CN102564064A - Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air - Google Patents
Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air Download PDFInfo
- Publication number
- CN102564064A CN102564064A CN2011104340028A CN201110434002A CN102564064A CN 102564064 A CN102564064 A CN 102564064A CN 2011104340028 A CN2011104340028 A CN 2011104340028A CN 201110434002 A CN201110434002 A CN 201110434002A CN 102564064 A CN102564064 A CN 102564064A
- Authority
- CN
- China
- Prior art keywords
- tributary
- air
- compressor
- pressure
- later stage
- 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.)
- Pending
Links
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The method involves expanding the main partial flow (11) of purified feed air (6) in expanding machine (16). The intermediate partial flow (12) of purified feed air is cooled to intermediate temperature and is recompacted in a cold compressor (19). The final partial flow (13) of compressed feed air (3) is expanded. The liquid oxygen product streams (30,32) are evaporated or pseudo vaporized, warmed to ambient temperature and withdrawn finally as the gaseous pressurized oxygen product stream (33). The portion of final partial flow is returned to the air compressor (28).
Description
Technical field
The present invention relates to obtain the method for amounts of pressurized gaseous product through low temperature air separating.
Background technology
Hausen/Linde for example, cryogenic technique, 1985 the 2nd edition the 4th chapter (the 281st to 337 page) method and apparatus of low temperature air separating is disclosed.
Distillation column system of the present invention is designed to double tower system (for example traditional Linde double tower system), perhaps is designed to three towers or multitower system.It can also have and be used to obtain especially other devices of inert gas of high purity product and/or other composition of air except nitrogen oxygen knockout tower, for example obtains argon gas and/or obtains the device of krypton-xenon.
In this process, pressurized liquid oxygen product stream is relatively evaporated with heat carrier, obtain as the amounts of pressurized gaseous product at last.This method is also referred to as interior compression.It is used to obtain compressed oxygen.For the situation of supercritical pressure, transformation mutually truly can not take place, but make product stream " false evaporation ".
The product stream that is in heat carrier and (vacation) evaporation under the high pressure relatively liquefy (perhaps false liquefaction, condition is that it is under the supercritical pressure).Heat carrier normally forms through portion of air, is " second tributary " through the feeding air of compression in the case.
For example (=US 2,712, and 738/US 2,784 for DE 830 805, DE 901 542; 572), DE 952 908, DE 11 03 363 (=US 3,083,544), (=US 3,214 for DE 11 12 997; 925), DE 11 24 529, DE 11 17 616 (=US 3,280,574), (=US 3,216 for DE 12 26 616; 206), DE 12 29 561 (=US 3,222,878), DE 11 99 293, (=US 3,371 for DE 11 87 248; 496), DE 12 35 347, DE 12 58 882 (=US 3,426,543), (=US 3 for DE 12 63 037; 401,531), (=US 3,416 for DE 15 01 722; 323), DE 15 01 723 (=US 3,500,651), (=US 4 for DE 253 132; 279,631), DE 26 46 690, (=US 4,555 for EP 93 448B1; 256), EP 384 483B1 (=US 5,036,672), (=US 5 for EP 505 812B1; 263,328), (=US 5,644 for EP 716 280B1; 934), EP 842 385B1 (=US 5,953,937), (=US 5 for EP 758 733B1; 845,517), (=US 6,038 for EP 895 045B1; 885), (=US 6,185,960B1), (=US 6 for EP 955 509A1 for DE 198 03 437A1, EP 949 471B1; 196,022B1), (=US 6,314 for EP 1 031 804A1; 755), DE 199 09 744A1, EP 1 067 345A1 (=US 6,336,345), (=US 6 for EP 1 074 805A1; 332,337), DE 199 54 593A1, (=US 6,477 for EP 1 134 525A1; 860), (=US 6,612,129B2), DE 102 13 212A1, DE 102 132 11A1, EP 1 357 342A1 or DE 102 38 282A1, DE 103 02 389A1, DE 103 34 559A1, DE 103 34 560A1, DE 103 32 863A1, EP 1 544 559A1, EP 1 585 926A1, DE 10 2,005 029 274A1, EP 1 666 824A1, EP 1 672 301A1, DE 10 2,005 028 012A1, WO 2007/033838A1, WO 2007/104449A1, EP 1 845 324A1, DE 10 2,006 032 731A1, EP 1 892 490A1, DE 10 2,007 014 643A1, EP 2 015 012A2, EP 2 015 013A2, EP 2 026 024A1, WO 2009/095188A2 or DE 10 2,008 016 355A1 disclose interior compression method for DE 100 13 073A1, EP 1 139 046A1, EP 1 146 301A1, EP 1 150 082A1, EP 1 213 552A1, DE 101 15 258A1, EP 1 284 404A1 (=US 2003/051504A1), EP 1 308 680A1.
Term " decompressor (Entspannungsmaschine) " comprises the various machines that are used to make process flow acting expansion.Decompressor preferably is made up of expansion turbine in the present invention.
" main heat exchanger " can be made up of one or more parallel connections and/or the heat transfer section that is connected in series, and for example is made up of one or more heat-exchangerss of the plate type unit.It is used for cooling off feed air stream with the indirect heat exchange from the backflow of distillation column system.
The application also comprises simultaneously the disclosed content of submitting to of German patent application (inner folder P10C124-DE=IC0362a), is called " parallel application " below, and with the disclosed content of the corresponding application of this parallel application.
WO 2008/110734A2 discloses a kind of method of aforementioned type.Conclusively for this method be, can close second decompressor, and with whole the 3rd tributaries in the second decompressor downstream drain in atmosphere, thereby make it not disturb distillation process.
Summary of the invention
Therefore the objective of the invention is to, provide the method and the corresponding device thereof of aforementioned type, its advantageous particularly ground operation economically.
This purpose is through realize according to the method for the invention.
In the method according to the invention, do not abandon the air (three tributary) of at least a portion, but it is sent back in the air compressor from second decompressor.Thus, improved on the one hand the productive rate of equipment, on the other hand second decompressor can carry on as usual with low especially outlet pressure promptly with than higher efficient work.
The outlet pressure of second decompressor preferably approximates the operating pressure (adding the upper pipeline loss) of lower pressure column.
In category of the present invention, can whole the 3rd tributaries be sent in the air compressor.Preferably at least 30%, especially at least 50% the 3rd tributary through acting is expanded is sent in the lower pressure column.(will be called " the 3rd tributary " through whole air streams of second decompressor guiding) at this
Can remaining through the 3rd tributary that acting is expanded an or wherein part be sent in the lower pressure column.
The 3rd tributary that for example can will do work in the porch (or wherein a part of) send in the air compressor.Substituting ground; Intergrade at air compressor is sent into; Wherein said air compressor is multistage structure, and has the first order and afterbody at least, wherein with at least a portion through the 3rd tributary that acting is expanded in first order downstream and in the end the one-level upper reaches return to air compressor.
From feeding air divide expenditure the 3rd tributary for example can be in the purifier downstream, approximately directly the later stage upstream of compressor, in later stage compressor downstream or the first decompressor downstream implement.But especially divide expenditure the 3rd tributary from feeding air through compression at the purifier upper reaches.
The air separation equipment of aforementioned type has pre-cooled device usually, therein will be through the feeding air of compression at the purifier upper reaches through cooling off, to remove the heat of compression with the direct or indirect heat exchange of cooling water.In the case, can be at pre-cooled device upstream from dividing expenditure the 3rd tributary through the feeding air that purifies.In various cryogenic air separation process, also can use this characteristic of the present invention in principle even without other above-mentioned characteristics; Promptly go out the air tributary in pre-cooled device upstream branch; The expansion of then doing work, and return in the air compressor and/or be disposed in the atmosphere; This especially is suitable for; Condition be another decompressor (this: produce refrigeration first decompressor); And two decompressors mechanically are connected with the later stage compressor, and especially one is connected with cryogenic compressor, and another later stage compressor with heat is connected.
Substituting ground is disposed to a part in the atmosphere through the 3rd tributary that acting is expanded perhaps extraly.This especially can be significant, and condition is the stress level that the outlet pressure of second decompressor is in lower pressure column.
In the method according to the invention, can whole feeding airs be carried out later stage compression together in the later stage of heat compressor, i.e. especially first, second and the 3rd tributary.(possibly divide the part air of expenditure from other purposes, so-called instrument air does not belong to " all feeding airs " at this.) go out the 3rd tributary of other part air then in the later stage of heat compressor downstream branch.This method especially is significant when turbine is connected in series, but also can under situation about being connected in parallel, use.
The air separation equipment of aforementioned type has pre-cooled device usually, therein air is directly or indirectly being cooled off in the heat exchange at the purifier upper reaches.Substituting ground carries out the later stage compression with first and second tributaries in the later stage of heat compressor, and makes the 3rd tributary walk around the later stage compressor of heat.At this, divide the 3rd tributary of other part air of expenditure at the later stage of heat upstream of compressor.
In another embodiment of the invention, the later stage compression is carried out in second tributary in the later stage of heat compressor, and made the first and the 3rd tributary walk around the later stage compressor of heat.At this, the branch in the 3rd tributary of other part air implements at the later stage of heat upstream of compressor equally, is perhaps dividing the downstream of paying the first and the 3rd tributary to implement jointly from the feed air stream of still not carrying out the later stage compression through purification.
For example the 3rd tributary is perhaps sent in second decompressor under the outlet pressure of the later stage of heat compressor greatly down about the outlet pressure of air compressor greatly.In the case, be divided into the first and the 3rd tributary at the upper reaches that acting is expanded.These two decompressors are connected in parallel.
Substituting ground, reducing pressure in first decompressor together with first tributary in the 3rd tributary, and sends into second decompressor discretely in the first decompressor downstream and first tributary.Promptly just be divided into the first and the 3rd tributary at the first decompressor upper reaches.These two decompressors are connected in series.
In the method, air compressor preferably utilize that external energy drives, be used for compressed-air actuated independent machine." independent machine " is to be understood that at this and is single-stage or compound compressor, and its compression stage all is connected with same drive unit, and wherein all compression stages are installed in the same shell, perhaps are connected with same transmission mechanism.In this air compressor, preferably whole feeding airs are compressed to apparently higher than the pressure of the maximum pressure of distillation column system, especially apparently higher than the pressure of high-pressure tower operating pressure.Pressure differential between the outlet pressure of air compressor and the operating pressure of high-pressure tower for example is at least 4 crust, preferably between 6 and 16 crust.In the scheme of this change, whole air that preferably will in air compressor, compress (except possible less part, for example instrument air) are divided into three tributaries fully.
In addition; Can also replenish nitrogen-Nei compression set in the method; Its mode is that liquid nitrogen product stream is discharged from distillation column system,, under the pressure of this raising, in main heat exchanger, evaporates or false evaporation to the pressure that improves with liquid-applied; Be heated to and be approximately environment temperature, discharge as gaseous nitrogen pressure product stream at last.
Set forth the present invention and other details in more detail according to illustrated embodiment in the accompanying drawing and according to the embodiment in the parallel application below.
Description of drawings
Shown in Figure 1 is the first embodiment of the present invention, wherein divides expenditure the 3rd tributary at pre-cooled device upstream; And
Fig. 2 to 4 is depicted as three other embodiment, wherein divides expenditure the 3rd tributary at pre-cooled device upstream.
The specific embodiment
In Fig. 1, atmospheric air is aspirated by air compressor 2 via pipeline 1 as feeding air, and be compressed to apparently higher than the pressure of the operating pressure of high-pressure tower 80.At this, air compressor especially with level Four, Pyatyi or six grades of formations, wherein all has intercooler with multistage between at different levels.To send into pre-cooled device 4 (" Precooling ") through the major part 42 of feeding air 3 of compression, therein with the heat of compression of the afterbody of air compressor with the direct or indirect heat exchange of cooling water in remove.To in the purifier 5 that preferably constitutes, purify through pre-cooled feeding air as molecular sieve adsorber (MS-Adsorber).In the present embodiment, will be divided into three tributaries through the feeding air 3 of compression:
-first tributary 11 is cooled to first medium temperature send into acting expansion in first decompressor 16 through pipeline 15 afterwards in main heat exchanger 14, send in the high-pressure tower 80 of distillation column system through pipeline 17 subsequently.
-second tributary 12 is cooled in main heat exchanger 14 is below or above first medium temperature or equals second medium temperature of first medium temperature; Discharge from main heat exchanger 14 through pipeline 18; In cryogenic compressor 19, continue compression; Under being higher than the 3rd medium temperature of second medium temperature, send into again in the main heat exchanger 14 through pipeline 20, and continue cooling at this, liquefying perhaps at last, the pressure in second tributary is to carry out vacation liquefaction under the postcritical situation.Make second tributary 21 of (vacation) liquefaction in choke valve 22, be decompressed to the pressure that is approximately high-pressure tower 80, send at last in the high-pressure tower 80.Also can a part directly be sent in the lower pressure column 90 through the 3rd tributary 23 of decompression.
-directly go out through the 3rd tributary 13 of the feeding air 3 of compression in pre-cooled device 4 upstream branch, and in main heat exchanger 14, do not cool off and just send into acting expansion in second decompressor 25.In the present embodiment; Air compressor 2 is fully sent into through pipeline 28 in acting is expanded the 3rd tributary 26 be decompressed to 1.2 to 6 crust for example, preferably be about the pressure of 1.3 crust; And at these upper reaches of one-level in the end for example, especially the intercooler upper reaches of work are sent in whole air streams under suitable pressure.
First and second tributaries 11,13 are delivered to the hot junction of main heat exchanger 14 through pipeline 7 and 10 from the outlet of purifier 5 together at this via the later stage compressor 8 of heat and later stage cooler 9.
Liquid oxygen product stream 30 is discharged from lower pressure column 90; In pump 31 with liquid-applied to the pressure (52) that improves; Evaporate in main heat exchanger, evaporating under the pressure of this raising or under pressure is higher than the situation of critical pressure, carry out vacation; Be heated to and be approximately environment temperature, discharge as gaseous oxygen pressure product stream 33 at last.
Compression set obtained in nitrogen pressure product also can utilize.For this reason; Liquid nitrogen product stream is discharged from high-pressure tower or its overhead condenser, main condenser; In pump with liquid-applied to the pressure that improves; In main heat exchanger, evaporate or under pressure is higher than the situation of critical pressure, carry out vacation evaporation at (pipeline 41) under the pressure of this raising, be heated to and be approximately environment temperature, at last as gaseous nitrogen pressure product stream (42) discharge.
From other backflows of distillation column system is gaseous oxygen 36, impure nitrogen 35 and pure nitrogen 36.In addition, liquid oxygen and liquid nitrogen both can be discharged from high-pressure tower (HPC), also can discharge from lower pressure column.Gaseous products is heated in main heat exchanger 14 is approximately environment temperature, discharge through pipeline 37,38 and 39 at last.
Can second tributary 7 is pre-cooled at the later stage of heat compressor 8 upper reaches in the optional channel group 40 of main heat exchanger 14.Might dispense the later stage cooler then.
The difference of Fig. 2 and Fig. 1 is following details:
The later stage compressor 8 of heat is walked around in-the first tributary 11 through pipeline 210.
-in pre-cooled device 4 and purifier 5 downstream from second tributary 7,12 fens expenditure the 3rd tributaries 13, deliver to the hot junction of main heat exchanger 14 through pipeline 210 with first tributary then.Subsequently the 3rd tributary 13 is cooled to medium temperature in main heat exchanger 14, and under this medium temperature, sends to acting expansion 25 through pipeline 24.
-will in main heat exchanger 14, be heated to through the 3rd tributary 28 that acting is expanded and be approximately environment temperature, and flow back into air compressor 2 through pipeline 29.
-guiding is a small amount of to reflux through main heat exchanger 14 (41/42 among Fig. 1).
The difference of Fig. 3 and Fig. 2 is following details:
It is not in main heat exchanger 14, to cool off that-Di three tributaries 13 are expanded before 25 in acting, but directly delivers to decompressor.
The only first process pipeline 28 and 29 in-the 3rd tributary 28 that guiding as shown in Figure 2 is expanded through doing work: the lower pressure column (LPC) of second portion being delivered to distillation column system through pipeline 27,227 via the low-temp. portion branch of main heat exchanger 14.
The difference of Fig. 4 and Fig. 2 is following details:
-will return to the inlet of air compressor 2 through the 3rd tributary 28 that acting is expanded through pipeline 329.
Parallel application show that also be embodiments of the invention with at least a portion through all embodiment that the 3rd tributary that acting is expanded returns to air compressor.When not carrying out the later stage compression in the second decompressor upper reaches in the 3rd tributary, can be similar to be shown in the purifier upper reaches and to divide from feeding air and pay the 3rd tributary through compression in pre-cooled device upstream or downstream at this accompanying drawing.
In the scheme of the change of all embodiment, can with a part or manifold the 3rd tributary 26 of expanding through acting deliver to air compressor other positions, send in the lower pressure column and/or be disposed to atmosphere.
Claims (10)
1. in distillation column system, pass through the method that low temperature air separating produces gaseous oxygen pressure product, in the method with at least one lower pressure column (90) and high-pressure tower (80)
-feeding air (1) is compressed in air compressor (2),
-will in purifier (5), purify at least in part through the feeding air (3) of compression,
-at least a portion (7) is carried out the later stage compression through the feeding air (6) that purifies in the later stage of heat compressor (8),
-the expansion of in first decompressor (16), doing work through first tributary (11,15) of the feeding air (6) that purifies, and send at least in part in (17) high-pressure tower (80),
-will in main heat exchanger (14), be cooled to medium temperature through second tributary (12) of the feeding air (6) that purifies; In cryogenic compressor (19), carry out the later stage compression, in main heat exchanger (14), continue cooling and liquefaction or false liquefaction, send into distillation column system (21 subsequently; 23) in
-the expansion of in second decompressor (25), doing work through the 3rd tributary (13) of feeding air (3) of compression,
-discharge liquid oxygen product stream (30,32) from distillation column system, with liquid-applied pressure (34) to raising; In main heat exchanger (14), evaporating under the pressure of this raising or false evaporation; Be heated to and be approximately environment temperature, discharge as gaseous oxygen pressure product stream (33) at last
-these two decompressors (16,25) are connected with one of the later stage compressor (8) of heat and these two machines of cryogenic compressor (18,19) separately,
It is characterized in that,
-at least a portion is returned to air compressor (28) through the 3rd tributary (26) that acting is expanded.
2. according to the method for claim 1; It is characterized in that; Air compressor (2) is multistage structure, and has the first order and afterbody at least, wherein with at least a portion through the 3rd tributary (26) that acting is expanded in first order downstream and in the end the one-level upper reaches send (28) to air compressor (2) back to.
3. according to the method for claim 1 or 2, it is characterized in that, divide expenditure the 3rd tributary (13) from feeding air (3) through compression at purifier (5) upper reaches.
4. according to the method for claim 3; It is characterized in that; The part (6) that will comprise first and second tributaries is cooled off in pre-cooled device (4) at purifier (5) upper reaches through the feeding air (3) of compression, and divides expenditure the 3rd tributary (13) at pre-cooled device (4) upper reaches from the feeding air (3) through compression.
5. according to the method for one of claim 1 to 4, it is characterized in that, a part is disposed to atmosphere through the 3rd tributary (26) that acting is expanded.
6. according to the method for one of claim 1 to 5, it is characterized in that, the later stage compression is carried out in first and second tributaries in the later stage of heat compressor (8), and make the 3rd tributary (13) walk around the later stage compressor (8) of heat.
7. according to the method for one of claim 1 to 5, it is characterized in that, the later stage compression is carried out in second tributary in the later stage of heat compressor, and make first tributary walk around the later stage compressor of heat.
8. according to the method for one of claim 1 to 7, it is characterized in that, the 3rd tributary (13) are sent under being approximately the outlet pressure of air compressor in second decompressor (25).
9. according to the method for one of claim 1 to 8, it is characterized in that, air compressor (2) be utilize that external energy drives, be used for compressed-air actuated independent machine.
10. according to the method for one of claim 1 to 9; It is characterized in that; Discharge liquid nitrogen product stream from distillation column system, to the pressure that improves, under the pressure of this raising, in main heat exchanger, evaporate or false evaporation with liquid-applied; Be heated to and be approximately environment temperature, discharge as gaseous nitrogen pressure product stream at last.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102010052544A DE102010052544A1 (en) | 2010-11-25 | 2010-11-25 | Process for obtaining a gaseous product by cryogenic separation of air |
| DE102010052544.8 | 2010-11-25 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102564064A true CN102564064A (en) | 2012-07-11 |
Family
ID=46410160
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011104340028A Pending CN102564064A (en) | 2010-11-25 | 2011-11-25 | Method and device for creating a gaseous, pressurised product by the cryogenic decomposition of air |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102564064A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105318661A (en) * | 2014-07-05 | 2016-02-10 | 林德股份公司 | Method and apparatus for the cryogenic separation of air |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1111321A (en) * | 1993-07-16 | 1995-11-08 | 气体产品与化学公司 | Integrated air separation-gas turbine electrical generation process |
| CN1168463A (en) * | 1996-02-12 | 1997-12-24 | 液体空气乔治洛德方法利用和研究有限公司 | Process and installation for producing high pressure oxygen |
| US5996373A (en) * | 1998-02-04 | 1999-12-07 | L'air Liquide, Societe Ananyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Cryogenic air separation process and apparatus |
| WO2005085728A1 (en) * | 2004-03-02 | 2005-09-15 | L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Cryogenic distillation method for air separation and installation used to implement same |
-
2011
- 2011-11-25 CN CN2011104340028A patent/CN102564064A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1111321A (en) * | 1993-07-16 | 1995-11-08 | 气体产品与化学公司 | Integrated air separation-gas turbine electrical generation process |
| CN1168463A (en) * | 1996-02-12 | 1997-12-24 | 液体空气乔治洛德方法利用和研究有限公司 | Process and installation for producing high pressure oxygen |
| US5996373A (en) * | 1998-02-04 | 1999-12-07 | L'air Liquide, Societe Ananyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Cryogenic air separation process and apparatus |
| WO2005085728A1 (en) * | 2004-03-02 | 2005-09-15 | L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Cryogenic distillation method for air separation and installation used to implement same |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105318661A (en) * | 2014-07-05 | 2016-02-10 | 林德股份公司 | Method and apparatus for the cryogenic separation of air |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101421575B (en) | Method and apparatus for fractionating air at low temperatures | |
| JP2909678B2 (en) | Method and apparatus for producing gaseous oxygen under pressure | |
| CN101925790B (en) | For the method and apparatus of low temperature air separating | |
| US6962062B2 (en) | Process and apparatus for the separation of air by cryogenic distillation | |
| CN1081782C (en) | Process and plant for the production of gaseous oxygen under pressure | |
| US6336345B1 (en) | Process and apparatus for low temperature fractionation of air | |
| CN101883963B (en) | Method and apparatus for the production of gas from air in highly flexible gaseous and liquid form by cryogenic distillation | |
| TW201607599A (en) | Method and device for the low-temperature separation of air at variable energy consumption | |
| CN110307694B (en) | Nitrogen production method and nitrogen production apparatus | |
| JPH05203348A (en) | Air separation by refining and its apparatus | |
| CN100378422C (en) | Cryogenic distillation method and system for air separation | |
| CN107606875A (en) | The method and apparatus that compressed nitrogen and liquid nitrogen are produced by low temperature air separating | |
| TW202140974A (en) | Process for cryogenic fractionation of air, air fractionation plant and integrated system composed of at least two air fractionation plants | |
| TW201637998A (en) | Method and apparatus for obtaining a compressed nitrogen product | |
| JPH06229668A (en) | Method and equipment for manufacturing gaseous oxygen | |
| US20090107177A1 (en) | Process and device for low temperature air fractionation | |
| CN102062515B (en) | Method and device for generating a helium-neon concentrate from air | |
| JP7451532B2 (en) | Apparatus and method for separating air by cryogenic distillation | |
| US5730004A (en) | Triple-column for the low-temperature separation of air | |
| CN102901322B (en) | Pressure nitrogen and the method and apparatus of pressure oxygen is obtained by Cryogenic air separation | |
| CN107076512B (en) | Method and device for variably obtaining argon by cryogenic separation | |
| CN216716763U (en) | Device for producing pure nitrogen by using single rectifying tower | |
| EP4464962A2 (en) | Ultra-high-purity oxygen production method and ultra-high-purity oxygen production apparatus | |
| CA2634483A1 (en) | Cryogenic air separation system | |
| US10436507B2 (en) | Process and apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20120711 |