CN1050260A - Cryogenic air separation process and equipment - Google Patents
Cryogenic air separation process and equipment Download PDFInfo
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- CN1050260A CN1050260A CN90107623A CN90107623A CN1050260A CN 1050260 A CN1050260 A CN 1050260A CN 90107623 A CN90107623 A CN 90107623A CN 90107623 A CN90107623 A CN 90107623A CN 1050260 A CN1050260 A CN 1050260A
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- 238000000926 separation method Methods 0.000 title claims abstract description 25
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 221
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 113
- 238000009833 condensation Methods 0.000 claims abstract description 66
- 230000005494 condensation Effects 0.000 claims abstract description 66
- 238000000034 method Methods 0.000 claims abstract description 54
- 238000001704 evaporation Methods 0.000 claims abstract description 16
- 230000008020 evaporation Effects 0.000 claims abstract description 14
- 230000006835 compression Effects 0.000 claims abstract description 13
- 238000007906 compression Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 239000001301 oxygen Substances 0.000 claims description 85
- 229910052760 oxygen Inorganic materials 0.000 claims description 85
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 84
- 238000001816 cooling Methods 0.000 claims description 20
- 238000002309 gasification Methods 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000002912 waste gas Substances 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 238000004821 distillation Methods 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000005292 vacuum distillation Methods 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- 239000002826 coolant Substances 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000005194 fractionation Methods 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims 13
- 238000009428 plumbing Methods 0.000 claims 13
- 230000001112 coagulating effect Effects 0.000 claims 1
- 238000000605 extraction Methods 0.000 claims 1
- 238000004134 energy conservation Methods 0.000 abstract description 4
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 12
- 229910052786 argon Inorganic materials 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 6
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000002650 habitual effect Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04321—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of oxygen
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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
- F25J3/04406—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 using a dual pressure main column system
- F25J3/04424—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 using a dual pressure main column system without thermally coupled high and low pressure columns, i.e. a so-called split columns
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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
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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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
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Adopt a kind of low temperature separating methods and equipment of energy-conservation rectifying air, can produce at least one steam fraction, a liquid fraction and a nitrogen product stream.Its process is, carries out the indirect heat exchange contact by same liquid fraction, and with the cold compression air setting of gaseous state, this moment, liquid fraction evaporation and air feed flowed condensation.Then, carry out indirect heat exchange contact by a steam fraction again and with the air feed evaporation of condensation, at this moment, the condensation of steam fraction, the air feed stream that uses evaporation then again carries out cryogenic separation as air feed with rectification method.
Description
This is the invention of a relevant air separating method.Specifically, the present invention proposes a kind of by air produce nitrogen, oxygen and (or) method and apparatus of argon.This is a kind of effective power-economizing method, has wherein used the heat transferring medium of the air of liquefaction as the high pressure condensing tower.
The cryogenic air separation process of standard is included as to be removed fine particulate matter and air feed is filtered and it is compressed to obtain separation energy thereupon.In general, air demand is through supercooling, and removed by absorbent and to resemble carbon dioxide and some such impurity of water vapour.Air-flow after above-mentioned processing is sent to and is carried out low temperature distillation.
Low temperature distillation or air separation comprise that pressure-air is fed to the one or more separation that works in low temperature to collapse.The composition of air comprises that oxygen, nitrogen, argon and rare gas can separate with the way of distillation in tower.
Low temperature processing comprises contacting of steam and liquid, and it depends on the not steam pressure of heterogeneity.Composition with high evaporation pressure, promptly more volatile or low-boiling composition has enrichment trend in gas phase; And having the composition of low evaporating pressure, composition promptly not volatile or that boiling point is high then has the trend of enrichment in liquid phase.
With liquefied mixture heating, make volatile component be enriched in gas phase and make not that volatile component is enriched in liquid phase, such separation process is exactly so-called the distillation.Partial condensation is a kind of separation method, and it is with the mixed vapour cooling, to collect the volatile component of gas phase, also collects the not volatile component of liquid phase simultaneously.
This method is called rectification method or is sometimes referred to as the continuous still method.It is made up of a series of part evaporation and condensation, comprises the countercurrent treatment of steam in the liquid phase, and the counter current contacting of gas phase and liquid phase is adiabatic, and comprises alternate integration or differential contact.
Use the so-called rectifying column of the employed device of partition method, destilling tower or the fractionating column of distillation principle separating mixture.
In this specification and claims, term " tower " is meant distillation or fractionating column (or district), also can be a contact tower (or contact zone).Be separation fluid mixtures, liquid and gas can carry out counter current contacting in tower.Actual conditions are, contacting of gas phase and liquid phase can be carried out on the tower tray of a series of and axis normal configuration or column plate, and these tower trays or column plate are normally bored a hole, and become corrugated, and it can make tower laterally expanded.Can use some fillers that tower is filled at these tower trays or column plate place.
" double tower " is meant a kind of high-pressure tower in this manual, and heat exchange can be carried out with the lower pressure column that is connected in its upper end.
In this manual, term " normal air separation method and equipment " is meant above-mentioned method and apparatus or other known air separating methods.
In this specification and claims, term " indirect heat exchange " is meant two kinds of liquid streams is carried out heat exchange, but they any contact do not take place itself or hand over and mix.
Traditionally, nitrogen, oxygen and (or) argon always adopts one of single tower method or these two kinds of basic skills of double tower method to produce.
With regard to nitrogen, Dan Tafa can produce high-quality gas nitrogen and liquid nitrogen under the pressure of about 6～10 crust.The recovery of nitrogen is subjected to the restriction of balance at the bottom of the tower.The nitrogen of producing with the method generally be in the initial air feed nitrogen content 50～60%.
Produce nitrogen greatly under the pressure of 1～4 crust with the double tower method, this is more more effective and can reclaim about 90% or more nitrogen from initial air than single tower method.Usually tower can repeatedly be put and with two towers separately with condensation one reboiler.Because this method is to produce nitrogen under quite low pressure, nitrogen further need be compressed, and has so just increased production and use cost.
In the prior art, the double tower method is that air is separated with low temperature distillation or rectification method, thereby obtains nitrogen-enriched stream at the top of high-pressure tower, and obtains oxygen-rich stream at lower curtate.The top that nitrogen-enriched stream is delivered to lower pressure column provides backflow to give this tower, and the oxygen-rich stream of bottom is then delivered to lower pressure column further with its separation.
In lower pressure column, the air-flow of sending into further separates with the low temperature distillation method, obtains oxygen-rich stream in the bottom.Top stream can be used as the nitrogen product and reclaims.When using double tower, high-pressure tower and lower pressure column are to be undertaken hot linked by condensation one reboiler.Therefore, in existing double tower method, be the nitrogen-enriched stream condensation that makes in the high-pressure tower, and do not allow gasification oxygen-rich stream condensation in the lower pressure column.
For given lower pressure column pressure, the air pressure that is fed to high-pressure tower is determined by the institute that forms of the nitrogen-enriched stream of the forming of gasification oxygen-rich stream, high-pressure tower condenser and lower pressure column reboiler.And also determine to a certain extent by the institute that forms of the nitrogen-enriched stream of condensation.Nitrogen-enriched stream is that quite pure existing other separation method is the variant of above-mentioned single tower method and double tower method, just has some additional characteristics, for example with overhead condenser or tower bottom reboiler.
The method that the present invention provides can be used for the energy-conservation production of nitrogen, oxygen and argon.
From in essence, the invention reside in and used gasification and liquefied air as the heating and cooling medium between the high-low pressure tower, what used in the past is nitrogen.
The present invention will carry out detailed explanation to nitrogen, but be applicable to the production of oxygen and argon too.People for being familiar with professional technology, know how to optimize temperature with will be apparent from, pressure and other conditions of work so that as the oxygen of major product and (or) output the best of argon.
Using air is that the condensation air energy more required than the condensation nitrogen-enriched stream lacks as the special benefits of heating and cooling medium.Because main energy consumption is in the compression of all gases, and, to lack during the consumption rate condensation nitrogen of the desired low pressure generation of condensation air under the fixed temperature.
For example, required pressure is 7 crust during the nitrogen condensation, and temperature is-180 ℃, and condensation air only is 6 crust, and temperature is-178 ℃, and temperature difference is 2 ℃ like this, pressure differential 1 crust, and the present invention has reduced energy consumption.
In existing technology, nitrogen is used to the heating and cooling medium between the high-low pressure tower.Must compress air feed and make it reach the desired high pressure of nitrogen, the therefore main energy-conservation requirement that is to reduce the compression air feed.
Method provided by the invention might be produced highly purified nitrogen, can reach more than 90% of initial air feed institute nitrogen content, can to the pressure limits of 5 crust, produce at 3 crust, and no matter be that elevated pressure nitrogen or low pressure nitrogen all can be produced.Also can distinguish or production simultaneously, and more energy-conservation than existing production method.
According to method of the present invention, air inlet will be handled, and removes moisture and impurity (for example carbon dioxide, methane etc.) through molecular sieve, aluminium oxide, silica gel etc., compresses then and sends into heat exchanger and carry out heat exchange with output products.
According to an embodiment, air inlet is divided into two groups, one group of bottom that is fed to high-pressure tower, and another group is fed to the condensation-reboiler that is positioned at the lower pressure column bottom.With air inlet be divided into equate component can obtain good as effect, use other ratios also to be fine certainly.
According to another embodiment, air inlet is divided into three groups, wherein two groups of condensation-reboilers that are fed to above-mentioned high-pressure tower and are in the lower pressure column bottom.The 3rd group then is subjected to expanding so that the cooling of factory to be provided, introduces lower pressure column then and carry out cryogenic separation.
First group of air inlet is separated into once the gasify rich nitrogen fraction and the oxygen enrichment fraction that once liquefies with the low temperature distillation method in high-pressure tower.Liquefaction oxygen enrichment fraction takes out and delivers to lower pressure column from the bottom of high-pressure tower.Deliver to second group of air inlet of condensation one reboiler of lower pressure column bottom and carry out in addition condensation of heat exchange by liquefaction oxygen enrichment with the lower pressure column bottom.At this moment, the liquefaction oxygen enrichment obtains evaporation, the condensation liquefaction air that produces in condensation one reboiler is delivered to the evaporator overhead condenser of high-pressure tower, carries out indirect heat exchange at this by the rich nitrogen fraction of the once gasification that produces in high-pressure tower and gasifies, and so just makes nitrogen obtain condensation.
According to an embodiment, the rich nitrogen fraction of the partial condensation in the high-pressure tower is separated and send into lower pressure column so that extra backflow to be provided.Meanwhile, coexist nitrogen in the high-pressure tower evaporator overhead condenser of second group of air inlet carries out indirect heat exchange and liquefies, and is introduced into lower pressure column then and carries out cryogenic separation.
In lower pressure column, second group of air inlet is separated into secondary nitrogen-enriched stream and secondary oxygen-rich stream in company with part from an oxygen enrichment fraction of high-pressure tower.
According to another embodiment, part secondary nitrogen-enriched stream can be used as the elevated pressure nitrogen product and takes out, and remaining part is used for providing backflow for lower pressure column.
According to another embodiment, part elevated pressure nitrogen product can be expanded, with cooling that factory is provided and add in the low pressure nitrogen product stream and go.
The secondary oxygen-rich stream that drops to the lower pressure column bottom gasifies by carry out the indirect heat exchange contact with the second group of air inlet that is subjected to condensation.By another embodiment, secondary oxygen enrichment fraction also can comprise three air feed fractions, it in introducing lower pressure column before overexpansion.
Part secondary oxygen-rich stream is fed to the evaporator overhead condenser of lower pressure column, is gasified by carrying out heat exchange contact with the condensation nitrogen that rises there.Like this, the secondary oxygen-rich stream of gasification can be used as refuse and takes out from evaporator overhead condenser, and is heating in condensation and the heat exchanger again.This heat exchange is carried out indirect heat exchange with air-flow and the air inlet handled.
If needed, useless oxygen can be subjected to expanding so that the cooling of factory to be provided.Perhaps, the useless oxygen of this nearly 70% purity can use as the fecund product in the occasion that need not high purity oxygen.
The used equipment of said method also can provide.Complete equipment comprises: be used for compressing the air compression plant of external feed stream, for removing the purifying plant that adopts from the carbon dioxide in the compressor air and water vapour, make the heat-exchange device that is cooled to low temperature from the compressed air in the purifying plant.One the single flash tower that head tower or evaporated on top one condenser be housed-it is used for the partial-air admission of automatic heat-exchanger in the future and carries out cryogenic separation.
An after-fractionating tower, it has a tower condenser in top and the tower reboiler in bottom, it can be separated into a secondary oxygen enrichment fraction and the rich nitrogen fraction of secondary by fractionation with it with the cooled compressed air inlet (having a part at least) after the circulation of the tower condenser in the top of tower reboiler in the bottom of after-fractionating tower and single flash tower and from the liquefaction oxygen enrichment (having a part at least) of single flash tower.
For the liquid oxygen that extracts the second distillation tower bottom provides some devices, it can import liquid oxygen the after-fractionating tower evaporator overhead condenser so that the indirect heat exchange of carrying out with rising steam in the after-fractionating tower to be provided.
Some expansion gears are provided, and it can expand the compressed air of introducing before the after-fractionating tower, equally also can be used for taking from the after-fractionating tower evaporator overhead condenser oxygen expansion and (or) be the expansion of nitrogen product that cooling is provided.
Fig. 1 represents the schematic flow sheet of the inventive method and equipment, and the product of being produced is a low pressure nitrogen.
Fig. 2 representation class is similar to the schematic flow sheet of Fig. 1, and just the expansion of air has replaced the expansion of waste gas.
The flow process signal that Fig. 3 represents method and apparatus of the present invention because of, the product of being produced is elevated pressure nitrogen and low pressure nitrogen.
Fig. 4 representation class is similar to the schematic flow sheet of Fig. 3, and wherein the part elevated pressure nitrogen is expanded to low pressure nitrogen.
Referring to flow chart 1, pure compress inlet air is introduced heat exchanger 30 by pipeline 20.Air is introduced the pressure of heat exchanger 30 and is preferably got about 5～20 scopes of clinging to, and in the ranks connect heat exchange by flowing to waste gas of discharging and product this moment, and air is cooled to low temperature.
Next step, air is divided into two groups, preferably is divided into equal two groups, certainly other ratios also can, first group of air inlet sent into high-pressure tower 32, remaining second group of reboiler 58 of sending into lower pressure column 34 through pipeline 22 and 60 through pipeline 22 and 62.
At high-pressure tower 32, pressure is preferably approximately got 5～20 crust.
First group of air feed sent into the bottom of tower 32, is lower than the bottom distillation tray, as among the figure 36.Air feed is divided into nitrogen rich vapor here one time, and it rises to the top and the Wu's part-oxygen enrichment that once liquefies of tower 32, and it reduces to the bottom of tower 32.
At least the rich nitrogen that a part once will be liquefied takes out from the bottom 58 of high-pressure tower, wherein approximately contains 35～40% oxygen, and this almost is the same ratio with prior art.
The oxygen enrichment that once liquefies passes through recooler 46 again after pipeline 54 takes out from the bottom of high-pressure tower 32, carry out indirect heat exchange with nitrogen product (through the top of pipeline 48 from lower pressure column 34) and waste gas (through the top condensation-evaporimeter 70 of pipeline 52 from lower pressure column 34) and further lower the temperature.
The once liquefaction oxygen enrichment of cooling is drawn from recooler 64, enters lower pressure column 34 again after valve 76 expands, on the chassis.
Second group of air feed enters the condensation-reboiler 58 of lower pressure column 34 bottoms, carries out heat exchange and condensation with the liquefaction oxygen enrichment of lower pressure column 34 bottoms.This just causes second group of air feed condensation and the evaporation of liquefaction oxygen enrichment.
Second group of air feed of condensation leaves the condensation-reboiler 58 of lower pressure column 34, enters recooler 46 through pipeline 82.The air of liquefaction comes out from recooler through pipeline 84, and expanding through valve 44 enters the condensation-reboiler of high-pressure tower 32.As needs, second group of air feed of the part of condensation can be through pipeline 90, by sending into lower pressure column 34 after valve 92 expansions with the air balance between control high-low pressure tower.
The rich nitrogen that once gasifies rises to the top of high-pressure tower 32 and enters condensation-reboiler 40.There, the same second group of condensation air that enters through valve 444 from the condensation-reboiler 58 of lower pressure column 34 of nitrogen steam carries out the indirect heat exchange contact.This just causes the air evaporation and the condensation of nitrogen steam of liquefaction.As shown in Figure 3 and Figure 4, partly or entirely the nitrogen fraction of condensation is recycled to high-pressure tower 32 so that required backflow to be provided.
All carry out indirect heat exchange and do not have the nitrogen steam of condensation all to can be used as the elevated pressure nitrogen recovery with second group of condensation air inlet, as shown in Figure 3, take out from the top of high-pressure tower 32 by pipeline 67.
If high-pressure nitrogen stream is very little or do not need, the nitrogen of partial condensation can be delivered to lower pressure column 34 and reflux as additional, and this part condensation nitrogen is through the top that pipeline 68 is taken from high-pressure tower 32, as shown in figures 1 and 3.Condensation nitrogen carries out indirect heat exchange with the nitrogen product of discharging with waste gas there and contacts then by recooler 66.From recooler 66, the nitrogen of condensation is sent into lower pressure column 34 by pipeline 68 after valve 78 expands.
Meanwhile, the gasification air of coming out from the condensation-reboiler at high-pressure tower 32 tops through pipeline 56 enters lower pressure column 34 and separated by pipeline 64, this and through the first time that pipeline 54 enters the liquefy situation of oxygen enrichment similar.
Take from the oxygen enrichment and take from the gasification air of the condensation-reboiler at high-pressure tower 32 tops of once liquefying of the bottom of tower 32, in tower 34, further be separated into rich nitrogen fraction of second gasification and secondary oxygen enrichment fraction through pipeline 56.
The rich nitrogen fraction of second gasification rises to the top of lower pressure column 34, and secondary oxygen enrichment fraction drops to the bottom of lower pressure column 34.
The secondary of part lower pressure column 34 bottoms liquefaction oxygen enrichment fraction takes out through pipeline 74 and by recooler 46, and secondary liquefaction oxygen enrichment further connects heat exchange in the ranks and cools off by flowing to the nitrogen that takes out from lower pressure column 34 tops through pipeline 48 with through the waste gas that pipeline 52 is sent from lower pressure column 34 evaporator overhead condensers there.
Secondary liquefaction oxygen enrichment is connected to secondary recooler 66 through pipeline 74 and carries out indirect heat exchange and further cooling with the nitrogen of sending from high-pressure tower 32 tops through pipeline 68 with through pipeline 52 from the useless oxygen flow of evaporator overhead condenser 70.
The secondary liquefaction oxygen enrichment of resulting cooling is introduced lower pressure column 34 tops by pipeline 74 after valve 72 expands evaporator overhead condenser 70 further cools off the secondary oxygen-rich stream.
Most of secondary nitrogen-enriched stream reclaims from the top of lower pressure column 34 by pipeline 48 as the nitrogen product.Nitrogen stream before output system through recooler 66 and 46 and heat exchanger 30 heat.
The remainder of secondary nitrogen-enriched stream carries out heat exchange and condensation with the liquefaction of the secondary in evaporated on top one recooler 70 of lower pressure column 34 oxygen enrichment in lower pressure column 34.The oxygen enrichment that liquefies this moment is evaporated, and the lower pressure column 34 that is condensed into of nitrogen provides backflow, and the oxygen-rich liquid of gasification, then heats by recooler 66,46 and heat exchanger 30 from 70 outputs of evaporated on top one condenser through pipeline 52.
After the heating, useless oxygen flow is by pulley expander 78 in heat exchanger 30, and air-flow expands so that the cooling of factory to be provided at this.
Hence one can see that, and said method has utilized air as cooling between the high-low pressure tower and heat medium.And in the prior art, normally heat is reached the bottom of lower pressure column with nitrogen-enriched stream.Attention: for a certain given nitrogen recycling method, promptly having under the identical oxygen-rich stream composition situation, the condensation nitrogen-enriched stream is more than condensation air institute energy requirement.In other words, for a certain given nitrogen recycling method, when using air as heat exchange medium, high-pressure tower can be worked under the lower pressure of this habitual existing method, therefore, and according to method of the present invention, for identical high-pressure tower pressure, lower pressure column can be worked under higher pressure.
Table 1 has been listed the estimated performance of the inventive method of above-mentioned production nitrogen shown in Figure 1.
Table 1
Air feed total flow pipeline 20 15462Nm
3/ n
Air feed pressure pipeline 20 10.2 crust absolute values
Nitrogen product flow pipeline 48 10514Nm
3/ n
Nitrogen purity 18vpm02
Waste gas (oxygen enrichment) flow pipeline 52 4948Nm
3/ n
Waste gas pressure pipeline 16 1.3 crust absolute values
22-160 ℃ of compressed-air lines
38-165.6 ℃ of liquefaction oxygen enrichment pipelines
82-167.5 ℃ of second group of air feed fraction of condensation pipelines
84-171 ℃ of second group of air feed fraction of condensation pipelines
Come autocondensation/reboiler 40 warps
56-172.6 ℃ of second group of gas supply lines of gasification
68-170.6 ℃ of the output nitrogen pipelines of tower 32
68-174.4 ℃ of the condensation nitrogen pipelines of tower 66 outputs
From 74-168.8 ℃ of the liquefaction oxygen enrichment pipelines of tower 34
From 74-174.4 ℃ of the liquefaction oxygen enrichment pipelines of condenser 66
72-179 ℃ on liquefaction oxygen enrichment valve after the expansion
48 177.6 ℃ of the nitrogen product pipelines of tower 34 outputs
The nitrogen product pipeline 48 5 crust abs of tower 34 outputs
From 52-178.9 ℃ of the useless oxygen flow pipelines of condenser 70
When adopting the scheme of Fig. 3 or Fig. 4, supply gas pressure is 21 crust, and the pressure of high-pressure tower 32 is about 20 crust, and the pressure of lower pressure column 34 is about 14 crust.
The various improvement projects of foregoing invention method and apparatus are open-and-shut for the people who knows this field, only otherwise below violating in claims to the specified scope and spirit of the present invention, these improvement projects can be used.
Claims (21)
1, a kind ofly adopts a destilling tower to come the separation method of fractionation Cryogenic air at least, its objective is to produce at least a gasification fraction, a kind of liquefaction fraction and a kind of nitrogen product stream.Improvement comprises:
The air feed stream of the compressed of a kind of gasification and cooling is provided;
Employing is carried out indirect heat exchange and is made the condensation of above-mentioned part air feed steam flow with above-mentioned a kind of (at least a) liquid fractions.Above-mentioned liquid fractions evaporation this moment, the condensation of air feed stream.
The method that employing is carried out indirect heat exchange with above-mentioned a kind of fraction that gasifies makes the above-mentioned condensation air feed of part evaporate.This moment, above-mentioned gasification fraction was subjected to condensation.
2, the described method of claim 1, wherein the air feed of above-mentioned gasification stream is further introduced the air feed that one of above-mentioned destilling tower separates as cryogenic rectification.
3, a kind ofly with the high pressure distillation tower air is carried out low temperature distillation and obtain the method for nitrogen, its objective is to produce an oxygen enrichment fraction the rich nitrogen fraction and have at least an above-mentioned oxygen enrichment fraction of a part to be incorporated into a low-pressure distillation column of once liquefying to produce a secondary oxygen enrichment fraction and the rich nitrogen fraction of secondary.Its improvement comprises:
Get in touch with the heating power of setting up between the high-low pressure tower as the heating and cooling medium with air.
4, method as claimed in claim 3 also comprises:
Air feed is divided into two groups.Introduce above-mentioned high-pressure tower for first group and carry out cryogenic separation, second group is carried out indirect heat exchange with above-mentioned secondary oxygen enrichment fraction, with above-mentioned secondary oxygen enrichment fraction and the second group of above-mentioned air feed fraction of condensation at least a portion of evaporation at least a portion.
Second group of air feed of above-mentioned condensation carried out indirect heat exchange with the above-mentioned once rich nitrogen fraction of condensation and evaporate second group of air feed of above-mentioned condensation with an above-mentioned oxygen enrichment fraction.
Second group of air feed of above-mentioned evaporation introduced above-mentioned lower pressure column carry out cryogenic separation.
5, the low temperature process of production nitrogen comprises from air:
A) the cold compression air feed with essentially no mixture and impurity is divided into two groups;
B) with high-pressure tower that evaporator overhead condenser is housed of above-mentioned first group of air input;
C) in above-mentioned high-pressure tower, adopt the low temperature distillation method that first group of above-mentioned air separation become an once rich nitrogen fraction and an oxygen enrichment fraction;
D) in above-mentioned high-pressure tower, take out an above-mentioned oxygen enrichment fraction of a part at least;
E) introduce the lower pressure column that bottom condensation one reboiler and evaporated on top one condenser are housed to an above-mentioned oxygen enrichment fraction of major general's part, carry out cryogenic separation there, be divided into the rich nitrogen fraction of a secondary and a secondary oxygen enrichment fraction;
F) second group of above-mentioned air feed introduced interior condensation one reboiler of above-mentioned lower pressure column;
G) by in above-mentioned lower pressure column, carrying out indirect heat exchange with second group of above-mentioned air feed condensation with above-mentioned secondary oxygen enrichment fraction.Have at least the above-mentioned secondary oxygen enrichment fraction of part to obtain evaporation there;
H) have at least second group of air feed of the above-mentioned condensation of part to be admitted to the evaporator overhead condenser of above-mentioned high-pressure tower;
I) have at least the air feed of second group of above-mentioned condensation of part in the evaporator overhead condenser of above-mentioned high-pressure tower, to obtain evaporation by carrying out indirect heat exchange at least partially in the once rich nitrogen fraction in the high-pressure tower together, like this, have at least the above-mentioned once rich nitrogen fraction of part to obtain condensation;
J) have at least the above-mentioned second group of air feed that partly carries out indirect heat exchange and evaporate to be imported into above-mentioned lower pressure column with the once rich nitrogen fraction in the above-mentioned high-pressure tower evaporator overhead condenser, purpose is to carry out cryogenic separation together with an above-mentioned oxygen enrichment fraction of at least a portion, is divided into the rich nitrogen fraction of a secondary and a secondary oxygen enrichment fraction;
K) have at least the enterprising rich nitrogen fraction of part in above-mentioned lower pressure column, to take out as product.
L) have at least the oxygen enrichment fraction of the above-mentioned time condensation of part in above-mentioned lower pressure column, to take out;
M) introduce the evaporator overhead condenser of above-mentioned lower pressure column to the oxygen enrichment fraction of the above-mentioned taking-up of major general's part;
N) have the above-mentioned secondary oxygen enrichment fraction of part at least by evaporating, make the rich nitrogen fraction condensation of above-mentioned secondary and provide backflow for lower pressure column there with carrying out indirect heat exchange at least partially in the rich nitrogen fraction of the secondary that rises in the above-mentioned lower pressure column;
O) have at least the secondary oxygen enrichment fraction of part evaporation to be discharged from as refuse from above-mentioned evaporator overhead condenser.
6, the desired method of claim 5 also comprises:
Have at least the once rich nitrogen fraction of the above-mentioned condensation of part to discharge from above-mentioned high-pressure tower as the elevated pressure nitrogen product.
7, the method for claim 5 requirement also comprises:
Have at least the once rich nitrogen fraction of the above-mentioned condensation of part to take from above-mentioned high-pressure tower, and have at least the once rich nitrogen fraction of the above-mentioned condensation that is removed of part to be admitted to above-mentioned lower pressure column.
8, the method for claim 5 requirement also comprises:
Further above-mentioned compression air feed is divided into three air feed fractions;
Expand so that cooling to be provided to three times above-mentioned air feed fractions of major general's part; And
Send into above-mentioned lower pressure column to the above-mentioned dilated air feed fraction of major general's part.
9, the method for claim 6 requirement further comprises:
The above-mentioned useless oxygen that has at least part to take from evaporator overhead condenser is subjected to expanding so that factory's cooling to be provided.
10, the method for claim 6 requirement also comprises:
Have at least the above-mentioned high-pressure tower product of part before discharging, to be expanded with above-mentioned low pressure nitrogen product.
11, the method for claim 5 requirement further comprises:
Connect heat exchange in the ranks and make the cooling of above-mentioned air feed with flowing to waste gas and product, and
Compress above-mentioned air feed make in high-pressure tower, obtain one be approximately 2～20 the crust pressure.
12, the method for claim 5 requirement comprises:
Above-mentioned at B) in first group of air feed be admitted to the Lower Half of above-mentioned high-pressure tower; And
Above-mentioned at D) in an oxygen enrichment fraction be removed from above-mentioned high-pressure tower bottom.
13, the method for claim 5 requirement comprises:
Above-mentioned at E) in an oxygen enrichment fraction be introduced into the Lower Half of above-mentioned lower pressure column; And
Above-mentioned at N) in secondary oxygen enrichment fraction take out from the bottom of above-mentioned lower pressure column.
14, the method for claim 5 requirement further comprises:
With Q) in the above-mentioned useless oxygen that obtains by the pulley expander so that cooling to be provided; And
Contact the useless oxygen heating that makes from the cooling of pulley expander by carry out indirect heat exchange with air feed.
15, the equipment by the compressed air production nitrogen that cools off comprises:
A single flash tower is wherein equipped one for the compression air feed that makes the above-mentioned cooling of part carries out the tower condenser in top of cryogenic separation by rectifying, and it is divided into an once rich nitrogen fraction and an oxygen enrichment fraction with air feed.
An after-fractionating tower, wherein be equipped with a tower condenser in top and the tower reboiler in bottom, they be used for a oxygen enrichment that the cold compression air feed of part after by the circulation of the tower condenser in the top of the tower reboiler in above-mentioned bottom and after-fractionating tower and single flash tower obtained from the single flash tower in company with part together rectifying isolate a secondary oxygen enrichment fraction and the rich nitrogen fraction of secondary.
Above-mentioned once with after-fractionating tower in plumbing installation, they are used to import the steam with extracting liq.
Contact once with the plumbing installation of after-fractionating tower, they are used for input and extracting liq and steam.
With the plumbing installation that the tower reboiler in the bottom of after-fractionating tower links to each other, they are used for direct cold compression air feed.
With the plumbing installation that the tower reboiler in the bottom of above-mentioned after-fractionating tower links to each other with the tower condenser in the top of single flash tower, the evaporator overhead condenser that they are used for the condensation air feed from the after-fractionating tower reboiler is transferred to the single flash tower goes.
With once steam coagulating the plumbing installation that tower links to each other with the tower condenser in the top of time condensation tower, they are used to extract from the gasification air of tower the condenser in the top of single flash tower and it are sent into after-fractionating tower compare and just carry out cryogenic separation; And
The plumbing installation that a same destilling tower links to each other with after-fractionating tower, they are used for extracting oxygen enrichment fraction of part and it being sent into after-fractionating tower from the single flash tower bottom, so that carry out cryogenic separation.
16, the equipment of claim 15 requirement also comprises:
With the continuous plumbing installation of the tower condenser in the top of after-fractionating tower and after-fractionating tower, they are used for above-mentioned oxygen enrichment fraction is taken out the back and it is sent into the tower condenser in top of after-fractionating tower from after-fractionating tower, so that carry out indirect heat exchange with the steam that rises in the after-fractionating tower.
With the plumbing installation that the tower condenser in the top of after-fractionating tower links to each other, they are used for the secondary oxygen enrichment is taken out as waste gas; And
The plumbing installation that a same destilling tower links to each other with after-fractionating tower, they are used for the rich nitrogen fraction taking-up of single flash tower and send into after-fractionating tower, so that the backflow of after-fractionating tower to be provided.
17, the equipment of claim 16 requirement also comprises:
The compression set that the air of importing from outer source of the gas for compression uses;
Remove the purifying plant of carbon dioxide, water vapour and other impurity in the compressed air;
Reach the heat-exchange device of low temperature from the compressed air of purifying plant for cooling;
With the plumbing installation that the after-fractionating tower evaporator overhead condenser links to each other, they are used for extraction and guiding liquids and steam;
The plumbing installation that same heat exchanger, single flash tower, after-fractionating tower link to each other, they are used for direct cold compression air feed;
Valving in the aforementioned tube duct device, they are used to regulate steam and liquid.By them, steam and liquid also can obtain expanding.
18, the equipment of claim 15 requirement also comprises:
With the plumbing installation that above-mentioned single flash tower links to each other with heat exchanger, they are used to extract the nitrogen product.
19, the equipment of claim 18 requirement also comprises:
With the expansion gear that above-mentioned plumbing installation links to each other, they are used to make part nitrogen product to expand so that cooling to be provided.
20, the equipment of claim 15 requirement also comprises:
The expansion gear of useless oxygen is used to expand.
21, the equipment of claim 15 requirement also comprises:
For the compression cold air before importing the time condensation tower of expanding so that the expansion gear of cooling to be provided.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US89/03926 | 1989-09-12 | ||
| PCT/US1989/003926 WO1993013373A1 (en) | 1989-09-12 | 1989-09-12 | Cryogenic air separation process and apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1050260A true CN1050260A (en) | 1991-03-27 |
Family
ID=22215224
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN90107623A Pending CN1050260A (en) | 1989-09-12 | 1990-09-11 | Cryogenic air separation process and equipment |
Country Status (10)
| Country | Link |
|---|---|
| EP (1) | EP0418139B1 (en) |
| JP (1) | JPH03170785A (en) |
| CN (1) | CN1050260A (en) |
| AU (1) | AU643232B2 (en) |
| CA (1) | CA2025013A1 (en) |
| DE (1) | DE69004647T2 (en) |
| ES (1) | ES2046740T3 (en) |
| RU (1) | RU2069293C1 (en) |
| WO (1) | WO1993013373A1 (en) |
| ZA (1) | ZA907188B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102042742A (en) * | 2009-10-09 | 2011-05-04 | 林德股份公司 | Method and device for generating liquid nitrogen from low temperature air separation |
| CN106595222A (en) * | 2015-10-20 | 2017-04-26 | 林德股份公司 | Plate heat exchanger-capacitor evaporator and method for cryogenic decomposition of air |
| CN112654827A (en) * | 2018-10-09 | 2021-04-13 | 林德有限责任公司 | Method and air separation plant for extracting one or more air products |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0836323B1 (en) * | 1991-02-20 | 2004-01-14 | Hitachi, Ltd. | Television telephone |
| US5257504A (en) * | 1992-02-18 | 1993-11-02 | Air Products And Chemicals, Inc. | Multiple reboiler, double column, elevated pressure air separation cycles and their integration with gas turbines |
| US5251450A (en) * | 1992-08-28 | 1993-10-12 | Air Products And Chemicals, Inc. | Efficient single column air separation cycle and its integration with gas turbines |
| US5251451A (en) * | 1992-08-28 | 1993-10-12 | Air Products And Chemicals, Inc. | Multiple reboiler, double column, air boosted, elevated pressure air separation cycle and its integration with gas turbines |
| DE19819263C2 (en) * | 1998-04-30 | 2003-08-21 | Linde Ag | Process and device for the production of pressurized nitrogen |
| CN109297260A (en) * | 2018-10-17 | 2019-02-01 | 浙江海天气体有限公司 | A kind of full nitrogen space division waste gas recovering device processed |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU523019B2 (en) * | 1978-05-25 | 1982-07-08 | Commonwealth Industrial Gases Limited, The | Separation of air |
| JPS58198677A (en) * | 1982-05-14 | 1983-11-18 | 株式会社日立製作所 | Method and device for separating air |
| US4582518A (en) * | 1984-09-26 | 1986-04-15 | Erickson Donald C | Nitrogen production by low energy distillation |
| US4707994A (en) * | 1986-03-10 | 1987-11-24 | Air Products And Chemicals, Inc. | Gas separation process with single distillation column |
| GB8800842D0 (en) * | 1988-01-14 | 1988-02-17 | Boc Group Plc | Air separation |
-
1989
- 1989-09-12 WO PCT/US1989/003926 patent/WO1993013373A1/en unknown
-
1990
- 1990-09-10 ZA ZA907188A patent/ZA907188B/en unknown
- 1990-09-10 CA CA002025013A patent/CA2025013A1/en not_active Abandoned
- 1990-09-11 JP JP2241040A patent/JPH03170785A/en active Pending
- 1990-09-11 ES ES199090402488T patent/ES2046740T3/en not_active Expired - Lifetime
- 1990-09-11 EP EP90402488A patent/EP0418139B1/en not_active Expired - Lifetime
- 1990-09-11 AU AU62375/90A patent/AU643232B2/en not_active Ceased
- 1990-09-11 CN CN90107623A patent/CN1050260A/en active Pending
- 1990-09-11 RU SU904830924A patent/RU2069293C1/en active
- 1990-09-11 DE DE90402488T patent/DE69004647T2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102042742A (en) * | 2009-10-09 | 2011-05-04 | 林德股份公司 | Method and device for generating liquid nitrogen from low temperature air separation |
| CN106595222A (en) * | 2015-10-20 | 2017-04-26 | 林德股份公司 | Plate heat exchanger-capacitor evaporator and method for cryogenic decomposition of air |
| CN112654827A (en) * | 2018-10-09 | 2021-04-13 | 林德有限责任公司 | Method and air separation plant for extracting one or more air products |
| CN112654827B (en) * | 2018-10-09 | 2022-12-06 | 林德有限责任公司 | Method and air separation plant for extracting one or more air products |
Also Published As
| Publication number | Publication date |
|---|---|
| ES2046740T3 (en) | 1994-02-01 |
| RU2069293C1 (en) | 1996-11-20 |
| DE69004647T2 (en) | 1994-03-10 |
| EP0418139A1 (en) | 1991-03-20 |
| DE69004647D1 (en) | 1993-12-23 |
| ZA907188B (en) | 1991-09-25 |
| EP0418139B1 (en) | 1993-11-18 |
| AU643232B2 (en) | 1993-11-11 |
| JPH03170785A (en) | 1991-07-24 |
| WO1993013373A1 (en) | 1993-07-08 |
| AU6237590A (en) | 1991-03-21 |
| CA2025013A1 (en) | 1991-03-13 |
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