A method for recovering low-pressure specific heat energy by high-speed vortex flow energy separation

Abstract

The present invention discloses a high-speed vortex flow energy separation and low-pressure specific heat energy recovery method, comprising the following steps: step S1, absorbing heat at a low temperature position on the refrigerant gas through an evaporator, and transferring the low-temperature and low-pressure gas into a compressor to form a high-temperature and high-pressure gas; step S2, discharging the high-temperature and high-pressure gas into a subcritical flow vortex heat exchanger, and the subcritical flow vortex heat exchanger releases heat at a high temperature position; step S3, after the low-temperature and low-pressure gas is condensed, a low-temperature and low-pressure vapor-liquid mixture is discharged from a cold-end vapor outlet of the subcritical flow vortex heat exchanger into an economizer, part of the gas in the high-temperature and high-pressure gas is heat-transferred in an inner cavity of the subcritical flow vortex heat exchanger, and then discharged from a hot-end vapor outlet of the subcritical flow vortex heat exchanger to an expansion valve for separate decompression, and then discharged into the economizer; step S4, collectively decompressing the low-temperature and low-pressure vapor-liquid mixture discharged into the economizer, which has the advantages of stronger heating capacity, low pressure ratio, high-temperature hot water, high heating energy efficiency ratio, and reasonable design and layout.

Description

Technical Field

[0001] The present invention belongs to the technical field of low-temperature waste heat recovery, and in particular relates to a method for recovering low-pressure specific heat energy by separating high-speed vortex flow energy. Background Art

[0002] In modern society, a large amount of low-temperature waste heat exists, such as heat dissipation in communication data centers, power generation cold-ends, and other industrial processes. This low-temperature heat is essentially dissipated into ambient heat sinks, resulting in significant energy waste. Direct reuse of this low-temperature heat is difficult, and often requires the necessary technical means, methods, and devices to collect, concentrate, and process it into high-temperature, high-quality heat for wider application.

[0003] like Figure 5 As shown, the existing heat pump heat energy recovery process mainly adopts a single-stage compression system, that is, evaporator A absorbs heat at low temperature → compressor B high pressure → condenser C1 releases heat at high temperature → expansion valve D is low temperature and low pressure → then returns to the evaporator to absorb heat at low temperature for a single-stage cycle, so as to achieve the purpose of collecting, concentrating and processing low-temperature heat energy into high-temperature heat energy. However, due to the influence of the thermophysical properties of the refrigerant (such as the critical temperature of R22 is 96℃ and the critical pressure is 4.99MPa) and the need for high heating energy efficiency, the pressure ratio is limited in the single-stage compression heating cycle, so the condensing temperature generally does not exceed t K =50℃ (i.e., high-temperature heat release temperature). Considering the logarithmic temperature difference of the condenser vapor-liquid heat transfer (about 10℃), the actual heating temperature is relatively low (about 40℃), which limits the application value and scope of low-temperature heat energy recovery.

[0004] In order to obtain a higher temperature of the water supply, such as Figure 6 As shown, a bipolar compression system is currently used, but the pressure ratio is increased. Although it can reach a high-temperature hot water of 65°C, the heating efficiency is low, resulting in high requirements for the material structure strength, thereby increasing the construction cost.

[0005] Regardless of whether it is a single-stage compression system or a bipolar compression system, a traditional condenser is usually used to achieve the high-temperature heat release function. The traditional condenser has a simple structure and uses a cooling medium to cool the high-temperature and high-pressure gaseous refrigerant. The fluid flow rate is generally 1m / s to 3m / s, and the heat release efficiency is low. Summary of the Invention

[0006] The present invention aims to provide a high-speed vortex flow energy separation and low-pressure ratio heat energy recovery method with high heat release efficiency and the generation of a subcritical flow state of refrigerant gas, so as to solve the problems that it is difficult to obtain high-temperature heating capacity at low pressure ratio using a single-stage compression system, resulting in limited application value and scope of low-temperature heat energy recovery, and the increased pressure ratio using a bipolar compression system resulting in low heating efficiency and high requirements on material structure strength.

[0007] To this end, the technical solution adopted by the present invention is: a high-speed vortex flow energy separation and low-pressure specific heat energy recovery method, comprising the following steps:

[0008] Step S1: The refrigerant gas is subjected to heat absorption at a low temperature by the evaporator to form a low-temperature, low-pressure gas state, and the low-temperature, low-pressure gas is transferred into the compressor to form a high-temperature, high-pressure gas;

[0009] Step S2: The high-temperature and high-pressure gas is discharged into a subcritical flow vortex heat exchanger, and then the high-temperature and high-pressure gas is subjected to high-temperature heat release by means of the subcritical flow vortex heat exchanger. The high-temperature and high-pressure gas enters the inner cavity of the subcritical flow vortex heat exchanger at a high speed and tangentially to form a high-speed vortex flow. Under the action of the high-speed centrifugal vortex, radial energy transfer and separation are generated, and the energy of the inner layer gas is transferred to the outer layer gas, thereby forming an inner layer of low-temperature and low-pressure gas and an outer layer of high-temperature and high-pressure gas;

[0010] Step S3: After the low-temperature and low-pressure gas is condensed, the low-temperature and low-pressure vapor-liquid mixture is discharged from the cold-end vapor outlet of the subcritical flow vortex heat exchanger into the economizer. Due to the high-speed rotation, part of the gas in the high-temperature and high-pressure gas approaches the critical temperature, thereby presenting a subcritical flow state, and heat is transferred in the inner cavity of the subcritical flow vortex heat exchanger. Then, the low-temperature and high-pressure vapor-liquid mixture after the heat transfer is discharged from the hot-end vapor outlet of the subcritical flow vortex heat exchanger to the expansion valve for separate decompression. The formed low-temperature and low-pressure vapor-liquid mixture is then discharged into the economizer.

[0011] In step S4, the low-temperature and low-pressure vapor-liquid mixture discharged into the economizer is transferred to the next expansion valve for collective decompression, and finally discharged back to the evaporator, and steps S1-S4 are repeated to perform a new round of heating cycle.

[0012] As a preferred embodiment of the above scheme, in step S2, the subcritical flow vortex heat exchanger includes an exchanger shell, an air inlet nozzle extending horizontally and laterally connected to the top of the exchanger shell, a cold end gas outlet centered at the left end of the exchanger shell, and a hot end gas outlet centered at the right end of the exchanger shell. The exchanger shell is in the shape of a long tube as a whole, and a heat exchange core tube is coaxially installed on the right middle part of the cavity. The heat exchange core tube divides the inner cavity of the exchanger shell into an energy separation zone and a cooling water zone. The left cavity of the exchanger shell is connected to the air inlet nozzle and serves as a gas vortex flow zone for high-speed tangentially entering high-pressure and high-temperature gas to form a high-speed vortex flow. The gas in the high-temperature and high-pressure gas in a subcritical flow state transfers heat with the cooling water zone by means of the heat exchange core tube. The cold end gas outlet is provided with a cold steam guide tube extending axially from the outside of the left end of the exchanger shell to the energy separation zone.

[0013] The air inlet nozzle extends horizontally and connects to the top of the exchanger shell, thus ensuring that high-temperature and high-pressure gas can enter horizontally at high speed. In the heat exchange core tube, the high-speed tangential wall flow will destroy the wall laminar flow that hinders heat transfer, making the airflow in a turbulent state, greatly improving the convective heat transfer coefficient between the airflow and the tube wall, and increasing the heat transfer capacity. Compared with existing condensers, when transferring the same amount of heat, the device volume is greatly reduced, and the heat transfer efficiency is high;

[0014] The subcritical flow vortex heat exchanger is completely different from the existing condenser technology principle, structure and efficiency. By generating critical high temperature, it increases the heat exchange temperature difference of the heat exchange core tube, increases the heat transfer capacity, and achieves the effects of low pressure ratio, high temperature hot water, and high heating energy efficiency ratio, greatly improving the overall benefit and value of low temperature heat energy recovery.

[0015] It is further preferred that the transition section of the gas vortex flow zone adjacent to the heat exchange core tube is provided with a tapered tube connected from the inner wall of the exchanger shell to the left end of the heat exchange core tube. The tapered tube is used to seal the left end of the cooling water zone and increase the gas flow rate in the gas vortex flow zone so that it swirls axially to the energy separation zone, serving two purposes at one stroke. In addition, the inner diameter is contracted in the transition section, the gas is compressed, the pressure is increased, and the molecular vibration frequency is accelerated, thereby increasing the gas vortex speed and guiding the gas flow direction. The design is exquisite.

[0016] Further preferably, the heat exchange core tube is provided with metal inner spiral fins on the inner wall and metal outer spiral fins on the outer wall, so that the gas in the subcritical flow state in the high-temperature and high-pressure gas can transfer heat to the cooling water area with the help of the metal inner spiral fins and the metal outer spiral fins, and the spiral density can be flexibly changed according to the actual heat transfer demand. The design is reasonable, and heat is transferred by the inner and outer fins together, ensuring efficient heat transfer.

[0017] The metal inner spiral fins and the metal outer spiral fins are both made of porous metal. Compared with ordinary metal plates, under the same plate specifications, porous metal can significantly increase the contact heat exchange area of gas molecules by nearly 20 times, and also prolong the heat exchange process inside and outside the heat exchange core tube, greatly improving the heat exchange capacity. Porous metal is mainly used for vibration reduction and sound absorption, but the large specific surface area of porous metal is rarely used. There is currently no precedent for its application in heat exchange equipment. The material selection is ingenious;

[0018] The outer ends of the metal outward-spiral fins are close to the inner wall of the exchanger shell, which increases the contact area between the cooling medium and the metal outward-spiral fins and improves the heat transfer effect; the metal inward-spiral fins are spaced apart from the inner end of the cold steam guide tube in both axial and radial directions, which effectively avoids the cold steam guide tube and the metal inward-spiral fins from colliding, causing mutual interference and affecting the heat transfer or cold air extraction effect, and the layout is reasonable.

[0019] It is further preferred that the left and right ends of the exchanger shell corresponding to the cooling water zone are radially provided with a cooling water inlet and a cooling water outlet, respectively, and cold water cooling is adopted, which has low cost and reasonable design; the hot end steam outlet diameter is located between the inner diameter of the heat exchange core tube and the cold end steam outlet diameter, and the design structure is reasonable to ensure that the low and high temperature stratified gases in the inner and outer layers flow out without confusion; the right end of the cold steam guide pipe is provided with a conical indented microporous plate, which has a reasonable structure, and the gas condensed into a gas-liquid mixed state can more conveniently flow out of the cold steam guide pipe through the conical indented microporous plate, thereby ensuring the export effect.

[0020] It is further preferred that in step S2, the high-temperature and high-pressure gas enters the inner cavity of the subcritical flow vortex heat exchanger tangentially at a speed of not less than 25 m / s to ensure the generation of vortexes, thereby generating a radial temperature gradient to form an inner layer of low-temperature and low-pressure gas and an outer layer of high-temperature and high-pressure gas.

[0021] Beneficial effects of the present invention:

[0022] (1) Compared with the single-stage compression system, which is difficult to obtain high-temperature heating capacity, resulting in limited application value and scope of low-temperature heat recovery, and the double-stage compression system with increased pressure ratio, resulting in low heating efficiency and high requirements for material structure strength, this solution uses a subcritical flow vortex heat exchanger to replace the traditional condenser under the framework of a low-pressure ratio single-stage compression system. High-temperature and high-pressure gas forms a high-speed vortex flow in the inner cavity of the subcritical flow vortex heat exchanger, and part of the high-temperature gas can approach the critical temperature and present a subcritical flow state, thereby directly achieving high-temperature hot water of 80℃ to 90℃ in the low-pressure ratio single-stage compression system; compared with the high-temperature hot water below 50℃ of the traditional condenser in the original single-stage compression system, the heating capacity is obviously stronger.

[0023] (2) High-pressure and high-temperature gas enters the gas vortex flow zone horizontally through the air inlet nozzle to form a high-speed vortex flow. After entering the energy separation zone, the gas molecules in the inner layer transfer kinetic energy to the gas molecules in the outer layer, causing the gas molecules in the inner layer to lose kinetic energy, reduce the vibration frequency, and reduce the temperature, while the gas molecules in the outer layer gain kinetic energy, increase the vibration frequency, and increase the temperature, thereby generating radial energy transfer and separation along the central axis of the energy separation zone. The inner layer is a low-temperature zone, and part of the gas is condensed into a low-temperature and low-pressure vapor-liquid mixture and discharged from the cold-end vapor outlet; while the outer layer is a high-temperature zone, and part of the gas rotating at high speed close to the critical temperature will present a subcritical flow state. After transferring heat to the cooling water in the cooling water zone through the heat exchange core tube, the condensed low-temperature and high-pressure vapor-liquid mixture is then discharged from the hot-end vapor outlet; the structure is interconnected and the design is exquisite.

[0024] (3) The hot end gas outlet of the subcritical flow vortex heat exchanger is connected to the expansion valve. Because the low-temperature and high-pressure gas-liquid mixture condensed after heat transfer cannot directly enter the economizer, it needs to be decompressed separately and turned into a low-temperature and low-pressure gas-liquid mixture before it can merge with the low-temperature and low-pressure gas-liquid mixture at the cold end gas outlet. The design and layout are reasonable.

[0025] To sum up, it has the advantages of stronger heating capacity, low pressure ratio, high temperature hot water, high heating energy efficiency ratio, and reasonable design and layout. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 Schematic diagram of fluid flow of the present invention.

[0027] Figure 2 is the lgp-h diagram of the refrigerant in steps S1-S4.

[0028] Figure 3 This is a structural cross-sectional view of a subcritical flow vortex heat exchanger.

[0029] Figure 4 for Figure 1 Right view of .

[0030] Figure 5 Schematic diagram of a single-stage compression system.

[0031] Figure 6 Schematic diagram of a two-stage compression system. DETAILED DESCRIPTION

[0032] The present invention will be further described below by way of examples and in conjunction with the accompanying drawings:

[0033] Combine Figure 1 — Figure 5 As shown, a high-speed vortex flow energy separation and low-pressure specific heat energy recovery method is implemented as follows:

[0034] Step S1: The refrigerant gas is subjected to heat absorption at a low temperature by the evaporator A so that the refrigerant gas is in a low-temperature and low-pressure gas state, and the low-temperature and low-pressure gas is transferred into the compressor B to form a high-temperature and high-pressure gas.

[0035] The low-temperature heat source evaporator A adopts a conventional horizontal shell and tube liquid-liquid heat exchanger, which has a low-temperature heat source water inlet / outlet and a refrigerant inlet / outlet. The refrigerant inlet is connected to the outlet of the thermal expansion valve D, and the refrigerant outlet is connected to the inlet of the low-pressure ratio compressor B. On both sides of the tube inside the low-temperature heat source evaporator A, low-temperature heat source water that provides heat energy flows outside the tube, and refrigerant that absorbs heat energy flows inside the tube. The low-temperature heat source water transfers heat energy to the refrigerant through the tube wall. After the refrigerant absorbs heat energy from the low-temperature heat source water, its physical state sublimates from low-pressure liquid to low-temperature and low-pressure gas.

[0036] The low-temperature, low-pressure vapor of the refrigerant is sucked into the low-pressure ratio compressor B. After being compressed by the compressor, the physical state of the refrigerant changes to a high-temperature, high-pressure vapor relative to that before compression; the high-temperature, high-pressure vapor of the refrigerant is sprayed into the subcritical flow vortex heat exchanger C connected thereto.

[0037] Step S2: The high-temperature and high-pressure gas is discharged into the subcritical flow vortex heat exchanger C, and then the high-temperature and high-pressure gas is subjected to high-temperature heat release with the help of the subcritical flow vortex heat exchanger C. The high-temperature and high-pressure gas enters the inner cavity of the subcritical flow vortex heat exchanger C at a high speed and tangentially to form a high-speed vortex flow, and radial energy transfer and separation are generated under the action of the high-speed centrifugal vortex. The energy of the inner layer gas will be transferred to the outer layer gas, thereby forming an inner layer of low-temperature and low-pressure gas and an outer layer of high-temperature and high-pressure gas.

[0038] In step S2, the high-temperature and high-pressure gas enters the inner cavity of the subcritical flow vortex heat exchanger C tangentially at a speed of not less than 25 m / s.

[0039] Step S3: low-temperature and low-pressure gas condensed into a low-temperature and low-pressure vapor-liquid mixed state G C The gas is discharged from the cold end gas outlet 3 of the subcritical flow vortex heat exchanger C to the economizer E. Part of the high-temperature and high-pressure gas is close to the critical temperature due to high-speed rotation, thus presenting a subcritical flow state, and heat is transferred in the inner cavity of the subcritical flow vortex heat exchanger C. Then, the low-temperature and high-pressure gas-liquid mixed state G after the heat transfer H The gas is discharged from the hot end gas outlet 4 of the subcritical flow vortex heat exchanger C to the expansion valve D for separate decompression, and the formed low-temperature and low-pressure gas-liquid mixture is then discharged into the economizer E.

[0040] In step S4, the low-temperature and low-pressure vapor-liquid mixture discharged into the economizer E is transferred to the next expansion valve D for collective decompression, and finally discharged back to the evaporator A. Steps S1-S4 are repeated to perform a new round of heating cycle.

[0041] In step S2, the subcritical flow vortex heat exchanger C consists of an exchanger shell 1, an air inlet nozzle 2 extending horizontally and connected to the top of the exchanger shell 1, a cold end gas outlet 3 centered at the left end of the exchanger shell 1, and a hot end gas outlet 4 centered at the right end of the exchanger shell 1.

[0042] The heat exchanger shell 1 is in the shape of a long tube as a whole, and a heat exchange core tube 11 is coaxially installed in the right middle part of the cavity.

[0043] The heat exchange core tube 11 divides the inner cavity of the exchanger shell 1 into an energy separation zone 5 and a cooling water zone 6. The left and right ends of the exchanger shell 1 corresponding to the cooling water zone 6 are radially provided with a cooling water inlet 61 and a cooling water outlet 62 respectively.

[0044] The left cavity of the exchanger housing 1 is connected to the air inlet nozzle 2 and serves as a gas vortex flow zone 7 for the high-speed tangentially entering high-pressure and high-temperature gas to form a high-speed vortex flow.

[0045] A transition section of the gas vortex flow region 7 adjacent to the heat exchange core tube 11 is provided with a tapered tube 8 connected from the inner wall of the exchanger shell 1 to the left end of the heat exchange core tube 11 .

[0046] The tapered pipe 8 is used to block the left end of the cooling water zone 6 and increase the gas flow rate in the gas vortex flow zone 7 to make it swirl axially to the energy separation zone 5 .

[0047] The high-temperature and high-pressure gas in a subcritical flow state transfers heat with the cooling water area 6 via the heat exchange core tube 11 .

[0048] The inner wall of the heat exchange core tube 11 is spirally circumferentially provided with metal inner spiral fins 111, and the outer wall is spirally circumferentially provided with metal outer spiral fins 112, so that the gas in the subcritical flow state in the high-temperature and high-pressure gas can transfer heat with the cooling water area 6 with the help of the metal inner spiral fins 111 and the metal outer spiral fins 112.

[0049] The metal inner-spinning ribs 111 and the metal outer-spinning ribs 112 are both made of porous metal.

[0050] The outer ends of the metal outward-turning fins 112 are close to the inner wall of the exchanger housing 1 .

[0051] There is a distance between the metal inwardly spiral fin 111 and the inner end of the cold steam guide pipe 31 in both the axial and radial directions.

[0052] The cold end gas outlet 3 is provided with a cold gas guide pipe 31 extending axially from the outside of the left end of the exchanger shell 1 to the energy separation zone 5 .

[0053] A conical inward-facing microporous plate is provided at the right end of the cold steam guide pipe 31 .

[0054] The diameter of the hot end gas outlet 4 is between the inner diameter of the heat exchange core tube 11 and the diameter of the cold end gas outlet 3.

[0055] The refrigerant is preferably Freon R-22, which has a critical pressure of 4.99 MPA. Conventional compression must be compressed to 4.99 MPA to reach the critical temperature, while this method only requires 1 MPA to reach the critical temperature of Freon R-22, greatly reducing energy consumption.

Claims

1. A high-speed vortex flow energy separation and low-pressure specific heat energy recovery method, characterized in that: The following steps are involved: Step S1: The refrigerant gas is subjected to low-temperature heat absorption by the evaporator (A) to form a low-temperature, low-pressure gas state, and the low-temperature, low-pressure gas is transferred into the compressor (B) to form a high-temperature, high-pressure gas; Step S2: The high-temperature and high-pressure gas is discharged into the subcritical flow vortex heat exchanger (C), and then the high-temperature and high-pressure gas is subjected to high-temperature heat release by means of the subcritical flow vortex heat exchanger (C). The high-temperature and high-pressure gas enters the inner cavity of the subcritical flow vortex heat exchanger (C) at high speed and tangentially to form a high-speed vortex flow. Under the action of the high-speed centrifugal vortex, radial energy transfer and separation are generated, and the energy of the inner layer gas is transferred to the outer layer gas, thereby forming an inner layer of low-temperature and low-pressure gas and an outer layer of high-temperature and high-pressure gas; Step S3, the low-temperature, low-pressure vapor-liquid mixture after the low-temperature, low-pressure gas is condensed is discharged from the cold-end vapor outlet (3) of the subcritical flow vortex heat exchanger (C) into the economizer (E), part of the high-temperature, high-pressure gas is close to the critical temperature due to high-speed rotation, and thus presents a subcritical flow state, and heat is transferred in the inner cavity of the subcritical flow vortex heat exchanger (C), and then the low-temperature, high-pressure vapor-liquid mixture after the heat transfer is discharged from the hot-end vapor outlet (4) of the subcritical flow vortex heat exchanger (C) to the expansion valve (D) for separate decompression, and the formed low-temperature, low-pressure vapor-liquid mixture is then discharged into the economizer (E); Step S4: The low-temperature, low-pressure vapor-liquid mixture discharged into the economizer (E) is transferred to the next expansion valve (D) for collective decompression, and finally discharged back to the evaporator (A). Steps S1-S4 are repeated to start a new round of heating cycle. In step S2, the subcritical flow vortex heat exchanger (C) includes an exchanger shell (1), an air inlet nozzle (2) extending horizontally and connected to the top of the exchanger shell (1), a cold end gas outlet (3) centrally located at the left end of the exchanger shell (1), and a hot end gas outlet (4) centrally located at the right end of the exchanger shell (1). The exchanger shell (1) is in the shape of a long tube as a whole, and a heat exchange core tube (11) is coaxially installed in the middle right part of the cavity. The heat exchange core tube (11) divides the inner cavity of the exchanger shell (1) into inner and outer parts. It is divided into an energy separation zone (5) and a cooling water zone (6). The left cavity of the exchanger shell (1) is connected to the air inlet nozzle (2) and serves as a gas vortex flow zone (7) for high-speed tangential high-pressure and high-temperature gas to form a high-speed vortex flow. The gas in the high-temperature and high-pressure gas in a subcritical flow state transfers heat with the cooling water zone (6) by means of a heat exchange core tube (11). The cold end gas outlet (3) is provided with a cold steam guide pipe (31) extending axially from the left end of the exchanger shell (1) to the energy separation zone (5). The exchanger shell (1) is provided with a cooling water inlet (61) and a cooling water outlet (62) at the left and right ends corresponding to the cooling water area (6), respectively; the hot end steam outlet (4) has a diameter between the inner diameter of the heat exchange core tube (11) and the diameter of the cold end steam outlet (3); and the right end of the cold steam guide tube (31) is provided with a conical inward-shaped microporous plate.

2. The high-speed vortex flow energy separation and low-pressure specific heat energy recovery method according to claim 1, characterized in that: The transition section of the gas vortex flow zone (7) adjacent to the heat exchange core tube (11) is provided with a tapered tube (8) connected from the inner wall of the exchanger shell (1) to the left end of the heat exchange core tube (11). The tapered tube (8) is used to seal the left end of the cooling water zone (6) and increase the gas flow rate of the gas vortex flow zone (7) to make it swirl axially to the energy separation zone (5).

3. The high-speed vortex flow energy separation and low-pressure specific heat energy recovery method according to claim 1, characterized in that: The heat exchange core tube (11) is provided with metal inner spiral fins (111) on the inner wall in a spiral manner, and metal outer spiral fins (112) on the outer wall in a spiral manner, so that the gas in the high-temperature and high-pressure gas in a subcritical flow state can transfer heat with the cooling water area (6) with the help of the metal inner spiral fins (111) and the metal outer spiral fins (112); the metal inner spiral fins (111) and the metal outer spiral fins (112) are both made of porous metal; the outer end of the metal outer spiral fin (112) is close to the inner wall of the exchanger shell (1), and there is a distance between the metal inner spiral fin (111) and the inner end of the cold steam guide tube (31) in both axial and radial directions.

4. The high-speed vortex flow energy separation and low-pressure specific heat energy recovery method according to claim 1, characterized in that: In step S2, the high-temperature and high-pressure gas enters the inner cavity of the subcritical flow vortex heat exchanger (C) at a speed of not less than 25 m / s.

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