CN216845327U - System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction - Google Patents

System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction Download PDF

Info

Publication number
CN216845327U
CN216845327U CN202220241779.6U CN202220241779U CN216845327U CN 216845327 U CN216845327 U CN 216845327U CN 202220241779 U CN202220241779 U CN 202220241779U CN 216845327 U CN216845327 U CN 216845327U
Authority
CN
China
Prior art keywords
rectifying tower
tower
pipeline
communicated
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202220241779.6U
Other languages
Chinese (zh)
Inventor
范庆虎
范金龙
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lianyungang Liquid Air Cryogenic Engineering Co ltd
Original Assignee
Lianyungang Liquid Air Cryogenic Engineering Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lianyungang Liquid Air Cryogenic Engineering Co ltd filed Critical Lianyungang Liquid Air Cryogenic Engineering Co ltd
Priority to CN202220241779.6U priority Critical patent/CN216845327U/en
Application granted granted Critical
Publication of CN216845327U publication Critical patent/CN216845327U/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • 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
    • F25J3/0214—Liquefied 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
    • F25J3/0238—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 2 carbon atoms 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double 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
    • F25J2200/74—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
    • 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
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids

Landscapes

  • 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)
  • Separation By Low-Temperature Treatments (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The utility model relates to a system for extracting and liquefying high-purity methane by utilizing liquefied natural gas, which comprises an LNG buffer tank, an LNG transfer pump, a lower rectifying tower, an upper rectifying tower bottom condensation evaporator, an upper rectifying tower top condensation heat exchanger, a lower rectifying tower top reflux tank, an upper rectifying tower top reflux tank and a heat exchanger; the system utilizes liquefied natural gas as a raw material, extracts, separates and liquefies methane to obtain high-purity liquid methane, adopts the low-temperature storage tank to store methane and adopts the low-temperature tank car to remotely deliver methane, and meets the requirements of different customers.

Description

System for extracting and liquefying high-purity methane by utilizing liquefied natural gas
Technical Field
The utility model relates to a technical field is prepared to high-purity gas, specifically say, relate to a system that utilizes liquefied natural gas to carry out high-purity methane and draw liquefaction.
Background
The main component of the conventional type of liquefied natural gas is methane (CH)4) Ethane (C)2H6) And alsoWith a small amount of propane (C)3H8) Nitrogen (N)2) Oxygen (O)2) Etc. of which CH4The volume fraction of C is 86.0% -97.5%4 +Alkane volume fraction is less than or equal to 2 percent, CO2Volume fraction is less than or equal to 0.01 percent, N2Volume fraction of less than or equal to 1 percent and O2Volume fraction is less than or equal to 0.1 percent, H2The S content is less than or equal to 3.5mg/m3。
High purity methane is CH4Methane with volume fraction more than or equal to 99.999 percent. The high-purity methane is not only used in the fields of preparation of standard mixed gas, catalyst evaluation, carburization and carbide generation of metals and alloys, microbial culture, refrigerants and the like, but also is gradually used for the manufacture of amorphous silicon solar cells, dry etching of large-scale integrated circuits or auxiliary gas addition of plasma etching gas.
At present, a system for extracting high-purity methane from liquefied natural gas does not exist, in order to meet the demand of the market on the high-purity methane, a device for extracting and liquefying the high-purity methane by utilizing the liquefied natural gas is necessary to be developed, the high-purity liquid methane is produced, a low-temperature storage tank is adopted for storage, and a low-temperature tank car is adopted for remote distribution, so that the demands of different customers are met.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the above-mentioned not enough that exists among the prior art, and provide a system that utilizes liquefied natural gas to carry out high-purity methane and draw liquefaction.
The utility model provides a technical scheme that above-mentioned problem adopted is: a system for extracting and liquefying high-purity methane by using liquefied natural gas is characterized in that: the device comprises an LNG buffer tank, an LNG transfer pump, a lower rectifying tower, an upper rectifying tower bottom condensation evaporator, an upper rectifying tower top condensation heat exchanger, a lower rectifying tower top reflux tank, an upper rectifying tower top reflux tank and a heat exchanger; the heat exchanger is provided with a channel A, a channel D and a channel E; the lower rectifying tower, the condensation evaporator at the bottom of the upper rectifying tower, the upper rectifying tower and the condensation heat exchanger at the top of the upper rectifying tower are arranged from bottom to top; the LNG buffer tank is used for storing liquefied natural gas, the LNG buffer tank is communicated with the inlet end of the channel A through a first pipeline, the LNG transfer pump is installed on the first pipeline, and the outlet end of the channel A is communicated with the middle gas inlet of the lower tower of the rectifying tower through a second pipeline; an air outlet at the upper part of the lower rectifying tower is communicated with an air inlet of a condensation evaporator at the bottom of the upper rectifying tower through a third pipeline; a liquid outlet of the condensation evaporator at the bottom of the upper tower of the rectifying tower is communicated with a liquid inlet of a reflux tank at the top of the lower tower of the rectifying tower through a fourth pipeline; a bottom liquid outlet of the reflux tank at the top of the lower rectifying tower is communicated with a reflux liquid inlet of the lower rectifying tower through a fifth pipeline, and a top gas outlet of the reflux tank at the top of the lower rectifying tower is communicated with a middle inlet of the upper rectifying tower through a sixth pipeline; a liquid outlet at the bottom of the upper tower of the rectifying tower is communicated with the inlet end of the channel D through a No. seven pipeline, and the outlet end of the channel D is communicated with a high-purity liquid methane product conveying pipeline; an air outlet at the upper part of the upper tower of the rectifying tower is communicated with an air inlet of a condensing heat exchanger at the top of the upper tower of the rectifying tower through an eighth pipeline; a liquid outlet of the condensation heat exchanger at the top of the upper tower of the rectifying tower is communicated with a liquid inlet of a reflux tank at the top of the upper tower of the rectifying tower through a ninth pipeline, a liquid outlet at the bottom of the reflux tank at the top of the upper tower of the rectifying tower is communicated with a reflux inlet of the upper tower of the rectifying tower through a tenth pipeline, a top gas outlet of the reflux tank at the top of the upper tower of the rectifying tower is communicated with an inlet end of a channel E through an eleventh pipeline, and an outlet end of the channel E is communicated with a purge gas output pipeline; and the bottom outlet of the lower tower of the rectifying tower is communicated with the inlet end of the channel E through a No. twelve pipeline.
Preferably, the system further comprises a refrigerant compressor, the heat exchanger is further provided with a channel B and a channel C, a refrigerant outlet of the refrigerant compressor is communicated with an inlet end of the channel C through a first refrigerant circulation pipeline, an outlet end of the channel C is communicated with a refrigerant inlet of a condensation evaporator at the bottom of the rectifying tower through a second refrigerant circulation pipeline, a refrigerant outlet of a condensation evaporator at the bottom of the rectifying tower is communicated with a refrigerant inlet of a condensation heat exchanger at the top of the rectifying tower through a third refrigerant circulation pipeline, a refrigerant outlet of a condensation heat exchanger at the top of the rectifying tower is communicated with an inlet end of the channel B through a fourth refrigerant circulation pipeline, and an outlet end of the channel B is communicated with a refrigerant inlet of the refrigerant compressor through a fifth refrigerant circulation pipeline.
Preferably, the LNG transfer pump is a centrifugal pump.
Preferably, the heat exchanger is an aluminum plate-fin heat exchanger.
Preferably, the condensation evaporator at the bottom of the upper tower part of the rectifying tower is a submerged plate-fin heat exchanger with two heat flows.
Preferably, the top condensing heat exchanger of the rectifying tower is a submerged plate-fin heat exchanger with a hot flow.
Preferably, the packing of the upper tower of the rectifying tower adopts aluminum corrugated regular packing.
Compared with the prior art, the utility model, have following advantage and effect: the system utilizes liquefied natural gas as a raw material, extracts, separates and liquefies methane to obtain high-purity liquid methane, adopts the low-temperature storage tank to store methane and adopts the low-temperature tank car to remotely deliver methane, and meets the requirements of different customers.
Drawings
In order to illustrate the embodiments of the present invention or the solutions in the prior art more clearly, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Description of reference numerals: an LNG buffer tank 1; an LNG transfer pump 2; a lower rectifying tower 3; the evaporator 4 is condensed at the bottom of the upper tower of the rectifying tower; a reflux tank 5 is arranged at the top of the lower tower of the rectifying tower; the rectifying tower is arranged on the tower 6; a condensing heat exchanger 7 is arranged at the top of the upper tower of the rectifying tower; a reflux tank 8 is arranged at the top of the rectifying tower; a refrigerant compressor 9; a heat exchanger 10; a first pipeline 11; a second pipeline 12; a third pipeline 13; line number four 14; a fifth pipeline 15; line number six 16; line number seven 17; a high purity liquid methane product delivery line 18; line eight 19; line No. nine, 20; a tenth pipe 21; line number eleven 22; a purge gas output line 23; a twelfth pipeline 24; a first refrigerant circulation line 25; a second refrigerant circulation line 26; a third refrigerant circulation line 27; a fourth refrigerant circulation line 28; and a fifth refrigerant circulation line 29.
Detailed Description
The present invention will be described in further detail by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and are not intended to limit the present invention.
Examples are given.
See fig. 1.
The embodiment of the invention discloses a system for extracting and liquefying high-purity methane by utilizing liquefied natural gas, which comprises an LNG buffer tank 1, an LNG transfer pump 2, a lower rectifying tower 3, an upper rectifying tower bottom condensation evaporator 4, an upper rectifying tower 6, an upper rectifying tower top condensation heat exchanger 7, a lower rectifying tower top reflux tank 5, an upper rectifying tower top reflux tank 8, a refrigerant compressor 9 and a heat exchanger 10. The heat exchanger 10 is provided with a channel A, a channel B, a channel C, a channel D and a channel E, the LNG conveying pump 2 adopts a centrifugal pump, the heat exchanger 10 adopts an aluminum plate-fin heat exchanger, the condensing evaporator 4 at the bottom of the upper tower part of the rectifying tower is an immersed plate-fin heat exchanger with two heat flows, the condensing heat exchanger 7 at the top of the upper tower part of the rectifying tower is an immersed plate-fin heat exchanger with one heat flow, and the filler of the upper tower 6 of the rectifying tower adopts aluminum corrugated regular filler.
In this embodiment, the lower rectifying tower 3, the upper rectifying tower bottom condensation evaporator 4, the upper rectifying tower 6 and the upper rectifying tower top condensation heat exchanger 7 are arranged from bottom to top. The whole rectifying tower system is composed of a lower rectifying tower 3, an upper rectifying tower bottom condensation evaporator 4, an upper rectifying tower 6, an upper rectifying tower top condensation heat exchanger 7, a lower rectifying tower top reflux tank 5, an upper rectifying tower top reflux tank 8, and pipelines and valves matched with the reflux tanks.
In this embodiment, LNG buffer tank 1 is used for storing liquefied natural gas, and LNG buffer tank 1 and passageway a's entrance point are through No. 11 switch-ons of a pipeline to LNG transfer pump 2 installs on No. 11 pipelines, and passageway a's exit end and rectifying column lower tower 3's middle part air inlet are through No. 12 switch-ons of No. two pipelines. The channel A has the function of warming, and the liquefied natural gas is gasified into gaseous natural gas.
In the embodiment, an air outlet at the upper part of the lower rectifying tower 3 is communicated with an air inlet of the condensation evaporator 4 at the bottom of the upper rectifying tower through a third pipeline 13; the liquid outlet of the upper tower bottom condensation evaporator 4 of the rectifying tower is communicated with the liquid inlet of the lower tower top reflux tank 5 of the rectifying tower through a fourth pipeline 14.
In this embodiment, the bottom liquid outlet of the reflux drum 5 at the top of the lower tower of the rectifying tower is communicated with the reflux inlet of the lower tower 3 of the rectifying tower through a fifth pipeline 15, and the top gas outlet of the reflux drum 5 at the top of the lower tower of the rectifying tower is communicated with the middle inlet of the upper tower 6 of the rectifying tower through a sixth pipeline 16.
In this embodiment, a liquid outlet at the bottom of the upper column 6 of the rectifying column is communicated with an inlet end of the channel D through a seventh pipeline 17, and an outlet end of the channel D is communicated with a high-purity liquid methane product conveying pipeline 18. An air outlet at the upper part of the upper tower 6 of the rectifying tower is communicated with an air inlet of a condensation heat exchanger 7 at the top of the upper tower of the rectifying tower through an eighth pipeline 19.
In this embodiment, a liquid outlet of the condensing heat exchanger 7 at the top of the upper column of the rectifying column is communicated with a liquid inlet of the reflux tank 8 at the top of the upper column of the rectifying column through a ninth pipeline 20, a liquid outlet at the bottom of the reflux tank 8 at the top of the upper column of the rectifying column is communicated with a reflux inlet of the upper column 6 of the rectifying column through a tenth pipeline 21, a top gas outlet of the reflux tank 8 at the top of the upper column of the rectifying column is communicated with an inlet end of the channel E through an eleventh pipeline 22, and an outlet end of the channel E is communicated with a purge gas output pipeline 23; the bottom outlet of the lower rectifying tower 3 is communicated with the inlet end of the channel E through a No. twelve pipeline 24.
In this embodiment, the refrigerant outlet of the refrigerant compressor 9 is connected to the inlet end of the channel C through a first refrigerant circulation pipeline 25, the outlet end of the channel C is connected to the refrigerant inlet of the upper tower bottom condensation evaporator 4 of the rectifying tower through a second refrigerant circulation pipeline 26, the refrigerant outlet of the upper tower bottom condensation evaporator 4 of the rectifying tower is connected to the refrigerant inlet of the upper tower top condensation heat exchanger 7 of the rectifying tower through a third refrigerant circulation pipeline 27, the refrigerant outlet of the upper tower top condensation heat exchanger 7 of the rectifying tower is connected to the inlet end of the channel B through a fourth refrigerant circulation pipeline 28, and the outlet end of the channel B is connected to the refrigerant inlet of the refrigerant compressor 9 through a fifth refrigerant circulation pipeline 29.
In this embodiment, the method for extracting and liquefying high-purity methane from liquefied natural gas by using the high-purity methane extraction and liquefaction system includes the steps of:
the method comprises the following steps: liquefied natural gas enters an LNG buffer tank 1, the liquefied natural gas in the LNG buffer tank 1 is pressurized through an LNG transfer pump 2, the pressurized liquefied natural gas enters a channel A of a heat exchanger 10 to be heated and gasified, and gasified gaseous natural gas comes out from the channel A;
step two: the gaseous natural gas from the channel A enters the bottom of a lower tower 3 of the rectifying tower, and is subjected to steam stripping rectification in the lower tower 3 of the rectifying tower to separate carbon dioxide and H2S, ethane, propane, C4And the alkane heavy components are separated, the separated alkane heavy components come out from the bottom of a lower tower 3 of the rectifying tower and enter a channel E of a heat exchanger 10 for rewarming, and the rewarming gas is used as purge gas to be discharged outside;
step three: gas coming out of the upper part of the lower rectifying tower 3 enters an upper rectifying tower bottom condensation evaporator 4, is cooled by the upper rectifying tower bottom condensation evaporator 4 and then enters a lower rectifying tower top reflux tank 5, and liquid coming out of the bottom of the lower rectifying tower top reflux tank 5 enters the top of the lower rectifying tower 3 and serves as reflux liquid of the lower rectifying tower 3; gas coming out of the top of a reflux tank 5 at the top of a lower tower of the rectifying tower enters from the middle of an upper tower 6 of the rectifying tower after the pressure is controlled by a regulating valve, and light components such as nitrogen, oxygen, hydrogen and the like are removed by rectification in the upper tower 6 of the rectifying tower;
step four: liquid discharged from the bottom of the upper tower 6 of the rectifying tower is high-purity liquid methane, and is subcooled by a channel D of the heat exchanger 10 and then is stored in an external storage tank as a high-purity liquid methane product; gas coming out of the top of the upper tower 6 of the rectifying tower enters a condensing heat exchanger 7 at the top of the upper tower of the rectifying tower, is cooled by the condensing heat exchanger 7 at the top of the upper tower of the rectifying tower and then enters a reflux tank 8 at the top of the upper tower of the rectifying tower, and liquid coming out of the bottom of the reflux tank 8 at the top of the upper tower of the rectifying tower enters from the top of the upper tower 6 of the rectifying tower and participates in rectification as reflux liquid of the upper tower 6 of the rectifying tower; and the gas coming out from the top of the reflux tank 8 at the top of the upper tower of the rectifying tower enters a channel E of the heat exchanger 10 for reheating, and is used as purge gas to be discharged outside after reheating.
In the embodiment, the cold quantity required by the heat exchanger 10 and the cold quantity required by the condensing heat exchanger 7 on the top of the upper tower of the rectifying tower are provided by closed-type cryogen first-stage throttling refrigeration; the circulating refrigeration method comprises the following steps: a refrigerant is pressurized by a refrigerant compressor 9 and then enters a channel C of a heat exchanger 10 for precooling, the refrigerant is precooled to a certain temperature and then comes out of the channel C, the coming out refrigerant enters a condensing evaporator 4 at the bottom of the upper tower of the rectifying tower, and is cooled and liquefied by the condensing evaporator 4 at the bottom of the upper tower of the rectifying tower, so that ascending steam stripping is provided for an upper tower 6 of the rectifying tower; liquid refrigerant coming out of the condensation evaporator 4 at the bottom of the upper tower of the rectifying tower enters the condensation heat exchanger 7 at the top of the upper tower of the rectifying tower after the pressure is controlled by a regulating valve, so that a cold source is provided for the condensation heat exchanger 7 at the top of the upper tower of the rectifying tower; gas refrigerant coming out of the condensing heat exchanger 7 at the top of the rectifying tower enters a channel B of the heat exchanger 10 to provide cooling capacity for the heat exchanger 10, and the gas refrigerant after being reheated by the heat exchanger 10 enters a refrigerant compressor 9 to realize the circulating compression throttling refrigeration of the refrigerant.
In addition, it should be noted that the specific embodiments described in the present specification may be different in the components, the shapes of the components, the names of the components, and the like, and the above description is only an example of the structure of the present invention. All the equivalent changes or simple changes made according to the structure, characteristics and principle of the utility model are included in the protection scope of the utility model. Those skilled in the art can modify or supplement the described embodiments or substitute them in a similar manner without departing from the scope of the invention as defined by the claims.

Claims (7)

1. A system for extracting and liquefying high-purity methane by using liquefied natural gas is characterized in that: the device comprises an LNG buffer tank (1), an LNG transfer pump (2), a lower rectifying tower (3), an upper rectifying tower bottom condensation evaporator (4), an upper rectifying tower (6), an upper rectifying tower top condensation heat exchanger (7), a lower rectifying tower top reflux tank (5), an upper rectifying tower top reflux tank (8) and a heat exchanger (10);
the heat exchanger (10) has a channel A, a channel D and a channel E;
the lower rectifying tower (3), the condensing evaporator (4) at the bottom of the upper rectifying tower, the upper rectifying tower (6) and the condensing heat exchanger (7) at the top of the upper rectifying tower are arranged from bottom to top;
the LNG buffer tank (1) is used for storing liquefied natural gas, the LNG buffer tank (1) is communicated with the inlet end of the channel A through a first pipeline (11), the LNG transfer pump (2) is installed on the first pipeline (11), and the outlet end of the channel A is communicated with the middle air inlet of the lower rectifying tower (3) through a second pipeline (12);
an air outlet at the upper part of the lower rectifying tower (3) is communicated with an air inlet of a condensation evaporator (4) at the bottom of the upper rectifying tower through a third pipeline (13); a liquid outlet of the condensation evaporator (4) at the bottom of the upper tower of the rectifying tower is communicated with a liquid inlet of the reflux tank (5) at the top of the lower tower of the rectifying tower through a fourth pipeline (14);
a liquid outlet at the bottom of the reflux tank (5) at the top of the lower rectifying tower is communicated with a reflux inlet of the lower rectifying tower (3) through a fifth pipeline (15), and a gas outlet at the top of the reflux tank (5) at the top of the lower rectifying tower is communicated with a middle inlet of the upper rectifying tower (6) through a sixth pipeline (16);
a liquid outlet at the bottom of the upper tower (6) of the rectifying tower is communicated with the inlet end of the channel D through a No. seven pipeline (17), and the outlet end of the channel D is communicated with a high-purity liquid methane product conveying pipeline (18); an air outlet at the upper part of the upper tower (6) of the rectifying tower is communicated with an air inlet of a condensing heat exchanger (7) at the top of the upper tower of the rectifying tower through an eighth pipeline (19);
a liquid outlet of the condensing heat exchanger (7) at the top of the upper tower of the rectifying tower is communicated with a liquid inlet of a reflux tank (8) at the top of the upper tower of the rectifying tower through a ninth pipeline (20), a liquid outlet at the bottom of the reflux tank (8) at the top of the upper tower of the rectifying tower is communicated with a reflux inlet of an upper tower (6) of the rectifying tower through a tenth pipeline (21), a top gas outlet of the reflux tank (8) at the top of the upper tower of the rectifying tower is communicated with an inlet end of a channel E through an eleventh pipeline (22), and an outlet end of the channel E is communicated with a purge gas output pipeline (23); and the bottom outlet of the lower rectifying tower (3) is communicated with the inlet end of the channel E through a No. twelve pipeline (24).
2. The system for high-purity methane extraction liquefaction by liquefied natural gas according to claim 1, wherein: the system also comprises a refrigerant compressor (9), the heat exchanger (10) is also provided with a channel B and a channel C,
the refrigerant outlet of the refrigerant compressor (9) is communicated with the inlet end of the channel C through a first refrigerant circulating pipeline (25), the outlet end of the channel C is communicated with the refrigerant inlet of the condensation evaporator (4) at the bottom of the rectifying tower upper tower through a second refrigerant circulating pipeline (26), the refrigerant outlet of the condensation evaporator (4) at the bottom of the rectifying tower upper tower is communicated with the refrigerant inlet of the condensation heat exchanger (7) at the top of the rectifying tower upper tower through a third refrigerant circulating pipeline (27), the refrigerant outlet of the condensation heat exchanger (7) at the top of the rectifying tower upper tower is communicated with the inlet end of the channel B through a fourth refrigerant circulating pipeline (28), and the outlet end of the channel B is communicated with the refrigerant inlet of the refrigerant compressor (9) through a fifth refrigerant circulating pipeline (29).
3. The system for high-purity methane extraction liquefaction by liquefied natural gas according to claim 1, wherein: the LNG transfer pump (2) adopts a centrifugal pump.
4. The system for extracting and liquefying high-purity methane by using liquefied natural gas as claimed in claim 1, wherein: the heat exchanger (10) adopts an aluminum plate-fin heat exchanger.
5. The system for extracting and liquefying high-purity methane by using liquefied natural gas as claimed in claim 1, wherein: the condensing evaporator (4) at the bottom of the upper tower part of the rectifying tower is an immersed plate-fin heat exchanger with two heat flows.
6. The system for high-purity methane extraction liquefaction by liquefied natural gas according to claim 1, wherein: the condensing heat exchanger (7) at the top of the rectifying tower is an immersed plate-fin heat exchanger with a strand of heat flow.
7. The system for high-purity methane extraction liquefaction by liquefied natural gas according to claim 1, wherein: the packing of the upper tower (6) of the rectifying tower adopts aluminum corrugated regular packing.
CN202220241779.6U 2022-01-28 2022-01-28 System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction Active CN216845327U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202220241779.6U CN216845327U (en) 2022-01-28 2022-01-28 System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202220241779.6U CN216845327U (en) 2022-01-28 2022-01-28 System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction

Publications (1)

Publication Number Publication Date
CN216845327U true CN216845327U (en) 2022-06-28

Family

ID=82089456

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202220241779.6U Active CN216845327U (en) 2022-01-28 2022-01-28 System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction

Country Status (1)

Country Link
CN (1) CN216845327U (en)

Similar Documents

Publication Publication Date Title
CN107014151B (en) Device and method for liquefying hydrogen
CN113776275B (en) Hydrogen liquefaction method under LNG cold energy precooling
CN112361712A (en) Hydrogen liquefaction equipment adopting helium refrigeration cycle system
CN103542692B (en) Based on the Unconventional forage liquefaction system of wrap-round tubular heat exchanger
CN114440552B (en) Method for extracting and liquefying high-purity methane by using liquefied natural gas
CN202813975U (en) Unconventional natural gas liquefaction system based on winding tubular heat exchanger
US11674749B2 (en) LNG production with nitrogen removal
CN113959176B (en) System and method for separating helium from liquefied natural gas flash gas
CN214095167U (en) Hydrogen liquefaction equipment adopting helium refrigeration cycle system
CN102628634B (en) Ternary-cycle cascade refrigeration natural gas liquefaction system and method thereof
CN216845327U (en) System for utilize liquefied natural gas to carry out high-purity methane and draw liquefaction
CN205090721U (en) Four component cryogens high pressure throttle refrigerating fluid ization natural gas system
CN208520082U (en) A kind of air liquefaction plant
US8991208B2 (en) Liquefaction process producing subcooled LNG
US20060021378A1 (en) Method of liquefying a hydrocarbon-rich flow
CN101625191B (en) Low-temperature gas liquefaction and separation system applying effect of segregation
CN205593289U (en) Liquefied natural gas's device
CN114777412A (en) Hydrogen liquefying plant with thermal siphon type hydrogen subcooler
CN211977383U (en) Helium liquefying and helium cold source supply device with different temperature grades
CN205718201U (en) The natural gas liquefaction system of mix refrigerant pre-cooling nitrogen expansion
CN219347032U (en) High-purity methane production device
US20090031755A1 (en) Natural gas liquefaction process to extend lifetime of gas wells
CN219531259U (en) Liquefying device with liquefied natural gas as cold source
WO2023226639A1 (en) Modular hydrogen liquefaction system
CN202501709U (en) Large-scale natural gas liquefaction device

Legal Events

Date Code Title Description
GR01 Patent grant
GR01 Patent grant