CN102564063A - Method and apparatus for separating air under low temperature - Google Patents

Method and apparatus for separating air under low temperature Download PDF

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Publication number
CN102564063A
CN102564063A CN2011103491266A CN201110349126A CN102564063A CN 102564063 A CN102564063 A CN 102564063A CN 2011103491266 A CN2011103491266 A CN 2011103491266A CN 201110349126 A CN201110349126 A CN 201110349126A CN 102564063 A CN102564063 A CN 102564063A
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tower
pressure
lower pressure
pressure column
column
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CN2011103491266A
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CN102564063B (en
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A·阿列克谢耶夫
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04745—Krypton and/or Xenon
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"

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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)

Abstract

A method and an apparatus for separating air under low temperature used in a nitrogen-oxygen separation distillation tower system are provided. The distillation tower system is provided with a high pressure tower (2) and a low pressure tower (3), wherein a first fluid (16,17,27) is ejected in liquid form from the high pressure tower (2) and guided into (22,23,30) the lower pressure tower (3). A first liquid ejection pump (15,28) is used to convey the first fluid from the high pressure tower to the low pressure tower.

Description

The method and apparatus of low temperature air separating
Technical field
The present invention relates to the method and the corresponding apparatus of low temperature air separating.
Background technology
These class methods often are designed to the double tower process, wherein especially lower pressure column are arranged on the high-pressure tower top.Substituting ground, lower pressure column and high-pressure tower can be to be used for three towers of air separation or the parts of multitower system.Other are used to obtain the particularly device of rare gas of high-purity product and/or other constituent of air except nitrogen-can also be provided with extraly the oxygen knockout tower, for example obtain argon and/or obtain the device of krypton-xenon.
Term " lower pressure column " and " high-pressure tower " generally use with common speech habits at this.These terms are meant be used for that nitrogen-oxygen separates two knockout towers arbitrarily, and wherein the operating pressure of high-pressure tower is higher than the operating pressure of lower pressure column.Under the situation of traditional double tower system, it meets common speech habits.For example in three tower bodies system, " lower pressure column " both can be represented the tower with minimum pressure, also can represent the tower (so-called intermediate pressure column) of intermediate pressure; " high-pressure tower " is the tower with maximum pressure, or the tower of intermediate pressure.
The preferred arrangement of two towers of said double tower is that so-called " tower self " arranged (overlapping tower), is positioned at the top of high-pressure tower at this lower pressure column.This arrangement mode is saved the space especially.More valuablely be; For liquid (from the rough oxygen of high-pressure tower bottom, from the washing-LIN on high-pressure tower top, optional extra fluid from the high-pressure tower medium position etc.) is transported to lower pressure column (directly or through the argon parts) from high-pressure tower; Do not use pump; Only carry liquid through pressure differential (usually, in high-pressure tower, be about 6 crust, in lower pressure column, be about 1.5 crust).
But (for example has greater than 50 000Nm more greatly 3The oxygen product of/h or greater than 250,000Nm 3Under the situation of the device raw air of/h), the size of tower causes this pressure differential to be not enough to liquid is delivered to the height of lower pressure column.In the case, in order to carry liquid, use one or more extra mechanical pumps.
But this method has important disadvantages.Because this additional hardware assembly causes significant extra cost.In addition, the availability of whole air-separating plant and reliability owing to these rotations and the machine that therefore is subject to basically disturb have a negative impact; The quantity of the machine of rotation is many more, then because mechanical disorder causes the probability of this failure of apparatus just high more.Can damage the economy of overall planning thus.
Common technical scheme is, all pumps all are installed in the double casing.At this, have only a pump normally to move, second unnecessary machine be with non-loaded mode synchronous operation (standby operation), but when first machine failure, can replace immediately and bear required function.Though this scheme has been improved availability, significantly improved the expense of device.
Summary of the invention
Therefore, the present invention is based on the purpose of the method that the said type of beginning is provided, and wherein reliably liquid is delivered to lower pressure column from high-pressure tower, and formation has the big air separation equipment that tower self is arranged in this way.
This purpose solves so that first fluid is delivered to the lower pressure column from high-pressure tower through using first liquid jet pump (Fl ü ssigkeitsstrahlpumpe).
Replace mechanical pump also to use liquid jet pump.The high-pressure spray that use has existed in equipment (throttling stream
Figure BSA00000607564800021
and interior compressive flow innenverdichtete
Figure BSA00000607564800022
) drives liquid jet pump, does not therefore need extra mechanical pump.
Liquid jet pump does not comprise mechanical moving element, and is therefore reliable especially and durable.In addition, the cost of liquid jet pump is starkly lower than mechanical pump, and this is because this equipment is quite simple, includes only a spot of member, and does not for example need motor to drive.
In category of the present invention, can also use two or more liquid jet pumps, so that second fluid and the fluid of choosing other wantonly are delivered to the lower pressure column from high-pressure tower.
In addition, the invention still further relates to the equipment of low temperature air separating.
Description of drawings
Accordinging in the accompanying drawings below, illustrated embodiment sets forth the present invention and other details of the present invention in more detail.
The specific embodiment
Do not demonstrate air compression plant, air cleaning unit, main heat exchanger and middle-pressure turbine in the drawings, make the pressure of a part of raw air from high pressure relief to high-pressure tower through it; These method steps constitute with common mode.To import from the gaseous air 1 (GAP) of main heat exchanger and be arranged in the high-pressure tower 2 of lower pressure column 3 belows.Can use portion of air 43 with the rough-krypton-xenon tower of heating at the device 35 that is used for obtaining krypton-xenon.Main condenser 4 is that condenser-reboiler is positioned between the two, connects high-pressure tower and lower pressure column through this main condenser with the mode of heat exchange.
High pressure air flow 5 i.e. joule-thomson-air (JL) (JT) is in than under the high-pressure tower 2 obvious higher pressure, and in choke valve 6 and/or generator turbine 7, reduces pressure to and be about the pressure of high-pressure tower.High pressure air flow through the overwhelming majority of decompression is liquid is distributed between high-pressure tower and lower pressure column in the present embodiment.First flow to the medium position of high-pressure tower 2 through pipeline 8.One or more medium positions that remainder flow to lower pressure column are to pass through cold-reverse stream pipe 12 and choke valve 11 through pipeline 9 and 10; Perhaps through pipeline 13 and 14, cold excessively-reverse stream pipe 12 and first liquid jet pump 15, it brings into play the effect of the driving stream of this first liquid jet pump.
At the bottom of the tower of high-pressure tower 2 liquid 16 cold excessively equally-carried out in the reverse stream pipe 12 cold; And process pipeline 17 flow to first liquid jet pump 15; This first liquid jet pump causes required pressure with it, with the height of the vaporization chamber of the overhead condenser 20 of the vaporization chamber of the overhead condenser 18 of the height that reaches lower pressure column or crude argon column 19 and pure argon column 21.The fraction medium position of ground connection through delivering to lower pressure column from the steam component 22 or the liquid components 23 of overhead condenser 18,20 during this time at the bottom of high-pressure tower-Ta.(as substituting shown in the figure, this first liquid jet pump 15 can directly be sent into liquid 17 at the bottom of a part of high-pressure tower-Ta in the lower pressure column 3; If there is not the device that obtains argon, what for to fraction at the bottom of all towers is all directly imported in the lower pressure column.)
To in nitrogen pump 25, cause high pressure from the liquid nitrogen 24 of the liquefied room of main condenser 4, and most of cold junction that flow to main heat exchanger through pipeline 26; Make perhaps (if this pressure is then overcritical) pseudo-evaporation of high pressure-nitrogen evaporation at this, be heated to environment temperature, and finally obtain (compression in so-called) as the high die pressing product of gaseous state.At this, pressure-air 5 is main as thermal source.The remainder 27 of institute's pumping is as the stream of the driving in second liquid jet pump 28, and this second liquid jet pump will be sent in the lower pressure column 3 from the liquid middle distillate 29,30 of high-pressure tower 2 according to the present invention.In this embodiment, the driving of second liquid jet pump stream 27 is under the pressure of 25 crust, and main flow is caused 6.5 crust by 5.5 crust.The mole that drives stream is about 1/3rd of main flow.The stream that will mix is then delivered to the cat head of lower pressure column.
The device that obtains argon is connected with pure argon column 21 with crude argon column 19 through pipeline 31,32, passes through pipeline 33 and is connected with the device 35 that is used to obtain krypton-xenon with 34.
Said equipment is discharged following product or residual gas:
● passed through the not purity nitrogen 36 of cold-reverse stream pipe 12 and main heat exchanger from the cat head of lower pressure column
● at the bottom of the tower of lower pressure column 2 near the top: liquid oxygen 38 and after flowing through main heat exchanger oxygen pump (not shown) through the gaseous oxygen 39 of interior compression
● the nitrogen that compresses in the warp from pipeline 26 (referring to top explanation)
● liquid nitrogen 40
● from the straight argon at the bottom of the tower of pure argon column 21 41; Wherein a part can be chosen wantonly through pipeline 42 and discharge, and presses as the nothing of gaseous state or discharge through the product of interior compression through main heat exchanger
● krypton-xenon concentrate (not shown).

Claims (4)

1. be used for the method for low temperature air separating (1,5) in the destilling tower system that is used for nitrogen-oxygen separation, this destilling tower system has high-pressure tower (2) and lower pressure column (3), wherein with first fluid (16,17; 29) discharge and importing (22,23 from high-pressure tower (2) with liquid state; 30) in the lower pressure column (3), it is characterized in that, use first liquid jet pump (15; 28) so that first fluid is delivered to the lower pressure column from high-pressure tower.
2. according to the method for claim 1, it is characterized in that, second fluid is discharged and imported the lower pressure column from high-pressure tower with liquid state, wherein use second liquid jet pump so that first fluid is delivered to the lower pressure column from high-pressure tower.
3. by being used for the equipment that destilling tower system that nitrogen-oxygen separates is used for low temperature air separating (1,5), this destilling tower system has high-pressure tower (2) and lower pressure column (3), and this equipment has and is used for first fluid (16,17; 29) discharge and with its importing (22,23 from high-pressure tower (2) with liquid form; 30) first transport in the lower pressure column (3) is characterized in that, said first transport has first liquid jet pump (15; 28).
4. according to the equipment of claim 3, this equipment has and is used for second fluid is discharged and with its second transport that imports lower pressure column, wherein said second transport has second liquid jet pump from high-pressure tower (2) with liquid form.
CN201110349126.6A 2010-11-09 2011-11-07 The method and apparatus of low temperature air separating Expired - Fee Related CN102564063B (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015127648A1 (en) * 2014-02-28 2015-09-03 Praxair Technology, Inc. Pressurized product stream delivery

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CN1080991A (en) * 1992-03-20 1994-01-19 林德股份公司 The method of low temperature air separating and air-separating plant
EP1055890A1 (en) * 1999-05-25 2000-11-29 L'air Liquide Société Anonyme pour l'étude et l'exploitation des procédés Georges Claude Cryogenic distillation system for air separation
CN1320798A (en) * 2000-03-29 2001-11-07 林德股份公司 Method and apparatus for low-temp. separation of air to produce compressed products
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