CN111928574A - Helium gas recovery system and method - Google Patents
Helium gas recovery system and method Download PDFInfo
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- CN111928574A CN111928574A CN202010733243.1A CN202010733243A CN111928574A CN 111928574 A CN111928574 A CN 111928574A CN 202010733243 A CN202010733243 A CN 202010733243A CN 111928574 A CN111928574 A CN 111928574A
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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
- F25J3/02—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
- F25J3/0257—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
- 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
- F25J3/028—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 noble gases
- F25J3/029—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 noble gases of helium
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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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
- F25J2200/02—Processes or apparatus using separation by rectification in a single 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/60—Natural gas or synthetic natural gas [SNG]
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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
- F25J2215/30—Helium
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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
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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- Chemical & Material Sciences (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention provides a helium recovery system and a method, which comprises a main heat exchanger, a refrigeration cycle mechanism, a rectifying tower and a gas-liquid separation device, wherein the refrigeration cycle mechanism, the rectifying tower and the gas-liquid separation device are communicated with an internal flow passage of the main heat exchanger; outlets are arranged at the top and the bottom of the rectifying tower, the outlet end at the bottom is communicated with the inlet end of the natural gas third cooling flow channel, and the gas outlet at the top is communicated with the inlet end of the natural gas fourth cooling flow channel; outlets are arranged at the top and the bottom of the gas-liquid separation device, and a top gas outlet is communicated with an inlet end of the helium reheating flow channel. The helium gas recovery system and the method can safely and efficiently recover and extract helium gas from helium-containing natural gas, reduce the cost, save the energy consumption, simplify the process flow of helium gas recovery and extraction and improve the economic value of helium gas recovery.
Description
Technical Field
The invention relates to the technical field of gas separation, in particular to a helium gas recovery system and a helium gas recovery method.
Background
Helium is a non-renewable resource, has a very small content in nature, and has wide application in the industries of semiconductor production, aerospace, photoelectron and the like due to the unique physical properties of helium. However, the content of helium in air is very small, the value of helium extraction is not high, helium is mainly contained in natural gas, and the content of helium in natural gas is up to 8% in some places, so that helium extraction from natural gas is a main industrial source.
At present, four methods are mainly used for extracting helium from helium-containing natural gas, namely a cryogenic separation method, a membrane separation method, a pressure swing adsorption method and a hydrate method, but the existing helium extraction process method has the problems of complex flow, high energy consumption, low economy, low utilization rate of raw material gas and the like.
Disclosure of Invention
The invention aims to provide helium recovery equipment with good stability and strong applicability, which simplifies the process flow of helium recovery and improves the economic value of helium recovery.
In order to achieve the purpose, the invention adopts the following technical scheme:
a helium recovery system comprising:
the natural gas heat recovery device comprises a main heat exchanger, wherein a natural gas first cooling flow channel, a natural gas second cooling flow channel, a natural gas third cooling flow channel, a natural gas fourth cooling flow channel and a helium reheating flow channel are arranged in the main heat exchanger, and the main heat exchanger is connected with a refrigeration circulation mechanism;
the top and the bottom of the rectifying tower are provided with outlets, the bottom outlet is communicated with the inlet end of the natural gas third cooling flow channel, and a top gas outlet is communicated with the inlet end of the natural gas fourth cooling flow channel; and
and the top gas outlet is communicated with the inlet end of the helium reheating flow channel.
Further, the refrigeration cycle mechanism includes:
the first refrigerant cooling flow channel, the second refrigerant cooling flow channel, the first refrigerant reheating flow channel, the second refrigerant reheating flow channel and the third refrigerant reheating flow channel are arranged in the main heat exchanger;
the nitrogen compression device is communicated with the inlet end of the first refrigerant cooling flow channel and the outlet end of the third refrigerant reheating flow channel;
the first-stage expansion device is communicated with the outlet end of the first refrigerant cooling flow channel and the inlet end of the third refrigerant reheating flow channel; and
and the second-stage expansion device is communicated with the outlet end of the refrigerant second cooling flow channel and the inlet end of the refrigerant third reheating flow channel.
Further, a cooling device is arranged between the natural gas first cooling flow channel and the natural gas second cooling flow channel.
Further, a reheating device is arranged between the first reheating flow channel and the second reheating flow channel of the refrigerant.
Preferably, a first throttle valve is arranged on a connecting pipeline between the outlet end of the natural gas second cooling flow channel and the rectifying tower, and a second throttle valve is arranged on a connecting pipeline between the bottom outlet of the rectifying tower and the inlet of the natural gas third cooling flow channel.
A helium recovery method comprising the steps of:
the natural gas raw material gas enters the main heat exchanger after being pressurized by the compressor, and is sequentially cooled in the natural gas first cooling flow channel, the cooling device and the natural gas second cooling flow channel;
the cooled feed gas is decompressed through a throttle valve I and then enters a rectifying tower, and is further cooled in a tower top condenser, so that non-condensable gas is separated;
the liquid phase component flows back to the bottom of the rectifying tower, is heated, throttled and depressurized by a second throttling valve, and enters a third natural gas cooling flow channel to be cooled to obtain an LNG product;
non-condensable gas components such as helium, nitrogen and the like enter a fourth natural gas cooling flow channel for cooling, and a crude liquid nitrogen product and a crude helium product are separated by a gas-liquid separation device;
and the crude helium enters a helium reheating flow channel to provide cold energy for the main heat exchanger, and the crude helium is used as a crude helium product for storage or further purification after being reheated.
The helium gas recovery system and the method can safely and efficiently recover and extract helium gas from helium-containing natural gas, and the system has the advantages of simple and convenient operation, reliable operation, cost reduction and energy consumption saving, simplifies the process flow of helium gas recovery and extraction, and improves the economic value of helium gas recovery.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention;
FIG. 2 is a schematic flow chart of the steps of the present invention;
in the figure: 1. a primary heat exchanger; 11. a natural gas first cooling flow channel; 12. a natural gas second cooling flow channel; 13. a natural gas third cooling flow channel; 14. a natural gas fourth cooling flow channel; 15. a helium reheating flow channel; 2. a refrigeration cycle mechanism; 21. a refrigerant first cooling flow path; 22. a refrigerant second cooling flow passage; 23. a first recuperative refrigerant flow channel; 24. a second refrigerant reheat flow channel; 25. a refrigerant third recuperative flow channel; 26. a nitrogen compression device; 27. a primary expansion device; 28. a secondary expansion device; 3. a rectifying tower; 4. a gas-liquid separation device; 5. a cooling device; 6. a reheating device; 7. a first throttling valve; 8. and a second throttle valve.
Detailed Description
A preferred embodiment of the present invention will be described in detail below with reference to the accompanying drawings.
The helium recovery system and the method as shown in fig. 1 comprise a main heat exchanger 1, a refrigeration cycle mechanism 2 communicated with an internal flow passage of the main heat exchanger, a rectifying tower 3 and a gas-liquid separation device 4, wherein a natural gas first cooling flow passage 11, a natural gas second cooling flow passage 12, a natural gas third cooling flow passage 13, a natural gas fourth cooling flow passage 14 and a helium reheating flow passage 15 are arranged in the main heat exchanger; outlets are arranged at the top and the bottom of the rectifying tower, the outlet at the bottom is communicated with the inlet end of the natural gas third cooling flow channel, and a gas outlet at the top is communicated with the inlet end of the natural gas fourth cooling flow channel; outlets are arranged at the top and the bottom of the gas-liquid separation device, and the top outlets are communicated with the inlet end of the helium reheating flow channel.
The refrigeration cycle mechanism 2 according to the present preferred embodiment includes a refrigerant first cooling flow passage 21, a refrigerant second cooling flow passage 22, a refrigerant first reheating flow passage 23, a refrigerant second reheating flow passage 24, and a refrigerant third reheating flow passage 25, which are provided in the main heat exchanger; a nitrogen compression device 26 communicated with the inlet end of the first refrigerant cooling flow channel and the outlet end of the third refrigerant reheating flow channel; a first-stage expansion device 27 communicating with the outlet end of the refrigerant first cooling flow channel and the inlet end of the refrigerant third reheating flow channel; and a secondary expansion device 28 communicating with the outlet end of the refrigerant second cooling flow path and the inlet end of the refrigerant third reheat flow path.
The helium recovery method as shown in fig. 2 comprises the steps of:
s1, pressurizing the natural gas raw material gas through a compressor, then feeding the pressurized natural gas raw material gas into a main heat exchanger, and sequentially cooling the natural gas raw material gas in a first natural gas cooling flow channel, a cooling device and a second natural gas cooling flow channel;
s2, decompressing the cooled raw material gas through a throttle valve I, then feeding the decompressed raw material gas into a rectifying tower, further cooling the decompressed raw material gas in a tower top condenser, and separating out non-condensable gas;
s3, feeding non-condensable gas components such as helium, nitrogen and the like into a fourth natural gas cooling flow channel for cooling, and separating a crude liquid nitrogen product and a crude helium product through a gas-liquid separation device;
and S4, enabling the crude helium to enter a helium reheating flow channel to provide cold for the main heat exchanger, and storing or further purifying the crude helium after reheating.
Example (b): the method comprises the following steps that (1) after natural gas raw material gas is pressurized to 4.1MPa through a compressor, the natural gas raw material gas enters a natural gas first cooling flow channel in a main heat exchanger, is cooled to-40 ℃ in the natural gas first cooling flow channel, is cooled to-73 ℃ in a cooling device, and is cooled to-112 ℃ through a natural gas second cooling flow channel;
the cooled raw material gas is decompressed to 2.1MPa through a first throttling valve and then enters a rectifying tower, the raw material gas is further cooled to-156 ℃ in a tower top condenser, and a cold source of the tower top condenser is provided by a reheating device; wherein the liquid phase component is taken as reflux liquid to flow back to a reboiler at the bottom of the rectifying tower, a heat source of the reboiler at the bottom of the tower is provided by a cooling device, liquefied natural gas in the reboiler at the bottom of the tower is heated to-110 ℃, throttled by a throttle valve II and depressurized to 0.2MPa, and enters a third natural gas cooling flow channel to be cooled to-160 ℃ to obtain an LNG product; non-condensable gas components such as helium, nitrogen and the like enter a fourth natural gas cooling flow channel in the main heat exchanger to be cooled to-185 ℃, and enter a low-temperature gas-liquid separation device 4 to separate a crude liquid nitrogen product and a crude helium product;
the crude helium enters a helium reheating flow channel to provide cold energy for the main heat exchanger, and is reheated to about 25 ℃ to be used as a crude helium product for storage or further purification.
The nitrogen expansion refrigeration process is communicated with the main heat exchanger 1 through the inlet and outlet of the nitrogen compressor 26, the first-stage expansion machine 27 and the second-stage expansion machine 28 to form a refrigeration cycle, and the specific flow is as follows:
nitrogen is pressurized to 3.6Mpa by a nitrogen compressor and then enters the first cooling flow channel of the refrigerant to be cooled to-40 ℃, and then is divided into two parts, one part of high-pressure nitrogen enters a first-stage expansion device to be expanded and cooled to-146 ℃, the other part of high-pressure nitrogen is further cooled to-104 ℃ in the second cooling flow channel of the refrigerant and then enters a second-stage expansion device to be expanded and cooled to-189 ℃, and then is heated to-186 ℃ in the first reheating flow channel of the refrigerant and then enters a reheating device to be heated to-176 ℃;
the heated low-temperature refrigerant passes through the refrigerant second reheating flow channel again, is heated to-146 ℃, is mixed with the low-temperature refrigerant at-146 ℃ at the outlet of the first-stage expansion device, enters the refrigerant third reheating flow channel for reheating to 16 ℃, and then returns to the inlet of the nitrogen compressor, so that the refrigeration cycle is completed.
In order to improve the working and energy utilization efficiency of the system, a cooling device 5 is arranged between the first cooling flow channel and the second cooling flow channel of the natural gas in the preferred embodiment; a reheating device 6 is arranged between the first reheating flow channel and the second reheating flow channel of the refrigerant; the outlet end of the natural gas second cooling flow channel is connected with a first throttle valve 7 arranged on a connecting pipeline of the rectifying tower, and a second throttle valve 8 is arranged on a connecting pipeline of the outlet end of the rectifying tower and the inlet end of the natural gas third cooling flow channel.
The above-mentioned embodiments are merely illustrative of the preferred embodiments of the present invention, and do not limit the scope of the present invention, and various modifications and improvements made to the technical solution of the present invention by those skilled in the art without departing from the spirit of the present invention should fall within the protection scope defined by the claims of the present invention.
Claims (6)
1. A helium recovery system, comprising:
the device comprises a main heat exchanger (1), wherein a natural gas first cooling flow channel (11), a natural gas second cooling flow channel (12), a natural gas third cooling flow channel (13), a natural gas fourth cooling flow channel (14) and a helium reheating flow channel (15) are arranged in the main heat exchanger, and the main heat exchanger is connected with a refrigeration circulation mechanism (2);
the rectifying tower (3) is communicated with the natural gas first cooling flow channel, outlets are formed in the top and the bottom of the rectifying tower, the bottom outlet is communicated with the inlet end of the natural gas third cooling flow channel, and a top gas outlet is communicated with the inlet end of the natural gas fourth cooling flow channel; and
and the gas-liquid separation device (4) is communicated with the outlet of the fourth natural gas cooling flow channel, outlets are formed in the top and the bottom of the gas-liquid separation device, and a top gas outlet is communicated with the inlet end of the helium reheating flow channel.
2. A helium recovery system as claimed in claim 1, wherein said refrigeration cycle mechanism (2) comprises:
the main heat exchanger comprises a first refrigerant cooling flow channel (21), a second refrigerant cooling flow channel (21), a first refrigerant reheating flow channel (23), a second refrigerant reheating flow channel (24) and a third refrigerant reheating flow channel (25) which are arranged in the main heat exchanger;
a nitrogen compression device (26) communicated with the inlet end of the first refrigerant cooling flow channel and the outlet end of the third refrigerant reheating flow channel;
a first stage expansion device (27) in communication with the outlet end of the refrigerant first cooling flow path and the inlet end of the refrigerant third reheat flow path; and
and a secondary expansion device (28) in communication with the outlet end of the second refrigerant cooling flow path and the inlet end of the third refrigerant reheat flow path.
3. A helium recovery system as claimed in claim 1, wherein a cooling means (5) is provided between said first cooling flow path (11) of natural gas and said second cooling flow path (12) of natural gas.
4. The helium gas recovery system and method as claimed in claim 1, wherein a recuperating device (6) is disposed between the first recuperating flow channel (23) and the second recuperating flow channel (24).
5. The helium recovery system of claim 1, wherein a first throttling valve (7) is arranged on a connecting pipeline between the outlet end of the natural gas second cooling flow channel (12) and the rectifying tower, and a second throttling valve (8) is arranged on a connecting pipeline between the bottom outlet of the rectifying tower (3) and the inlet of the natural gas third cooling flow channel (13).
6. A helium recovery method based on the helium recovery system of any one of claims 1 to 5, comprising the steps of:
the natural gas raw material gas enters the main heat exchanger after being pressurized by the compressor, and is sequentially cooled in the natural gas first cooling flow channel, the cooling device and the natural gas second cooling flow channel;
the cooled feed gas is decompressed through a throttle valve I and then enters a rectifying tower, and is further cooled in a tower top condenser, so that non-condensable gas is separated;
the liquid phase component flows back to the bottom of the rectifying tower, is heated, throttled and depressurized by a second throttling valve, and enters a third natural gas cooling flow channel to be cooled to obtain an LNG product;
non-condensable gas components such as helium, nitrogen and the like enter a fourth natural gas cooling flow channel for cooling, and a crude liquid nitrogen product and a crude helium product are separated by a gas-liquid separation device;
and the crude helium enters a helium reheating flow channel to provide cold energy for the main heat exchanger, and the crude helium is used as a crude helium product for storage or further purification after being reheated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010733243.1A CN111928574A (en) | 2020-07-27 | 2020-07-27 | Helium gas recovery system and method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010733243.1A CN111928574A (en) | 2020-07-27 | 2020-07-27 | Helium gas recovery system and method |
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| CN111928574A true CN111928574A (en) | 2020-11-13 |
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| CN202010733243.1A Pending CN111928574A (en) | 2020-07-27 | 2020-07-27 | Helium gas recovery system and method |
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| CN (1) | CN111928574A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2614947C1 (en) * | 2016-05-11 | 2017-03-31 | Публичное акционерное общество "Газпром" | Method for natural gas processing with c2+ recovery and plant for its implementation |
| CN108731381A (en) * | 2018-06-13 | 2018-11-02 | 中国石油工程建设有限公司 | A kind of process unit and method of liquefied natural gas coproduction liquid helium |
| US20200088465A1 (en) * | 2018-09-13 | 2020-03-19 | Air Products And Chemicals, Inc. | Helium Extraction from Natural Gas |
| CN210892360U (en) * | 2019-08-12 | 2020-06-30 | 北京恒泰洁能科技有限公司 | Device for extracting helium from natural gas |
| CN213020534U (en) * | 2020-07-27 | 2021-04-20 | 合肥万豪能源设备有限责任公司 | Helium recovery system |
-
2020
- 2020-07-27 CN CN202010733243.1A patent/CN111928574A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2614947C1 (en) * | 2016-05-11 | 2017-03-31 | Публичное акционерное общество "Газпром" | Method for natural gas processing with c2+ recovery and plant for its implementation |
| CN108731381A (en) * | 2018-06-13 | 2018-11-02 | 中国石油工程建设有限公司 | A kind of process unit and method of liquefied natural gas coproduction liquid helium |
| US20200088465A1 (en) * | 2018-09-13 | 2020-03-19 | Air Products And Chemicals, Inc. | Helium Extraction from Natural Gas |
| CN210892360U (en) * | 2019-08-12 | 2020-06-30 | 北京恒泰洁能科技有限公司 | Device for extracting helium from natural gas |
| CN213020534U (en) * | 2020-07-27 | 2021-04-20 | 合肥万豪能源设备有限责任公司 | Helium recovery system |
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