CN208332859U - Helium and liquefied system are proposed from natural gas - Google Patents
Helium and liquefied system are proposed from natural gas Download PDFInfo
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- CN208332859U CN208332859U CN201820403350.6U CN201820403350U CN208332859U CN 208332859 U CN208332859 U CN 208332859U CN 201820403350 U CN201820403350 U CN 201820403350U CN 208332859 U CN208332859 U CN 208332859U
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- heat exchanger
- gas
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- nitrogen
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- 239000001307 helium Substances 0.000 title claims abstract description 245
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 245
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 150
- 239000003345 natural gas Substances 0.000 title claims abstract description 57
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract 58
- 238000005406 washing Methods 0.000 claims abstract description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 166
- 239000007789 gas Substances 0.000 claims description 94
- 229910052757 nitrogen Inorganic materials 0.000 claims description 82
- 239000007788 liquid Substances 0.000 claims description 66
- 238000001816 cooling Methods 0.000 claims description 48
- 238000012545 processing Methods 0.000 claims description 34
- 238000000746 purification Methods 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 29
- 230000003197 catalytic effect Effects 0.000 claims description 22
- 239000007791 liquid phase Substances 0.000 claims description 21
- 230000001590 oxidative effect Effects 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 10
- 229910052760 oxygen Inorganic materials 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 238000012546 transfer Methods 0.000 claims description 9
- 239000007792 gaseous phase Substances 0.000 claims description 8
- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 239000012071 phase Substances 0.000 claims description 8
- 238000004891 communication Methods 0.000 claims description 7
- 238000005201 scrubbing Methods 0.000 claims description 7
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 6
- 230000006837 decompression Effects 0.000 claims description 6
- 238000007701 flash-distillation Methods 0.000 claims description 6
- 238000005057 refrigeration Methods 0.000 claims description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 5
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 238000004900 laundering Methods 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 239000011344 liquid material Substances 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 2
- 210000000582 semen Anatomy 0.000 claims 1
- MCWJHOCHKYKWMK-UHFFFAOYSA-N helium Chemical compound [He].[He] MCWJHOCHKYKWMK-UHFFFAOYSA-N 0.000 description 188
- 238000000034 method Methods 0.000 description 12
- 230000008569 process Effects 0.000 description 9
- 230000001172 regenerating effect Effects 0.000 description 8
- 229960004424 carbon dioxide Drugs 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 125000004122 cyclic group Chemical group 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007380 fibre production Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000003384 imaging method Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 239000013307 optical fiber Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
Helium and liquefied system, including level-one heat exchanger are proposed in the slave natural gas of the utility model；Two-stage heat exchanger passes through piping connection with level-one heat exchanger；Methane rectifier column passes through piping connection with two-stage heat exchanger；Cold washing tower passes through piping connection with methane rectifier column；Denitrification column passes through piping connection with methane rectifier column.The technical solution of the utility model structure is simple, can mention helium from natural gas with efficiency is higher and liquefies.
Description
Technical field
The utility model relates to the recyclings of chemical industry tail gas, mention helium and liquefied from natural gas more particularly to one kind
System.
Background technique
Helium has important role in defence and military and scientific research because of its unique property, using its -268.9
DEG C low boiling point, liquid helium can be used in low-temperature superconducting and relevant cryogenic refrigerating system, in addition core of the helium in medical field
It is cooling to be used as superconducting electromagnet in MR imaging apparatus, is used as heat transfer medium in nuclear power apparatus, is used as in optical fiber production cold
But gas is protected with inertia, and is used as leak detection medium in vacuum leak hunting.
China's helium consumption figure is big, and helium low output, is substantially from foreign import, and helium is important to be present in naturally
In gas, the main source that helium is helium is mentioned from natural gas at present.
The helium industrially applied at present is mainly extracted from natural gas, and extracting helium from natural gas technology seems extremely important,
It is major way that helium is mentioned from natural gas currently with the method for low temperature, but prior art efficiency is lower.
Utility model content
The technical problem to be solved by the present invention is to provide a kind of higher helium and liquefied of mentioning from natural gas of efficiency
System.
Helium and liquefied system are proposed in the slave natural gas of the utility model, comprising:
Level-one heat exchanger for the processing that cools for the first time to unstripped gas；
Two-stage heat exchanger for cooling again to the unstripped gas that cools that treated for the first time, with described one
Grade heat exchanger passes through piping connection；
It is logical with the two-stage heat exchanger for the first throttle valve to the unstripped gas decompression processing after cooling again
Cross piping connection；
For handling decompression treated unstripped gas gas-liquid separation, the unstripped gas is made to isolate gaseous phase materials and liquid phase
First gas-liquid separator of material passes through piping connection with the first throttle valve；
The liquid phase material outlet of first gas-liquid separator passes through pipeline connection with LNG storage tank；The gas of first gas-liquid separator
Phase materials outlet is connected to the air inlet of BOG compressor；
For cooling down the three-stage heat exchanger of processing to the gas after BOG compressor compresses, with BOG compressor
Gas outlet connection；
For being cooled again the level Four heat exchanger of processing to the gas after BOG compressor compresses；With it is described
Three-stage heat exchanger passes through piping connection；
For being cooled three times the Pyatyi heat exchanger of processing to the gas after BOG compressor compresses；With it is described
Level Four heat exchanger passes through piping connection；
For making the nitrogen in the gas, oxygen liquid turn to mixes liquid to the gas scrubbing after BOG compressor compresses
It is detached from away after material, only remains the cold washing tower of helium, pass through piping connection with the Pyatyi heat exchanger；
For making mixes liquid feed separation go out the denitrification column of nitrogen to the mixes liquid low-temperature material rectifying, with institute
It states cold washing tower and passes through piping connection.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the discharge of methane mouth and methane of denitrification column
Discharge pipe connection, the methane discharge pipe pass through Pyatyi heat exchanger, and the methane discharge pipe and the first pipeline, the second pipeline connect
It connecing, the first pipeline is connected to LNG storage tank, and second throttle is provided on the first pipeline, and the second pipeline is connected to cold washing tower,
Booster pump is provided on second pipeline, the nitrogen outlet of denitrification column is connect with nitrogen discharge pipe, the nitrogen discharge pipe
By Pyatyi heat exchanger, level Four heat exchanger, so that the nitrogen rewarming in the nitrogen discharge pipe, the helium of cold washing tower
Outlet is connect with helium discharge pipe, and the helium discharge pipe passes through Pyatyi heat exchanger, level Four heat exchanger, so that the helium
Helium rewarming in gas discharge pipe.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include:
Helium catalytic oxidation treatment for helium discharge pipe to be discharged keeps hydrogen, alkane component in the helium anti-
The catalytic oxidizing equipment that should be removed is connected to helium discharge pipe；
For to the helium purification process after catalytic oxidation treatment removing, moisture, carbon dioxide in the helium
Room temperature purification devices, connect with catalytic oxidizing equipment.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein it further include helium liquefaction device, the helium liquid
Makeup is set including the helium compressor for compressing to helium, the Dewar container for liquefied nitrogen tank for storing liquid nitrogen, helium compressor and liquid
Nitrogen Dewar tank is described to send helium tube road successively after for compressed helium and purification process by sending helium pipeline connection
Helium precool forecooler, for after precooling helium for the first time cool handle first heat exchanger, for pair
The helium that cools that treated for the first time cools processing for the second time, makes the liquefied second heat exchanger of the helium, use
In the liquid helium throttle valve to the liquid helium reducing pressure by regulating flow that cools that treated for the second time, room temperature purification devices and helium tube road is sent to connect
It is logical, room temperature purification devices and send the tie point on helium tube road between helium compressor, forecooler, the sudden strain of a muscle of Dewar container for liquefied nitrogen tank top
Vapor phase outlet is connected by the entrance of helium gas back pipe and helium compressor, so that Dewar container for liquefied nitrogen tank flashes off being pressed for helium
Contracting, helium gas back pipe pass through second heat exchanger, first heat exchanger, forecooler.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include helium delivery pipe, the helium
It one end of delivery pipe and send helium pipeline connection, helium delivery pipe and the tie point on helium tube road is sent to be located at first heat exchanger, be pre-chilled
Between device, the other end of helium delivery pipe is connect with helium gas back pipe, the other end of helium delivery pipe and the company of helium gas back pipe
For contact between first heat exchanger, second heat exchanger, helium delivery pipe successively passes through the first expanding machine, the first heat exchange
Device, the second expanding machine, second heat exchanger, so that the helium in helium delivery pipe is by the first expander decrease temperature and pressure
Reason is cooled down by first heat exchanger, is provided cooling capacity after the processing of the second expander decrease temperature and pressure for second heat exchanger.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the liquid phase material of the first gas-liquid separator
Outlet is connected to LNG storage tank by transfer pipeline, and third throttle valve is provided on transfer pipeline.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include nitrogen refrigeration system, the nitrogen
Gas refrigeration system includes nitrogen compressor and the 4th throttle valve, and the outlet of nitrogen compressor passes through the 5th pipeline and the 4th throttling
The inlet communication of valve, the outlet of the 4th throttle valve is by the inlet communication of the 6th pipeline and nitrogen compressor, so that by described the
For nitrogen reflux after the throttling cooling of four throttle valves to nitrogen compressor, the 5th pipeline passes through level Four heat exchanger, denitrification column tower bottom
Reboiler, Pyatyi heat exchanger, the 6th pipeline pass through condenser, Pyatyi heat exchanger, the friendship of level Four heat at the top of denitrification column respectively
Parallel operation, the nitrogen in the 5th pipeline cool in level Four heat exchanger, denitrification column tower bottom reboiler, Pyatyi heat exchanger,
Condenser of the nitrogen of 6th pipeline at the top of denitrification column, Pyatyi heat exchanger provide cooling capacity in level Four heat exchanger.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the 5th pipe of one end connection of the 7th pipeline
The tie point of road, the other end the 6th pipeline of connection of the 7th pipeline, the 7th pipeline and the 5th pipeline is located at denitrification column tower bottom and boils again
Between device, Pyatyi heat exchanger, the tie point of the 7th pipeline and the 6th pipeline be located at level Four heat exchanger, Pyatyi heat exchanger it
Between, the 7th pipeline passes through level Four heat exchanger, third expanding machine, Pyatyi heat exchanger.
Helium and liquefied system are proposed in the slave natural gas of the utility model, comprising:
BOG compressor for being compressed to unstripped gas；
For the three-stage heat exchanger for the processing that cools for the first time to compressed unstripped gas, with the BOG compressor
Pass through piping connection；
For being cooled again the level Four heat exchanger of processing to the gas after BOG compressor compresses；With it is described
Three-stage heat exchanger passes through piping connection；
For being cooled three times the Pyatyi heat exchanger of processing to the gas after BOG compressor compresses；With it is described
Level Four heat exchanger passes through piping connection；
For making the nitrogen in the gas, oxygen liquid turn to mixes liquid to the gas scrubbing after BOG compressor compresses
It is detached from away after material, only remains the cold washing tower of helium, pass through piping connection with the Pyatyi heat exchanger；
For making mixes liquid feed separation go out the denitrification column of nitrogen to the mixes liquid low-temperature material rectifying, with institute
It states cold washing tower and passes through piping connection.
The technical solution of the utility model structure is simple, can mention helium from natural gas with efficiency is higher and liquefies.
Detailed description of the invention
Fig. 1 be the utility model slave natural gas in mention helium and liquefied system embodiment one structural schematic diagram；
Fig. 2 be the utility model slave natural gas in mention helium and liquefied system embodiment two structural schematic diagram；
Fig. 3 is the structural schematic diagram of catalytic oxidizing equipment；
Fig. 4 is the structural schematic diagram of room temperature purification devices.
Specific embodiment
As shown in Figure 1, proposing helium and liquefied system in the slave natural gas of the utility model, comprising:
Level-one heat exchanger E1 for the processing that cools for the first time to unstripped gas；
Two-stage heat exchanger E2 for cooling again to the unstripped gas that cools that treated for the first time, with level-one
Heat exchanger E1 passes through piping connection；
For the first throttle valve V1 to the unstripped gas decompression processing after cooling again, pass through with two-stage heat exchanger
Piping connection；
For handling decompression treated unstripped gas gas-liquid separation, unstripped gas is made to isolate gaseous phase materials and liquid phase material
The first gas-liquid separator 101, pass through piping connection with first throttle valve V1；
The liquid phase material outlet of first gas-liquid separator passes through pipeline connection with LNG storage tank 102；First gas-liquid separator
101 gaseous phase materials outlet is connected to the air inlet of BOG compressor B6；
For cooling down the three-stage heat exchanger E3 of processing to the gas after BOG compressor compresses, compressed with BOG
The gas outlet of machine B6 is connected to；
For being cooled again the level Four heat exchanger E4 of processing to the gas after BOG compressor compresses；With three
Grade heat exchanger E3 passes through piping connection；
For being cooled three times the Pyatyi heat exchanger E5 of processing to the gas after BOG compressor compresses；With four
Grade heat exchanger E4 passes through piping connection；
For making the nitrogen in gas, oxygen liquid turn to mixes liquid material to the gas scrubbing after BOG compressor compresses
It is detached from away afterwards, only remains the cold washing tower T2 of helium, pass through piping connection with Pyatyi heat exchanger；
For making mixes liquid feed separation go out the denitrification column T3 of nitrogen, with low temperature to mixes liquid low-temperature material rectifying
Scrubbing tower T2 passes through piping connection.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the discharge of methane mouth and first of denitrification column T3
Alkane discharge pipe 11 connects, and methane discharge pipe 11 passes through Pyatyi heat exchanger E5, and methane discharge pipe 11 and the first pipeline 1, second are managed
Road 2 connects, and the first pipeline 1 is connected to LNG storage tank 102, is provided with second throttle V2 on the first pipeline 1, the second pipeline 2 with it is low
Temperature laundering tower T2 is connected to, and is provided with booster pump P1 on the second pipeline 2.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the nitrogen outlet and nitrogen of denitrification column T3
The connection of gas discharge pipe, nitrogen discharge pipe passes through Pyatyi heat exchanger E5, level Four heat exchanger E4, so that the nitrogen in nitrogen discharge pipe
Gas rewarming.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the helium outlet of cold washing tower T2
It is connect with helium discharge pipe 10, helium discharge pipe 10 passes through Pyatyi heat exchanger E5, level Four heat exchanger E4, so that helium is discharged
Helium rewarming in pipe 10.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include:
Helium catalytic oxidation treatment for helium discharge pipe 10 to be discharged reacts the hydrogen in helium, alkane component
The catalytic oxidizing equipment B3 of removal, is connected to helium discharge pipe 10；
Room temperature for the helium purification process after catalytic oxidation treatment removing, moisture, carbon dioxide in helium
Purification devices B4 is connect with catalytic oxidizing equipment B3.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include helium liquefaction device, helium liquefaction dress
Set including the helium compressor B5 for being compressed to helium, the Dewar container for liquefied nitrogen tank 104 for storing liquid nitrogen, helium compressor B5 with
Dewar container for liquefied nitrogen tank 104 send helium tube road 80 successively by for compressed helium and purifying by sending helium tube road 80 to be connected to
Helium precools after processing forecooler E8, for cooling for the first time to the helium after precooling and handling first heat exchanger
E9, for cooling for the second time processing to the helium that cools that treated for the first time, make liquefied second heat exchange of helium
Device E10, for the liquid helium throttle valve 60 to the liquid helium reducing pressure by regulating flow that cools that treated for the second time, room temperature purification devices B4 with
It send helium tube road 80 to be connected to, room temperature purification devices and send the tie point on helium tube road 80 between helium compressor, forecooler, liquid nitrogen
The flash distillation gaseous phase outlet at the top of Dewar tank 104 is connected by the entrance of helium gas back pipe and helium compressor, so that liquid nitrogen is shut out
Crock 104 flashes off being compressed for helium, and helium gas back pipe passes through second heat exchanger E10, first heat exchanger E9, forecooler
E8。
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include helium delivery pipe 21, helium is defeated
Send one end of pipe to be connected to helium tube road 80 is sent, helium delivery pipe 21 and send the tie point on helium tube road 80 be located at first heat exchanger,
Between forecooler, the other end of helium delivery pipe 21 is connect with helium gas back pipe, the other end and helium gas back of helium delivery pipe
For the tie point of pipe between first heat exchanger, second heat exchanger, helium delivery pipe 21 successively passes through the first expanding machine
ET1, first heat exchanger E9, the second expanding machine ET2, second heat exchanger E10, so that the helium in helium delivery pipe is by first
Expanding machine ET1 expands decrease temperature and pressure processing, expands at decrease temperature and pressure by first heat exchanger cooling E9, by the second expanding machine ET2
Cooling capacity is provided after reason for second heat exchanger E10.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein forecooler E8 is Liquid nitrogen precooler device.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the gas gas-phase objects of the first gas-liquid separator 101
Material outlet is connected to the air inlet of BOG compressor B6 by third pipeline 3, and third pipeline 3 passes through two-stage heat exchanger E2, level-one
Heat exchanger E1, so that the gas of third pipeline 3 rewarming in two-stage heat exchanger, level-one heat exchanger.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the gas vent and BOG of LNG storage tank 102
The air inlet of compressor B6 is connected to by the 4th pipeline 4, and the 4th pipeline 4 passes through three-stage heat exchanger E3, so that the 4th pipeline 4
Gas rewarming in three-stage heat exchanger E3.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the liquid phase material of the first gas-liquid separator
Outlet is connected to LNG storage tank by transfer pipeline 50, and third throttle valve V3 is provided on transfer pipeline 50.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include nitrogen refrigeration system, nitrogen system
Cooling system includes nitrogen compressor B2 and the 4th throttle valve V4, and the outlet of nitrogen compressor passes through the 5th pipeline 5 and Section four
The inlet communication of valve V4 is flowed, the outlet of the 4th throttle valve passes through the inlet communication of the 6th pipeline 6 and nitrogen compressor B2, so that by
For nitrogen reflux after the throttling cooling of 4th throttle valve to nitrogen compressor, the 5th pipeline passes through level Four heat exchanger, denitrification column tower
Bottom reboiler E7, Pyatyi heat exchanger, the 6th pipeline pass through condenser E6, Pyatyi heat exchanger, four at the top of denitrification column respectively
Grade heat exchanger, the nitrogen in the 5th pipeline 5 are cold in level Four heat exchanger, denitrification column tower bottom reboiler, Pyatyi heat exchanger
But cool down, condenser E6 of the nitrogen of the 6th pipeline at the top of denitrification column, Pyatyi heat exchanger, provide in level Four heat exchanger it is cold
Amount.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein the 5th pipe of one end connection of the 7th pipeline 7
The tie point of road, the other end the 6th pipeline of connection of the 7th pipeline 7, the 7th pipeline and the 5th pipeline is located at denitrification column tower bottom and boils again
Between device, Pyatyi heat exchanger, the tie point of the tie point of the 7th pipeline and the 5th pipeline, the 7th pipeline and the 6th pipeline is located at
Between level Four heat exchanger, Pyatyi heat exchanger, the 7th pipeline is handed over by level Four heat exchanger, third expanding machine ET3, Pyatyi heat
Parallel operation.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein further include azeotrope circularly cooling system
System, azeotrope cycle refrigeration system is along the azeotrope that azeotrope flow direction successively includes for compressing to azeotrope
The outlet of the liquid phase azeotrope of compressor E1 and the second gas-liquid separator V103, the second gas-liquid separator V103 passes through the 8th pipe
Road 8 is connected to the 5th throttle valve V5, and the 5th throttle valve V5 connects the entrance of azeotrope compressor B1 by cryogen return line 22,
The gas phase azeotrope outlet of second gas-liquid separator V103 passes through the inlet communication of the 9th pipeline 9 and the 6th throttle valve V6, the
The outlet of six throttle valves is connected to by the tenth pipeline with cryogen return line 22, so that by the gas after the throttling cooling of the 6th throttle valve
It mixes cryogen and is back to azeotrope compressor, the 8th pipeline 8 passes through level-one heat exchanger, and the 9th pipeline 9 is by level-one warm
Exchanger, two-stage heat exchanger, the tenth pipeline pass through two-stage heat exchanger, and cryogen return line 22 passes through level-one heat exchanger,
Liquid phase azeotrope in 8th pipeline is cooling in level-one heat exchanger, and the liquid phase azeotrope in the 9th pipeline 9 is in level-one
Cooling in heat exchanger, two-stage heat exchanger, the liquid phase azeotrope in the tenth pipeline provides cooling capacity in two-stage heat exchanger,
Liquid phase azeotrope in cryogen return line 22 provides cooling capacity in level-one heat exchanger.
Helium and liquefied system are proposed in the slave natural gas of the utility model, comprising:
BOG compressor for being compressed to unstripped gas；
For the three-stage heat exchanger for the processing that cools for the first time to compressed unstripped gas, pass through with BOG compressor
Piping connection；
For being cooled again the level Four heat exchanger of processing to the gas after BOG compressor compresses；With three-level
Heat exchanger passes through piping connection；
For being cooled three times the Pyatyi heat exchanger of processing to the gas after BOG compressor compresses；With level Four
Heat exchanger passes through piping connection；
For making the nitrogen in gas, oxygen liquid turn to mixes liquid material to the gas scrubbing after BOG compressor compresses
It is detached from away afterwards, only remains the cold washing tower of helium, pass through piping connection with Pyatyi heat exchanger；
For making mixes liquid feed separation go out the denitrification column of nitrogen, being washed with low temperature to mixes liquid low-temperature material rectifying
It washs tower and passes through piping connection.
The technical solution of the utility model structure is simple, can mention helium from natural gas with efficiency is higher and liquefies.
The method that the technical solution of the utility model is related to includes: that the natural gas containing helium enters heat exchanger；Through being subcooled
Solidifying cooling, cryogenic rectification produce helium, and obtain LNG product simultaneously；Helium by catalysis oxidation and purification devices purification after, into
Enter helium liquefaction device, helium is liquefied, produces liquid helium.
The technical solution of the utility model process flow is stable, can be to recycle helium in the slave natural gas of greater efficiency, mention
The high economic value of product.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein azeotrope compressor, nitrogen compressor
It can be the compressor of the forms such as reciprocating compressor, centrifugal compressor, helical-lobe compressor.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein azeotrope group be divided into nitrogen, methane,
Ethylene, propane, iso-butane and isopentane any combination composition.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein cold washing tower, denitrification column can be sieve
Plate tower, packed tower, plate column.
Helium and liquefied system are proposed in the slave natural gas of the utility model, wherein heat exchanger can be handed over for plate-fin heat
Parallel operation and around tubing heat exchanger.
The advantages of the technical solution of the utility model is: process flow is stablized, and is greater than 95% to the rate of recovery of helium, is obtained
99% or more raw helium gas purity, and the rate of recovery of methane is greater than 99%, and product yield is big, and purity is high obtains liquid helium purity
99.999% or more.
Embodiment one
The structure of the embodiment one of helium and liquefied system is proposed in the slave natural gas of the utility model as shown in Figure 1, utilizing
Helium is mentioned from natural gas for the progress of above-described embodiment one and liquefied process is as follows:
Enter this system by the unstripped gas of purified treatment from battery limit (BL), is handed over through level-one heat exchanger E1 and second level heat
After parallel operation E2 cooling, it is depressured through throttle valve, into the first gas-liquid separator 101, the gas phase isolated is through two-stage heat exchanger
BOG compressor B6 is returned after E2 and level-one heat exchanger E1 rewarming, liquid phase material enters LNG storage tank 102, gas after throttle valve is depressured
BOG compressor B6 is mutually removed after three-stage heat exchanger E3 rewarming.
Azeotrope is after azeotrope compressor B1 pressurization, and through 103 gas-liquid separation of the second gas-liquid separator, liquid phase is into one
After grade heat exchanger E1 cools, after throttle valve is depressured, converge with the gaseous phase materials of return, gas phase is through level-one heat exchanger
After E1 and two-stage heat exchanger E2 cooling, after throttle valve is depressured, two-stage heat exchanger E2 is returned to, and converge with liquid phase cryogen,
Most afterwards after level-one heat exchanger E1 rewarming, azeotrope compressor B1 entrance is returned to, the cyclic process of cryogen is completed.
Respectively from the gaseous phase materials of the first gas-liquid separator 101 and LNG storage tank 102, after BOG compressor B6 pressurization,
After three-stage heat exchanger E3 heat exchange cooling, level Four heat exchanger E4, Pyatyi heat exchanger E5 are entered back into, after cooling, entrance is low
The bottom temperature laundering tower T2, in cold washing tower, liquid phase methane component is sprayed into from tower top, by heat and mass transfer process, from tower top
98.8% helium is obtained, helium removes catalytic oxidizing equipment after Pyatyi heat exchanger E5, level Four heat exchanger E4 rewarming, low
The liquid phase material that temperature laundering tower tower bottom obtains is into denitrification column T3.
Rich nitrogen tail gas is obtained in denitrification column T3 tower top, is out after Pyatyi heat exchanger E5, level Four heat exchanger E4 rewarming
System.LNG product is obtained in tower bottom, after Pyatyi heat exchanger E5 cooling, is divided into two strands, one removes LNG after throttle valve is depressured
Storage tank 102, in addition after stock-traders' know-how booster pump P1 pressurization, into the top of cold washing tower.
Nitrogen into after heat exchanger, denitrification column tower bottom reboiler E7, is divided into two after nitrogen compressor B2 pressurization
Stock is depressurized through throttle valve after one stock-traders' know-how Pyatyi heat exchanger E5 cooling, into denitrification column overhead condenser E6, is provided for tower top cold
After amount, Pyatyi heat exchanger E5 out；Other stock-traders' know-how level Four heat exchanger E4 enters back into third expanding machine ET3 expansion, cooling drop
After pressure, Pyatyi heat exchanger E5 is returned to, and with after in addition one converges, through level Four heat exchanger E4 rewarming, turn again to compression
Machine entrance completes the cyclic process of nitrogen.
Raw helium gas enters catalytic oxidizing equipment B3, in catalytic oxidizing equipment, by helium hydrogen and alkane component it is anti-
It should fall, subsequently into room temperature purification devices B4, by moisture and carbon dioxide eliminating, subsequently into helium liquefaction device.
Helium converges after helium compressor B5 pressurization with helium after purification, is pre-chilled after converging with forecooler E8.Pre-cooling
In device, liquid nitrogen LN2 becomes gas nitrogen GN2 after exchanging heat and goes out forecooler, after the pre-cooled device E8 of helium cools, is divided into two strands, and one
After stock-traders' know-how first heat exchanger E9, second heat exchanger E10 cooling, after throttle valve reducing pressure by regulating flow, into liquid helium Dewar tank
104, liquid helium product is produced, the gas phase helium Returning heat-exchanger of flash distillation returns helium compressor after over-heat-exchanger rewarming
B5；In addition after one enters the first expanding machine ET1 decrease temperature and pressure, continue to cool down through first heat exchanger E9, it is swollen using second
Swollen machine ET2 expands decrease temperature and pressure, after providing cooling capacity for second heat exchanger E10, converges with the helium of flash distillation, finally passes through first
After heat exchanger E9 and forecooler E8 rewarming, helium compressor B5 entrance is returned to, completes helium compression circulation.
Embodiment two
The structure of the embodiment two of helium and liquefied system is proposed in the slave natural gas of the utility model as shown in Fig. 2, utilizing
Helium is mentioned from natural gas for the progress of above-described embodiment two and liquefied process is as follows:
It after BOG from battery limit (BL), with heat exchanger E3 heat exchange, is pressurized through BOG compressor B6, pressurized BOG and heat are handed over
After parallel operation E3 heat exchange cooling, into heat exchanger E4, E5, after cooling, into the bottom cold washing tower T2, in cold washing tower
In, liquid phase methane component is sprayed into from tower top, by heat and mass transfer process, 98.8% helium is obtained from tower top, through heat exchanger
Catalytic oxidizing equipment is removed after E5, E4 rewarming, in the liquid phase material that tower bottom obtains into denitrification column T3.In the richness that denitrogenation column overhead obtains
Nitrogen tail gas goes out system after heat exchanger E5, E4 rewarming, in the LNG product that tower bottom obtains, after heat exchanger E5 cooling, point
At two strands, one goes out battery limit (BL) after throttle valve is depressured, in addition after stock-traders' know-how booster pump P1 pressurization, into the top of cold washing tower
Portion.
Nitrogen is after nitrogen compressor B2 pressurization, into heat exchanger E4, after denitrification column tower bottom reboiler E7, is divided into two
Stock depressurizes after one stock-traders' know-how heat exchanger E5 cooling through throttle valve, into denitrification column overhead condenser E6, after providing cooling capacity for tower top,
Heat exchanger E5 out, in addition a stock-traders' know-how heat exchanger E4, enters back into expanding machine ET3 and expands, after decrease temperature and pressure, Returning heat-exchanger
E5, and with after in addition one converges, through heat exchanger E4 rewarming, suction port of compressor is turned again to, completes the cyclic process of nitrogen.
Raw helium gas enters catalytic oxidizing equipment B3, in catalytic oxidizing equipment, by helium hydrogen and alkane component it is anti-
It should fall, subsequently into room temperature purification devices B4, by moisture and carbon dioxide eliminating, subsequently into helium liquefaction device.
Helium converges after helium compressor B5 pressurization with helium after purification, is pre-chilled after converging with forecooler E8.Pre-cooling
In device, liquid nitrogen LN2 becomes gas nitrogen GN2 after exchanging heat and goes out forecooler, after the pre-cooled device E8 of helium cools, is divided into two strands, and one
It is raw into liquid helium Dewar tank after throttle valve reducing pressure by regulating flow after stock-traders' know-how first heat exchanger E9, second heat exchanger E10 cooling
Output liquid helium product, the gas phase helium Returning heat-exchanger of flash distillation return helium compressor B5 after over-heat-exchanger rewarming；Separately
After outer one enters the first expanding machine ET1 decrease temperature and pressure, continue to cool down through first heat exchanger E9, using the second expanding machine
ET2 expands decrease temperature and pressure, after providing cooling capacity for second heat exchanger E10, converges with the helium of flash distillation, finally hands over by the first heat
After parallel operation E9 and forecooler E8 rewarming, helium compressor B5 entrance is returned to, completes helium compression circulation.
In conjunction with shown in Fig. 3, Fig. 4, catalytic oxidizing equipment B3 includes that heater E1 ' and heater E1 ' pass through piping connection
Reactor R1 ' and water cooler E2 '.Water cooler E2 ' is connect by pipeline with the top of reactor R1 '.Catalytic oxidizing equipment B3
It further include providing the oxygen pipeline of oxygen for reactor R1 '.
The workflow of catalytic oxidizing equipment is as follows: unstripped gas (helium) enters the present apparatus, first passes through heater heating and rises
Wen Hou, into reactor, oxygen pipeline provides oxygen for reactor, after reaction, by the hydrocarbon oxidation in unstripped gas at two
Carbonoxide and water export subsequent processing after water cooler E2 water cooling.
Room temperature purification devices B4 includes the dry purification column V3 ' of the first dry purification column V2 ' and second, be filled in tower 3A and
Helium is all connected at the top of 4A molecular sieve, the first drying purification column V2 ' and the second drying purification column V3 ' and enters pipeline, and first is dry
The bottom of dry purification column V2 ' and the bottom of the second dry purification column V3 ' are separately connected the first dry helium gas efferent duct, the second drying
Helium efferent duct is provided with the first control valve V30 ' on the first dry helium gas efferent duct, is arranged on the second dry helium gas efferent duct
There is the second control valve V40 '.
The bottom of first dry purification column V2 ' and the bottom of the second dry purification column V3 ' are separately connected the first regenerating tube, the
Two regenerating tubes are provided with third control valve V60 ' on the first regenerating tube, the 4th control valve V50 ' are provided on the second regenerating tube.The
One regenerating tube, the second regenerating tube are connect with regenerative vacuum pump P1 '.
When room temperature purification devices B4 works, the switching of two towers is used, and a tower is in adsorbed state, and in addition a tower is in regeneration shape
State, when regeneration, are parsed the impurity that molecular sieve adsorbs by regenerative vacuum pump P1 '.
Above are merely preferred embodiments of the utility model, it is noted that for the ordinary skill people of the art
For member, without departing from the principle of this utility model, it can also make several improvements and retouch, these improvements and modifications
Also it should be regarded as the protection scope of the utility model.
Claims (9)
1. one kind proposes helium and liquefied system from natural gas characterized by comprising
Level-one heat exchanger for the processing that cools for the first time to unstripped gas；
Two-stage heat exchanger for cooling again to the unstripped gas that cools that treated for the first time, with the level-one heat
Exchanger passes through piping connection；
For the first throttle valve to the unstripped gas decompression processing after cooling again, pass through pipe with the two-stage heat exchanger
Road connection；
For handling decompression treated unstripped gas gas-liquid separation, the unstripped gas is made to isolate gaseous phase materials and liquid phase material
The first gas-liquid separator, pass through piping connection with the first throttle valve；
The liquid phase material outlet of first gas-liquid separator passes through pipeline connection with LNG storage tank；The gas gas-phase objects of first gas-liquid separator
Material outlet is connected to the air inlet of BOG compressor；
For cooling down the three-stage heat exchanger of processing to the gas after BOG compressor compresses, with going out for BOG compressor
Port connection；
For being cooled again the level Four heat exchanger of processing to the gas after BOG compressor compresses；With the three-level
Heat exchanger passes through piping connection；
For being cooled three times the Pyatyi heat exchanger of processing to the gas after BOG compressor compresses；With the level Four
Heat exchanger passes through piping connection；
For making the nitrogen in the gas, oxygen liquid turn to mixes liquid material to the gas scrubbing after BOG compressor compresses
It is detached from away afterwards, only remains the cold washing tower of helium, pass through piping connection with the Pyatyi heat exchanger；
It is and described low for making mixes liquid feed separation go out the denitrification column of nitrogen to the mixes liquid low-temperature material rectifying
Temperature laundering tower passes through piping connection.
2. helium and liquefied system are proposed from natural gas as described in claim 1, which is characterized in that the discharge of methane of denitrification column
It mouthful is connect with methane discharge pipe, the methane discharge pipe is by Pyatyi heat exchanger, the methane discharge pipe and the first pipeline, the
Two piping connections, the first pipeline are connected to LNG storage tank, and second throttle is provided on the first pipeline, and the second pipeline is washed with low temperature
Tower connection is washed, is provided with booster pump on second pipeline, the nitrogen outlet of denitrification column is connect with nitrogen discharge pipe, the nitrogen
Gas discharge pipe passes through Pyatyi heat exchanger, level Four heat exchanger, so that the nitrogen rewarming in the nitrogen discharge pipe, cold washing
The helium outlet of tower is connect with helium discharge pipe, and the helium discharge pipe passes through Pyatyi heat exchanger, level Four heat exchanger, with
Make the helium rewarming in the helium discharge pipe.
3. helium and liquefied system are proposed from natural gas as claimed in claim 2, which is characterized in that further include:
Helium catalytic oxidation treatment for helium discharge pipe to be discharged removes the hydrogen in the helium, alkane component reaction
The catalytic oxidizing equipment removed is connected to helium discharge pipe；
Room temperature for the helium purification process after catalytic oxidation treatment removing, moisture, carbon dioxide in the helium
Purification devices are connect with catalytic oxidizing equipment.
4. helium and liquefied system are proposed from natural gas as claimed in claim 3, which is characterized in that further include helium liquefaction dress
It sets, the helium liquefaction device includes the helium compressor for compressing to helium, the Dewar container for liquefied nitrogen tank for storing liquid nitrogen, helium
Compressor and Dewar container for liquefied nitrogen tank by sending helium pipeline connection, it is described send helium tube road successively pass through for compressed helium and
After purification process helium precool forecooler, for after precooling helium for the first time cool processing the first heat exchange
Device, for cooling for the second time processing to the helium that cools that treated for the first time, make liquefied second heat of the helium
Exchanger, for the liquid helium throttle valve to the liquid helium reducing pressure by regulating flow that cools that treated for the second time, room temperature purification devices with give
Helium pipeline connection, room temperature purification devices and send the tie point on helium tube road between helium compressor, forecooler, Dewar container for liquefied nitrogen tank
The flash distillation gaseous phase outlet at top is connected by the entrance of helium gas back pipe and helium compressor, so that Dewar container for liquefied nitrogen tank flashes off helium
Gas is compressed, and helium gas back pipe passes through second heat exchanger, first heat exchanger, forecooler.
5. helium and liquefied system are proposed from natural gas as claimed in claim 4, which is characterized in that further include helium conveying
Pipe, one end of the helium delivery pipe and send helium pipeline connection, and helium delivery pipe is located at the first heat with the tie point for sending helium tube road
Between exchanger, forecooler, the other end of helium delivery pipe is connect with helium gas back pipe, the other end and helium of helium delivery pipe
The tie point of return pipe between first heat exchanger, second heat exchanger, helium delivery pipe successively pass through the first expanding machine,
First heat exchanger, the second expanding machine, second heat exchanger, so that the helium in helium delivery pipe is dropped by the first expander
The processing of temperature drop pressure is cooled down by first heat exchanger, is mentioned after the processing of the second expander decrease temperature and pressure for second heat exchanger
Semen donors.
6. helium and liquefied system are proposed from natural gas as claimed in claim 5, which is characterized in that the first gas-liquid separator
Liquid phase material outlet is connected to LNG storage tank by transfer pipeline, and third throttle valve is provided on transfer pipeline.
7. helium and liquefied system are proposed from natural gas as claimed in claim 6, which is characterized in that further include nitrogen refrigeration system
System, the nitrogen refrigeration system include nitrogen compressor and the 4th throttle valve, and the outlet of nitrogen compressor passes through the 5th pipeline
With the inlet communication of the 4th throttle valve, the outlet of the 4th throttle valve passes through the inlet communication of the 6th pipeline and nitrogen compressor, with
The nitrogen reflux for making to be throttled by the 4th throttle valve after cooling to nitrogen compressor, the 5th pipeline by level Four heat exchanger,
Denitrification column tower bottom reboiler, Pyatyi heat exchanger, the 6th pipeline pass through condenser at the top of denitrification column, Pyatyi heat exchange respectively
Device, level Four heat exchanger, the nitrogen in the 5th pipeline is in level Four heat exchanger, denitrification column tower bottom reboiler, Pyatyi heat exchanger
In cool, condenser of the nitrogen of the 6th pipeline at the top of denitrification column, Pyatyi heat exchanger provide in level Four heat exchanger
Cooling capacity.
8. helium and liquefied system are proposed from natural gas as claimed in claim 7, which is characterized in that one end of the 7th pipeline connects
The tie point of logical 5th pipeline, the other end the 6th pipeline of connection of the 7th pipeline, the 7th pipeline and the 5th pipeline is located at denitrification column
Between tower bottom reboiler, Pyatyi heat exchanger, the tie point of the 7th pipeline and the 6th pipeline is located at level Four heat exchanger, Pyatyi heat
Between exchanger, the 7th pipeline passes through level Four heat exchanger, third expanding machine, Pyatyi heat exchanger.
9. one kind proposes helium and liquefied system from natural gas characterized by comprising
BOG compressor for being compressed to unstripped gas；
For the three-stage heat exchanger for the processing that cools for the first time to compressed unstripped gas, pass through with the BOG compressor
Piping connection；
For being cooled again the level Four heat exchanger of processing to the gas after BOG compressor compresses；With the three-level
Heat exchanger passes through piping connection；
For being cooled three times the Pyatyi heat exchanger of processing to the gas after BOG compressor compresses；With the level Four
Heat exchanger passes through piping connection；
For making the nitrogen in the gas, oxygen liquid turn to mixes liquid material to the gas scrubbing after BOG compressor compresses
It is detached from away afterwards, only remains the cold washing tower of helium, pass through piping connection with the Pyatyi heat exchanger；
It is and described low for making mixes liquid feed separation go out the denitrification column of nitrogen to the mixes liquid low-temperature material rectifying
Temperature laundering tower passes through piping connection.
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| CN201820403350.6U CN208332859U (en) | 2018-03-23 | 2018-03-23 | Helium and liquefied system are proposed from natural gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201820403350.6U CN208332859U (en) | 2018-03-23 | 2018-03-23 | Helium and liquefied system are proposed from natural gas |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107228526A (en) * | 2017-07-03 | 2017-10-03 | 成都深冷液化设备股份有限公司 | A kind of LNG flashed vapours carry helium, denitrogenation and reliquefaction installation |
| CN108458549A (en) * | 2018-03-23 | 2018-08-28 | 中科瑞奥能源科技股份有限公司 | Helium and liquefied System and method for are carried from natural gas |
| CN111170290A (en) * | 2020-01-07 | 2020-05-19 | 中国科学院高能物理研究所 | Device and process for extracting helium from natural gas |
| CN113108551A (en) * | 2021-05-17 | 2021-07-13 | 中石化中原石油工程设计有限公司 | Process and device for extracting high-purity helium in liquefied natural gas production process |
| CN113247873A (en) * | 2021-06-02 | 2021-08-13 | 四川杰瑞恒日天然气工程有限公司 | System and method for recovering helium in natural gas |
| CN113883827A (en) * | 2021-10-29 | 2022-01-04 | 四川空分设备(集团)有限责任公司 | Helium purification and liquefaction system |
| CN116951900A (en) * | 2023-08-30 | 2023-10-27 | 宁夏天利丰能源利用有限公司 | Natural gas liquefaction and high-purity helium extraction integrated process |
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- 2018-03-23 CN CN201820403350.6U patent/CN208332859U/en not_active Withdrawn - After Issue
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107228526A (en) * | 2017-07-03 | 2017-10-03 | 成都深冷液化设备股份有限公司 | A kind of LNG flashed vapours carry helium, denitrogenation and reliquefaction installation |
| CN108458549A (en) * | 2018-03-23 | 2018-08-28 | 中科瑞奥能源科技股份有限公司 | Helium and liquefied System and method for are carried from natural gas |
| CN108458549B (en) * | 2018-03-23 | 2023-11-21 | 中科瑞奥能源科技股份有限公司 | System and method for extracting helium from natural gas and liquefying same |
| CN111170290A (en) * | 2020-01-07 | 2020-05-19 | 中国科学院高能物理研究所 | Device and process for extracting helium from natural gas |
| CN113108551A (en) * | 2021-05-17 | 2021-07-13 | 中石化中原石油工程设计有限公司 | Process and device for extracting high-purity helium in liquefied natural gas production process |
| CN113247873A (en) * | 2021-06-02 | 2021-08-13 | 四川杰瑞恒日天然气工程有限公司 | System and method for recovering helium in natural gas |
| CN113247873B (en) * | 2021-06-02 | 2022-07-01 | 四川杰瑞恒日天然气工程有限公司 | Recovery system and method for helium in natural gas |
| CN113883827A (en) * | 2021-10-29 | 2022-01-04 | 四川空分设备(集团)有限责任公司 | Helium purification and liquefaction system |
| CN113883827B (en) * | 2021-10-29 | 2023-03-03 | 四川空分设备(集团)有限责任公司 | Helium purification and liquefaction system |
| CN116951900A (en) * | 2023-08-30 | 2023-10-27 | 宁夏天利丰能源利用有限公司 | Natural gas liquefaction and high-purity helium extraction integrated process |
| CN116951900B (en) * | 2023-08-30 | 2024-08-09 | 宁夏天利丰能源利用有限公司 | Natural gas liquefaction and high-purity helium extraction integrated process |
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