A skid-mounted natural gas processing device

Abstract

The present invention relates to a skid-mounted natural gas processing device. The natural gas processing device is skid-mounted as a whole and shipped out of the factory. The on-site assembly is simple and quick, and the device is convenient for transportation. With its convenient and quick construction method and safe and reliable operation mode, it adopts two-stage compression and two-stage separation. It can efficiently recover the associated gas resources of the oil field according to different oil field scales and gathering and transportation conditions, and is convenient for subsequent harmless treatment and deep processing of downstream products, so that the resources can be fully utilized, which is beneficial to oil field production and safety management.

Description

Technical Field

[0001] The invention relates to the field of natural gas processing, and in particular to a skid-mounted natural gas processing device. Background Art

[0002] During the production process of oil fields, some associated gas is produced while oil is being extracted. The main component of associated gas is C1, and it also contains some C2, C3, C4 and C5. + Heavy hydrocarbons such as carbon dioxide, hydrogen sulfide, nitrogen, and mechanical impurities need to be purified and processed before they can be used. Like petroleum, associated gas is also a resource with high economic value. However, due to the limitations of the scale of the oil field and the conditions of gathering and transportation, especially for some remote oil fields, associated gas has not been reasonably utilized. Because it cannot be stored, part of it is usually directly used as crude oil heating fuel, and the rest is vented and burned, or even allowed to evaporate and discharge into the air. This disposal method not only brings certain safety hazards to oilfield well sites and gathering and transportation stations, causing air pollution in the oil field, but also is a huge waste of resources. The skid-mounted natural gas processing unit, with its convenient and fast construction method and safe and reliable operation mode, can efficiently recover oilfield associated gas resources for different oil field scales and gathering and transportation conditions, facilitate subsequent harmless treatment, and carry out deep processing of downstream products at the same time, so that resources can be fully utilized, which is beneficial to oilfield production and safety management. Summary of the invention

[0003] The technical problem to be solved by the present invention is to provide a skid-mounted natural gas processing device which is easy to move and install and can efficiently recover associated gas resources in oil fields.

[0004] The technical solution of the present invention to solve the above technical problems is as follows: a skid-mounted natural gas processing device, installed on multiple skid blocks, includes a natural gas compressor unit, a second water cooler, a first liquid separator tank, a first heat exchange and cooling device group and a second liquid separator tank, the natural gas compressor unit includes a first compression chamber and a second compression chamber, the inlet of the first compression chamber is used to introduce natural gas, the outlet of the first compression chamber is connected to the inlet of the first liquid separator tank through the second water cooler, the gas phase outlet of the first liquid separator tank is connected to the inlet of the second compression chamber, the outlet of the second compression chamber is connected to the inlet of the second liquid separator tank through the first heat exchange and cooling device group, and the gas phase outlet of the second liquid separator tank is used to discharge the processed natural gas.

[0005] The beneficial effects of the present invention are as follows: the natural gas processing device is skid-mounted as a whole and shipped out of the factory. The on-site assembly is simple and quick, and it is easy to transport. With its convenient and quick construction method and safe and reliable operation mode, it can efficiently recover oilfield associated gas resources for different oil field scales and gathering and transportation conditions. Natural gas processing in the prior art usually adopts one-stage compression and water cooling treatment, the separation is not thorough, and the oilfield associated gas cannot be effectively utilized. The skid-mounted natural gas processing device of the present invention adopts two-stage compression and two-stage separation, which can effectively obtain purified dry gas and oilfield mixed hydrocarbon products. The process is simple, the equipment is compact, and the operation is convenient, which is convenient for subsequent harmless treatment and deep processing of downstream products.

[0006] Based on the above technical solution, the present invention can also be improved as follows.

[0007] Furthermore, it also includes an exhaust device, a desulfurization tower group and a raw material buffer tank, the inlet of the exhaust device is connected to the raw gas inlet pipeline, and the outlet is connected to the inlet of the desulfurization tower group, the outlet of the desulfurization tower group is connected to the inlet of the raw material buffer tank, and the gas phase outlet of the raw material buffer tank is connected to the inlet of the first compression chamber of the natural gas compressor group.

[0008] The beneficial effect of adopting the above further scheme is: the vacuum device draws the raw gas into the system and desulfurizes it in the desulfurization tower group, the gas-liquid separation is initially achieved in the raw buffer tank, and the gas phase is discharged from the gas phase outlet of the raw buffer tank and enters the natural gas compressor unit for compression.

[0009] Furthermore, the vacuum device includes a vacuum pump, a first water cooler and a vacuum pump buffer tank, the inlet of the vacuum pump is connected to the raw gas inlet pipeline, the outlet of the vacuum pump is connected to the heat medium inlet of the first water cooler, the heat medium outlet of the first water cooler is connected to the inlet of the vacuum pump buffer tank, and the gas phase outlet of the vacuum pump buffer tank is connected to the inlet of the desulfurization tower group.

[0010] The beneficial effect of adopting the above further scheme is: the vacuum pump draws in the raw gas, which is cooled by the first water cooler, and part of the gaseous mixed hydrocarbons are cooled and liquefied, and then enter the vacuum pump buffer tank for gas-liquid separation, and the gas phase enters the subsequent desulfurization tower group.

[0011] Furthermore, the desulfurization tower group includes a first desulfurization tower and a second desulfurization tower connected in parallel or in series, the outlet of the vacuum device is connected to the inlet of the first desulfurization tower and / or the inlet of the second desulfurization tower, and the outlet of the first desulfurization tower and / or the outlet of the second desulfurization tower are both connected to the inlet of the raw material buffer tank.

[0012] The beneficial effect of adopting the above further scheme is that the two desulfurization towers can be connected in series or in parallel. When connected in parallel, the desulfurization efficiency is high and it is convenient to replace the desulfurizer in one of the desulfurization towers. When connected in series, the desulfurization is more thorough. The connection method of the two desulfurization towers can be flexibly selected according to the sulfur content in the product.

[0013] Furthermore, the first heat exchange and cooling device group includes a reboiler, a third water cooler and a first heat exchanger, the outlet of the second compression chamber is connected to the gas phase inlet of the reboiler, the gas phase outlet of the reboiler is connected to the heat medium inlet of the third water cooler, the heat medium outlet of the third water cooler is connected to the heat medium inlet of the first heat exchanger, and the heat medium outlet of the first heat exchanger is connected to the inlet of the secondary liquid separation tank.

[0014] The beneficial effect of adopting the above further scheme is that the pressurized natural gas flows through the reboiler to provide a heat source, then passes through the third water cooler to cool down, passes through the first heat exchanger to cool down to 15 degrees Celsius, separates gas and liquid, and then enters the secondary liquid separator to separate the gas phase and liquid phase.

[0015] Furthermore, it also includes an electric heater, a first drying tower, a second drying tower and a second heat exchange and cooling device group; the gas phase outlet of the secondary liquid separation tank is respectively connected to the inlet of the first drying tower or the inlet of the second drying tower, the outlet of the first drying tower or the outlet of the second drying tower is connected to the inlet of the second heat exchange and cooling device group, the outlet of the second heat exchange and cooling device group is connected to the refrigerant inlet of the first heat exchanger, the refrigerant outlet of the first heat exchanger is connected to the purified dry gas external transmission pipeline, the refrigerant outlet of the first heat exchanger is also respectively connected to the inlet of the electric heater or the outlet of the electric heater, the outlet of the electric heater is respectively connected to the outlet of the first drying tower or the outlet of the second drying tower, and the inlet of the first drying tower or the inlet of the second drying tower is connected to the purified dry gas external transmission pipeline.

[0016] The beneficial effect of adopting the above further scheme is that the separated gas phase is dried by the drying tower and cooled and separated by the second heat exchange and cooling device group, and provides cooling capacity for the first heat exchanger. Part of the purified dry gas discharged from the refrigerant outlet of the first heat exchanger is transmitted to the outside, and the other part is regenerated and heated by the electric heater, and reversely enters the first drying tower or the second drying tower for backwashing to achieve desorption of the molecular sieve in the drying tower. After the desorption is completed, the purified dry gas discharged from the refrigerant outlet of the first heat exchanger directly reverses to the first drying tower or the second drying tower to achieve cooling of the molecular sieve.

[0017] Furthermore, the first heat exchange and cooling device group also includes a distillation tower, and the second heat exchange and cooling device group includes a second heat exchanger, a front cooling heat exchanger, an evaporative heat exchanger, a rear cooling heat exchanger, a low-temperature separator and a refrigerant circulation device; the outlet of the first drying tower or the outlet of the second drying tower is connected to the heat medium inlet of the second heat exchanger, the heat medium outlet of the second heat exchanger is connected to the heat medium inlet of the front cooling heat exchanger, the heat medium outlet of the front cooling heat exchanger is connected to the heat medium inlet of the evaporative heat exchanger, the heat medium outlet of the evaporative heat exchanger is connected to the heat medium inlet of the rear cooling heat exchanger, the heat medium outlet of the rear cooling heat exchanger is connected to the inlet of the low-temperature separator, and the gas outlet of the low-temperature separator is connected to the heat medium outlet of the rear cooling heat exchanger. The liquid phase outlet of the low-temperature separator is connected to the inlet of the distillation tower, the liquid phase outlet of the distillation tower is connected to the liquid phase inlet of the reboiler, and the liquid phase outlet of the reboiler is connected to an external mixed hydrocarbon storage tank; the gas phase outlet of the distillation tower is connected to the inlet of the first liquid separator.

[0018] The beneficial effect of adopting the above further scheme is that the material coming out of the drying tower is cooled to -51°C by the second heat exchanger, the front cooling heat exchanger, the evaporation heat exchanger and the rear cooling heat exchanger in sequence, and then enters the low temperature separator, and the separated liquid phase C3 + The components are connected to an external mixed hydrocarbon storage tank after C2 is removed from the distillation tower. The dry gas components of the low-temperature separator are expanded and separated by heat. The temperature of the gaseous cold phase is -70°C. The gaseous cold phase enters the post-cooling heat exchanger and the pre-cooling heat exchanger in turn to recover cold energy.

[0019] Furthermore, the low-temperature separator includes a low-temperature separator body and a cold dry gas heat separation device arranged inside the low-temperature separator body, and the cold dry gas heat separation device is a velocity generator or a vortex tube.

[0020] The beneficial effects of adopting the above further scheme are: using a vortex tube or a velocity generator to replace the existing expander function, realizing the heat separation of cold and dry gas under deep cold state, which is cost-effective; improving the stability of production operation of the device under field operation conditions, and improving the operation rate and efficiency of the device.

[0021] Furthermore, it also includes an inlet buffer tank and a drainage water separation tank, the inlet of the inlet buffer tank is connected to the raw gas inlet pipeline, the outlet of the inlet buffer tank, the liquid phase outlet of the vacuum buffer tank, the liquid phase outlet of the raw material buffer tank and the liquid phase outlet of the first-level liquid separation tank are all connected to the liquid phase inlet of the drainage water separation tank, the sewage outlet of the drainage water separation tank is connected to an external sewage tank, and the outlet of the first drying tower or the outlet of the second drying tower is connected to the pressurized gas inlet of the drainage water separation tank.

[0022] The beneficial effect of adopting the above further scheme is: the imported buffer tank plays the role of stabilizing the air pressure and flow rate of the raw gas inlet pipeline, and at the same time can realize the separation of oil, water and mechanical impurities. The separated light oil enters the drainage water separation tank, and the drainage water separation tank separates the oily wastewater and the light oil, and the oily wastewater enters the external sewage tank.

[0023] Furthermore, the natural gas compressor unit includes a first natural gas compressor and a second natural gas compressor, the first natural gas compressor and the second natural gas compressor are arranged in parallel, and both have the first compression chamber and the second compression chamber.

[0024] The beneficial effect of adopting the above further solution is that two natural compressors are arranged in parallel to ensure working efficiency and facilitate equipment maintenance.

[0025] The beneficial effects of the present invention are as follows: the skid-mounted natural gas processing device is mainly used for harmless treatment and comprehensive utilization of petroleum associated gas resources of different scales in remote oil fields, and various socialized products are processed and produced, which are market-oriented and sold on the spot to create economic benefits. According to the different qualities and gas volumes of the oil fields, low-temperature separation or cold oil absorption methods are used to dehydrate, remove heavy hydrocarbons, and remove acidic gases, and initially obtain two products: purified dry gas and oilfield mixed hydrocarbons; the process can be carried out in the following two ways, the more common way is: two-stage compression (0.12→0.75→2.15MPa), two-stage refrigeration (shallow cooling + velocity generator or vortex tube), and two-stage separation, which is characterized by simple process, compact equipment, and easy operation; the other way is: two-stage compression (0.12→0.75→2.15MPa), one-stage refrigeration (shallow cooling), and cold oil absorption, which is characterized by high light hydrocarbon yield (C3 + The yield is ≥90%). The complete set of natural gas processing equipment is skid-mounted and shipped from the factory. 1~3×10 4 Nm 3 The device group skid of / d includes: four production group skids (7.2×2.5×2.7m), a main control room and an air compressor room (7×2.5×2.6m), a raw gas buffer tank (30m 3 ), a product tank (50m 3 ) and complete sets of automation control systems and complete sets of power distribution systems; 4~8×104 Nm 3 / d device is two 50m 3 The product tank and skid-mounted structure are enlarged in the same proportion (8.8×3.2×3m). After storage, the mixed hydrocarbon products are directly loaded for export, or further processed into liquefied petroleum gas and stable light hydrocarbon products; a part of the purified dry gas product is returned to the oil field as fuel gas for crude oil heating, and the rest is exported to the gas pipeline network; according to the specific conditions of each region, a natural gas power generation device can be configured to convert natural gas resources into electricity for external supply; or CNG and LNG devices can be equipped to process and sell market products. The complete set of equipment is designed according to field working conditions, and the on-site assembly is simple and fast; the project operation requires low investment and quick results.

[0026] The device of the present invention operates safely, efficiently and stably, and plays an important role in promoting the realization of closed-type mining in oil fields, eliminating potential safety hazards, and energy conservation, emission reduction, environmental protection and other aspects. According to the overall deployment of various oil field companies to create resource-saving enterprises, the application of skid-mounted natural gas processing devices has a good prospect for oil and gas fields with large mining areas, scattered mining areas and difficult gathering and transportation, and will produce greater economic and social benefits.

[0027] The natural gas processing device of the present invention is suitable for the working conditions of "dispersed gas sources and field operations" in remote oil fields. The production device has perfect technology (low energy consumption), compact equipment (skid-mounted), and high automation level (PLC full process control). Its technical characteristics are mainly reflected in the following aspects:

[0028] 1. The overall structure of the device is compact. Under the premise of meeting the design specifications of the fifth-level natural gas station, the overall skid-mounted and rigorous structure saves space and floor space to the maximum extent, and the skid-mounted combined structure and orientation can be adjusted according to the on-site terrain conditions.

[0029] 2. The entire production device is designed as a mobile vehicle-mounted skid-mounted device, which can be easily relocated as the gas source assembly site changes; the plug-in signal cable, power cable and metal process hose assembly are skid-connected, which greatly reduces the workload of on-site assembly. Without special circumstances, water, electricity and gas conditions are available, after the device is put on site, installation, commissioning and production are generally completed within 15 working days.

[0030] 3. All equipment is designed according to field operation standards and can be used in open-air operations around the clock. It does not require cumbersome logistical support and utility engineering configuration, and the equipment is refined and simple.

[0031] 4. There are no direct-burning open flame equipment such as heating furnaces and heat medium furnaces. Both strong and weak electrical equipment adopt explosion-proof design, which complies with the design specifications of petroleum and natural gas engineering and has good safety performance.

[0032] 5. According to different gas source quality conditions, different process configurations can be adopted, such as two-stage compression + low-temperature condensation or cold oil absorption. The process terminal can perform efficient gas-liquid separation and absorption at minus 35℃ and 2.0MPa to obtain satisfactory light hydrocarbon yields; it can meet various process requirements such as light hydrocarbon production, natural gas purification, commercial natural gas pipeline transportation or CNG, LNG processing, etc. The device has large operation flexibility and can adjust the equipment load according to the actual working conditions to achieve the best combination of energy consumption and benefits.

[0033] 6. The physical low-temperature separation process is adopted, and the production process is fully closed; there is no discharge of "three wastes" and no environmental pollution.

[0034] 7. According to the project conditions, the purified dry gas can be directly exported, used for natural gas power generation, or further processed into CNG and LNG products; the mixed hydrocarbon products can be directly loaded and exported as crude chemical raw materials, and the output can reach a certain scale (≥15t / d). Distillation facilities can also be added to further process them into liquefied petroleum gas and stable light hydrocarbon products to achieve greater economic benefits.

[0035] 8. Use vortex tube or velocity generator to replace the expander function to achieve heat separation of cold and dry gas under deep cold state, which is cost-effective; improve the stability of production operation under field operation conditions of the device, and improve the operation rate and efficiency of the device.

[0036] 9. Both the water cooler and the heat exchanger use high-efficiency rust-proof aluminum plate-fin heat exchangers, and the heat exchange of multiple logistics is reasonably set to make full use of the heat source and the cooling capacity of the medium, reduce energy consumption, and reduce the operating cost of the device.

[0037] 10. Multiple water coolers are installed together to form a centralized water cooler. The centralized water cooler adopts a dry and wet dual-use design to adapt to production operations under water shortage conditions. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 This is a schematic diagram of a skid-mounted natural gas processing device of the present invention;

[0039] Figure 2 for Figure 1 A magnified image of area A;

[0040] Figure 3 for Figure 1 Enlarged view of area B;

[0041] Figure 4 for Figure 1 Enlarged view of area C in the middle;

[0042] Figure 5 for Figure 1 Enlarged view of area D in the middle;

[0043] Figure 6 This is the main view of the velocity generator;

[0044] Figure 7 for Figure 6 Sectional view of EE;

[0045] Figure 8 The diagram is a top view of the structure of a skid-mounted natural gas processing device of the present invention.

[0046] In the accompanying drawings, the components represented by the reference numerals are listed as follows:

[0047] 1. Vacuum pump, 2. Vacuum pump buffer tank, 3. First desulfurization tower, 4. Second desulfurization tower, 5. Raw material buffer tank, 6. First natural gas compressor, 7. Second natural gas compressor, 8. Primary liquid separator, 9. Reboiler, 10. Secondary liquid separator, 11. First drying tower, 12. Second drying tower, 13. Front cooling heat exchanger, 14. Evaporation heat exchanger, 15. Post cooling heat exchanger, 16. Low temperature separator, 17. Distillation tower, 18. Electric heater, 19. Import buffer tank, 20. Drainage water separator, 21. Ejector, 22. Oil separator, 23. Refrigeration compressor compressor, 24, refrigerant storage tank, 25, economizer, 26, velocity generator, 261, gaseous hot phase outlet, 262, air inlet, 263, bolts, 264, end cover, 265, main shell, 266, air outlet pipe, 267, balance pipe, 27, centralized water cooler, 301, first water cooler, 302, second water cooler, 303, third water cooler, 304, fourth water cooler, 305, fifth water cooler, 306, sixth water cooler, 204, second heat exchanger, 205, first heat exchanger, 102, concentrator, 103, condensate cooler. DETAILED DESCRIPTION

[0048] The principles and features of the present invention are described below. The examples given are only used to explain the present invention and are not used to limit the scope of the present invention.

[0049] like Figure 1-Figure 8 As shown, the present embodiment provides a skid-mounted natural gas processing device, which is installed on a plurality of skid blocks, and includes a natural gas compressor unit, a second water cooler 302, a first liquid separator tank 8, a first heat exchange and cooling device group, and a second liquid separator tank 10. The natural gas compressor unit includes a first compression chamber and a second compression chamber. The inlet of the first compression chamber is used to introduce natural gas, and the outlet of the first compression chamber is connected to the inlet of the first liquid separator tank 8 through the second water cooler 302. The gas phase outlet of the first liquid separator tank 8 is connected to the inlet of the second compression chamber, and the outlet of the second compression chamber is connected to the inlet of the second liquid separator tank 10 through the first heat exchange and cooling device group. The gas phase outlet of the second liquid separator tank 10 is used to discharge the processed natural gas.

[0050] As a further scheme of this embodiment, it also includes an exhaust device, a desulfurization tower group and a raw material buffer tank 5, the inlet of the exhaust device is connected to the raw gas inlet pipeline, and the outlet is connected to the inlet of the desulfurization tower group, the outlet of the desulfurization tower group is connected to the inlet of the raw material buffer tank 5, and the gas phase outlet of the raw material buffer tank 5 is connected to the inlet of the first compression chamber of the natural gas compressor group.

[0051] As a further scheme of this embodiment, the vacuum device includes a vacuum pump 1, a first water cooler 301 and a vacuum pump buffer tank 2, the inlet of the vacuum pump 1 is connected to the raw gas inlet pipeline, and the outlet is connected to the heat medium inlet of the first water cooler 301, the heat medium outlet of the first water cooler 301 is connected to the inlet of the vacuum pump buffer tank 2, and the gas phase outlet of the vacuum pump buffer tank 2 is connected to the inlet of the desulfurization tower group.

[0052] As a further scheme of this embodiment, the desulfurization tower group includes a first desulfurization tower 3 and a second desulfurization tower 4 connected in parallel or in series, the outlet of the exhaust device is connected to the inlet of the first desulfurization tower 3 and / or the inlet of the second desulfurization tower 4, and the outlet of the first desulfurization tower 3 and / or the outlet of the second desulfurization tower 4 are both connected to the inlet of the raw material buffer tank 5.

[0053] As a further scheme of this embodiment, the first heat exchange and cooling device group includes a reboiler 9, a third water cooler 303 and a first heat exchanger 205, the outlet of the second compression chamber is connected to the gas phase inlet of the reboiler 9, the gas phase outlet of the reboiler 9 is connected to the heat medium inlet of the third water cooler 303, the heat medium outlet of the third water cooler 303 is connected to the heat medium inlet of the first heat exchanger 205, and the heat medium outlet of the first heat exchanger 205 is connected to the inlet of the secondary liquid separation tank 10.

[0054] As a further scheme of this embodiment, it also includes an electric heater 18, a first drying tower 11, a second drying tower 12 and a second heat exchange and cooling device group; the gas phase outlet of the secondary liquid separation tank 10 is respectively connected to the inlet of the first drying tower 11 or the inlet of the second drying tower 12, the outlet of the first drying tower 11 or the outlet of the second drying tower 12 is connected to the inlet of the second heat exchange and cooling device group, the outlet of the second heat exchange and cooling device group is connected to the refrigerant inlet of the first heat exchanger 205, the refrigerant outlet of the first heat exchanger 205 is connected to the purified dry gas external transmission pipeline, the refrigerant outlet of the first heat exchanger 205 is also respectively connected to the inlet of the electric heater 18 or the outlet of the electric heater 18, the outlet of the electric heater 18 is respectively connected to the outlet of the first drying tower 11 or the outlet of the second drying tower 12, and the inlet of the first drying tower 11 or the inlet of the second drying tower 12 are both connected to the purified dry gas external transmission pipeline.

[0055] As a further solution of this embodiment, the first heat exchange and cooling device group further includes a distillation tower 17, and the second heat exchange and cooling device group includes a second heat exchanger 204, a front cooling heat exchanger 13, an evaporative heat exchanger 14, a rear cooling heat exchanger 15, a low-temperature separator 16 and a refrigerant circulation device; the outlet of the first drying tower 11 or the outlet of the second drying tower 12 is connected to the heat medium inlet of the second heat exchanger 204, the heat medium outlet of the second heat exchanger 204 is connected to the heat medium inlet of the front cooling heat exchanger 13, the heat medium outlet of the front cooling heat exchanger 13 is connected to the heat medium inlet of the evaporative heat exchanger 14, the heat medium outlet of the evaporative heat exchanger 14 is connected to the heat medium inlet of the rear cooling heat exchanger 15, and the heat medium outlet of the rear cooling heat exchanger 15 is connected to the inlet of the low-temperature separator 16, The gaseous cold phase outlet of the low-temperature separator 16 is connected to the refrigerant inlet of the after-cooling heat exchanger 15, the refrigerant outlet of the after-cooling heat exchanger 15 is connected to the refrigerant inlet of the front-cooling heat exchanger 13, the refrigerant outlet of the front-cooling heat exchanger 13 is connected to the refrigerant inlet of the first heat exchanger 205, the outlet of the refrigerant circulation device is connected to the refrigerant inlet of the evaporative heat exchanger 14, and the refrigerant outlet of the evaporative heat exchanger 14 is connected to the inlet of the refrigerant circulation device; the liquid phase outlet of the low-temperature separator 16 is connected to the inlet of the distillation tower 17, the liquid phase outlet of the distillation tower 17 is connected to the liquid phase inlet of the reboiler 9, and the liquid phase outlet of the reboiler 9 is connected to an external mixed hydrocarbon storage tank; the gas phase outlet of the distillation tower 17 is connected to the inlet of the first liquid separation tank 8.

[0056] As a further solution of this embodiment, the low-temperature separator 16 includes a low-temperature separator body and a cold dry gas heat separation device arranged inside the low-temperature separator body, and the cold dry gas heat separation device is a velocity generator or a vortex tube.

[0057] As a further scheme of the present embodiment, it also includes an inlet buffer tank 19 and a drainage water separation tank 20, the inlet of the inlet buffer tank 19 is connected to the raw gas inlet pipeline, the outlet of the inlet buffer tank 19, the liquid phase outlet of the vacuum buffer tank 2, the liquid phase outlet of the raw material buffer tank 5 and the liquid phase outlet of the primary liquid separation tank 8 are all connected to the liquid phase inlet of the drainage water separation tank 20, the sewage outlet of the drainage water separation tank 20 is connected to an external sewage tank, and the outlet of the first drying tower 11 or the outlet of the second drying tower 12 is connected to the pressurized gas inlet of the drainage water separation tank 20.

[0058] As a further solution of this embodiment, the natural gas compressor unit includes a first natural gas compressor 6 and a second natural gas compressor 7. The first natural gas compressor 6 and the second natural gas compressor 7 are arranged in parallel and both have the first compression chamber and the second compression chamber.

[0059] like Figure 1-Figure 5 As shown, the specific working process of the present invention is as follows:

[0060] The raw gas from the joint station consists of about 70% C1, 10% C2, and 20% C3, C4, and C5. + Heavy hydrocarbons, as well as water, carbon dioxide, hydrogen sulfide, nitrogen, mechanical impurities and other components. Figure 1 and Figure 2 As shown, the raw gas inlet pipeline transports the raw gas from the joint station to the vacuum pump 1, and after being cooled by the first water cooler 301, it enters the vacuum pump buffer tank 2, and the raw gas is separated into gas and liquid in the vacuum pump buffer tank 2. Figure 1 and Figure 3 As shown, after the gas phase is discharged, it enters the first desulfurization tower 3 and the second desulfurization tower 4 connected in series or in parallel, and enters the raw material buffer tank 5 after desulfurization. The gas and liquid are separated in the raw material buffer tank 5, and the gas phase enters the first compression chamber of the first natural gas compressor 6 and the second natural gas compressor 7 for primary compression. The gas is pressurized from 0.12MPa to 0.75MPa, and is cooled from 100°C to 25°C through the second water cooler 302. It flows through the confluence device 102 and enters the primary liquid separator 8. The gas and liquid are separated in the primary liquid separator 8. The gas phase is discharged from the gas phase outlet on the top of the primary liquid separator 8 and enters the second compression chamber of the first natural gas compressor 6 and the second natural gas compressor 7 for secondary compression. The gas is pressurized from 0.75MPa to 2.15MPa. Figure 1 and Figure 4 As shown, the boosted natural gas flows through the reboiler 9 to provide heat source, then passes through the third water cooler 303 to cool down, passes through the first water cooler 205 to cool down to 15°C, and then enters the secondary liquid separation tank 10 for gas-liquid separation. The separated gas phase enters the first drying tower 11 or the second drying tower 12 for deep dehydration to less than 10PPm. The drying tower is filled with 4A molecular sieves for cyclic thermal regeneration. Figure 1 and Figure 5 As shown, the dehydrated natural gas flows through the ejector 21 and then enters the second heat exchanger 204 to recover cold and cool down, and then enters the front cold heat exchanger 13, the evaporative heat exchanger 14 and the rear cold heat exchanger 15 in sequence to cool down to about -51°C. The gas-liquid mixed phase after cooling enters the low-temperature separator 16 for gas-liquid separation. The low-temperature separator 16 is provided with a velocity generator 26. The velocity generator 26 separates the separated gas phase into a gaseous cold phase (about -70°C) and a gaseous hot phase (about -19°C). The gaseous cold phase enters the rear cold heat exchanger 15 to provide a cold source. The gas phase temperature at the refrigerant outlet of the rear cold heat exchanger 15 is about -35°C, and then enters the front cold heat exchanger 13 to provide a cold source. The gas phase temperature at the refrigerant outlet of the front cold heat exchanger 13 is about 15°C, and then enters the first heat exchanger 205 from the refrigerant inlet of the first heat exchanger 205 to realize heat exchange, as shown in FIG. Figure 4As shown, part of the dry gas after heat exchange is used for drying tower regeneration, part of it is used for crude oil heating in the reverse transmission station, and the rest of the gas goes upward into the purified dry gas transmission pipeline.

[0061] like Figure 5 As shown, the refrigerant circulation device includes an oil separator 22, a refrigeration compressor 23, a refrigerant storage tank 24, an economizer 25, a fifth water cooler 305 and a sixth water cooler 306. The refrigerant is propane or Freon or liquid ammonia. The refrigerant is stored in the refrigerant storage tank 24, flows through the economizer 25 and enters the evaporative heat exchanger 14 to provide a cold source, and then flows from the refrigerant outlet of the evaporative heat exchanger 14 to the refrigeration compressor 23 for compression, and then enters the oil separator 22 to separate the gas phase and the lubricating oil. The gas phase refrigerant is cooled to 35°C and liquefied by the sixth water cooler 306, and then enters the refrigerant storage tank 24.

[0062] The gaseous hot phase (about -19°C) separated from the low-temperature separator 16 passes through the second heat exchanger 204 to cool the heat medium flowing through it, and then a part of it passes through the combiner 102 to enter the primary liquid separation tank 8, and the other part enters the raw material buffer tank 5.

[0063] The liquid phase (-51°C) separated from the low-temperature separator 16 is discharged and heat-exchanged to -30°C through the refrigerant channel of the condensate cooler 103, and then enters the distillation tower 17 used in conjunction with the reboiler 9. After gas-liquid separation, the gaseous C1 and C2 enter the primary liquid separator 8 through the confluence 102, and the liquid phase heats up to 25°C with the natural gas flowing through the reboiler 9. The liquid phase C3, C4 and C5 + Enter the mixed hydrocarbon storage tank along the pipeline.

[0064] Specifically, Figure 3 As shown, the first desulfurization tower 3 and the second desulfurization tower 4 connected in series or in parallel can be connected in parallel or in series, and can be positive or reversible when connected in series. The first valve F1 and the second valve F2 are respectively provided on the pipeline connecting the inlet of the first desulfurization tower 3 and the inlet of the second desulfurization tower 4 with the gas phase outlet of the vacuum pump buffer tank 2, and the fifth valve F5 and the sixth valve F6 are respectively provided on the pipeline connecting the outlet of the first desulfurization tower 3 and the outlet of the second desulfurization tower 4 with the raw material buffer tank 5. The outlet of the first desulfurization tower 3 is connected to the inlet of the second desulfurization tower 4 through a pipeline and a third valve F3 is provided on the pipeline. The inlet of the first desulfurization tower 3 and the outlet of the second desulfurization tower 4 are connected through a pipeline and a fourth valve F4 is provided on the pipeline. The gas phase outlet of the vacuum pump buffer tank 2 and the inlet of the raw material buffer tank 5 are connected through a pipeline and a seventh valve F7 is provided on the pipeline.

[0065] When desulfurization treatment is not required, close the first valve F1, the second valve F2, the third valve F3, the fourth valve F4, the fifth valve F5 and the sixth valve F6, open the seventh valve F7, and the gas phase outlet of the vacuum buffer tank 2 is directly connected to the inlet of the raw material buffer tank 5.

[0066] When the first desulfurization tower 3 and the second desulfurization tower 4 are connected in parallel, the third valve F3, the fourth valve F4 and the seventh valve F7 are closed, and the first valve F1, the second valve F2, the fifth valve F5 and the sixth valve F6 are opened. The gas phase discharged from the vacuum pump buffer tank 2 enters the first desulfurization tower 3 and the second desulfurization tower 4 respectively, and then enters the raw material buffer tank 5 respectively. When the desulfurizer in the desulfurization tower needs to be replaced, any desulfurization tower can be cut off and replaced on the basis of the two towers in parallel. Specifically, when the desulfurizer in the first desulfurization tower 3 needs to be replaced, the first valve F1 and the fifth valve F5 can be closed; when the desulfurizer in the second desulfurization tower 4 needs to be replaced, the second valve F2 and the sixth valve F6 can be closed.

[0067] When the first desulfurization tower 3 and the second desulfurization tower 4 are connected in series, two series connection methods can be adopted. The first method is that the natural gas first enters the first desulfurization tower 3 and then enters the second desulfurization tower 4, opens the first valve F1, the third valve F3 and the sixth valve F6, and closes the second valve F2, the fourth valve F4, the fifth valve F5 and the seventh valve F7. The second method is that the natural gas first enters the second desulfurization tower 4 and then enters the first desulfurization tower 3, opens the second valve F2, the fourth valve F4 and the fifth valve F5, and closes the first valve F1, the third valve F3, the sixth valve F6 and the seventh valve F7.

[0068] Specifically, Figure 4As shown, the first drying tower 11 or the second drying tower 12 is arranged in parallel, one of the two drying towers is in an adsorption state, and the other is in a desorption regeneration state. After desorption is completed, the states of the two towers are switched. A ninth valve F9 and an eleventh valve F11 are respectively provided on the pipelines connecting the inlet of the first drying tower 11 and the inlet of the second drying tower 12 with the gas phase outlet of the secondary liquid separator 10, a thirteenth valve F13 and a fifteenth valve F15 are respectively provided on the pipelines connecting the outlet of the first drying tower 11 and the outlet of the second drying tower 12 with the second heat exchanger 204, an eighth valve F8 and a tenth valve F10 are respectively provided on the pipelines connecting the inlet of the first drying tower 11 and the inlet of the second drying tower 12 with the heat medium inlet of the fourth water cooler 304, the hot coal outlet of the fourth water cooler 304 is connected to the purified dry gas transmission pipeline, and the first drying tower 11 is connected to the gas phase outlet of the second water cooler 304, and the hot coal outlet of the first drying tower 11 is connected to the purified dry gas transmission pipeline. A twelfth valve F12 and a fourteenth valve F14 are respectively provided on the pipes connecting the outlet of tower 11 and the outlet of the second drying tower 12 with the outlet of the electric heater 18, an eighteenth valve F18 is provided on the connecting pipe between the refrigerant outlet of the first heat exchanger 205 and the inlet of the electric heater 18, the refrigerant outlet of the first heat exchanger 205 and the outlet pipeline of the electric heater 18 are connected through a connecting pipe, a seventeenth valve F17 is provided on the connecting pipe, the connecting pipe at the outlet end of the seventeenth valve F17 is also connected to the heat medium inlet of the fourth water cooler 304 through a pipe, and a sixteenth valve F16 is provided on the pipe.

[0069] When the first drying tower 11 is in the adsorption state and the second drying tower 12 is in the desorption state, the ninth valve F9, the thirteenth valve F13, the tenth valve F10, the fourteenth valve F14 and the eighteenth valve F18 are opened, and the eleventh valve F11, the fifteenth valve F15, the eighth valve F8, the twelfth valve F12 and the sixteenth valve F16 are closed. First, the seventeenth valve F17 is in the closed state, and the gas phase discharged from the second liquid separation tank 10 passes through the first drying tower 11 and enters the second heat exchanger 204. A part of the natural gas discharged from the refrigerant outlet of the first heat exchanger 205 passes through the eighteenth valve F18 and enters the electric heater 18 to be heated to 200. ℃, and then enters the second drying tower 12 in reverse through the fourteenth valve F14, heats the molecular sieve for desorption, and then is discharged from the inlet of the second drying tower 12, passes through the tenth valve F10 and the fourth water cooler 304 for cooling and external transmission, after heating and desorption for 4 hours, closes the eighteenth valve F18 and opens the seventeenth valve F17, and the natural gas part discharged from the refrigerant outlet of the first heat exchanger 205 passes through the seventeenth valve F17, reversely enters the second drying tower 12 to cool the molecular sieve for 4 hours, and then closes the tenth valve F10 and the fourteenth valve F14, opens the sixteenth valve F16, and the natural gas is directly externally transmitted through the pipeline where the sixteenth valve F16 is located. The states of the two drying towers are switched every 24 hours. After the switching, the valves are in the following states: the eleventh valve F11, the fifteenth valve F15, the eighth valve F8, the twelfth valve F12 and the eighteenth valve F18 are open, and the ninth valve F9, the thirteenth valve F13, the tenth valve F10, the fourteenth valve F14, the sixteenth valve F16 and the seventeenth valve F17 are closed. The gas phase discharged from the second liquid separator 10 passes through the second drying tower 12 and enters the second heat exchanger 204. A part of the natural gas discharged from the refrigerant outlet of the first heat exchanger 205 passes through the eighteenth valve F18 and enters the electric heater 18 to be heated to 200°C, and then passes through the twelfth valve F12 to reversely enter the first drying tower 11, heats the molecular sieve for desorption, and then is discharged from the inlet of the first drying tower 11, passes through the eighth valve F8 and the fourth water cooler 304 to cool down and transport outward. After heating and desorption for 4 hours, the eighteenth valve F18 is closed and the seventeenth valve F17 is opened. A part of the natural gas discharged from the refrigerant outlet of the first heat exchanger 205 passes through the seventeenth valve F17, reversely enters the first drying tower 11 to cool down the molecular sieve for 4 hours, then the eighth valve F8 and the twelfth valve F12 are closed, the sixteenth valve F16 is opened, and the natural gas is directly transported outward through the pipeline where the sixteenth valve F16 is located.

[0070] Specifically, an inlet buffer tank 19 is connected to the raw gas inlet pipeline, and the inlet buffer tank 19 stabilizes the natural gas in the system. The outlet of the inlet buffer tank 19, the liquid phase outlet of the vacuum pump buffer tank 2, the liquid phase outlet of the raw material buffer tank 5 and the liquid phase outlet of the first liquid separator 8 are all connected to the liquid phase inlet of the drainage water separator 20, and water and light oil enter the drainage water separator 20. Part of the pressurized gas at the outlet of the first drying tower 11 and the second drying tower 12 enters from the gas phase inlet of the drainage water separator 20 along the pipeline to provide low temperature and pressure for the drainage water separator 20. The oily wastewater separated in the drainage water separator 20 enters the sewage tank, and the light oil separated in the drainage water separator 20 and the liquid phase separated by the secondary liquid separator 10 are cooled and separated by the condensate cooler 103. The gas phase enters the ejector 21, and the liquid phase goes to the mixed hydrocarbon storage tank.

[0071] Specifically, Figure 6 and Figure 7 As shown, the velocity generator 26 includes an end cover 264, a main shell 265 and an air outlet pipe 266. The end cover 264 and the main shell 265 are ground together and fixedly connected by bolts 263. An air inlet 262 is arranged along a parabola from a tangent direction between one end of the end cover 264 and one end of the main shell 265. The width d of the air inlet 262 is 2.5 mm. The diameter of the main shell 265 is 400 mm. The main shell 265 has a gaseous hot phase outlet 261 and a balance pipe 267 arranged along a tangent direction. The air outlet pipe 266 is fixedly connected to the middle of the other end of the main shell 265 and communicates with the inner cavity of the main shell 265. The end cover 264 is also fixedly connected to a guide plate arranged inside the main shell 265. After the gas enters from the air inlet 262, it forms a high-speed vortex in the main shell 265. The gas temperature at the center of the main shell 265 is relatively low, which is called the gas cold phase and is discharged from the gas outlet 266. The gas temperature around the main shell 265 is relatively high, which is called the gas hot phase and is discharged from the gas hot phase outlet 261. Figure 6 As shown, the gaseous hot phase outlet 261 is connected to the balance pipe 267, and the gaseous hot phase outlet 261 and the balance pipe 267 are both connected to the inner cavity of the main shell 265. A valve for controlling the flow rate is provided on the gaseous hot phase outlet 261 pipeline, and the gaseous hot phase outlet 261 and the balance pipe 267 are also provided with a regulating valve, such as Figure 6 As shown, the gas rotates counterclockwise at a speed of 1 Mach in the main shell 265, and part of the gaseous hot phase is discharged from the gaseous hot phase outlet 261. One end of the balance pipe 267 is connected to the main shell 265 and the gaseous hot phase outlet 261, and the other end is closed. Another part of the gaseous hot phase returns to the main shell 265 through the balance pipe 267.

[0072] Specifically, Figure 8As shown, in the present invention, the heat medium pipes of the first water cooler 301, the second water cooler 302, the third water cooler 303, the fourth water cooler 304, the fifth water cooler 305 and the sixth water cooler 306 are installed side by side to form a centralized water cooler 27, which provides refrigerant in a centralized manner, has a compact structure, and is more energy-efficient. The centralized water cooler 27 and multiple heat exchangers use high-efficiency rust-proof aluminum plate-fin heat exchangers, and the heat exchange of multiple streams is reasonably set to make full use of the heat source and the cooling capacity of the medium, reduce energy consumption, and reduce the operating cost of the device. The skid-mounted natural gas processing device of the present invention is installed on the first skid M101, the second skid M102, the third skid M103 and the fourth skid M104 respectively, with a compact and rigorous structure, and the position and combination structure of each skid can be flexibly adjusted according to the on-site terrain conditions.

[0073] In the present invention, the valve opening or closing can be realized by adopting the control method of the prior art, or by manual adjustment. For the sake of simplicity, it will not be repeated here. Figure 1-Figure 5 When describing the relationship between devices, the term 'connect' or 'connected' refers to connection through pipelines unless otherwise clearly specified and limited.

[0074] In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0075] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0076] In the description of this specification, the description with reference to the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0077] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0078] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A skid-mounted natural gas processing device, characterized in that: It is installed on a plurality of skids, and comprises a natural gas compressor unit, a second water cooler (302), a first liquid separator tank (8), a first heat exchange and cooling device group, and a second liquid separator tank (10). The natural gas compressor unit comprises a first compression chamber and a second compression chamber. The inlet of the first compression chamber is used to introduce natural gas. The outlet of the first compression chamber is connected to the inlet of the first liquid separator tank (8) through the second water cooler (302). The gas phase outlet of the first liquid separator tank (8) is connected to the inlet of the second compression chamber. The outlet of the second compression chamber is connected to the inlet of the second liquid separator tank (10) through the first heat exchange and cooling device group. The gas phase outlet of the second liquid separator tank (10) is used to discharge the treated natural gas. The first heat exchange and cooling device group comprises a reboiler (9), a third water cooler (303) and a first heat exchanger (205); the outlet of the second compression chamber is connected to the gas phase inlet of the reboiler (9); the gas phase outlet of the reboiler (9) is connected to the heat medium inlet of the third water cooler (303); the heat medium outlet of the third water cooler (303) is connected to the heat medium inlet of the first heat exchanger (205); and the heat medium outlet of the first heat exchanger (205) is connected to the inlet of the secondary liquid separation tank (10); The skid-mounted natural gas processing device further comprises an electric heater (18), a first drying tower (11), a second drying tower (12) and a second heat exchange and cooling device group; the gas phase outlet of the secondary liquid separation tank (10) is respectively connected to the inlet of the first drying tower (11) or the inlet of the second drying tower (12); the first drying tower (11) or the second drying tower (12) is filled with 4A type molecular sieve; the outlet of the first drying tower (11) or the outlet of the second drying tower (12) is connected to the inlet of the second heat exchange and cooling device group; the outlet of the second heat exchange and cooling device group is connected to the outlet of the second drying tower (11); The refrigerant outlet of the first heat exchanger (205) is connected to the refrigerant inlet of the first heat exchanger (205), the refrigerant outlet of the first heat exchanger (205) is connected to the purified dry gas external transmission pipeline, the refrigerant outlet of the first heat exchanger (205) is also connected to the inlet of the electric heater (18) or the outlet of the electric heater (18), the outlet of the electric heater (18) is connected to the outlet of the first drying tower (11) or the outlet of the second drying tower (12), and the inlet of the first drying tower (11) or the inlet of the second drying tower (12) is connected to the purified dry gas external transmission pipeline; The first heat exchange and cooling device group further comprises a distillation tower (17); the second heat exchange and cooling device group comprises a second heat exchanger (204), a front cooling heat exchanger (13), an evaporative heat exchanger (14), a rear cooling heat exchanger (15), a low-temperature separator (16) and a refrigerant circulation device; the outlet of the first drying tower (11) or the outlet of the second drying tower (12) is connected to the heat medium inlet of the second heat exchanger (204); the heat medium outlet of the second heat exchanger (204) is connected to the heat medium inlet of the front cooling heat exchanger (13); the heat medium outlet of the front cooling heat exchanger (13) is connected to the heat medium inlet of the evaporative heat exchanger (14); the heat medium outlet of the evaporative heat exchanger (14) is connected to the heat medium inlet of the rear cooling heat exchanger (15); the heat medium outlet of the rear cooling heat exchanger (15) is connected to the inlet of the low-temperature separator (16); and the low-temperature separator (16) is connected to the heat medium inlet of the rear cooling heat exchanger (15). The gaseous cold phase outlet of the separator (16) is connected to the refrigerant inlet of the after-cooling heat exchanger (15), the refrigerant outlet of the after-cooling heat exchanger (15) is connected to the refrigerant inlet of the front-cooling heat exchanger (13), the refrigerant outlet of the front-cooling heat exchanger (13) is connected to the refrigerant inlet of the first heat exchanger (205), the outlet of the refrigerant circulation device is connected to the refrigerant inlet of the evaporative heat exchanger (14), and the refrigerant outlet of the evaporative heat exchanger (14) is connected to the inlet of the refrigerant circulation device; the liquid phase outlet of the low-temperature separator (16) is connected to the inlet of the distillation tower (17), the liquid phase outlet of the distillation tower (17) is connected to the liquid phase inlet of the reboiler (9), and the liquid phase outlet of the reboiler (9) is connected to an external mixed hydrocarbon storage tank; the gas phase outlet of the distillation tower (17) is connected to the inlet of the first-stage liquid separation tank (8).

2. A skid-mounted natural gas processing device according to claim 1, characterized in that: It also includes an air extraction device, a desulfurization tower group and a raw material buffer tank (5), wherein the inlet of the air extraction device is connected to the raw material gas inlet pipeline, and the outlet thereof is connected to the inlet of the desulfurization tower group, the outlet of the desulfurization tower group is connected to the inlet of the raw material buffer tank (5), and the gas phase outlet of the raw material buffer tank (5) is connected to the inlet of the first compression chamber of the natural gas compressor group.

3. The skid-mounted natural gas processing device according to claim 2, characterized in that: The air extraction device comprises an air extractor (1), a first water cooler (301) and an air extractor buffer tank (2); the inlet of the air extractor (1) is connected to a raw gas inlet pipeline, the outlet of the air extractor (1) is connected to a heat medium inlet of the first water cooler (301), the heat medium outlet of the first water cooler (301) is connected to an inlet of the air extractor buffer tank (2), and the gas phase outlet of the air extractor buffer tank (2) is connected to an inlet of the desulfurization tower group.

4. The skid-mounted natural gas processing device according to claim 2, characterized in that: The desulfurization tower group comprises a first desulfurization tower (3) and a second desulfurization tower (4) connected in parallel or in series, the outlet of the air extraction device is connected to the inlet of the first desulfurization tower (3) and / or the inlet of the second desulfurization tower (4), and the outlet of the first desulfurization tower (3) and / or the outlet of the second desulfurization tower (4) are both connected to the inlet of the raw material buffer tank (5).

5. The skid-mounted natural gas processing device according to claim 1, characterized in that: The low-temperature separator (16) comprises a low-temperature separator body and a cold dry gas heat separation device arranged inside the low-temperature separator body, wherein the cold dry gas heat separation device is a velocity generator or a vortex tube.

6. The skid-mounted natural gas processing device according to claim 1, characterized in that: It also includes an inlet buffer tank (19) and a drainage water separation tank (20), wherein the inlet of the inlet buffer tank (19) is connected to the raw gas inlet pipeline, the outlet of the inlet buffer tank (19) and the liquid phase outlet of the first-level liquid separation tank (8) are both connected to the liquid phase inlet of the drainage water separation tank (20), the sewage outlet of the drainage water separation tank (20) is connected to an external sewage tank, and the outlet of the first drying tower (11) or the outlet of the second drying tower (12) is connected to the pressurized gas inlet of the drainage water separation tank (20).

7. A skid-mounted natural gas processing device according to any one of claims 1 to 6, characterized in that: The natural gas compressor unit comprises a first natural gas compressor (6) and a second natural gas compressor (7); the first natural gas compressor (6) and the second natural gas compressor (7) are arranged in parallel and both have the first compression chamber and the second compression chamber.

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