EP1209431A1 - Process and apparatus for the production of nitrogen and oxygen - Google Patents
Process and apparatus for the production of nitrogen and oxygen Download PDFInfo
- Publication number
- EP1209431A1 EP1209431A1 EP01127958A EP01127958A EP1209431A1 EP 1209431 A1 EP1209431 A1 EP 1209431A1 EP 01127958 A EP01127958 A EP 01127958A EP 01127958 A EP01127958 A EP 01127958A EP 1209431 A1 EP1209431 A1 EP 1209431A1
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- Prior art keywords
- pressure column
- low pressure
- nitrogen
- oxygen
- liquid
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- 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.)
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Classifications
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
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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
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
- F25J3/04412—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 in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high 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
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
Definitions
- the invention relates to a process for the production of oxygen and nitrogen Cryogenic air separation in a rectification system that includes a pressure column and has a low pressure column, with the process feed air into the pressure column initiated, an oxygen-containing liquid fraction removed from the pressure column and is fed into the low pressure column, gaseous nitrogen from the Low pressure column in a top condenser by indirect heat exchange with an evaporating cooling fluid is at least partially condensed Low pressure column and / or a nitrogen product stream removed from the pressure column and an oxygen product stream is discharged from the low pressure column.
- EP 1022530 A1 Methods with head cooling of the low pressure column are known from EP 1022530 A1, WO 9819122 or EP 811816 A2 known.
- a process of the type mentioned at the outset is shown in EP 955509 A1.
- the invention has for its object a method of the type mentioned and specify a corresponding device that is particularly economical work.
- cooling fluid for the top condenser Low pressure column is formed by an intermediate liquid, which is from a Intermediate point of the low pressure column is withdrawn.
- this cooling liquid is caused by the bottom liquid Pressure column formed.
- the invention has two advantages.
- the composition of the cooling fluid can be chosen so that the Product yield, in particular the oxygen yield is increased.
- the cooling fluid has a lower pressure so that it is before it is introduced into the Head capacitor only has to be throttled relatively slightly; corresponding the flash gas losses are lower.
- the intermediate liquid, which is used as cooling fluid in the top condenser, from an intermediate point is subtracted, which is above the point at which the oxygen-containing liquid Fraction from the pressure column is fed into the low pressure column. Between there are, for example, 10 to 20 theoretical floors.
- the process can use liquid nitrogen from or from the low pressure column Top condenser removed and discharged as a liquid nitrogen product.
- the process preferably has a nitrogen cycle on.
- cycle nitrogen becomes gaseous from the upper area of the pressure column withdrawn and compressed in a circuit compressor, a first partial flow of compressed cycle nitrogen is relieved of work and a second Partial stream of the compressed cycle nitrogen liquefied and into the rectification system fed back and / or taken as a further liquid nitrogen product.
- Such a cycle can also be carried out without oxygen production, for example with Use of the bottom liquid from low pressure column or pressure column as cooling fluid in the top condenser of the low pressure column.
- the liquefied circulating nitrogen can be one of the Columns of the rectification system are fed, preferably the pressure column. The the corresponding amount can then be a liquid nitrogen and / or oxygen product be withdrawn from the rectification system.
- Top nitrogen from the pressure column is liquefied in a main condenser. That included generated condensate is at least partially, preferably largely, as Return to the pressure column abandoned. Another part of the condensate can be on top introduced into the low pressure column and / or immediately as a liquid nitrogen product subtracted from.
- the circuit can be designed as a two or more turbine system by one third partial stream of compressed cycle nitrogen independent of the first Partial stream is relaxed while working.
- the invention also relates to a device according to claim 8 or 9.
- An oxygen-containing liquid fraction (8) from the bottom of the pressure column is in one Cooled subcooler 9 and via line 10 at an intermediate point in the Low pressure column 5 initiated.
- gaseous top nitrogen is converted into a first part 11 in Main condenser 6 at least partially, preferably completely liquefied.
- the the condensate 12 produced thereby becomes a first part 13 as a return flow onto the head the pressure column 4 abandoned.
- a second part 14 of the main capacitor 6 condensed nitrogen 11 is introduced into the low pressure column.
- liquid nitrogen 19 is drawn off and on Separation of flash gas in a separator 20 via line 21 as a liquid Withdrawn nitrogen product and introduced a tank 22.
- the flash gas 23 is the Residual gas 16 admixed.
- the residual mixture 24 is in the subcoolers 25, 9 and Main heat exchanger 2 warmed up and finally via line 27 into the atmosphere blown off and / or as a regeneration gas for the device, not shown Purification of the feed air used.
- a second partial stream of the compressed cycle nitrogen is passed through line 42 two series-connected post-compressors 43, 45, each of which has an after-cooler 44, 46 follows.
- the second partial flow continues to the first circuit heat exchanger 37 (Line 47), is further cooled in the second circuit heat exchanger 40 and finally liquefied or - in the third circuit heat exchanger 48 supercritical pressure - pseudo-liquefied.
- a third partial flow of the compressed cycle nitrogen is combined with the second partial flow through the post-compressors 43, 45 and the first and second Circuit heat exchanger 37, 40 out.
- the third substream 56 becomes one cold turbine 57 led.
- the work-relieved, relaxed third partial flow overflows Line 58 through the three circuit heat exchangers 48, 40, 37 to the entry of Circuit compressor back.
- the cold parts of the system are in an insulating housing (cold box) 64 arranged.
- the bottom liquid 8, 10 from the pressure column 4th also be introduced into the low pressure column 5 directly above the sump, the simultaneously represents the evaporation space of the main condenser 6.
- the cooling fluid 15 for the top condenser 7 either from the bottom of the Low pressure column withdrawn or directly from the pressure column sump liquid 10 are branched off.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Catalysts (AREA)
Abstract
Description
Die Erfindung betrifft ein Verfahren zur Erzeugung von Sauerstoff und Stickstoff durch Tieftemperaturzerlegung von Luft in einem Rektifiziersystem, das eine Drucksäule und eine Niederdrucksäule aufweist, wobei bei dem Verfahren Einsatzluft in die Drucksäule eingeleitet, eine sauerstoffhaltige flüssige Fraktion aus der Drucksäule entnommen und in die Niederdrucksäule eingespeist wird, gasförmiger Stickstoff aus der Niederdrucksäule in einem Kopfkondensator durch indirekten Wärmeaustausch mit einem verdampfenden Kühlfluid mindestens teilweise kondensiert wird, der Niederdrucksäule und/oder der Drucksäule ein Stickstoff-Produktstrom entnommen und aus der Niederdrucksäule ein Sauerstoff-Produktstrom abgeführt wird.The invention relates to a process for the production of oxygen and nitrogen Cryogenic air separation in a rectification system that includes a pressure column and has a low pressure column, with the process feed air into the pressure column initiated, an oxygen-containing liquid fraction removed from the pressure column and is fed into the low pressure column, gaseous nitrogen from the Low pressure column in a top condenser by indirect heat exchange with an evaporating cooling fluid is at least partially condensed Low pressure column and / or a nitrogen product stream removed from the pressure column and an oxygen product stream is discharged from the low pressure column.
Verfahren mit Kopfkühlung der Niederdrucksäule sind aus EP 1022530 A1,
WO 9819122 oder EP 811816 A2 bekannt. Ein Prozess der eingangs genannten Art ist
in EP 955509 A1 gezeigt.Methods with head cooling of the low pressure column are known from EP 1022530 A1,
WO 9819122 or EP 811816 A2 known. A process of the type mentioned at the outset is shown in EP 955509 A1.
Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art und eine entsprechende Vorrichtung anzugeben, die wirtschaftlich besonders günstig arbeiten.The invention has for its object a method of the type mentioned and specify a corresponding device that is particularly economical work.
Diese Aufgabe wird dadurch gelöst, dass das Kühlfluid für den Kopfkondensator der Niederdrucksäule durch eine Zwischenflüssigkeit gebildet wird, die von einer Zwischenstelle der Niederdrucksäule abgezogen wird.This object is achieved in that the cooling fluid for the top condenser Low pressure column is formed by an intermediate liquid, which is from a Intermediate point of the low pressure column is withdrawn.
Bei EP 955509 A1 wird diese Kühlflüssigkeit dagegen durch die Sumpfflüssigkeit der Drucksäule gebildet. Im Vergleich hierzu weist die Erfindung zwei Vorteile auf. Zum einen kann die Zusammensetzung des Kühlfluids so gewählt werden, dass die Produktausbeute, insbesondere die Sauerstoffausbeute erhöht wird. Zum anderen weist das Kühlfluid einen niedrigeren Druck auf, sodass es vor seiner Einleitung in den Kopfkondensator nur relativ geringfügig abgedrosselt werden muss; entsprechend geringer sind die Flashgas-Verluste. In EP 955509 A1, on the other hand, this cooling liquid is caused by the bottom liquid Pressure column formed. In comparison, the invention has two advantages. To the On the one hand, the composition of the cooling fluid can be chosen so that the Product yield, in particular the oxygen yield is increased. On the other hand the cooling fluid has a lower pressure so that it is before it is introduced into the Head capacitor only has to be throttled relatively slightly; corresponding the flash gas losses are lower.
Zur Optimierung der Sauerstoffausbeute ist es günstig, wenn die Zwischenflüssigkeit, die als Kühlfluid im Kopfkondensator eingesetzt wird, von einer Zwischenstelle abgezogen wird, die oberhalb der Stelle liegt, an der die sauerstoffhaltige flüssige Fraktion aus der Drucksäule in die Niederdrucksäule eingespeist wird. Dazwischen liegen beispielsweise 10 bis 20 theoretische Böden.To optimize the oxygen yield, it is advantageous if the intermediate liquid, which is used as cooling fluid in the top condenser, from an intermediate point is subtracted, which is above the point at which the oxygen-containing liquid Fraction from the pressure column is fed into the low pressure column. Between there are, for example, 10 to 20 theoretical floors.
Bei dem Verfahren kann flüssiger Stickstoff aus der Niederdrucksäule oder aus deren Kopfkondensator abgezogen und als flüssiges Stickstoffprodukt abgeführt werden. Insbesondere in diesem Fall weist der Prozess vorzugsweise einen Stickstoff-Kreislauf auf. Dabei wird Kreislauf-Stickstoff gasförmig aus dem oberen Bereich der Drucksäule abgezogen und in einem Kreislauf-Verdichter verdichtet, wobei ein erster Teilstrom des verdichteten Kreislauf-Stickstoffs arbeitsleistend entspannt wird und ein zweiter Teilstrom des verdichteten Kreislauf-Stickstoffs verflüssigt und in das Rektifiziersystem zurückgespeist und/oder als weiteres flüssiges Stickstoffprodukt entnommen wird. Ein derartiger Kreislauf kann auch ohne Sauerstoffproduktion, beispielsweise mit Verwendung der Sumpfflüssigkeit von Niederdrucksäule oder Drucksäule als Kühlfluid im Kopfkondensator der Niederdrucksäule, eingesetzt werden.The process can use liquid nitrogen from or from the low pressure column Top condenser removed and discharged as a liquid nitrogen product. In this case in particular, the process preferably has a nitrogen cycle on. Here, cycle nitrogen becomes gaseous from the upper area of the pressure column withdrawn and compressed in a circuit compressor, a first partial flow of compressed cycle nitrogen is relieved of work and a second Partial stream of the compressed cycle nitrogen liquefied and into the rectification system fed back and / or taken as a further liquid nitrogen product. On Such a cycle can also be carried out without oxygen production, for example with Use of the bottom liquid from low pressure column or pressure column as cooling fluid in the top condenser of the low pressure column.
Durch die arbeitsleistende Entspannung des ersten Teilstroms des Kreislauf-Stickstoffs wird Kälte erzeugt, die über den verflüssigten zweiten Teilstrom weitertransportiert und zur Erhöhung der Flüssigproduktion eingesetzt werden kann. Die Flüssigkeit aus dem Kreislauf kann beispielsweise direkt als flüssiges Stickstoff-Produkt abgezogen werden. Altemativ oder zusätzlich kann der verflüssigte Kreislauf-Stickstoff einer der Säulen des Rektifiziersystems zugespeist werden, vorzugsweise der Drucksäule. Die entsprechende Menge kann dann als flüssiges Stickstoff- und/oder Sauerstoff-Produkt aus dem Rektifiziersystem abgezogen werden.Due to the relaxation of the first partial flow of circulating nitrogen refrigeration is generated, which is transported via the liquefied second partial flow and can be used to increase liquid production. The liquid from the The cycle can be drawn off directly as a liquid nitrogen product, for example become. Alternatively or additionally, the liquefied circulating nitrogen can be one of the Columns of the rectification system are fed, preferably the pressure column. The the corresponding amount can then be a liquid nitrogen and / or oxygen product be withdrawn from the rectification system.
Kopfstickstoff der Drucksäule wird in einem Hauptkondensator verflüssigt. Das dabei erzeugte Kondensat wird mindestens zum Teil, vorzugsweise zum größten Teil, als Rücklauf auf die Drucksäule aufgegeben. Ein weiterer Teil des Kondensats kann oben in die Niederdrucksäule eingeleitet und/oder unmittelbar als flüssiges Stickstoffprodukt abgezogen werden. Top nitrogen from the pressure column is liquefied in a main condenser. That included generated condensate is at least partially, preferably largely, as Return to the pressure column abandoned. Another part of the condensate can be on top introduced into the low pressure column and / or immediately as a liquid nitrogen product subtracted from.
Der Kreislauf kann als Zwei- oder Mehr-Turbinen-System ausgeführt sein, indem ein dritter Teilstrom des verdichteten Kreislauf-Stickstoffs unabhängig vom ersten Teilstrom arbeitsleistend entspannt wird.The circuit can be designed as a two or more turbine system by one third partial stream of compressed cycle nitrogen independent of the first Partial stream is relaxed while working.
Die Erfindung betrifft außerdem eine Vorrichtung gemäß Patentanspruch 8
beziehungsweise 9.The invention also relates to a device according to
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand eines in der Zeichnung dargestellten Ausführungsbeispiels näher erläutert.The invention and further details of the invention are described below of an embodiment shown in the drawing.
Verdichtete und gereinigte Einsatzluft strömt über Leitung 1 in einen
Hauptwärmetauscher 2 und wird dort auf etwa Taupunkt abgekühlt. Über Leitung 3
wird die kalte Luft der Drucksäule 4 des Rektifiziersystems zugeführt, das aus der
Drucksäule 4, der Niederdrucksäule 5, dem Hauptkondensator 6 und dem
Kopfkondensator 7 besteht.Compressed and cleaned feed air flows into a
Eine sauerstoffhaltige flüssige Fraktion (8) vom Sumpf der Drucksäule wird in einem
Unterkühler 9 abgekühlt und über Leitung 10 an einer Zwischenstelle in die
Niederdrucksäule 5 eingeleitet.An oxygen-containing liquid fraction (8) from the bottom of the pressure column is in one
Am Kopf der Drucksäule 4 wird gasförmiger Kopfstickstoff zu einem ersten Teil 11 im
Hauptkondensator 6 mindestens teilweise, vorzugsweise vollständig verflüssigt. Das
dabei erzeugte Kondensat 12 wird zu einem ersten Teil 13 als Rücklauf auf den Kopf
der Drucksäule 4 aufgegeben. Ein zweiter Teil 14 des im Hauptkondensator 6
kondensierten Stickstoffs 11 wird in die Niederdrucksäule eingeleitet.At the top of the
Vom Sumpf der Niederdrucksäule, der gleichzeitig den Verdampfungsraum des
Hauptkondensators 6 darstellt, wird ein flüssiger Sauerstoff-Produktstrom 61
abgezogen. Eine Restmenge 62 Sauerstoffs wird dem unteren Teil der
Niederdrucksäule gasförmig entnommen, im Hauptwärmetauscher 2 angewärmt und
schließlich über Leitung 63 in Richtung des Verbrauchers abgegeben. In dem Beispiel
erfolgt der Produkt-Abzug aus der Säule hauptsächlich in Flüssigform; alternativ oder
zusätzlich könnte der Sauerstoff-Produktstrom gasförmig aus der Säule herausgeführt
werden. Bei Flüssigabzug ist anschließend ist eine Nutzung als Flüssigprodukt -
gegebenenfalls nach Unterkühlung - und/oder eine Verdampfung - beispielsweise unter
erhöhtem Druck - möglich. Eine derartige Verdampfung kann durch indirekten
(Nebenkondensator oder Innenverdichtung) oder direkten Wärmeaustausch
(Mischsäule) durchgeführt werden.From the sump of the low pressure column, which also the evaporation chamber of the
Represents
Von einer Zwischenstelle der Niederdrucksäule 5, die in dem Beispiel zwölf praktische
oder neun theoretische Böden oberhalb der Zuspeisung der Drucksäulen-Sumpfflüssigkeit
10 liegt, wird ein Kühlfluid 15 in flüssiger Form abgezogen, unterkühlt
(25) und in den Verdampfungsraum des Kopfkondensators 7 der Niederdrucksäule
geführt. Dort verdampft es bis auf eine kleine Spülmenge 60 vollständig und wird
schließlich über Leitung 16 als Restgas abgezogen. Im Verflüssigungsraum des
Kopfkondensators 7 wird gasförmiger Stickstoff 17 vom Kopf der Niederdrucksäule
mindestens teilweise, vorzugsweise vollständig verflüssigt und über Leitung 18 in die
Niederdrucksäule 5 zurückgespeist.From an intermediate point of the
Am Kopf der Niederdrucksäule wird flüssiger Stickstoff 19 abgezogen und nach
Abtrennung von Flashgas in einem Abscheider 20 über Leitung 21 als flüssiges
Stickstoffprodukt abgezogen und einen Tank 22 eingeleitet. Das Flashgas 23 wird dem
Restgas 16 zugemischt. Das Restgemisch 24 wird in den Unterkühlern 25, 9 und im
Hauptwärmetauscher 2 angewärmt und schließlich über Leitung 27 in die Atmosphäre
abgeblasen und/oder als Regeneriergas für die nicht dargestellte Vorrichtung zur
Reinigung der Einsatzluft verwendet.At the top of the low pressure column,
Vom Kopf der Drucksäule wird über Leitung 28 Kreislauf-Stickstoff entnommen, zum
Hauptwärmetauscher 2 geführt (29), dort auf etwa Umgebungstemperatur angewärmt
und über die Leitungen 30, 31, 32 zum Eintritt eines Kreislauf-Verdichters 33 geführt.
(Dieser Drucksäulen-Stickstoff 28 stellt vorzugsweise die einzige Zufuhr zum Stickstoff-Kreislauf
dar; auf einen Feedgas-Verdichter zum Einführen von Niederdruck-Stickstoff
in den Kreislauf kann somit verzichtet werden.) Stromabwärts eines Nachkühlers 34
wird ein erster Teilstrom 36 des verdichteten Kreislauf-Stickstoffs 35 abgetrennt, in
einem ersten Kreislauf-Wärmetauscher 37 auf eine erste Zwischentemperatur
abgekühlt und in einer warmen Turbine 38 arbeitsleistend entspannt. Das Abgas 39
der warmen Turbine 38 wird in einem zweiten Kreislauf-Wärmetauscher 40 und im
ersten Kreislauf-Wärmetauscher 37 wieder angewärmt und zum Kreislaufverdichter 33
zurückgeführt (Leitungen 41, 32). From the top of the
Über Leitung 42 wird ein zweiter Teilstrom des verdichteten Kreislauf-Stickstoffs durch
zwei seriell geschaltete Nachverdichter 43, 45 geführt, denen jeweils ein Nachkühler
44, 46 folgt. Der zweite Teilstrom fließt weiter zum ersten Kreislauf-Wärmetauscher 37
(Leitung 47), wird im zweiten Kreislauf-Wärmetauscher 40 weiter abgekühlt und
schließlich im dritten Kreislauf-Wärmetauscher 48 verflüssigt beziehungsweise - bei
überkritischem Druck - pseudo-verflüssigt. Nach Entspannung auf etwa Drucksäulen-Druck
in einem Drosselventil 49 wird der verflüssigte zweite Teilstrom 50, 52 - nach
Abtrennung gasförmiger Bestandteile in einem Abscheider 51 - in die Drucksäule 4
eingeführt (52). Flashgas 53 aus dem Abscheider 51 wird über die Leitungen 54
und/oder 55 zum Kreislauf-Verdichter 33 zurückgeführt.A second partial stream of the compressed cycle nitrogen is passed through
Ein dritter Teilstrom des verdichteten Kreislauf-Stickstoffs wird gemeinsam mit dem
zweiten Teilstrom durch die Nachverdichter 43, 45 und den ersten und zweiten
Kreislauf-Wärmetauscher 37, 40 geführt. Bei einer zweiten Zwischentemperatur, die
niedriger als die erste Zwischentemperatur ist, wird der dritte Teilstrom 56 zu einer
kalten Turbine 57 geführt. Der arbeitsleistend entspannte dritte Teilstrom strömt über
Leitung 58 durch die drei Kreislauf-Wärmetauscher 48, 40, 37 zum Eintritt des
Kreislauf-Verdichters zurück.A third partial flow of the compressed cycle nitrogen is combined with the
second partial flow through the post-compressors 43, 45 and the first and second
Die kalten Teile der Anlage sind in einem isolierenden Gehäuse (Coldbox) 64 angeordnet.The cold parts of the system are in an insulating housing (cold box) 64 arranged.
Bei dem Ausführungsbeispiel sind verschiedene Abwandlungen denkbar. Falls kein
Sauerstoffprodukt gewünscht ist, kann die Sumpfflüssigkeit 8, 10 von der Drucksäule 4
auch unmittelbar über dem Sumpf in die Niederdrucksäule 5 eingeleitet werden, der
gleichzeitig den Verdampfungsraum des Hauptkondensators 6 darstellt. In diesem Fall
würde das Kühlfluid 15 für den Kopfkondensator 7 entweder aus dem Sumpf der
Niederdrucksäule abgezogen oder unmittelbar aus der Drucksäulen-Sumpfflüssigkeit
10 abgezweigt werden.Various modifications are conceivable in the exemplary embodiment. If not
Oxygen product is desired, the
Claims (9)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10058332A DE10058332A1 (en) | 2000-11-24 | 2000-11-24 | Method and device for generating oxygen and nitrogen |
DE10058332 | 2000-11-24 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1209431A1 true EP1209431A1 (en) | 2002-05-29 |
EP1209431B1 EP1209431B1 (en) | 2004-06-09 |
Family
ID=7664493
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP01127958A Expired - Lifetime EP1209431B1 (en) | 2000-11-24 | 2001-11-23 | Process and apparatus for the production of nitrogen and oxygen |
Country Status (4)
Country | Link |
---|---|
US (1) | US6490884B2 (en) |
EP (1) | EP1209431B1 (en) |
AT (1) | ATE268893T1 (en) |
DE (2) | DE10058332A1 (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20150168058A1 (en) * | 2013-12-17 | 2015-06-18 | L'air Liquide, Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Apparatus for producing liquid nitrogen |
US20150168057A1 (en) * | 2013-12-17 | 2015-06-18 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process for producing liquid nitrogen |
CN109676367A (en) * | 2018-12-28 | 2019-04-26 | 乔治洛德方法研究和开发液化空气有限公司 | A kind of method of heat exchanger assemblies and the assembly heat exchanger assemblies |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4832719A (en) * | 1987-06-02 | 1989-05-23 | Erickson Donald C | Enhanced argon recovery from intermediate linboil |
US5137559A (en) * | 1990-08-06 | 1992-08-11 | Air Products And Chemicals, Inc. | Production of nitrogen free of light impurities |
WO1998019122A1 (en) * | 1996-10-30 | 1998-05-07 | Linde Aktiengesellschaft | Method and device for producing compressed nitrogen |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4439220A (en) * | 1982-12-02 | 1984-03-27 | Union Carbide Corporation | Dual column high pressure nitrogen process |
US5006139A (en) * | 1990-03-09 | 1991-04-09 | Air Products And Chemicals, Inc. | Cryogenic air separation process for the production of nitrogen |
US5697229A (en) * | 1996-08-07 | 1997-12-16 | Air Products And Chemicals, Inc. | Process to produce nitrogen using a double column plus an auxiliary low pressure separation zone |
US5682762A (en) * | 1996-10-01 | 1997-11-04 | Air Products And Chemicals, Inc. | Process to produce high pressure nitrogen using a high pressure column and one or more lower pressure columns |
EP0955509B1 (en) * | 1998-04-30 | 2004-12-22 | Linde Aktiengesellschaft | Process and apparatus to produce high purity nitrogen |
DE19902255A1 (en) | 1999-01-21 | 2000-07-27 | Linde Tech Gase Gmbh | Process and device for the production of pressurized nitrogen |
-
2000
- 2000-11-24 DE DE10058332A patent/DE10058332A1/en not_active Withdrawn
-
2001
- 2001-11-23 EP EP01127958A patent/EP1209431B1/en not_active Expired - Lifetime
- 2001-11-23 US US09/990,365 patent/US6490884B2/en not_active Expired - Fee Related
- 2001-11-23 DE DE50102525T patent/DE50102525D1/en not_active Expired - Fee Related
- 2001-11-23 AT AT01127958T patent/ATE268893T1/en not_active IP Right Cessation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4832719A (en) * | 1987-06-02 | 1989-05-23 | Erickson Donald C | Enhanced argon recovery from intermediate linboil |
US5137559A (en) * | 1990-08-06 | 1992-08-11 | Air Products And Chemicals, Inc. | Production of nitrogen free of light impurities |
WO1998019122A1 (en) * | 1996-10-30 | 1998-05-07 | Linde Aktiengesellschaft | Method and device for producing compressed nitrogen |
Also Published As
Publication number | Publication date |
---|---|
DE50102525D1 (en) | 2004-07-15 |
EP1209431B1 (en) | 2004-06-09 |
US6490884B2 (en) | 2002-12-10 |
ATE268893T1 (en) | 2004-06-15 |
US20020062658A1 (en) | 2002-05-30 |
DE10058332A1 (en) | 2002-05-29 |
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