Low-temperature flare gas warming system

Abstract

The utility model discloses a low temperature torch gas heating system, including torch liquid separator tank, degassing tank, low temperature torch gas and low pressure steam are set up in the upper portion of torch liquid separator tank through static mixer, and the lower portion of torch liquid separator tank is connected with degassing tank through pipeline, the torch gas after heating that the upper portion of torch liquid separator tank adopts enters torch pipe network, and the torch gas after heating that the top of degassing tank adopts enters torch pipe network, and the condensed water after degassing that the bottom of degassing tank discharges enters sewage treatment field, the utility model discloses static mixer is carried out to the mixing of low temperature torch gas and low pressure steam, prevents the problem of uneven mixing, local low temperature icing.

Description

Technical Field

[0001] This utility model belongs to the field of low-temperature flare gas heating technology, and in particular relates to a low-temperature flare gas heating system. Background Technology

[0002] Ethylene is one of the world's largest producers and consumers of basic organic chemical raw materials, and ethylene production capacity is also an important indicator of a country's petrochemical level. In recent years, several large-scale ethylene plants have been built in China. These plants release large quantities of cryogenic flare gas containing ethylene and propylene under accident conditions, and this flare gas may also contain some cryogenic liquid. From a safety and environmental protection perspective, this cryogenic flare gas is not allowed to be directly sent to the flare head for combustion. Therefore, the cryogenic flare gas must be heated before entering the flare head.

[0003] Existing heating methods include: The Chinese patent application number CN201410337644.X uses a heat exchanger to directly heat ethylene with steam. However, due to the extremely low temperature of the low-temperature flare liquid (-99°C), the temperature of the heat exchanger tube wall is far below 0°C. This causes the steam condensate to freeze on the heat exchanger tube wall before it can be discharged, which may eventually lead to blockage of the heat exchanger and prevent the flare gas from being heated.

[0004] The Chinese patent application CN201510104867.6 proposes a method that involves setting up two sets of methanol vaporizers, using methanol as an intermediate medium as a heat source to heat the low-temperature flare condensate and low-temperature flare gas. While this technology can effectively prevent the steam and condensate from freezing on the heat exchanger tube walls, it requires the design of four heat exchange devices, along with numerous supporting instruments and meters, resulting in a significant investment. Furthermore, the process of steam heating methanol first, followed by methanol heating the low-temperature flare gas, leads to a slow response time.

[0005] The Chinese patent application CN201910189697.4 describes a method involving three devices: a cryogenic flare gas separator, a cold flare tank condensate vaporizer, and a cold flare main heater. Methanol, an intermediate medium, is used as the heat source to vaporize and heat the cryogenic flare gas and condensate. This method requires designing three devices, and the cold flare tank condensate vaporizer has a complex structure, resulting in high investment and complex control. Furthermore, steam first heats methanol, which then heats the cryogenic flare gas, leading to a slow response time. Utility Model Content

[0006] In view of this, the present invention aims to provide a low-temperature flare gas heating system to solve at least one technical problem in the background art.

[0007] The purpose of this invention is to overcome the shortcomings of the existing technology, such as the problems of ice formation on the heat exchange tube walls and poor safety when using a steam heater to directly heat ethylene, and the problems of multiple equipment, long process, high investment and slow response when using methanol as an intermediate heating medium to heat low-temperature flare gas. The invention provides an optimized low-temperature flare gas heating system, specifically an engineering design scheme that automatically injects low-pressure steam directly into the low-temperature flare gas for heating, automatically stops steam injection, separates liquids in a separator, and degasses the gas in a degassing tank. This improves system safety, simplifies the process, reduces investment and increases response speed.

[0008] To achieve the above objectives, the technical solution of this utility model is implemented as follows: A low-temperature flare gas heating system includes a flare separator and a degassing tank. Low-temperature flare gas and low-pressure steam are mixed by a static mixer and then enter from the top of the flare separator. The bottom of the flare separator is connected to the degassing tank via a pipeline. The heated flare gas collected from the top of the flare separator enters the flare pipeline network, and the heated flare gas collected from the top of the degassing tank enters the flare pipeline network. The degassed condensate discharged from the bottom of the degassing tank enters the wastewater treatment plant.

[0009] Furthermore, the cryogenic flare gas is connected to the static mixer through a first pipeline, and a cryogenic flare gas flow meter is installed on the first pipeline.

[0010] Furthermore, the low-pressure steam is connected to the static mixer via a second pipe, which is equipped with a parallel interlocking device.

[0011] Furthermore, the parallel interlocking device includes a first parallel pipe and a second parallel pipe; The first parallel pipeline is equipped with a first low-pressure steam valve and a first flow-limiting orifice plate; The second parallel pipeline is equipped with a second low-pressure steam valve and a second flow-limiting orifice plate.

[0012] Furthermore, a second flare gas pipeline for heating is provided at the top of the flare separator; The first heated flare gas pipeline is equipped with a first heated flare gas thermometer and a second heated flare gas thermometer. After the first heating, the flare gas thermometer is electrically connected to the first controller, and the first controller is electrically connected to the low-temperature flare gas flow meter, the first low-pressure steam valve, and the second low-pressure steam valve. After the second heating, the flare gas thermometer is electrically connected to the second controller, and the second controller is electrically connected to the first low-pressure steam valve and the second low-pressure steam valve respectively.

[0013] Furthermore, the static mixer is connected to the top of the flare separator via a pipe.

[0014] Furthermore, a flare separator level gauge is installed on one side of the flare separator via a pipeline.

[0015] Furthermore, a separating bag is provided at the bottom of the flare separating tank, the separating bag is connected to the flare separating tank, and the lower part of the separating bag is connected to one side of the degassing tank through a third pipe, and a first valve is provided on the third pipe; A liquid level gauge is installed on one side of the liquid separator via a pipe.

[0016] Furthermore, a degassing tank level gauge is installed on one side of the degassing tank via a pipeline; The degassing tank is equipped with a remote thermometer; The bottom of the degassing tank is equipped with a condensate pipe after degassing, and the top of the degassing tank is equipped with a flare gas pipe after the first extraction heating. A second valve is installed on the condensate pipe after degassing.

[0017] Furthermore, an external coil is installed on one side of each of the separating tank, separating bag, and degassing tank.

[0018] Compared with existing technologies, the low-temperature flare gas heating system of this utility model has the following advantages: 1. This application solves the problem of ice formation on the heat exchanger tube walls when directly heating ethylene with a steam heater. It employs an automatic steam injection system to heat the cryogenic flare gas, eliminating the need for methanol as an intermediate heating medium. This reduces the number of equipment units from four or five to two. The heated cryogenic flare gas meets national standards, simplifying the process, reducing investment by approximately 50%, improving safety, and increasing response speed.

[0019] 2. This application uses a static mixer to mix low-temperature flare gas and low-pressure steam, which prevents uneven mixing and local low-temperature freezing problems.

[0020] 3. The flare separator of this application is changed from a conventional cold flare separator (-70 to -104℃) to a normal temperature flare gas separator (20 to 40℃). The operating temperature is changed from low temperature to normal temperature, which reduces the difficulty of equipment material selection, reduces the harshness of operation, and improves safety.

[0021] 4. This application incorporates a parallel interlocking device, which ensures that low-pressure steam can be promptly introduced for heating after the low-temperature flare gas is released, while also considering economic efficiency by promptly shutting off the heating steam after the flare gas has been heated. This improves the safety and reliability of the system.

[0022] 5. This application uses a degassing tank to fully degas the condensate at a certain temperature and time, reducing the hydrocarbon content in the condensate, meeting the standards for wastewater treatment plants, and improving the safety of wastewater treatment plants. Attached Figure Description

[0023] The accompanying drawings, which form part of this utility model, are used to provide a further understanding of the utility model. The illustrative embodiments of the utility model and their descriptions are used to explain the utility model and do not constitute an undue limitation of the utility model. In the drawings: Figure 1 This is a schematic diagram of a low-temperature flare gas heating system proposed in this utility model.

[0024] Explanation of reference numerals in the attached figures: 1. Flare separator; 2. Degassing tank; 3. Static mixer; 4. Low-temperature flare gas flow meter; 5. Flare separator level gauge; 6. Separator level gauge; 7. Degassing tank level gauge; 8. Flare gas thermometer after first heating; 9. Flare gas thermometer after second heating; 10. First low-pressure steam valve; 11. First flow-limiting orifice plate; 12. Second low-pressure steam valve; 13. Second flow-limiting orifice plate; 14. Separator; 15. First valve; 16. Second valve; 17. Remote thermometer; 18. First controller; 19. Second controller. Detailed Implementation

[0025] It should be noted that, unless otherwise specified, the embodiments and features described in these embodiments of the present invention can be combined with each other.

[0026] The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0027] In the description of this utility model, it should be understood that the terms "center," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicating orientation or positional relationships based on the orientation or positional relationships shown in the accompanying drawings, are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, features defined with "first," "second," etc., may explicitly or implicitly include one or more of that feature. In the description of this utility model, unless otherwise stated, "a plurality of" means two or more.

[0028] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0029] Example 1 A low-temperature flare gas heating system includes a flare separator 1 and a degassing tank 2. Low-temperature flare gas and low-pressure steam are mixed by a static mixer 3 and then enter from the top of the flare separator 1. The bottom of the flare separator 1 is connected to the degassing tank 2 through a pipeline. The heated flare gas collected from the top of the flare separator 1 enters the flare pipeline network, and the heated flare gas collected from the top of the degassing tank 2 enters the flare pipeline network. The degassed condensate discharged from the bottom of the degassing tank 2 enters the wastewater treatment plant.

[0030] The low-temperature flare gas is connected to the static mixer 3 through the first pipeline, and the first pipeline is equipped with a low-temperature flare gas flow meter 4. The low-pressure steam is connected to the static mixer 3 through the second pipeline, and the second pipeline is equipped with a parallel interlocking device.

[0031] The parallel interlocking device includes a first parallel pipe and a second parallel pipe; the first parallel pipe is equipped with a first low-pressure steam valve 10 and a first flow-limiting orifice plate 11; the second parallel pipe is equipped with a second low-pressure steam valve 12 and a second flow-limiting orifice plate 13.

[0032] The top of the flare separator 1 is equipped with a second flare gas pipeline after heating; the first flare gas pipeline after heating is equipped with a first flare gas thermometer 8 and a second flare gas thermometer 9; the first flare gas thermometer 8 is electrically connected to the first controller 18, the first controller 18 is electrically connected to the low-temperature flare gas flow meter 4, the first low-pressure steam valve 10 and the second low-pressure steam valve 12; the second flare gas thermometer 9 is electrically connected to the second controller 19, the second controller 19 is electrically connected to the first low-pressure steam valve 10 and the second low-pressure steam valve 12 respectively.

[0033] The static mixer 3 is connected to the top of the flare separator 1 via a pipe. A level gauge for the flare separator 1 is installed on one side of the flare separator 1 via a pipe.

[0034] The bottom of the flare separator 1 is equipped with a separator 14, which is connected to the flare separator 1. The lower part of the separator 14 is connected to one side of the degassing tank 2 via a third pipe, and a first valve 15 is installed on the third pipe. A level gauge 6 for the separator 14 is installed on one side of the separator 14 via a pipe. A level gauge for the degassing tank 2 is installed on one side of the degassing tank 2 via a pipe. A remote thermometer 17 is installed inside the degassing tank 2. A post-degassing condensate pipe is installed at the bottom of the degassing tank 2, and a first-stage heated flare gas pipe is installed at the top of the degassing tank 2. A second valve 16 is installed on the post-degassing condensate pipe. An external coil is installed on one side of the separator, separator 14, and degassing tank 2.

[0035] Example 2 This utility model relates to a cryogenic flare gas heating system, comprising a flare separator 1 and a degassing tank 2. Cryogenic flare gas from an ethylene plant or ethylene spherical tank, with a temperature of -70 to -104°C and a pressure of 0.05 to 0.5 MPaG, is metered by a cryogenic flare gas flow meter 4 and then thoroughly mixed with low-pressure steam (pressure 0.4 to 1.0 MPaG, higher than the flare gas pressure) in a static mixer 3. The cryogenic flare gas absorbs heat from the steam and heats up to 20 to 40°C. Approximately 85% (by mass) of the low-pressure steam condenses into condensate at 20 to 40°C. The uncondensed steam (approximately 15%) forms a gas-liquid two-phase flow with the heated flare gas and flows by gravity into the flare separator 1.

[0036] The flare separator 1 operates at a pressure of 0.05–0.5 MPaG and a temperature of 20–40°C. Its main function is to separate the gas and liquid phases. The separator can effectively separate droplets with a diameter of not less than 600 micrometers. Its volume design must simultaneously meet the volume required for gas-liquid separation and the volume of condensate produced by continuous discharge of flare gas for 20–30 minutes. The separated gas phase at the top of the separator is detected by thermometers 8 and 9 before entering the flare pipeline network. The separator is equipped with a remote level gauge 5 for monitoring the liquid level. Both the separator body and the bottom-mounted separator are equipped with external coils, heated by low-pressure steam or hot water to prevent condensate from freezing. The separator is also equipped with a remote level gauge 6 for monitoring the liquid level.

[0037] When the level gauge flare in the separator tank (level 5) or the level gauge 6 in the separator bag indicates a level, the system periodically discharges the condensate in batches to the degassing tank 2 for degassing treatment. The degassing tank operates at a pressure of 0.05–0.5 MPaG and a temperature of 45–60°C. The tank is equipped with an external coil heating element and a remote thermometer 17 to monitor the internal temperature. A remote level gauge 7 is also installed to prevent the level from becoming too high or too low. After the condensate is kept at a constant temperature in the degassing tank 2 for a certain period, the dissolved hydrocarbons, such as ethylene, have largely evaporated. The condensate is then discharged to the wastewater treatment plant through a pipe at the bottom of the tank. This process is repeated until all the condensate in the separator tank has been treated.

[0038] This utility model is equipped with the following two automatic interlocks, which ensure that steam can be introduced in time to raise the temperature after the low-temperature flare gas is released, while also taking into account the economic efficiency of operation and realizing the timely cut-off of steam after the temperature is raised: Interlock Z1 (First Controller 18): When the flare gas thermometer 8 experiences a low-low alarm after the first heating (three-out-of-two logic, three independent and identical flare gas thermometers 8 installed side by side, continuously comparing the measured values ​​of these three instruments), it will be triggered only when at least two of the instruments reach or exceed the alarm set value, or when the low-temperature flare gas flow meter 4 experiences a high-high alarm, automatically opening the corresponding first low-pressure steam valve 10 and second low-pressure steam valve 12. Each steam valve is equipped with a first flow-limiting orifice plate 11 and a second flow-limiting orifice plate 13 to control the steam injection rate and avoid excessive pressure fluctuations in the steam pipeline network and pipeline vibration.

[0039] Interlock Z2 (Second Controller 19): When the flare gas temperature 9 reaches a high-high alarm after the second heating, the first low-pressure steam valve 10 and the first low-pressure steam valve 12 are automatically closed.

[0040] a. System Simplification and Investment Optimization: By setting up an interlocked automatic steam injection system to heat the low-temperature flare gas, the intermediate heating medium of methanol was eliminated, reducing the original four to five units to two. After heating, the flare gas meets national standards, the process is significantly simplified, investment is reduced by approximately 50%, and system safety and response speed are improved.

[0041] b. Improved mixing method: A static mixer is used to achieve uniform mixing of low-temperature flare gas and low-pressure steam, effectively avoiding the problem of local low-temperature icing.

[0042] c. Separation and Anti-freeze Structure Design: A flare-type liquid separator and a degassing tank are installed. The heated gas and liquid phases are separated in the liquid separator, with most of the vapor condensing into liquid water. The liquid separator is equipped with a liquid separator package, and both the tank body and the degassing tank are equipped with external coils, using low-pressure steam or hot water for heating to prevent freezing inside the tank.

[0043] d. Automatic interlocking control strategy: A two-level interlocking system is implemented to balance timely heating with operational economy. Z1 Interlock: When the thermometer 8 at the top of the flare separator shows a low-low alarm (two out of three logic) or the cryogenic flare gas flow meter 4 shows a high-high alarm, the first low-pressure steam valve 10 and the second low-pressure steam valve 12 are automatically opened. A flow-limiting orifice plate is provided after the valve to stabilize the steam injection rate and avoid pipeline pressure fluctuations and pipeline vibration.

[0044] Z2 Interlock: When thermometer 9 detects a high-high alarm, it automatically closes the first low-pressure steam valve 10 and the second low-pressure steam valve 12.

[0045] e. Optimization of equipment operating conditions: The flare separator has been changed from the original low temperature condition (-70 to -104℃) to normal temperature operation (20 to 40℃), which reduces the difficulty of equipment material selection and the harshness of operation, and improves safety and operational reliability.

[0046] f. Condensate treatment and environmental compliance: The condensate is fully degassed by a deaeration tank at a set temperature and time, effectively reducing the hydrocarbon content and ensuring that the wastewater meets the acceptance standards of the sewage treatment plant, thus guaranteeing the safe operation of subsequent treatment processes.

[0047] Example 3 3000m³ of ethylene plant 3 Taking an ethylene spherical tank fire as an example, the calculated discharge rate of the ethylene spherical tank under this condition is 82 t / h, the temperature is -87℃, and the back pressure of the flare network is 0.15 MPaG. When the safety valve starts to discharge, the initial small amount of cryogenic flare gas discharged passes through flow meter 4, static mixer 3, and enters flare separator 1. The cryogenic gas phase passes through the discharge main pipe thermometer 8. When the temperature of thermometer 8 reaches -15℃, a low-low alarm (two out of three) is triggered, interlock Z1 is activated, and the low-pressure steam valve XV1 is automatically opened, with a steam flow rate of 2 t / h. As the discharge rate of the safety valve gradually increases, the cryogenic flare gas flow meter 4 triggers a high-high alarm (alarm value 25 t / h), and the low-pressure steam valve XV2 is automatically opened, with a steam flow rate of 2.5 t / h. In this way, the total steam flow rate reaches 4.5 t / h, which can ensure that the temperature reaches 25℃ after thorough mixing with the cryogenic flare gas, that is, separation in flare separator 1 at 25℃.

[0048] As the safety valve reseated, the discharge volume gradually decreased. The temperature of the flare gas after separation in flare separator 1 gradually increased from 25°C. When the discharge temperature reached 60°C, a high-high alarm was triggered, and the first low-pressure steam valve 10 and the second low-pressure steam valve 12 were automatically closed.

[0049] The level gauge 5 shows a liquid level, and the condensate is discharged in batches to the degassing tank 2 for degassing. The degassing tank operates at a pressure of 0.15 MPaG and a temperature of 55℃. After the degassing tank is kept at a constant temperature for 50 minutes, almost all hydrocarbons such as ethylene in the condensate have evaporated, and the wastewater in the tank is discharged to the wastewater treatment plant through the bottom pipe. This process is repeated until all the condensate in the separatory tank 1 is treated.

[0050] Example 4 A naphtha cracking unit producing ethylene was releasing 123 t / h of cryogenic ethylene at -95°C during a power outage, with a flare network back pressure of 0.05 MPaG. When the safety valve began releasing, a small amount of cryogenic flare gas initially passed through flow meter 4, static mixer 3, and entered flare separator 1. The cryogenic gas phase passed through the discharge main thermometer 8. When the thermometer 8 reached -15°C, a low-low alarm (two out of three) was triggered, interlock Z1 was activated, and the low-pressure steam valve XV1 was automatically opened, allowing a steam flow rate of 3.1 t / h. As the release from the safety valve gradually increased, the cryogenic flare gas flow meter 4 triggered a high-high alarm (alarm value 25 t / h), automatically opening the low-pressure steam valve XV2, allowing a steam flow rate of 3.8 t / h. This brought the total steam flow rate to 6.9 t / h, ensuring sufficient mixing with the cryogenic flare gas to reach a temperature of 25°C, allowing for separation within flare separator 1 at 25°C.

[0051] As the safety valve reseated, the discharge volume gradually decreased. The temperature of the flare gas after separation in flare separator 1 gradually increased from 25°C. When the discharge temperature reached 60°C, a high-high alarm was triggered, and the first low-pressure steam valve 10 and the second low-pressure steam valve 12 were automatically closed.

[0052] The level gauge 5 shows a liquid level, and the condensate is discharged in batches to the degassing tank 2 for degassing. The degassing tank operates at a pressure of 0.05 MPaG and a temperature of 52℃. After the degassing tank is kept at a constant temperature for 45 minutes, almost all hydrocarbons such as ethylene in the condensate have evaporated, and the wastewater in the tank is discharged to the wastewater treatment plant through the bottom pipe. This process is repeated until all the condensate in the separatory tank 1 is treated.

[0053] As can be seen from the data in Examples 3 and 4, the engineering design scheme adopted in this application, which involves automatically injecting steam directly into the cryogenic flare gas for heating, automatically stopping the steam injection, separating the liquid in a separator, and degassing in a degassing tank, solves the problems of icing on the heat exchanger tube walls and poor safety when using a steam heater to directly heat ethylene. At the same time, it eliminates the intermediate heating medium of methanol, solving the problems of multiple equipment, long processes, high investment, and slow response speed when using methanol as an intermediate heating medium for heating cryogenic flare gas. This method improves system safety, simplifies the process, reduces investment, and improves response speed.

[0054] The above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.

Claims

1. A low-temperature flare gas heating system, characterized in that: Including flare separator and degassing tank; The low-temperature flare gas and low-pressure steam are mixed by a static mixer and then enter from the top of the flare separator. The bottom of the flare separator is connected to the degassing tank through a pipeline. The heated flare gas collected from the top of the flare separator enters the flare pipeline network, and the heated flare gas collected from the top of the degassing tank enters the flare pipeline network. The degassed condensate discharged from the bottom of the degassing tank enters the wastewater treatment plant.

2. The low-temperature flare gas heating system according to claim 1, characterized in that: The cryogenic flare gas is connected to the static mixer through the first pipeline, and a cryogenic flare gas flow meter is installed on the first pipeline.

3. The low-temperature flare gas heating system according to claim 1, characterized in that: Low-pressure steam is connected to a static mixer via a second pipe, which is equipped with a parallel interlocking device.

4. A low-temperature flare gas heating system according to claim 3, characterized in that: The parallel interlocking device includes a first parallel pipe and a second parallel pipe; The first parallel pipeline is equipped with a first low-pressure steam valve and a first flow-limiting orifice plate; The second parallel pipeline is equipped with a second low-pressure steam valve and a second flow-limiting orifice plate.

5. A low-temperature flare gas heating system according to claim 4, characterized in that: The top of the flare separator is equipped with a second flare gas pipeline after heating. The first heated flare gas pipeline is equipped with a first heated flare gas thermometer and a second heated flare gas thermometer. After the first heating, the flare gas thermometer is electrically connected to the first controller, and the first controller is electrically connected to the low-temperature flare gas flow meter, the first low-pressure steam valve, and the second low-pressure steam valve. After the second heating, the flare gas thermometer is electrically connected to the second controller, and the second controller is electrically connected to the first low-pressure steam valve and the second low-pressure steam valve respectively.

6. A low-temperature flare gas heating system according to claim 1, characterized in that: The static mixer is connected to the top of the flare separator via piping.

7. A low-temperature flare gas heating system according to claim 1, characterized in that: A flare separator level gauge is installed on one side of the flare separator via a pipe.

8. A low-temperature flare gas heating system according to claim 1, characterized in that: The bottom of the flare separator is equipped with a separator bag, which is connected to the flare separator. The lower part of the separator bag is connected to one side of the degassing tank through a third pipe, and a first valve is installed on the third pipe. A liquid level gauge is installed on one side of the liquid separator via a pipe.

9. A low-temperature flare gas heating system according to claim 8, characterized in that: A level gauge is installed on one side of the degassing tank via a pipeline; The degassing tank is equipped with a remote thermometer; The bottom of the degassing tank is equipped with a condensate pipe after degassing, and the top of the degassing tank is equipped with a flare gas pipe after the first extraction heating. A second valve is installed on the condensate pipe after degassing.

10. A low-temperature flare gas heating system according to claim 9, characterized in that: The separator, separator bag, and degassing tank are all equipped with an external coil on one side.

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