of the present invention.

[0017] DESCRIPTION OF THE REFERENCE NUMERALS 2 tangential inlet of the mixture; 3 inner cylinder; 4 outer cylinder; 5 spiral heat exchange fin; 6 conical body; 8 first impeller; 9 second impeller; 10 overflow pipe; 11 first outlet of the heavy components; 12 axial inlet of the mixture; 13 axial through-port of the working medium; 16 manifold; 17 fourth impeller; 18 secondary cyclone tube; 19 second outlet of the heavy components; 20 secondary overflow pipe; 31 inner swirl chamber; 41 annular cavity. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0018] The following is a detailed description of the specific embodiments of the present invention with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only for the purpose of illustration and explanation of the present invention, and are not intended to limit the present invention.

[0019] In the ranges disclosed herein, the endpoints and any values are not limited to the exact ranges or values. These ranges or values should be understood to include values close to these ranges or values. For numerical ranges, between the endpoint values of each range, between the endpoint values and individual point values of each range, and between individual point values, they can be combined with each other to obtain one or more new numerical ranges, and these numerical ranges should be regarded as specifically disclosed herein.

[0020] In the present invention, unless otherwise stated, the orientation terms such as "upper, lower, top, bottom" generally refer to the directions shown in the drawings or the mutual positional relationship of the components in the vertical, perpendicular or gravitational directions. In the present invention, the light component refers to the phase with a smaller density or particle size, and the heavy component refers to the other phase with a larger particle size or density.

[0021] The present invention discloses a two-phase separation device, and the two-phase separation device includes a two-phase separator, as Figure 1 shown, the two-phase separator includes: an inner swirl member, an inner cylinder 3, and an inner swirl chamber 31 formed by surrounding the inner cylinder 3. The inner swirl member is used to form a downward swirl in the inner swirl chamber 31 to achieve the primary separation of the two-phase mixture, obtaining a primary separation inner swirl containing light components and a primary separation outer swirl containing heavy components; a secondary swirl tube 18 is coaxially arranged in the inner swirl chamber 31, and the upper end of the secondary swirl tube 18 is spaced from and covers a collecting tube 16 to form a secondary separation section. A secondary swirl generating member is installed in the secondary separation section. The secondary swirl generating member is used to introduce the primary separation inner swirl from the annular gap between the secondary swirl tube 18 and the collecting tube 16 into the secondary separation section and form a swirl for secondary separation. Through the setting of the two-phase separator of the present invention, the process flow can be shortened while performing secondary separation, the floor area of the equipment can be reduced, the separation and heat exchange efficiency can be optimized, the production intensity can be improved, and the equipment investment cost can be reduced.

[0022] In some embodiments of the present invention, a tapered body 6 that tapers upward is provided at the bottom end of the inner swirl chamber 31. The annular gap between the tapered body 6 and the chamber wall of the inner swirl chamber 31 forms a first heavy component outlet 11; the top end of the tapered body 6 extends upward to form the secondary swirl tube 18, and the end face opening at the bottom end of the tapered body 6 forms a second heavy component outlet 19; one end of the secondary overflow pipe 20 penetrates through the collecting tube 16 and extends into the secondary swirl tube 18, and the other end extends out of the outer shape of the inner swirl chamber 31 to form a second light component outlet; an overflow pipe 10 is provided through the top wall of the inner swirl chamber 31, the overflow pipe 10 is sleeved outside the secondary overflow pipe 20, and the annular gap between the secondary overflow pipe 20 and the overflow pipe 10 forms a first light component outlet.

[0023] Thus, the two-phase mixture to be separated enters the inner swirl chamber 3 to form an axial inner swirl for primary separation to form a primary separation inner swirl and a primary separation outer swirl. After passing through the tapered body, the primary separation outer swirl carries the heavy component fluid out from the heavy component outlet 11, and the primary separation inner swirl rises. Among them, the lighter components in the primary separation inner swirl are discharged from the first light component outlet, and the heavier components are introduced by the secondary swirl generating member into the space surrounded by the secondary swirl tube 18 and the collecting tube 16, and first generate a swirl through the secondary swirl generating member for further swirl separation (secondary separation). The lighter components separated in the secondary separation are discharged from the second light component outlet, and the heavier components separated in the secondary separation are discharged from the second heavy component outlet.

[0024] In some embodiments of the present invention, the secondary swirl tube 18 gradually expands along its extending direction to form a generally funnel shape with the cone 6.

[0025] In some embodiments of the present invention, the secondary swirl member is arranged as a fourth impeller 17 sleeved on the secondary overflow pipe; there are no special requirements for the fourth impeller 17 in the present invention, as long as it can introduce the heavier components in the primary separated inner swirl flow into the secondary separation section and generate swirl, which will not be elaborated herein.

[0026] In some embodiments of the present invention, the cone 6 is a frustum of a cone and is coaxially arranged with the inner cylinder 3. The large end diameter of the cone 6 R c is 0.3 - 0.8 times the bottom diameter of the inner cylinder 3. The cone 6 can be Figure 7 the shown cone. The height of this cone L h is 0.01 - 0.1 times the length of the inner cylinder 3. It should be noted that the top of this cone is horizontally cut off by (1 / 4 - 1 / 2) L h to form the cone 6 of the present invention, and the top of this cone 6 extends upward to form the secondary swirl tube 18.

[0027] In some embodiments of the present invention, as Figure 1 shown, the inner swirl member includes a first inner swirl member and a second inner swirl member along the flow direction of the material in the inner swirl chamber 31. Among them, the two-phase material generates swirl for the first time through the first inner swirl member and then generates swirl for the second time through the second inner swirl member; thus, the fluid to be separated (two-phase mixture) enters the inner cylinder 3 for swirl separation and then reaches the second inner swirl member. After passing through the second inner swirl member, the swirl is further strengthened and then continues to flow downward for swirl separation.

[0028] In some embodiments of the present invention, preferably, the first inner swirl member includes Form A or Form B. Among them, Form A has a higher swirl intensity, and Form B has a more compact external dimension: Form A: As Figures 1 - 3 shown, the first inner swirl member is arranged as a tangential inlet 2 for the mixture opened along the tangent of the inner cylinder 3. The fluid to be separated enters the inner swirl chamber 31 from the tangential inlet 2 of the mixture to form a swirl and flows downward through the second inner swirl member; in some embodiments of the present invention, the flow cross-section of the tangential inlet 2 of the mixture is rectangular, circular or elliptical.

[0029] Form B: As Figures 4 - 5 shown, the first inner swirl member is arranged as a first impeller 8 sleeved on the overflow pipe 10, and the gap between the overflow pipe 10 and the inner cylinder 3 forms an axial inlet 12 for the two-phase mixture for feeding.

[0030] In some embodiments of the present invention, in Form B, the first impeller 8 includes 2 to 15 blades. The angle between the blades of the first impeller 8 and the incoming flow direction of the two-phase material is -60° to 60°. The height of the blades of the first impeller 8 is 0.1 to 10 times the width. The width of the blades of the first impeller 8 is 0.3 to 1 times the distance between the overflow pipe 10 and the inner cylinder 3.

[0031] In some embodiments of the present invention, the second inner swirling member is provided as a third impeller 15 sleeved on the outer wall of the manifold 16. There are no special requirements for the structure of the third impeller in the present invention, as long as it can strengthen the swirl to make the material swirl again. The present invention will not elaborate on this.

[0032] In some embodiments of the present invention, the distance between the installation position of the first inner swirling flow member and the mixture axial inlet 12 is 0 to 0.1 times the length of the inner cylinder 3. The distance between the installation positions of the first inner swirling flow member and the second inner swirling member in the height direction is 0.05 to 0.9 times the length of the inner cylinder 3.

[0033] On the basis of the foregoing disclosure, in some embodiments of the present invention, the two-phase separator includes an outer cylinder 4. The outer cylinder 4 is sleeved outside the inner cylinder 3 and a circular cavity 41 is formed between the outer cylinder 4 and the inner cylinder 3. The circular cavity 41 is used for circulating a heat exchange medium to perform a wall-type heat exchange with the inner swirling flow cavity 31. Thus, the two-phase separation device of the present invention integrates swirl separation and material cooling heat exchange, and can complete the quenching or waste heat recovery process while achieving efficient separation of the material. The present invention has the advantages of shortening the process flow, reducing the floor area of the equipment, and increasing the production intensity.

[0034] To enhance heat exchange, in some embodiments of the present invention, as Figure 6 shown, heat exchange fins are provided on the outer wall of the inner cylinder 3. Preferably, the heat exchange fins are provided as spiral heat exchange fins 5 extending along the axial direction of the inner cylinder 3.

[0035] In some embodiments of the present invention, the width of the spiral heat exchange fins 5 L w is 0.1 to 1 times the width of the inner swirling flow cavity 31, and the pitch L j is 0.01 to 1 times the total length of the outer cylinder 4, and the total height is 0.5 to 1 times the total length of the outer cylinder 4.

[0036] In some embodiments of the present invention, as Figure 1 shown, the inner cylinder 3 is provided as a straight cylinder, and the length-diameter ratio of the inner cylinder 3 is 1 to 100; or, as Figure 3As shown, the inner cylinder 3 includes a straight cylinder section and a conical cylinder section connected to the straight cylinder section. Among them, the proportion of the straight cylinder section in the length of the inner cylinder 3 is 0 to 1, and the angle between the cylinder wall of the conical cylinder section and the central axis of the inner cylinder 3 is 2.5° to 15°.

[0037] In some embodiments of the present invention, an outer swirl member is provided in the annular cavity 41, and the outer swirl member causes the heat exchange medium to form an axial swirl (outer swirl) in the annular cavity 41. In this way, the present invention has two flow spaces of inner swirl and outer swirl, integrating swirl separation and material cooling heat exchange into one, achieving efficient separation of materials while completing the quenching or waste heat recovery process, and at the same time improving the heat exchange efficiency with the help of the outer swirl member and the spiral heat exchange fins.

[0038] In some embodiments of the present invention, the outer swirl member includes Form C or Form D, where: Form C: As Figures 1 - 3 shown, the outer swirl member is provided as a tangential inlet for the heat exchange medium opened on the side wall of the outer cylinder 4, and the tangential inlet for the heat exchange medium is provided at the upper or lower part of the outer cylinder 4 to achieve co-current heat exchange or counter-current heat exchange with the material in the inner cylinder.

[0039] Form D: As Figures 4 - 5 shown, the outer swirl member is provided as a second impeller 9 sleeved on the inner cylinder 3, and both ends of the outer cylinder 4 are opened to form a working fluid axial through-port (reference numerals 13 or 14 in the figure) for passing the heat exchange medium.

[0040] In some embodiments of the present invention, in Form D, the distance between the installation position of the second impeller 9 and the axial through-port of the heat exchange medium at the upper end of the outer cylinder 4 is 0 to 0.98 times the length of the outer cylinder 4. The second impeller 9 includes 2 to 15 blades, the angle between the blades of the second impeller 9 and the oncoming flow direction of the heat exchange medium is -60° to 60°, the height of the blades of the second impeller 9 is 0.1 to 10 times the width, and the width of the blades of the second impeller 9 is 0.3 to 1 times the distance between the inner cylinder and the outer cylinder.

[0041] To improve the throughput and heat exchange / separation efficiency, in some embodiments of the present invention, multiple two-phase separators are provided, and the multiple two-phase separators are connected in series and / or in parallel to achieve multi-stage separation of the two-phase mixture. For example, multiple two-phase separators are connected in series. After the light components separated in the inner cylinder leave the upper unit through the overflow pipe, they can enter the next unit through the series pipeline again from the tangential inlet 2 of the mixture or the axial inlet 12 of the mixture, realizing multi-stage separation of the two-phase mixture. In this way, the present invention has good scalability, and multiple optimizations of throughput and processing performance can be easily achieved through series and / or parallel forms.

[0042] The present invention has no special requirements for the heat exchange medium, which can be at least one of water vapor, water, molten salt, and heat transfer oil commonly used in the prior art, and the present invention will not elaborate on this any further.

[0043] In some embodiments of the present invention, the two-phase material system to be separated is a gas-liquid, gas-solid, or liquid-solid two-phase mixture, such as the nitrobenzene hydrogenation process gas.

[0044] The advantages of the present invention will be illustrated by the following examples, but the present invention is not limited thereto.

[0045] Example 1 Adopt a two-phase separation device as shown in Figure 1 which includes a two-phase separator. The two-phase separator includes: an inner swirl member, an inner cylinder 3, and an inner swirl chamber 31 formed by surrounding the inner cylinder 3. A tapered body 6 that tapers upward is provided at the bottom end of the inner swirl chamber 31. The annular gap between the tapered body 6 and the chamber wall of the inner swirl chamber 31 forms a first outlet 11 for the heavy components; the tapered body 6 is set as a truncated cone and is coaxially arranged with the inner cylinder 3. The top end of the tapered body 6 extends upward to form a secondary swirl tube 18, and the end face opening at the bottom end of the tapered body 6 forms a second outlet 19 for the heavy components; a collecting tube 16 is spacedly covered on the upper end of the secondary swirl tube 18 to form a secondary separation section. A secondary swirl generating member is installed in the secondary separation section. One end of the secondary overflow pipe 20 penetrates through the collecting tube 16 and extends into the secondary swirl tube 18, and the other end extends out of the outer shape of the inner swirl chamber 31 to form a second outlet for the light components; an overflow pipe 10 is provided through the top wall of the inner swirl chamber 31. The overflow pipe 10 is sleeved outside the secondary overflow pipe 20. The annular gap between the secondary overflow pipe 20 and the overflow pipe 10 forms a first outlet for the light components. The secondary swirl generating member is set as a fourth impeller 17 sleeved on the secondary overflow pipe 20.

[0046] The inner swirl member includes a first inner swirl member and a second inner swirl member along the flow direction of the material to be separated in the inner swirl chamber 31. The first inner swirl member adopts form A: the first inner swirl member is set as a mixture tangential inlet 2 opened in the tangential direction of the inner cylinder 3; the second inner swirl member is set as a third impeller 15 sleeved on the outer wall of the collecting tube 16. The two-phase separator includes an outer cylinder 4 sleeved outside the inner cylinder 3 and having an annular cavity 41 formed between the outer cylinder 4 and the inner cylinder 3. A spiral heat exchange fin 5 is arranged along the axial direction of the inner cylinder 3. An outer swirl member is provided in the annular cavity 41. The outer swirl member adopts form C: the outer swirl member is set as a heat exchange medium tangential inlet opened in the tangential direction of the side wall of the outer cylinder 4.

[0047] The inner cylinder 3 is set as a straight cylinder with a length-to-diameter ratio of 9; the diameter of the outer cylinder 4 is 2.5 times that of the inner cylinder 3, and the length is 0.83 times that of the inner cylinder 3; the large end diameter of the tapered body 6 R c is 0.6 times the bottom end diameter of the inner cylinder 3, and the height of the tapered body 6L h It is 0.09 times the length of the inner cylinder 3; the distance between the installation positions of the first inner swirl member and the second inner swirl member in the height direction is 0.45 times the length of the inner cylinder tube; the width of the spiral heat exchange fin 5 L w is 0.7 times the width of the inner swirl chamber 31, and the pitch L j is 0.05 times the total length of the outer cylinder 4, and the total height is 0.84 times the total length of the outer cylinder 4.

[0048] The mixture to be separated is the crude product of the gas-phase nitrobenzene hydrogenation unit. The feed temperature is 165 °C, and the flow rate is 450 m 3 / h. After heat exchange and condensation and simultaneous swirl separation by the device of the present invention, the temperature is 50 °C. The crude aniline product condenses into a liquid product, which is separated from other non-condensable components. The separation efficiency of the liquid product (aniline, water) is 99.5%, and the purity of the gaseous product recycle hydrogen is 99.2%.

[0049] Example 2 Different from Example 1, the secondary separation section does not install the auxiliary swirl member (the fourth impeller 17), and the rest is the same as Example 1.

[0050] Result: The separation efficiency of the liquid product (aniline, water) is 91.5%, and the purity of the gaseous product recycle hydrogen is 91.5%.

[0051] Example 3 Different from Example 1, the second inner swirl member (the third impeller 15) is not provided in the inner swirl chamber 31, and the rest is the same as Example 1.

[0052] Result: The separation efficiency of the liquid product (aniline, water) is 95.2%, and the purity of the gaseous product recycle hydrogen is 96.3%.

[0053] Comparative Example 1 Different from Example 1, no secondary separation is provided in the inner swirl chamber 31, that is, there are no structures such as the secondary swirl tube 18, the secondary overflow tube 20, the manifold 16, the fourth impeller 17, the second outlet for heavy components 19, and the second outlet for light components, etc. The rest is the same as Example 1.

[0054] Result: The separation efficiency of the liquid product (aniline, water) is 90.1%, and the purity of the gaseous product recycle hydrogen is 90.3%.

[0055] The preferred embodiments of the present invention have been described in detail above in conjunction with the accompanying drawings. However, the present invention is not limited thereto. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solutions of the present invention, including combinations of each specific technical feature in any suitable manner. To avoid unnecessary repetition, the present invention will not separately describe various possible combination methods. However, these simple modifications and combinations should equally be regarded as the content disclosed by the present invention and fall within the protection scope of the present invention.

Claims

1. A two-phase separation device, characterized in that, The two-phase separation device includes a two-phase separator, and the two-phase separator includes: An inner cylinder body (3) is provided with an inner swirl chamber (31) and an inner swirl member. The inner swirl member is used to form a downward swirl in the inner swirl chamber (31) to achieve primary separation of the two-phase mixture, obtaining a primary separation inner swirl and a primary separation outer swirl; A secondary swirl tube (18) is arranged in the inner swirl chamber (31). The upper end of the secondary swirl tube (18) is covered with a collecting tube (16) to form a secondary separation section. A secondary swirl generating member is installed in the secondary separation section. The secondary swirl generating member is used to introduce the primary separation inner swirl from the annular gap between the secondary swirl tube (18) and the collecting tube (16) into the secondary separation section and form a swirl for secondary separation.

2. The two-phase separation device according to claim 1, characterized in that, A tapered body (6) that tapers upward is arranged at the bottom end of the inner swirl chamber (31). The annular gap between the tapered body (6) and the chamber wall of the inner swirl chamber (31) forms a first outlet (11) for the heavy components; and / or The top end of the tapered body (6) extends upward to form a secondary swirl tube (18), and the end face opening at the bottom end of the tapered body (6) forms a second outlet (19) for the heavy components.

3. The two-phase separation device according to claim 1 or 2, characterized in that, One end of a secondary overflow pipe (20) penetrates through the collecting tube (16) and extends into the secondary swirl tube (18), and the other end extends out of the outer shape of the inner swirl chamber (31) to form a second outlet for the light components; and / or An overflow pipe (10) is provided through the top wall of the inner swirl chamber (31). The overflow pipe (10) is sleeved outside the secondary overflow pipe (20). The annular gap between the secondary overflow pipe (20) and the overflow pipe (10) forms a first outlet for the light components; Preferably, the secondary swirl generating member is arranged as a fourth impeller (17) sleeved on the secondary overflow pipe (20).

4. The two-phase separation device according to claim 1, characterized in that The inner swirl member includes a first inner swirl member and a second inner swirl member along the material flow direction. Among them, the two-phase material is swirled once by the first inner swirl member and then swirled twice by the second inner swirl member; Preferably, the first inner swirl member includes Form A or Form B, where: Form A: The first inner swirl member is arranged as a tangential mixture inlet (2) opened on the tangent of the inner cylinder body (3); Form B: The first inner swirl member is arranged as a first impeller (8) sleeved on the overflow pipe (10). The gap between the overflow pipe (10) and the inner cylinder body (3) forms an axial mixture inlet (12) for feeding the two-phase mixture.

5. The two-phase separation device according to claim 4, characterized in that The second inner swirl member is arranged as a third impeller (15) sleeved on the outer wall of the collecting tube (16); and / or The distance between the installation position of the first inner swirl member and the axial mixture inlet (12) is 0 to 0.1 times the length of the inner cylinder body (3); and / or The distance between the installation positions of the first inner swirl member and the second inner swirl member in the height direction is 0.05 to 0.9 times the length of the inner cylinder body (3).

6. The two-phase separation device according to claim 1, characterized in that, The two-phase separator includes an outer cylinder body (4), the outer cylinder body (4) is sleeved outside the inner cylinder body (3), and an annular cavity (41) is formed between the outer cylinder body (4) and the inner cylinder body (3), and the annular cavity (41) is used for flowing a heat exchange medium to perform a wall heat exchange with the inner swirl chamber (31); and / or Heat exchange fins are arranged on the outer wall of the inner cylinder body (3), preferably the heat exchange fins are spiral heat exchange fins (5) extending along the axial direction of the inner cylinder body (3); and / or The inner cylinder body (3) is a straight cylinder, preferably the length-diameter ratio of the inner cylinder body (3) is 1 to 100; or The inner cylinder body (3) includes a straight cylinder section and a conical cylinder section connected to the straight cylinder section. Among them, the proportion of the straight cylinder section in the length of the inner cylinder body (3) is 0 to 1, preferably the included angle between the cylinder wall of the conical cylinder section and the central axis of the inner cylinder body (3) is 2.5° to 15°.

7. The two-phase separation device according to claim 6, characterized in that, An outer swirl member is arranged in the annular cavity (41), and the outer swirl member makes the heat exchange medium form an axial swirl in the annular cavity (41); and / or The diameter of the outer cylinder body (4) is 1.1 to 3 times the diameter of the inner cylinder body (3), and the length is 0.5 to 0.98 times the length of the inner cylinder body (3); and / or The width of the spiral heat exchange fin (5) L w is 0.1 to 1 times the width of the inner swirling flow cavity (31), and the pitch L j is 0.01 to 1 times the total length of the outer cylinder (4), and the total height is 0.5 to 1 times the total length of the outer cylinder (4).

8. The two-phase separation device according to claim 7, characterized in that The outer swirl member includes Form C or Form D, where: Form C: The outer swirl member is arranged as a tangential inlet for the heat exchange medium opened on the side wall of the outer cylinder body (4), and the tangential inlet for the heat exchange medium is arranged at the upper part or the lower part of the outer cylinder body (4); Form D: The outer swirl member is arranged as a second impeller (9) sleeved on the inner cylinder body (3), and the two ends of the outer cylinder body (4) are opened to form a working medium axial through port (13) for passing the heat exchange medium.

9. The two-phase separation device according to claim 8, characterized in that, In Form D, The distance between the installation position of the second impeller (9) and the axial through port of the heat exchange medium at the upper end of the outer cylinder body (4) is 0 to 0.98 times the length of the outer cylinder body (4); The second impeller (9) includes 2 to 15 blades; and / or The included angle between the blades of the second impeller (9) and the oncoming flow direction of the heat exchange medium is -60° to 60°; and / or The height of the blades of the second impeller (9) is 0.1 to 10 times the width; and / or The width of the blades of the second impeller (9) is 0.3 to 1 times the distance between the inner cylinder and the outer cylinder.

10. The two-phase separation device according to any one of claims 1-9, characterized in that, A plurality of two-phase separators are provided, and the plurality of two-phase separators are connected in series and / or in parallel to achieve multi-stage separation of the two-phase mixture; and / or The two-phase mixture to be separated is a gas-liquid, gas-solid or liquid-solid two-phase mixture.

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