CN204787595U - Draw device of argon gas in natural gas - Google Patents
Draw device of argon gas in natural gas Download PDFInfo
- Publication number
- CN204787595U CN204787595U CN201520393425.3U CN201520393425U CN204787595U CN 204787595 U CN204787595 U CN 204787595U CN 201520393425 U CN201520393425 U CN 201520393425U CN 204787595 U CN204787595 U CN 204787595U
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- CN
- China
- Prior art keywords
- nitrogen
- tower
- argon
- helium
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 title claims abstract description 144
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 229910052786 argon Inorganic materials 0.000 title claims abstract description 72
- 239000007789 gas Substances 0.000 title claims abstract description 43
- 239000003345 natural gas Substances 0.000 title claims abstract description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 114
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 54
- 239000001307 helium Substances 0.000 claims abstract description 37
- 229910052734 helium Inorganic materials 0.000 claims abstract description 37
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000000746 purification Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 43
- 239000000284 extract Substances 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000000605 extraction Methods 0.000 abstract description 3
- -1 feed gas compressor Chemical compound 0.000 abstract description 2
- 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
- 229910001873 dinitrogen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000004821 distillation Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 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 2
- 230000005494 condensation Effects 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
- XKRFYHLGVUSROY-BJUDXGSMSA-N argon-39 atom Chemical compound [39Ar] XKRFYHLGVUSROY-BJUDXGSMSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 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
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 210000000582 semen Anatomy 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
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model provides a draw device of argon gas in natural gas, including feed gas compressor, precooling system, purification system and the main heat exchanger of pipe connection, its characterized in that, above -mentioned device still including helium knockout tower, helium knockout tower reboiler, remove the nitrogen column, remove the methane tower, pure argon column, subcooler and pipeline, the valve of connecting above -mentioned parts, the utility model discloses the device utilizes the natural gas high, radiationless for raw material extraction's argon gas purity, simultaneously the utility model discloses a device uses full rectification technology, and continuous operating time is long, and equipment is stable.
Description
Technical field
The utility model relates to gas component and is separated, and more particularly the utility model relates to a kind of device utilizing Full distillation to extract argon gas from natural gas.
Background technology
The aerial content of argon gas is 0.93%, and helium is 5.2ppm.Helium in atmosphere content very little, normally extracts from natural gas.And in atmosphere, argon content ranking the 3rd, rich content, it is convenient to extract, and all adopts air to be raw material so argon gas extracts.Present more than 10,000 large empty dividing were typically equipped with Full distillation Argon recovery subsystem.Common flow process is: air is compressed to required pressure through air compressor machine, removes carbon dioxide, water and hydrocarbon partial through precooling purifying.Be divided into two parts before entering ice chest, a part enters turbo-expander end and is pressurized to 0.65 ~ 0.8MPa, is then cooled to 20 DEG C through cooler, enters after main heat exchanger is cooled to-120 DEG C ~-140 DEG C, enter expander to slightly higher than upper tower pressure, enter Shang Ta.Another part air is through main heat exchanger and the gas that backflowed is cooled to liquefaction, start to be separated after entering lower tower, the air entering lower tower bottom passes column plate and carries out caloic exchange with the phegma on column plate, such result is, obtain pure nitrogen gas on Xia Ta top, obtain oxygen-enriched liquid air at tower Fu.Lower top of tower overwhelming majority nitrogen enters the condensation side of condenser/evaporator, and nitrogen is by releasing heat the evaporation of the liquid oxygen of upper tower bottom there, self obtains condensation and as lower tower phegma.Part liquid nitrogen is also had after the mistake of subcooler is cold, to be sent to upper top of tower, the phegma of top of tower on work.Excessively cold through subcooler of the oxygen-enriched liquid air extracted out from the tower Fu of lower tower, enters tower top as upper tower phegma after throttling.Oxygen product finally produces in upper tower rectifying, extracts oxygen out and enters main heat exchanger, go out device and send as gas product after oxygen re-heat from upper tower bottom.Pure nitrogen gas is extracted out from upper top of tower, first in subcooler by pure liquid nitrogen and oxygen-enriched liquid air re-heat, then enter in main heat exchanger and go out device after re-heat.Draw dirty nitrogen from upper tower top, through subcooler, main heat exchanger re-heat to 21 DEG C cooling box, then enter electric heater as regenerating molecular sieve gas, excessive gas emptying.In the middle part of upper tower, extract a certain amount of argon fraction send into crude argon column, crude argon column is structurally divided into two sections, and the phegma bottom second segment argon column sends into first paragraph top as phegma through liquor pump, obtains purity and is about 98.5%Ar, 2ppmO through crude argon column rectifying
2crude argon, send in the middle part of pure argon column through liquefier post liquefaction, bottom pure argon column, obtain seminal fluid argon through pure argon column rectifying.The advantage of the method is argon abundant raw material, and extraction cost is low.But although argon content is enriched in air, argon also has multiple isotope, stable coordination have argon-40 (
40ar) natural content 99.6%, argon-36 (
36ar) natural content 0.34% and argon-38 (
38ar) natural content 0.06%.And the argon-39 of the instability to generate via cosmic-ray bombardment argon-40 (
39ar), so, be limited to the argon gas impact in air, its argon isotope cannot be separated, its radiation can affect the requirement of the special occasions such as laboratory to argon gas, especially, now during a lot of laboratory situations requirement several part per billion impurity content, air is that the argon gas of raw material obviously can not meet its requirement.
Utility model content
The purpose of this utility model is each component feature of absence for prior art and natural gas, provide a kind of from natural gas Full distillation extract the device of argon gas, ensure that extraction equipment is stable, efficient simultaneously.
The utility model solves the problems of the technologies described above adopted technical scheme:
The device of argon gas is extracted in a kind of natural gas, include feed gas compressor, chilldown system, purification system and main heat exchanger that pipeline connects, it is characterized in that, said apparatus also include helium knockout tower, helium knockout tower reboiler, nitrogen-rejection column, except methane tower, pure argon column, subcooler and pipeline, valve that above-mentioned parts are connected, natural gas is successively through feed gas compressor, after chilldown system and purification system, cooling in main heat exchanger also enters helium knockout tower after helium knockout tower reboiler is condensed into liquid, the liquid obtained bottom helium knockout tower enters nitrogen-rejection column after choke valve step-down, the mixed liquor of methane and argon gas and trace nitrogen component are extracted out and are entered except methane tower bottom nitrogen-rejection column, methane enters subcooler recovery cold from extracting out in liquid form except methane tower bottom, a small amount of nitrogen is contained from except methane top of tower crude argon out, enter pure argon column and obtain satisfactory straight argon liquid.
In order to optimize said apparatus further, the concrete measure taked also comprises:
Said apparatus also has nitrogen circulation compressor, above-mentioned helium knockout tower, nitrogen-rejection column, except methane tower, pure argon column correspondingly arrange and be connected with helium knockout tower reboiler, helium knockout tower condenser/evaporator, nitrogen-rejection column reboiler, nitrogen-rejection column condenser/evaporator, except methane tower reboiler, except methane tower condenser/evaporator, pure argon column reboiler, pure argon column condenser/evaporator.
Above-mentioned subcooler is also connected with liquid nitrogen gas-liquid separator.
Above-mentioned device also includes the decompressor be connected with subcooler with above-mentioned heat exchanger.
Apply device of the present utility model and to carry out in natural gas argon gas when extracting, first by natural gas entering fractionating column ice chest after being compressed to required pressure in compressor after chilldown system, purification system purifying.Then, cool in main heat exchanger again after the reboiler at the bottom of helium knockout tower is condensed into liquid, enter helium knockout tower.Be separated tower top from helium and obtain the emptying after main heat exchanger re-heat of raw helium gas.Bottom helium knockout tower, liquid out enters nitrogen-rejection column after choke valve step-down.Most of the nitrogen component is discharged from nitrogen-rejection column top, enters nitrogen circulating system.The mixed liquor of methane and argon gas and trace nitrogen component are extracted out and are entered except methane tower bottom nitrogen-rejection column, and methane enters subcooler recovery cold, main heat exchanger re-heat from extracting out in liquid form except methane tower bottom, gives user or its use.Finally, contain a small amount of nitrogen from except methane top of tower crude argon out, enter pure argon column, trace nitrogen gas Component seperation, bottom pure argon column, obtain satisfactory straight argon liquid.
Circulating nitrogen gas through nitrogen compressor compression laggard enter main heat exchanger cooling, then enter nitrogen-rejection column reboiler, except methane tower reboiler, pure argon column reboiler, for the nitrogen-rejection column of correspondence, provide heat except methane tower, pure argon column.After converging from three tower reboilers liquid nitrogen out, some enters liquid nitrogen gas-liquid separator after subcooler cools throttling again, bottom gas-liquid separator, liquid nitrogen out enters the condenser/evaporator of four rectifying columns as low-temperature receiver, for rectifying provides liquid.From another strand of nitrogen that heat exchanger is come in, from heat exchanger out after enter decompressor, expand after nitrogen enter subcooler reclaim cold.Nitrogen after gasifying with condenser/evaporator again, liquid nitrogen gas-liquid separator top nitrogen out and enter after subcooler reclaims cold from the nitrogen of reboiler part out, one is merged into nitrogen-rejection column top nitrogen out, enter nitrogen pressure contracting after entering main heat exchanger re-heat and participate in circulation, if any unnecessary nitrogen, in this emptying.
Compared with prior art, the utility model is that raw material extracts argon gas with natural gas, and the divided gas flow purity obtained is high, radiationless, and device of the present utility model uses Full distillation technique simultaneously, and continuous operating time is long, and equipment is stablized.
Accompanying drawing explanation
Fig. 1 is schematic flow sheet of the present utility model.
Detailed description of the invention
In order to make the purpose of this utility model, technical scheme and advantage clearly, below with reference to accompanying drawing, the technical solution of the utility model is further elaborated.
Fig. 1 is schematic flow sheet of the present utility model.
Reference numeral is wherein: feed gas compressor 1; Chilldown system 2; Purification system 3; Main heat exchanger 4; Helium knockout tower 5; Helium knockout tower reboiler 6; Nitrogen-rejection column 7; Nitrogen-rejection column 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 condenser/evaporator 15; Pure argon column condenser/evaporator 16; Liquid nitrogen gas-liquid separator 17; Subcooler 18; Decompressor 22; Nitrogen circulation compressor 23; Vavuum pump 24.
Carry out detailed and concrete introduction below by specific embodiment to the utility model, to make better to understand the utility model, but following embodiment does not limit the utility model scope.
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: 700Nm
3/ h
Unstripped gas after being compressed to the required pressure of 4.0MPa (G) in feed gas compressor 1 after chilldown system 2 cools to 10 DEG C, purification system 3 purifying enters fractionating column ice chest after removing water (dew point <-65 DEG C and carbon dioxide content <1ppm of water).In main heat exchanger 4, be cooled to-135 DEG C again after helium knockout tower reboiler 6 is condensed into liquid (because helium is difficult to liquefaction, actual liquefaction rate is 83%), enter helium knockout tower 5.Helium knockout tower number of theoretical plate 10 pieces, obtains raw helium gas (helium purity is 65.82%) from helium knockout tower 5 top after main heat exchanger 4 re-heat is to 17 DEG C, goes out tower supply user.
Bottom helium knockout tower 5, liquid is out depressurized to after 0.15MPa (G) through choke valve and enters nitrogen-rejection column 7.The theoretical cam curve of nitrogen-rejection column 7 is 60 pieces, and most of the nitrogen component is discharged from nitrogen-rejection column 7 top, and the nitrogen amount of discharge is 608Nm
3/ h, nitrogen gas purity is: 99.997%, enters nitrogen circulating system.The mixed liquor of methane and argon gas and trace nitrogen component are extracted out and are entered except methane tower 9 bottom nitrogen-rejection column 7, and methane enters subcooler 18 reclaim cold, main heat exchanger 4 re-heat from except extracting out in liquid form bottom methane tower 9, and give user or its use, methane content is 121Nm
3/ h.From except methane tower 9 top crude argon out contains a small amount of nitrogen, (component is: argon gas: 99.938%; Nitrogen: 0.0615%), enters pure argon column 11, trace nitrogen gas Component seperation, bottom pure argon column 11, obtains satisfactory straight argon liquid.
Cyclic nitrogen tolerance is 4000Nm
3/ h through nitrogen compressor compress 23 laggard enter main heat exchanger 4 cool to-120 DEG C, then enter nitrogen-rejection column reboiler 8 (2757Nm
3/ h), except methane tower reboiler 10 (160Nm
3/ h), pure argon column reboiler 12 (20Nm
3/ h), for the nitrogen-rejection column 7 of correspondence, provide heat except methane tower 9, pure argon column 11.Some (2010Nm after converging from three tower reboilers liquid nitrogen out
3/ h) through subcooler 18 cool-153.6 DEG C be throttled to 0.04MPa (G) again after enter liquid nitrogen gas-liquid separator 17, bottom gas-liquid separator 17, amount of liquid nitrogen is out 947.2Nm
3/ h, enters the condenser/evaporator (13,14,15,16) of four rectifying columns, for rectifying provides liquid as low-temperature receiver.From another gang of nitrogen (1060Nm that heat exchanger 4 is come in
3/ h), from heat exchanger out after enter decompressor 22, expand into-171.8 DEG C, 0.4MPa (G), after expanding, nitrogen enters subcooler 18 and reclaims cold.With the nitrogen after condenser/evaporator gasifies, liquid nitrogen gas-liquid separator 17 top nitrogen out and from the nitrogen of reboiler part out enter subcooler reclaim cold after re-heat to-155.9 DEG C, one is merged into nitrogen-rejection column 7 top nitrogen out, enter main heat exchanger 4 re-heat and enter nitrogen pressure contracting participation circulation after 17 DEG C, if any unnecessary nitrogen, in this emptying.
The utility model is that raw material extracts argon gas with natural gas, and the divided gas flow purity obtained is high, radiationless, and device of the present utility model uses Full distillation technique simultaneously, and continuous operating time is long, and equipment is stablized.
Be described in detail specific embodiment of the utility model above, but it is just as example, the utility model is not restricted to specific embodiment described above.To those skilled in the art, any equivalent modifications that the utility model is carried out and substituting also all among category of the present utility model.Therefore, not departing from the equalization conversion and amendment done under spirit and scope of the present utility model, all should be encompassed in scope of the present utility model.
Claims (4)
1. in a natural gas, extract the device of argon gas, include feed gas compressor (1), chilldown system (2), purification system (3) and main heat exchanger (4) that pipeline connects, it is characterized in that, described device also include helium knockout tower (5), helium knockout tower reboiler (6), nitrogen-rejection column (7), except methane tower (9), pure argon column (11), subcooler (18) and pipeline, valve that above-mentioned parts are connected, natural gas is successively through feed gas compressor (1), after chilldown system (2) and purification system (3), cooling in main heat exchanger (4) also enters helium knockout tower (5) after helium knockout tower reboiler (6) is condensed into liquid, the liquid obtained in helium knockout tower (5) bottom enters nitrogen-rejection column (7) after choke valve step-down, the mixed liquor of methane and argon gas and trace nitrogen component are extracted out from nitrogen-rejection column (7) bottom and are entered except methane tower (9), methane enters subcooler (18) recovery cold from extracting out in liquid form except methane tower (9) bottom, a small amount of nitrogen is contained from except methane tower (9) top crude argon out, enter pure argon column (11) and obtain satisfactory straight argon liquid.
2. in a kind of natural gas according to claim 1, extract the device of argon gas, it is characterized in that, described device also has nitrogen circulation compressor (23), described helium knockout tower (5), nitrogen-rejection column (7), except methane tower (9), pure argon column (11) correspondingly arranges and is connected with helium knockout tower reboiler (6), helium knockout tower condenser/evaporator (13), nitrogen-rejection column reboiler (8), nitrogen-rejection column condenser/evaporator (14), except methane tower reboiler (10), except methane tower condenser/evaporator (15), pure argon column reboiler (12), pure argon column condenser/evaporator (16).
3. extract the device of argon gas in a kind of natural gas according to claim 1, it is characterized in that, described subcooler (18) is also connected with liquid nitrogen gas-liquid separator (17).
4. extract the device of argon gas in a kind of natural gas according to claim 1, it is characterized in that, also include the decompressor (22) be connected with subcooler (18) with described heat exchanger (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520393425.3U CN204787595U (en) | 2015-06-08 | 2015-06-08 | Draw device of argon gas in natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520393425.3U CN204787595U (en) | 2015-06-08 | 2015-06-08 | Draw device of argon gas in natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204787595U true CN204787595U (en) | 2015-11-18 |
Family
ID=54527620
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520393425.3U Withdrawn - After Issue CN204787595U (en) | 2015-06-08 | 2015-06-08 | Draw device of argon gas in natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204787595U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104848654A (en) * | 2015-06-08 | 2015-08-19 | 上海启元空分技术发展股份有限公司 | Method and device for extracting argon from natural gas |
| CN106052301A (en) * | 2016-08-03 | 2016-10-26 | 上海启元气体发展有限公司 | Method for separating <20>Ne from neon |
| CN108413706A (en) * | 2018-05-15 | 2018-08-17 | 瀚沫能源科技（上海）有限公司 | A kind of concentration of krypton xenon and neon helium concentrate integrating apparatus and method containing circulating nitrogen gas |
-
2015
- 2015-06-08 CN CN201520393425.3U patent/CN204787595U/en not_active Withdrawn - After Issue
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104848654A (en) * | 2015-06-08 | 2015-08-19 | 上海启元空分技术发展股份有限公司 | Method and device for extracting argon from natural gas |
| CN104848654B (en) * | 2015-06-08 | 2018-06-29 | 上海启元空分技术发展股份有限公司 | A kind of method and apparatus that argon gas is extracted in natural gas |
| CN106052301A (en) * | 2016-08-03 | 2016-10-26 | 上海启元气体发展有限公司 | Method for separating <20>Ne from neon |
| CN106052301B (en) * | 2016-08-03 | 2019-01-18 | 上海启元气体发展有限公司 | A method of separating 20Ne from neon |
| CN108413706A (en) * | 2018-05-15 | 2018-08-17 | 瀚沫能源科技（上海）有限公司 | A kind of concentration of krypton xenon and neon helium concentrate integrating apparatus and method containing circulating nitrogen gas |
| CN108413706B (en) * | 2018-05-15 | 2023-10-03 | 瀚沫能源科技（上海）有限公司 | Integrated device and method for concentrating krypton and xenon and concentrating neon and helium with circulating nitrogen |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20151118 Effective date of abandoning: 20180629 |
|
| AV01 | Patent right actively abandoned |