Multi-stream intermediate medium coiled tube type heat exchanger and use method thereof
By designing a multi-stream intermediate medium-winding tube heat exchanger, the condensation drainage plate is optimized by using multiple spiral coiled heat exchanger tubes and intermediate cooling medium, the problems of cross-contamination, equipment vibration and insufficient operational safety in traditional heat exchangers when transferring cold volume under high temperature differences are solved, and efficient cooling energy recovery and safe operation of equipment are achieved.
Patent Information
- Application Number
- CN202411873119.X
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-18
- Publication Date
- 2025-03-07
AI Technical Summary
Traditional multi-stranded flow tube heat exchangers are prone to cross-contamination problems when dealing with multiple working media, and may cause vibration and damage to the equipment when transferring cold volume under large temperature differences. The prior art lacks operational safety when transferring cold volume under high temperature differences.
A multi-stream intermediate medium-winding tube heat exchanger is designed. By setting up the heat exchange chamber of the main medium I and the intermediate cooling distribution module, multiple spiral coiled heat exchange tubes are used to increase the heat exchange area, realize the full recovery and utilization of cold energy, and optimize the flow direction of the condensation drainage plate distribution refrigerant through the intermediate cooling medium to ensure the safe operation of the equipment under high temperature differences.
It improves energy utilization, realizes full recycling and utilization of cold energy, reduces process operation energy consumption, significantly improves heat exchange efficiency, and ensures the safety and stability of the equipment under high temperature differences.
Smart Images
Figure CN119573307A_ABST
Abstract
Description
Technical Field
[0001] The present invention belongs to the field of LNG cold energy recovery and utilization, and specifically relates to a multi-stream intermediate medium coil heat exchanger and a use method thereof, which can recover a large amount of cold energy released during the gasification process of LNG. Background Art
[0002] Heat exchanger, also known as heat exchanger, is a device used to achieve heat transfer, which transfers part of the heat of hot fluid to cold fluid. In industrial production, heat exchangers play a vital role and are widely used in many fields such as petroleum, chemical industry, electricity, metallurgy, shipbuilding, machinery, food, pharmaceuticals, etc. According to the different structures and working principles, heat exchangers can be divided into many types, such as plate heat exchangers, shell and tube heat exchangers, spiral plate heat exchangers, spray heat exchangers and hybrid heat exchangers.
[0003] LNG, as a liquid form of natural gas, releases a large amount of cold energy during the gasification process. If it is not recovered, this part of cold energy will be wasted. By designing and applying a heat exchanger for LNG cold energy recovery, this part of cold energy can be effectively recovered and converted into other forms of energy or used in other industrial processes, thereby improving the overall efficiency of energy utilization. Recycling LNG cold energy can reduce dependence on traditional energy sources and thus reduce energy consumption. At the same time, since the products of LNG combustion are mainly water and carbon dioxide, it has less environmental pollution compared to traditional energy sources such as coal and oil. Therefore, by recycling LNG cold energy, greenhouse gas emissions can also be indirectly reduced, which is helpful for environmental protection. The recovery of cold energy plays an important role in reducing process energy consumption and optimizing energy structure. In many industrial production processes, such as air separation, light hydrocarbon separation, food freezing, etc., a low temperature environment is required. Using LNG cold energy for these processes can significantly reduce production costs and improve the economic benefits of enterprises.
[0004] In a conventional multi-stream wound tube heat exchanger, since multiple working media exist in the tube at the same time, cross contamination between different media may occur. In addition, as the number of multi-stream pipes increases, the outlet end of the pipe may vibrate, which may damage the heat exchanger equipment. Furthermore, compared with the prior art, the present invention realizes the transfer of cold capacity under a large temperature difference while ensuring the safe operation of the equipment. Summary of the invention
[0005] In order to solve at least one of the problems existing in the prior art, the present invention proposes a multi-stream intermediate medium coil heat exchanger suitable for LNG cold energy recovery and utilization, which recovers liquid carbon dioxide and the cold energy carried by LNG to provide cooling for other production links in the corresponding industrial system, thereby realizing full energy recovery and utilization and multi-energy complementarity.
[0006] In order to achieve the purpose of the present invention, the present invention provides a multi-stream intermediate medium coil heat exchanger suitable for LNG cold energy recovery and utilization, including a main medium I heat exchange module and an intermediate cooling distribution module, that is, the tank body is divided into a first module and a second module, the main medium I heat exchange module is provided with a heat exchange cavity E1 section, and the intermediate cooling distribution module is provided with a heat exchange cavity E2 section;
[0007] The heat exchange chamber E1 section is provided with a main medium I tube bundle, the heat exchange chamber E2 section is provided with a medium II tube bundle and a medium III tube bundle, and the main medium I tube bundle is located above the medium II tube bundle and the medium III tube bundle, and the intermediate cooling distribution module is provided with a medium II inlet, a medium III inlet, a medium II outlet and a medium III outlet, and the two ends of the medium II tube bundle are respectively connected to the medium II inlet and the medium II outlet.
[0008] Furthermore, the main medium I tube bundle, medium II tube bundle and medium III tube bundle inside the tank body all include multiple heat exchange tubes, and each heat exchange tube is spirally coiled into a cylindrical shape, and multiple heat exchange tubes are stacked from top to bottom along the axial direction. The multi-tube coiled heat exchanger designs the tube bundle into three or more heat exchange tubes, each of which is spirally coiled to form an independent heat exchange tube. These heat exchange tubes are nested and arranged in order from the inner layer to the outer layer in the radial direction. By adopting a small tube diameter and nesting multiple heat exchange tubes in this way, the total heat exchange area can be significantly increased, so that the heat exchange efficiency equivalent to that of a large heat exchange tube can be achieved. Under the premise of maintaining the same heat exchange effect, this design can reduce the manufacturing cost; conversely, under the condition of the same cost, it can achieve a higher heat exchange efficiency.
[0009] The coiled tube type increases the heat exchange area, and the heat exchange efficiency can be increased by 13.5% under the same equipment cost.
[0010] Furthermore, an intermediate cooling medium optimized condensation guide plate is provided in the tank body, which is used to guide the refrigerant after heat exchange in the heat exchange cavity E1 section to the heat exchange cavity E2 section. In the main medium I heat exchange module, the refrigerant after heat exchange in the heat exchange cavity E1 section passes through the intermediate cooling medium optimized condensation guide plate and enters the heat exchange cavity E2 section of the intermediate cooling distribution module.
[0011] Furthermore, the intermediate cooling medium optimized condensation guide plate is used to distribute the flow direction of the refrigerant condensed by the medium 1 heat exchange module to the intermediate cooling distribution module. The intermediate cooling medium optimized condensation guide plate separates the first module from the second module in the tank body and is inclined at 30° to guide the refrigerant flowing down after heat exchange in the heat exchange chamber E1 section to the inlet of the medium II tube bundle.
[0012] Furthermore, the refrigerant includes but is not limited to any one of Freon refrigerants and light hydrocarbon refrigerants.
[0013] Furthermore, the Freon refrigerant includes but is not limited to any one of R23, R507, and R410a.
[0014] Furthermore, the light hydrocarbon refrigerant includes but is not limited to any one of ethane and propane.
[0015] Furthermore, the main medium I includes but is not limited to any one of LNG and liquid carbon dioxide.
[0016] Furthermore, the medium II includes but is not limited to gaseous carbon dioxide.
[0017] Furthermore, the medium III includes but is not limited to liquid water.
[0018] Furthermore, a pressure indicator for monitoring the pressure inside the shell is arranged inside the shell.
[0019] Furthermore, a safety valve group is arranged on the shell.
[0020] Furthermore, an end plate is provided in the tank body, and the main medium I tube bundle, medium II tube bundle and medium III tube bundle are all fixed on the end plate.
[0021] Furthermore, it also includes an anti-collision plate, which is located in the tank body and arranged between the end plate and the inner wall of the tank body, so that the refrigerant in the shell side cannot contact the inner wall of the tank body, and is used to protect the tank body from scouring and corrosion by the refrigerant in the shell side.
[0022] The present invention also provides a method for using a multi-stream wound tube heat exchanger, comprising the following steps:
[0023] The main medium I, medium II and medium III enter the main medium I tube bundle, medium II tube bundle and medium III tube bundle from the main medium I inlet, medium II inlet and medium III inlet respectively;
[0024] The refrigerant exchanges heat with the main medium I in the heat exchange chamber E1;
[0025] After the heat exchange, the main heat exchange media of the tube pass, medium I, medium II and medium III, flow out from the medium II outlet, medium II outlet and medium III outlet respectively. After the refrigerant exchanges heat with the main medium I and liquefies, it drips by gravity and enters the heat exchange chamber E2 to exchange heat with medium II and medium III. After the refrigerant exchanges heat with medium II and medium III in the heat exchange chamber E2 and vaporizes, it rises to the heat exchange chamber E1 section.
[0026] Compared with the prior art and the current status, the present invention has at least the following beneficial effects:
[0027] 1. Improve energy utilization rate. The multi-stream intermediate medium coil heat exchanger proposed in the present invention recovers the cold energy released by LNG gasification, thereby achieving full recovery and utilization of the cold energy.
[0028] 2. It has good energy-saving and consumption-reducing benefits. The multi-stream intermediate medium coil-wound heat exchanger proposed in the present invention can be used in parallel at both ends of the main medium I gasification system. The heat exchanger is used to transfer the cold energy carried by the main medium I, and the cold energy is used to cool the raw gas and chilled water, which can reduce the energy consumption of process operation and the energy consumption of the refrigeration unit. Taking the LNG cold energy recovery process with a flow rate of 10.8t / h, a temperature of -27℃, and a pressure of 1.6MPa as an example, the multi-stream intermediate medium coil-wound heat exchanger proposed in the present invention is used to recover the cold energy it carries for cooling the raw gas and chilled water, and the annual electricity saving can reach 2.354×10 6 kWh.
[0029] 3. Good safety performance, easy maintenance and management. The principle of this multi-stream tube-wound intermediate medium heat exchanger is mature, and the related equipment and facilities have rich practical application experience in other cold energy utilization fields; the integrated process device for liquefied carbon dioxide cold energy recovery and utilization with the same principle as this equipment can be connected in parallel at both ends of the carbon dioxide gasification system in the general production process. The use of the process device has little effect on the original carbon dioxide gasification process and refrigeration process. This set of integrated devices can be cut off under special working conditions, and the system has high flexibility.
[0030] 4. High heat exchange efficiency. The present invention adopts the circulation of multiple refrigerant streams for heat exchange and the tube bundle is spirally wound to increase the heat exchange area. In the device of the present invention, multiple streams of raw gas are simultaneously heat exchanged in one device, which also improves the heat exchange efficiency compared with the conventional heat exchanger design.
[0031] 5. The present invention is particularly suitable for situations where it is necessary to process multiple working media at the same time, transfer a large amount of heat under large temperature difference conditions, and the operating pressure of the medium in the pipe is high. BRIEF DESCRIPTION OF THE DRAWINGS
[0032] Figure 1 A cross-sectional view of a multi-stream intermediate medium coiled tube heat exchanger provided in an embodiment of the present invention.
[0033] Figure 2 A front view of a multi-stream intermediate medium coiled tube heat exchanger provided in an embodiment of the present invention.
[0034] Figure 3 A side view of a multi-stream intermediate medium coiled tube heat exchanger provided in an embodiment of the present invention.
[0035] Figure 4 A cross-sectional top view of a multi-stream intermediate medium wound tube heat exchanger provided in an embodiment of the present invention.
[0036] In the figure, 1 is the refrigerant inlet, 2 is the feed baffle, 3 is the main medium I inlet, 4 is the tank body, 5 is the medium II gasification tube bundle, 6 is the main medium I outlet, 7 is the intermediate cooling medium optimization condensation guide plate, 8 is the shell side, 9 is the gaseous medium II inlet, 10 is the medium III inlet, 11 is the medium II outlet, 12 is the medium III outlet, 13 is the medium II tube bundle, 14 is the medium III tube bundle, 15 is the bracket, 16 is the refrigerant outlet, 17 is the pressure indicator, 18 is the safety valve group, 19 is the differential pressure liquid level transmitter, 20 is the liquid collecting bag, 21 is the sewage outlet, 22 is the end plate, and 23 is the anti-collision plate. DETAILED DESCRIPTION
[0037] In order to better understand the present invention, the present invention is further described below in conjunction with the accompanying drawings and embodiments, but the scope of protection claimed by the present invention is not limited to the scope described in the embodiments.
[0038] The terms used in this specification are for the purpose of describing specific embodiments only and are not intended to limit this specification. The singular forms of "a", "the" and "the" used in one or more embodiments of this specification and the appended claims are also intended to include plural forms unless the context clearly indicates other meanings. It should also be understood that the term "and / or" used in one or more embodiments of this specification refers to and includes any or all possible combinations of one or more associated listed items.
[0039] In addition, in the present invention, the descriptions of "first", "second", etc. are only used for descriptive purposes, and do not specifically refer to the order or sequence, nor are they used to limit the present invention. They are only used to distinguish components or operations described with the same technical terms, and cannot be understood as indicating or implying their relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In addition, the technical solutions between the various embodiments can be combined with each other, but they must be based on the ability of ordinary technicians in the field to implement them. When the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection required by the present invention.
[0040] See also Figure 1 The present invention provides a heat exchanger suitable for a multi-stream intermediate medium. The multi-stream intermediate medium heat exchanger includes a bracket 15 and a tank body 4 arranged on the bracket 15. The tank body 4 has a cylinder diameter of 1.7m and a cylinder height of 8.5m. The overall height of the heat exchanger is 10m. It can be understood that in other embodiments, the size of the tank body 4 can take other values as needed.
[0041] The tank body 4 includes a first module and a second module separated by an intermediate medium optimized condensation drainage plate 7, wherein a heat exchange chamber E1 section is arranged in the first module, and a heat exchange chamber E2 section is arranged in the second module. The heat exchange chamber E1 section and the heat exchange chamber E2 section both include a shell side 8, that is, the heat exchange chamber E1 section and the heat exchange chamber E2 section are connected through the shell side 8. An intermediate medium for heat exchange with the main medium I is introduced into the shell side 8; a main medium I tube bundle 5 is provided in the heat exchange chamber E1 section, and a medium II tube bundle 13 and a medium III tube bundle 14 are provided in the heat exchange chamber E2, and the main medium I tube bundle 5 is located above the medium II tube bundle 13 and the medium III tube bundle 14; and the medium II tube bundle 13 and the medium III tube bundle 14 are coiled in parallel in the heat exchange chamber E2; a liquid collecting bag 20 is provided in the heat exchange chamber E2 section in the tank body 4, and the liquid collecting bag 20 is communicated with the shell side 8, and is used to store impurities brought into the refrigerant due to pipeline aging or other reasons; a main medium I inlet 3 and a main medium I outlet 6 are provided on the tank body 4 and at a position corresponding to the heat exchange chamber E1 section, and the main medium I inlet 3 is communicated with the main medium I tube bundle 5, and the main medium I is introduced into the main medium I tube bundle 5.
[0042] The top of the tank body 4 is provided with a refrigerant inlet 1 , and the bottom is provided with a refrigerant outlet 16 , and both the refrigerant inlet 1 and the refrigerant outlet 16 are communicated with the shell side 8 .
[0043] The shell side 8 is filled with refrigerant, and the main medium I is introduced into the main medium I tube bundle 5 located in the heat exchange chamber E1 section. The refrigerant exchanges heat with the main medium I, and the temperature of the main medium I increases after the heat exchange and is discharged through the main medium I outlet 6. The refrigerant is liquefied by heat exchange with the main medium I and drips by gravity, and is drained to the heat exchange chamber E2 section by the intermediate cooling medium optimized condensation guide plate 7, and then rises to the heat exchange chamber E1 section after heat exchange and gasification with the medium II and medium III in the heat exchange chamber E2 section.
[0044] A medium II tube bundle 13 and a medium III tube bundle 14 are arranged in the heat exchange chamber E2 section. A medium II outlet 11, a medium III outlet 12, a medium II inlet 9 and a medium III inlet 10 are arranged on the tank body 4 and at a position corresponding to the heat exchange chamber E2 section. The medium II inlet 9 and the medium II outlet 11 are respectively communicated with the inlet and outlet of the medium II tube bundle 13, and the medium III inlet 10 and the medium III outlet 12 are respectively communicated with the inlet and outlet of the medium III tube bundle 14. Medium II enters the medium II tube bundle 13 through the medium II inlet 11 and exchanges heat with the refrigerant that is liquefied by heat exchange with the main medium I and drips due to gravity. After heat exchange, medium II is discharged from the medium II outlet 11. Medium III enters the medium III tube bundle 14 through the medium III inlet 12 and exchanges heat with the refrigerant that is liquefied by heat exchange with the main medium I, and medium III is discharged from the medium III outlet 12.
[0045] The types of the refrigerant include Freon refrigerants such as R23, R507, R410a, or various light hydrocarbon refrigerants such as ethane, propane, and mixtures thereof. In some embodiments of the present invention, the intermediate medium refrigerant is R507.
[0046] In some embodiments of the present invention, a pressure indicator 17 is provided on the outer wall of the shell side 8. By providing the pressure indicator 17 to monitor the pressure of the shell side 8, early warning can be given for leakage of refrigerant, CO2 or medium III in the shell.
[0047] In some embodiments of the present invention, a safety valve group 18 is provided on the outer wall of the shell side 8. When the machine is shut down for a long time, the increase in the temperature of the intermediate medium refrigerant in the shell side 8 will cause the pressure to increase, exceeding the pressure that the shell side 8 can withstand. At this time, the safety valve group 18 can be used to release the overpressure; in addition, when the refrigerant or CO2 leaks in an accident condition, the pressure exceeding the shell side 8 can also be released through the safety valve group 18, thereby improving the safety performance of the device.
[0048] In some embodiments of the present invention, an end plate 22 is provided in the shell side 8, and the main medium I tube bundle 5, the medium II tube bundle 13 and the medium III tube bundle 14 are all fixed on the end plate 22, and the main medium I tube bundle 5, the medium II tube bundle 13 and the medium III tube bundle 14 can be fixed in the shell side 8 through the end plate 22.
[0049] In some embodiments of the present invention, a drain port 21 is provided at the bottom of the liquid collecting bag 20, and impurities such as iron filings etc. brought into the refrigerant due to pipeline aging or other reasons are discharged through the drain port 21.
[0050] In some embodiments of the present invention, a differential pressure level transmitter 19 is further provided on the liquid collecting bag 20. The pressure conditions in the liquid collecting bag 20 and the shell side 8 are monitored according to the liquid level of the refrigerant in the liquid collecting bag 20.
[0051] In some embodiments of the present invention, an anti-collision plate 23 is further provided in the tank body 4 to prevent the refrigerant in the shell side from contacting the inner wall of the tank body 4 .
[0052] In some embodiments of the present invention, for ease of understanding, taking the refrigerant as R507 as an example, the main medium I is LNG, with a flow rate of 10.8 t / h, a temperature of -90°C, and a pressure of 1.6 MPa, the medium II is gaseous carbon dioxide, with a flow rate of 21.2 t / h, a temperature of 40°C, and a pressure of 0.14 MPa, and the medium III is liquid water, with a flow rate of 90 t / h, a temperature of 5.7°C, and a pressure of 0.2 MPa;
[0053] The gaseous refrigerant R507 enters the heat exchange chamber E1 through the refrigerant inlet 1; the -90℃ LNG is passed into the main medium I tube bundle 5 of the heat exchange chamber E1 section through the main medium I inlet 1, and performs a heat exchange with the gaseous refrigerant R507 with a flow rate of 20.4t / h, a temperature of 1℃, and a pressure of 0.6MPa in the shell side 8. After the heat exchange, the LNG (main medium I) is gasified into gaseous carbon dioxide and the temperature rises to -70℃. The gaseous refrigerant R507 absorbs cold energy to generate The liquid refrigerant R507 is liquefied and its temperature is reduced to -3.1℃. The liquid refrigerant R507 then drips under the action of gravity and flows through the intermediate cooling medium optimization condensation guide plate 7 between the first module and the second module. Most of it flows to the inlet end of the medium II tube bundle 13 of the heat exchange cavity E2 section, and a small part flows to the medium III tube bundle 14 of the heat exchange cavity E2 section, and at the same time, it is mixed with the gaseous CO with a flow rate of 21.2t / h, a temperature of 40℃ and a pressure of 0.14MPa. 2 (Medium II) and water (Medium III) with a flow rate of 90t / h, a temperature of 5.7℃ and a pressure of 0.2MPa are subjected to secondary heat exchange. The temperature of the liquid refrigerant R507 rises to gasification and rises to 1℃, and then naturally rises back to the heat exchange chamber E1 section under the action of gravity for circulating heat exchange; the temperature of the gaseous carbon dioxide in the medium II tube bundle 13 drops to 40℃ after heat exchange; the temperature of the liquid water in the medium III tube bundle 14 drops to 2℃ after heat exchange.
[0054] In the heat exchange process of the above embodiment of the present invention, the upper heat exchange is the heat exchange between LNG and gaseous refrigerant R507, and the heat exchange efficiency is 0.75; the lower heat exchange is the heat exchange between liquid refrigerant R507 and gaseous carbon dioxide and the heat exchange between liquid refrigerant R507 and liquid water, and the heat exchange efficiencies are 0.65 and 0.75 respectively; according to the total heat exchange area of 385m 2 The equipment cost estimation shows that the investment cost of the heat exchanger is about 378,000 yuan; compared with heat exchangers with the same equipment cost, its heat exchange efficiency is 13.5% higher.
[0055] In the coil-wound intermediate medium heat exchanger provided by the aforementioned embodiment of the present invention, the refrigerant R507 flows entirely through the shell side 8, and the carbon dioxide and water flow entirely through the tube side.
[0056] The above embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. For those skilled in the art, other different forms of changes or modifications can be made based on the above description. It is not necessary and impossible to list all the embodiments here. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the claims of the present invention.
Claims
1. A multi-stream intermediate medium coil heat exchanger, characterized in that: It comprises a tank body (4), wherein a heat exchange chamber E1 section and a heat exchange chamber E2 section located below the heat exchange chamber E1 section are arranged in the tank body (4), and the heat exchange chamber E1 section is connected with the heat exchange chamber E2 section through a shell side (8); The shell side (8) can accommodate refrigerant, a main medium I tube bundle (5) is arranged in the heat exchange cavity E1 section, a medium II tube bundle (13) and a medium III tube bundle (14) are arranged in the heat exchange cavity E2 section, and the main medium I tube bundle (5) is located above the medium II tube bundle (13), and the gaseous medium II tube bundle (13) is coiled in parallel above the medium III tube bundle (14); A main medium I inlet (3) and a main medium I outlet (6) are provided on the tank body (4) at a position corresponding to the heat exchange chamber E1 section, and two ends of the main medium I tube bundle (5) are respectively connected to the main medium I inlet (3) and the main medium I outlet (6); A medium II outlet (11), a medium III outlet (12), a medium II inlet (9) and a medium III inlet (10) are provided on the tank body (4) at a position corresponding to the heat exchange chamber E3 section. Two ends of the medium II tube bundle (13) are respectively connected to the medium II outlet (11) and the medium II inlet (9). Two ends of the medium III tube bundle (14) are respectively connected to the medium III outlet (12) and the medium III inlet (10).
2. A multi-stream intermediate medium coiled heat exchanger according to claim 1, characterized in that: The main medium I tube bundle (5), medium II tube bundle (13) and medium III tube bundle (14) inside the tank body (4) all include a plurality of heat exchange tubes, each of which is spirally wound into a cylinder shape, and a plurality of heat exchange cylinders formed by the plurality of heat exchange tubes are stacked from top to bottom along the axial direction.
3. The multi-stream intermediate medium coiled heat exchanger according to claim 1, characterized in that: An anti-collision plate (23) is also provided inside the tank body (4) to prevent the refrigerant in the shell side from contacting the inner wall of the tank body (4).
4. The multi-stream intermediate medium coiled heat exchanger according to claim 1, characterized in that: The first module is provided with a pressure indicator (17) for monitoring the pressure of the tank (4).
5. The multi-stream intermediate medium coiled heat exchanger according to claim 1, characterized in that: The tank body (4) is provided with a safety valve group (18).
6. The multi-stream intermediate medium coiled heat exchanger according to claim 1, characterized in that: An intermediate cooling medium optimized condensation guide plate (7) is arranged in the tank body (4) and is used to guide the refrigerant after heat exchange in the heat exchange cavity E1 section to the heat exchange cavity E2 section.
7. The heat exchanger for multiple-stream intermediate medium according to claim 1, characterized in that: An end plate (22) is arranged in the tank body (4), and the main medium I tube bundle (5), the medium II tube bundle (13) and the medium III tube bundle (14) are all fixed on the end plate (22).
8. A multi-stream intermediate medium coiled heat exchanger according to any one of claims 1 to 7, characterized in that: The heat exchange chamber E2 is provided with a liquid collecting bag (20), and a sewage outlet (21) is provided at the bottom of the liquid collecting bag (20).
9. The multi-stream intermediate medium coiled heat exchanger according to claim 8, characterized in that: A differential pressure liquid level transmitter (19) is arranged on the liquid collecting bag (20).
10. A method for using the multi-stream wound tube heat exchanger according to any one of claims 1 to 9, characterized in that: The steps include: The main medium I, medium II and medium III enter the main medium I tube bundle (5), the medium II tube bundle (13) and the medium III tube bundle (14) from the main medium I inlet (3), the medium II inlet (9) and the medium III inlet (10) respectively; The refrigerant exchanges heat with the main medium I in the heat exchange chamber E1 section; After the heat exchange, the main heat exchange media of the tube side, medium I, medium II and medium III, flow out from the medium II outlet (6), medium II outlet (11) and medium III outlet (12) respectively. The refrigerant exchanges heat with the main medium I and liquefies, then drips by gravity and enters the heat exchange chamber E2 section to exchange heat with medium II and medium III. The refrigerant exchanges heat with medium II and medium III in the heat exchange chamber E2 section and vaporizes, then rises to the heat exchange chamber E1 section.