EP0410832A1 - Verdampfer-Kondensator für eine Zweisäulenanlage zur Luftzerlegung - Google Patents

Verdampfer-Kondensator für eine Zweisäulenanlage zur Luftzerlegung Download PDF

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Publication number
EP0410832A1
EP0410832A1 EP90401934A EP90401934A EP0410832A1 EP 0410832 A1 EP0410832 A1 EP 0410832A1 EP 90401934 A EP90401934 A EP 90401934A EP 90401934 A EP90401934 A EP 90401934A EP 0410832 A1 EP0410832 A1 EP 0410832A1
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EP
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Prior art keywords
exchanger
oxygen
passages
liquid
auxiliary
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
EP90401934A
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English (en)
French (fr)
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EP0410832B1 (de
Inventor
Maurice Grenier
Pierre Petit
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of EP0410832A1 publication Critical patent/EP0410832A1/de
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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
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04818—Start-up of the process
    • 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
    • F25J3/04769—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
    • F25J3/04763—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.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • F25J5/005—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 in a reboiler-condenser, e.g. within a 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"
    • 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
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
    • 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
    • F25J2250/10—Boiler-condenser with superposed stages
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/902—Apparatus
    • Y10S62/903—Heat exchange structure

Definitions

  • the present invention relates to vaporizers-condensers for air distillation installations. It relates firstly to an apparatus for vaporizing oxygen and for condensing nitrogen for a double air distillation column of the type comprising at least one main heat exchanger disposed in the tank of the low pressure column, this exchanger being of trickling type and having oxygen passages, means for causing excess liquid oxygen to flow in these passages, means for evacuating all of the vaporized oxygen and excess liquid oxygen by means of the the lower end of the same passages, nitrogen passages in indirect heat exchange relationship with the oxygen passages, means for supplying the nitrogen passages with nitrogen gas coming from the medium pressure column, and means for return the condensed nitrogen to the medium pressure column.
  • the liquid oxygen which is in the bottom of the low pressure column is vaporized by heat exchange with the nitrogen gas taken off at the head of the medium pressure column.
  • the temperature difference between oxygen and nitrogen made necessary by the structure of the heat exchanger imposes the operating pressure of the medium pressure column. It is therefore desirable that this temperature difference is as small as possible, in order to minimize the expenses linked to the compression of the air to be treated injected into the medium pressure column.
  • Drip type vaporizers are very advantageous due to their excellent heat exchange performance, and can be achieved reliably and economically using the technology described in EP-A-130 122 in the name of the applicant.
  • the liquids stored on the trays of the upper column bottom column are pressure
  • the argon mixture column associated with the double column or even the liquids stored on the trays of the lower column (medium pressure column) if no action is taken regarding the operation of the liquid ascent valve rich, will end up poured into the tank of the low pressure column, precisely where the vaporizer-condenser is installed.
  • the object of the invention is to solve the problem of re-initiating the heat exchanger relatively economically.
  • the subject of the invention is a vaporizer-condenser of the aforementioned type, characterized in that the main heat exchanger is arranged so as to be at least partially submerged during an operation stop of the double column, and in that the apparatus comprises at least one auxiliary heat exchanger adapted to ensure only the vaporization of liquid when the main exchanger is at least partially submerged.
  • the auxiliary exchanger is a flow type exchanger comprising oxygen passages, means for causing excess liquid oxygen to flow in these passages, nitrogen passages in relation to indirect heat exchange with oxygen passages, means for supplying passages from nitrogen to nitrogen gas coming from the medium pressure column, and means for returning the condensed nitrogen to the medium pressure column, the auxiliary exchanger being situated entirely above the maximum level of the liquid in the tank of the column low pressure, and means are provided for raising this liquid to the top of the oxygen passages of the auxiliary exchanger as well as means for returning liquid from the lower end of the auxiliary exchanger to the top of the passages main exchanger oxygen.
  • the auxiliary exchanger is an exchanger of the same type as the main exchanger and is disposed substantially at the same level as the latter in the tank of the low pressure column, the top of the oxygen passages of the 'auxiliary exchanger being supplied exclusively by a pipe for raising the liquid contained in this tank.
  • the auxiliary heat exchanger is a bath type exchanger arranged below the main exchanger in the tank of the low pressure column.
  • the invention also relates to a double column air distillation installation, comprising a vaporization-condensation apparatus as defined above.
  • each column comprising distillation trays 3 or an equivalent structure of heat and material exchange.
  • Column 1 which operates at around 6 bar absolute, is limited by a cylindrical ferrule 4, and column 2, which operates a little above atmospheric pressure, by a cylindrical ferrule 5.
  • the two columns are separated by a bottom 6 curved upwards.
  • the head nitrogen of column 1 is condensed by vaporizing liquid oxygen reaching the tank of column 2, by means of an indirect heat exchanger 7 of the trickle type.
  • the exchanger 7 is essentially constituted by a large parallelepiped block, for example 1 to 1.5 square meters of horizontal section and 3 to 6 meters in height, formed of a stack of a large number of parallel vertical plates in aluminum which define between them flat passages.
  • Each of these passages contains aluminum waves forming spacers and fins and is delimited by vertical or horizontal bars.
  • Part of these passages, for example one passage in two, is an oxygen passage, and the remaining passages are nitrogen passages.
  • the oxygen passages are supplied from above with liquid oxygen by means of a liquid retention 8 formed at the top of the changer, closed laterally and open downwards.
  • the nitrogen passages are closed on all sides and are supplied laterally with gaseous nitrogen, near their upper end, by means of a semi-cylindrical box 9 with a horizontal axis, which communicates with the top of the column 1 by 1 'through a pipe 10.
  • Condensed nitrogen is collected laterally at the bottom of the same passages by another semi-cylindrical box 11 with a horizontal axis and, from there, is returned to column 1 by a pipe 12.
  • the latter opens out in a channel 13 which ensures a guard of liquid nitrogen.
  • the block of the exchanger 7 is assembled by brazing in the furnace.
  • a liquid oxygen bath 14 is present in the tank of the column 2, and its level N is located below the lower end of the exchanger 7, at a small distance from the latter.
  • a pump 15 raises via a line 16 a flow D of liquid oxygen in the reservoir 8, which also receives a flow D of liquid oxygen from the plates of the column 2.
  • a flow D of oxygen is vaporized in the exchanger 7 , so that a flow D of excess liquid oxygen falls into the bath 14. The flows can deviate more or less from the value D in practice.
  • the pump 15 can be replaced by any other means for raising the liquid, for example by a thermosyphon or "extraction” with the gas constituted by an indirect heat exchanger 15A heated by a suitable fluid, which can be "rich liquid ". from the tank in column 1, as is conventional in the art.
  • a suitable fluid which can be "rich liquid ". from the tank in column 1, as is conventional in the art.
  • this variant is shown in dashed lines, and there is also shown a pipe 17 for withdrawing gaseous oxygen from column 2 and a pipe 18 for withdrawing liquid nitrogen from column 1.
  • level N is provided a short distance below the exchanger 7, as indicated above.
  • the "load in use” of numerous trays collects in the tank of column 2, and the liquid rises to a level N1 for which the exchanger 7 is partially submerged.
  • a certain height of liquid is present in the lower part of the oxygen passages of this exchanger.
  • the tank of the column 2 contains two main heat exchangers 7 arranged in parallel at the same level as in FIG. 1, that is to say with their lower end very close to the bottom 6, just above the level N of the liquid oxygen bath.
  • the reservoir 8 is common to the two exchangers.
  • the installation includes an auxiliary ferrule liaire 19 containing an auxiliary heat exchanger 20.
  • This exchanger is also of the trickle type and has the same constitution as the exchanger 7.
  • the shell 19 is closed at the top by an upper bottom 21 and at the bottom by a bottom bottom 22, which is located above the level of the reservoir 8 of the exchangers 7.
  • the pipe 16 for raising the liquid emerges at the top of the shell 19; a pipe 23 connects the bottom 22 to the retainer 8, and pipes 24 and 24A respectively connect the space located just below the exchanger 20 and the space located below the bottom 21 to the region of the shell 5 located just above the reservoir 8.
  • the pump 15 rises liquid oxygen from the bath 14 to the top of the shell 19 to maintain an auxiliary retention 25 of liquid at the top of the exchanger 20. About half of this liquid flow is vaporized in this exchanger, and the excess of liquid oxygen as well as the vaporized oxygen pass into the ferrule 5 via the lines 23 and 24. The excess of liquid oxygen is added to the liquid oxygen falling from the plates of the column 2 in the reservoir 8, and approximately half of the total flow of liquid oxygen supplying the latter is vaporized in the exchangers 7, the excess liquid being taken up by the pump 15.
  • the tank liquid in column 2 rises to level N1 as in Fig. 1.
  • the pump 15 rises the liquid at the top of the auxiliary exchanger 20, which, by its position, has remained in operating condition. Part of the liquid flow is therefore vaporized by the only exchanger 20, and the excess liquid as well as the vaporized liquid passes as previously into the shell 15, via the lines 23 and 24.
  • the level of the liquid gradually decreases in column 2, and when the level N is almost restored, the exchangers 7 can operate again.
  • the exchanger 20 is dimensioned so as to allow the installation to process the air flow rate necessary for priming the plates so that their "charge in use" is reconstituted, this air flow rate being less than the flow rate corresponding to the normal operation of the installation.
  • the additional shell 19 and the auxiliary exchanger 20 are constantly used as an additional heat exchange surface, which improves the thermal performance of the installation.
  • the exchanger 20 could be arranged at a level lower than the reservoir 8 or even than the level N1, with an additional pump fitted to the pipe 23.
  • the shell 19 can be constituted by the exchanger block itself in its current part.
  • the exchangers 7 are three in number and are arranged as in FIG. 2, side by side and just above the bath 14, with a common retainer 8.
  • the auxiliary exchanger consists of three exchangers 20A identical to the exchangers 7 and arranged in column 2, just above these.
  • the pipe 16 comprises a branch 16A opening into the retaining 25A of the exchangers 20A, and a branch 16B opening into the retaining 8 of the exchangers 7. These pipes are equipped with respective stop valves 26A, 26B.
  • the liquid oxygen bath 14 is at level N.
  • the valve 26A is closed and the valve 26B is open.
  • Auxiliary exchangers 20A are supplied with liquid oxygen only by the plates of column 2, vaporize approximately half of this flow and supply the rest to the reservoir 8.
  • a flow of the same order is raised by the pump 15 to the reservoir 8, half of the total flow is vaporized in the exchangers 7, and the rest falls into the bath 14.
  • exchangers 20 of FIG. 2 and 20A of FIG. 3 could be made so as to allow the evacuation of the liquid vaporized from above, as described in the abovementioned EP-A.
  • two main exchangers 7 and two auxiliary exchangers 20B are provided side by side in the shell 5.
  • the four exchangers have their lower ends located a short distance above level N; they are all identical, with one difference: the two exchangers 7 have a common retainer 8 open upwards as in the previous examples, while the two exchangers 20B have a common retainer 25B hermetically covered by a horizontal horizontal feed box -cylindrical 27 into which the pipe 16 opens.
  • a pipe 27A starts from the top of the box 27, leaves the ferrule 5, is fitted outside of the latter with a valve 27B and opens into the ferrule 5, at - above level N.
  • valve 27B In normal operation of the installation, the valve 27B is open. The same flow reaches the reservoir 8 coming from the plates and the reservoir 25B via the pipe 16. Each exchanger vaporizes approximately a quarter of this flow, and the excess liquid falls into the bath 14 to be raised by the pump 15.
  • Fig. 5 shows a solution which can be considered as a variant of FIG. 2: the ferrule 19 is at a lower level than in FIG. 2, the bottom 22 being approximately at the level of the bottom 6 of the double column.
  • the pipe 24 connects as in FIG. 2 the space located just below the exchanger 20 at the region of the shell 5 located above the reservoir 8.
  • the pipe 24A is equipped with a valve 24B.
  • valves 29 and 24B are open, and the level N is established in the two ferrules 5 and 19.
  • the exchanger 20 constitutes an additional evaporator-condenser supplied with liquid oxygen by line 16 while the exchanger 7 is supplied with liquid oxygen by the plates 3 only.
  • valve 29 is closed simultaneously with the pump stopping, which prevents immersion of the exchanger 20.
  • liquid is vaporized by the only exchanger 20 , and it is two-phase fluid which returns to column 2 via line 24.
  • valve 29 Another possibility is to leave the valve 29 open.
  • the exchanger 20 is then partially submerged like the exchanger 7 during the stops of the installation, and the restart is carried out by closing the valve 24B and creating by means of the pump 15 an overpressure in the upper bottom of the shell. 19, analogously to what has been described with reference to FIG. 4.
  • This restart mode with the submerged exchanger 20 can also be carried out with the valve 29 closed.
  • the level N is such that the exchangers 20C are almost entirely submerged.
  • the reservoir 8 of the exchangers 7 is supplied only with liquid oxygen coming from the plates. About half of the flow is vaporized in these exchangers, and the rest falls into the bath 14. The exchangers 20C vaporizing this excess flow, it is therefore not in principle necessary to flow the liquid back to the reservoir 8.
  • bath vaporizers have a lower yield than trickle vaporizers, it may be preferable to size the 20C exchangers so that they vaporize only a small fraction of the flow of liquid oxygen, the excess flow then being raised in reservoir 8 as before.
  • the solution of FIG. 6 is more particularly suitable for cases where relatively moderate heat exchange performance is acceptable, for example a temperature difference of the order of 1 ° C. between the medium pressure nitrogen and the liquid oxygen.

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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)
EP90401934A 1989-07-28 1990-07-04 Verdampfer-Kondensator für eine Zweisäulenanlage zur Luftzerlegung Expired - Lifetime EP0410832B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8910223A FR2650379B1 (fr) 1989-07-28 1989-07-28 Appareil de vaporisation-condensation pour double colonne de distillation d'air, et installation de distillation d'air comportant un tel appareil
FR8910223 1989-07-28

Publications (2)

Publication Number Publication Date
EP0410832A1 true EP0410832A1 (de) 1991-01-30
EP0410832B1 EP0410832B1 (de) 1992-12-16

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EP90401934A Expired - Lifetime EP0410832B1 (de) 1989-07-28 1990-07-04 Verdampfer-Kondensator für eine Zweisäulenanlage zur Luftzerlegung

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Country Link
US (1) US5071458A (de)
EP (1) EP0410832B1 (de)
JP (1) JP2985892B2 (de)
KR (1) KR910003342A (de)
BR (1) BR9003676A (de)
CA (1) CA2022168C (de)
DE (1) DE69000593T2 (de)
ES (1) ES2036408T3 (de)
FR (1) FR2650379B1 (de)
PT (1) PT94834A (de)
ZA (1) ZA905895B (de)

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EP0469780A1 (de) * 1990-07-31 1992-02-05 The BOC Group plc Tiefsieden von verflüssigtem Gas
EP1094286A1 (de) * 1999-10-20 2001-04-25 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP0567360B2 (de) † 1992-03-24 2002-06-12 L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Apparat zum Überführen einer Flüssigkeit
US6430961B1 (en) 1999-10-20 2002-08-13 Linde Aktiengesellschaft Process and device for the low-temperature fractionation of air

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US5438836A (en) * 1994-08-05 1995-08-08 Praxair Technology, Inc. Downflow plate and fin heat exchanger for cryogenic rectification
US5699671A (en) * 1996-01-17 1997-12-23 Praxair Technology, Inc. Downflow shell and tube reboiler-condenser heat exchanger for cryogenic rectification
DE19605500C1 (de) * 1996-02-14 1997-04-17 Linde Ag Vorrichtung und Verfahren zum Verdampfen einer Flüssigkeit
US5775129A (en) * 1997-03-13 1998-07-07 The Boc Group, Inc. Heat exchanger
GB9705889D0 (en) * 1997-03-21 1997-05-07 Boc Group Plc Heat exchange method and apparatus
US5956972A (en) * 1997-12-23 1999-09-28 The Boc Group, Inc. Method of operating a lower pressure column of a double column distillation unit
DE59901114D1 (de) * 1998-01-30 2002-05-08 Linde Ag Verfahren und vorrichtung zum verdampfen von flüssigem sauerstoff
US6264809B1 (en) 1998-10-30 2001-07-24 Pti Advanced Filtration, Inc. Enhanced membrane electrode devices useful for electrodeposition coating
DE19921949A1 (de) * 1999-05-12 2000-11-16 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
FR2807826B1 (fr) * 2000-04-13 2002-06-14 Air Liquide Echangeur vaporisateur-condenseur du type a bain
DE10027140A1 (de) * 2000-05-31 2001-12-06 Linde Ag Mehrstöckiger Badkondensator
US6349566B1 (en) 2000-09-15 2002-02-26 Air Products And Chemicals, Inc. Dephlegmator system and process
FR2822079B1 (fr) * 2001-03-16 2003-05-16 Air Liquide Procede et installation de production d'oxygene ultra-pur par distillation d'air
US6393866B1 (en) 2001-05-22 2002-05-28 Praxair Technology, Inc. Cryogenic condensation and vaporization system
DE10205878A1 (de) * 2002-02-13 2003-08-21 Linde Ag Tieftemperatur-Luftzerlegungsverfahren
FR2853723B1 (fr) * 2003-04-10 2007-03-30 Air Liquide Procede et installation de traitement d'un bain de liquide riche en oxygene recueilli en pied d'une colonne de distillation cryogenique
US7266976B2 (en) * 2004-10-25 2007-09-11 Conocophillips Company Vertical heat exchanger configuration for LNG facility
US20070028649A1 (en) * 2005-08-04 2007-02-08 Chakravarthy Vijayaraghavan S Cryogenic air separation main condenser system with enhanced boiling and condensing surfaces
EP1890099A1 (de) 2006-08-08 2008-02-20 Linde Aktiengesellschaft Rücklaufkondensator
FR2916523B1 (fr) * 2007-05-21 2014-12-12 Air Liquide Capacite de stockage, appareil et procede de production de monoxyde de carbone et/ou d'hydrogene par separation cryogenique integrant une telle capacite.
US9476641B2 (en) * 2007-09-28 2016-10-25 Praxair Technology, Inc. Down-flow condenser reboiler system for use in an air separation plant
US9453674B2 (en) * 2013-12-16 2016-09-27 Praxair Technology, Inc. Main heat exchange system and method for reboiling
US9488408B2 (en) * 2014-01-29 2016-11-08 Praxair Technology, Inc. Condenser-reboiler system and method
EP3176526A1 (de) * 2015-12-03 2017-06-07 Linde Aktiengesellschaft Verfahren und anordnung zum überführen von fluid
US12359875B2 (en) * 2020-09-04 2025-07-15 Clean Power Hydrogen Group Limited Heat exchanger
KR102877555B1 (ko) * 2022-11-30 2025-10-27 재단법인 포항산업과학연구원 활성 코크스의 제조방법 및 이를 이용하여 제조된 활성 코크스

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US4606745A (en) * 1984-05-30 1986-08-19 Nippon Sanso Kabushiki Kaisha Condenser-evaporator for large air separation plant

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FR2542421B1 (fr) * 1983-03-08 1985-07-05 Air Liquide Procede et appareil pour produire un gaz a haute purete par vaporisation d'un liquide cryogenique
FR2547898B1 (fr) * 1983-06-24 1985-11-29 Air Liquide Procede et dispositif pour vaporiser un liquide par echange de chaleur avec un deuxieme fluide, et leur application a une installation de distillation d'air

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Publication number Priority date Publication date Assignee Title
DE1152432B (de) * 1962-04-21 1963-08-08 Linde Eismasch Ag Platten-Kondensator-Verdampfer, insbesondere fuer Gas- und Luftzerleger
US4606745A (en) * 1984-05-30 1986-08-19 Nippon Sanso Kabushiki Kaisha Condenser-evaporator for large air separation plant

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0469780A1 (de) * 1990-07-31 1992-02-05 The BOC Group plc Tiefsieden von verflüssigtem Gas
EP0567360B2 (de) † 1992-03-24 2002-06-12 L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren und Apparat zum Überführen einer Flüssigkeit
EP1094286A1 (de) * 1999-10-20 2001-04-25 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
US6430961B1 (en) 1999-10-20 2002-08-13 Linde Aktiengesellschaft Process and device for the low-temperature fractionation of air

Also Published As

Publication number Publication date
KR910003342A (ko) 1991-02-27
BR9003676A (pt) 1991-09-03
ZA905895B (en) 1991-05-29
CA2022168A1 (fr) 1991-01-29
AU5985790A (en) 1991-01-31
DE69000593D1 (de) 1993-01-28
JP2985892B2 (ja) 1999-12-06
FR2650379B1 (fr) 1991-10-18
PT94834A (pt) 1993-10-29
AU625706B2 (en) 1992-07-16
FR2650379A1 (fr) 1991-02-01
ES2036408T3 (es) 1993-05-16
DE69000593T2 (de) 1993-04-22
US5071458A (en) 1991-12-10
CA2022168C (fr) 1995-03-14
EP0410832B1 (de) 1992-12-16
JPH0370977A (ja) 1991-03-26

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