CN202216489U - Containing CO2Device for separating krypton-xenon concentrate from methane - Google Patents
Containing CO2Device for separating krypton-xenon concentrate from methane Download PDFInfo
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- CN202216489U CN202216489U CN201120259308XU CN201120259308U CN202216489U CN 202216489 U CN202216489 U CN 202216489U CN 201120259308X U CN201120259308X U CN 201120259308XU CN 201120259308 U CN201120259308 U CN 201120259308U CN 202216489 U CN202216489 U CN 202216489U
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 40
- PDEXVOWZLSWEJB-UHFFFAOYSA-N krypton xenon Chemical compound [Kr].[Xe] PDEXVOWZLSWEJB-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000012141 concentrate Substances 0.000 title claims abstract description 15
- 239000012530 fluid Substances 0.000 claims description 72
- 238000012856 packing Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 5
- 239000004744 fabric Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 8
- 229910052743 krypton Inorganic materials 0.000 abstract description 8
- 229910052724 xenon Inorganic materials 0.000 abstract description 8
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 abstract description 7
- 238000000926 separation method Methods 0.000 abstract description 7
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 abstract description 7
- 238000006243 chemical reaction Methods 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract description 4
- 239000003463 adsorbent Substances 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000011031 large-scale manufacturing process Methods 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 description 12
- 239000001569 carbon dioxide Substances 0.000 description 9
- 239000007788 liquid Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000002808 molecular sieve Substances 0.000 description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 101100008049 Caenorhabditis elegans cut-5 gene Proteins 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000003727 cerebral blood flow Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000004087 circulation Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 239000003870 refractory metal Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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Abstract
The utility model relates to a device for containing CO2The device for separating the krypton-xenon concentrate from the methane comprises three rectifying towers, and each rectifying tower is internally provided with a reboiler. The utility model can separate and purify krypton and xenon by low-temperature rectification, thereby avoiding the requirements of using catalyst and adsorbent and high-temperature reaction in the prior separation technology; the krypton and xenon extraction rate is high, the cost is low, and continuous large-scale production can be realized.
Description
Technical field
The utility model relates to a kind of air-separating plant, relates in particular to a kind of CO of containing
2Separator with the krypton-xenon concentrate of methane.
Background technology
Krypton, xenon are rare gas, and content is extremely low in the atmosphere, are widely used in electronics industry, electric light source industry, also are used for gas laser and plasma jet.For example, the bulb that fills with pure krypton, xenon with compare with the argon filling bulb of power have the luminance height, advantages such as volume is little, the life-span is long, power saving, be used to make mine lamp in a large number; Because its transmissivity is high especially, the irradiation light and the runway indicator lamp of cross-country battlebus in the time of can being used to make night fighting, the health care aspect is used for measure cerebral blood flow, and its isotope can be used as the tracing agent; Radiokrypton can be used for the leak detection of closed container and the METHOD FOR CONTINUOUS DETERMINATION of material thickness, also can be made into the atomic lamp that does not need electric energy; 2500 ℃ of high temperature be can generate behind the xenon lamp concave surface optically focused and welding or cutting refractory metal such as titanium, molybdenum etc. can be used for.
Air separation is one of important method of preparation krypton, xenon; But, can in krypton, xenon concentrate, bring in the air separation process a large amount of carbon dioxide and hydrocarbon (being mainly methane), especially along with the rising of krypton-xenon concentrate concentration; Hydrocarbon concentration also can increase; In case too high levels can be hypersaturated state and separate out, form explosive.The carbon dioxide in the krypton-xenon concentrate commonly used at present and the separation method of methane comprise and use catalysis method and absorption method that these methods normally will make oxygen and methane carry out chemical reaction under 450 ~ 500 ℃ high temperature, and produce carbon dioxide and water; And then use molecular sieve adsorber to deviate from carbon dioxide and water at normal temperatures; Need carry out hot reactivation after molecular sieve adsorption is saturated.Like Li Xiangzai " 4000m
3/ h empty branch krypton xenon extraction element case study and rectification " (metallurgical power, 2010, (6): 63 ~ 65) in the device of disclosed removal hydrocarbon, carbon dioxide, extraction krypton xenon; Comprise the methane system that removes, eight big systems such as molecular sieve adsorption system form, with poor krypton liquid gasification; 480 ℃ of electrical heating to catalytic reaction temperature, methane reacts under catalyst action with oxygen in removing the methane catalyst oven, produces carbon dioxide and water; Send into molecular sieve adsorber after the cooling and remove carbon dioxide and water simultaneously; Molecular sieve adsorber is at least two, a use, another regeneration.
But this equipment and method have obvious defects, as:
1) because exothermic heat of reaction, if methane content is too high in the krypton xenon mixture, then during a catalytic process, the catalyst converter outlet temperature can surpass the serviceability temperature of catalyst, promptly will carry out repeatedly catalysis, and flow process is complicated, and energy consumption is high and influence the recovery rate of krypton xenon mixture;
2) used non-renewable adsorbent or catalyst, service life is limited; And generally use palladium catalyst, cost an arm and a leg;
3) the part krypton-xenon concentrate after the molecular sieve adsorber pressure release is accomplished can't get into lower procedure, perhaps emptying or recovery.If emptying then influences the recovery rate of krypton xenon greatly.If reclaim again, it is complicated then to reclaim technology, increases equipment investment and maintenance cost.
The utility model content
The utility model provides the separator of the krypton-xenon concentrate of a kind of CO2 of containing and methane; Comprise three rectifying columns and cryogenic fluid pipe-line system; Can remove carbon dioxide and methane through the mode of cryogenic rectification, overcome shortcoming and defect such as the conventional art separation costs is high, krypton xenon productive rate is low.
The utility model contains the separator of the krypton-xenon concentrate of CO2 and methane; Comprise first rectifying column, second rectifying column and the 3rd rectifying column; The outlet of the first rectifying column overhead fraction links to each other with second rectifying column inlet, and the outlet of the second rectifying column tower bottom distillate links to each other with the 3rd rectifying column inlet; Be equipped with reboiler at the bottom of three rectifying Tatas.
Three rectifying column inlets are preferably placed at the middle part of rectifying column.
Reboiler adopts the electric heater of power regulating eqiupment control to carry out the heat transmission, correctly controls the thermic load of reboiler.
A kind of preferred implementation according to the said separator of the utility model; Wherein, Also comprise cryogenic fluid pipe-line system and cold switching equipment, said cryogenic fluid pipe-line system comprises fluid source conveyance conduit and the cryogen pipeline that connects through the cold switching equipment.
Condenser/evaporator is all also installed at said three rectifying column tops, said cryogen pipeline be provided with three outlets respectively with said three rectifying columns in condenser/evaporator inlet be connected.
Also comprise fluid return line, said fluid return line connects said condenser/evaporator outlet.
According to the further preferred implementation of the above-mentioned separator of the utility model, wherein, also comprise the normal temperature fluid line, the normal temperature fluid line is respectively equipped with three outlets, is provided with three outlets with said cryogen pipeline respectively and is communicated with.
Said normal temperature fluid line entrance can also communication of fluid source conveyance conduit.
According to another further preferred implementation of the above-mentioned separator of the utility model, wherein, said fluid return line is communicated with said cold switching equipment.
According to the further preferred implementation of the above-mentioned separator of the utility model, wherein, said fluid reflux tube is communicated with said cold switching equipment through after the decompressor.
According to the third further preferred implementation of the above-mentioned separator of the utility model, said cold switching equipment also is provided with the cryogenic fluid pipeline.
The above-mentioned separator of the utility model also comprises auxiliary heat exchanger, and the fluid source conveyance conduit is successively through said cold switching equipment and said auxiliary heat exchanger; Said cryogenic fluid pipeline is successively through said secondary heat exchanger and said cold switching equipment
The utility model separator; Wherein, All fill the stainless steel cloth structured packing in three rectifying columns; Be respectively equipped with a plurality of temperature elements at the different up and down section faces of packing layer, the multivariable arithmetic element that the data that each temperature element is obtained are all sent into the DCS system is carried out logical operation and is drawn a mean temperature, and according to the valve opening of this temperature control tower top distillate; Said temperature measuring unit connects the multivariable arithmetic element of DCS system through data wire.
Temperature element described in every rectifying column is provided with 5 ~ 15.
The utility model separator can be realized the separation and the purification of krypton-xenon concentrate through the mode of cryogenic rectification, need not high temperature and expensive catalyst and adsorbent, compares with existing krypton xenon extraction element, and recovery rate is higher, but also can realize CO
2Recovery with methane.
Description of drawings
Fig. 1 is the utility model separator embodiment 1 structural representation;
Fig. 2 is the utility model separator embodiment 2 structural representations;
Fig. 3 is the utility model separator embodiment 3 structural representations.
The specific embodiment
The utility model provide a kind of be used for separating contain CO
2With the device of methane krypton-xenon concentrate, adopt three rectifying column series connection, realize the separation and the purifying of krypton xenon through the mode of cryogenic rectification.
See figures.1.and.2 below, the utility model separator is carried out detailed introduction and description through specific embodiment, so that better understand the utility model content, but following embodiment does not limit the novel scope of this practicality.
With reference to Fig. 1, the utility model contains CO
2Separator with the methane krypton-xenon concentrate; Comprise first rectifying column 2, second rectifying column 3 and the 3rd rectifying column 4; The outlet of first rectifying column, 2 overhead fractions is communicated with the inlet of second rectifying column, 3 medium positions, and the outlet of second rectifying column, 3 tower bottom distillates connects the inlet of the 3rd rectifying column 4 medium positions.
Heater (reboiler) all is installed in three rectifying columns, can be the heating of electric heater or fluid, and among Fig. 1, mark 16 is for carrying out the fluid or the electric heater of indirect at the bottom of the tower.
All fill the stainless steel cloth structured packing in three rectifying columns; Be respectively equipped with a plurality of temperature elements at the different up and down section faces of packing layer; The multivariable arithmetic element that the data that each temperature element is obtained are all sent into the DCS system is carried out logical operation and is drawn a mean temperature, and according to the valve opening of this temperature control tower top distillate.
Temperature element described in every rectifying column is provided with 5-15.
The raw material krypton-xenon concentrate 1 that contains carbon dioxide and methane is sent into the middle part of first rectifying column 2; 0.8 carry out rectifying under ℃ condition of ~ 1.2MPa and-100 ~-37; High-boiling-point impurity CO2 accumulates at the bottom of the tower of this tower along with liquid 6 is discharged from, and the cut 5 that obtains at cat head is sent into the middle part of second rectifying column 3, carries out rectifying under ℃ condition of 0.3 ~ 0.5MPa and-145 ~-120; Methane has mainly concentrated in the gas 7 and has discharged, and Kr, Xe etc. just has been collected at and has sent into the 3rd rectifying column 4 in the liquid 8.
Liquid 8 is incorporated in the tower 4, and rectifying under ℃ condition of 0.2 ~ 0.4MPa and-135 ~-80 obtains liquid 10 at the bottom of tower, and its key component is Xe, is not less than 99.99% through detecting molar content; Obtain fluid 9 at cat head, its key component is Kr, and through detecting, molar content is not less than 99.99%.
On the basis of embodiment 1, the utility model separator also comprises cryogenic fluid pipe-line system and cold switching equipment 17, and said cryogenic fluid pipe-line system comprises the fluid source conveyance conduit 11 and cryogen pipeline 12 that connects through cold switching equipment 17; Be provided with fluid reflux tube 14 in addition.
Three rectifying column tops are equipped with condenser/evaporator, and cryogen pipeline 12 is provided with three outlets and links to each other with the condenser/evaporator inlet at three rectifying column tops respectively, and the condenser/evaporator outlet links to each other with fluid reflux tube 14.
In the distillation process; Fluid source conveyance conduit 11 is sent fluid into cold switching equipment 17 (like heat exchanger) refrigeration and is become cryogen; The low temperature circulation is sent into condenser/evaporator by cryogen pipeline 12; In condenser/evaporator, carry out exchange heat with overhead fraction, the overhead fraction cooling, the cryogen after the heat exchange is seen off through fluid reflux tube 14.
In order better to control the cryogen temperature; In the present embodiment, can also be provided with normal temperature fluid hose 19, normal temperature fluid hose 19 be provided with three outlets; And be communicated with three outlets of cryogen pipe 12 respectively; The normal temperature fluid mixes the back and gets into condenser/evaporator with cryogen, through regulating the flow velocity and the flow of normal temperature fluid and cryogen, can realize the accurate control to sink temperature.
The inlet of normal temperature fluid hose 19 can be communicated with fluid source conveyance conduit 11, and the fluid in the fluid source conveyance conduit 11 is divided into two strands, and one gets into normal temperature fluid hose 19, and another strand gets into cold switching equipment 17.
Cold source in the cold switching equipment 17 can be liquid nitrogen or other cold-producing mediums; In the case; Cold switching equipment 17 also is provided with cryogenic fluid pipeline 15, and liquid nitrogen is sent into cold switching equipment 17 by cryogenic fluid pipeline 15, and the fluid of sending into fluid source conveyance conduit 11 carries out the cold exchange.
Generally speaking; Can be lower than fluid through the cryogenic fluid temperature behind the condenser/evaporator without condenser/evaporator 17 coolings; For this reason, in the present embodiment, can also fluid return line 14 ports of export be carried out the cold exchange through condenser/evaporator 17 and fluid source conveyance conduit 11 interior fluids.In the case, can also be provided with auxiliary heat exchanger 18 in the present embodiment, fluid freezes after fluid source conveyance conduit 11 is through cold switching equipment 17, auxiliary heat exchanger 18 and becomes cryogen, gets into cryogenic flow and threads a pipe 12; Cryogenic fluid pipeline 15 passes through cold switching equipment 17 through auxiliary heat exchanger 18 earlier again; Temperature descended after fluid in the fluid source conveyance conduit 11 freezed through cold switching equipment 17 for the first time, in auxiliary heat exchanger 15, carried out the cold exchange with the lower liquid nitrogen of temperature then.
With reference to Fig. 3, on the basis of embodiment 1, according to each fluid line, different with embodiment 2 is in the present embodiment, not use cold-producing mediums such as liquid nitrogen, but the fluid in the fluid return line 14 is carried out swell refrigeration according to embodiment 2 said modes.
For this reason, in the present embodiment, fluid return line 14 ports of export are provided with decompressor 151, and fluid return line 14 is through getting into cold switching equipment 17 after the decompressor 15.
Fluid in the fluid return line 14 is sent into swell refrigeration in the decompressor 15, becomes low-temperature receiver, sends into cold switching equipment 17 then, carries out the cold exchange with fluid source conveyance conduit 11 interior fluids.
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 (10)
1. one kind contains CO
2Separator with the krypton-xenon concentrate of methane is characterized in that, comprises three rectifying columns; The outlet of the first rectifying column overhead fraction links to each other with second rectifying column inlet, and the outlet of the second rectifying column tower bottom distillate links to each other with the 3rd rectifying column inlet; Be equipped with reboiler at the bottom of three rectifying Tatas.
2. separator according to claim 1 is characterized in that,
Also comprise cryogenic fluid pipe-line system and cold switching equipment, said cryogenic fluid pipe-line system comprises fluid source conveyance conduit and the cryogen pipeline that connects through the cold switching equipment;
Condenser/evaporator is all also installed at said three rectifying column tops, said cryogen pipeline be provided with three outlets respectively with said three rectifying columns in condenser/evaporator inlet be connected.
3. separator according to claim 2 is characterized in that,
Also comprise the normal temperature fluid line, the normal temperature fluid line is respectively equipped with three outlets, is provided with three outlets with said cryogen pipeline respectively and is communicated with;
Also comprise fluid return line, said fluid return line connects said condenser/evaporator outlet.
4. separator according to claim 3 is characterized in that, said normal temperature fluid line entrance communication of fluid source conveyance conduit.
5. separator according to claim 3 is characterized in that, said fluid return line is communicated with said cold switching equipment.
6. separator according to claim 5 is characterized in that, said cold switching equipment also is provided with the cryogenic fluid pipeline.
7. separator according to claim 6 is characterized in that, also comprises auxiliary heat exchanger, and the fluid source conveyance conduit is successively through said cold switching equipment and said auxiliary heat exchanger; Said cryogenic fluid pipeline is successively through said secondary heat exchanger and said cold switching equipment.
8. separator according to claim 5 is characterized in that, said fluid reflux tube is communicated with said cold switching equipment through after the decompressor.
9. require any described separator in 1 ~ 8 according to aforesaid right, it is characterized in that, all fill the stainless steel cloth structured packing in three rectifying columns, be respectively equipped with a plurality of temperature elements at the different up and down section faces of packing layer; Said temperature measuring unit connects the multivariable arithmetic element of DCS system through data wire.
10. separator according to claim 9 is characterized in that, said temperature element is made as 5 ~ 15.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120259308XU CN202216489U (en) | 2011-07-21 | 2011-07-21 | Containing CO2Device for separating krypton-xenon concentrate from methane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120259308XU CN202216489U (en) | 2011-07-21 | 2011-07-21 | Containing CO2Device for separating krypton-xenon concentrate from methane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202216489U true CN202216489U (en) | 2012-05-09 |
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ID=46015739
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120259308XU Expired - Fee Related CN202216489U (en) | 2011-07-21 | 2011-07-21 | Containing CO2Device for separating krypton-xenon concentrate from methane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202216489U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102538393A (en) * | 2011-07-26 | 2012-07-04 | 上海启元空分技术发展股份有限公司 | Method for separating concentrated krypton-xenon containing CO2 and methane |
| CN103712416A (en) * | 2013-12-27 | 2014-04-09 | 上海启元空分技术发展股份有限公司 | Method for controlling power of reboiler of crude krypton and xenon evaporating tower |
-
2011
- 2011-07-21 CN CN201120259308XU patent/CN202216489U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102538393A (en) * | 2011-07-26 | 2012-07-04 | 上海启元空分技术发展股份有限公司 | Method for separating concentrated krypton-xenon containing CO2 and methane |
| CN103712416A (en) * | 2013-12-27 | 2014-04-09 | 上海启元空分技术发展股份有限公司 | Method for controlling power of reboiler of crude krypton and xenon evaporating tower |
| CN103712416B (en) * | 2013-12-27 | 2016-06-22 | 上海启元空分技术发展股份有限公司 | The method controlling crude krypton xenon concentration tower reboiler power |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120509 Termination date: 20190721 |
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| CF01 | Termination of patent right due to non-payment of annual fee |