Double-fluid swirl injection temperature reduction device and method

Abstract

The invention discloses a double-fluid swirl injection temperature reduction device which comprises a receiving chamber, a contraction section, a mixing section and an expansion section, a high-pressure liquid inlet upper header is arranged at the upper end of the receiving chamber, a high-temperature gas inlet is formed in the side face of the receiving chamber, and a cage-shaped heat exchange tube is arranged in the receiving chamber; the upper end of the cage-shaped heat exchange tube is connected with a high-pressure liquid inlet upper header, the lower end of the cage-shaped heat exchange tube is connected with the upper end of a heat exchange tube lower header, and the lower end of the heat exchange tube lower header is connected with a nozzle; a rotational flow piece is arranged in the heat exchange tube lower collecting tube; high-pressure and low-temperature liquid enters the cage-shaped heat exchange tube, high-temperature and low-pressure gas transversely washes the cage-shaped heat exchange tube for primary heat exchange, and the high-pressure and low-temperature liquid is converted into high-pressure two-phase flow in the heat exchange process; the high-pressure two-phase flow and the high-temperature low-pressure gas are subjected to second-stage heat exchange through the rotational flow piece, and then the high-temperature low-pressure gas is sprayed out after being boosted through the nozzle. The pressure energy of a high-pressure medium can be fully utilized, sufficient heat exchange is achieved, a low-pressure medium is boosted, sufficient mixing of the medium is guaranteed, and the functions of temperature reduction mixing and boosting are integrated.

Description

Technical Field

[0001] The invention belongs to the technical field of temperature reduction mixing devices and relates to a dual-fluid swirl injection temperature reduction device and method. Background Art

[0002] The cooling and mixing devices currently used are divided into Venturi opening type and atomizing water seal type according to different application processes. Among them, the former is more common in thermal power plants, while other chemical plants have adopted the latter more in recent years. The processes used by both have a certain pressure loss. The former has a simple structure and poor atomization. It uses interception to carry out air flow impact mixing and cooling, which has a large pressure loss. The atomization and pressure loss conditions of the latter have improved a lot, but there is still pressure loss, and in order to adjust to a reasonable atomization pressure range, the high-pressure liquid medium needs to be depressurized, wasting the pressure energy of the high-quality liquid medium. The characteristics of the above devices often conflict with the process requirements of downstream equipment that require a certain pressure head, and it is necessary to add a booster pump or other booster devices, which consumes additional electricity or provides a high-pressure kinetic energy medium as power. Summary of the invention

[0003] The purpose of the present invention is to overcome the above-mentioned defects and provide a dual-fluid swirl jet cooling device and method, which solves the technical problem that the existing cooling and mixing devices waste the pressure energy of the high-pressure medium and the thermal energy of the high-temperature medium. The present invention can fully utilize the pressure energy of the high-pressure medium, fully exchange heat, increase the pressure of the low-pressure medium and ensure sufficient mixing of the medium, and has both cooling, mixing and pressure-increasing functions.

[0004] In order to achieve the above-mentioned object of the invention, the present invention provides the following technical solutions:

[0005] A dual-fluid swirl jet cooling device, comprising a receiving chamber, a contraction section, a mixing section and an expansion section connected in sequence from top to bottom, characterized in that an upper header for a high-pressure liquid inlet is provided at the upper end of the receiving chamber, a high-temperature gas inlet is provided at the side of the receiving chamber, and a cage-shaped heat exchange tube is provided inside the receiving chamber;

[0006] The upper end of the cage-shaped heat exchange tube is connected to the upper header of the high-pressure liquid inlet, the lower end of the cage-shaped heat exchange tube is connected to the upper end of the lower header of the heat exchange tube, and the lower end of the lower header of the heat exchange tube is connected to the nozzle;

[0007] A swirl element is provided in the lower header of the heat exchange tube;

[0008] High-pressure and low-temperature liquid enters the cage-shaped heat exchange tube from the high-pressure liquid inlet upper header, and high-temperature and low-pressure gas enters the receiving chamber from the high-temperature gas inlet, horizontally flushing the cage-shaped heat exchange tube for primary heat exchange. During the heat exchange process, the high-pressure and low-temperature liquid is partially vaporized and converted into a high-pressure and low-temperature two-phase flow; the high-pressure and low-temperature two-phase flow is ejected from the nozzle through the swirl element, and the high-pressure two-phase flow and the high-temperature and low-pressure gas are in direct contact at the nozzle outlet for secondary heat exchange.

[0009] Furthermore, the cage-shaped heat exchange tube includes a plurality of heat exchange tubes evenly distributed along the circumference of the receiving chamber;

[0010] Each heat exchange tube includes an upper section, a middle section and a lower section, wherein the middle section is parallel to the axis of the receiving chamber, and the angles between the upper section and the lower section and the axis of the receiving chamber are 30° to 60°.

[0011] Furthermore, the distance between each heat exchange tube and the inner wall of the receiving chamber is 1 / 4 to 1 / 2 of the diameter of the receiving chamber.

[0012] Further, the high temperature gas inlet is disposed eccentrically relative to the receiving chamber;

[0013] The primary swirl of the high-temperature and low-pressure gas after entering from the high-temperature gas inlet and the secondary swirl formed by the high-pressure and low-temperature two-phase flow at the swirl element are in opposite directions.

[0014] Further, the central axis of the high temperature gas inlet is perpendicular to the central axis of the receiving chamber;

[0015] Assume that the distance between the central axis of the high-temperature gas inlet and the contact surface of the matching flange on the receiving chamber is d1, and the distance between the upper and lower pairs of flange contact surfaces in the receiving chamber is d2, d1 = 1 / 3d2 ~ 1 / 2d2.

[0016] Further, it also includes a central support cylinder;

[0017] The upper and lower ends of the central support tube are both closed. The central support tube is installed between the lower end of the high-pressure liquid inlet upper header and the upper end of the heat exchange tube lower header, and is located inside the cage-shaped heat exchange tube;

[0018] The central support tube is a hollow structure, and air holes for balancing the internal and external gas pressures are arranged on the side walls of the central support tube.

[0019] Furthermore, the central support tube includes an upper section, a middle section and a lower section, wherein the middle section is a cylindrical section, and the upper section and the lower section are both conical sections;

[0020] The diameter of the cylindrical section of the central support tube is 1 / 2 to 2 / 3 of the diameter of the receiving chamber.

[0021] The axes of the high-pressure liquid inlet upper header, the central support tube, the heat exchange tube lower header, the nozzle and the receiving chamber are collinear.

[0022] Furthermore, the distance between the swirl element and the lower end of the cage-shaped heat exchange tube is greater than or equal to the diameter of the lower header of the heat exchange tube;

[0023] The nozzle is located above or below the inlet of the mixing section, and the distance between the nozzle and the inlet of the mixing section is ±1 times the diameter of the mixing section;

[0024] The ratio of the length to the diameter of the mixing section is ≥3.

[0025] Furthermore, the nozzle is a two-phase flow nozzle, and the flow size of the nozzle throat is ≥5mm;

[0026] The nozzle has an outlet expansion section, and the outlet expansion angle is 7° to 20°.

[0027] A dual-fluid swirl jet cooling method is implemented by using the dual-fluid swirl jet cooling device, comprising:

[0028] High-pressure and low-temperature liquid enters the cage-shaped heat exchange tube from the high-pressure liquid inlet upper header to achieve liquid rectification and distribution;

[0029] High-temperature, low-pressure gas enters the receiving chamber from the high-temperature gas inlet and flushes the cage-shaped heat exchange tubes horizontally for primary heat exchange;

[0030] The high-pressure and low-temperature two-phase flow generated by the cage-shaped heat exchange tube after the first-stage heat exchange is collected in the lower header of the heat exchange tube;

[0031] The high-pressure and low-temperature two-phase flow ejected from the nozzle through the swirl element is rectified and distributed, and performs the second-stage heat exchange with the high-temperature and low-pressure gas;

[0032] The nozzle cooperates with the contraction section and the mixing section to increase the pressure of the high-temperature and low-pressure gas.

[0033] Compared with the prior art, the present invention has at least one of the following beneficial effects:

[0034] (1) The present invention creatively proposes a dual-fluid swirl jet cooling device, which fully utilizes the pressure energy of the high-pressure medium, fully exchanges heat, and pressurizes the low-pressure medium and ensures sufficient mixing of the medium through two swirls, two-stage heat exchange, one-stage atomization and pressure increase, and has both cooling, mixing and pressure increase functions;

[0035] (2) The present invention designs a cage-shaped heat exchange tube close to the wall of the receiving chamber, which is conducive to full contact and lateral convection flow between the gas medium and the liquid medium, thereby enhancing the heat transfer coefficient;

[0036] (3) The present invention can enhance the structural stability of the cage-shaped heat exchange tube through the central support tube, and at the same time play a role in stabilizing and rectifying the flow field of the high-temperature medium, thereby enhancing the heat exchange with the low-temperature medium in the cage-shaped heat exchange tube;

[0037] (4) The present invention uses a swirl element to distribute and rectify the flow field of gas and liquid media, so that the two-phase medium can be sprayed out at a high speed and stably, thereby performing stable suction work on the high-temperature medium after preliminary cooling;

[0038] (5) The present invention adopts a structure in which a two-way flow nozzle and a contraction section cooperate to play the role of jet suction, secondary temperature reduction, and medium mixing, which can realize the suction and pressure increase of low-pressure and high-temperature media, increase the pressure of the high-temperature media to meet the downstream demand for pressure head, and achieve the purpose of saving the pressure energy of the high-pressure medium and the thermal energy of the high-temperature medium;

[0039] (6) The present invention enhances the atomization of droplets in the bidirectional flow through the coordination of the nozzle and the contraction section, creates good conditions for heat exchange and cooling in the downstream, and ensures sufficient mixing of gas and liquid. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] Figure 1 It is a schematic diagram of a dual-fluid swirl injection cooling device of the present invention;

[0041] In the figure, 1-high-pressure liquid inlet upper header, 2-cage-shaped heat exchange tube, 3-central support tube, 4-receiving chamber, 5-high-temperature gas inlet, 6-lower header of heat exchange tube, 7-swirl element, 8-nozzle, 9-contraction section, 10-mixing section, 11-expansion section. DETAILED DESCRIPTION

[0042] The following detailed description of the present invention will make the features and advantages of the present invention more clear and explicit.

[0043] The word "exemplary" is used exclusively herein to mean "serving as an example, embodiment, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. Although various aspects of the embodiments are shown in the drawings, the drawings are not necessarily drawn to scale unless otherwise noted.

[0044] The present invention relates to an internal flow field reorganization technology that integrates the functions of injection boosting and temperature reduction and mixing, and specifically relates to a jet cooling device that can fully mix and cool during operation, and in which a dual-fluid medium is used as a power medium for boosting. The internal flow field of the dual-fluid swirl jet cooling device of the present invention fully utilizes the pressure energy of the high-pressure medium, fully exchanges heat, boosts the pressure of the low-pressure medium, and ensures sufficient mixing of the medium, and has both cooling, mixing, and pressure-boosting functions.

[0045] The present invention is a method for combining a cage-shaped heat exchange tube and a two-phase flow swirl nozzle, and its core process flow includes an energy conversion process of two swirls, one atomization, and two-stage heat exchange. The method includes the following:

[0046] (1) The incoming high-pressure and low-temperature liquid flows in a dispersed manner along the circumferentially evenly distributed cage-shaped heat exchange structure, rectifying and distributing the upstream liquid;

[0047] (2) The incoming high-temperature, low-pressure gas enters the receiving chamber using an eccentric swirl flow, which scours the cage-shaped heat exchange tubes horizontally to enhance the primary heat exchange;

[0048] (3) The two-phase flow fluid generated after the first stage of heat exchange in the cage-shaped heat exchange tube is collected in the lower header;

[0049] (4) A central support tube that is not connected to other components is set at the center of the cage-shaped heat exchange tube.

[0050] (5) A two-phase flow swirl rectifying component is provided in the lower header to rectify and distribute the gas-liquid two-phase flow and stabilize the flow field.

[0051] (6) A two-phase flow nozzle is provided in the lower section of the lower header, which cooperates with the mixing and contracting section of the shell to increase the pressure of the low-pressure medium.

[0052] The core idea of ​​the technical solution of the present invention lies in the integration of the technical functions of injection pressure boosting and temperature reduction mixing.

[0053] The present invention provides a dual-fluid swirl jet cooling device, wherein the angle between the upper and lower parts of the cage-shaped heat exchange tube and the axis is about 30° to 60°, so as to avoid the generation of a gas medium retention area and release thermal stress. The cage-shaped heat exchange tube is close to the container wall of the receiving chamber and is evenly distributed on the AA section. A primary heat exchange process occurs in this area, in which the high-pressure liquid medium is partially vaporized and changes from a liquid phase medium to a dual-fluid medium.

[0054] The low-pressure and high-temperature gas swirl flows eccentrically into the receiving chamber and flushes the cage-shaped heat exchanger horizontally, thereby strengthening the heat exchange between the low-pressure and high-temperature gas and the high-pressure and low-temperature liquid and promoting the vaporization of the liquid medium.

[0055] A central support tube is provided between the cage-shaped heat exchange tube and the lower header. The central support tube supports and stabilizes the internal parts, and at the same time plays a role in rectifying the flow field in the inlet area, thereby enhancing the heat exchange of high-temperature gas in the cage-shaped heat exchange tube area.

[0056] A swirl rectifying component is arranged in the header upstream of the nozzle, and the nozzle cooperates with the mixing and contracting section to use the high-pressure two-phase flow as the power medium to perform secondary heat exchange cooling and pressure-increasing on the low-pressure and high-temperature gas.

[0057] More specifically, Figure 1 The present invention discloses a dual-fluid swirl jet cooling device, comprising: a cage-shaped heat exchange tube 2, a high-temperature gas inlet 5, a heat exchange tube lower header 6, a swirl element 7 provided on the heat exchange tube lower header 6, a nozzle 8 and a mixing contraction section 9. High-pressure and low-temperature medium enters the cage-shaped heat exchange tube 2 from the inlet 1 in a dispersed manner, and the angle between the upper and lower parts of the cage-shaped heat exchange tube and the axis is about 30° to 60°, so as to avoid the generation of a gas medium retention area and release thermal stress. The cage-shaped heat exchange tube 2 is close to the container wall of the receiving chamber 4 and is evenly distributed on the AA section.

[0058] The low-pressure high-temperature gas enters the receiving chamber 4 eccentrically from the low-pressure high-temperature gas inlet 5. The high-temperature low-pressure gas enters the receiving chamber in a swirl flow along the container wall and flushes the cage-shaped heat exchanger horizontally. The distance between the central axis of the low-pressure high-temperature gas inlet 5 and the upper end line of the receiving chamber is 1 / 3 to 1 / 2 of the length between the contact surfaces of the upper and lower pairs of flanges of the receiving chamber.

[0059] In the present invention, the high-pressure low-temperature medium has a pressure of ≥3500 kpaA and a temperature of ≤150°C, and the low-pressure high-temperature gas has a pressure of ≤101 kpaA and a temperature of ≥450°C.

[0060] The receiving chamber is generally divided into three sections: upper, middle and lower. The upper section and the middle section, as well as the middle section and the lower section are connected by upper and lower flanges respectively, so that the internal components can be inspected and replaced or the receiving chamber can be replaced. The above receiving chamber length refers to the distance between the contact surfaces of the upper and lower pairs of flanges.

[0061] The lower ends of the cage-shaped heat exchange tubes 2 are collected at the lower heat exchange tube header 6. A central support tube 3 is provided in the middle of the cage-shaped heat exchange tube 2. The central support tube is composed of upper and lower conical sections and a middle straight section to release thermal stress. The central support tube 3 is mechanically connected to the lower heat exchange tube header 6 and the upper header 1 for the high-pressure liquid inlet but not connected. Air holes are left on the central support tube 3 to balance the internal and external pressures. The diameter 3 of the central support tube is 1 / 2 to 2 / 3 of the diameter of the receiving chamber 4.

[0062] A swirl element 7 is provided inside the lower header 6 of the heat exchange tubes. The distance between the swirl element 7 and the lower end of the cage-shaped heat exchange tubes 2 is at least 1 times the diameter of the lower header 6 .

[0063] A nozzle 8 is provided at the lower end of the swirl element 7 , and the distance between the nozzle and the inlet of the mixing section 10 is approximately ±1 times the diameter of the mixing section 10 .

[0064] The nozzle 8 is a two-phase flow nozzle, and the flow size of the nozzle throat is ≥5mm. Due to the expansion of the two-phase flow, the nozzle 8 has an outlet expansion section, and the outlet expansion angle is 7° to 20°.

[0065] The ratio of the length to the diameter of the mixing section 10 is ≥3.

[0066] The present invention arranges cage-shaped evenly distributed heat exchange tubes near the wall surface at the high-temperature medium inlet area, and the cold and hot mediums undergo a primary heat exchange, the high-temperature medium outside the heat exchange tubes is preliminarily cooled, and a part of the cooling liquid medium in the heat exchange tubes is evaporated to form a two-phase medium. This heat exchange is an indirect heat exchange of the cold and hot mediums without contact.

[0067] The specific volume of the two-phase medium is greater than that of the pure liquid medium. The heat energy of the high-temperature medium is converted into the kinetic energy of the low-temperature medium, which is beneficial to the downstream suction work of the high-temperature low-pressure medium. At the same time, the cooling of the high-temperature gas reduces its specific volume, thereby reducing the suction work load. The pressure energy of the cooling medium and the heat energy of the high-temperature medium are fully utilized.

[0068] The high-temperature gas medium eccentrically swirls into the receiving chamber, fully contacts and flows in lateral convection with the cage-shaped heat exchange tubes evenly distributed near the wall, thus enhancing the heat transfer coefficient. At the downstream nozzle outlet section, the high-temperature medium continues to flow close to the wall in a circular tornado, which helps to slow down the scouring of the mixing section 10 wall by the unvaporized liquid medium in the nozzle, thus extending the service life of the equipment.

[0069] The present invention provides a central support tube in the middle of the cage-shaped heat exchange tube. First, the dual-fluid nozzle is prone to vibration during operation, and the support tube plays a role in strengthening the structural stability of the cage-shaped heat exchange tube to avoid vibration during operation. In addition, the cooperation between the central support tube and the wall of the equipment plays a role in stabilizing and rectifying the flow field of the high-temperature medium, so that the high-temperature medium flows in an annular direction close to the wall, thereby enhancing the heat exchange with the low-temperature medium in the cage-shaped heat exchange tube.

[0070] The present invention uses a swirl element to distribute and rectify the flow field of gas and liquid media. The dual-fluid medium is directly ejected from the nozzle, which is prone to pulse-like unstable vibration. Through the rectification of the flow field by the swirl element, the liquid medium flows along the nozzle wall, and the gaseous medium is ejected from the center of the nozzle to form an air cavity. Thus, the dual-phase medium is ejected at a high speed and stably, and then the high-temperature medium after preliminary cooling is stably sucked and worked.

[0071] The present invention adopts a structure that matches a two-way flow nozzle and a contraction section. The structure plays the role of injection suction, secondary temperature reduction, and medium mixing. Due to the presence of high-pressure gas in the two-phase flow medium ejected from the nozzle, the structure can achieve the suction and pressure-increasing effect on the low-pressure high-temperature medium. By increasing the pressure of the high-temperature medium, the downstream demand for the pressure head is met, which plays an energy-saving role in saving the pressure energy of the high-pressure medium and the thermal energy of the high-temperature medium. The presence of atomized liquid medium in the two-phase flow medium can directly contact with the high-temperature medium for secondary heat exchange. Through the non-contact primary heat exchange upstream and the direct contact secondary heat exchange of the nozzle outlet, the heat exchange of the cold and hot media is sufficient to achieve the purpose of cooling the high-temperature medium.

[0072] The present invention can enhance the atomization of droplets in bidirectional flow through the cooperation of the nozzle and the contraction section. The primary swirl of the eccentric inlet of the high-temperature medium and the secondary swirl of the swirl rectifying member upstream of the nozzle cooperate with each other, and the two swirls rotate in opposite directions, so that the nozzle outlet contraction section forms an annular air-water structure of air-water-air, and the impact of the inner and outer double-layer airflows on the droplets can achieve the most ideal atomization effect, creating good conditions for heat exchange and cooling downstream, so that the gas and liquid are fully mixed.

[0073] Embodiment 1:

[0074] High-temperature low-pressure steam capacity is 5000kg / h, working temperature is 450℃, inlet working pressure is 101kpa. Low-temperature high-pressure liquid capacity is 1200kg / h, temperature is 150℃, pressure is 3500kpa.

[0075] The outlet pressure is required to be no less than 100 kpa and the temperature is required to be no more than 180°C. Common designs cannot meet such low pressure loss requirements. Through the design proposed by the present invention, there is no pressure drop at the final outlet, but the pressure can be increased to 118 kpa and the temperature can be reduced to 178°C, meeting the process parameter requirements.

[0076] The receiving room of the equipment is equipped with 8 cage-shaped heat exchange tubes, arranged as shown in the cross section Figure 1 In the AA cross-sectional diagram, the heat exchange tubes are set close to the tube wall and are evenly distributed in a circle. The two ends of the receiving chamber are flange-connected, and the cage-shaped heat exchange tubes and nozzles can be regularly inspected and repaired, or they can be reset and replaced according to changes in specific working conditions. The setting of this cage-shaped heat exchanger obtains a two-phase flow motive medium with stronger working capacity through a first-stage heat exchange. The saturated steam in the two-phase flow medium is about 550kg / h, and the liquid mass is about 650kg / h. In addition, the cooling of the high-temperature gas reduces the gas volume flow rate from about 460m 3 / h reduced to about 360m 3 / h, reducing the flow rate and pressure loss, while alleviating the work load of the downstream power medium.

[0077] After the two-phase flow medium merges into the lower header 6 of the heat exchange tube, the flow of the gas-liquid two-phase medium in the pipeline is prone to pulsation and vibration. The present invention relies on the central support tube 3 on the one hand, and the swirl element 7 in the lower header on the other hand to solve the above problems. Due to the different specific gravities of gas and liquid, they will be roughly separated after passing through the swirl element, with the liquid with a larger specific gravity close to the tube wall and the gas with a smaller specific gravity close to the middle position, thus forming a stable flow field of liquid surrounding gas.

[0078] The two-phase flow continues to flow downward through the nozzle 8. The flow velocity in this area increases to the critical sound velocity, the volume expansion pressure decreases, and the liquid continues to vaporize in this area. The entire nozzle area will undergo throttling expansion, and a large amount of absorbed heat will be exchanged with the high-temperature medium. If the traditional pure liquid nozzle under non-depressurization conditions is used, the minimum size of each nozzle hole is only about 2.7 mm, which is very easy to clog and wear. In serious cases, it is necessary to stop the operation for maintenance. The narrowest point of the two-phase flow under equal quality is expanded to about 5 mm or more, which basically solves the problem of liquid impurity clogging.

[0079] The present invention has been described in detail above in conjunction with specific implementations and exemplary examples, but these descriptions cannot be understood as limiting the present invention. Those skilled in the art understand that, without departing from the spirit and scope of the present invention, a variety of equivalent substitutions, modifications or improvements may be made to the technical solution of the present invention and its implementation methods, all of which fall within the scope of the present invention. The scope of protection of the present invention shall be subject to the attached claims.

[0080] The contents not described in detail in the specification of the present invention belong to the common knowledge of those skilled in the art.

Claims

1. A dual-fluid swirl jet cooling device, comprising a receiving chamber (4), a contraction section (9), a mixing section (10) and an expansion section (11) connected in sequence from top to bottom, characterized in that: A high-pressure liquid inlet upper header (1) is provided at the upper end of the receiving chamber (4), a high-temperature gas inlet (5) is provided at the side of the receiving chamber (4), and a cage-shaped heat exchange tube (2) is provided inside the receiving chamber (4); The upper end of the cage-shaped heat exchange tube (2) is connected to the high-pressure liquid inlet upper header (1), the lower end of the cage-shaped heat exchange tube (2) is connected to the upper end of the heat exchange tube lower header (6), and the lower end of the heat exchange tube lower header (6) is connected to the nozzle (8); A swirl element (7) is provided in the lower header (6) of the heat exchange tube; High-pressure and low-temperature liquid enters the cage-shaped heat exchange tube (2) from the high-pressure liquid inlet upper header (1), and high-temperature and low-pressure gas enters the receiving chamber (4) from the high-temperature gas inlet (5), and laterally flushes the cage-shaped heat exchange tube (2) to perform primary heat exchange. During the heat exchange process, the high-pressure and low-temperature liquid is partially vaporized and converted into a high-pressure and low-temperature two-phase flow; the high-pressure and low-temperature two-phase flow is ejected from the nozzle (8) through the swirl element (7), and the high-pressure two-phase flow and the high-temperature and low-pressure gas are in direct contact at the nozzle (8) outlet to perform secondary heat exchange.

2. A dual-fluid swirl jet cooling device according to claim 1, characterized in that: The cage-shaped heat exchange tube (2) comprises a plurality of heat exchange tubes evenly distributed along the circumference of the receiving chamber (4); Each heat exchange tube comprises an upper section, a middle section and a lower section, wherein the middle section is parallel to the axis of the receiving chamber (4), and the angles between the upper section and the lower section and the axis of the receiving chamber (4) are 30° to 60°.

3. A dual-fluid swirl jet cooling device according to claim 2, characterized in that: The distance between each heat exchange tube and the inner wall of the receiving chamber (4) is 1 / 4 to 1 / 2 of the diameter of the receiving chamber (4).

4. A dual-fluid swirl jet cooling device according to claim 1, characterized in that: The high temperature gas inlet (5) is eccentrically arranged relative to the receiving chamber (4); The primary swirl flow after the high-temperature low-pressure gas enters from the high-temperature gas inlet (5) and the secondary swirl flow formed by the high-pressure low-temperature two-phase flow at the swirl element (7) are in opposite directions.

5. The dual-fluid swirl jet cooling device according to claim 1, characterized in that: The central axis of the high-temperature gas inlet (5) is perpendicular to the central axis of the receiving chamber (4); Assume that the distance between the central axis of the high-temperature gas inlet (5) and the contact surface of the matching flange on the receiving chamber (4) is d1, and the distance between the upper and lower pairs of flange contact surfaces of the receiving chamber (4) is d2, d1 = 1 / 3d2 ~ 1 / 2d2.

6. The dual-fluid swirl jet cooling device according to claim 1, characterized in that: Also includes a central support cylinder (3); The upper and lower ends of the central support tube (3) are both closed. The central support tube (3) is installed between the lower end of the high-pressure liquid inlet upper header (1) and the upper end of the heat exchange tube lower header (6), and is located inside the cage-shaped heat exchange tube (2); The central support tube (3) is a hollow structure, and a gas hole for balancing the internal and external gas pressures is provided on the side wall of the central support tube (3).

7. A dual-fluid swirl jet cooling device according to claim 6, characterized in that: The central support tube (3) comprises an upper section, a middle section and a lower section, wherein the middle section is a cylindrical section, and the upper section and the lower section are both conical sections; The diameter of the cylindrical section of the central support tube (3) is 1 / 2 to 2 / 3 of the diameter of the receiving chamber (4). The axes of the high-pressure liquid inlet upper header (1), the central support tube (3), the heat exchange tube lower header (6), the nozzle (8) and the receiving chamber (4) are collinear.

8. The dual-fluid swirl jet cooling device according to claim 1, characterized in that: The distance between the swirl element (7) and the lower end of the cage-shaped heat exchange tube (2) is greater than or equal to the diameter of the lower header (6) of the heat exchange tube; The nozzle (8) is located above or below the inlet of the mixing section (10), and the distance between the nozzle (8) and the inlet of the mixing section (10) is ±1 times the diameter of the mixing section (10); The ratio of the length to the diameter of the mixing section (10) is ≥3.

9. The dual-fluid swirl jet cooling device according to claim 1, characterized in that: The nozzle (8) is a two-phase flow nozzle, and the flow size of the nozzle throat is ≥5mm; The nozzle (8) has an outlet expansion section, and the outlet expansion angle is 7° to 20°.

10. A dual-fluid swirl jet cooling method, characterized in that: The dual-fluid swirl jet cooling device according to any one of claims 1 to 9 is implemented, comprising: High-pressure low-temperature liquid enters the cage-shaped heat exchange tube (2) from the high-pressure liquid inlet upper header (1), thereby achieving liquid rectification and distribution; High-temperature low-pressure gas enters the receiving chamber (4) from the high-temperature gas inlet (5) and laterally flushes the cage-shaped heat exchange tube (2) to perform primary heat exchange; The high-pressure and low-temperature two-phase flow generated by the cage-shaped heat exchange tube (2) after the first-stage heat exchange is collected in the lower header (6) of the heat exchange tube; The high-pressure and low-pressure two-phase flow ejected from the nozzle (8) through the swirl element (7) is rectified and distributed, and performs a second-stage heat exchange with the high-temperature and low-pressure gas; The nozzle (8) cooperates with the contraction section (9) and the mixing section (10) to increase the pressure of the high-temperature low-pressure gas.

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