CN114440552B - Method for extracting and liquefying high-purity methane by using liquefied natural gas - Google Patents
Method for extracting and liquefying high-purity methane by using liquefied natural gas Download PDFInfo
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- CN114440552B CN114440552B CN202210108138.8A CN202210108138A CN114440552B CN 114440552 B CN114440552 B CN 114440552B CN 202210108138 A CN202210108138 A CN 202210108138A CN 114440552 B CN114440552 B CN 114440552B
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- refrigerant
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 68
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000010992 reflux Methods 0.000 claims abstract description 62
- 239000007788 liquid Substances 0.000 claims abstract description 60
- 238000003860 storage Methods 0.000 claims abstract description 6
- 239000003507 refrigerant Substances 0.000 claims description 77
- 239000007789 gas Substances 0.000 claims description 34
- 238000010926 purge Methods 0.000 claims description 10
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 9
- 238000005057 refrigeration Methods 0.000 claims description 9
- 239000003345 natural gas Substances 0.000 claims description 7
- 229910052782 aluminium Inorganic materials 0.000 claims description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 238000012856 packing Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 230000001174 ascending effect Effects 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000009826 distribution Methods 0.000 abstract description 2
- 239000000284 extract Substances 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- XTFIVUDBNACUBN-UHFFFAOYSA-N 1,3,5-trinitro-1,3,5-triazinane Chemical compound [O-][N+](=O)N1CN([N+]([O-])=O)CN([N+]([O-])=O)C1 XTFIVUDBNACUBN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 238000007792 addition Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- -1 H 2 S Chemical compound 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910021417 amorphous silicon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001312 dry etching Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000001020 plasma etching Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
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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
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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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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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
- F25J3/0214—Liquefied natural gas
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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
- F25J3/0228—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
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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
- F25J3/0228—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
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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
- F25J3/0228—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
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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
- 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
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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
- 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
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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
- 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
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/60—Methane
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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
- 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
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
Abstract
The invention relates to a method for extracting and liquefying high-purity methane by utilizing liquefied natural gas, which is implemented by adopting a high-purity methane extracting and liquefying system, wherein the high-purity methane extracting and liquefying system comprises an LNG buffer tank, an LNG delivery pump, a lower rectifying tower, a condensing evaporator at the upper tower bottom of the rectifying tower, an upper rectifying tower, a condensing heat exchanger at the upper tower top of the rectifying tower, a reflux tank at the lower tower top of the rectifying tower, a reflux tank at the upper tower top of the rectifying tower and a heat exchanger. The method uses liquefied natural gas as raw material, extracts, separates and liquefies methane to obtain high-purity liquid methane, uses a low-temperature storage tank to store and uses a low-temperature tank wagon to carry out long-distance distribution, and meets the requirements of different customers.
Description
Technical Field
The invention relates to the technical field of high-purity gas preparation, in particular to a method for extracting and liquefying high-purity methane by using liquefied natural gas.
Background
The main components of the conventional liquefied natural gas are methane (CH 4), ethane (C 2H6), a small amount of propane (C 3H8), nitrogen (N 2), oxygen (O 2) and the like, wherein the volume fraction of CH 4 is 86.0% -97.5%, the volume fraction of C 4 + alkane is less than or equal to 2%, the volume fraction of CO 2 is less than or equal to 0.01%, the volume fraction of N 2 is less than or equal to 1%, the volume fraction of O 2 is less than or equal to 0.1%, and the content of H 2 S is less than or equal to 3.5mg/m 3.
The high-purity methane refers to methane with the volume fraction of CH 4 being 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 metal and alloy, microorganism culture, refrigerant and the like, but also is gradually used for auxiliary addition of gas in amorphous silicon solar cell manufacturing, large-scale integrated circuit dry etching or plasma etching.
At present, a system and a method for extracting high-purity methane from liquefied natural gas are not available, so that in order to meet the market demand for high-purity methane, it is necessary to develop a device and a method for extracting high-purity methane by using liquefied natural gas, producing high-purity liquid methane, storing the high-purity liquid methane by using a low-temperature storage tank, and remotely distributing the high-purity methane by using a low-temperature tank wagon, so as to meet different customer demands.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a method for extracting and liquefying high-purity methane by using liquefied natural gas.
The invention solves the problems by adopting the following technical scheme: the method for extracting and liquefying high-purity methane by using liquefied natural gas is implemented by adopting a high-purity methane extracting and liquefying system, wherein the high-purity methane extracting and liquefying system comprises an LNG buffer tank, an LNG delivery pump, a lower rectifying tower, a condensing evaporator at the upper bottom of the rectifying tower, an upper rectifying tower, a condensing heat exchanger at the upper top of the rectifying tower, a reflux tank at the lower top of the rectifying tower, a reflux tank at the upper top of the rectifying tower and a heat exchanger, and the heat exchanger is provided with a channel A, a channel D and a channel E; the method is characterized in that: the method for extracting and liquefying high-purity methane by using liquefied natural gas comprises the following steps:
Step one: the liquefied natural gas enters an LNG buffer tank, the liquefied natural gas in the LNG buffer tank is pressurized by an LNG delivery pump, the pressurized liquefied natural gas enters a channel A of a heat exchanger to be heated and gasified, and gasified gaseous natural gas exits from the channel A;
step two: the gaseous natural gas from the channel A enters the bottom of the lower tower of the rectifying tower, stripping and rectifying are carried out in the lower tower of the rectifying tower, alkane heavy components are separated, the separated alkane heavy components come out of the bottom of the lower tower of the rectifying tower and enter a channel E of a heat exchanger for rewarming, and the rewarming is carried out to serve as purge gas to be out of the boundary;
step three: the gas coming out of the upper part of the lower tower of the rectifying tower enters a condensing evaporator at the upper tower bottom of the rectifying tower, is cooled by the condensing evaporator at the upper tower bottom of the rectifying tower, enters a reflux tank at the lower tower top of the rectifying tower, and the liquid coming out of the bottom of the reflux tank at the lower tower top of the rectifying tower enters the lower tower top of the rectifying tower to be used as reflux liquid of the lower tower of the rectifying tower; the gas coming out from the top of the reflux tank at the top of the lower tower of the rectifying tower enters from the middle part of the upper tower of the rectifying tower after the pressure is controlled by the regulating valve, and the light components are removed by rectification in the upper tower of the rectifying tower;
Step four: the liquid from the bottom of the rectifying tower is high-purity liquid methane, and after being supercooled through a channel D of the heat exchanger, the liquid is stored as a high-purity liquid methane product to be taken as an external storage tank; the gas from the top of the rectifying tower enters a condensing heat exchanger at the top of the rectifying tower, is cooled by the condensing heat exchanger at the top of the rectifying tower and enters a reflux tank at the top of the rectifying tower, and the liquid from the bottom of the reflux tank at the top of the rectifying tower enters from the top of the rectifying tower and is used as reflux liquid at the top of the rectifying tower to participate in rectification; the gas coming out from the top of the reflux tank at the top of the rectifying tower enters a channel E entering a heat exchanger for rewarming, and the rewarmed gas is used as purge gas to go outside the boundary.
Preferably, the high purity methane extraction liquefaction system further comprises a refrigerant compressor, and the heat exchanger further comprises a channel B and a channel C; the refrigerant outlet of the refrigerant compressor is communicated with the inlet end of the channel C through a first refrigerant circulation pipeline, the outlet end of the channel C is communicated with the refrigerant inlet of the condensing evaporator at the bottom of the upper tower of the rectifying tower through a second refrigerant circulation pipeline, the refrigerant outlet of the condensing evaporator at the bottom of the upper tower of the rectifying tower is communicated with the refrigerant inlet of the condensing heat exchanger at the top of the rectifying tower through a third refrigerant circulation pipeline, the refrigerant outlet of the condensing heat exchanger at the top of the upper tower of the rectifying tower is communicated with the inlet end of the channel B through a fourth refrigerant circulation pipeline, and the outlet end of the channel B is communicated with the refrigerant inlet of the refrigerant compressor through a fifth refrigerant circulation pipeline.
Preferably, the cold energy required by the heat exchanger and the cold energy required by the condensing heat exchanger at the top of the rectifying tower is provided by closed-type refrigerant primary throttling refrigeration; the circulating refrigeration method comprises the following steps: the refrigerant is pressurized by a refrigerant compressor and then enters a channel C of a heat exchanger for precooling, precooled to a certain temperature and comes out of the channel C, the discharged refrigerant enters a condensing evaporator at the upper tower bottom of the rectifying tower and is cooled and liquefied by the condensing evaporator at the upper tower bottom of the rectifying tower, and ascending stripping is provided for the upper tower of the rectifying tower; the liquid refrigerant from the condensing evaporator at the bottom of the upper tower of the rectifying tower enters the condensing heat exchanger at the top of the upper tower of the rectifying tower after the pressure is controlled by the regulating valve, so as to provide a cold source for the condensing heat exchanger at the top of the upper tower of the rectifying tower; gaseous refrigerant from the top of the rectifying tower to condense the heat exchanger enters the channel B of the heat exchanger, provides cold energy for the heat exchanger, and the gaseous refrigerant after the heat exchanger rewarming enters the refrigerant compressor to realize the circulating compression throttling refrigeration of the refrigerant.
Preferably, the lower rectifying tower, the condensing evaporator at the upper tower bottom of the rectifying tower, the upper rectifying tower and the condensing heat exchanger at the upper tower top of the 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 delivery pump is arranged on the first pipeline, and the outlet end of the channel A is communicated with the middle air inlet of the lower tower of the rectifying tower through a second pipeline; the upper air outlet of the lower tower of the rectifying tower is communicated with the air inlet of the condensing evaporator at the bottom of the upper tower of the rectifying tower through a third pipeline; the liquid outlet of the condensing evaporator at the bottom of the upper tower of the rectifying tower is communicated with the liquid inlet of the reflux tank at the top of the lower tower of the rectifying tower through a fourth pipeline; the bottom liquid outlet of the reflux tank at the top of the lower tower of the rectifying tower is communicated with the reflux liquid inlet of the lower tower of the rectifying tower through a fifth pipeline, and the top gas outlet of the reflux tank at the top of the lower tower of the rectifying tower is communicated with the middle inlet of the upper tower of the rectifying tower through a sixth pipeline; the bottom liquid outlet of the upper tower of the rectifying tower is communicated with the inlet end of a channel D through a seventh pipeline, and the outlet end of the channel D is communicated with a high-purity liquid methane product conveying pipeline; the upper air outlet of the upper tower of the rectifying tower is communicated with the air inlet of the condensing heat exchanger at the top of the upper tower of the rectifying tower through a eighth pipeline; the liquid outlet of the condensing heat exchanger at the top of the rectifying tower is communicated with the liquid inlet of the reflux tank at the top of the rectifying tower through a pipeline with nine numbers, the liquid outlet at the bottom of the reflux tank at the top of the rectifying tower is communicated with the reflux liquid inlet of the upper tower of the rectifying tower through a pipeline with ten numbers, the gas outlet at the top of the reflux tank at the top of the rectifying tower is communicated with the inlet end of a channel E through a pipeline with eleven numbers, and the outlet end of the channel E is communicated with a purge gas output pipeline; the bottom outlet of the lower tower of the rectifying tower is communicated with the inlet end of the channel E through a twelve-number pipeline.
Preferably, the LNG transfer pump is a centrifugal pump.
Preferably, the heat exchanger is an aluminum plate-fin heat exchanger.
Preferably, the condensing evaporator at the bottom of the upper tower of the rectifying tower is an immersed plate-fin heat exchanger with two heat flows.
Preferably, the condensing heat exchanger at the top of the rectifying tower is an immersed plate-fin heat exchanger with a heat flow.
Preferably, the packing of the upper tower of the rectifying tower adopts aluminum corrugated regular packing.
Compared with the prior art, the invention has the following advantages and effects: the system uses liquefied natural gas as raw materials, extracts and separates methane, liquefies the methane to obtain high-purity liquid methane, uses a low-temperature storage tank to store the methane, and uses a low-temperature tank wagon to carry out long-distance distribution, thereby meeting the requirements of different customers.
Drawings
In order to more clearly illustrate the embodiments of the invention or the solutions in the prior art, a brief description will be given below of the drawings that are needed in the description of the embodiments or the prior art, it being obvious that the drawings in the description below are some embodiments of the invention and that other drawings can be obtained from them without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural view of an embodiment of the present invention.
Reference numerals illustrate: an LNG buffer tank 1; an LNG transfer pump 2; a rectifying tower lower tower 3; a condensing evaporator 4 is arranged at the bottom of the upper tower of the rectifying tower; a reflux tank 5 at the lower top of the rectifying tower; a rectifying tower upper tower 6; a condensing heat exchanger 7 at the top of the rectifying tower; a reflux drum 8 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; a fourth pipeline 14; a fifth pipeline 15; a sixth pipeline 16; a seventh pipeline 17; a high purity liquid methane product transfer line 18; a pipeline No. 19; a line No. 20; a tenth pipeline 21; eleven lines 22; a purge gas output line 23; a twelve-line 24; a refrigerant circulation line 25; a 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 not limited to the following examples.
Examples
See fig. 1.
The embodiment discloses a high-purity methane extraction liquefaction system, which is a system device for extracting and liquefying high-purity methane by utilizing liquefied natural gas, and comprises an LNG buffer tank 1, an LNG delivery 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 delivery 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 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 of the rectifying tower is an immersed plate-fin heat exchanger with one heat flow, and the packing of the upper tower 6of the rectifying tower adopts aluminum corrugated regular packing.
In this embodiment, the lower rectifying tower 3, the upper rectifying tower bottom condensing evaporator 4, the upper rectifying tower 6 and the upper rectifying tower top condensing heat exchanger 7 are arranged from bottom to top. The whole rectifying tower system is composed of a rectifying tower lower tower 3, a rectifying tower upper tower bottom condensing evaporator 4, a rectifying tower upper tower 6, a rectifying tower upper tower top condensing heat exchanger 7, a rectifying tower lower tower top reflux tank 5, a rectifying tower upper tower top reflux tank 8, and matched pipelines, valves and the like.
In this embodiment, the LNG buffer tank 1 is used for storing liquefied natural gas, the LNG buffer tank 1 is connected to an inlet end of the channel a through a first pipeline 11, and the LNG transfer pump 2 is installed on the first pipeline 11, and an outlet end of the channel a is connected to a middle air inlet of the lower tower 3 of the rectifying tower through a second pipeline 12. The channel A has the function of heating, and is the natural gas which is gasified by liquefied natural gas into gas.
In the embodiment, an air outlet at the upper part of a lower tower 3 of the rectifying tower is communicated with an air inlet of a condensing evaporator 4 at the bottom of the upper tower of the rectifying tower through a third pipeline 13; the liquid outlet of the condensing evaporator 4 at the upper tower bottom of the rectifying tower is communicated with the liquid inlet of the reflux tank 5 at the lower tower top of the rectifying tower through a fourth pipeline 14.
In this embodiment, the bottom liquid outlet of the reflux drum 5 at the bottom of the lower tower of the rectifying tower is connected to 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 bottom of the lower tower of the rectifying tower is connected to the middle inlet of the upper tower 6 of the rectifying tower through a sixth pipeline 16.
In this embodiment, the bottom liquid outlet of the upper tower 6 of the rectifying tower is connected to the inlet end of the channel D through a seventh pipeline 17, and the outlet end of the channel D is connected to a high-purity liquid methane product conveying pipeline 18. The upper air outlet of the upper rectifying tower 6 is communicated with the air inlet of the condensing heat exchanger 7 at the top of the upper rectifying tower through a eighth pipeline 19.
In this embodiment, the liquid outlet of the condensing heat exchanger 7 at the top of the rectifying tower is connected with the liquid inlet of the reflux drum 8 at the top of the rectifying tower through a pipeline No. 20, the liquid outlet at the bottom of the reflux drum 8 at the top of the rectifying tower is connected with the reflux inlet of the reflux drum 6 at the top of the rectifying tower through a pipeline No. 21, the gas outlet at the top of the reflux drum 8 at the top of the rectifying tower is connected with the inlet end of the channel E through a pipeline No. eleven 22, and the outlet end of the channel E is connected with the purge gas output pipeline 23; the bottom outlet of the lower tower 3 of the rectifying tower is communicated with the inlet end of the channel E through a twelve-number pipeline 24.
In this embodiment, the refrigerant outlet of the refrigerant compressor 9 is connected to the inlet end of the channel C through the first refrigerant circulation line 25, the outlet end of the channel C is connected to the refrigerant inlet of the condensing evaporator 4 at the bottom of the upper rectifying tower through the second refrigerant circulation line 26, the refrigerant outlet of the condensing evaporator 4 at the bottom of the upper rectifying tower is connected to the refrigerant inlet of the condensing heat exchanger 7 at the top of the upper rectifying tower through the third refrigerant circulation line 27, the refrigerant outlet of the condensing heat exchanger 7 at the top of the upper rectifying tower is connected to the inlet end of the channel B through the fourth refrigerant circulation line 28, and the outlet end of the channel B is connected to the refrigerant inlet of the refrigerant compressor 9 through the fifth refrigerant circulation line 29.
In this embodiment, the method for extracting and liquefying the liquefied natural gas by using the high-purity methane extraction and liquefaction system includes the following steps:
Step one: the liquefied natural gas enters an LNG buffer tank 1, the liquefied natural gas in the LNG buffer tank 1 is pressurized by an LNG delivery pump 2, the pressurized liquefied natural gas enters a channel A of a heat exchanger 10 for heating and gasification, and gasified gaseous natural gas exits from the channel A;
step two: the gaseous natural gas from the channel A enters the bottom of the lower tower 3 of the rectifying tower, stripping rectification is carried out in the lower tower 3 of the rectifying tower, carbon dioxide, H 2 S, ethane, propane, C 4 and alkane heavy components above are separated, the separated alkane heavy components enter the channel E of the heat exchanger 10 after coming out from the bottom of the lower tower 3 of the rectifying tower for rewarming, and the rewarmed alkane heavy components are used as purge gas to be outside;
Step three: the gas coming out of the upper part of the lower rectifying tower 3 enters a condensing evaporator 4 at the upper tower bottom of the rectifying tower, is cooled by the condensing evaporator 4 at the upper tower bottom of the rectifying tower, enters a reflux tank 5 at the lower tower top of the rectifying tower, and the liquid coming out of the bottom of the reflux tank 5 at the lower tower top of the rectifying tower enters the top of the lower rectifying tower 3 to be used as reflux liquid of the lower rectifying tower 3; the gas coming out from the top of the reflux tank 5 at the top of the lower tower of the rectifying tower enters from the middle part of the 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: the liquid from the bottom of the upper tower 6 of the rectifying tower is high-purity liquid methane, and after being supercooled through a channel D of the heat exchanger 10, the liquid is stored as a high-purity liquid methane product to be taken as an external storage tank; the gas from the top of the upper rectifying tower 6 enters a condensing heat exchanger 7 at the top of the upper rectifying tower, is cooled by the condensing heat exchanger 7 at the top of the upper rectifying tower and enters a reflux tank 8 at the top of the upper rectifying tower, and the liquid from the bottom of the reflux tank 8 at the top of the upper rectifying tower enters from the top of the upper rectifying tower 6 and is used as reflux liquid of the upper rectifying tower 6 to participate in rectification; the gas coming out from the top of the reflux tank 8 at the top of the rectifying tower enters a channel E entering a heat exchanger 10 for rewarming, and the rewarmed gas is used as purge gas to be outside the boundary.
In the embodiment, the cooling capacity required by the heat exchanger 10 and the cooling capacity required by the condensing heat exchanger 7 at the top of the rectifying tower are provided by closed-type refrigerant primary throttling refrigeration; the circulating refrigeration method comprises the following steps: the refrigerant is pressurized by a refrigerant compressor 9 and then enters a channel C of a heat exchanger 10 for precooling, precooled to a certain temperature and comes out of the channel C, the coming refrigerant enters a condensing evaporator 4 at the upper tower bottom of the rectifying tower and is cooled and liquefied by the condensing evaporator 4 at the upper tower bottom of the rectifying tower, and ascending stripping is provided for the upper tower 6 of the rectifying tower; the liquid refrigerant from the condensing evaporator 4 at the upper tower bottom of the rectifying tower enters the condensing heat exchanger 7 at the upper tower top of the rectifying tower after the pressure is controlled by the regulating valve, so as to provide a cold source for the condensing heat exchanger 7 at the upper tower top of the rectifying tower; the gaseous 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 cold for the heat exchanger 10, and the gaseous refrigerant after being rewarmed by the heat exchanger 10 enters a refrigerant compressor 9 to realize circulating compression throttling refrigeration of the refrigerant.
In addition, it should be noted that the specific embodiments described in the present specification may vary from part to part, from name to name, etc., and the above description in the present specification is merely illustrative of the structure of the present invention. Equivalent or simple changes of the structure, characteristics and principle of the present invention are included in the protection scope of the present invention. Those skilled in the art may make various modifications or additions to the described embodiments or substitutions in a similar manner without departing from the scope of the invention as defined in the accompanying claims.
Claims (9)
1. The method for extracting and liquefying high-purity methane by utilizing liquefied natural gas is implemented by adopting a high-purity methane extracting and liquefying system, wherein the high-purity methane extracting and liquefying system comprises an LNG buffer tank (1), an LNG delivery pump (2), a lower rectifying tower (3), an upper rectifying tower bottom condensing evaporator (4), an upper rectifying tower (6), an upper rectifying tower top condensing heat exchanger (7), a lower rectifying tower top reflux tank (5), an upper rectifying tower top reflux tank (8) and a heat exchanger (10), and the heat exchanger (10) is provided with a channel A, a channel D and a channel E; the method is characterized in that: the method for extracting and liquefying high-purity methane by using liquefied natural gas comprises the following steps:
Step one: the liquefied natural gas enters an LNG buffer tank (1), the liquefied natural gas in the LNG buffer tank (1) is pressurized by an LNG delivery 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 exits from the channel A;
Step two: gaseous natural gas from the channel A enters the bottom of a lower tower (3) of the rectifying tower, stripping and rectifying are carried out in the lower tower (3) of the rectifying tower, alkane heavy components are separated, the separated alkane heavy components enter a channel E of a heat exchanger (10) after coming out from the bottom of the lower tower (3) of the rectifying tower for rewarming, and the rewarmed alkane heavy components are used as purge gas to go outside;
Step three: the gas coming out of the upper part of the lower rectifying tower (3) enters a condensing evaporator (4) at the upper tower bottom of the rectifying tower, is cooled by the condensing evaporator (4) at the upper tower bottom of the rectifying tower and enters a reflux tank (5) at the lower tower top of the rectifying tower, and the liquid coming out of the bottom of the reflux tank (5) at the lower tower top of the rectifying tower enters the top of the lower rectifying tower (3) to be used as reflux liquid of the lower rectifying tower (3); the gas coming out from the top of the reflux tank (5) at the top of the lower tower of the rectifying tower enters from the middle part of the upper tower (6) of the rectifying tower after the pressure is controlled by a regulating valve, and the light components are removed by rectification in the upper tower (6) of the rectifying tower;
Step four: the liquid coming out from the bottom of the upper tower (6) of the rectifying tower is high-purity liquid methane, and after being supercooled through a channel D of a heat exchanger (10), the liquid is stored as a high-purity liquid methane product to be used as an external storage tank; the gas from the top of the upper rectifying tower (6) enters a condensing heat exchanger (7) at the top of the upper rectifying tower, is cooled by the condensing heat exchanger (7) at the top of the upper rectifying tower and enters a reflux tank (8) at the top of the upper rectifying tower, and the liquid from the bottom of the reflux tank (8) at the top of the upper rectifying tower enters from the top of the upper rectifying tower (6) and is taken as reflux liquid of the upper rectifying tower (6) to participate in rectification; the gas coming out from the top of the reflux tank (8) at the top of the upper column of the rectifying column enters a channel E entering a heat exchanger (10) for rewarming, and the rewarmed gas is used as purge gas to go outside the boundary.
2. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 1, wherein: the high-purity methane extraction liquefaction system further comprises a refrigerant compressor (9), and the heat exchanger (10) is further 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 circulation pipeline (25), the outlet end of the channel C is communicated with the refrigerant inlet of the condensing evaporator (4) at the bottom of the upper part of the rectifying tower through a second refrigerant circulation pipeline (26), the refrigerant outlet of the condensing evaporator (4) at the bottom of the upper part of the rectifying tower is communicated with the refrigerant inlet of the condensing heat exchanger (7) at the top of the rectifying tower through a third refrigerant circulation pipeline (27), the refrigerant outlet of the condensing heat exchanger (7) at the top of the rectifying tower is communicated with the inlet end of the channel B through a fourth refrigerant circulation 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 circulation pipeline (29).
3. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 2, wherein: the cold energy required by the heat exchanger (10) and the cold energy required by the condensing heat exchanger (7) at the top of the rectifying tower is provided by closed-type refrigerant primary throttling refrigeration;
The circulating refrigeration method comprises the following steps: the refrigerant is pressurized by a refrigerant compressor (9) and then enters a channel C of a heat exchanger (10) for precooling, the precooled refrigerant comes out of the channel C to a certain temperature, the discharged refrigerant enters a condensing evaporator (4) at the upper bottom of the rectifying tower, and is cooled and liquefied by the condensing evaporator (4) at the upper bottom of the rectifying tower to provide ascending stripping for the upper tower (6) of the rectifying tower; the liquid refrigerant from the condensing evaporator (4) at the upper tower bottom of the rectifying tower enters the condensing heat exchanger (7) at the upper tower top of the rectifying tower after the pressure is controlled by the regulating valve, so as to provide a cold source for the condensing heat exchanger (7) at the upper tower top of the rectifying tower; the gaseous 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), cold energy is provided for the heat exchanger (10), and the gaseous refrigerant after the rewarming of the heat exchanger (10) enters a refrigerant compressor (9) to realize the circulating compression throttling refrigeration of the refrigerant.
4. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 1, wherein: the lower rectifying tower (3), the upper rectifying tower bottom condensing evaporator (4), the upper rectifying tower (6) and the upper rectifying tower top condensing heat exchanger (7) 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 delivery pump (2) is arranged on the first pipeline (11), and the outlet end of the channel A is communicated with the middle air inlet of the lower tower (3) of the rectifying tower through a second pipeline (12);
An air outlet at the upper part of the lower tower (3) of the rectifying tower is communicated with an air inlet of a condensing evaporator (4) at the bottom of the upper tower of the rectifying tower through a third pipeline (13); the liquid outlet of the condensing evaporator (4) at the bottom of the upper tower of the rectifying tower is communicated with the liquid inlet of the reflux tank (5) at the top of the lower tower of the rectifying tower through a fourth pipeline (14);
The bottom liquid outlet of the reflux tank (5) at the lower top of the rectifying tower is communicated with the reflux liquid inlet of the lower rectifying tower (3) through a fifth pipeline (15), and the top air outlet of the reflux tank (5) at the lower top of the rectifying tower is communicated with the middle inlet of the upper rectifying tower (6) through a sixth pipeline (16);
The bottom liquid outlet of the upper tower (6) of the rectifying tower is communicated with the inlet end of a channel D through a seventh 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 upper part of the top of the rectifying tower through a eighth pipeline (19);
The liquid outlet of the condensing heat exchanger (7) at the top of the rectifying tower is communicated with the liquid inlet of the reflux tank (8) at the top of the rectifying tower through a pipeline (20) with No. nine, the liquid outlet at the bottom of the reflux tank (8) at the top of the rectifying tower is communicated with the reflux liquid inlet of the reflux tank (6) at the top of the rectifying tower through a pipeline (21) with No. ten, the gas outlet at the top of the reflux tank (8) at the top of the rectifying tower is communicated with the inlet end of the channel E through a pipeline (22) with No. eleven, and the outlet end of the channel E is communicated with the 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 twelve-line pipeline (24).
5. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 1, wherein: the LNG transfer pump (2) adopts a centrifugal pump.
6. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 1, wherein: the heat exchanger (10) is an aluminum plate-fin heat exchanger.
7. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 1, wherein: the condensing evaporator (4) at the bottom of the rectifying tower is an immersed plate-fin heat exchanger with two heat flows.
8. The method for extracting and liquefying high-purity methane by using 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 heat flow.
9. The method for extracting and liquefying high-purity methane by using liquefied natural gas according to claim 1, wherein: the packing of the upper tower (6) of the rectifying tower adopts aluminum corrugated regular packing.
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| DE19906602A1 (en) * | 1999-02-17 | 2000-08-24 | Linde Ag | Production of pure methane comprises rectifying liquefied methane from a natural gas storage tank |
| RU2296922C1 (en) * | 2006-03-31 | 2007-04-10 | ООО Производственный кооператив Научно-производственная фирма "ЭКИП" | Method for producing pure methane |
| CN203949442U (en) * | 2014-07-09 | 2014-11-19 | 吴启 | Methane gas recovery device of liquefied |
| CN106979666A (en) * | 2017-04-19 | 2017-07-25 | 苏州市兴鲁空分设备科技发展有限公司 | Methane purifying plant |
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| DE19906602A1 (en) * | 1999-02-17 | 2000-08-24 | Linde Ag | Production of pure methane comprises rectifying liquefied methane from a natural gas storage tank |
| RU2296922C1 (en) * | 2006-03-31 | 2007-04-10 | ООО Производственный кооператив Научно-производственная фирма "ЭКИП" | Method for producing pure methane |
| CN203949442U (en) * | 2014-07-09 | 2014-11-19 | 吴启 | Methane gas recovery device of liquefied |
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