EP1336805A1 - Tieftemperatur-Luftzerlegungsverfahren - Google Patents

Tieftemperatur-Luftzerlegungsverfahren Download PDF

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Publication number
EP1336805A1
EP1336805A1 EP02009897A EP02009897A EP1336805A1 EP 1336805 A1 EP1336805 A1 EP 1336805A1 EP 02009897 A EP02009897 A EP 02009897A EP 02009897 A EP02009897 A EP 02009897A EP 1336805 A1 EP1336805 A1 EP 1336805A1
Authority
EP
European Patent Office
Prior art keywords
falling film
film evaporator
liquid
pressure column
oxygen
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP02009897A
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German (de)
English (en)
French (fr)
Inventor
Horst Corduan
Dietrich Rottmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority to DE10205878A priority Critical patent/DE10205878A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP02009897A priority patent/EP1336805A1/de
Priority to CNB031038697A priority patent/CN100380078C/zh
Priority to JP2003034815A priority patent/JP2003240430A/ja
Priority to US10/365,610 priority patent/US7134297B2/en
Publication of EP1336805A1 publication Critical patent/EP1336805A1/de
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—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
    • 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
    • F25J2250/04—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 invention relates to a method for the low-temperature separation of air in one Rectification unit, which includes a pressure column, a low pressure column and a condenser-evaporator system with at least two falling film evaporators, wherein oxygen-rich liquid from the low pressure column into the evaporation passages of the first falling film evaporator is introduced and partially evaporated and not evaporated oxygen-rich liquid from the first falling film evaporator into the second falling film evaporator is directed.
  • a condenser-evaporator system In a low-temperature air separation plant with one pressure column and one Low pressure column is opposed to liquid oxygen from the low pressure column gaseous nitrogen from the top of the pressure column in indirect heat exchange evaporates, the nitrogen condensing.
  • Such a condenser-evaporator system is usually referred to as the main capacitor.
  • the main capacitor is used almost exclusively as a circulating capacitor or designed as a falling film evaporator.
  • the Condenser block in a bath of the liquid to be evaporated.
  • the too evaporating liquid enters the evaporation passages from below and is in the Heat exchange against that flowing through the liquefaction passages Heating medium evaporates at least partially.
  • the resulting gas becomes liquid from the bath in the evaporation passages dragged. This thermal siphon effect creates a natural one Liquid circulation through the circulation condenser without additional aids Pumping liquid is necessary.
  • the liquid to be evaporated via a distribution system which also forms a gas seal, from above in the evaporation passages initiated.
  • the liquid overflows as a liquid film the walls separating the evaporation and liquefaction passages down and partially evaporates.
  • the resulting steam and the non-evaporated Residual liquid emerges from the falling film evaporator at the bottom.
  • This type of evaporator has a particularly low pressure loss in the evaporation passages and is therefore generally cheaper in energy terms than a circulation evaporator.
  • the ratio can change, at least in the short term Low pressure column of falling liquid and at the top of the pressure column change the resulting gaseous nitrogen.
  • this can lead to the ratio of in the evaporation passages of liquid entering and into the Liquefaction passages flowing heating medium decreases.
  • the evaporation passages can run dry and more volatile substances can accumulate in these.
  • the present invention is therefore based on the object of a method of the beginning to indicate the type mentioned, the energetically and operationally particularly cheap and where the accumulation of heavy volatile substances in the Falling film evaporator is avoided.
  • This object is achieved by a method of the type mentioned at the outset, in which oxygen-rich liquid from the sump of the low pressure column into the Evaporation passages of the first falling film evaporator and into the Evaporation passages of the second falling film evaporator is initiated.
  • the evaporation passages of the second falling film evaporator are According to the invention with non-evaporated liquid from the first falling film evaporator fed.
  • To prevent the falling film evaporator from running dry prevent liquid from entering the sump of the low pressure column Evaporation passages of the first falling film evaporator directed.
  • Even in the Evaporation passages of the second falling film evaporator must be total evaporation the liquid can be avoided.
  • the first falling film evaporator to supply with so much liquid from the sump of the low pressure column that enough unevaporated liquid remains in the second falling film evaporator is forwarded.
  • the second falling film evaporator is not evaporated Liquid from the first falling film evaporator and the other with one appropriate amount of liquid supplied from the bottom of the low pressure column, so that dry running is prevented.
  • the mixture emerging from the first falling film evaporator is advantageous generated vapor and unevaporated liquid into an essentially vapor containing part and a substantially liquid-containing part separately. Only the liquid is passed on to the second falling film evaporator.
  • the Vapor fraction is returned to the low pressure column or as a gaseous one Product taken from the system.
  • the invention is not based on the arrangement of only two cascaded falling film evaporators limited. It has varied Plant type and size also proven to be cheap, three or more falling film evaporators to be arranged in a row, i.e. the one emerging from the second falling film evaporator is not evaporated liquid to a third falling film evaporator. Furthermore, it can be advantageous if the first and / or the second falling film evaporator one or several other falling film evaporators are connected in parallel. In this case preferably those from the first and all connected in parallel to this Falling film evaporator emerging liquid merged and onto the second Falling film evaporators and any falling film evaporators arranged parallel to this distributed.
  • the first and second falling film evaporators are advantageous two to five times as much oxygen-rich liquid is supplied as vaporous oxygen in the respective falling film evaporator is generated. With this procedure is ensures that there is no dry running, i.e. no total evaporation of the liquid oxygen.
  • the second falling film evaporator only that in the first falling film evaporator evaporated amount of liquid from the bottom of the Low pressure column can be added. In other words: the first falling film evaporator becomes two to five times as much liquid from the bottom of the low pressure column fed as the second falling film evaporator.
  • the individual falling film evaporators are preferably arranged in such a way that those from the liquid emerging from the first falling film evaporator due to gravity alone Using a pump in the second falling film evaporator flows. The same applies of course for the flow connection between the second and one any third falling film evaporator.
  • the falling film evaporators are preferably further arranged so that the from the condensed nitrogen escaping from the second (or third) falling film evaporator static pressure back into the pressure column and the bottom from the second (or third) falling film evaporator due to evaporation of liquid oxygen static pressure flow back into the low pressure column to pump or others To save funding.
  • Figure 1 shows schematically a rectification unit for cryogenic air separation with a pressure column 1 and a low pressure column 2, as they are from the prior art is known. For the sake of clarity, the figure is limited to that for the Heat exchange between the pressure column 1 and the low pressure column 2 essential Components.
  • the rectification unit shown has two falling film evaporators 3, 4 which be used as the main condenser of the air separation plant.
  • the pressure column 1 and the low pressure column 2 are arranged side by side, the falling film evaporators 3, 4 are located above the pressure column 1.
  • gaseous nitrogen is drawn off via line 5 and via lines 6 and 7 into the respective liquefaction passages Falling film evaporator 3 and 4 initiated.
  • the one from the liquefaction passages of the The two falling-film evaporators 3, 4 then escaping nitrogen via lines 8 or 9 again applied to the top of the pressure column 1 as the return liquid.
  • the Falling film evaporators 3, 4 are arranged so that the nitrogen after the condensation can fall back into the pressure column 1 in the falling film evaporators 3, 4 with a gradient, without the need for a pump.
  • the oxygen-rich accumulating in the sump 10 of the low pressure column 2 Liquid is pumped to the top of the two with the help of a pump 11 via line 12 Falling film evaporator 3, 4 promoted and in with the upper header 31 of each Falling film evaporator 3, 4 connected jar 20 throttled.
  • Standing vessel 20 is a certain liquid level above the Evaporation passages maintained. On the one hand, this provides the necessary static pressure to determine the vapor generated in the evaporation passages and the to convey non-evaporated liquid down through the evaporation passages. On the other hand, this fluid level ensures that there is no vapor from the headspace the falling film evaporator 3, 4 enters the respective evaporation passages.
  • the vapor-liquid mixture is then via line 13 in the Low pressure column 2 returned.
  • Another line 14 branches off from line 13, via which vaporous oxygen can be removed as a product of the system.
  • One the upper and the lower header 31 of the two falling film evaporators 3, 4 connecting line 30 is used to a possible overpressure or underpressure in one to balance the header 31.
  • the two falling film evaporators 3, 4 are operated with an excess of oxygen-rich liquid in order to prevent them from running dry. For example, 100,000 Nm 3 / h of oxygen are to be evaporated in the main condenser, ie 50,000 Nm 3 / h are generated in each falling film evaporator 3, 4. For safety reasons, the falling film evaporators 3, 4 are charged with three times the amount of liquid oxygen, ie with 150,000 Nm 3 / h each. In total, 300,000 Nm 3 / h of liquid oxygen are conveyed by the pump 11 from the sump 10 of the low-pressure column 2 to the top of the falling film evaporators 3, 4.
  • the height of the pressure column should be 14 m and the falling film evaporators 3, 4 should each have a height of 8 m.
  • FIG. 2 shows a rectification unit corresponding to FIG. 1, the two Falling film evaporators 203, 204 are arranged according to the invention.
  • the pressure column 1 and the low pressure column 2 and the pump 211 are set up on the ground.
  • the falling film evaporator 203 is located above the falling film evaporator 204, so that a fluid emerging from the falling film evaporator 203 below due to the Gravity can flow to the top of falling film evaporator 204.
  • Both Falling film evaporators 203, 204 are analogous to FIG. 1 via lines 205, 206, 207 supplied with pressurized nitrogen from the pressure column 1 as the heating medium.
  • the one from the Liquefaction passages emerging nitrogen is via lines 208, 209 in the Pressure column 1 returned.
  • the lower falling film evaporator 204 is arranged so that the outlet openings of its liquefaction passages above the Pressure column 1 are. The return of the condensed nitrogen to the Pressure column 1 can be done without using
  • the liquid oxygen withdrawn from the sump 10 of the low pressure column 2 becomes partly via line 215 on top of the falling film evaporator 203, partly via line 216 pumped on top of the falling film evaporator 204.
  • the separator 219 the generated steam and the excess liquid are separated. The latter is then over Line 217 on top of the falling film evaporator 204, the generated steam is returned via lines 232 and 218 to the low pressure column 2 or partially withdrawn as a product via line 214.
  • Line 230 is used to equalize the pressure between the upper and lower ends of the Falling film evaporator 203.
  • the falling film evaporator 204 is made with the excess liquid via line 217 the upper falling film evaporator 203 and via line 216 with fresh liquid fed.
  • the one emerging from the evaporation passages of this evaporator 204 The vapor-liquid mixture is fed via line 218 into the low-pressure column 2 returned.
  • the boundary conditions of the air separation plant according to FIG. 2 should correspond to those of the plant according to FIG. 1.
  • each falling film evaporator 203, 204 in turn, 50,000 Nm 3 / h of gaseous oxygen are to be generated.
  • the ratio of the application of liquid oxygen to the amount of steam generated should also be three.
  • 150,000 Nm 3 / h of liquid oxygen must be fed into the upper falling film evaporator 203.
  • 50,000 Nm 3 / h of oxygen vapor and 100,000 Nm 3 / h of excess liquid are obtained.
  • 50,000 Nm 3 / h liquid oxygen are added via line 216, which is pumped to this point by the pump 211.
  • the mixture of excess liquid from the falling film evaporator 203 and fresh oxygen is fed to the lower falling film evaporator 204.
  • the lower falling film evaporator 204 also delivers 50,000 Nm 3 / h of vaporous oxygen and 100,000 Nm 3 / h of excess liquid.
  • the pump 211 must deliver a total of 200,000 Nm 3 / h of liquid oxygen.
  • the total delivery head is greater than in the arrangement according to FIG. 1.
  • the pump 211 must deliver the liquid oxygen via the height of the pressure column 1 and the two falling film evaporators 203, 204.
  • the pump energy is proportional to the product of the amount of liquid and total head.
  • the energy cost is higher in the manner known from the prior art arrangement according to FIG 1 thus by 10% than the inventive arrangement according to Figure 2.
  • the pump 11 to be designed for 300,000 Nm 3 / h of liquid oxygen, while in the solution according to the invention a pump 211 designed for 200,000 Nm 3 / h of liquid oxygen is sufficient.
  • the pump 211 can be made one third smaller than the pump 11.
  • FIG. 3 shows an alternative embodiment of the arrangement according to FIG. 2 shown.
  • This embodiment differs from that according to FIG. 2 only in that that the two falling film evaporators 203, 204 are connected directly to one another.
  • the Upper falling film evaporator 203 sits directly on with its gas-liquid separator 219 the upper standing vessel 220 of the falling film evaporator 204.
  • Between the two Falling film evaporators 203, 204 are thus a component 219, 220 in which the vapor generated in the upper falling film evaporator 203 from the corresponding one Excess liquid is separated and the excess liquid together with the fresh liquid supplied from the in connection with the explanation of the standing vessel 20 in FIG. 1 for reasons.
  • the piping of the two Falling film evaporator 203, 204 is thereby considerably simplified.
  • the arrangement according to the invention of three falling film evaporators can be seen in FIG.
  • the excess liquid of the top falling film evaporator 403 on top of the evaporation passages of the falling film evaporator 404 and the Excess liquid of this falling film evaporator 404 in turn in the top Falling film evaporator 421 passed.
  • Each of the falling film evaporators 403, 404, 421 is over the pump 411 and the lines 415, 416, 422 from the sump 10 of the Low pressure column 2 additionally supplied with fresh liquid oxygen.
  • the single ones Falling film evaporators 403, 404, 421 are analogous to the embodiment according to FIG Pipelines 417, 423 connected. A direct connection between the falling film evaporators 403, 404, 421 analogous to FIG. 3, so that the lines 417, 423 are omitted possible.
  • a total of 100,000 Nm 3 / h of vaporous oxygen should again be generated, ie 33,333 Nm 3 / h of steam in each falling film evaporator 403, 404, 421.
  • the individual falling film evaporators 403, 404, 421 are also to be acted upon again by a factor of three.
  • the following table shows the pump energy ratios for different pressure column heights between 14m and 24m when using the falling film evaporator arrangement according to the invention in comparison to the conventional arrangement.
  • the relative energy requirements are compared in the case of a parallel arrangement of the falling film evaporators (1 floor), the arrangement according to the invention of two falling film evaporators in series one above the other (2 floors) and in the case of an arrangement according to the invention of three serial falling film evaporators one above the other (3 floors).
  • the energy requirement is standardized in each case on the use of two falling film evaporators (2 floors) connected in series at a pressure column height of 14 m.
  • the overall height of the falling film evaporators is assumed to be 8 m.
  • Pressure column height [in meters] Relative energy requirements (standardized on 2 floors with pressure column height 14m) 1. floor 2 floors 3 floors 14 1.10 1.00 1.06 15 1.15 1.03 1.08 16 1.20 1.07 1.11 17 1.25 1.10 1.14 18 1.30 1.13 1.17 19 1.35 1.17 1.19 20 1.40 1.20 1.22 21 1.45 1.23 1.25 22 1.50 1.27 1.28 23 1.55 1.30 1.31 24 1.60 1.33 1.33
  • Table 2 shows the pump's energy requirements as a function of the pressure column height, whereby the variant with 2 levels was standardized to 1 for each pressure column height.
  • the values entered in the "1 level” and “3 levels” columns thus directly show the energy ratio of the respective arrangement to the corresponding arrangement with two serial falling film evaporators.
  • Pressure column height [in meters] Relative energy requirements (standardized on 2 floors) 1. floor 2 floors 3 floors 14 1.10 1.00 1.06 15 1.11 1.00 1.05 16 1.12 1.00 1.04 17 1.14 1.00 1.04 18 1.16 1.00 1.03 19 1.17 1.00 1.02 20 1.18 1.00 1.02 21 1.18 1.00 1.01 22 1.18 1.00 1.01 23 1.19 1.00 1.00 24 1.20 1.00 1.00

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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)
EP02009897A 2002-02-13 2002-05-02 Tieftemperatur-Luftzerlegungsverfahren Withdrawn EP1336805A1 (de)

Priority Applications (5)

Application Number Priority Date Filing Date Title
DE10205878A DE10205878A1 (de) 2002-02-13 2002-02-13 Tieftemperatur-Luftzerlegungsverfahren
EP02009897A EP1336805A1 (de) 2002-02-13 2002-05-02 Tieftemperatur-Luftzerlegungsverfahren
CNB031038697A CN100380078C (zh) 2002-02-13 2003-02-13 低温空气分离方法
JP2003034815A JP2003240430A (ja) 2002-02-13 2003-02-13 低温空気精留法
US10/365,610 US7134297B2 (en) 2002-02-13 2003-02-13 Low-temperature air fractionation process

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10205878A DE10205878A1 (de) 2002-02-13 2002-02-13 Tieftemperatur-Luftzerlegungsverfahren
DE10205878 2002-02-13
EP02009897A EP1336805A1 (de) 2002-02-13 2002-05-02 Tieftemperatur-Luftzerlegungsverfahren

Publications (1)

Publication Number Publication Date
EP1336805A1 true EP1336805A1 (de) 2003-08-20

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Application Number Title Priority Date Filing Date
EP02009897A Withdrawn EP1336805A1 (de) 2002-02-13 2002-05-02 Tieftemperatur-Luftzerlegungsverfahren

Country Status (5)

Country Link
US (1) US7134297B2 (ja)
EP (1) EP1336805A1 (ja)
JP (1) JP2003240430A (ja)
CN (1) CN100380078C (ja)
DE (1) DE10205878A1 (ja)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010142894A3 (fr) * 2009-06-12 2012-11-15 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil et procédé de séparation d'air par distillation cryogénique
CN103998883A (zh) * 2011-09-20 2014-08-20 林德股份公司 低温分离空气的方法和设备
WO2015167699A3 (en) * 2014-05-01 2015-12-30 Praxair Technology, Inc. System and method for production of argon by cryogenic rectification of air
US10060673B2 (en) 2014-07-02 2018-08-28 Praxair Technology, Inc. Argon condensation system and method
US10337792B2 (en) 2014-05-01 2019-07-02 Praxair Technology, Inc. System and method for production of argon by cryogenic rectification of air

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1837614A1 (de) * 2006-03-23 2007-09-26 Linde Aktiengesellschaft Verfahren und Vorrichtung zum Verdampfen einer sauerstoffangereicherten Einsatzflüssigkeit und Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
FR2955926B1 (fr) * 2010-02-04 2012-03-02 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
WO2014173496A2 (de) * 2013-04-25 2014-10-30 Linde Aktiengesellschaft Verfahren zur gewinnung eines luftprodukts in einer luftzerlegungsanlage mit zwischenspeicherung und luftzerlegungsanlage
US11320198B2 (en) * 2020-06-25 2022-05-03 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procedes Georges Claude Method for improved startup of an air separation unit having a falling film vaporizer

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5699671A (en) * 1996-01-17 1997-12-23 Praxair Technology, Inc. Downflow shell and tube reboiler-condenser heat exchanger for cryogenic rectification
EP0926457A2 (en) * 1997-12-23 1999-06-30 The Boc Group, Inc. Method of operating the lower pressure column of a double distillation column
USRE36435E (en) * 1989-07-28 1999-12-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Vaporization-condensation apparatus for air distillation double column, and air distillation equipment including such apparatus

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS60253782A (ja) * 1984-05-30 1985-12-14 日本酸素株式会社 大型空気分離装置用凝縮器
FR2650379B1 (fr) * 1989-07-28 1991-10-18 Air Liquide Appareil de vaporisation-condensation pour double colonne de distillation d'air, et installation de distillation d'air comportant un tel appareil
US5122174A (en) * 1991-03-01 1992-06-16 Air Products And Chemicals, Inc. Boiling process and a heat exchanger for use in the process
FR2685459B1 (fr) * 1991-12-18 1994-02-11 Air Liquide Procede et installation de production d'oxygene impur.
DE59901114D1 (de) * 1998-01-30 2002-05-08 Linde Ag Verfahren und vorrichtung zum verdampfen von flüssigem sauerstoff
DE19950570A1 (de) * 1999-10-20 2001-04-26 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
USRE36435E (en) * 1989-07-28 1999-12-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Vaporization-condensation apparatus for air distillation double column, and air distillation equipment including such apparatus
US5699671A (en) * 1996-01-17 1997-12-23 Praxair Technology, Inc. Downflow shell and tube reboiler-condenser heat exchanger for cryogenic rectification
EP0926457A2 (en) * 1997-12-23 1999-06-30 The Boc Group, Inc. Method of operating the lower pressure column of a double distillation column

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010142894A3 (fr) * 2009-06-12 2012-11-15 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil et procédé de séparation d'air par distillation cryogénique
CN103998883A (zh) * 2011-09-20 2014-08-20 林德股份公司 低温分离空气的方法和设备
CN103998883B (zh) * 2011-09-20 2016-12-14 林德股份公司 低温分离空气的方法和设备
WO2015167699A3 (en) * 2014-05-01 2015-12-30 Praxair Technology, Inc. System and method for production of argon by cryogenic rectification of air
US9291389B2 (en) 2014-05-01 2016-03-22 Praxair Technology, Inc. System and method for production of argon by cryogenic rectification of air
US9599396B2 (en) 2014-05-01 2017-03-21 Praxair Technology, Inc. System and method for production of crude argon by cryogenic rectification of air
US10337792B2 (en) 2014-05-01 2019-07-02 Praxair Technology, Inc. System and method for production of argon by cryogenic rectification of air
US10060673B2 (en) 2014-07-02 2018-08-28 Praxair Technology, Inc. Argon condensation system and method
US10082333B2 (en) 2014-07-02 2018-09-25 Praxair Technology, Inc. Argon condensation system and method
US10190819B2 (en) 2014-07-02 2019-01-29 Praxair Technology, Inc. Argon condensation system and method
US10247471B2 (en) 2014-07-02 2019-04-02 Praxair Technology, Inc. Argon condensation system and method

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US7134297B2 (en) 2006-11-14
US20040055331A1 (en) 2004-03-25
DE10205878A1 (de) 2003-08-21

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