J-T valve dehydration and dealkylation device

Abstract

The utility model discloses a J-T valve dehydration and dealkylation device which comprises a skid-mounted frame, a pretreatment module, a dehydration and dealkylation module and a three-phase separation module are arranged on the skid-mounted frame, and the dehydration and dealkylation module is connected with the pretreatment module through a J-T valve. According to the utility model, the pretreatment module, the dehydration and dealkylation module and the three-phase separation module are all integrated in the compact skid-mounted frame, so that the occupied area is greatly reduced, the installation, transportation and relocation of the device are more convenient and faster, and the operation cost is reduced. Meanwhile, a J-T valve is arranged to be connected with the pretreatment module and the dealkylation module, and condensation and separation of moisture and hydrocarbons in the feed gas are further promoted based on the Joule-Thomson throttling expansion principle. And the efficient and stable dehydration and dealkylation effects are ensured while the occupied area is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of natural gas equipment, and particularly relates to a J-T valve dehydration and dehydrocarbonization device. Background Art

[0002] The natural gas from the wellhead is almost saturated with water vapor. When the natural gas containing saturated water enters the pipeline, under certain conditions, natural gas hydrates may be formed, blocking valves, pipelines and equipment, and reducing the pipeline transportation capacity. At the same time, if the natural gas contains CO 2 and H 2 S, acids will be formed in the presence of water, corroding pipelines and equipment. Therefore, it is necessary to dehydrate natural gas and control the hydrocarbon dew point of natural gas to meet the commodity gas quality index and avoid two-phase gas-liquid flow.

[0003] Most of the existing natural gas dehydration and dehydrocarbonization processes are equipped with two sets of devices separately, resulting in large floor area, high operation cost, inconvenient operation and large investment cost. Summary of the Utility Model

[0004] The purpose of the utility model is to provide a J-T valve dehydration and dehydrocarbonization device to solve the problem that most of the existing natural gas dehydration and dehydrocarbonization processes are equipped with two sets of devices separately, resulting in large floor area and high operation cost mentioned in the above background art.

[0005] To solve the above technical problems, the utility model provides a J-T valve dehydration and dehydrocarbonization device, which includes a skid-mounted frame. A pretreatment module, a dehydration and dehydrocarbonization module and a three-phase separation module are arranged on the skid-mounted frame. The pretreatment module is used for preliminary gas-liquid separation and precooling of the raw gas. The dehydration and dehydrocarbonization module is used for dehydrating and dehydrocarbonizing the pretreated raw gas. The dehydration and dehydrocarbonization module is connected to the pretreatment module through a J-T valve. The three-phase separation module is used for three-phase separation of the liquid after dehydration and dehydrocarbonization.

[0006] Further, the pretreatment module includes a production separator and a raw gas precooler. The inlet of the production separator is communicated with the outlet of an external raw gas compressor. The inlet of the raw gas precooler is communicated with the outlet of the production separator. The outlet of the raw gas precooler is communicated with the inlet of the J-T valve. The raw gas precooler is communicated with an external lean liquid injection pump.

[0007] Further, the dehydration and dehydrocarbonization module includes a low-temperature separator. The inlet of the low-temperature separator is communicated with the outlet of the J-T valve. The cold dry gas outlet of the low-temperature separator is communicated with the raw gas precooler. The alcohol-hydrocarbon liquid outlet of the low-temperature separator is communicated with the inlet of an external MEG heat exchange tank.

[0008] Further, the three-phase separation module includes an MEG electric heater, an MEG rich liquid three-phase separator, and a condensate three-phase separator. The inlet of the MEG electric heater is communicated with the outlet of the external MEG heat exchange tank. The inlet of the MEG rich liquid three-phase separator is communicated with the outlet of the MEG electric heater. The produced water outlet of the MEG rich liquid three-phase separator is communicated with the inlet of an external MEG filter. The condensate three-phase separator is used for three-phase separation of the condensate generated in the feed compressor and the production separator. The produced water outlet of the condensate three-phase separator is communicated with a produced water tank.

[0009] Further, the three-phase separation module further includes a condensate flash tank. The inlet of the condensate flash tank is respectively communicated with the condensate outlets of the condensate three-phase separator and the MEG rich liquid three-phase separator. The condensate oil outlet of the condensate flash tank is communicated with a condensate oil tank.

[0010] Further, the flash gas outlets of the condensate three-phase separator and the condensate flash tank are respectively communicated with the flash gas outlet pipeline of the MEG rich liquid three-phase separator.

[0011] Further, a fuel gas buffer tank is further included. The flash gas outlet pipeline of the MEG rich liquid three-phase separator, the product gas outlet of the raw gas pre-cooler, and the exported natural gas pipeline are all communicated with the inlet of the fuel gas buffer tank. The condensate outlet of the fuel gas buffer tank is communicated with the condensate flash tank. The outlet of the fuel gas buffer tank is communicated with an external outlet fuel gas pipeline.

[0012] Further, safety valve vent openings are provided on the outlet pipelines of the production separator, the raw gas pre-cooler, the low-temperature separator, the MEG rich liquid three-phase separator, the condensate three-phase separator, the fuel gas buffer tank, and the outlet fuel gas pipeline.

[0013] The beneficial effects of the present utility model are as follows: By integrating the pretreatment module, the dehydration and dehydrocarbonization module, and the three-phase separation module in a compact skid-mounted frame, the present utility model greatly reduces the floor area, and also makes the installation, transportation, and relocation of the device more convenient and fast, reducing the operation cost. At the same time, a J-T valve is provided to connect the pretreatment module and the dehydrocarbonization module. Based on the Joule-Thomson throttling expansion principle, the condensation and separation of water and hydrocarbons in the raw gas are further promoted. That is, while reducing the floor area, an efficient and stable dehydration and dehydrocarbonization effect is ensured. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 is a schematic three-dimensional structure diagram of the dehydration and dehydrocarbonization skid of the embodiment of the present utility model.

[0015] Figure 2 is a schematic front view structure diagram of the dehydration and dehydrocarbonization skid of the embodiment of the present utility model.

[0016] Figure 3 This is the first - layer floor plan of the dehydration and dehydrocarbonation skid for the embodiment of the present utility model.

[0017] Figure 4 This is the second - layer floor plan of the dehydration and dehydrocarbonation skid for the embodiment of the present utility model.

[0018] Figure 5 This is the third - layer floor plan of the dehydration and dehydrocarbonation skid for the embodiment of the present utility model.

[0019] Figure 6 This is the process schematic diagram of the embodiment of the present utility model.

[0020] Wherein: 1. Production separator; 2. Raw gas pre - cooler; 3. J - T valve; 4. Low - temperature separator; 5. MEG rich liquid three - phase separator; 6. Condensate three - phase separator; 7. Condensate flash tank; 8. Fuel gas buffer tank; 9. Vent pipeline; 10. Skid - mounted frame. Detailed implementation manners

[0021] Next, the technical solutions in the embodiments of the present utility model will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present utility model. Obviously, the described embodiments are only one embodiment of the present utility model, rather than all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without making creative efforts belong to the protection scope of the present utility model.

[0022] To make the purpose, technical solutions and advantages of the present application clearer, the following further details the present application in conjunction with the accompanying drawings and specific embodiments.

[0023] In the following description, references to "an embodiment", "embodiment", "an example", "example", etc. indicate that the described embodiment or example may include a specific feature, structure, characteristic, property, element or limit, but not every embodiment or example necessarily includes the specific feature, structure, characteristic, property, element or limit. Additionally, repeated use of the phrase "according to an embodiment of the present application" although it may refer to the same embodiment, does not necessarily refer to the same embodiment.

[0024] Such as Figure 1-6As shown in the figure, the utility model discloses a dehydration and dehydrocarbonation device for a J-T valve 3, which comprises a skid-mounted frame 10. A pretreatment module, a dehydration and dehydrocarbonation module and a three-phase separation module are arranged on the skid-mounted frame 10. The pretreatment module is used for preliminary gas-liquid separation and precooling of the raw gas. The dehydration and dehydrocarbonation module is used for dehydrating and dehydrocarbonating the pretreated raw gas. The dehydration and dehydrocarbonation module and the pretreatment module are connected by the J-T valve 3. The three-phase separation module is used for three-phase separation of the liquid after dehydration and dehydrocarbonation. Through the three-phase separation module, effective separation of condensate, light hydrocarbons, ethylene glycol and flash vapor in the condensate and alcohol-hydrocarbon liquid can be achieved, and they are classified and collected for reuse to meet environmental protection requirements.

[0025] In this embodiment, the skid-mounted frame 10 can be provided with a multi-layer structure, that is, the pretreatment module, the dehydration and dehydrocarbonation module and the three-phase separation module are all integrated in a compact frame, extending longitudinally, greatly reducing the floor area. At the same time, the skid-mounted frame 10 also makes the installation, transportation and relocation of the device more convenient and fast, reducing the operation cost. The J-T valve 3 is arranged to connect the raw gas precooler 2 of the treatment module and the low-temperature separator 4 of the dehydration and dehydrocarbonation module. Based on the Joule-Thomson throttling expansion principle, when the high-pressure gas passes through the J-T valve 3, the pressure decreases and the temperature drops, thereby further promoting the condensation and separation of moisture and hydrocarbons in the raw gas.

[0026] In the utility model, by integrating the pretreatment module, the dehydration and dehydrocarbonation module and the three-phase separation module in a compact skid-mounted frame 10, the floor area is greatly reduced, and the installation, transportation and relocation of the device are made more convenient and fast, reducing the operation cost. At the same time, the J-T valve 3 is arranged to connect the pretreatment module and the dehydrocarbonation module. Based on the Joule-Thomson throttling expansion principle, the condensation and separation of moisture and hydrocarbons in the raw gas are further promoted. That is, while reducing the floor area, the efficient and stable dehydration and dehydrocarbonation effect is ensured.

[0027] In one embodiment, the pretreatment module comprises a production separator 1 and a raw gas precooler 2. The inlet of the production separator 1 is communicated with the outlet of an external raw gas compressor. The inlet of the raw gas precooler 2 is communicated with the outlet of the production separator 1. The outlet of the raw gas precooler 2 is communicated with the inlet of the J-T valve 3. The raw gas precooler 2 is communicated with an external lean liquid injection pump. The lean liquid injection pump is arranged outside the device and is used for injecting ethylene glycol into the raw gas precooler 2. It belongs to an auxiliary pipeline and is prior art, so it will not be elaborated here.

[0028] The production separator 1 is mainly used for the preliminary separation of liquids in the raw gas, that is, separating the raw natural gas from the accompanying liquid hydrocarbons and moisture. The raw gas separated by the production separator 1 is cooled in the raw gas pre-cooler 2 to facilitate subsequent processing steps (such as condensation, liquefaction, etc.), and also helps to remove the moisture and hydrocarbons therein. The heat-exchanged and cooled raw gas expands through throttling and depressurization in the J-T valve 3 to generate low temperature. At the same time, the lean liquid injection pump injects ethylene glycol into the raw gas pre-cooler 2 to adsorb water molecules in the natural gas.

[0029] In one embodiment, the dehydrocarbon module includes a cryogenic separator 4. The inlet of the cryogenic separator 4 is connected to the outlet of the J-T valve 3. The cold and dry gas outlet of the cryogenic separator 4 is connected to the raw gas pre-cooler 2. The alcohol-hydrocarbon liquid outlet of the cryogenic separator 4 is connected to the inlet of an external MEG heat exchange tank. The MEG heat exchange tank is arranged outside the device and is used for heat-exchanging the alcohol-hydrocarbon liquid coming out from the bottom of the cryogenic separator 4 to raise its temperature, which is convenient for subsequent three-phase separation in the three-phase separation module. Its auxiliary pipeline belongs to the prior art and will not be elaborated here.

[0030] The throttled raw gas is separated in the cryogenic separator 4 to separate alcohol-hydrocarbon liquid and cold and dry gas. The separated cold and dry gas enters the raw gas pre-cooler 2 to exchange heat with the wet purified gas before dehydration. The reheated dry natural gas is used as product gas and sent to the external transmission device through the system. The alcohol-hydrocarbon liquid outlet of the cryogenic separator 4 is connected to the inlet of an external MEG heat exchange tank, which is used for heat-exchanging the alcohol-hydrocarbon liquid coming out from the bottom of the cryogenic separator 4 to raise its temperature, which is convenient for subsequent three-phase separation in the three-phase separation module.

[0031] In one embodiment, the three-phase separation module includes an MEG electric heater, an MEG rich liquid three-phase separator 5 and a condensate three-phase separator 6. The inlet of the MEG electric heater is connected to the outlet of the external MEG heat exchange tank. The inlet of the MEG rich liquid three-phase separator 5 is connected to the outlet of the MEG electric heater. The produced water outlet of the MEG rich liquid three-phase separator 5 is connected to the inlet of an external MEG filter. The condensate three-phase separator 6 is used for three-phase separation of the condensate generated in the raw material compressor and the production separator 1. The produced water outlet of the condensate three-phase separator 6 is connected to the produced water tank.

[0032] The alcohol-hydrocarbon liquid heated by the MEG heat exchange tank enters the MEG electric heater for heating to increase its temperature and steam pressure, thereby promoting the alcohol-hydrocarbon separation process. The heated alcohol-hydrocarbon liquid enters the MEG rich liquid three-phase separator 5 to separate the liquid rich in ethylene glycol (MEG) and hydrocarbon-containing liquid from the gas, and collect the separated ethylene glycol and hydrocarbon condensate. That is, what the MEG rich liquid three-phase separator 5 separates are alcohol, condensate and flash vapor. The MEG filter is arranged outside the device and is used for removing impurities and pollutants in the ethylene glycol, which is convenient for the regeneration of ethylene glycol. Its auxiliary pipeline belongs to the prior art and will not be elaborated here.

[0033] The condensate three-phase separator 6 separates the condensate (such as water and hydrocarbon liquids) generated in the raw material compressor and the production separator 1 from the gas, separates the natural gas in the condensate, reduces the loss of natural gas, and at the same time recovers and stores the produced gas field water to prevent environmental pollution. That is, what the condensate three-phase separator 6 separates out are condensate, gas field water, and flash vapor. This three-phase separation module can separate and reuse the alcohol liquid, light hydrocarbon, and flash vapor in the alcohol-hydrocarbon liquid.

[0034] In one embodiment, the three-phase separation module further includes a condensate flash tank 7. The inlet of the condensate flash tank 7 is respectively communicated with the condensate outlets of the condensate three-phase separator 6 and the MEG-rich liquid three-phase separator 5. The condensate oil outlet of the condensate flash tank 7 is communicated with the condensate oil tank, and flash evaporation of this part of the condensate is carried out to achieve gas-liquid separation and hydrocarbon recovery.

[0035] In one embodiment, the flash vapor outlets of the condensate three-phase separator 6 and the condensate flash tank 7 are respectively communicated with the flash vapor outlet pipeline of the MEG-rich liquid three-phase separator 5, and the flash vapor is centrally collected and utilized, simplifying the design and maintenance of the system, reducing the complexity of the pipeline layout, and thus reducing the construction and operation costs.

[0036] In one embodiment, it further includes a fuel gas buffer tank 8. The flash vapor outlet pipeline of the MEG-rich liquid three-phase separator 5, the product gas outlet branch pipeline of the raw material gas pre-cooler 2, and the exported natural gas pipeline are all communicated with the inlet of the fuel gas buffer tank 8. The condensate outlet of the fuel gas buffer tank 8 is communicated with the condensate flash tank 7, and the outlet of the fuel gas buffer tank 8 is communicated with the external outlet fuel gas pipeline. The fuel gas buffer tank 8 helps to balance the supply and demand of the fuel gas, ensuring that the system can flexibly respond to changing working conditions and load demands. At the same time, it regulates the flow rate and pressure fluctuations of the fuel gas, reduces the impact on the system, and improves the stability and reliability of the system. The exported fuel gas can be transported to other modules for use through the external outlet fuel pipeline after being metered.

[0037] In one embodiment, safety valve vent openings are provided on the outlet pipelines of the production separator 1, the raw material gas pre-cooler 2, the low-temperature separator 4, the MEG-rich liquid three-phase separator 5, the condensate three-phase separator 6, the fuel gas buffer tank 8, and the exported fuel gas pipeline.

[0038] That is, in the embodiment, to prevent the working pressure of the raw material gas from overpressurizing, a safety valve is installed on the production separator 1 for venting, and a manual vent is configured. To prevent the working pressure of the product gas from overpressurizing, a safety valve is installed on the external transmission pipeline of the raw material gas pre-cooler 2 for venting, and a manual vent is configured. To prevent the working pressure of the cold dry gas from overpressurizing, a safety valve is installed on the outlet pipeline of the low-temperature separator 4 for venting, a manual vent is configured, and an emergency cut-off valve is configured. To ensure the pressure in the MEG rich liquid three-phase separator 5, a safety valve vent is provided on the MEG rich liquid three-phase separator 5. To ensure the pressure in the condensate flash tank 7, a safety valve vent is provided on the condensate flash tank 7. To ensure the pressure in the condensate three-phase separator 6, a safety valve vent is provided on the condensate three-phase separator 6. To prevent the outlet fuel gas from overpressurizing, safety valves are installed on both the fuel gas buffer tank 8 and the outlet fuel gas pipeline, and are configured to a manual vent.

[0039] The design concept of the present utility model is as follows:

[0040] In this embodiment, the skid-mounted frame 10 of the device is arranged in three layers, which is called the dehydration and dehydrocarbonation skid. The raw material gas pre-cooler 2, the condensate three-phase separator 6, and the MEG rich liquid three-phase separator 5 are placed on the first layer; the production separator 1, the J-T valve 3, the MEG electric heater, the condensate flash tank 7, and the fuel gas buffer tank 8 are arranged on the second layer; the safety valve vent pipeline 9 is centrally arranged on the third layer. The low-temperature separator 4 is placed beside the dehydration and dehydrocarbonation skid.

[0041] The raw material gas is pressurized by the raw material gas compressor and then piped to the production separator 1 for gas-liquid separation; the raw material gas separated by the production separator 1 is piped to the raw material gas pre-cooler 2, where it exchanges heat and is pre-cooled with the cold dry gas from the low-temperature separator 4, and ethylene glycol from the lean liquid injection pump is injected to adsorb water molecules in the natural gas. The cooled wet purified gas undergoes throttling expansion through the J-T valve 3 and then enters the low-temperature separator 4 for separation. The separated cold dry gas enters the raw material gas pre-cooler 2 to exchange heat with the wet purified gas before dehydration, and the reheated dry natural gas is used as the product gas and sent to the external transmission device through the system. The alcohol-hydrocarbon liquid discharged from the bottom of the low-temperature separator 4 enters the MEG heat exchange tank for heat exchange, and the heated alcohol-hydrocarbon liquid goes to the MEG electric heater for heating. The heated alcohol-hydrocarbon liquid goes to the MEG rich liquid three-phase separator 5. The flash gas separated by the MEG rich liquid three-phase separator 5 goes to the fuel gas buffer tank 8, the ethylene glycol goes to the MEG filter, and the condensate goes to the condensate flash tank 7.

[0042] The condensate from the bottom of the production separator 1 and the condensate from the raw gas compressor manifold enter the condensate three-phase separator 6. The flash gas separated by the condensate three-phase separator 6 goes to the flash gas outlet pipeline of the MEG three-phase separator, the produced water goes to the produced water tank, and the condensate goes to the condensate flash tank 7. The condensate from the condensate three-phase separator 6, the fuel gas buffer tank 8, and the MEG rich liquid three-phase separator 5 enter the condensate flash tank 7. The flash gas separated by the condensate flash tank 7 goes to the flash gas outlet pipeline of the MEG three-phase separator, and the condensate oil goes to the condensate oil tank. The flash gas outlet pipeline of the MEG rich liquid three-phase separator 5, the product gas at the outlet of the raw gas pre-cooler 2, and the natural gas in the export pipeline enter the fuel gas buffer tank 8. The exported fuel gas is metered and then used in other modules. This design process is simple, the design is compact, there are few equipment, and the operation cost is low; the skid-mounted device is adopted, which reduces the on-site construction volume, shortens the construction period, reduces the construction cost, and is convenient for transportation; the principles of physical dehydration and cryogenic dehydrocarbonation are comprehensively applied, and functions such as dehydration, dehydrocarbonation, and three-phase separation are integrated into a set of device systems, which is convenient for operation.

[0043] By integrating the pretreatment module, the dehydration and dehydrocarbonation module, and the three-phase separation module into a compact skid-mounted frame 10, the present utility model greatly reduces the floor area and also makes the installation, transportation, and relocation of the device more convenient and fast, reducing the operation cost. At the same time, a J-T valve 3 is set to connect the pretreatment module and the dehydration and dehydrocarbonation module. Based on the Joule-Thomson throttling expansion principle, it further promotes the condensation and separation of water and hydrocarbons in the raw gas. That is, while reducing the floor area, it ensures an efficient and stable dehydration and dehydrocarbonation effect.

[0044] The above description of the disclosed embodiments enables those skilled in the art to implement or use the present utility model. Various modifications to these embodiments will be obvious to those skilled in the art, and the general principles defined herein can be implemented in other embodiments without departing from the spirit or scope of the utility model. Therefore, the present utility model will not be limited to the embodiments shown herein, but will conform to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A JT valve dehydration and dehydrocarbon device, characterized by: It comprises a skid-mounted frame, on which a pretreatment module, a dehydration and dehydrocarbonization module and a three-phase separation module are arranged. The pretreatment module is used for performing preliminary gas-liquid separation and precooling on the raw gas, the dehydration and dehydrocarbonization module is used for dehydrating and dehydrocarbonizing the pretreated raw gas, the dehydration and dehydrocarbonization module is connected to the pretreatment module via a JT valve, and the three-phase separation module is used for performing three-phase separation on the liquid after dehydration and dehydrocarbonization.

2. A JT valve dehydration and dehydrocarbon removal device according to claim 1, characterized in that: The pretreatment module includes a production separator and a raw gas precooler, the inlet of the production separator is connected to the outlet of an external raw gas compressor, the inlet of the raw gas precooler is connected to the outlet of the production separator, the outlet of the raw gas precooler is connected to the inlet of the JT valve, and the raw gas precooler is connected to an external lean liquid injection pump.

3. A JT valve dehydration and dehydrocarbonization device according to claim 2, characterized in that: The dehydration and dehydrocarbonization module includes a low-temperature separator, the inlet of the low-temperature separator is connected to the outlet of the JT valve, the cold dry gas outlet of the low-temperature separator is connected to the raw gas precooler, and the alcohol hydrocarbon liquid outlet of the low-temperature separator is connected to the inlet of the external MEG heat exchange tank.

4. A JT valve dehydration and dehydrocarbon removal device according to claim 3, characterized in that: The three-phase separation module includes a MEG electric heater, a MEG rich liquid three-phase separator and a condensate three-phase separator. The inlet of the MEG electric heater is connected to the outlet of the external MEG heat exchange tank, the inlet of the MEG rich liquid three-phase separator is connected to the outlet of the MEG electric heater, the gas field water outlet of the MEG rich liquid three-phase separator is connected to the inlet of the external MEG filter, the condensate three-phase separator is used to perform three-phase separation on the condensate produced in the raw material compressor and the production separator, and the gas field water outlet of the condensate three-phase separator is connected to the gas field water tank.

5. A JT valve dehydration and dehydrocarbonation device according to claim 4, characterized in that: The three-phase separation module further comprises a condensate flash tank, the inlet of which is respectively connected to the condensate outlets of the condensate three-phase separator and the MEG rich liquid three-phase separator, and the condensate oil outlet of the condensate flash tank is connected to the condensate oil tank.

6. A JT valve dehydration and dehydrocarbon removal device according to claim 5, characterized in that: The flash gas outlets of the condensate three-phase separator and the condensate flash tank are respectively communicated with the flash gas outlet pipeline of the MEG rich liquid three-phase separator.

7. A JT valve dehydration and dehydrocarbon removal device according to claim 6, characterized in that: It also includes a fuel gas buffer tank. The flash gas outlet pipeline of the MEG rich liquid three-phase separator, the product gas outlet branch pipeline of the raw gas precooler and the external natural gas pipeline are all connected to the inlet of the fuel gas buffer tank, the condensate outlet of the fuel gas buffer tank is connected to the condensate flash tank, and the outlet of the fuel gas buffer tank is connected to the external outlet fuel gas pipeline.

8. A JT valve dehydration and dehydrocarbon removal device according to claim 7, characterized in that: The production separator, the raw gas precooler, the outlet pipeline of the low-temperature separator, the MEG rich liquid three-phase separator, the condensate three-phase separator, the fuel gas buffer tank and the outlet fuel gas pipeline are all provided with safety valve vents.

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