CN1124345A - Method and apparatus for seperating air in low temperature - Google Patents

Method and apparatus for seperating air in low temperature Download PDF

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Publication number
CN1124345A
CN1124345A CN95105025A CN95105025A CN1124345A CN 1124345 A CN1124345 A CN 1124345A CN 95105025 A CN95105025 A CN 95105025A CN 95105025 A CN95105025 A CN 95105025A CN 1124345 A CN1124345 A CN 1124345A
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pressure stage
low
stage
pressure
liquid
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威廉·罗德
迪特里希·勒特曼
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • 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
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • 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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04478—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Abstract

The present invention provides a method and device of separating air at the lower temperature. At least a part of compressed, refined and cooled air is introduced into a pressure stage of a double stage rectification column. An oxygen fraction 11 and a nitrogen-containing fraction are taken out as product from a low pressure stage. A lower region of the low pressure stage is connected to an upper region of the pressure stage in heat exchange. In the normal operation, almost all flux liquid flowing down on the low pressure stage is taken out of the lower region of the low pressure means to be introduced into a buffer. A liquid from the buffer undergoes an indirect heat exchange with a condensed gas from the upper region of the pressure stage to be partially evaporated. Vapor and thus generated is supplied to the lower region of a low pressure column. At least the portion of the liquid as intact is returned to the bugger to be stored.

Description

The method of low temperature air separating and device
The present invention relates to a kind of method and device of low temperature air separating, in described method, air is compressed, purify, cooling, be admitted in the pressure stage of two stage rectification equipment then at least in part, then, at least a fraction that flows out from pressure stage is further separated low-pressure stage, and the oxygen fraction and the nitrogenous fraction that extract in the low-pressure stage flow as product, and make the lower area of low-pressure stage and the upper area of pressure stage be heat exchange relationship.
The principle of seperating air by rectification has been disclosed in the document of relevant handbook [for example the 4th chapter of 4.5 chapters of " cryogenic technique " of being write by Hausen/Linde (1985 the 2nd edition) or " chemical technology " second volume (the 3rd edition) of being write by Winnacker/Kuechler] and " distillation of air " [chemical engineering progress 63 volumes 35 pages-59 pages (Latimer writes)].Above-mentioned two stage rectification carries out in a double tower in a usual manner, and the low-pressure stage of double tower is set at the top of pressure stage.(low-pressure stage of double tower and pressure stage also can divide and be arranged in principle.) evaporate the backflow that is formed for pressure stage by making the liquid that flows out from low-pressure stage, simultaneously, in low-pressure stage, produce the steam that rises.This indirect heat exchange is carried out in a condenser/evaporator, and this evaporimeter is arranged in the lower pressure column, is in the bottom (Sumpf) of lower pressure column in the mode of routine.This in principle arrangement is favourable, because saved some pipe specials that the evaporation channel and the lower pressure column of condenser/evaporator are coupled together.Also there is shortcoming.So, condenser/evaporator is not unessential for the total height of double tower, and therefore, the cost of device is higher.In addition, when device was out of service, whole phegmas of low-pressure stage flowed into the bottom, and are polluted by nitrogen.Therefore, when device starts once more, prolonged start-up time, till providing the pure oxygen product again, started and to finish.
The object of the present invention is to provide a kind of specification to begin described method and apparatus, they are favourable economically, especially by reducing cost or making it have superiority economically by the flexibility that improves operation.
The technical scheme that realizes above-mentioned purpose is: when stable operation, the phegma that all flows into low-pressure stage is substantially extracted out from the lower area of low-pressure stage, and it is sent in the buffer container, from described buffer container, extract liquid, make itself and a gas for the treatment of condensation that flows out from the pressure stage upper area carry out indirect heat exchange and the part evaporation; The steam that forms is sent into the lower area of low-pressure stage at least in part, and remaining liq is sent back in the buffer container at least in part.
Air separation unit entered normal running status after term " stable operation " meant and starts end herein, in this state, (in the situation of interchangeable storing apparatus, at least 10 minutes remain with all the time in the device to a couple of days or several weeks the product that needs) feed stream and product stream are kept constant substantially in the very long cycle.
According to the present invention, when stable operation, substantially whole phegmas are sent in the buffer container (for example receiver).That is to say, the small part phegma can be imported another road, for example extract or discharge by a safety dumping mouth as liquid form product.But that part of phegma that forms the rising steam in tower should be imported in the above-mentioned buffer container at least.
The preferably adiabatic receiver of above-mentioned buffer container.Again liquid is extracted out from above-mentioned jar, made it to carry out indirect heat exchange with the nitrogen rich vapor that flows out from pressure column and evaporate.The portion gas at least (preferably most of gas) that produces in the said process is imported lower pressure column, and form the steam with the rising of phegma reverse flow in this tower, another part gas can be used as oxygen product when needed and is extracted.Usually, this part oxygen by with the air heat to be separated that is roughly environment temperature of its adverse current.The part that the liquid that extracts from receiver is not evaporated during carrying out indirect heat exchange (for example with the backflow of flowing out from above-mentioned tower) is sent back to the buffer container again.
Aforesaid liquid can expense be carried with pump cheaply.For example pump can be arranged on the downstream of surge tank, also can on the pipeline from the low-pressure stage to the buffer container, establish pump, perhaps on above-mentioned pipeline, set up a pump again, this moment, buffer container itself or be arranged on made the top of the heat exchanger of the liquid evaporation of flowing out from jar, perhaps was in above under the atmospheric state.
Because unevaporated phegma mixes with a jar interior retentate, does not need to keep the height of liquid in the lower pressure column.According to method of the present invention, perhaps only (for example need keep extremely low liquid height, be about 300 to 2000mm water columns with liquid height in the known method so far and compare, only need keep 10mm to the highest 50mm water column), perhaps retain liquid not fully in the bottom of low-pressure stage (Sumpf).
Owing to shifted out condenser/evaporator, more help and needn't in tower, retain soiling solution, therefore, the corresponding building height that reduces rectifying column.This is especially favourable for the large-scale setting that the double tower height reaches 40m.In addition, because carbohydrate is in low-pressure stage bottom rather than the trend of increase is arranged in tower, also be very favourable with regard to operational reliability, and great surge volume is arranged in the container.
In addition, can to obtain substantially be pure oxygen product all the time in the evaporation of thing in the monoblock type buffer container can be under tower moves the situation of imperfect stability (under the situation about breaking down or rate of air circulation variation has taken place) by jar.Because the quality of the oxygen product that flows out from lower pressure column and the fluctuation of output are cushioned, the inventive method uses very flexible.
Moreover, the integrated control procedure of simplifying this method in the buffer container.Thus, controlled variable is the height of liquid in the jar.This variable can observe simply, and obviously is in non-critical state.What only must guarantee is that jar can not be emptied completely or all be full of, and the containing quantity in jar in principle can be in above-mentioned arbitrarily change between the two.(, in fact often keep medium liquid height in order to utilize buffering effect really.) this is for the height that need observe out pot liquid sometimes, it is enough increasing or reduce the cold and/or inner product of extraneous biography cold when liquid height decline or rising then.Can realize above-mentioned adjustment process automatically in principle.Because need to mate refrigeratory capacity at normal in service in the long time interval (according to the size of jar, about 10 hours to 5 days finish), above-mentioned control also can manually be carried out.In the method, for example work done in turbine is expanded and is obtained cold by means of air or nitrogen, like this, and for example available refrigeratory capacity of manually suitably regulating turbine.
If for making the liquid of extracting out the container from buffering partly evaporate the indirect heat exchange of carrying out is to carry out then more favourable with the form of sedimentation film evaporation (Fallfilmverdampfung).Relevant heat exchanger is described at " application of evaporation and evaporation technique " (1981) 3.5.5 chapters that Billet writes as the details of sedimentation film evaporator work.About 25% to 75% (weight) in this sedimentation film evaporator, preferably the liquid that goes out from the buffering container flow of 40% to 60% (weight) is evaporated.Residue sends back in the jar again usually.
In some applications, for example in the steel industry, very unstable to the demand of air products especially oxygen.Do not have other application possibility as fruit product, air separation plant must stop production sometimes.Because daytime, energy expenditure was changeable, air separation unit is operation by spells usually.Because of (perhaps also possible) after the above-mentioned reason outage because of after the outage that breaks down, device need restart, because device itself also is in cold state, reaches stable state heavily again and can provide the product of predetermined purity often to need the long period (up to 2 hours) to rectifying action.
The important improvement of the inventive method is: when outage begins, will send into the lower area of pressure stage from the phegma that low-pressure stage flows out.
It is open already in the DE-A-3732363 document to store phegma.But in the described method of the document, need special equipment to receive phegma.Method of the present invention needs optional equipment hardly, can adopt the safety dumping pipeline of originally just having installed to derive phegma, only needs to link to each other with pressure stage, and for example the pipeline through importing separation of air communicates with pressure stage.
When device damaged, the air compressor machine stall made the connection disconnection that phegma is imported buffer container, and makes towards the pipeline of pressure column open-minded.(if the pipeline that communicates with jar is arranged on the top of the pipeline that communicates with pressure column, does not then need to disconnect the pipeline that communicates with jar).Therefore still be deposited in the phegma in the lower pressure column owing to the bottom that influences the feed pressure tower of its gravity, can prevent that nitrogenous phegma from polluting the product that is deposited in pot bottom.
When restarting, can in the shortest time, resupply pure oxygen product.After the air compressor machine entry into service a few minutes molecular sieve just can the purifying air, the pressure tower weight reaches its operating pressure again.In case have the overhead stream over-heat-exchanger of the gas of certain pressure from pressure stage, the oxygen that flows out from jar is with regard to start vaporizer, and wherein, the fraction that evaporates (oxygen that flows out from jar) can be directly as the product with general purity.The time (as 1 minute to 5 minutes) that rectifying action reaches steady operational status can remedy by the liquid that is stored in the surge tank is evaporated, and can not influence the purity or the output of product.
The invention still further relates to a kind of device as the described low temperature air separating of claim 4 to 6.
An embodiment represented below in conjunction with accompanying drawing is described in detail the present invention and other content of the present invention.As for as in the flow process as the details of expand producing cold turbine or directly air being imported lower pressure column not shown through the signal of having simplified greatly.Air compressed and that purify is sent in the pressure stage 3 of twin-stage tower 2 by pipeline 1.(part air to be separated also can directly be admitted to low-pressure stage 4, for example after work done is expanded).The gas at pressure stage top is admitted in the condenser/evaporator 6 and all condensations of quilt through pipeline 5, and formed liquid flow back into the top of pressure stage 3 through pipeline 7 simultaneously.The partially liq of feed pressure level is as the phegma in the pressure column 3, and another part liquid is admitted in the lower pressure column 4.(can link to each other with pressure column 3 with the pipeline 8 that above-mentioned lower pressure column communicates, also can directly link to each other) with the condensate conduit 7 of condenser/evaporator 6.In addition, bottom liquid (Sumpfflussigkeit) 9 that flows out from pressure column by throttling, extracts rich nitrogen product stream 10 in the centre position of lower pressure column 4 from the lower pressure column top.Extract the phegma of lower pressure column 4 through pipeline 11 from the lower end of lower pressure column.When stable operation, above-mentioned phegma is made up of the oxygen of the residual impurity that contains 100ppm to 20%, and best above-mentioned residual impurity content is 0.3% to 10%.Pipeline 11 is installed in the bottom of comparison near the container that constitutes lower pressure column 4, therefore, at the bottom of the tower, seldom or does not in fact at all have liquid.
Liquid oxygen 12 flows into as in the oxygen holder 13 of buffer container.Can flow pipeline 14 by product when needing and extract a part as liquid form product.In the embodiment shown in the figures, keep pressure in jars 13, therefore, have certain pressure from above-mentioned jar of liquid that flows out, flows into as the condenser/evaporator 6 of sedimentation film evaporator through pipeline 16 by pump 15.(in the stress-free situation of hold-up vessel, said pump should be arranged on the pipeline 16.
Discharge through pipeline 17 from the two-phase mixed flow that the boiler channel of condenser/evaporator 6 flows out, the part of its steam part flows back in the lower pressure column 4 through pipeline 18, and another part is extracted as oxygen product stream 19.The remaining liq part sends back in the buffer container 13 through pipeline 12 again.
Another root fluid pipeline 20 communicates with the lower area of low-pressure stage 4, and preferably this pipeline is arranged on the outlet part that is lower than pipeline 11.When the normal operation of device, the aforesaid liquid pipeline is obstructed.(in case of necessity, for safety, can make occasionally small amount of liquid flow through this opening and discharge and abandon it by the safe outlet shown in the end).When interrupt run, the valve 21 that air compressor machine restores on the pipeline 11 of back is closed, and makes it and jars 13 disconnections that be connected, and simultaneously, opens by part 22, makes in the phegma inflow pressure column that flows into bottom the lower pressure column, and is retained in the bottom of pressure column.(according to pipeline 11 and 20 and the arrangement of low-pressure stage 4 link positions, phegma is only flowed out through pipeline 20, in this case, can save the valve 21 on the pipeline 11).
When device restarts, in the extremely short time, purer oxygen product is discharged through pipeline 19.That is to say that in case pressure stage 3 reaches required operating pressure, 5 of top gas flow to condenser/evaporator 6, evaporate in above-mentioned evaporimeter.Because the pure oxygen that will flow out from surge tank 13 input evaporation side, and then, the gas products in the pipeline 19 can provide use again at any time.Starting time (promptly occurring stable product design institute elapsed time in lower pressure column once more) also can be adjusted by thing in the part evaporator.Because low-pressure stage neutrality can provide the oxygen with adequate purity behind condenser/evaporator 6 start vaporizers, the phegma (11) that flows out from lower pressure column after the entry into service comprises conventional component equally, and can flow in the jar 13 through pipeline 12 immediately.
Being connected between low-pressure stage 4 one sides and the pipeline 17,/12 18 and 11 also can realize by the big pipe of an independent cross section, make the reverse flow each other of liquid and steam, 17/12 in above-mentioned pipeline is between the opposite side of the evaporation path of condenser/evaporator 6 and surge tank 13.

Claims (6)

1, the method of low temperature air separating, wherein air is compressed, purify, cooling, gone at least in part then in the pressure stage (3) of two stage rectification equipment (2), at least a fraction (8 that in this process, obtains, 9) flow into low-pressure stage (4) from pressure stage (3), and in low-pressure stage, further separate, the oxygen fraction (11) and the nitrogenous fraction (10) that extract in the low-pressure stage (4) flow as product, the lower area of low-pressure stage (4) and the upper area of pressure stage are heat exchange relationship, it is characterized in that when stable operation, the phegma (11) that all flows into low-pressure stage (4) is substantially extracted out from the lower area of low-pressure stage, and with in its buffer container of importing (13), extract stream (16) from buffering container (13) makes it to carry out indirect heat exchange and be evaporated with the condensed gas (5) for the treatment of from the outflow of pressure stage (3) upper area; Formed steam (17,18) is imported the lower area of low-pressure stage (4) at least in part, and will in indirect heat exchange, send back in the buffer container (13) by left partially liq at least (17,12).
2, the method for claim 1, it is characterized in that making the indirect heat exchange process of liquid stream (16) the part evaporation of extracting from buffering container (13) is to carry out with the form of sedimentation film evaporation.
3, method as claimed in claim 1 or 2 when it is characterized in that outage begins, will import the lower area of pressure stage (3) from the phegma (20) that low-pressure stage (4) flows out.
4, the device of low temperature air separating, it comprises an air compressor machine, a cleaning equipment, a heat exchanger, a twin-stage rectifying device (2) of forming by pressure column (3) and lower pressure column (4), an and condenser/evaporator (6), this evaporimeter communicates with the upper area of pressure column (3) through steam flow ipe (5) and condensate liquid reflux line (7), and has an evaporation channel that makes the liquid evaporation of flowing out from lower pressure column (4) lower area, it is characterized in that also comprising the reflux pipeline (11 that links to each other with buffering container (13) with the low-pressure stage lower area, 12), the fluid pipe (16) that leads to the evaporation channel inlet of condenser/evaporator (6) from buffering container (13), the evaporation tubes (17 that connects evaporation channel outlet and lower pressure column (4) lower area, 18), and the backpass ductwork (17,12) of the liquid between outlet of loopback evaporation channel and the buffer container (13).
5, device as claimed in claim 4 is characterized in that above-mentioned condenser/evaporator (6) is the sedimentation film evaporator.
6, as claim 4 or 5 described devices, it is characterized in that also comprising the fluid pipe (20) that leads to pressure column (3) from the lower area of lower pressure column (4), on this pipeline, be equipped with by part (22).
CN95105025A 1994-05-04 1995-05-04 Method and apparatus for seperating air in low temperature Pending CN1124345A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4415747A DE4415747C2 (en) 1994-05-04 1994-05-04 Method and device for the low-temperature separation of air
DEP4415747.9 1994-05-04

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CN1124345A true CN1124345A (en) 1996-06-12

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EP (1) EP0681153B1 (en)
JP (1) JPH0842962A (en)
KR (1) KR950033380A (en)
CN (1) CN1124345A (en)
DE (2) DE4415747C2 (en)
ES (1) ES2106594T3 (en)
GR (1) GR3025534T3 (en)
PL (1) PL308454A1 (en)
TW (1) TW288984B (en)

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CN100436989C (en) * 2004-01-29 2008-11-26 宝山钢铁股份有限公司 Method for preparing high purity oxygen using full low pressure air separation plant
CN108014601A (en) * 2016-11-04 2018-05-11 林德股份公司 Method and apparatus for purification gas
CN112629160A (en) * 2020-12-21 2021-04-09 华能（天津）煤气化发电有限公司 Air separation natural reheat overhauling method

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DE19732887A1 (en) * 1997-07-30 1999-02-04 Linde Ag Air separation process
US6272884B1 (en) 1998-04-08 2001-08-14 Praxair Technology, Inc. Rapid restart system for cryogenic air separation plant
FR2797942B1 (en) * 1999-08-24 2001-11-09 Air Liquide VAPORIZER-CONDENSER AND CORRESPONDING AIR DISTILLATION SYSTEM
FR2802825B1 (en) * 1999-12-23 2002-05-03 Air Liquide DISTILLATION SEPARATION APPARATUS AND METHOD FOR CLEANING A CONDENSER VAPORIZER OF THE APPARATUS
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DE4415747A1 (en) 1995-11-16
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EP0681153B1 (en) 1997-09-10
PL308454A1 (en) 1995-11-13
EP0681153A1 (en) 1995-11-08
GR3025534T3 (en) 1998-02-27
ES2106594T3 (en) 1997-11-01
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JPH0842962A (en) 1996-02-16
KR950033380A (en) 1995-12-22

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