CN212747065U - High-nitrogen and helium-containing natural gas liquefaction and crude helium and nitrogen extraction system - Google Patents
High-nitrogen and helium-containing natural gas liquefaction and crude helium and nitrogen extraction system Download PDFInfo
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Abstract
The utility model discloses a high nitrogen and contain helium natural gas liquefaction and thick helium and nitrogen extraction system belongs to extraction system technical field, including thick helium condenser, thick helium condenser communicates respectively has second liquid nitrogen throttling valve, liquid nitrogen subcooler, thick helium separator and demethanizer condensation separator, thick helium separator communicates respectively has liquid nitrogen subcooler and first liquid nitrogen choke valve, the other end intercommunication of first liquid nitrogen choke valve has flash steam separator, flash steam separator intercommunication has the liquid nitrogen subcooler, liquid nitrogen subcooler intercommunication has liquid nitrogen evaporating pressure control valve, the other end intercommunication of liquid nitrogen evaporating pressure control valve has demethanizer condenser, and natural gas diffuses a little, and helium extraction efficiency is high, draws production and nitrogen gas product to the nitrogen gas in the natural gas simultaneously, and economic benefits is good.
Description
Technical Field
The utility model relates to an extraction system especially relates to a high nitrogenous and contain helium natural gas liquefaction and thick helium and nitrogen extraction system, belongs to extraction system technical field.
Background
Helium is one of inert gases, is an important strategic material, has very important use in the aspects of aerospace, national defense, semiconductor production, nuclear magnetic resonance and gas leakage detection as a protective gas and an ultralow-temperature refrigerant, is mainly present in natural gas, and helium extracted from the natural gas is a main industrial source of the helium; for natural gas with low nitrogen content, crude helium can be extracted from LNG flash evaporation gas after natural gas liquefaction, but in the prior art, the natural gas is diffused more when being extracted, the efficiency of extracting helium is low, energy waste caused by production of liquid nitrogen and nitrogen products by extracting nitrogen from natural gas cannot be realized, and cyclic utilization cannot be realized.
SUMMERY OF THE UTILITY MODEL
The main object of the utility model is to provide a high nitrogenous and contain helium natural gas liquefaction and crude helium and nitrogen extraction system and solve above-mentioned problem.
The purpose of the utility model can be achieved by adopting the following technical scheme:
the system comprises a crude helium condenser, wherein the crude helium condenser is respectively communicated with a second liquid nitrogen throttling valve, a liquid nitrogen subcooler, a crude helium separator and a demethanizer condensation separator, the crude helium separator is respectively communicated with a liquid nitrogen subcooler and a first liquid nitrogen throttling valve, the other end of the first liquid nitrogen throttling valve is communicated with a flash steam separator, the flash steam separator is communicated with a liquid nitrogen subcooler, the liquid nitrogen subcooler is communicated with a liquid nitrogen evaporation pressure control valve, the other end of the liquid nitrogen evaporation pressure control valve is communicated with a demethanizer condenser, one side of the demethanizer condenser is provided with a demethanizer, the other side of the demethanizer is provided with a demethanizer reboiler, the demethanizer is communicated with the demethanizer condenser, and the demethanizer condensation separator is respectively communicated with the demethanizer and the demethanizer condenser, the demethanizer condenser is communicated with a circulating nitrogen throttling valve, the other end of the circulating nitrogen throttling valve is respectively communicated with the second liquid nitrogen throttling valve and a liquid nitrogen subcooler, the liquid nitrogen subcooler is communicated with a natural gas subcooling heat exchanger, the natural gas subcooling heat exchanger is respectively communicated with a mixed refrigerant three-stage throttling valve and a natural gas low-temperature throttling valve, the other end of the natural gas low-temperature throttling valve is communicated with a natural gas denitrification tower, one side of the natural gas denitrification tower is provided with a denitrification tower reboiler, the denitrification tower reboiler is communicated with a mixed refrigerant two-stage throttling valve, a natural gas subcooling heat exchanger and a natural gas liquefaction heat exchanger, the natural gas denitrification tower is also communicated with the demethanizer, the demethanizer reboiler is communicated with the natural gas subcooling heat exchanger and the natural gas liquefaction heat exchanger, and the mixed refrigerant two-stage, the natural gas denitrogenation tower intercommunication has natural gas high temperature choke valve, the other end intercommunication of natural gas high temperature choke valve has the natural gas liquefaction heat exchanger, the natural gas liquefaction heat exchanger intercommunication has the heavy hydrocarbon separator, just the heavy hydrocarbon separator with natural gas high temperature choke valve intercommunication.
Preferably, the natural gas liquefaction heat exchanger is communicated with a high-pressure mixed refrigerant separator and a mixed refrigerant first-stage throttling valve, the mixed refrigerant first-stage throttling valve is communicated with a natural gas precooling heat exchanger, the other end of the mixed refrigerant first-stage throttling valve is communicated with the high-pressure mixed refrigerant separator, the high-pressure mixed refrigerant separator is further communicated with the natural gas precooling heat exchanger, the natural gas precooling heat exchanger is communicated with a first mixed refrigerant compressor, the first mixed refrigerant compressor is communicated with a mixed refrigerant intersegmental cooler, the mixed refrigerant intersegmental cooler is communicated with a mixed refrigerant intersegmental separator, and the mixed refrigerant intersegmental separator is respectively communicated with the mixed refrigerant increasing pump and the second mixed refrigerant compressor.
Preferably, the second mixed refrigerant compressor is communicated with a mixed refrigerant final cooler, the mixed refrigerant booster pump is communicated with a mixed refrigerant final cooler, the other end of the mixed refrigerant final cooler is communicated with a mixed refrigerant final separator, and the mixed refrigerant final separator is communicated with the natural gas precooling heat exchanger.
Preferably, the natural gas precooling heat exchanger is communicated with a circulating nitrogen compressor, the natural gas precooling heat exchanger is also communicated with a flash steam compressor, and the flash steam compressor is communicated with a demethanizer.
Preferably, the flash evaporation steam separator outputs liquid nitrogen and a part of liquid nitrogen input value in the crude helium condenser, the natural gas precooling heat exchanger inputs natural gas and outputs heavy hydrocarbon, the circulating nitrogen compressor outputs nitrogen, and the output nitrogen is communicated with the natural gas precooling heat exchanger and is input into the natural gas precooling heat exchanger.
Preferably, the natural gas pre-cooling heat exchanger outputs flash steam to the flash steam compressor, and the natural gas pre-cooling heat exchanger outputs mixed refrigerant to the first mixed refrigerant compressor.
The utility model has the advantages of:
the utility model provides a high nitrogen and contain helium natural gas liquefaction and crude helium and nitrogen extraction system, the natural gas diffuses a little, and the helium extraction efficiency is high, to the nitrogen extraction production liquid nitrogen and nitrogen gas product in the natural gas simultaneously, economic benefits is good;
the separation of the light components such as nitrogen, helium and the like from the natural gas adopts two towers for separation, the natural gas is firstly denitrified to safe content, then the methane in the demethanizer is separated, the content of the methane in the light components such as nitrogen, helium and the like can be reduced to below 1ppm, the loss of the methane is reduced, and the yield of the liquefied natural gas is improved;
the crude helium is extracted by adopting a condensation separation method, meanwhile, components such as helium dissolved in liquid nitrogen are subjected to throttling flash evaporation, and then the components are compressed by a flash evaporation gas compressor and directly enter a demethanizer for recovery, the process is simplified, the channels of part of heat exchangers can be reduced, the extraction rate of the helium is increased, and the purity of the liquid nitrogen and the nitrogen is further improved. Wherein, the liquid nitrogen can be used for refining helium, and the nitrogen can be used as the nitrogen required by a factory and the daily supplement of a mixed refrigerant circulating system;
a nitrogen circulating refrigeration system is arranged to provide cold energy for the condenser of the demethanizer and the condensation and separation of helium and nitrogen;
the natural gas is liquefied by adopting single mixed refrigerant three-stage throttling refrigeration, wherein the two-stage refrigerant and the three-stage refrigerant respectively provide heat for a denitrification tower reboiler and a demethanizer reboiler, the process is relatively simple, and the energy consumption is relatively low.
Drawings
Fig. 1 is a process flow diagram of a preferred embodiment of a high nitrogen and helium containing natural gas liquefaction and crude helium and nitrogen extraction system according to the present invention.
In the figure: 1-a natural gas precooling heat exchanger, 2-a natural gas liquefaction heat exchanger, 3-a natural gas supercooling heat exchanger, 4-a heavy hydrocarbon separator, 5-a natural gas high temperature throttle valve, 6-a natural gas low temperature throttle valve, 7-a natural gas denitrogenation tower, 8-a denitrogenation tower reboiler, 9-a demethanization tower, 10-a demethanization tower condenser, 11-a demethanization tower reboiler, 12-a demethanization tower condensate separator, 13-a crude helium condenser, 14-a crude helium separator, 15-a first liquid nitrogen throttle valve, 16-a flash gas separator, 17-a flash gas compressor, 18-a circulating nitrogen gas compressor, 19-a liquid nitrogen subcooler, 20-a circulating nitrogen throttle valve, 21-a liquid nitrogen evaporation pressure control valve, 22-a second liquid nitrogen throttle valve, 23-a first mixed refrigerant compressor, 24-a mixed refrigerant inter-stage cooler, 25-a mixed refrigerant inter-stage separator, 26-a mixed refrigerant booster pump, 27-a mixed refrigerant final stage cooler, 28-a mixed refrigerant final stage separator, 29-a high-pressure mixed refrigerant separator, 30-a mixed refrigerant two-stage throttling valve, 31-a mixed refrigerant three-stage throttling valve, 32-a mixed refrigerant one-stage throttling valve and 33-a second mixed refrigerant compressor.
Detailed Description
In order to make the technical solutions of the present invention clearer and clearer for those skilled in the art, the present invention will be described in further detail with reference to the following embodiments and the accompanying drawings, but the embodiments of the present invention are not limited thereto.
As shown in fig. 1, the system for liquefying natural gas containing high nitrogen and high helium and extracting crude helium and nitrogen provided by this embodiment includes a crude helium condenser 13, the crude helium condenser 13 is respectively communicated with a second liquid nitrogen throttling valve 22, a liquid nitrogen subcooler 19, a crude helium separator 14 and a demethanizer condensate separator 12, the crude helium separator 14 is respectively communicated with a liquid nitrogen subcooler 19 and a first liquid nitrogen throttling valve 15, the other end of the first liquid nitrogen throttling valve 15 is communicated with a flash vapor separator 16, the flash vapor separator 16 is communicated with the liquid nitrogen subcooler 19, the liquid nitrogen subcooler 19 is communicated with a liquid nitrogen evaporation pressure control valve 21, the other end of the liquid nitrogen evaporation pressure control valve 21 is communicated with a demethanizer condenser 10, one side of the demethanizer condenser 10 is provided with a demethanizer 9, the other side of the demethanizer 9 is provided with a demethanizer reboiler 11, the demethanizer 9 is communicated with the demethanizer condenser 10, the demethanizer condensation separator 12 is respectively communicated with a demethanizer 9 and a demethanizer condenser 10, the demethanizer condenser 10 is communicated with a circulating nitrogen throttle valve 20, the other end of the circulating nitrogen throttle valve 20 is respectively communicated with a second liquid nitrogen throttle valve 22 and a liquid nitrogen subcooler 19, the liquid nitrogen subcooler 19 is communicated with a natural gas subcooling heat exchanger 3, the natural gas subcooling heat exchanger 3 is respectively communicated with a mixed refrigerant three-stage throttle valve 31 and a natural gas low-temperature throttle valve 6, the other end of the natural gas low-temperature throttle valve 6 is communicated with a natural gas denitrogenation tower 7, one side of the natural gas denitrogenation tower 7 is provided with a denitrogenation tower reboiler 8, the denitrogenation tower reboiler 8 is communicated with a mixed refrigerant two-stage throttle valve 30, the natural gas subcooling heat exchanger 3 and a natural gas liquefaction heat exchanger 2, the natural gas denitrogenation tower 7 is also, mix cryogen two-stage throttling valve 30 respectively with natural gas liquefaction heat exchanger 2 and natural gas supercooling heat exchanger 3 intercommunication, 7 intercommunications in natural gas denitrogenation tower have natural gas high temperature choke valve 5, the other end intercommunication of natural gas high temperature choke valve 5 has natural gas liquefaction heat exchanger 2, 2 intercommunications in natural gas liquefaction heat exchanger have heavy hydrocarbon separator 4, and heavy hydrocarbon separator 4 and natural gas high temperature choke valve 5 intercommunication.
In the figure: 1-a natural gas precooling heat exchanger, 2-a natural gas liquefaction heat exchanger, 3-a natural gas supercooling heat exchanger, 4-a heavy hydrocarbon separator, 5-a natural gas high temperature throttle valve, 6-a natural gas low temperature throttle valve, 7-a natural gas denitrogenation tower, 8-a denitrogenation tower reboiler, 9-a demethanization tower, 10-a demethanization tower condenser, 11-a demethanization tower reboiler, 12-a demethanization tower condensate separator, 13-a crude helium condenser, 14-a crude helium separator, 15-a first liquid nitrogen throttle valve, 16-a flash gas separator, 17-a flash gas compressor, 18-a circulating nitrogen gas compressor, 19-a liquid nitrogen subcooler, 20-a circulating nitrogen throttle valve, 21-a liquid nitrogen evaporation pressure control valve, 22-a second liquid nitrogen throttle valve, 23-first mixed refrigerant compressor, 24-mixed refrigerant interstage cooler, 25-mixed refrigerant interstage separator, 26-mixed refrigerant booster pump, 27-mixed refrigerant final stage cooler, 28-mixed refrigerant final stage separator, 29-high pressure mixed refrigerant separator, 30-mixed refrigerant two-stage throttle valve, 31-mixed refrigerant three-stage throttle valve, 32-mixed refrigerant one-stage throttle valve and 33-second mixed refrigerant compressor
The raw material natural gas after deacidification, dehydration and demercuration sequentially passes through the upper parts of a natural gas precooling heat exchanger 1 and a natural gas liquefying heat exchanger 2 and then is connected with a heavy hydrocarbon separator 4, the heavy hydrocarbon at the bottom of the heavy hydrocarbon separator 4 sequentially passes through the upper part of the natural gas liquefying heat exchanger 2 and the natural gas precooling heat exchanger 1 to be stored, the natural gas at the top of the heavy hydrocarbon separator 4 passes through the liquefying heat exchanger 2 and then is divided into two strands, one strand is connected with the middle part of a natural gas denitrification tower 7 through a natural gas low-temperature throttling valve 6, the other strand sequentially passes through the natural gas supercooling heat exchanger 3 and the natural gas low-temperature throttling valve 6 to be connected with the top of a natural gas denitrification tower 7, the bottom of the natural gas denitrification tower 7 is connected with a denitrification tower reboiler 8, the LNG at the bottom of the denitrification tower reboiler 8 passes through, the top gas of the demethanizer 9 is connected with a methane tower condensation separator 12 through a denitrogenation tower condenser 10 in sequence, and the bottom of the methane tower condensation separator 12 is connected with the top of the demethanizer 9; the bottom of the demethanizer 9 is connected with an evaporator, natural gas at the bottom of the evaporator is sent to a natural gas liquefaction storage device through a natural gas supercooling heat exchanger, and the top of a condensation separator is connected with a crude helium separator through a crude helium condenser. Crude helium at the top of the crude helium separator sequentially passes through the liquid nitrogen subcooler, the natural gas supercooling heat exchanger, the natural gas liquefaction heat exchanger and the natural gas precooling heat exchanger to go to the downstream process. The bottom of the crude helium separator is connected with the crude helium flash tank through a throttle valve, the top of the crude helium flash tank is connected with the inlet of a flash gas compressor through a liquid nitrogen subcooler, a natural gas subcooled heat exchanger, a natural gas liquefied heat exchanger and a natural gas precooling heat exchanger in sequence, and the outlet of the flash gas compressor is connected with a demethanizer. The nitrogen at the outlet of a nitrogen circulating compressor in the nitrogen circulating refrigeration system is divided into two parts after passing through a natural gas precooling heat exchanger, a natural gas liquefying heat exchanger, a natural gas supercooling heat exchanger and a liquid nitrogen subcooler in sequence, one part is connected with a demethanizer condenser through a throttle valve, the other part is connected with a crude helium condenser through a throttle valve, the circulating nitrogen from the demethanizer condenser is converged with the circulating nitrogen from the crude helium condenser through a pressure control valve and then passes through the liquid nitrogen subcooler, the natural gas supercooling heat exchanger, the natural gas liquefying heat exchanger and the natural gas precooling heat exchanger in sequence, and then the inlet of. In the single mixed refrigerant three-stage throttling refrigeration cycle, a liquid-phase refrigerant of the mixed refrigerant final-stage separator is connected with a first-stage throttling valve after passing through a natural gas precooling heat exchanger, and a gas-phase refrigerant of the mixed refrigerant final-stage separator is connected with a high-pressure refrigerant separator through a natural gas precooling heat exchanger; the liquid-phase mixed refrigerant at the bottom of the high-pressure refrigerant separator is connected with the secondary throttle valve through the natural gas liquefaction heat exchanger and the denitrification tower evaporator in sequence; the gas-phase refrigerant at the top of the high-pressure refrigerant separator is connected with the three-stage throttling valve sequentially through the natural gas liquefaction heat exchanger, the demethanizer reboiler and the natural gas supercooling heat exchanger, the mixed refrigerant from the three-stage throttling valve is converged through the natural gas supercooling heat exchanger and then passes through the natural gas liquefaction heat exchanger, then is converged with the mixed refrigerant from the first-stage throttling valve and then passes through the natural gas precooling heat exchanger, and then is connected with the inlet of the mixed refrigerant compressor, and the outlet of the first section of the mixed refrigerant compressor is connected with the mixed refrigerant intersegmental separator through the mixed refrigerant intersegmental cooler; the gas refrigerant at the top of the mixed refrigerant intersegmental separator is connected with the second-section inlet of the mixed refrigerant compressor, and the liquid refrigerant at the lower part of the mixed refrigerant intersegmental separator is connected with the inlet of the refrigerant booster pump; liquid-phase refrigerant at the outlet of the refrigerant booster pump is converged with gas-phase refrigerant at the outlet of the two sections of the refrigerant compressor and then is connected with a mixed refrigerant final-stage separator through a mixed refrigerant final-stage cooler, so that the circulation is completed.
In the embodiment, the natural gas liquefaction heat exchanger 2 is communicated with a high-pressure mixed refrigerant separator 29 and a mixed refrigerant first-stage throttle valve 32, the mixed refrigerant first-stage throttle valve 32 is communicated with the natural gas pre-cooling heat exchanger 1, the other end of the mixed refrigerant first-stage throttle valve 32 is communicated with the high-pressure mixed refrigerant separator 29, the high-pressure mixed refrigerant separator 29 is further communicated with the natural gas pre-cooling heat exchanger 1, the natural gas pre-cooling heat exchanger 1 is communicated with a first mixed refrigerant compressor 23, the first mixed refrigerant compressor 23 is communicated with a mixed refrigerant inter-stage cooler 24, the mixed refrigerant inter-stage cooler 24 is communicated with a mixed refrigerant inter-stage separator 25, and the mixed refrigerant inter-stage separator 25 is respectively communicated with a mixed refrigerant increasing pump 26 and a second mixed refrigerant compressor 33.
In the present embodiment, the second mixed refrigerant compressor 33 is communicated with the mixed refrigerant final stage cooler 27, the mixed refrigerant booster pump 26 is communicated with the mixed refrigerant final stage cooler 27, the other end of the mixed refrigerant final stage cooler 27 is communicated with the mixed refrigerant final stage separator 28, and the mixed refrigerant final stage separator 28 is communicated with the natural gas pre-cooling heat exchanger 1.
In this embodiment, the natural gas pre-cooling heat exchanger 1 is communicated with a circulating nitrogen compressor 18, the natural gas pre-cooling heat exchanger 1 is further communicated with a flash vapor compressor 17, and the flash vapor compressor 17 is communicated with the demethanizer 9.
In this embodiment, the flash steam separator 16 outputs liquid nitrogen and a part of the liquid nitrogen is input into the crude helium condenser 13, the natural gas precooling heat exchanger 1 inputs natural gas and outputs heavy hydrocarbon, the circulating nitrogen compressor 18 outputs nitrogen, and the output nitrogen is communicated with the natural gas precooling heat exchanger 1 and is input into the natural gas precooling heat exchanger 1.
In this embodiment, the natural gas pre-cooling heat exchanger 1 outputs flash steam to the flash steam compressor 17, and the natural gas pre-cooling heat exchanger 1 outputs a mixed refrigerant to the first mixed refrigerant compressor 23.
Above, only the further embodiments of the present invention are shown, but the protection scope of the present invention is not limited thereto, and any person skilled in the art can replace or change the technical solution and the concept of the present invention within the protection scope of the present invention.
Claims (6)
1. A high nitrogen and helium-containing natural gas liquefaction and crude helium and nitrogen extraction system is characterized in that: the device comprises a crude helium condenser (13), wherein the crude helium condenser (13) is respectively communicated with a second liquid nitrogen throttling valve (22), a liquid nitrogen subcooler (19), a crude helium separator (14) and a demethanizer condensation separator (12), the crude helium separator (14) is respectively communicated with the liquid nitrogen subcooler (19) and a first liquid nitrogen throttling valve (15), the other end of the first liquid nitrogen throttling valve (15) is communicated with a flash steam separator (16), the flash steam separator (16) is communicated with the liquid nitrogen subcooler (19), the liquid nitrogen subcooler (19) is communicated with a liquid nitrogen evaporation pressure control valve (21), the other end of the liquid nitrogen evaporation pressure control valve (21) is communicated with a demethanizer condenser (10), a demethanizer (9) is installed on one side of the demethanizer condenser (10), and a demethanizer reboiler (11) is installed on the other side of the demethanizer (9), the methane removing tower (9) is communicated with a methane removing tower condenser (10), a methane removing tower condensation separator (12) is communicated with the methane removing tower (9) and the methane removing tower condenser (10) respectively, the methane removing tower condenser (10) is communicated with a circulating nitrogen throttle valve (20), the other end of the circulating nitrogen throttle valve (20) is communicated with a second liquid nitrogen throttle valve (22) and a liquid nitrogen subcooler (19) respectively, the liquid nitrogen subcooler (19) is communicated with a natural gas subcooled heat exchanger (3), the natural gas subcooled heat exchanger (3) is communicated with a mixed refrigerant three-level throttle valve (31) and a natural gas low-temperature throttle valve (6) respectively, the other end of the natural gas low-temperature throttle valve (6) is communicated with a natural gas nitrogen removing tower (7), and a nitrogen removing tower (8) is installed on one side of the natural gas nitrogen removing tower (7), the denitrification tower reboiler (8) is communicated with a mixed refrigerant two-section throttling valve (30), a natural gas supercooling heat exchanger (3) and a natural gas liquefaction heat exchanger (2), the natural gas denitrification tower (7) is also communicated with the demethanizer (9), the demethanizer reboiler (11) is communicated with the natural gas supercooling heat exchanger (3) and the natural gas liquefaction heat exchanger (2), the mixed refrigerant two-section throttle valve (30) is respectively communicated with the natural gas liquefaction heat exchanger (2) and the natural gas supercooling heat exchanger (3), the natural gas denitrification tower (7) is communicated with a natural gas high-temperature throttle valve (5), the other end of the natural gas high-temperature throttle valve (5) is communicated with a natural gas liquefaction heat exchanger (2), the natural gas liquefaction heat exchanger (2) is communicated with a heavy hydrocarbon separator (4), and the heavy hydrocarbon separator (4) is communicated with the natural gas high-temperature throttling valve (5).
2. The high nitrogen and helium containing natural gas liquefaction and crude helium and nitrogen extraction system of claim 1, wherein: the natural gas liquefaction heat exchanger (2) is communicated with a high-pressure mixed refrigerant separator (29) and a mixed refrigerant primary throttle valve (32), the mixed refrigerant first-stage throttle valve (32) is communicated with a natural gas precooling heat exchanger (1), the other end of the mixed refrigerant primary throttle valve (32) is communicated with the high-pressure mixed refrigerant separator (29), the high-pressure mixed refrigerant separator (29) is also communicated with the natural gas precooling heat exchanger (1), the natural gas pre-cooling heat exchanger (1) is communicated with a first mixed refrigerant compressor (23), the first mixed refrigerant compressor (23) is communicated with a mixed refrigerant inter-segment cooler (24), the mixed refrigerant inter-stage cooler (24) is communicated with a mixed refrigerant inter-stage separator (25), the mixed refrigerant inter-stage separator (25) is respectively communicated with the mixed refrigerant increasing pump (26) and the second mixed refrigerant compressor (33).
3. The high nitrogen and helium containing natural gas liquefaction and crude helium and nitrogen extraction system of claim 2, wherein: the second mixed refrigerant compressor (33) is communicated with a mixed refrigerant final cooler (27), the mixed refrigerant booster pump (26) is communicated with the mixed refrigerant final cooler (27), the other end of the mixed refrigerant final cooler (27) is communicated with a mixed refrigerant final separator (28), and the mixed refrigerant final separator (28) is communicated with the natural gas pre-cooling heat exchanger (1).
4. The high nitrogen and helium containing natural gas liquefaction and crude helium and nitrogen extraction system of claim 3, wherein: the natural gas precooling heat exchanger (1) is communicated with a circulating nitrogen compressor (18), the natural gas precooling heat exchanger (1) is also communicated with a flash steam compressor (17), and the flash steam compressor (17) is communicated with a demethanizer (9).
5. The high nitrogen and helium containing natural gas liquefaction and crude helium and nitrogen extraction system of claim 4, wherein: the flash evaporation steam separator (16) output liquid nitrogen and a part of liquid nitrogen input value in the crude helium condenser (13), natural gas and output have heavy hydrocarbon in natural gas precooling heat exchanger (1) input, circulation nitrogen compressor (18) output has nitrogen gas, and the nitrogen gas of output with natural gas precooling heat exchanger (1) intercommunication and input to in the natural gas precooling heat exchanger (1).
6. The high nitrogen and helium containing natural gas liquefaction and crude helium and nitrogen extraction system of claim 5, wherein: flash steam is output to the flash steam compressor (17) from the natural gas pre-cooling heat exchanger (1), and mixed refrigerant is output to the first mixed refrigerant compressor (23) from the natural gas pre-cooling heat exchanger (1).
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Cited By (5)
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| CN113686098A (en) * | 2021-09-27 | 2021-11-23 | 西南石油大学 | Natural gas liquefaction and helium recovery method |
| CN113831942A (en) * | 2021-10-22 | 2021-12-24 | 中石化石油工程技术服务有限公司 | Natural gas liquefaction denitrification system and process |
| CN115060041A (en) * | 2022-06-28 | 2022-09-16 | 四川空分集团工程有限公司 | Liquid-air supercooling reflux expansion double-tower production nitrogen extraction system and method |
| WO2023124919A1 (en) * | 2021-12-29 | 2023-07-06 | 长庆工程设计有限公司 | System for purifying helium gas, method, and application |
| WO2024036837A1 (en) * | 2022-08-19 | 2024-02-22 | 长庆工程设计有限公司 | System for extracting helium from helium-poor natural gas and co-producing multiple products, and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113686098A (en) * | 2021-09-27 | 2021-11-23 | 西南石油大学 | Natural gas liquefaction and helium recovery method |
| CN113831942A (en) * | 2021-10-22 | 2021-12-24 | 中石化石油工程技术服务有限公司 | Natural gas liquefaction denitrification system and process |
| CN113831942B (en) * | 2021-10-22 | 2024-02-13 | 中石化石油工程技术服务有限公司 | Natural gas liquefaction denitrification system and process |
| WO2023124919A1 (en) * | 2021-12-29 | 2023-07-06 | 长庆工程设计有限公司 | System for purifying helium gas, method, and application |
| CN115060041A (en) * | 2022-06-28 | 2022-09-16 | 四川空分集团工程有限公司 | Liquid-air supercooling reflux expansion double-tower production nitrogen extraction system and method |
| CN115060041B (en) * | 2022-06-28 | 2024-04-05 | 四川空分集团工程有限公司 | System and method for producing nitrogen by liquid-air supercooling, backflow and expansion double towers |
| WO2024036837A1 (en) * | 2022-08-19 | 2024-02-22 | 长庆工程设计有限公司 | System for extracting helium from helium-poor natural gas and co-producing multiple products, and method |
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