EP0723106A1 - Process for the preparation of cold gas - Google Patents

Process for the preparation of cold gas Download PDF

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Publication number
EP0723106A1
EP0723106A1 EP19950108739 EP95108739A EP0723106A1 EP 0723106 A1 EP0723106 A1 EP 0723106A1 EP 19950108739 EP19950108739 EP 19950108739 EP 95108739 A EP95108739 A EP 95108739A EP 0723106 A1 EP0723106 A1 EP 0723106A1
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Prior art keywords
gas
pressure
heat exchange
liquid
exchange unit
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EP19950108739
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German (de)
French (fr)
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EP0723106B1 (en
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Georg Veranneman
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Linde GmbH
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Linde GmbH
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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
    • F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
    • F25D3/00—Devices using other cold materials; Devices using cold-storage bodies
    • F25D3/10—Devices using other cold materials; Devices using cold-storage bodies using liquefied gases, e.g. liquid air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2201/00—Vessel construction, in particular geometry, arrangement or size
    • F17C2201/01—Shape
    • F17C2201/0104—Shape cylindrical
    • F17C2201/0109—Shape cylindrical with exteriorly curved end-piece
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2205/00—Vessel construction, in particular mounting arrangements, attachments or identifications means
    • F17C2205/03—Fluid connections, filters, valves, closure means or other attachments
    • F17C2205/0302—Fittings, valves, filters, or components in connection with the gas storage device
    • F17C2205/0338—Pressure regulators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/035—Propane butane, e.g. LPG, GPL
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/035—High pressure (>10 bar)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/036—Very high pressure (>80 bar)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/04—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by other properties of handled fluid before transfer
    • F17C2223/042—Localisation of the removal point
    • F17C2223/046—Localisation of the removal point in the liquid
    • F17C2223/047—Localisation of the removal point in the liquid with a dip tube
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/061—Level of content in the vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/0626—Pressure

Definitions

  • the invention relates to a method for producing temperature-defined, cold gas by indirect heat exchange with a cryogenic, liquefied medium.
  • a problem here is that especially when using low-cost liquid nitrogen as a cooling medium - the liquid nitrogen temperature at 2 bar pressure is approximately - 190 ° C - other gases (Ar, O 2 , air, ..) and also Nitrogen can be liquefied even in unfavorable operating situations, e.g. at higher consumption gas pressures or at times the gas consumption is at a standstill, and malfunctions based on this can occur during operation.
  • the cold gas to be produced is cooled by indirect heat exchange, in particular with its cryogenic liquefied form, the gas being set beforehand to a fixed base pressure p B and brought to the same pressure level in indirect heat exchange with the liquefied form , the liquid state in turn being kept at a second pressure p 2 , which is higher than the base pressure, and the associated boiling temperature.
  • liquid oxygen set at 12 bar is at the boiling point at 123 K (-150 ° C), while O 2 gas set at 10 bar only liquefies at 120 K (-153 ° C).
  • the cooling is preferably carried out to such an extent that the gas assumes the temperature of the cooling liquid phase. In this way, a very precise maintenance of the intended cold gas temperature is achieved.
  • the liquid gas that is also used as the cold gas is used as the coolant. This results in the possibility of adding the coolant to the gas to be cooled after its use in cooling the gas and ultimately its evaporation, and thus to achieve double use.
  • the liquid gas which has the highest liquefaction point in the mixture must be used for the cooling process by indirect heat exchange.
  • a nitrogen-oxygen mixture for example, oxygen.
  • a particular advantage of the invention is that it can easily be used to produce a cold gas which is directly adjacent to the vapor pressure curve of the respective medium with regard to its temperature.
  • the p 2 pressure level is to be set, for example, only 0.5 bar, but preferably 1 to 3 bar, above the base pressure level. Even in this operating situation there is no risk of liquefaction of the gas to be cooled.
  • the O 2 cold gas supply system shown in FIG. 1 has a liquid oxygen tank 1, which is connected via a connecting line 2 connected to the bottom to a heat exchange unit 4, consisting of a container with an internal pipe coil 7.
  • a valve 3 for switching the flow of liquid oxygen from the storage tank 1 to the heat exchange unit 4 is arranged in the connecting line 2.
  • the valve 3 is connected to a level meter 5 located on the container of the heat exchange unit 4 and both elements, ie valve 3 and level meter 5, keep the level of the liquid oxygen in the heat exchange unit 4 at a desired level.
  • a pressure regulator 6, which regulates the pressure in the heat exchange unit 4, is connected to the gas space of the heat exchange unit 4 that arises above.
  • the gas to be removed from the heat exchange unit 4 at excess pressure is fed to the coil 7, for which purpose a connecting line 9 is provided between the pressure regulator 6 and the coil 7.
  • the pipe coil 7, on the other hand, is supplied with gaseous (!) Oxygen via a feed line 10, a pressure regulator 8 arranged therein setting the base pressure p B required according to the invention, which is lower than the pressure in the heat exchange unit.
  • the oxygen gas supplied via line 10 can be of different origins in accordance with the system diagram shown; it can either also have been removed from the storage container 1 and brought into the gaseous state by means of an evaporator 11, or it can also come from another oxygen source - for example an adsorptive or permeative air separator.
  • a pressure level of 2 bar is set in the pipe coil 7 by means of the pressure regulator 8.
  • this pressure is referred to as the base pressure p B.
  • the liquefaction point of oxygen is at a temperature of 97 K (-176 ° C).
  • a suitable pressure setting for the heat exchanger unit 4, starting from this base pressure P B is a pressure p 2 , which is 1 to approx. 20 bar higher for example in a pressure setting of 12 bar. This pressure setting is carried out by means of the control valve 6.
  • the condensing temperature of oxygen at 2 bar pressure is - as already stated - 97 K, and with this setting of the heat exchange unit 7 it is therefore only possible to reach a temperature of 123 K (-150 ° C) (123 K is the cooling limit at 12 bar ).
  • the liquefaction temperature of the oxygen would be 125 K and the consumption gas thus provided could be one Heat exchanger temperature of 123 K thus condensed and thus an operational malfunction can be caused. This is very advantageously avoided with the system presented here and the settings mentioned.
  • the method can also be used with pure media other than oxygen, e.g. with nitrogen and argon.
  • oxygen as the cooling medium
  • any other gas which boils deeper than oxygen, and in particular also low-boiling oxygen-containing gas mixtures with settings such as those associated with oxygen, are advantageously and reliably cooled can.
  • Corresponding media are, for example, nitrogen, argon, but also dry air, helium, hydrogen and mixtures thereof. The same possibilities as with oxygen - but at a higher temperature level - also arise with cryogenic and liquid carbon dioxide. The temperature range that can be achieved is -25 to -56 ° C.
  • Cold gas obtained in this way can be used for all known applications such as blown film and strip cooling, cold gas polishing and therapeutic purposes (see documents mentioned at the beginning) as well as for new possibilities - such as cold gas freshening for the present invention, for which a patent has been applied for, or for flame cutting workpieces with cold oxygen.

Abstract

In a process for producing a cold gas at a defined temp., the gas is first adjusted to a predetermined base pressure (pB) and kept at this pressure whilst it is brought into indirect heat transfer contact with the liquid form of the same gas, the liquid being maintained at a second pressure (p2) (which is higher than the base pressure) and at its b. pt. Also claimed is an appts. having a storage tank (1) for the liquefied gas connected by a liquid gas line to heat exchange unit (4) comprising a vessel with an internal heat exchanger (7). The appts. also includes a level controller (5) for the liq. in the heat transfer unit, a pressure controller (6) for the liq. connected to the upper part of the heat transfer unit, a gas supply line (10) connecting the heat exchanger with one or more sources of gas, and a pressure controller (8) in the gas supply pipe.

Description

Die Erfindung betrifft ein Verfahren zur Herstellung von temperaturdefiniertem, kaltem Gas durch indirekten Wärmetausch mit einem tiefkalten, verflüssigt vorliegenden Medium.The invention relates to a method for producing temperature-defined, cold gas by indirect heat exchange with a cryogenic, liquefied medium.

Es ist beispielsweise bekannt, kaltes Gas aus dem zugehörigen tiefkalten Flüssiggas durch verdampfen und partielles Anwärmen bereitzustellen (siehe DE-PS 41 34 108, insbes. Figur). Hierbei ist es schwierig, die Temperatur des erhaltenen Gases in engeren Grenzen einzustellen, da sich beispielsweise abhängig von der Verbrauchsmenge oder der Umgebungstemperatur die Verdampfungs- und Erwärmungsbedingungen ändern.
Ebenso bekannt ist es, kaltes Gas durch Vermischen mit tiefkaltem Flüssiggas herzustellen (DE-OS 32 42 881). Eine bekannte Möglichkeit insbesondere auch zur Erzeugung tiefkalter Gasströme besteht auch in einer Abkühlung in indirektem Wärmetausch mit einem tiefkalten Flüssiggas (vgl. DE-PS 38 27 417). Ein Problem dabei besteht darin, daß gerade bei der Anwendung von besonders preiswert verfügbarem, tiefkaltem Flüssigstickstoff als Kühlmedium - die Flüssigstickstofftemperatur bei 2 bar Druck beträgt ca. - 190°C - andere Gase (Ar, O2, Luft,..) und auch Stickstoff selbst in ungünstigen Betriebssituationen, z.B. bei höheren Verbrauchsgasdrücken oder zeitweise ruhendem Gasverbrauch, verflüssigt werden und somit darauf begründete Störungen im Betrieb auftreten können.It is known, for example, to provide cold gas from the associated cryogenic liquid gas by vaporization and partial heating (see DE-PS 41 34 108, in particular FIG.). It is difficult to set the temperature of the gas obtained within narrow limits, since the evaporation and heating conditions change, for example, depending on the amount consumed or the ambient temperature.
It is also known to produce cold gas by mixing it with cryogenic liquid gas (DE-OS 32 42 881). A known possibility, in particular also for generating cryogenic gas flows, is also cooling by indirect heat exchange with a cryogenic liquid gas (cf. DE-PS 38 27 417). A problem here is that especially when using low-cost liquid nitrogen as a cooling medium - the liquid nitrogen temperature at 2 bar pressure is approximately - 190 ° C - other gases (Ar, O 2 , air, ..) and also Nitrogen can be liquefied even in unfavorable operating situations, e.g. at higher consumption gas pressures or at times the gas consumption is at a standstill, and malfunctions based on this can occur during operation.

Aufgabenstellung der vorliegenden Erfindung war es daher, ein Verfahren zur Herstellung von kaltem Gas auf der Basis eines indirekten Wärmetausches mit einem tiefkalten Flüssiggas anzugeben, das auf möglichst aufwandsarme und einfache Weise eine betriebssichere und auch temperaturgenaue Bereitstellung von Kaltgas ergibt.It was therefore an object of the present invention to provide a method for producing cold gas on the basis of an indirect heat exchange with a cryogenic liquid gas, which results in an operationally reliable and also temperature-accurate provision of cold gas in a simple and inexpensive manner.

Diese Aufgabenstellung wird erfindungsgemäß dadurch gelöst, daß das herzustellende, kalte Gas durch indirekten Wärmetausch insbesondere mit seiner tiefkalt verflüssigten Form abgekühlt wird, wobei das Gas vorab auf einen festgelegten Basisdruck pB eingestellt wird und auf eben diesem Druckniveau in indirekten Wärmetausch mit der verflüssigten Form gebracht wird, wobei wiederum die flüssige Zustandsform auf einem zweiten, im Vergleich zum Basisdruck erhöhten Druck p2 und der zugehörigen Siedetemperatur gehalten wird.This object is achieved according to the invention in that the cold gas to be produced is cooled by indirect heat exchange, in particular with its cryogenic liquefied form, the gas being set beforehand to a fixed base pressure p B and brought to the same pressure level in indirect heat exchange with the liquefied form , the liquid state in turn being kept at a second pressure p 2 , which is higher than the base pressure, and the associated boiling temperature.

Durch die erfindungsgemäße Maßgabe für die Drücke von Gas und Flüssiggas der selben Art wird verhindert, daß in irgendeiner Betriebssituation eine Verflüssigung des gasförmigen Mediums beim Wärmetausch auftreten kann. Solange der flüssige Zustand des Mediums auf einem höheren Druckniveau als der gasförmige ist, kann das entsprechende, am Siedepunkt befindliche Flüssiggas das niedriger gespannte Gas nicht kondensieren. Beispielsweise befindet sich auf 12 bar eingestellter Flüssigsauerstoff bei 123 K (-150°C) am Siedepunkt, während auf 10 bar eingestelltes O2-Gas sich erst bei 120 K (-153°C) verflüssigt.The requirement according to the invention for the pressures of gas and liquefied gas of the same type prevents the liquefaction of the gaseous medium during heat exchange in any operating situation. As long as the liquid state of the medium is at a higher pressure level than the gaseous one, the corresponding liquid gas at the boiling point cannot condense the lower-tension gas. For example, liquid oxygen set at 12 bar is at the boiling point at 123 K (-150 ° C), while O 2 gas set at 10 bar only liquefies at 120 K (-153 ° C).

Bevorzugt wird erfindungsgemäß die Abkühlung soweit geführt, daß das Gas die Temperatur der kühlenden Flüssigphase annimmt. Auf diese Weise wird eine sehr genaue Einhaltung der beabsichtigen Kaltgastemperatur erzielt.According to the invention, the cooling is preferably carried out to such an extent that the gas assumes the temperature of the cooling liquid phase. In this way, a very precise maintenance of the intended cold gas temperature is achieved.

Generell ergibt sich gemäß der Erfindung der Umstand, daß als Kühlmittel dasjenige Flüssiggas eingesetzt wird, das auch als Kaltgas zur Anwendung kommt. Daraus ergibt sich die Möglichkeit, das Kühlmittel nach seinem Einsatz beim Abkühlen des Gases und letzlich seiner Verdampfung dem abzukühlenden Gas hinzuzufügen und so eine Doppelnutzung zu erzielen.In general, according to the invention, there is the fact that the liquid gas that is also used as the cold gas is used as the coolant. This results in the possibility of adding the coolant to the gas to be cooled after its use in cooling the gas and ultimately its evaporation, and thus to achieve double use.

Handelt es sich um ein Gasgemisch aus dem Kaltgas gebildet werden soll, so ist für den Abkühlprozeß durch indirekten Wärmetausch dasjenige Flüssiggas einzusetzen, das im Gemisch den höchsten Verflüssigungspunkt besitzt. Im Falle eines Stickstoff-Sauerstoff-Gemisches also beispielsweise Sauerststoff.If it is a gas mixture from which cold gas is to be formed, then the liquid gas which has the highest liquefaction point in the mixture must be used for the cooling process by indirect heat exchange. In the case of a nitrogen-oxygen mixture, for example, oxygen.

Ein besonderer Vorteil der Erfindung besteht darin, daß es mit ihr problemlos gelingt, ein Kaltgas, das hinsichtlich seiner Temperatur unmittelbar benachbart zur Dampfdruckkurve des jeweiligen Mediums liegt, herzustellen. Hierzu ist das p2-Druckniveau beispielsweise lediglich 0,5 bar, vorzugsweise jedoch 1 bis 3 bar, über dem Basisdruckniveau einzustellen. Auch in dieser Betriebssituation ist keinerlei Gefahr einer Verflüssigung des abzukühlenden Gases vorhanden.A particular advantage of the invention is that it can easily be used to produce a cold gas which is directly adjacent to the vapor pressure curve of the respective medium with regard to its temperature. For this purpose, the p 2 pressure level is to be set, for example, only 0.5 bar, but preferably 1 to 3 bar, above the base pressure level. Even in this operating situation there is no risk of liquefaction of the gas to be cooled.

Eine erfindungsgemäße Vorrichtung ist gekennzeichnet durch

  • einen Flüssiggasspeichertank, der über eine Flüssiggasleitung mit einer, aus einem Behälter mit innenliegendem Wärmetauscher bestehenden, Wärmetauscheinheit verbunden ist,
  • einen Pegelstandsregler für Flüssiggas am Behälter der Wärmetauscheinheit,
  • einem am Behälter der Wärmetauscheinheit kopfseitig angeschlossenen Druckregler,
  • eine Gaszuleitung, die den innenliegenden Wärmetauscher mit einer Gasquelle verbindet, und durch einen Druckregler, der sich in dieser Gaszuleitung befindet.
A device according to the invention is characterized by
  • a liquefied gas storage tank which is connected via a liquefied gas line to a heat exchange unit consisting of a container with an internal heat exchanger,
  • a level controller for liquid gas on the tank of the heat exchange unit,
  • a pressure regulator connected to the head of the heat exchange unit,
  • a gas supply line, which connects the internal heat exchanger to a gas source, and a pressure regulator, which is located in this gas supply line.

Im folgenden wird die Erfindung an einem Ausführungsbeispiel und in Verbindung mit den Figuren näher erläutert. Es zeigt:

Figur 1
eine erfindungsgemäße Anlage zur Herstellung von tiefkaltem Sauerstoffgas;
Figur 2
einen Ausschnitt aus der Dampfdruckkurve von Sauerstoff.
The invention is explained in more detail below using an exemplary embodiment and in conjunction with the figures. It shows:
Figure 1
a plant according to the invention for the production of cryogenic oxygen gas;
Figure 2
a section of the vapor pressure curve of oxygen.

Die in Figur 1 gezeigte O2-Kaltgasversorgungsanlage besitzt einen Flüssigsauerstofftank 1, der über eine bodenseitig angeschlossene Verbindungsleitung 2 mit einer Wärmetauscheinheit 4, bestehend aus einem Behälter mit innenliegender Rohrschlange 7, verbunden ist. In der Verbindungsleitung 2 ist ein Ventil 3 zur Schaltung des Flüssigsauerstoffzuflusses vom Speichertank 1 zur Wärmetauscheinheit 4 angeordnet. Das Ventil 3 steht in Verbindung mit einem am Behälter der Wärmetauscheinheit 4 befindlichen Pegelstandsmesser 5 und beide Elemente, also Ventil 3 und Pegelstandsmesser 5, halten den Pegel des Flüssigsauerstoffs in der Wärmetauscheinheit 4 auf einem gewünschten Niveau.The O 2 cold gas supply system shown in FIG. 1 has a liquid oxygen tank 1, which is connected via a connecting line 2 connected to the bottom to a heat exchange unit 4, consisting of a container with an internal pipe coil 7. A valve 3 for switching the flow of liquid oxygen from the storage tank 1 to the heat exchange unit 4 is arranged in the connecting line 2. The valve 3 is connected to a level meter 5 located on the container of the heat exchange unit 4 and both elements, ie valve 3 and level meter 5, keep the level of the liquid oxygen in the heat exchange unit 4 at a desired level.

Am oben entstehenden Gasraum der Wärmetauscheinheit 4 ist ein Druckregler 6 angeschlossen, der den Druck in der Wärmetauscheinheit 4 regelt. Das bei Überdruck aus der Wärmetauscheinheit 4 abzuführende Gas wird der Rohrschlange 7 zugeführt, wozu eine Verbindungsleitung 9 zwischen dem Druckregler 6 und der Rohrschlange 7 vorgesehen ist. Die Rohrschlange 7 wird andererseits über eine Zuleitung 10 mit gasförmigem (!) Sauerstoff versorgt, wobei ein darin angeordneter Druckregler 8 den erfindungsgemäß geforderten, im Vergleich zum Druck in der Wärmetauscheinheit niedrigeren Basisdruck pB einstellt. Das über die Leitung 10 zugeführte Sauerstoffgas kann gemäß gezeigtem Anlagenschema unterschiedlicher Herkunft sein; es kann entweder ebenfalls aus dem Speicherbehälter 1 entnommen und mittels eines Verdampfers 11 in den gasförmigen Zustand gebracht worden sein, oder es kann auch aus einer sonstigen Sauerstoffquelle - beispielsweise einem adsorptiven oder permeativen Luftzerleger - stammen.A pressure regulator 6, which regulates the pressure in the heat exchange unit 4, is connected to the gas space of the heat exchange unit 4 that arises above. The gas to be removed from the heat exchange unit 4 at excess pressure is fed to the coil 7, for which purpose a connecting line 9 is provided between the pressure regulator 6 and the coil 7. The pipe coil 7, on the other hand, is supplied with gaseous (!) Oxygen via a feed line 10, a pressure regulator 8 arranged therein setting the base pressure p B required according to the invention, which is lower than the pressure in the heat exchange unit. The oxygen gas supplied via line 10 can be of different origins in accordance with the system diagram shown; it can either also have been removed from the storage container 1 and brought into the gaseous state by means of an evaporator 11, or it can also come from another oxygen source - for example an adsorptive or permeative air separator.

Zur weiteren Verdeutlichung der Erfindung werden im folgenden Zahlenbeispiele für die geschilderte Anlage vorgestellt, wobei die als Figur 2 beigefügte Dampfdruckkurve von Sauerstoff weitere Informationen liefert.To further clarify the invention, numerical examples for the system described are presented in the following, the vapor pressure curve of oxygen added as FIG. 2 providing further information.

Besteht also beispielsweise die Zielsetzung darin, ein kaltes O2-Gas auf einem Druckniveau von etwa 2 bar bereitzustellen, so resultiert, daß in der Rohrschlange 7 mittels des Druckreglers 8 ein Druckniveau von 2 bar eingestellt wird. Dieser Druck wird erfindungsgemäß als Basisdruck pB bezeichnet. Bei 2 bar liegt der Verflüssigungspunkt von Sauerstoff bei einer Temperatur von 97 K (-176°C).Eine geeignete Druckeinstellung für die Wärmetauschereinheit 4 besteht, ausgehend von diesem Basisdruck PB in einem 1 bis ca. 20 bar höheren Druck p2, also beispielsweise in einer Druckeinstellung von 12 bar. Diese Druckeinstellung wird mittels des Regelventils 6 vorgenommen.For example, if the objective is to provide a cold O 2 gas at a pressure level of about 2 bar, the result is that a pressure level of 2 bar is set in the pipe coil 7 by means of the pressure regulator 8. According to the invention, this pressure is referred to as the base pressure p B. At 2 bar, the liquefaction point of oxygen is at a temperature of 97 K (-176 ° C). A suitable pressure setting for the heat exchanger unit 4, starting from this base pressure P B , is a pressure p 2 , which is 1 to approx. 20 bar higher for example in a pressure setting of 12 bar. This pressure setting is carried out by means of the control valve 6.

Die Verflüssigungs- bzw. Siedetemperatur von Sauerstoff bei 12 bar liegt höher als bei 2 bar, nämlich bei 123 K (=-150 °C - siehe Punkt B in Figur 2). Daraus folgt, daß das Temperaturniveau in der Wärmetauschereinheit 4 so ist, daß keine Verflüssigung des 2-bar-Verbrauchsgases in der Rohrschlange 7 auch bei einem zeitweise auf Null sinkenden Gasverbrauch eintreten kann (siehe Punkt C in Fig. 2). Die Verflüssigungstemperatur von Sauerstoff bei 2 bar Druck beträgt - wie bereits ausgeführt - 97 K, und es kann bei dieser Einstellung der Wärmetauscheinheit 7 also lediglich eine Temperatur von 123 K (-150°C) erreicht werden (123 K ist die Kühlgrenze bei 12 bar).The liquefaction or boiling temperature of oxygen at 12 bar is higher than at 2 bar, namely at 123 K (= -150 ° C - see point B in Figure 2). It follows that the temperature level in the heat exchanger unit 4 is such that no liquefaction of the 2 bar consumable gas in the coil 7 can occur even if the gas consumption drops temporarily to zero (see point C in FIG. 2). The condensing temperature of oxygen at 2 bar pressure is - as already stated - 97 K, and with this setting of the heat exchange unit 7 it is therefore only possible to reach a temperature of 123 K (-150 ° C) (123 K is the cooling limit at 12 bar ).

Vergleicht man damit die naheliegendste Ausgestaltung einer derartigen Kaltgasbereitstellung, nämlich daß das Verbrauchsgas auf dem höherliegenden Druckniveau p1 des Speicherbehälters 1 bereitgestellt wird, also beispielsweise etwa mit 14 bar, so läge die Verflüssigungstemperatur des Sauerstoffs bei 125 K und das so bereitgestellte Verbrauchsgas könnte bei einer Wärmetauschertemperatur von 123 K also kondensiert und somit eine Betriebsstörung verursacht werden. Dies wird mit der hier vorgestellten Anlage und den genannten Einstellungen sehr vorteilhaft vermieden.If you compare the most obvious design of such a cold gas supply, namely that the consumption gas is provided at the higher pressure level p 1 of the storage container 1, for example at about 14 bar, the liquefaction temperature of the oxygen would be 125 K and the consumption gas thus provided could be one Heat exchanger temperature of 123 K thus condensed and thus an operational malfunction can be caused. This is very advantageously avoided with the system presented here and the settings mentioned.

Mit der beschriebenen Anlage ist es ferner problemlos möglich, auch andere, deutlich höher liegende Verbrauchsgasdrücke als 2 bar anzubieten, so lange nur der Basisgasdruck wenigstens 0,5 bar, vorzugsweise 1 bis 3 bar, unterhalb der Druckeinstellung in der Wärmetauschereinheit 4 - also dem Druck p2 - verbleibt. Es ist im oben geschilderten Beispiel also ohne weiteres möglich, Verbrauchsgas mit ca. 10 bar anzubieten. Bei 10 bar weist Sauerstoff eine Verflüssigungstemperatur von 120 K auf und dieser kann daher - obwohl bereits sehr nahe an der Dampfdruckkurve des Sauerstoffs liegend - bei einer Wärmetauschereinstellung von 12 bar und einer daraus folgenden Temperatureinstellung der Wärmetauscheinheit 4 von 123 K noch völlig betriebssicher geliefert werden (siehe Punkt A in Figur 2).With the system described, it is also possible to offer other, significantly higher consumption gas pressures than 2 bar, as long as the base gas pressure is at least 0.5 bar, preferably 1 to 3 bar, below the pressure setting in the heat exchanger unit 4 - that is, the pressure p 2 - remains. In the example described above, it is therefore easily possible to offer consumable gas at approximately 10 bar. At 10 bar, oxygen has a liquefaction temperature of 120 K and this can therefore - although very close to the vapor pressure curve of the oxygen horizontal - with a heat exchanger setting of 12 bar and a resulting temperature setting of the heat exchange unit 4 of 123 K can still be delivered in a completely reliable manner (see point A in FIG. 2).

Somit ist - bei der in der Praxis ohne Schwierigkeiten möglichen Bereitstellung von Flüssiggas in einem Speichertank auf einem Druckniveau von bis zu 25 bar - erfindungsgemäß die Zurverfügungstellung von Kaltgas auch auf höheren Drücken und mit Temperaturen unterhalb von -130 °C - unter sehr genauer Einhaltung des Temperaturniveaus - problemlos möglich.Thus, in the case of the provision of liquid gas in a storage tank at a pressure level of up to 25 bar, which is possible in practice without difficulty, the provision of cold gas even at higher pressures and at temperatures below -130.degree Temperature levels - easily possible.

Selbstverständlich ist die Anwendung des Verfahrens auch bei anderen Reinmedien als Sauerstoff möglich, z.B. bei Stickstoff und Argon. Darüber hinaus liegt es auch im Rahmen der Erfindung, daß beim Einsatz von beispielsweise Sauerstoff als Kühlmedium neben Sauerstoff auch jedes andere, tiefer als Sauerstoff siedende Gas und insbesondere auch tiefersiedende, sauerstoffhaltige Gasgemische mit Einstellungen, wie sie zu Sauerstoff gehören, vorteilhaft und betriebssicher abgekühlt werden können. Entsprechende Medien sind beispielsweise Stickstoff, Argon, aber auch trockene Luft, Helium, Wasserstoff und Gemische davon. Ebensolche Möglichkeiten wie mit Sauerstoff - jedoch auf höherem Temperaturniveau - ergeben sich ferner auch mit tiefkaltem und flüssigem Kohlendioxid. Der erreichbare Temperaturbereich ist hierbei -25 bis -56°C.Of course, the method can also be used with pure media other than oxygen, e.g. with nitrogen and argon. In addition, it is also within the scope of the invention that when using, for example, oxygen as the cooling medium, in addition to oxygen, any other gas which boils deeper than oxygen, and in particular also low-boiling, oxygen-containing gas mixtures with settings such as those associated with oxygen, are advantageously and reliably cooled can. Corresponding media are, for example, nitrogen, argon, but also dry air, helium, hydrogen and mixtures thereof. The same possibilities as with oxygen - but at a higher temperature level - also arise with cryogenic and liquid carbon dioxide. The temperature range that can be achieved is -25 to -56 ° C.

So gewonnenes Kaltgas kann für alle bekannten Anwendungen wie Blasfolien- und Bandkühlen, Kaltgaspolieren und Therapiezwecke eingesetzt werden (siehe eingangs genannte Dokumente) sowie auch für neue Möglichkeiten - etwa das gleichzeitig zum zu vorliegender Erfindung zum Patent angemeldete Kaltgasfrischen oder zum Brennschneiden von Werkstücken mit Kaltsauerstoff.Cold gas obtained in this way can be used for all known applications such as blown film and strip cooling, cold gas polishing and therapeutic purposes (see documents mentioned at the beginning) as well as for new possibilities - such as cold gas freshening for the present invention, for which a patent has been applied for, or for flame cutting workpieces with cold oxygen.

Claims (9)

Verfahren zur Herstellung von temperaturdefiniertem, kaltem Gas durch indirekten Wärmetausch mit einem tiefkalten, verflüssigt vorliegenden Medium, dadurch gekennzeichnet, daß das herzustellende, kalte Gas durch indirekten Wärmetausch insbesondere mit seiner tiefkalt verflüssigten Form abgekühlt wird, wobei das Gas vorab auf einen festgelegten Basisdruck pB eingestellt wird und auf eben diesem Druckniveau in indirekten Wärmetausch mit der verflüssigten Form gebracht wird, wobei wiederum die flüssige Zustandsform auf einem zweiten, im Vergleich zum Basisdruck erhöhten Druck p2 und der zugehörigen Siedetemperatur gehalten wird.A process for the production of temperature-defined, cold gas by indirect heat exchange with a cryogenic, liquefied medium, characterized in that the cold gas to be produced is cooled by indirect heat exchange, in particular with its cryogenic liquefied form, the gas being preliminarily brought up to a fixed base pressure p B is set and brought to this pressure level in indirect heat exchange with the liquefied form, the liquid state in turn being kept at a second pressure p 2 , which is higher than the base pressure, and the associated boiling temperature. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Abkühlung soweit geführt wird, daß das Gas die Temperatur der kühlenden Flüssigphase annimmtA method according to claim 1, characterized in that the cooling is carried out so far that the gas assumes the temperature of the cooling liquid phase Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das p2-Druckniveau lediglich 1 bis 3 bar höher als das Basisdruckniveau eingestellt wird.Method according to Claim 1 or 2, characterized in that the p 2 pressure level is set only 1 to 3 bar higher than the base pressure level. Verfahren nach einem der Ansprüchen 1 bis 3, dadurch gekennzeichnet, daß das verflüssigte Medium nach seinem Einsatz beim Abkühlen des Gases und letztlich seiner Verdampfung dem abzukühlenden Gas hinzugefügt wird.Process according to one of Claims 1 to 3, characterized in that the liquefied medium is added to the gas to be cooled after it has been used to cool the gas and, ultimately, after it has evaporated. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, daß - wenn aus einem Gasgemisch ein Kaltgas gebildet werden soll - für den indirekten Wärmetausch dasjenige Flüssiggas eingesetzt wird, das im Gemisch den höchsten Verflüssigungspunkt besitzt.Method according to one of claims 1 to 4, characterized in that - if a cold gas is to be formed from a gas mixture - the liquid gas which has the highest liquefaction point in the mixture is used for the indirect heat exchange. Vorrichtung zur Herstellung von kaltem Gas, gekennzeichnet durch - einen Flüssiggasspeichertank (1), der über eine Flüssiggasleitung mit einer, aus einem Behälter mit innenliegendem Wärmetauscher (7) bestehenden, Wärmetauscheinheit (4) verbunden ist, - einem Pegelstandsregler (5) für Flüssiggas am Behälter der Wärmetauscheinheit, - einem am Behälter der Wärmetauscheinheit oben angeschlossenen Druckregler (6), - eine Gaszuleitung (10), die den innenliegenden Wärmetauscher mit einer oder mehreren Gasquellen verbindet,
und durch einen Druckregler (8), der sich in dieser Gaszuleitung befindet. Device for producing cold gas, characterized by a liquid gas storage tank (1) which is connected via a liquid gas line to a heat exchange unit (4) consisting of a container with an internal heat exchanger (7), - a level controller (5) for liquid gas on the container of the heat exchange unit, - a pressure regulator (6) connected to the tank of the heat exchange unit at the top, a gas feed line (10) which connects the internal heat exchanger to one or more gas sources,
and by a pressure regulator (8) which is located in this gas feed line. Vorrichtung nach Anspruch 6,dadurch gekennzeichnet, daß der Druckregler (6) an der Wärmetauscheinheit (4) auf einen höheren Druck als der Druckregler (8) in der Gaszuleitung (10) eingestellt ist.Apparatus according to claim 6, characterized in that the pressure regulator (6) on the heat exchange unit (4) is set to a higher pressure than the pressure regulator (8) in the gas feed line (10). Vorrichtung nach einem der Ansprüche 6 bis 7, dadurch gekennzeichnet, daß die Gaszuleitung (10) mit dem Flüssiggasspeichertank (1) verbunden ist, wobei in der Verbindung ein Verdampfer (11) angeordnet ist.Device according to one of claims 6 to 7, characterized in that the gas feed line (10) is connected to the liquid gas storage tank (1), an evaporator (11) being arranged in the connection. Vorrichtung nach einem der Ansprüche 6 bis 8, dadurch gekennzeichnet, daß die Ausgangsseite des Druckreglers (6) an der Wärmetauscheinheit mit dem Wärmetauscher (7) verbunden ist.Device according to one of claims 6 to 8, characterized in that the output side of the pressure regulator (6) on the heat exchange unit is connected to the heat exchanger (7).
EP19950108739 1995-01-23 1995-06-07 Process for the preparation of cold gas Expired - Lifetime EP0723106B1 (en)

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DE1995101872 DE19501872A1 (en) 1995-01-23 1995-01-23 Process for the production of cold gas

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2120475A5 (en) * 1971-01-05 1972-08-18 Air Liquide Liquid purification by evaporation - using closed circuit heat exchange system
DE2438194A1 (en) * 1974-08-08 1976-02-19 Messer Griesheim Gmbh Dissolving methane in liquid propane - at reduced temp. to increase the amount of liquid fuel
DE3242881A1 (en) 1982-11-19 1984-05-24 Sauerstoffwerk Westfalen AG, 4400 Münster Process and apparatus for the production of a cold gas stream
DE3827417C1 (en) 1988-08-12 1989-08-31 Messer Griesheim Gmbh, 6000 Frankfurt, De
DE4134108C1 (en) 1991-10-15 1993-05-06 Linde Ag, 6200 Wiesbaden, De Steel strip metal coating - by passing through melt container, then up between two slot nozzles fed with e.g. liq. nitrogen@ to accelerate cooling
US5255525A (en) * 1991-10-22 1993-10-26 Mg Industries System and method for atomization of liquid metal

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2120475A5 (en) * 1971-01-05 1972-08-18 Air Liquide Liquid purification by evaporation - using closed circuit heat exchange system
DE2438194A1 (en) * 1974-08-08 1976-02-19 Messer Griesheim Gmbh Dissolving methane in liquid propane - at reduced temp. to increase the amount of liquid fuel
DE3242881A1 (en) 1982-11-19 1984-05-24 Sauerstoffwerk Westfalen AG, 4400 Münster Process and apparatus for the production of a cold gas stream
DE3827417C1 (en) 1988-08-12 1989-08-31 Messer Griesheim Gmbh, 6000 Frankfurt, De
EP0354350A2 (en) * 1988-08-12 1990-02-14 Messer Griesheim Gmbh Process for autogenous cutting with liquid oxygen
DE4134108C1 (en) 1991-10-15 1993-05-06 Linde Ag, 6200 Wiesbaden, De Steel strip metal coating - by passing through melt container, then up between two slot nozzles fed with e.g. liq. nitrogen@ to accelerate cooling
US5255525A (en) * 1991-10-22 1993-10-26 Mg Industries System and method for atomization of liquid metal

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EP0723106B1 (en) 1998-12-23
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DE59504630D1 (en) 1999-02-04

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