DE849850C - Process for the separation of air - Google Patents
Process for the separation of airInfo
- Publication number
- DE849850C DE849850C DEM4587D DEM0004587D DE849850C DE 849850 C DE849850 C DE 849850C DE M4587 D DEM4587 D DE M4587D DE M0004587 D DEM0004587 D DE M0004587D DE 849850 C DE849850 C DE 849850C
- Authority
- DE
- Germany
- Prior art keywords
- pressure column
- air
- liquid
- medium
- oxygen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
-
- 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
-
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
-
- 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/06—Lifting of liquids by gas lift, e.g. "Mammutpumpe"
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
Verfahren zur Zerlegung von Luft Bei der Zerlegung von Luft durch Verflüssigung und Rektifikation wird meist die bekannte doppelte Zerlegung verwandt, da nur nach diesem Verfahren gleichzeitig hohe Reinheiten und gute Ausbeuten der gewünschten Produkte erzielt werden können. Dabei wird die Luft in einer unter Überdruck, im allgemeinen 3,5 bis 5,5 atü, stehenden Kolonne (i. Zerlegungsstufe) in ein mit Sauerstoff angereichertes Gemisch und den sogenannten Waschstickstoff zerlegt, während in einer darüber angeordneten Niederdruckkolonne (2. Zerlegungsstufe) dann eine Zerlegung in fast reinen Sauerstoff und Stickstoff erfolgt. Ein Nachteil dieses Verfahtens ist die große Bauhöhe der beiden übereinandergestellten Kolonnen, die für viele Anwendungszwecke untragbar ist. Man ist deshalb schon seit langer Zeit bestrebt, mit zwei nebeneinander aufgestellten Kolonnen auszukommen, jedoch konnten die bisher vorgeschlagenen Anordnungen noch nicht befriedigen, da sich dabei ohne zusätzliche Hilfsmittel nicht die hohen Reinheiten erreichen ließen, wie im normalen Zweisäulenapparat mit übereinander angeordneten Kolonnen. Es besteht nämlich immer die Schwierigkeit, den unter der Niederdruckkolonne sich sammelnden reinen flüssigen Sauerstoff in den Verdampferraum des Kondensators am oberen Ende der Mitteldruckkolonne zu' heben. Unter Anwendung einer Pumpe für den flüssigen Sauerstoff wäre es zwar möglich diese Nachteile zu überwinden, jedoch ist der Betrieb einer solchen Maschine, in, dem sonst ruhenden Apparat auch unter den erschwerenden Bedingungen der tiefen Temperaturen aus Gründen der Betriebssicherheit unerwünscht.Process for the separation of air In the separation of air by Liquefaction and rectification are usually used in the well-known double decomposition, because only after this process high purities and good yields of the desired products can be achieved. The air is in a pressurized, generally 3.5 to 5.5 atmospheres, standing column (in the decomposition stage) in a with Oxygen-enriched mixture and the so-called scrubbing nitrogen decomposed while then one in a low-pressure column arranged above (2nd decomposition stage) It is broken down into almost pure oxygen and nitrogen. One downside to this The process is the great height of the two stacked columns, the is unsustainable for many uses. That's why you've been around for a long time endeavored to get by with two columns set up side by side, but could the arrangements proposed so far are not yet satisfactory, since doing so without Additional aids did not allow the high purities to be achieved, as in normal Two-column apparatus with columns arranged one above the other. Because it always exists the difficulty of the pure liquid collecting under the low-pressure column Oxygen in the Evaporation chamber of the condenser at the upper end the medium pressure column to 'lift. Using a pump for the liquid Oxygen would be able to overcome these disadvantages, but the operation is such a machine, in the otherwise idle apparatus even among the aggravating ones Conditions of low temperatures are undesirable for reasons of operational safety.
Nach dem Verfahren der vorliegenden Anmeldung wird nun die Hebung des flüssigen SaueYstöffs vom unteren Ende der Ni.ederdruckkolonne bis zum oberen Ende der Mitteldruckkolonne dadurch bewirkt, daß ein Teil des flüssigen Sauerstoffs in einem Verdampfer verdampft wird und durch die Dampfblasen die Flüssigkeit in entsprechender Weise gehoben wird. Als Wärmequelle für die teilweise Verdampfung des flüssigen Sauerstoffs dient dabei vorzugsweise ein Teil des -am oberen E-ti.de der Mitteldruckkolonne gasförmig unter Druck anfallenden Stickstoffs.According to the method of the present application, the elevation of the liquid SaueYstöffs from the lower end of the pressure column to the upper The end of the medium pressure column causes some of the liquid oxygen is evaporated in a vaporizer and through the vapor bubbles the liquid is in is lifted in a corresponding manner. As a heat source for partial evaporation of the liquid oxygen is preferably a part of the -am upper E-ti.de the medium pressure column gaseous under pressure accumulating nitrogen.
Eine beispielsweise Ausführung des Verfahrens der Anmeldung ist in der Abbildung gezeidhnet, wobei nur der eigentliche Zerlegungsvorgang,- nicht aber der vorgeschaltete Wärmeaustausch dargesiellt sind. Die tiefgekühlte und im Gegenstrom zu den Zerlegungsprodukten teilweise verflüssigte Luft tritt durch Leitung L1 in die unter einem Druck von etwa 5 atü arbeitende Mitteldruckkolomne A ein. Der Rücklauf für diese Kolonne wird in dem Kondensator B erzeugt, der außen durch flüssigen Sauerstoff gekühlt ist. In dieser Mitteldruckkolönne erfolgt die Zei#legung in die Vorprodukte Rohsauerstoff (unten) und Wasch@:stickstoff (oben), die durch die Ventile H bzw. K in der Niederdruckkolonne entspannt werden. Hier erfolgt sodann die Zerlegung der Luft in den im Flüssigkeitsbad D sich sammelnden reinen flüssigen Sauerstoff und den durch Leitung N abziehenden gasförmigen Stickstoff. Um nun den flüssigen Sauerstoff vom Boden der Niederdruckkolonne in den Verdampferraum der Mitteldruckkolonne zu heben, ist erfindungsgemäß der Verdampfer E angeordnet. In ihm wird ein Teil des Sauerstoffs durch Beheizung mit gasförmigem Stickstoff, der aus dem oberen Ende der Mitteldruckkolonne abgenommen wird, verdampft. Die entstehenden Gasblasen heben dann, wie in einer Mammutpumpe, die nichtverdampfte Flüssigke-i-tin den Verdampferraum des Kondensators B. In diesem Verdampfer E wird beispielsweise 1/s des aus D kommenden flüssigen Sauerstoffs verdampft. Aus i kg flüssigen Sauerstoff, das bei 1,5 atü einen Raum von o,8o 1 einnimmt, entsteht dann ein Gemisch von o,67 kg = o,6o 1 Flüssigkeit und 0,33 kg = 5.4,6 1 Dampf. Die mittlere Wichte dieses Gemisches beträgt also 1 : 55,2 = o,oo18 kg je Liter. Es ist also 62 mal leichter als der flüssige Sauerstoff und mithinkönnte dieHöhendifferenz zwischen dem Verdampfer E und der Flüssigkeitsoberfläche in B 62mal so groß sein, als die Höhendifferenz zwischen dem Verdampfer E und der Flüssigkeitsoberfläche in D.An example of the implementation of the process of the application is shown in the figure, with only the actual dismantling process, but not the upstream heat exchange, being shown. The deep-frozen air, which is partially liquefied in countercurrent to the decomposition products, enters medium-pressure column A, which operates at a pressure of about 5 atmospheres, through line L1. The reflux for this column is generated in the condenser B, which is cooled on the outside by liquid oxygen. In this medium-pressure column, the primary products crude oxygen (bottom) and scrubbing nitrogen (top), which are depressurized through valves H and K in the low-pressure column, take place. Here then the air is broken down into the pure liquid oxygen that collects in the liquid bath D and the gaseous nitrogen that is withdrawn through line N. In order to lift the liquid oxygen from the bottom of the low-pressure column into the evaporator space of the medium-pressure column, the evaporator E is arranged according to the invention. In it, part of the oxygen is evaporated by heating with gaseous nitrogen, which is taken from the upper end of the medium-pressure column. The resulting gas bubbles then lift the non-evaporated liquid into the evaporator space of the condenser B, as in a mammoth pump. In this evaporator E, for example, 1 / s of the liquid oxygen coming from D is evaporated. From 1 kg of liquid oxygen, which takes up a space of 0.8 o 1 at 1.5 atmospheres, a mixture of o.67 kg = o.6o 1 liquid and 0.33 kg = 5.4.6 1 vapor is created. The mean specific weight of this mixture is 1: 55.2 = 0.018 kg per liter. It is therefore 62 times lighter than liquid oxygen and the difference in height between the evaporator E and the liquid surface in B could be 62 times as great as the height difference between the evaporator E and the liquid surface in D.
Praktisch kann man sich natürlich mit einer wesentlich geringeren Verdampfung begnügen, selbst unter Berücksichtigung aller Strömungswiderstände, die in den Rohrleitungen überwunden werden müssen.In practice, of course, you can deal with a much lower one Satisfy evaporation, even taking into account all flow resistances, which must be overcome in the pipelines.
Um ein Herablaufen des flüssigen Sauerstoffs neben den aufsteigenden Gasblasen in den Steigrohren P möglichst zu vermeiden, ist es vorteilhaft, hierfür Rohre mit kleinen lichten Weiten vorzusehen. Aus diesem Grunde ist es bei größeren zu fördernden Flüssigkeitsmengen günstiger, an Stelle von einem weiten Rohr mehrere Rohre mit kleiner lichter Weite vorzugsweise unter io mm anzuordnen, die oberhalb des Flüssigkeitsspiegels in den Verdampferraum des Kondensators B einmünden.About a run down of the liquid oxygen next to the rising one To avoid gas bubbles in the riser pipes P as far as possible, it is advantageous for this Provide pipes with small clearances. For this reason it is with larger ones more favorable amounts of liquid to be conveyed, instead of one wide pipe several Pipes with a smaller clear width should preferably be arranged below 10 mm, and those above of the liquid level open into the evaporator chamber of the condenser B.
Die im Verdampfer E eingebaute Austauschfläche stellt keinen zusätzlichen Aufwand dar, denn je mehr hier bereits verdampft wird, desto weniger Wärme muß im Kondensator B übertragen werden. Das Ventil G wird dabei vorteilhaft so einreguliert, daß praktisch der gesamte durch E strömende Stickstoff verflüssigt wird. Die Einregelung der nötigen Waschstickstoffmenge kann sodann durch Ventil K erfolgen.The exchange surface built into the evaporator E does not represent any additional Effort, because the more that is already evaporated here, the less heat has to be in the Capacitor B are transferred. The valve G is advantageously adjusted so that that practically all of the nitrogen flowing through E is liquefied. The adjustment the necessary amount of scrubbing nitrogen can then be carried out through valve K.
Zur Teilverflüssigung des Sauerstoffs in E kann an Stelle von Stickstoff auch .eine andere Wärmequelle, beispielsweise ein Teilstrom der zu zerlegenden Luft dienen.To partially liquefy the oxygen in E, instead of nitrogen also. Another heat source, for example a partial flow of the air to be broken down to serve.
Außer zur Zerlegung von Luft ist das Verfahren auch in all den Fällen anwendbar, bei denen bisher mit zwei übereinandergestellten durch einen Kondensator miteinander verbundenen Kolonne gearbeitet wird und bei denen die große Bauhöhe dieser Anordnung von Nachteil ist.In addition to the separation of air, the procedure is also in all cases applicable where previously with two superimposed by a capacitor interconnected column is worked and in which the large overall height this arrangement is disadvantageous.
Claims (3)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DEM4587D DE849850C (en) | 1944-01-27 | 1944-01-27 | Process for the separation of air |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DEM4587D DE849850C (en) | 1944-01-27 | 1944-01-27 | Process for the separation of air |
Publications (1)
Publication Number | Publication Date |
---|---|
DE849850C true DE849850C (en) | 1952-09-18 |
Family
ID=7292742
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DEM4587D Expired DE849850C (en) | 1944-01-27 | 1944-01-27 | Process for the separation of air |
Country Status (1)
Country | Link |
---|---|
DE (1) | DE849850C (en) |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2913882A (en) * | 1954-05-06 | 1959-11-24 | Air Prod Inc | Method and apparatus for fraction-ating gaseous mixtures |
US3131045A (en) * | 1958-05-19 | 1964-04-28 | Air Prod & Chem | Method and apparatus for fractionating gaseous mixtures |
EP0637725A1 (en) * | 1993-08-06 | 1995-02-08 | Praxair Technology, Inc. | Cryogenic rectification system for lower pressure operation |
EP1363094A1 (en) * | 2002-05-03 | 2003-11-19 | Air Products And Chemicals, Inc. | System and method for introducing low pressure reflux to a high pressure column without a pump |
FR2853406A1 (en) * | 2003-04-01 | 2004-10-08 | Air Liquide | Procedure for separating air by cryogenic distillation uses two-column separator and pressure reducing valve opening at set pressure |
FR2853405A1 (en) * | 2003-04-01 | 2004-10-08 | Air Liquide | Cryogenic distillation air separation procedure and plant uses lightening gas formed at least partly from purging gas drawn from vaporizer-condenser |
EP1837614A1 (en) * | 2006-03-23 | 2007-09-26 | Linde Aktiengesellschaft | Process and device for the vaporisation of an oxygen enriched liquid and process and device for the cryogenic separation of air |
EP1837615A1 (en) * | 2006-03-23 | 2007-09-26 | Linde Aktiengesellschaft | Method and device for an oxygen enriched fluid and method and device for low temperature decomposition of air |
EP3176526A1 (en) * | 2015-12-03 | 2017-06-07 | Linde Aktiengesellschaft | Method and assembly for transferring fluid |
EP3910274A1 (en) * | 2020-05-13 | 2021-11-17 | Linde GmbH | Method for the low-temperature decomposition of air and air separation plant |
-
1944
- 1944-01-27 DE DEM4587D patent/DE849850C/en not_active Expired
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2913882A (en) * | 1954-05-06 | 1959-11-24 | Air Prod Inc | Method and apparatus for fraction-ating gaseous mixtures |
US3131045A (en) * | 1958-05-19 | 1964-04-28 | Air Prod & Chem | Method and apparatus for fractionating gaseous mixtures |
EP0637725A1 (en) * | 1993-08-06 | 1995-02-08 | Praxair Technology, Inc. | Cryogenic rectification system for lower pressure operation |
EP1363094A1 (en) * | 2002-05-03 | 2003-11-19 | Air Products And Chemicals, Inc. | System and method for introducing low pressure reflux to a high pressure column without a pump |
FR2853406A1 (en) * | 2003-04-01 | 2004-10-08 | Air Liquide | Procedure for separating air by cryogenic distillation uses two-column separator and pressure reducing valve opening at set pressure |
FR2853405A1 (en) * | 2003-04-01 | 2004-10-08 | Air Liquide | Cryogenic distillation air separation procedure and plant uses lightening gas formed at least partly from purging gas drawn from vaporizer-condenser |
EP1837614A1 (en) * | 2006-03-23 | 2007-09-26 | Linde Aktiengesellschaft | Process and device for the vaporisation of an oxygen enriched liquid and process and device for the cryogenic separation of air |
EP1837615A1 (en) * | 2006-03-23 | 2007-09-26 | Linde Aktiengesellschaft | Method and device for an oxygen enriched fluid and method and device for low temperature decomposition of air |
EP3176526A1 (en) * | 2015-12-03 | 2017-06-07 | Linde Aktiengesellschaft | Method and assembly for transferring fluid |
EP3910274A1 (en) * | 2020-05-13 | 2021-11-17 | Linde GmbH | Method for the low-temperature decomposition of air and air separation plant |
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