CN216898061U - Nitrogen-containing natural gas denitrification liquefaction device - Google Patents

Nitrogen-containing natural gas denitrification liquefaction device Download PDF

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Publication number
CN216898061U
CN216898061U CN202122137567.1U CN202122137567U CN216898061U CN 216898061 U CN216898061 U CN 216898061U CN 202122137567 U CN202122137567 U CN 202122137567U CN 216898061 U CN216898061 U CN 216898061U
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channel
inlet
pipeline
nitrogen
denitrification
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马忠
池红军
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Sichuan Shudao Equipment Technology Co ltd
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Sichuan Shudao Equipment Technology Co ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/18—External refrigeration with incorporated cascade loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The utility model discloses a nitrogen-containing natural gas denitrification liquefying device, which solves the technical problem that in the prior art, non-condensable gases such as nitrogen and the like are circularly accumulated in a natural gas liquefying device, so that BOG is continuously increased. The device comprises a main heat exchanger (2), a heavy hydrocarbon separator (3), a denitrification tower (4), a denitrification tower condenser (5), a denitrification tower reflux tank (6), an LNG storage tank (7), a BOG heater (8), a BOG compressor (9) and an MR separator (10). The cold quantity at the top of the denitrification tower is from light refrigerant with high nitrogen content separated at low temperature, so that the yield of the methane in the device is ensured; the heat source at the bottom of the tower is from high-temperature feed gas, so that the content of nitrogen in the liquefied natural gas is lower than 1%. The method has the advantages of simple flow, low production cost, high methane extraction rate, high denitrification efficiency, strong operability, safety, reliability and low energy consumption, and can obtain good environmental protection benefit and economic benefit.

Description

Nitrogen-containing natural gas denitrification liquefaction device
Technical Field
The utility model relates to a natural gas liquefaction device, in particular to a nitrogen-containing natural gas denitrification liquefaction device.
Background
In recent years, natural gas is used as a preferred fuel in many countries, and the development and utilization of natural gas are the mainstream of energy development in the world today. The natural gas contains hydrocarbons as main components and also contains a small amount of non-hydrocarbons, such as non-condensable gases like nitrogen, argon, helium, etc. When the content of non-condensable gas (such as nitrogen, argon, helium and the like) in natural gas is high, the calorific value of the natural gas is influenced, and the energy consumption in the liquefaction process is high. According to european standards (EN1160), the nitrogen content (mole fraction) in the Liquefied Natural Gas (LNG) product should be less than 5%, and experience has shown that the rollover phenomenon during storage and transportation of LNG can be effectively avoided by controlling the nitrogen content in LNG to be less than 1% and by enhancing monitoring of boil-off gas.
In the natural gas liquefaction process, after the BOG generated by the large LNG tank is compressed by the BOG compressor, one part of the BOG is used as fuel gas of a liquefaction plant, and the other part of the BOG needs to be fed into the cold box again for reliquefaction. In this process, noncondensable gases such as nitrogen gas are cyclically accumulated in the device, and if the noncondensable gases such as nitrogen are not removed, BOG generated in the LNG tank is increased continuously, thereby forming a vicious circle.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a nitrogen-containing natural gas denitrification liquefaction device, which aims to solve the technical problem that in the prior art, non-condensable gases such as nitrogen and the like are circularly accumulated in a natural gas liquefaction device, so that BOG is continuously increased.
In order to realize the purpose, the utility model provides the following technical scheme:
the utility model provides a nitrogen-containing natural gas denitrification liquefaction device which comprises a main heat exchanger, a heavy hydrocarbon separator, a denitrification tower condenser, a denitrification tower reflux tank, an LNG storage tank, a BOG heater, a BOG compressor and an MR low-temperature separator, wherein the main heat exchanger is connected with the heavy hydrocarbon separator;
a raw material natural gas channel I, a raw material natural gas channel II, a BOG channel, a liquefied natural gas channel I, a nitrogen-rich tail gas channel I, a high-pressure liquid phase refrigerant channel I, a high-pressure gas phase refrigerant channel II, a high-pressure liquid phase refrigerant channel II and a backflow refrigerant channel I are arranged in the main heat exchanger;
a nitrogen-rich tail gas channel II and a return refrigerant channel II are arranged in the denitrogenation tower condenser;
the inlet end of the raw material natural gas channel I is connected with an external raw material gas purification pipeline, the outlet end of the raw material natural gas channel I is connected with an inlet 3-A of a heavy hydrocarbon separator, an outlet 3-B of the heavy hydrocarbon separator is connected with an external heavy hydrocarbon heating and storing pipeline, an outlet 3-C pipeline of the heavy hydrocarbon separator is divided into a pipeline I and a pipeline II, the pipeline I is connected with an inlet 4-F of a denitrification tower, the pipeline II is connected with the inlet end of the raw material natural gas channel I, the outlet end of the raw material natural gas channel I is connected with an inlet 4-A of the denitrification tower, an outlet 4-C of the denitrification tower is connected with an inlet end of a nitrogen-rich tail gas channel II, an outlet end of the nitrogen-rich tail gas channel II is connected with an inlet 6-A of a denitrification tower reflux tank, and an outlet 6-C of the denitrification tower reflux tank is connected with an inlet 4-D of the denitrification tower, an outlet 6-B of the nitrogen-rich tail gas channel I is connected with an inlet end of a nitrogen-rich tail gas channel I, an outlet end of the nitrogen-rich tail gas channel I is connected with an external nitrogen-rich gas-removing fuel gas pipeline, an inlet end of a liquefied natural gas channel I is connected with an outlet 4-E of the nitrogen removal tower, an outlet end of the liquefied natural gas channel I is connected with an inlet 7-A of an LNG storage tank, an outlet 7-B of the LNG storage tank is connected with an inlet 8-A of a BOG heater, the BOG compressor is respectively connected with an outlet 8-B of the BOG heater and an inlet end of the BOG channel, an outlet end of the BOG channel is connected with an inlet 4-B of the nitrogen removal tower, an inlet end of a high-pressure liquid-phase refrigerant channel I is connected with an external high-pressure liquid-phase pipeline, and an outlet end of the high-pressure liquid-phase refrigerant channel I is connected with an inlet 110-A of a return refrigerant channel I, the inlet end of the high-pressure gas-phase refrigerant channel I is connected with an external high-pressure refrigerant gas-phase pipeline, the outlet end of the high-pressure gas-phase refrigerant channel I is connected with the inlet 10-A of the MR low-temperature separator, the outlet 10-B of the MR low-temperature separator is connected with the inlet end of the high-pressure liquid-phase refrigerant channel II, the outlet end of the high-pressure liquid-phase refrigerant channel II is connected with the inlet 110-B of the backflow refrigerant channel I, the outlet 10-C of the MR low-temperature separator is connected with the inlet end of the high-pressure gas-phase refrigerant channel II, the outlet end pipeline of the high-pressure gas-phase refrigerant channel II is divided into a pipeline III and a pipeline IV, the pipeline III is connected with the inlet 110-C of the backflow refrigerant channel I, the pipeline IV is connected with the inlet end of the backflow refrigerant channel II of the condenser of the denitrification tower, the outlet end of the backflow refrigerant channel II of the condenser of the denitrification tower is connected with the inlet 110-C of the backflow refrigerant channel I, and the return refrigerant channel I is connected with a return refrigerant pipeline.
Optionally or preferably, the main heat exchanger and the denitrogenation tower condenser can be any one of a plate-fin heat exchanger, a wound tube heat exchanger or a shell-and-tube heat exchanger.
Optionally or preferably, the denitrification tower is a packed tower or a plate tower.
Optionally or preferably, a connecting pipeline between the outlet end of the BOG channel and the inlet 4-B of the denitrification tower is provided with a regulating valve B; a regulating valve c is arranged on a connecting pipeline between the outlet end of the raw natural gas channel I and the inlet 4-A of the denitrification tower; a regulating valve e is arranged on a connecting pipeline between the outlet end of the high-pressure liquid-phase refrigerant channel I and the inlet 110-A of the return refrigerant channel I; a regulating valve f is arranged on a connecting pipeline between the outlet end of the high-pressure liquid-phase refrigerant channel II and the inlet 110-B of the return refrigerant channel I; and a regulating valve g is arranged on a connecting pipeline between the pipeline III and the inlet 110-C of the return refrigerant channel I.
Optionally or preferably, the pipeline I is provided with an adjusting valve a, a tower kettle of the denitrification tower is provided with a temperature digital controller b, and the temperature digital controller b controls the adjusting valve a logically.
Optionally or preferably, a regulating valve d is arranged on a connecting pipeline between the outlet 7-B of the LNG storage tank and the inlet 8-a of the BOG heater, and a pressure digital controller e is arranged on the LNG storage tank and controls the regulating valve d logically.
Optionally or preferably, a regulating valve h is arranged on a connecting pipeline between the outlet end of the liquefied natural gas channel I and the inlet 7-A of the LNG storage tank, a liquid level digital controller a is arranged at a tower kettle of the denitrification tower, and the liquid level digital controller a controls the regulating valve h logically.
Optionally or preferably, a regulating valve i is arranged on a connecting pipeline between the outlet 6-B of the nitrogen removal tower reflux tank and the inlet end of the nitrogen-rich tail gas channel I, a pressure digital controller d is arranged on the nitrogen removal tower reflux tank, and the pressure digital controller d controls the regulating valve i logically.
Optionally or preferably, an adjusting valve j is arranged on a connecting pipeline between the pipeline IV and the inlet end of the return refrigerant channel II of the denitrification tower condenser, a temperature digital controller c is arranged on a connecting pipeline between the outlet end of the nitrogen-rich tail gas channel II and the inlet 6-A of the denitrification tower reflux tank, and the temperature digital controller c controls the adjusting valve j logically.
Based on the technical scheme, the embodiment of the utility model can at least produce the following technical effects:
(1) compared with the prior art, the nitrogen-containing natural gas denitrification liquefying device is improved in the aspect of uniform heat distribution on the connection relationship of the device. The utility model adopts the technical scheme that the high-temperature-pumped feed gas in the main heat exchanger enters the tower kettle of the denitrification tower to control the temperature of the tower kettle and control the content of nitrogen in LNG, thereby reducing the setting of a reboiler of the denitrification tower. Meanwhile, the device increases the BOG re-liquefaction denitrification process, effectively solves the problem of the cyclic accumulation of nitrogen in the process of liquefying natural gas, reduces the phenomenon that the nitrogen content of LNG is high and the LNG turns over, avoids the condition that safety accidents are possibly caused due to the fact that the upper density and the lower density of the storage tank are inconsistent, and has the advantages of safety, reliability, wide practicability and the like.
(2) The utility model provides a liquefaction process for nitrogen removal of nitrogen-containing natural gas, which sequentially carries out heavy hydrocarbon removal treatment and nitrogen removal treatment on natural gas to be treated and heating, compressing and retreating the generated BOG and has the advantages of simple process, low production cost, high methane extraction rate, strong operability, safety, reliability and the like.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
In the figure: 1. a purified feed gas line; 2. a primary heat exchanger; 3. a heavy hydrocarbon separator; 4. a denitrification tower; 5. a denitrogenation tower condenser; 6. a denitrification tower reflux tank; 7. an LNG storage tank; 8. a BOG heater; 9. a BOG compressor; 10. an MR cryoseparator; 11. adjusting valve b; 12. adjusting valve c; 13. adjusting a valve d; 14. adjusting a valve e; 15. adjusting the valve f; 16. adjusting a valve g; 17. adjusting a valve h; 18. adjusting a valve i; 19. adjusting a valve j; 20. a fuel gas line; 21. a return refrigerant line; 22. a high pressure refrigerant gas phase line; 23. a high pressure refrigerant liquid phase line; 24. a liquid level digital controller a; 25. a temperature digital controller b; 26. a temperature digital controller c; 27. a pressure digital controller d; 28. a pressure digital controller e; 29. adjusting a valve a; 101-raw material natural gas channel I, 102-raw material natural gas channel II, 103-BOG channel, 104-liquefied natural gas channel I, 105-nitrogen-rich tail gas channel I, 106-high-pressure liquid phase refrigerant channel I, A7-high-pressure gas phase refrigerant channel I, 108-high-pressure gas phase refrigerant channel II, 109-high-pressure liquid phase refrigerant channel II, 110-reflux refrigerant channel I, 501-nitrogen-rich tail gas channel II and 502-reflux refrigerant channel II; 30. a pipeline I; 31. a pipeline II; 32. a line III; 33. line IV.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below. It is to be understood that the described embodiments are merely exemplary of the utility model, and not restrictive of the full scope of the utility model. All other embodiments, which can be derived by a person skilled in the art from the examples given herein without any inventive step, are within the scope of the present invention.
Examples
As shown in fig. 1:
the utility model provides a nitrogen-containing natural gas denitrification liquefaction device which comprises a main heat exchanger 2, a heavy hydrocarbon separator 3, a denitrification tower 4, a denitrification tower condenser 5, a denitrification tower reflux tank 6, an LNG storage tank 7, a BOG heater 8, a BOG compressor 9 and an MR low-temperature separator 10;
a raw material natural gas channel I101, a raw material natural gas channel II 102, a BOG channel 103, a liquefied natural gas channel I104, a nitrogen-rich tail gas channel I105, a high-pressure liquid phase refrigerant channel I106, a high-pressure gas phase refrigerant channel IA 7, a high-pressure gas phase refrigerant channel II 108, a high-pressure liquid phase refrigerant channel II 109 and a return refrigerant channel I110 are arranged in the main heat exchanger 2;
a nitrogen-rich tail gas channel II 501 and a return refrigerant channel II 502 are arranged in the denitrification tower condenser 5;
the inlet end of the raw material natural gas channel I101 is connected with an external purification raw material gas pipeline 1, the outlet end of the raw material natural gas channel I101 is connected with an inlet 3-A of a heavy hydrocarbon separator 3, an outlet 3-B of the heavy hydrocarbon separator 3 is connected with an external heavy hydrocarbon heating and storing pipeline, an outlet 3-C pipeline of the heavy hydrocarbon separator 3 is divided into a pipeline I30 and a pipeline II 31, the pipeline I30 is connected with an inlet 4-F of a denitrification tower 4, the pipeline II 31 is connected with the inlet end of the raw material natural gas channel I101, the outlet end of the raw material natural gas channel I101 is connected with an inlet 4-A of the denitrification tower 4, an outlet 4-C of the denitrification tower 4 is connected with an inlet end of a nitrogen-rich tail gas channel II 501, the outlet end of the nitrogen-rich tail gas channel II 501 is connected with an inlet 6-A of a denitrification tower reflux tank 6, an outlet 6-C of the denitrification tower reflux tank 6 is connected with an inlet 4-D of the denitrification tower 4, an outlet 6-B of the denitrification tower reflux tank 6 is connected with an inlet end of a nitrogen-rich tail gas channel I105, an outlet end of the nitrogen-rich tail gas channel I105 is connected with an external nitrogen-rich gas-removing fuel gas pipeline 20, an inlet end of an liquefied natural gas channel I104 is connected with an outlet 4-E of the denitrification tower 4, an outlet end of the liquefied natural gas channel I104 is connected with an inlet 7-A of an LNG storage tank 7, an outlet 7-B of the LNG storage tank 7 is connected with an inlet 8-A of a BOG heater 8, a BOG compressor 9 is respectively connected with an outlet 8-B of the BOG heater 8 and an inlet end of the BOG channel 103, an outlet end of the BOG channel 103 is connected with the inlet 4-B of the denitrification tower 4, an inlet end of a high-pressure liquid phase refrigerant channel I106 is connected with an external high-pressure liquid phase refrigerant pipeline 23, the outlet end of the high-pressure liquid-phase refrigerant channel I106 is connected with the inlet 110-A of the backflow refrigerant channel I110, the inlet end of the high-pressure gas-phase refrigerant channel IA 7 is connected with an external high-pressure refrigerant gas-phase pipeline 22, the outlet end of the high-pressure gas-phase refrigerant channel IA 7 is connected with the inlet 10-A of the MR low-temperature separator 10, the outlet 10-B of the MR low-temperature separator 10 is connected with the inlet end of the high-pressure liquid-phase refrigerant channel II 109, the outlet end of the high-pressure liquid-phase refrigerant channel II 109 is connected with the inlet 110-B of the backflow refrigerant channel I110, the outlet 10-C of the MR low-temperature separator 10 is connected with the inlet end of the high-pressure gas-phase refrigerant channel II 108, the outlet pipeline of the high-pressure gas-phase refrigerant channel II 108 is divided into a pipeline III 32 and a pipeline IV 33, the pipeline III 32 is connected with the inlet 110-C of the backflow refrigerant channel I110, the pipeline IV 33 is connected with the inlet end of a return refrigerant channel II 502 of the denitrification tower condenser 5, the outlet end of the return refrigerant channel II 502 of the denitrification tower condenser 5 is connected with an inlet 110-C of a return refrigerant channel I110, and the return refrigerant channel I110 is connected with a return refrigerant pipeline 21.
According to the utility model, through reasonably designing the gas and liquid flow in the nitrogen removal process of the nitrogen-containing natural gas, the heat and cold of each product component are fully utilized, the energy consumption for treating the nitrogen-containing natural gas with the same volume is effectively saved, and the treatment cost of the nitrogen-containing natural gas is reduced; meanwhile, a BOG denitrification reprocessing line is additionally arranged in the pipeline of the device, so that the content of nitrogen in the natural gas stored in the treated LNG storage tank is further reduced, the problem that the LNG is high in nitrogen content and rolls over due to the fact that the nitrogen is accumulated circularly in the process of liquefying the natural gas is effectively solved, the situation that safety accidents are possibly caused due to the fact that the upper density and the lower density of the LNG storage tank are inconsistent is avoided, and the device has the advantages of being safe, reliable, wide in practicability and the like.
Optionally or preferably, the main heat exchanger 2 and the denitrification tower condenser 5 can be any one of a plate-fin heat exchanger, a wound-tube heat exchanger or a shell-and-tube heat exchanger.
Alternatively or preferably, the denitrification tower 4 is a packed tower or a plate tower.
Optionally or preferably, a regulating valve B11 is arranged on a connecting line between the outlet end of the BOG channel 103 and the inlet 4-B of the denitrification tower 4; a connecting pipeline between the outlet end of the raw natural gas channel I101 and the inlet 4-A of the denitrification tower 4 is provided with an adjusting valve c 12; a connecting pipeline between the outlet end of the high-pressure liquid-phase refrigerant channel I106 and the inlet 110-A of the return refrigerant channel I110 is provided with an adjusting valve e 14; a regulating valve f15 is arranged on a connecting pipeline between the outlet end of the high-pressure liquid-phase refrigerant channel II 109 and the inlet 110-B of the return refrigerant channel I110; and a regulating valve g16 is arranged on a connecting pipeline between the pipeline III 32 and the inlet 110-C of the return refrigerant channel I110.
According to the utility model, the regulating valves with different functions are reasonably arranged in the denitrification device, so that the production flow of the denitrification device can be conveniently and orderly regulated and managed according to the actual needs in the production process, and the operability of the device is stronger.
Optionally or preferably, the pipeline i 30 is provided with a regulating valve a29, the bottom of the denitrification tower 4 is provided with a temperature digital controller b25, and the temperature digital controller b25 controls the regulating valve a29 in a logic mode.
Optionally or preferably, a regulating valve d13 is arranged on a connecting line between the outlet 7-B of the LNG storage tank 7 and the inlet 8-a of the BOG heater 8, a pressure digital controller e28 is arranged on the LNG storage tank 7, and the pressure digital controller e28 controls the regulating valve d13 in a logic mode.
Optionally or preferably, a regulating valve h17 is arranged on a connecting pipeline between the outlet end of the liquefied natural gas channel I104 and the inlet 7-A of the LNG storage tank 7, a liquid level digital controller a24 is arranged at the bottom of the denitrification tower 4, and the liquid level digital controller a24 controls the regulating valve h17 in a logic mode.
Optionally or preferably, a regulating valve i18 is arranged on a connecting line between the outlet 6-B of the denitrification tower reflux tank 6 and the inlet end of the nitrogen-rich tail gas channel I105, a pressure digital controller d27 is arranged on the denitrification tower reflux tank 6, and the pressure digital controller d27 controls the regulating valve i18 in a logic mode.
Optionally or preferably, a regulating valve j19 is arranged on a connecting pipeline between the pipeline IV 33 and the inlet end of the return refrigerant channel II 502 of the denitrification tower condenser 5, a temperature digital controller c26 is arranged on a connecting pipeline between the outlet end of the nitrogen-rich tail gas channel II 501 and the inlet 6-A of the denitrification tower reflux tank 6, and the temperature digital controller c26 controls the regulating valve j19 in a logic mode.
The utility model adds the controllers with different functions and the regulating valves which can be controlled logically in the denitrification device respectively, and further leads the device to control the corresponding valves according to the requirements of each device on data such as temperature, pressure or liquid level and the like in the denitrification treatment process, thereby more accurately regulating the denitrification process of the natural gas and improving the scientificity, convenience and operability of the whole device.
The utility model provides a use of a nitrogen-containing natural gas denitrification liquefaction device, which specifically comprises the following processing steps:
s1, a natural gas treatment process, wherein purified and pressurized purified natural gas enters a raw material natural gas channel I101 of a main heat exchanger 2 through a purified raw material gas pipeline 1 to be precooled to-60 ℃, then enters a heavy hydrocarbon separator 3 to be subjected to gas-liquid separation, bottom low-temperature liquid is heated and stored from a liquid phase outlet 3-B of the heavy hydrocarbon separator 3, top low-temperature gas leaves from a gas phase outlet 3-C of the heavy hydrocarbon separator 3 and is divided into two parts, the main part returns to a raw material natural gas channel II 102 of the main heat exchanger 2 to be continuously cooled to-162 ℃, then is regulated to 0.2MpaG through a regulating valve C12 and is sent to an inlet 4-A of a denitrification tower 4 to be rectified, the other small part is regulated to 0.2MpaG through a regulating valve a29 and is sent to an inlet 4-F of the denitrification tower 4, a tower kettle of the denitrification tower 4 is provided with a temperature digital controller B25, the temperature of the bottom of the denitrogenation tower 4 is adjusted by adjusting a valve a 29. The low-temperature gas at the top outlet 4-C of the denitrification tower 4 enters a nitrogen-rich tail gas channel II 501 of a denitrification tower condenser 5 to be cooled to-165 ℃ and then enters a denitrification tower reflux tank 6 to be subjected to gas-liquid separation, the low-temperature liquid at the bottom returns to the inlet 4-D of the denitrification tower 4 from a liquid phase outlet 6-C of the denitrification tower reflux tank 6, the low-temperature gas at the top enters a nitrogen-rich tail gas channel I105 of a main heat exchanger 2 from a gas phase outlet 6-B of the denitrification tower reflux tank 6 to be subjected to heat exchange and temperature rise to 35 ℃ and then is sent to a cold box, the product liquid at the bottom outlet 4-E of the denitrification tower 4 is sent to a liquefied natural gas channel I104 of the main heat exchanger 2 to be continuously cooled to-162 ℃ and then is decompressed to 0.05MpaG through a pressure regulating valve 17 and then is sent to an LNG storage tank. The LNG storage tank 7 is provided with a pressure digital controller e28, the pressure of the LNG storage tank 7 is maintained by the gas BOG at the top of the LNG storage tank through an adjusting valve d13, the BOG discharged from the LNG storage tank 7 is reheated to normal temperature through a BOG heater 8, then compressed to 0.9MpaG through a BOG compressor 9, cooled to 40 ℃, enters a BOG channel 103 of the main heat exchanger 2 to be cooled to-162 ℃, then adjusted to 0.2MpaG through an adjusting valve B11, and then sent to an inlet 4-B of the denitrification tower 4 for rectification and separation.
S2, a cooling liquid treatment process, wherein high-pressure liquid-phase refrigerant is sent to a high-pressure liquid-phase refrigerant channel I106 of the main heat exchanger 2 through a high-pressure refrigerant liquid-phase pipeline 23 to be cooled to-60 ℃, and then is throttled and cooled by an adjusting valve e14 and returns to a return refrigerant channel I110 to provide cooling capacity for the upper part of the main heat exchanger 2. High-pressure gas-phase refrigerant is sent to a high-pressure gas-phase refrigerant channel IA 7 of a main heat exchanger 2 through a high-pressure refrigerant gas-phase pipeline 22 to be cooled to minus 110 ℃, then enters an MR low-temperature separator 10 to be subjected to gas-liquid separation, low-temperature liquid at the bottom returns to a high-pressure liquid-phase refrigerant channel II 109 of the main heat exchanger 2 from a liquid-phase outlet 10-B of the MR low-temperature separator 10 to be cooled to minus 162 ℃, then is throttled and cooled by an adjusting valve f15 and returns to a return refrigerant channel I110 of the main heat exchanger 2, low-temperature gas at the top returns to a high-pressure gas-phase refrigerant channel II 108 of the main heat exchanger 2 from a gas-phase outlet 10-C of the MR low-temperature separator 10 to be cooled to minus 162 ℃, then is divided into two parts, one part is throttled and cooled by an adjusting valve g16 and then returns to the return refrigerant channel I110 of the main heat exchanger 2, the other part is throttled and cooled by an adjusting valve j19, then enters a return refrigerant channel II 502 of a denitrification tower condenser 5 to be cooled to cool gas-phase outlet 4-C of a denitrification tower 4, after the temperature of the nitrogen-rich gas is restored to-163 ℃, the nitrogen-rich gas returns to the return refrigerant channel I110 of the main heat exchanger 2. The returned mixed refrigerant is reheated to normal temperature in the return refrigerant channel I110 of the main heat exchanger 2 and then is discharged out of the cold box.
Experimental data
The following composition data can be obtained by the examples of the present invention:
Figure DEST_PATH_GDA0003589973370000081
according to the material balance, the nitrogen content of the LNG discharged from the main heat exchanger is 0.7228%, the nitrogen content is less than 1% according to general acceptance in the industry, and the recovery rate of methane is 99.74%.
The cold source at the top of the denitrification tower of the device comes from nitrogen and methane separated by high-pressure gas-phase refrigerant at low temperature, secondary separation is carried out, the refrigeration temperature is low, and the energy consumption is 1-2% lower than that of the conventional rectification.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.

Claims (9)

1. A liquefying plant that nitrogen natural gas denitrogenates which characterized in that: the system comprises a main heat exchanger (2), a heavy hydrocarbon separator (3), a denitrification tower (4), a denitrification tower condenser (5), a denitrification tower reflux tank (6), an LNG storage tank (7), a BOG heater (8), a BOG compressor (9) and an MR low-temperature separator (10);
a raw material natural gas channel I (101), a raw material natural gas channel II (102), a BOG channel (103), a liquefied natural gas channel I (104), a nitrogen-rich tail gas channel I (105), a high-pressure liquid phase refrigerant channel I (106), a high-pressure gas phase refrigerant channel I (A7), a high-pressure gas phase refrigerant channel II (108), a high-pressure liquid phase refrigerant channel II (109) and a return refrigerant channel I (110) are arranged in the main heat exchanger (2);
a nitrogen-rich tail gas channel II (501) and a return refrigerant channel II (502) are arranged in the denitrification tower condenser (5);
the inlet end of raw materials natural gas passageway I (101) is connected with outside purification raw materials gas pipeline (1), the exit end of raw materials natural gas passageway I (101) is connected with the entry 3-A of heavy hydrocarbon separator (3), the export 3-B of heavy hydrocarbon separator (3) heat with outside heavy hydrocarbon and go to store the pipeline and be connected, the pipeline of export 3-C of heavy hydrocarbon separator (3) divide into pipeline I (30) and pipeline II (31), pipeline I (30) be connected with the entry 4-F of denitrogenation tower (4), pipeline II (31) are connected with the inlet end of raw materials natural gas passageway I (101), the exit end of raw materials natural gas passageway I (101) is connected with the entry 4-A of denitrogenation tower (4), the exit 4-C of denitrogenation tower (4) meets with the inlet end of rich nitrogen tail gas passageway II (501), the outlet end of the nitrogen-rich tail gas channel II (501) is connected with the inlet 6-A of the denitrification tower reflux tank (6), the outlet 6-C of the denitrification tower reflux tank (6) is connected with the inlet 4-D of the denitrification tower (4), the outlet 6-B of the denitrification tower reflux tank (6) is connected with the inlet end of the nitrogen-rich tail gas channel I (105), the outlet end of the nitrogen-rich tail gas channel I (105) is connected with an external nitrogen-rich gas-removing fuel gas pipeline (20), the inlet end of the liquefied natural gas channel I (104) is connected with the outlet 4-E of the denitrification tower (4), the outlet end of the liquefied natural gas channel I (104) is connected with the inlet 7-A of the LNG storage tank (7), the outlet 7-B of the LNG storage tank (7) is connected with the inlet 8-A of the BOG heater (8), and the BOG compressor (9) is respectively connected with the outlet 8-B of the BOG heater (8) and the inlet 8-A of the BOG channel (103) The inlet end of the BOG channel (103) is connected with the inlet 4-B of the denitrification tower (4), the inlet end of the high-pressure liquid-phase refrigerant channel I (106) is connected with an external high-pressure refrigerant liquid-phase pipeline (23), the outlet end of the high-pressure liquid-phase refrigerant channel I (106) is connected with the inlet 110-A of the backflow refrigerant channel I (110), the inlet end of the high-pressure gas-phase refrigerant channel I (A7) is connected with an external high-pressure refrigerant gas-phase pipeline (22), the outlet end of the high-pressure gas-phase refrigerant channel I (A7) is connected with the inlet 10-A of the MR low-temperature separator (10), the outlet 10-B of the MR low-temperature separator (10) is connected with the inlet end of the high-pressure liquid-phase refrigerant channel II (109), the outlet end of the high-pressure liquid-phase refrigerant channel II (109) is connected with the inlet 110-B of the backflow refrigerant channel I (110), the outlet 10-C of the MR low-temperature separator (10) is connected with the inlet end of a high-pressure gas-phase refrigerant channel II (108), the outlet pipeline of the high-pressure gas-phase refrigerant channel II (108) is divided into a pipeline III (32) and a pipeline IV (33), the pipeline III (32) is connected with the inlet 110-C of a return refrigerant channel I (110), the pipeline IV (33) is connected with the inlet end of a return refrigerant channel II (502) of a denitrification tower condenser (5), the outlet end of the return refrigerant channel II (502) of the denitrification tower condenser (5) is connected with the inlet 110-C of the return refrigerant channel I (110), and the return refrigerant channel I (110) is connected with a return refrigerant pipeline (21).
2. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 1, wherein: the main heat exchanger (2) and the denitrogenation tower condenser (5) can be any one of a plate-fin heat exchanger, a wound tube heat exchanger or a shell-and-tube heat exchanger.
3. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 1, wherein: the denitrification tower (4) is a packed tower or a plate tower.
4. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 1, wherein: a connecting pipeline between the outlet end of the BOG channel (103) and the inlet 4-B of the denitrification tower (4) is provided with an adjusting valve B (11); a regulating valve c (12) is arranged on a connecting pipeline between the outlet end of the raw material natural gas channel I (101) and the inlet 4-A of the denitrification tower (4); a regulating valve e (14) is arranged on a connecting pipeline between the outlet end of the high-pressure liquid-phase refrigerant channel I (106) and the inlet 110-A of the return refrigerant channel I (110); a regulating valve f (15) is arranged on a connecting pipeline between the outlet end of the high-pressure liquid-phase refrigerant channel II (109) and the inlet 110-B of the return refrigerant channel I (110); and a regulating valve g (16) is arranged on a connecting pipeline between the pipeline III (32) and the inlet 110-C of the return refrigerant channel I (110).
5. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 4, wherein: the pipeline I (30) is provided with an adjusting valve a (29), the tower kettle of the denitrification tower (4) is provided with a temperature digital controller b (25), and the temperature digital controller b (25) controls the adjusting valve a (29) in a logic mode.
6. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 4, wherein: and a regulating valve d (13) is arranged on a connecting pipeline between an outlet 7-B of the LNG storage tank (7) and an inlet 8-A of the BOG heater (8), a pressure digital controller e (28) is arranged on the LNG storage tank (7), and the pressure digital controller e (28) controls the regulating valve d (13) in a logic mode.
7. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 4, wherein: the LNG storage tank inlet 7-A is connected with the outlet end of the liquefied natural gas channel I (104) through a pipeline, a regulating valve h (17) is arranged on the connecting pipeline between the outlet end of the liquefied natural gas channel I and the inlet 7-A of the LNG storage tank (7), a tower kettle of the denitrification tower (4) is provided with a liquid level digital controller a (24), and the liquid level digital controller a (24) controls the regulating valve h (17) in a logic mode.
8. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 4, wherein: and a regulating valve i (18) is arranged on a connecting pipeline between an outlet 6-B of the denitrification tower reflux tank (6) and an inlet end of the nitrogen-rich tail gas channel I (105), a pressure digital controller d (27) is arranged on the denitrification tower reflux tank (6), and the pressure digital controller d (27) is used for logically controlling the regulating valve i (18).
9. The nitrogen-containing natural gas denitrification liquefaction plant according to claim 4, wherein: and a connecting pipeline between the inlet end of the return refrigerant channel II (502) of the pipeline IV (33) and the denitrification tower condenser (5) is provided with a regulating valve j (19), a connecting pipeline between the outlet end of the nitrogen-rich tail gas channel II (501) and the inlet 6-A of the denitrification tower reflux tank (6) is provided with a temperature digital controller c (26), and the temperature digital controller c (26) controls the regulating valve j (19) in a logic mode.
CN202122137567.1U 2021-09-06 2021-09-06 Nitrogen-containing natural gas denitrification liquefaction device Active CN216898061U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113776278A (en) * 2021-09-06 2021-12-10 成都深冷液化设备股份有限公司 Nitrogen-containing natural gas denitrification liquefaction device and technology

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113776278A (en) * 2021-09-06 2021-12-10 成都深冷液化设备股份有限公司 Nitrogen-containing natural gas denitrification liquefaction device and technology
CN113776278B (en) * 2021-09-06 2024-05-14 四川蜀道装备科技股份有限公司 Nitrogen-containing natural gas denitrification liquefying device and process

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