EP1037004A1 - Appareil et procédé pour séparer un mélange de gaz à basse température - Google Patents

Appareil et procédé pour séparer un mélange de gaz à basse température Download PDF

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Publication number
EP1037004A1
EP1037004A1 EP00105042A EP00105042A EP1037004A1 EP 1037004 A1 EP1037004 A1 EP 1037004A1 EP 00105042 A EP00105042 A EP 00105042A EP 00105042 A EP00105042 A EP 00105042A EP 1037004 A1 EP1037004 A1 EP 1037004A1
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EP
European Patent Office
Prior art keywords
heat exchanger
condenser
section
line
passages
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.)
Granted
Application number
EP00105042A
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German (de)
English (en)
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EP1037004B1 (fr
Inventor
Augustin Dipl.-Ing. Rampp
Manfred Dipl.-Phys. Sotzek
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Linde GmbH
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Linde GmbH
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Priority to EP00105042A priority Critical patent/EP1037004B1/fr
Publication of EP1037004A1 publication Critical patent/EP1037004A1/fr
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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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • 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
    • F25J3/044—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 single pressure main column system only
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers

Definitions

  • the invention relates to a device for decomposing a gas mixture at low Temperature with a separation column, with a heat exchanger block, the one Has main heat exchanger section and a condenser-evaporator section, the condenser-evaporator section evaporation passages and Has condensation passages, with a first feed gas line for supply from feed gas to the main heat exchanger section, with a second Feed gas line for introducing cooled feed gas into the separation column, with a first liquid line leading from the lower area of the separation column to the inlet the evaporation passages leads, with a gas line leading from the top of the Separation column leads to the condensation passages, and with a return line to Introduction of condensate formed in the condensation passages into the upper ones Area of the separation column.
  • the most important field of application of the invention is the low temperature decomposition of Air in single or multi-column processes, especially the production of nitrogen from air in a one-pillar process.
  • Separatiation column is understood here to mean a conventional mass transfer column which Rectification trays, packing (disordered packing) and / or ordered packing as Contains mass transfer elements, in particular a rectification or distillation column.
  • a device of the type mentioned is known from JP-A-10206012 ( Figure 3).
  • the main heat exchanger and condenser evaporator are not as common Usually formed by separate heat exchanger blocks but are in one Integrated heat exchanger block that a main heat exchanger section Cooling of air against reverse flows as well as a condenser-evaporator section for the recovery of reflux liquid by evaporation of the Has bottom liquid of the separation column.
  • This integrated design has a contrast conventional systems have the advantage of lower investment costs.
  • the liquid contained in the heat exchanger block of the plant according to JP-A-10206012 is evaporated, contains the main components oxygen, nitrogen and argon also those air components that are less volatile than oxygen and in which Air cleaning upstream of the main heat exchanger section does not come from the Feed air were removed.
  • the oxygenated Bottom liquid from the separation column in the heat exchanger block according to JP-A-10206012 there is a risk that some of these less volatile components will not completely evaporates, but accumulates in the liquid within the Condenser-evaporator section is present. With such enrichments, for example of hydrocarbons, would be a major security risk expect.
  • the invention has for its object a device of the aforementioned Specify the type and corresponding procedure that are cheaper to operate, especially in a particularly safe and economical way. This object is achieved in that a phase separation device is provided
  • the one with the exit of the evaporation passages and the other with a second liquid line is connected, which from the phase separation device to Entry of the evaporation passages leads and also a connection with one Has flush line.
  • the device according to the invention enables safe operation of the integrated device Heat exchanger blocks without business interruption.
  • the liquid in the Condenser-evaporator section only partially evaporated and the resultant Steam is separated from the remaining liquid in the phase separator Cut.
  • the latter becomes a first part via the second liquid line Entry of the evaporation passages of the condenser-evaporator section returned and continuously to a second part via a flushing line or discarded discontinuously.
  • Unwanted concentration is prevented by the division of the liquid remaining portion from the phase separation device, which is enriched with volatile components in the event of air separation. This makes it possible to discharge less volatile impurities and to keep their content in the evaporation passages below a non-hazardous limit (for example less than 500 ppm CH 4 equivalent).
  • a non-hazardous limit for example less than 500 ppm CH 4 equivalent.
  • the proportion of the liquid overturned via the liquid line is seven to 15 times, preferably eight to ten times the amount evaporated in the evaporation passages (the relative amounts given here and hereinafter refer to molar amounts).
  • 0.05 to 0.5%, preferably 0.1 to 0.2% of the total amount of gas mixture to be separated is discarded as flushing quantity via the flushing line.
  • the heat exchanger block is preferably in the invention by a Plate heat exchanger formed, especially by a soldered aluminum plate heat exchanger.
  • the main heat exchanger section is located here preferably above the condenser-evaporator section.
  • Insert heat exchanger block In general, only one becomes in the device according to the invention Insert heat exchanger block. This can be made in one piece, for example be or by joining (for example by means of flanges) two or several sections can be produced. However, the invention can also be applied to larger ones Systems are applied by placing two or more such heat exchanger blocks can be connected in parallel. Each of these heat exchange blocks then has one Main heat exchanger section and a condenser-evaporator section.
  • the main area of application of the invention is in single-column systems in which the Condenser-evaporator section preferably the top condenser of the only one Represents separation column.
  • the invention is basically based on other processes applicable with two or more columns; for example, the main capacitor a double column system formed by the condenser-evaporator section become.
  • the phase separation device can be implemented in different ways. To the it can be caused by a vessel arranged outside the heat exchanger block be formed via a line with the exit of the evaporation passages connected is.
  • the phase separation device is replaced by a Collector in the form of a header arranged on the side of the heat exchanger block educated; alternatively, one can be on both sides of the heat exchanger block corresponding header can be arranged.
  • Under "Header” is a distribution or To understand collection device in fluid communication with a certain group of passages of a heat exchanger block and to Serve to supply or to withdraw fluid flowing through this passage. This one mentioned headers can for example be semi-tubular.
  • the phase separation device by a within the Heat exchanger blocks in the transition between the condenser-evaporator section and Main heat exchanger section arranged area formed.
  • liquid line there are also various alternatives for the construction of the liquid line.
  • she can be arranged outside the heat exchanger block or through passages be formed within the heat exchanger block.
  • the second variant is available especially when the phase separation within the heat exchanger block is carried out; for example, the otherwise can be used for this purpose Continuation of the passages for cooling the gas mixture to be broken down be used at the lower end of the main heat exchanger section are interrupted.
  • the vapor from the phase separator is preferably the Main heat exchanger section fed at its cold end.
  • the heat exchanger block used in the invention can be used in any process and every system can be used, in which a first fluid in one Main heat exchanger section cooled and a second fluid in a condenser-evaporator section be evaporated against a condensing third fluid.
  • the passages for the gas from the top of the separation column can continue without interruption over the entire length of the Go through heat exchanger blocks.
  • the gas is in the gas line in the Transition area between the main heat exchanger section and the condenser-evaporator section inserted into the heat exchanger block, with a part after Flows into the main heat exchanger section at the top, heated and as a product is withdrawn, another part down into the condensation passages of the Condenser-evaporator section flows and is liquefied there.
  • the passages for those coming from the lower area of the separation column Fraction can be carried out continuously in a similar manner.
  • the phase separation device can be arranged within the heat exchanger block the vapor formed in the evaporation passages in the same passages flow through the main heat exchanger section.
  • At least one group of passages of the heat exchanger block is preferred between the main heat exchanger section and the condenser-evaporator section interrupted.
  • the heat exchanger block as a soldered aluminum plate heat exchanger is realized, the interruption of passages horizontally or diagonally arranged walls (end strips, sidebars) made in the transition area between the main heat exchanger section and Condenser-evaporator section are arranged.
  • Such walls can be used for Example the passages for cooling the gas mixture to be broken down on it Complete the bottom and / or the evaporation passages on the top.
  • the steam can run out the phase center device to be initiated in Heat the main heat exchanger section against the feed gas to be cooled.
  • Claims 4 and 5 relate to configurations of the invention Device with regard to the flow in the evaporation passages are particularly advantageous.
  • the gas to be condensed is the upper end of the Capacitor section supplied and flows in cocurrent with the formed Condensate within the condensation passages down.
  • the invention also relates to a method according to claims 7 to 9 and an application of the device and / or the method according to claim 10.
  • Compressed and cleaned feed air 1 flows in the example of FIG. 1 as a gas mixture to be broken down (feed gas) into the main heat exchanger section 51 of a heat exchanger block 50, which also has a condenser-evaporator section 52.
  • feed gas feed gas
  • the feed air is cooled to approximately dew point and then fed into the separation column 3 via line 2
  • Nitrogen 4 (the "first fraction") becomes gaseous above the top of the separation column 3 withdrawn and flows to the heat exchanger block 50 in the transition region between Main heat exchanger section 51 and condenser-evaporator section 52 too.
  • a first part of the gaseous nitrogen is passed up into the passages 53 of the main heat exchanger section and finally via a Product line 62 withdrawn.
  • Another part of the nitrogen 4 flows into the Condenser-evaporator section condensation passages 54 down and condenses at least partially, preferably essentially completely or completely.
  • the condensate is on the return line 5 to the top of the Separation column 3 returned. If necessary, a part can be removed as a liquid product (not shown).
  • An oxygen-enriched (“second") fraction 7 becomes liquid from the bottom of the Separation column 3 withdrawn, relaxed (8) and via line 9 to the lower end of Condenser-evaporator section 52 transported. (Lines 7 and 9 form the "First liquid line”.)
  • the evaporation passages 55 of the condenser-evaporator section 52 of the heat exchanger block 50 is the partially oxygenated fraction evaporated.
  • the evaporation passages 55 are closed at their upper end.
  • the header 56 acts as Phase separator.
  • the vaporous part is in the heat exchanger block returned to the lower end of the main heat exchanger section, the extensions 57 of the evaporation passages 55 are used for heating become.
  • the liquid remaining portion is outside via a liquid line 58 deducted the heat exchanger block 50 and at least a part 59 to returned to the lower end of the evaporation passages 55.
  • Another part is about the purge line 61 discarded continuously or discontinuously.
  • the system can be supplied with cold to compensate for insulation losses by Liquid nitrogen via line 6 and / or a liquefied mixture via line 10 of air gases and / or liquid oxygen in the separation column 3 and / or in the Evaporation passages 55 of the condenser-evaporator section 52 are fed becomes.
  • internal cooling is used completely eliminated by means of work-relieving relaxation of a turbine.
  • the process cold can be obtained in whole or in part by relieving the pressure of a process gas, as shown in FIG. 2 .
  • a part 201 of the residual gas generated in the evaporation 55 is removed from the heating passages 57 of the main heat exchanger section 51 at an intermediate temperature and expanded in a turbine 202 to perform work.
  • the expanded residual gas 203 is returned to the main heat exchanger section 51, near its cold end.
  • the expanded residual gas is finally warmed to ambient temperature and removed (205).
  • the representation of Figure 3 is not to scale.
  • the amount of The main heat exchanger section 51 is in reality, for example, 2 to 5 m, preferably about 3.5 m; the capacitor section 52 is, for example, 1 to 2 m, preferably about 3.5 m high.
  • Double lines in FIG. 3 mean end strips (Sidebars), which seal a passage close to the side, top or bottom.
  • the preferred direction of the corrugated sheets arranged within the passages (Fins) is indicated by a triplet of short lines.
  • Feed air 1 flows into the header 301, which is only shown in the left section of FIG. 3 (cross section A ).
  • the introduced gas is distributed over the entire width of the passage 303 by means of the obliquely arranged fins 302.
  • the air passages 303 are closed on their underside by two obliquely arranged sidebars 304.
  • the cooled air is removed via a header 305 and flows via line 2 to the separation column.
  • nitrogen is introduced from the gas line 4 into the condensation passages 54 via a further header 306.
  • the condensate is drawn off at the lower end via a header 307 and passed via the return line 5 to the top of the separation column.
  • the nitrogen header 306 connected to the condensation passages of cross section A is also shown in the middle section of FIG. 3, which shows a cross section of type B.
  • the header 306 also communicates with the passages 53 shown there.
  • the part of the nitrogen which is supplied via line 4 and which does not flow into the condensation passages 54 flows into the passages 53 of the main heat exchanger section and is heated there.
  • the warm nitrogen gas is led to the product line 62 via a header 308.
  • the lower continuation 309 of the passages 53, which is part of the condenser section, has no function in the exemplary embodiment in the context of the heat exchange process. Header 310 and line 311 only serve to vent the lower section of passages B.
  • the cross sections C serve only for the treatment of the oxygen-enriched ("second") fraction 9, which originates from the bottom of the separation column.
  • This is called a two-phase mixture via a connector 312 centrally into a header 313 introduced, which covers the entire underside of the heat exchanger block 50.
  • a perforated plate 314 extends over the entire horizontal cross section of the Headers 313. It serves to distribute those contained in the two-phase mixture Steam bubbles on the entire horizontal cross section.
  • Within the Evaporation passages 55 increases the liquid-vapor mixture through the Thermosiphon effect upwards and to the left below the sidebar 315 respectively on the right into the two headers 56a, 56b, which as Phase separator act.
  • the steam portion flows upwards into the Main heat exchanger section 52, more precisely in the continuation 57 of the Evaporation passages 55 above the sidebar 315.
  • the warm gas is over pulled a header 318 to the residual gas line 63.
  • the remaining liquid flows in the pipes 58a, 58b, which form the "second liquid line", down and mostly back into header 313 via connection piece 316a, 316b.
  • a smaller part can flow via the connecting pieces 317a, 317b to the flushing line shown in FIG.
  • Each of these measures has a particularly uniform effect Flow through the evaporation passages 55.
  • The is particularly advantageous simultaneous application of several or all of these measures.
  • the even Flow improves heat transfer and increases the operational safety of the Capacitor section.

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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)
EP00105042A 1999-03-17 2000-03-09 Appareil et procédé pour séparer un mélange de gaz à basse température Expired - Lifetime EP1037004B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP00105042A EP1037004B1 (fr) 1999-03-17 2000-03-09 Appareil et procédé pour séparer un mélange de gaz à basse température

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE19911909 1999-03-17
DE19911909 1999-03-17
EP99113350 1999-07-09
EP99113350 1999-07-09
EP00105042A EP1037004B1 (fr) 1999-03-17 2000-03-09 Appareil et procédé pour séparer un mélange de gaz à basse température

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EP1037004A1 true EP1037004A1 (fr) 2000-09-20
EP1037004B1 EP1037004B1 (fr) 2003-08-06

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CZ297345B6 (cs) * 2001-10-16 2006-11-15 Ateko, A. S. Zarízení pro nízkoteplotní separaci plynu
EP2053328A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Procédé pour la séparation cryogénique d'air
EP2053329A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Installation d'industrie électronique et procédé de fonctionnement d'une installation d'industrie électronique
EP2053331A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Procédé et dispositif de séparation de l'air à basse température
WO2009063146A1 (fr) * 2008-03-28 2009-05-22 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur et appareil de séparation d'air par distillation cryogénique incorporant un tel échangeur

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US5324452A (en) * 1992-07-08 1994-06-28 Air Products And Chemicals, Inc. Integrated plate-fin heat exchange reformation
US5765631A (en) * 1994-12-21 1998-06-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Fluid circulation apparatus
US5901578A (en) * 1998-05-18 1999-05-11 Praxair Technology, Inc. Cryogenic rectification system with integral product boiler

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Cited By (6)

* Cited by examiner, † Cited by third party
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CZ297345B6 (cs) * 2001-10-16 2006-11-15 Ateko, A. S. Zarízení pro nízkoteplotní separaci plynu
EP2053328A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Procédé pour la séparation cryogénique d'air
EP2053329A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Installation d'industrie électronique et procédé de fonctionnement d'une installation d'industrie électronique
EP2053331A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Procédé et dispositif de séparation de l'air à basse température
EP2053330A1 (fr) * 2007-10-25 2009-04-29 Linde Aktiengesellschaft Procédé de séparation de l'air à basse température
WO2009063146A1 (fr) * 2008-03-28 2009-05-22 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur et appareil de séparation d'air par distillation cryogénique incorporant un tel échangeur

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