CN104848654B - A kind of method and apparatus that argon gas is extracted in natural gas - Google Patents
A kind of method and apparatus that argon gas is extracted in natural gas Download PDFInfo
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- CN104848654B CN104848654B CN201510310285.3A CN201510310285A CN104848654B CN 104848654 B CN104848654 B CN 104848654B CN 201510310285 A CN201510310285 A CN 201510310285A CN 104848654 B CN104848654 B CN 104848654B
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- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 title claims abstract description 194
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 164
- 229910052786 argon Inorganic materials 0.000 title claims abstract description 97
- 239000007789 gas Substances 0.000 title claims abstract description 53
- 239000003345 natural gas Substances 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000001307 helium Substances 0.000 claims abstract description 46
- 229910052734 helium Inorganic materials 0.000 claims abstract description 46
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000000746 purification Methods 0.000 claims abstract description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 187
- 229910052757 nitrogen Inorganic materials 0.000 claims description 88
- 239000007788 liquid Substances 0.000 claims description 70
- 238000000605 extraction Methods 0.000 claims description 12
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 11
- 239000000284 extract Substances 0.000 claims description 9
- 238000004781 supercooling Methods 0.000 claims description 4
- 238000002309 gasification Methods 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims 1
- 238000004821 distillation Methods 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000004064 recycling Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- XKRFYHLGVUSROY-BJUDXGSMSA-N argon-39 atom Chemical compound [39Ar] XKRFYHLGVUSROY-BJUDXGSMSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- XKRFYHLGVUSROY-AHCXROLUSA-N argon-36 Chemical compound [36Ar] XKRFYHLGVUSROY-AHCXROLUSA-N 0.000 description 1
- XKRFYHLGVUSROY-YPZZEJLDSA-N argon-38 Chemical compound [38Ar] XKRFYHLGVUSROY-YPZZEJLDSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
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- Separation By Low-Temperature Treatments (AREA)
Abstract
The present invention provides the devices that argon gas is extracted in a kind of natural gas, include feed gas compressor, chilldown system, purification system and the main heat exchanger of pipeline connection, it is characterized in that, above device further includes helium knockout tower, helium separation tower reboiler, nitrogen-rejection column, except methane tower, pure argon column, subcooler and the pipeline for connecting above-mentioned component, valve；Invention also provides the methods that argon gas is extracted using natural gas as raw material, and obtained purity of argon is high, radiationless, while methods and apparatus of the present invention, using Full distillation technique, continuous operating time is long, and equipment is stablized.
Description
Technical field
The present invention relates to gas component separation, and more specifically the present invention relates to one kind to utilize Full distillation from natural gas
Extract the separation method of argon gas and corresponding device.
Background technology
The aerial content of argon gas is 0.93%, and helium is 5.2ppm.Content is very little in air for helium, typically from
It is extracted in natural gas.And in air, argon content ranking the 3rd, rich content, extraction is convenient, so argon gas extraction uses
Air is raw material.Present more than 10,000 big space divisions are typically equipped with Full distillation Argon recovery subsystem.Common flow is：Air is through pneumatics
Machine is compressed to required pressure, and removing carbon dioxide, water and hydrocarbon partial are removed in pre-cooled purifying.It is divided into before ice chest is entered
Two parts, a part are pressurized to 0.65~0.8MPa into turbine expansion generator terminal, then 20 DEG C are cooled to through cooler, into master
It is extremely more slightly higher than upper tower pressure into expander after heat exchanger is cooled to -120 DEG C~-140 DEG C, into upper tower.Another part
Air is by main heat exchanger and air cooling of being backflowed is to liquefaction, into lower tower after proceed by separation, into lower tower bottom
Air pass through column plate and on column plate phegma carry out caloic exchange, as a result, obtaining purity nitrogen on Xia Ta tops
Gas obtains oxygen-enriched liquid air in tower Fu.Lower top of tower overwhelming majority nitrogen enters the condensation side of condenser/evaporator, and nitrogen leads to there
It crosses and heat is released in the liquid oxygen evaporation of upper tower bottom, itself condensed and be used as lower tower phegma.Also part liquid nitrogen is passed through
It is sent to top of tower after the supercooling of cooler, the phegma of top of tower on work.The oxygen-enriched liquid air extracted out from the tower Fu of lower tower is through supercooling
The supercooling of device enters upper tower top as upper tower phegma after throttling.Oxygen product is finally generated in upper tower rectifying, from upper tower bottom
Extraction oxygen enters main heat exchanger, and device is gone out after oxygen re-heat and is sent out as product gas.Pure nitrogen gas is extracted out from upper top of tower, first
By pure liquid nitrogen and oxygen-enriched liquid air re-heat in subcooler, subsequently into going out device after re-heat in main heat exchanger.Draw from upper tower top
Go out dirty nitrogen, through subcooler, main heat exchanger re-heat to 21 DEG C of cooling box, subsequently into electric heater as regenerating molecular sieve gas
Body, excessive gas emptying.A certain amount of argon fraction is extracted in the middle part of from upper tower and is sent into crude argon column, crude argon column is divided into two in structure
Section, the phegma of second segment argon column bottom are sent at the top of first segment as phegma through liquid pump, are obtained through crude argon column rectifying pure
Spend about 98.5%Ar, 2ppm O2Crude argon, after liquefier liquefies be sent into pure argon column in the middle part of, through pure argon column rectifying in pure argon column
Bottom obtains sperm argon.The advantage of the method is argon abundant raw material, and extraction cost is low.But although argon content is rich in air
Richness, but argon also have a variety of isotopes, stable isotope have argon -40 (40Ar) natural content 99.6%, argon -36 (36Ar)
Natural content 0.34% and argon -38 (38Ar) natural content 0.06%.And it is generated not via cosmic-ray bombardment argon -40
Stable argon -39 (39Ar), so, the argon gas being limited in air influences, and argon isotope can not detach, and radiation can influence
Requirement of the special occasions such as laboratory to argon gas, especially many laboratory situations require several part per billion impurity contents now
When, air obviously cannot meet its requirement for the argon gas of raw material.
Invention content
The purpose of the present invention is being directed to each component feature of the absence of the prior art and natural gas, provide a kind of from natural
The method and apparatus of Full distillation extraction argon gas in gas, while ensure extracting method and stable equipment operation, efficiently.
Technical solution is used by the present invention solves above-mentioned technical problem：
A kind of method that argon gas is extracted in natural gas, includes the following steps：
Step 1：Natural gas is compressed in feed gas compressor after required pressure and is pre-chilled and purifies by chilldown system
System after purification, cools down and after helium separation tower reboiler is condensed into liquid, into helium knockout tower in main heat exchanger；
Step 2：Enter nitrogen-rejection column, most of nitrogen component after throttle valve is depressured in the liquid that helium separation tower bottom obtains
Nitrogen circulating system is escaped and enter at the top of from nitrogen-rejection column as circulating nitrogen gas, methane and the mixed liquor of argon gas and trace nitrogen component
Enter from tower bottom extraction is denitrogenated except methane tower, methane from except methane tower bottom extract out in liquid form recycled into subcooler it is cold
Amount contains a small amount of nitrogen from the crude argon come out except methane top of tower, into pure argon column, trace nitrogen gas component is detached, from essence
Argon column bottom obtains satisfactory straight argon liquid.
To optimize above-mentioned extracting method, the concrete measure taken further includes：
Above-mentioned circulating nitrogen gas in step 1 enters main heat exchanger after nitrogen circulation compressor compresses and cools down, and enters back into and removes
Nitrogen tower reboiler, except methane tower reboiler, pure argon column reboiler, provide heat for corresponding nitrogen-rejection column, except methane tower, pure argon column
Amount.
In step 1 after denitrogenating tower reboiler, converging except the liquid nitrogen that methane tower reboiler, pure argon column reboiler come out, one
Part enters liquid nitrogen gas-liquid separator after subcooler cools and throttles again, is come out from above-mentioned liquid nitrogen gas-liquid separator bottom
Liquid nitrogen as low-temperature receiver enter helium knockout tower condenser/evaporator, nitrogen-rejection column condenser/evaporator, except methane tower condenser/evaporator and
Pure argon column condenser/evaporator provides liquid for rectifying.
The part nitrogen come in from heat exchanger out enters expanding machine, this part nitrogen after expansion later from heat exchanger
With the nitrogen after four corresponding condenser/evaporators gasifications, the nitrogen at the top of liquid nitrogen gas-liquid separator out and from accordingly again
After the part nitrogen that boiling device comes out enters subcooler recycling cold together, finally the nitrogen with being come out at the top of nitrogen-rejection column merges into one
Stock, into main heat exchanger re-heat after enter nitrogen circulation compressor participate in cycle.
The present invention also provides in a kind of natural gas extract argon gas device, include pipeline connection feed gas compressor,
Chilldown system, purification system and main heat exchanger, which is characterized in that above device has further included helium knockout tower, helium knockout tower
Reboiler, nitrogen-rejection column, except methane tower, pure argon column, subcooler and the pipeline for connecting above-mentioned component, valve；Natural gas is successively
After feed gas compressor, chilldown system and purification system, cooled down in main heat exchanger and detach tower reboiler by helium
Enter helium knockout tower after being condensed into liquid, enter after throttle valve is depressured in the liquid that helium separation tower bottom obtains and denitrogenate
The mixed liquor and trace nitrogen component of tower, methane and argon gas enter from tower bottom extraction is denitrogenated except methane tower, and methane is from except methane tower
Bottom extracts out in liquid form into subcooler and recycles cold, contains a small amount of nitrogen from the crude argon come out except methane top of tower,
Satisfactory straight argon liquid is obtained into pure argon column.
In order to advanced optimize above device, the concrete measure taken further includes：
Above device also has nitrogen circulation compressor, above-mentioned helium knockout tower, nitrogen-rejection column, except methane tower, pure argon column phase
Ground is answered to set and is connected with helium separation tower reboiler, helium knockout tower condenser/evaporator, denitrogenates tower reboiler, nitrogen-rejection column condensation
Evaporator, except methane tower reboiler, except methane tower condenser/evaporator, pure argon column reboiler, pure argon column condenser/evaporator.
Above-mentioned subcooler is also associated with liquid nitrogen gas-liquid separator.
Above-mentioned device further includes the expanding machine being connected with above-mentioned heat exchanger and subcooler.
When carrying out argon gas extraction in natural gas using methods and apparatus of the present invention, first natural gas is compressed in compressor
Enter fractionating column ice chest after purification by chilldown system, purification system after to required pressure.Then, it is cooled down again in main heat exchanger
After the reboiler at helium knockout tower bottom is condensed into liquid, into helium knockout tower.Raw helium gas is obtained from helium separation tower top
It is vented after main heat exchanger re-heat.The liquid come out from helium separation tower bottom enters nitrogen-rejection column after throttle valve is depressured.Big portion
Nitrogen component is divided to be discharged at the top of nitrogen-rejection column, into nitrogen circulating system.The mixed liquor and trace nitrogen component of methane and argon gas from except
The extraction of nitrogen tower bottom enters except methane tower, methane from except methane tower bottom extract out in liquid form into subcooler recycling cold,
Main heat exchanger re-heat, gives user or it is used.Finally, contain a small amount of nitrogen from the crude argon come out except methane top of tower, enter
Pure argon column detaches trace nitrogen gas component, satisfactory straight argon liquid is obtained from pure argon column bottom.
Circulating nitrogen gas after nitrogen compressor compresses enter main heat exchanger cool down, enter back into denitrogenate tower reboiler, except methane tower again
Device, pure argon column reboiler are boiled, heat is provided for corresponding nitrogen-rejection column, except methane tower, pure argon column.It is come out from three tower reboilers
Some enters liquid nitrogen gas-liquid separator after subcooler cools and throttles again after liquid nitrogen converges, from gas-liquid separator bottom
The liquid nitrogen that portion comes out enters the condenser/evaporator of four rectifying columns as low-temperature receiver, and liquid is provided for rectifying.Come in from heat exchanger
Another strand of nitrogen out enters expanding machine later from heat exchanger, and nitrogen enters subcooler recycling cold after expansion.With condensing steaming again
Nitrogen out and the nitrogen of the part from reboiler out entered at the top of nitrogen, liquid nitrogen gas-liquid separator after hair device gasification
Cooler recycling cold after, with nitrogen-rejection column at the top of out nitrogen merge into one, into main heat exchanger re-heat after enter nitrogen pressure
Contracting participates in cycle, if any extra nitrogen, is vented herein.
Compared with prior art, the present invention extracts argon gas by raw material of natural gas, and obtained separation gas purity is high, no spoke
It penetrates, while methods and apparatus of the present invention, using Full distillation technique, continuous operating time is long, and equipment is stablized.
Description of the drawings
Fig. 1 is the flow diagram of the present invention.
Specific embodiment
To make the objectives, technical solutions, and advantages of the present invention clearer, below with reference to attached drawing to the skill of the present invention
Art scheme is further elaborated.
Fig. 1 is the flow diagram of the present invention.
Reference numeral therein is：Feed gas compressor 1；Chilldown system 2；Purification system 3；Main heat exchanger 4；Helium detaches
Tower 5；Helium detaches tower reboiler 6；Nitrogen-rejection column 7；Denitrogenate tower reboiler 8；Except methane tower 9；Except methane tower reboiler 10；Pure argon column
11；Pure argon column reboiler 12；Helium knockout tower condenser/evaporator 13；Nitrogen-rejection column condenser/evaporator 14；Except methane tower condensation evaporation
Device 15；Pure argon column condenser/evaporator 16；Liquid nitrogen gas-liquid separator 17；Subcooler 18；Expanding machine 22；Nitrogen circulation compressor 23；
Vacuum pump 24.
The present invention is described in more detail below by specific embodiment, for a better understanding of the present invention,
But following embodiments are not intended to limit the scope of the invention.
Embodiment 1
Feed gas composition：Helium 1.58%；Argon gas：0.27%；Nitrogen：81.91%；Methane：16.23%；Other are water
And carbon dioxide；Flow is：700Nm3/h
Unstripped gas is compressed to after pressure needed for 4.0MPa (G) after the cooling of chilldown system 2 extremely in feed gas compressor 1
10 DEG C, the purifying removing water (dew point of water of purification system 3<- 65 DEG C and carbon dioxide content<1ppm) enter fractionating column ice chest afterwards.
Be cooled in main heat exchanger 4-135 DEG C using helium separation tower reboiler 6 be condensed into liquid (due to helium it is difficult to liquefy,
Actual liquefaction rate is after 83%), into helium knockout tower 5.10 pieces of helium knockout tower number of theoretical plate, is pushed up from helium knockout tower 5
User is supplied to going out tower after 17 DEG C through 4 re-heat of main heat exchanger to raw helium gas (helium purity be 65.82%).
The liquid come out from 5 bottom of helium knockout tower enters nitrogen-rejection column 7 after throttle valve is depressurized to 0.15MPa (G).It denitrogenates
The theoretical cam curve of tower 7 is 60 pieces, and most of nitrogen component is discharged from 7 top of nitrogen-rejection column, and the nitrogen amount of discharge is 608Nm3/ h, nitrogen
Gas purity is：99.997%, into nitrogen circulating system.The mixed liquor and trace nitrogen component of methane and argon gas are from 7 bottom of nitrogen-rejection column
Portion's extraction enters except methane tower 9, and methane recycles cold, master from being extracted out in liquid form into subcooler 18 except 9 bottom of methane tower
4 re-heat of heat exchanger, gives user or it is used, methane content 121Nm3/h.Contain less from except the crude argon of 9 top of methane tower out
(component is amount nitrogen：Argon gas：99.938%；Nitrogen：0.0615%), into pure argon column 11, trace nitrogen gas component is detached, from
11 bottom of pure argon column obtains satisfactory straight argon liquid.
Cyclic nitrogen tolerance is 4000Nm3/ h cools to -120 DEG C after nitrogen compressor compression 23 into main heat exchanger 4, enters back into
Denitrogenate 8 (2757Nm of tower reboiler3/ h), except 10 (160Nm of methane tower reboiler3/ h), 12 (20Nm of pure argon column reboiler3/ h), be
Corresponding nitrogen-rejection column 7, except methane tower 9, pure argon column 11 provide heat.The liquid nitrogen come out from three tower reboilers has one after converging
Divide (2010Nm3/ h) enter liquid nitrogen gas-liquid point after subcooler 18 cools to -153.6 DEG C and is throttled to 0.04MPa (G) again
From device 17, the amount of liquid nitrogen come out from 17 bottom of gas-liquid separator is 947.2Nm3/ h enters the cold of four rectifying columns as low-temperature receiver
Solidifying evaporator (13,14,15,16), liquid is provided for rectifying.Another gang of nitrogen (1060Nm to come in from heat exchanger 43/ h), from
Heat exchanger out enters expanding machine 22 later, is expanded into -171.8 DEG C, 0.4MPa (G), nitrogen enters subcooler 18 and returns after expansion
Receive cold.With after condenser/evaporator gasifies nitrogen, the top of liquid nitrogen gas-liquid separator 17 nitrogen out and go out from reboiler
Re-heat converges to -155.9 DEG C with the nitrogen of 7 top of nitrogen-rejection column out after the nitrogen for the part come enters subcooler recycling cold
Into one, cycle is participated in into 4 re-heat of main heat exchanger to nitrogen pressure contracting is entered after 17 DEG C, if any extra nitrogen, is vented herein.
The present invention extracts argon gas by raw material of natural gas, and obtained separation gas purity is high, radiationless, while the present invention
Method and apparatus use Full distillation technique, and continuous operating time is long, and equipment is stablized.
Specific embodiments of the present invention are described in detail above, but it is intended only as example, it is of the invention and unlimited
It is formed on particular embodiments described above.To those skilled in the art, it is any to the equivalent modifications that carry out of the present invention and
It substitutes also all among scope of the invention.Therefore, the impartial conversion made without departing from the spirit and scope of the invention and
Modification, all should be contained within the scope of the invention.
Claims (8)
1. the method for argon gas is extracted in a kind of natural gas, which is characterized in that include the following steps：
Step 1：It is pre-chilled after natural gas is compressed to required pressure in feed gas compressor (1) by chilldown system (2) and pure
Change system (3) after purification, is cooled down and after helium separation tower reboiler (6) is condensed into liquid in main heat exchanger (4), is entered
Helium knockout tower (5)；
Step 2：Enter nitrogen-rejection column (7), most of nitrogen group after throttle valve is depressured in the liquid that helium knockout tower (5) bottom obtains
Nitrogen circulating system point is escaped and enter at the top of the nitrogen-rejection column (7) as circulating nitrogen gas, the mixed liquor of methane and argon gas and micro
From nitrogen-rejection column (7) bottom, extraction enters except methane tower (9) nitrogen component, and methane from except extracting out methane tower (9) bottom in liquid form
Cold is recycled into subcooler (18), contains a small amount of nitrogen from except the crude argon at the top of methane tower (9) out, into pure argon column
(11), trace nitrogen gas component is detached, satisfactory straight argon liquid is obtained from pure argon column (11) bottom.
2. the method for argon gas is extracted in a kind of natural gas according to claim 1, which is characterized in that described in step 2
Circulating nitrogen gas through nitrogen circulation compressor (23) compression after enter main heat exchanger (4) cool down, enter back into denitrogenate tower reboiler (8),
It is corresponding nitrogen-rejection column (7), except methane tower (9), pure argon column (11) except methane tower reboiler (10), pure argon column reboiler (12)
Heat is provided.
3. the method for argon gas is extracted in a kind of natural gas according to claim 2, which is characterized in that from denitrogenating in step 2
Tower reboiler (8), except methane tower reboiler (10), pure argon column reboiler (12) come out liquid nitrogen converge after, a part was passed through
Cooler (18) cools throttle again after enter liquid nitrogen gas-liquid separator (17), go out from liquid nitrogen gas-liquid separator (17) bottom
The liquid nitrogen come enters helium knockout tower condenser/evaporator (13), nitrogen-rejection column condenser/evaporator (14), except methane tower is cold as low-temperature receiver
Solidifying evaporator (15) and pure argon column condenser/evaporator (16), liquid is provided for rectifying.
4. the method for argon gas is extracted in a kind of natural gas according to claim 2, which is characterized in that from main heat exchanger (4)
The part nitrogen come in, from main heat exchanger (4) out after enter expanding machine (22), this part nitrogen after expansion in helium
Knockout tower condenser/evaporator (13), nitrogen-rejection column condenser/evaporator (14) are condensed except methane tower condenser/evaporator (15) and pure argon column
Nitrogen at the top of nitrogen, liquid nitrogen gas-liquid separator (17) after evaporator (16) gasification out enters subcooler (18) and recycles together
After cold, finally with nitrogen-rejection column (7) at the top of out nitrogen merge into one, into main heat exchanger (4) re-heat after enter nitrogen
Recycle compressor (23) participates in cycle.
5. in a kind of natural gas extract argon gas device, include pipeline connection feed gas compressor (1), chilldown system (2),
Purification system (3) and main heat exchanger (4), which is characterized in that described device has further included helium knockout tower (5), helium knockout tower
Reboiler (6), nitrogen-rejection column (7), except methane tower (9), pure argon column (11), subcooler (18) and the pipe for connecting above-mentioned component
Road, valve；Natural gas is successively after feed gas compressor (1), chilldown system (2) and purification system (3), in main heat exchanger
(4) it is cooled down in and enters helium knockout tower (5) after helium separation tower reboiler (6) is condensed into liquid, in helium knockout tower
(5) liquid that bottom obtains enters nitrogen-rejection column (7) after throttle valve is depressured, the mixed liquor and trace nitrogen component of methane and argon gas from
The extraction of nitrogen-rejection column (7) bottom enters except methane tower (9), and methane is from except extracting out in liquid form into supercooling methane tower (9) bottom
Device (18) recycles cold, contains a small amount of nitrogen from except the crude argon at the top of methane tower (9) out, is accorded with into pure argon column (11)
Close the straight argon liquid of requirement.
6. the device of argon gas is extracted in a kind of natural gas according to claim 5, which is characterized in that described device also has
Nitrogen circulation compressor (23), the helium knockout tower (5), nitrogen-rejection column (7) are correspondingly set except methane tower (9), pure argon column (11)
It puts and is connected with helium separation tower reboiler (6), helium knockout tower condenser/evaporator (13), denitrogenates tower reboiler (8), nitrogen-rejection column
Condenser/evaporator (14), except methane tower reboiler (10), except methane tower condenser/evaporator (15), pure argon column reboiler (12), essence
Argon column condenser/evaporator (16).
7. the device of argon gas is extracted in a kind of natural gas according to claim 5, which is characterized in that the subcooler (18)
It is also associated with liquid nitrogen gas-liquid separator (17).
8. in a kind of natural gas according to claim 5 extract argon gas device, which is characterized in that further included with it is described
The expanding machine (22) that main heat exchanger (4) is connected with subcooler (18).
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| CN109734064B (en) * | 2019-01-03 | 2020-12-18 | 北京中科富海低温科技有限公司 | A helium gas production system and production method |
| CN110608582B (en) * | 2019-09-10 | 2024-07-26 | 苏州市兴鲁空分设备科技发展有限公司 | Argon tail gas recovery and purification device |
| CN110542279B (en) * | 2019-09-10 | 2024-07-26 | 苏州市兴鲁空分设备科技发展有限公司 | Argon tail gas recovery and purification device containing methane and hydrocarbon |
| CN114777420B (en) * | 2022-03-31 | 2024-08-02 | 中科瑞奥能源科技股份有限公司 | System and method for recovering argon and high-purity methane in hydrogen system |
| CN115371359B (en) * | 2022-08-25 | 2023-06-16 | 北京航天试验技术研究所 | Sabat device reaction gas separation liquefaction system and method applied to Mars surface |
| CN116987536B (en) * | 2023-06-15 | 2024-03-08 | 英德市西洲气体有限公司 | Argon removal process for methane tower |
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