CN202216490U - Extraction device for high-purity liquid neon - Google Patents
Extraction device for high-purity liquid neon Download PDFInfo
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- CN202216490U CN202216490U CN2011203498468U CN201120349846U CN202216490U CN 202216490 U CN202216490 U CN 202216490U CN 2011203498468 U CN2011203498468 U CN 2011203498468U CN 201120349846 U CN201120349846 U CN 201120349846U CN 202216490 U CN202216490 U CN 202216490U
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/028—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/028—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases
- F25J3/029—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases of helium
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/30—Helium
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/32—Neon
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/30—Quasi-closed internal or closed external helium refrigeration cycle
Abstract
The utility model discloses an extraction device for high-purity liquid neon, which comprises a condensation and adsorption system for extracting the high-purity liquid neon and a closed refrigeration cycle system of a double-helium expansion turbine for supplying cooling capacity, wherein the condensation and adsorption system cools feed gas after the feed gas is pressurized, neon-helium mixed gas can be obtained after nitrogen, oxygen and the like in the feed gas can be removed by adopting a low-temperature condensation method and a low-temperature adsorption method, and then the neon-helium mixed gas continues to be cooled so as to obtain the high-purity liquid neon by adopting a low-temperature distillation method. The closed refrigeration cycle system adopts the double-helium expansion turbine to meet the requirement on the cooling capacity in the extraction process of the liquid neon.
Description
Technical field
The utility model relates to the device that a kind of gas separates, and specifically, the utility model relates to a kind of by the device that extracts high-purity fluid neon in the He-Ne mist.Relate in particular to the low pressure kind of refrigeration cycle of forming by a kind of miniature high rotating speed gas bearing helium turbo-expander, the device of the cold that needs is provided for separation process.
Background technology
Neon is a kind of inert gas, and its content in air is merely 18.18 * 10
-6Yet along with development of science and technology, it is used for industrial every field as important energy in a large number.As in electronics industry, neon can be used for the filling medium of neon light and high pressure neon lamp, counting tube etc.; It can be used for laser technology; Because of liquid neon has advantages such as boiling point is low, its low temperature cold source that can be used as between 26 ~ 40K uses; Neon also can be used for study of high energy physics.
In the preparation technology of neon, adopt empty point-score to prepare neon mostly, it comprises that the employing crude Ne-He column extracts a spot of thick ne-He mixture continuously earlier.Contain hydrogen this moment in the thick ne-He mixture volume fraction is 2～5%; Afterwards, in thick ne-He mixture, add a certain amount of oxygen, make oxygen and hydrogen carry out chemical reaction fully and generate water, carry out dehydrogenation and handle, and the volume fraction of each component is generally neon 51%, helium 15%, nitrogen 32.5%, oxygen 1.5% in the thick ne-He mixture after the dehydrogenation.And afterwards, the thick ne-He mixture after the dehydrogenation can be used ne-He mixture gas compressor, drier, and device such as cooler, concentrates after the accumulation some and denitrogenates.When the temperature of removing nitrogen equipment at 65K (making the evaporating pressure of liquid nitrogen reach 0.12bar) with vavuum pump when slightly the condensing pressure of ne-He mixture is 30bar; Nitrogen and oxygen in the thick ne-He mixture are condensed, and remaining trace nitrogen and oxygen carry out adsorbing and removing in the gas phase that is not condensed under uniform temp.Obtain like this that the neon volume fraction is about 78%, the ne-He mixture body of helium about 22%.Carrying out neon helium afterwards again separates.
In traditional separating in the technology of neon helium, comprised rectifying column, gas-liquid separator and the condenser system of cold is provided for whole technology by thick ne-He mixture body.Be low-temperature receiver generally in the condenser system in early days, under liquid hydrogen temperature, the temperature of ne-He mixture be reduced to the three phase point temperature near neon, make neon liquefaction to adopt liquid hydrogen.Thereby reach the purpose that neon helium separates.Complexity and danger in view of liquid hydrogen production.Modern technologies are to adopt ne-He mixture high pressure (200bar) the second throttle refrigeration of band liquid nitrogen forecooler to make neon liquefaction, are the defective that low-temperature receiver exists thereby overcome liquid hydrogen.As, U.S. Patent Publication US2010/0221168A1; In the extraction equipment of the liquid neon of China publication number CN101530717A, all adopt the liquid nitrogen condensation evaporimeter required cold to be provided, thereby make neon liquefaction to system.The method that yet this employing liquid nitrogen is a low-temperature receiver prepares neon at first need consume the liquid nitrogen cold that the external world provides, and secondly neon helium separation equipment belongs to high-tension apparatus, brings unsafe hidden danger for the manufacturing and the operation of equipment.
The utility model content
The utility model provides a kind of extraction element of high-purity fluid neon; It is to employing liquid hydrogen in the existing high-purity neon extraction element or liquid nitrogen is the deficiency of low-temperature receiver; It adopts two helium turbo-expanders to realize whole neon leaching process mesolow kind of refrigeration cycle; Cold is provided, thereby extracts highly purified liquid neon.
The extraction element of the utility model high-purity fluid neon, realize its purpose through following technical scheme:
A kind of high-purity fluid neon extraction element wherein, comprises condensation adsorption system and closed cryogenic cycles system; Said condensation adsorption system comprises I level heat exchanger, II level heat exchanger, I level gas-liquid separator, II level gas-liquid separator, absorber and rectifying column;
The material inlet of said I level heat exchanger is connected with the unstrpped gas pipeline;
The material outlet of said I level heat exchanger is connected with I level gas-liquid separator material inlet, the gas vent of I level gas-liquid separator is connected with the absorber material inlet, and the material outlet of absorber is connected with the material inlet of II level heat exchanger, the material outlet of II level heat exchanger is connected with the material inlet of II level gas-liquid separator, the liquid outlet of II level gas-liquid separator is connected with the material inlet of rectifying column;
Said rectifying Tata still place is provided with high-purity fluid neon and extracts mouth;
Said closed cryogenic cycles system comprises I level helium turbo-expander and II level helium turbo-expander and circulated helium pipeline;
Said circulated helium pipeline comprises admission line and backflows pipeline; Said admission line is connected II level helium turbo-expander through behind I level heat exchanger and the II level heat exchanger after through the compressor that is used to collect compressed helium successively, and between I level heat exchanger and II level heat exchanger, is connected I level helium turbo-expander; The said pipeline that backflows is risen by said II level helium turbo-expander, through returning said compressor behind II level heat exchanger and the I level heat exchanger.
Above-mentioned high-purity fluid neon extraction element, wherein, said condensation adsorption system also comprises thick ne-He mixture gas compressor and gas-drying apparatus; Said unstrpped gas pipeline is connected with the material inlet of said I level heat exchanger with gas-drying apparatus through thick ne-He mixture gas compressor successively afterwards.
Above-mentioned high-purity fluid neon extraction element, wherein, said rectifying column is provided with the neon extraction opening, and said neon extraction opening is connected with the import of said thick ne-He mixture gas compressor.
Above-mentioned high-purity fluid neon extraction element, wherein, said condensation adsorption system also comprises III level gas-liquid separator, said III level separator material inlet is connected with the liquid outlet of said I level gas-liquid separator; And the gas vent of said III level separator is connected with the import of said thick ne-He mixture gas compressor.
Above-mentioned high-purity fluid neon extraction element wherein, is equipped with the choke valve that is used to regulate pressure between said II level gas-liquid separator and the rectifying column and between III level separator and the said I level gas-liquid separator.
Above-mentioned high-purity fluid neon extraction element, wherein, the liquid outlet of said III level separator is through pipeline emptying behind said I level heat exchanger.
Above-mentioned high-purity fluid neon extraction element, wherein, said I level heat exchanger, II level heat exchanger, I level gas-liquid separator, II level gas-liquid separator, III level separator, rectifying column and gas absorber all are arranged in the multilayer heat insulation vacuum tank.
Above-mentioned high-purity fluid neon extraction element, wherein, the gas vent of said II level gas-liquid separator is connected with outside helium gathering-device after through said II level heat exchanger, I level heat exchanger.
In the extraction element of the utility model high-purity fluid neon, whole process using scattered control system (DCS system), thereby the monitoring of concentration of component in the device various piece of realization the utility model, and the setting of device various piece working condition is regulated.
The utility model is compared with conventional art and is had the following advantages:
1) the utility model adopts the closed cryogenic cycles system of two helium turbo-expanders, in the liquid neon leaching process cold being provided.
2) adopt the utility model when extracting high-purity liquid neon, to reclaim raw helium gas.
3) the utility model process structure is simple, and easy operating, control in use is applicable to high-purity neon industry large-scale production demand.
Description of drawings
Fig. 1 is the structural representation of the utility model,
Among the figure, 1 for thick ne-He mixture compressor, 2 for 4A mole sieve drier, 3 and 8 be heat exchanger, 4,6 and 9 be gas-liquid separator, 5 and 10 be choke valve, 7 for absorber, 11 for rectifying column, 13 for helium compressor, 14 and 15 be the helium turbo-expander, 16 for vavuum pump, 17 for the multilayer heat insulation vacuum tank.
The specific embodiment
A kind of high-purity fluid neon of the utility model extraction element comprises the condensation adsorption system of purification high-purity fluid neon and the closed cryogenic cycles system that is used to provide cold.The ne-He mixture body of the utility model after can dehydrogenation is unstrpped gas (volume fraction of each component is generally neon 51%, helium 15%, nitrogen 32.5%, oxygen 1.5% in the thick ne-He mixture after the dehydrogenation), the highly purified liquid neon of therefrom purifying.
Embodiment 1:
As shown in Figure 1, said condensation adsorption system comprises that said condensation adsorption system also comprises thick ne-He mixture gas compressor 1,4A mole sieve drier 2, I level heat exchanger 3, II level heat exchanger 8, I level gas-liquid separator 4, II level gas-liquid separator 9 and rectifying column 11.Between said gas-liquid separator 9 and rectifying column 11, be provided with the choke valve 10 that is used to regulate fluid pressure.
Said thick ne-He mixture gas compressor 1 is connected with outside unstrpped gas pipeline; Be used to feed the ne-He mixture body after the dehydrogenation; Said crude Ne-He body hybrid compressor 1 is connected with the material inlet of said gas-drying apparatus 2 and said I level heat exchanger 3 successively; The ne-He mixture body is pressurized to about 30bar through said thick ne-He mixture compressor 1 after the dehydrogenation like this; And after 4A mole sieve drier 2 dryings remove moisture, get into along pipeline 18 and in heat exchanger 3, to be condensed to about 65K, this moment, the nitrogen and the oxygen (about nitrogen and oxygen more than 95%) of the overwhelming majority were condensed.
The material outlet of said I level heat exchanger 3 is connected with I level gas-liquid separator 4 material inlets; Condensed oxygen and nitrogen are sent in the said I level gas-liquid separator 4; The gas vent of said I level gas-liquid separator is connected with the absorber material inlet, and the material outlet of absorber is connected with the material inlet of II level heat exchanger; The material outlet of II level heat exchanger 8 is connected with the material inlet of II level gas-liquid separator 9; The liquid outlet of II level gas-liquid separator 9 is connected with the material inlet of rectifying column 11 again, wherein, is provided with choke valve 10 between said II level gas-liquid separator 9 and the said rectifying column 11.And the gas vent of said II level gas-liquid separator 9 is connected with outside helium gathering-device through said II level heat exchanger 8, I level heat exchanger 3 backs.After condensed nitrogen and oxygen get into said I level gas-liquid separator 4 in by heat exchanger 3, be separated into the liquid and gas component; Gaseous component (wherein the neon volume fraction is about 76.8%, helium 22%) obtains pure ne-He mixture after pipeline 21 gets into silica gel absorption devices 7, its neon volume fraction is 77.7%, helium 22.3%.
Pure ne-He mixture is cooled to (wherein 97% neon is condensed) behind the 26K through gas exchanger 8, and in said II level gas-liquid separator 9, carries out the gas-liquid separation of II level; The liquid phase component that obtains (neon volume fraction be 98%, helium 1.9%) gets into rectifying column 11 through choke valve 10 throttling expansions to 1.7bar.And after pipeline 22 is successively through said I level heat exchanger 3, II level heat exchanger 8, get into the helium gathering-device by the gas component (wherein the volume fraction of helium reaches about 90%) that obtains in the said II level gas-liquid separator 9, be used for high-purity helium and purify or do his in addition and use.Can be the DX type laboratory stainless steel cloth structured packing that filling Switzerland Suhl longevity company makes in the described rectifying column, the rectifying column reboiler adopts the electrical heating of power regulating eqiupment control to carry out the heat transmission, correctly controls the thermic load of reboiler.
Neon and helium rectifying separation in rectifying column 11, and, enter liquid neon storage facility along pipeline 23 by obtaining highly purified liquid neon (the neon volume fraction is greater than 99.999%) at the bottom of the tower.
Said closed cryogenic cycles system comprises that I level helium turbo-expander 14 is with II level helium turbo-expander 15 and the circulated helium pipeline that is used to be connected each device.The bearing of described helium turbo-expander adopts the gas hydrostatic and hydrodynamic bearing.The helium turbo-expander adopts the blower fan braking, and the medium of blower fan is a helium.Among the figure, and two described helium turbo- expanders 14 and 15 all adopt chilled water unit 12, are used to realize the cold exchange of said helium turbo-expander.
Said circulated helium pipeline comprises admission line and backflows pipeline; Said admission line one end connects one and is used to compress the compressor 13 of collecting helium; And by 13 on said compressor; Be connected II level helium turbo-expander 15 through behind I level heat exchanger 3 and the II level heat exchanger 8 successively, and between I level heat exchanger 3 and II level heat exchanger 8, be connected I level helium turbo-expander 14; And the said pipeline that backflows successively through returning compressor 13 inlets behind II level heat exchanger 8 and the I level heat exchanger 3, is realized circulated helium by 15 of said II level helium turbo-expanders.During work; Helium is compressed to 10bar through admission line through said compressor 13, is cooled to back entering helium turbo-expander 14 about 83K along pipeline 24 through heat exchanger 3, and helium is expanded to 3.5bar, temperature is reduced to 62K; Get into heat exchanger 8 along pipeline 25 then, carry out exchange heat; Feed helium turbo-expander 15 afterwards, helium is expanded to 1.3bar, and after temperature was reduced to 24K, the helium after the expansion returned helium compressor 13 after pipeline 26 feeds heat exchanger 8 and 3 re-heats once more, carries out pressurized circulation and uses.
Embodiment 2:
On the basis of said embodiment 1, said condensation adsorption system is added an III level gas-liquid separator 6, and said III level gas-liquid separator 6 material inlets are connected with the liquid outlet of said I level gas-liquid separator 4.Wherein, separating the liquid phase component that obtains by said I level gas-liquid separator 4 can carry out the gas-liquid separation of III level, and the gas vent of said III level separator 6 is connected with said thick ne-He mixture gas compressor 1 import through after valve 5 throttlings are to the 1.5bar.Gaseous component (the neon volume fraction is about 89%), the gaseous component that obtains also returns in the said thick ne-He mixture gas compressor 1 recycle along pipeline 20.
And the liquid phase component that obtains in the said III level separator 6 gets into said heat exchanger 3 re-heats through pipeline 19 (volume fraction of neon is about 0.5%, and all the other major parts are nitrogen), carries out entering atmosphere after exchange heat reaches normal temperature.
And also be provided with the neon extraction opening on the said rectifying column 11; Said neon extraction opening is connected with 1 import of said crude Ne-He body hybrid compressor; The gaseous component that in rectifying column 11, obtains (the neon volume fraction is about 98.9%, helium be 1.1%) returns in the said thick ne-He mixture gas compressor 1 recycle.
The gas vent of said II level gas-liquid separator 9 is connected with outside helium gathering-device through said II level heat exchanger 8, I level heat exchanger 3 backs.Separating the gaseous component (wherein the helium volume fraction is about 90%) that obtains collects after pipeline 22 process heat exchangers 3 and 8 re-heats.Wherein, the concentration of helium is higher, can be used as the unstrpped gas of follow-up helium extraction process or is used for other, and its economic worth is higher.
Wherein, said I level heat exchanger 3, II level heat exchanger 8, I level gas-liquid separator 4, II level gas-liquid separator 9, III level separator 6, rectifying column 11 all are arranged in the multilayer heat insulation vacuum tank 17 with the pipeline etc. that is connected between gas absorber 7 and the said equipment.Described multilayer heat insulation vacuum tank 17, vacuum requires 1 * 10
-4About mbar, and leak rate requires to reach 1 * 10
-7MbarL/s.Effectively reduce duration of work like this, said apparatus and extraneous exchange heat.
More than the specific embodiment of the utility model is described in detail, but it is just as example, the utility model is not restricted to the specific embodiment of above description.To those skilled in the art, any equivalent modifications that the utility model is carried out with substitute also all among the category of the utility model.Therefore, impartial conversion and the modification under spirit that does not break away from the utility model and scope, done all should be encompassed in the scope of the utility model.
Claims (8)
1. a high-purity fluid neon extraction element is characterized in that, comprises condensation adsorption system and closed cryogenic cycles system; Said condensation adsorption system comprises I level heat exchanger, II level heat exchanger, I level gas-liquid separator, II level gas-liquid separator, absorber and rectifying column;
The material inlet of said I level heat exchanger is connected with the unstrpped gas pipeline;
The material outlet of said I level heat exchanger is connected with I level gas-liquid separator material inlet, the gas vent of I level gas-liquid separator is connected with the absorber material inlet, and the material outlet of absorber is connected with the material inlet of II level heat exchanger, the material outlet of II level heat exchanger is connected with the material inlet of II level gas-liquid separator, the liquid outlet of II level gas-liquid separator is connected with the material inlet of rectifying column;
Said rectifying Tata still place is provided with high-purity fluid neon and extracts mouth;
Said closed cryogenic cycles system comprises I level helium turbo-expander and II level helium turbo-expander and circulated helium pipeline;
Said circulated helium pipeline comprises admission line and backflows pipeline; Said admission line is connected II level helium turbo-expander through behind I level heat exchanger and the II level heat exchanger after through the compressor that is used to collect compressed helium successively, and between I level heat exchanger and II level heat exchanger, is connected I level helium turbo-expander; The said pipeline that backflows is risen by said II level helium turbo-expander, through returning said compressor behind II level heat exchanger and the I level heat exchanger.
2. high-purity fluid neon extraction element according to claim 1 is characterized in that said condensation adsorption system also comprises thick ne-He mixture gas compressor and gas-drying apparatus; Said unstrpped gas pipeline is connected with the material inlet of said I level heat exchanger with gas-drying apparatus through thick ne-He mixture gas compressor successively afterwards.
3. high-purity fluid neon extraction element according to claim 2 is characterized in that said rectifying column is provided with the neon extraction opening, and said neon extraction opening is connected with the import of said thick ne-He mixture gas compressor.
4. high-purity fluid neon extraction element according to claim 2 is characterized in that said condensation adsorption system also comprises III level gas-liquid separator, and said III level separator material inlet is connected with the liquid outlet of said I level gas-liquid separator; And the gas vent of said III level separator is connected with the import of said thick ne-He mixture gas compressor.
5. high-purity fluid neon extraction element according to claim 4 is characterized in that, is equipped with the choke valve that is used to regulate pressure between said II level gas-liquid separator and the rectifying column and between III level separator and the said I level gas-liquid separator.
6. high-purity fluid neon extraction element according to claim 4 is characterized in that, the liquid outlet of said III level separator is through pipeline emptying behind said I level heat exchanger.
7. high-purity fluid neon extraction element according to claim 6; It is characterized in that said I level heat exchanger, II level heat exchanger, I level gas-liquid separator, II level gas-liquid separator, III level separator, rectifying column and gas absorber all are arranged in the multilayer heat insulation vacuum tank.
8. high-purity fluid neon extraction element according to claim 1 is characterized in that, the gas vent of said II level gas-liquid separator is connected with outside helium gathering-device after through said II level heat exchanger, I level heat exchanger.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011203498468U CN202216490U (en) | 2011-09-19 | 2011-09-19 | Extraction device for high-purity liquid neon |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011203498468U CN202216490U (en) | 2011-09-19 | 2011-09-19 | Extraction device for high-purity liquid neon |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105987580A (en) * | 2016-02-03 | 2016-10-05 | 安徽万瑞冷电科技有限公司 | Neon and helium rare gas separating and refining process method with refrigerator as cold source |
| CN107917578A (en) * | 2017-11-13 | 2018-04-17 | 益通天然气股份有限公司 | A kind of mixed-refrigerant cycle liquefied natural gas self-purifying system |
| CN108373144A (en) * | 2018-05-24 | 2018-08-07 | 浙江智海化工设备工程有限公司 | A kind of thick neon helium is refined to remove hydrogen system |
| CN109442868A (en) * | 2018-10-26 | 2019-03-08 | 中船重工鹏力（南京）超低温技术有限公司 | A method of removing deoxygenation nitrogen separating-purifying neon helium |
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2011
- 2011-09-19 CN CN2011203498468U patent/CN202216490U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105987580A (en) * | 2016-02-03 | 2016-10-05 | 安徽万瑞冷电科技有限公司 | Neon and helium rare gas separating and refining process method with refrigerator as cold source |
| CN107917578A (en) * | 2017-11-13 | 2018-04-17 | 益通天然气股份有限公司 | A kind of mixed-refrigerant cycle liquefied natural gas self-purifying system |
| CN107917578B (en) * | 2017-11-13 | 2019-10-25 | 益通天然气股份有限公司 | A kind of mixed-refrigerant cycle liquefied natural gas self-purifying system |
| CN108373144A (en) * | 2018-05-24 | 2018-08-07 | 浙江智海化工设备工程有限公司 | A kind of thick neon helium is refined to remove hydrogen system |
| CN109442868A (en) * | 2018-10-26 | 2019-03-08 | 中船重工鹏力（南京）超低温技术有限公司 | A method of removing deoxygenation nitrogen separating-purifying neon helium |
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