MX2010013697A - Nitrogen liquefier retrofit for an air separation plant. - Google Patents

Nitrogen liquefier retrofit for an air separation plant.

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Publication number
MX2010013697A
MX2010013697A MX2010013697A MX2010013697A MX2010013697A MX 2010013697 A MX2010013697 A MX 2010013697A MX 2010013697 A MX2010013697 A MX 2010013697A MX 2010013697 A MX2010013697 A MX 2010013697A MX 2010013697 A MX2010013697 A MX 2010013697A
Authority
MX
Mexico
Prior art keywords
nitrogen
liquid
stream
rich
current
Prior art date
Application number
MX2010013697A
Other languages
Spanish (es)
Inventor
David Ross Parsnick
Todd Alan Skare
Original Assignee
Praxair Technology Inc
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=41445836&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=MX2010013697(A) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Praxair Technology Inc filed Critical Praxair Technology Inc
Publication of MX2010013697A publication Critical patent/MX2010013697A/en

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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
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
    • F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
    • 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.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work 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
    • F25J3/04654—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
    • F25J3/04703—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 being arranged in more than one vessel
    • 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
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F25J3/04715—The auxiliary column system simultaneously produces 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
    • 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
    • F25J3/04763—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
    • F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
    • 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
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • 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
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods

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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)
  • Motor Or Generator Cooling System (AREA)
  • Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)

Abstract

A method is disclosed for increasing liquid production involving retrofitting an existing air separation plant with a nitrogen liquefier. The nitrogen liquefier liquefies a nitrogen-rich vapor stream (130) withdrawn from the higher pressure column (44) to return a nitrogen-rich liquid stream (132) to the higher pressure column. This increases liquid nitrogen reflux to the higher pressure column to in turn increase the production of liquid oxygen containing column bottoms of the higher pressure column and therefore, the production of oxygen-rich liquid (96) in the lower pressure column (46). The increased production of the oxygen-rich liquid allows a liquid oxygen product to be taken at an increased rate or for the liquid oxygen product to be taken in the first instance, if the plant is not designed to produce such a product. Also liquid nitrogen and argon products can be produced at an increased rate as a result of the retrofit.

Description

ADAPTATION OF NITROGEN LIQUEUR FOR AIR SEPARATION PLANT mpo of the invention The present invention relates to an existing air-to-air separation method with a lichen, where the high-pressure, nitrogen-rich steam associated with a lower pressure operating pressure in a transfer ratio is liquefied and introduced. again in the upper column to increase the reflux in the upper column and the production of oxygen rich bottom products of a pressure column in such a way as to allow or increase the production of liquid oxygen products and possibly of other uids from air separation plants, Background of the Invention main heat exchanger at a temperature with air rectification. The air after it is cooled is introduced to an upper pressure column, producing an ascending vapor phase that becomes or in nitrogen. The overhead product of the resulting tromer column is condensed to produce an insoluble packing that becomes even richer in liquid and vapor oxides and is contacted by the mass transfer contact which may be structured packing or possibly, In any case, the contact produces products rich in crude oil in the pressure column above oxygen.
A stream of the bottom products of crude rich liquid is then introduced to the pressure and will be further refined in oxygen-rich liquid column products that are collected. trógeno produced from the nitrogen-rich steam head product. The trógeno vapor stream is condensed in the condenser against the oxygen rich liquid vap to produce a stream of nitrogen that is used in the reflux of the upper col l ion and the lower pressure column. Current of liquid rich in nitrogen can be oduced. The oxygen and nitrogen products are imitated from the upper and lower pressure columns before the main heat exchanger to assist incoming air.
An argon product can also be produced in an argon-rich stream of the pressure column by etching such a stream into an argon column. The argon o is collected as a head-to-stream product from it can be extracted. The column reflows condensing part of the rich product As is well known in the art, the cooling and heat exchanger heat losses through the insulation of an a which is used to contain the column such as the above, are to be imparted to the cryogenic rectification plant. . This cooling can be imparted to the part of the air that will be rectified by the main heat exchanger and expanding the expander. The expansion work is extracted from the resulting chilled p re entering the lower part of the upper pressure. In addition, the refrigeration split by an expander connected to the ferior column. The degree to which cooling is imparted to the air stop will determine the amount of products that can be produced, commonly from the oxygen rich liquid column products produced in the lower pressure, but also possibly from the s effective cooling curve characteristics. The average pressure of the upper pressure column, the middle pressure trógeno, also of the upper column and after the heat exchange system of the separating plant has been completely heated, and the pressure nitrogen product low low pressure lumina, all are fed to the licógeno. The resulting liquid nitrogen can be top-loaded from the top pressure column or provide cooling to produce the benzened products from the air separation plant. In US No. 4,883,518, the nitrogen vapor is the upper pressure column and is divided in two c current through the nitrogen liquefier exchangers and the other current passes through main heat exchangers. The two ran for nitrogen are introduced in a compressor of r wanted to use the described blenders tentes. As will be discussed, the present invention, in nays, provides a method for adapting an existing air pattern with a nitrous liquor and increases the ability to remove a liquid product and optionally, a nitrogen product to liquidate the production of liquid. argon when such a plant is argon column. On the other hand, the liquidator does not imply the high degree of prior integration. evé Description of the Invention The present invention provides an existing air separation plant method for preventing the production of at least one liquid product.
According to the method, air is separated from existing air separation. The existing air plant has at least pressure columns a nitrogen-rich vapor stream of one portion the top pressure column. The vapidogen stream is liquefied in the nitrogen liquefier for a nitrogen-rich liquid stream and at least one stream of nitrogen-rich liquid is introduced at a higher pressure. This increases the reflux of the liquid in the upper pressure column, the crude column production of the crude oxygen column forms a higher pressure column and, therefore, a liquid formed in a lower region of the lower column.
At least one liquid product is removed from the air portion and comprises a liquid stream composed of an oxygen-rich liquid.
Preferably, within the nitrogen nitrogen stream liquefier, which comprises the nitrogen rich cor, it is heated within an interc heat exchanger and after rboexpansor is introduced to generate the extraction current d turbine extraction current is heated d heat exchanger and combined with the current a in nitrogen. The remaining part of the cold com flow inside the heat exchanger and expansion of the upper pressure column. The stream of nitrogen is formed at least partially combined.
Preferably, the expansion work of the turbocharger compresses the accelerator. The stant expansion of the combined current produces a current of the liquid and vapor phases of the biphasic current to form a vapor phase current and a liquid stream. The vapor phase current is combined with a steam stream rich in nitrogen to form the cor tor of nitrogen before its introduction to the exchange.
The nitrogen-rich current is removed from the stream which does not increase the concentration of argon-rich oxygen. Where the addition part rich in nitrogen is not produced, the recovery can be increased by increasing the oxygen production and the elimination of the liquid current.
The nitrogen liquefier can be operated intermittently so that at least one stream of product can be stored for future use.
In addition, the existing air separation plant should be such that the existing junction points of the upper pressure window of the separating plant for connection to the nitrogen liquefier, if the same as those that will adapt. reve Description of Drawings Although the specification concludes with the claims a nitrogen-rich liquefier to be adapted and c the upper pressure column of the separating plant illustrated in Figure 1.
Detailed Description of the Invention With reference to Figure 1 an existing air plant 1 is illustrated for exemplary purposes discussed above, includes a column of pressure higher than oxygen column of very high purity and columns to produce liquid argon as a product. However, for exemplary purposes only, and the present applicability in an air separation plant is either an upper pressure column and a lower column or one which also includes a vertical column.
An air stream 10 after the filtering filtering 12 is compressed in an incipient compress 14. After the compression heat s a rear cooler 16, the air stream 10 s The stream of compressed and purified air 20 ntonces is divided into a first portion 22 and an orifice 24. The first portion 22 is used in the effrigeration gene for the plant. An extraccombined stream with the first portion 22 and recycle compressor 28 is introduced. After the elimination gives compression in a subsequent cooler 30, the resulting compression is divided into a first branch 32 and a second subsidiary stream 34. subsidiary orifice 32 The main heat exchanger 36 is cooled completely and the second container 34 is introduced into an accelerator compressor 8. After the heat removal from the compressor the rear cooler 40, the compressed stream resides inside the main heat exchanger turbine 42 where the work of the e can use to drive the accel compressor . In addition, the air separation plant 1 ta cooperates with a low-ratio column 50 associated with additional stage 52 to separate the argon that will be discussed. In addition, a very high oxygen column 54 is provided to produce a very high purity progenitor which is also discussed. CAD upper pressure column 44, pressure column, low ratio column 50, additional stage column liquid oxygen column of very high purity 54 mass transfer elements such as structures or trays to contain the phases of the mixtures which are introduced into the others in intimate contact and thus rectifi ezclas.
The second portion 24 of the cold compress air stream completely inside the heat exchanger and is divided into a first subsidiary stream 6. directly in the lower pressure column 70 is combined with the liquid stream to combine a combined stream 72 which is introduced in upper pressure 44. The introduction of the unit 72 together with the first portion 60 initiates the f a vapor phase rising within an upper coil 44 which becomes even purer in ra producing the vapetrogenic column head product.
A stream of the overhead polymer product as stream 74 is condensed into condenser heater 48. A first portion 76 is not a reflux stream to a pressure column and a second portion 78 is subcooled from a main heat exchanger 36 and is used. for flow the lower pressure column 46. A portion 80 sea optionally as a nitrogen product. refluxing for the additional stripping column 52. This partially vaporizes the crude liquid stream 84 to produce a liquid stream 88 and a vapor phase stream 89 which is the lower pressure column 46 for refl icing. , another liquid oxygen stream is to be introduced into the lower pressure column 46. A illustrate, but as known in the art, the crude liquid currents 84 and 87 will expand by valve introduction in the lower pressure column to modrients are at a pressure suitable for the intro l column.
The descending liquid phase within the lower colloid 46 produces a liquid rich in oxygen porized by the condenser reheater 48. The same can be taken as a product stream of the 90-fluid product. ) and then in the 36 incipal exchanger at close ambient temperatures. In addition to gaseous oxygen product 96 it can be mined from the lower pressure column 46 which is rich in vaporized oxygen which is produced by the liquid phase in the lower part of the lower pressure 46 by the condensed reheater of the product. of oxygen gas 96 and the liquid oxygen carrier 90 may have approximately 99.5 volume percent.
A vapor stream containing argon 98 containing more than about 10 percent volatil and less than 1 ppm nitrogen can be removed from lower pressure 46 and introduced into the low 50 mixture. This creates a head product of a in argon and a rich column bottom product in the middle of the low 50 column. The product of mbea by a pump 108 again to the laction column 50 as a pumped stream 110. The elimination: Inegen produces a gon column head product. A stream rich in argon 112 can be introduced heat exchanger 86 to produce an argon stream 114, an argon discharge stream 116 to prevent the accumulation of non-condensing nitrogen from liquid argon product 120 can be elongated argon column. additional step 52 as a liquid argon tube which may contain approximately 1 ppm nitrogen and approximately oxygen.
A stream of liquid oxygen 122 which is free hydrocarbon and nitrogen can be removed from the low-ratio argon 50 and introduced into the very high purity collagen 54 as a feed for the purity liquid oxygen product stream. uid 90 and potentially a product stream: liquid rust 80. The degree to which the discharge is produced, the total cooling that is imparted to the air gap 1. During the decrease of the air separation plant 1 the rear products are produced at a lower speed. For the production of the liquid products, during the reduced conditions and during the normal operation of the air stop 1, a liquefier 2 can be adapted in air separation 1. The liquefier 2 is illustrated in the steam stream rich in Nitrogen 130 is introduced 2 which liquefies the nitrogen-rich steam stream and the nitrogen-rich liquid stream 132 rifts to the upper pressure column 44. servar which is only the vapor stream rich in 0 which is removed and the liquid stream rich in 2 is the one that is introduced again in the column d or in oxygen. In addition, the product stream of jude 80 and the liquid oxygen stream of purity? 4 can also be removed at a higher speed.
As it can be seen by the experts in the liquid nitrogen product, it is not due to the excessive speed that would affect the purity of the a in argon 98. However, the increasing amount of liquid that is introduced to the pressure column If there is no production of nitrogen product stream, it will increase the argon concentration inside the a in argon 98 and thereby increase the recovery at which the product stream of argon 0 can be removed from the additional stage column. , in one mode of operation, the nitroge stream is removed at a rate that does not affect the concentration of the argon-rich current 98 or alternative to eliminate at a lower velocity or not be eliminated at Nitrogen converter 2 according to the present invention to build with the standard junction points 128 and empty the simple connection of the nitrogen liquifier anta. For example, junction points 128 and 129 covered pockets or closed and capped valves that are attached to a standard plant design. An oducts of plants could be designed in such a way as to design junctions 128 and 129. This would allow the nitrogen modifier 2 to be realized in an efficient manner if the same will be desired in any plant of production. Once used, the plant of separe 1 could be used to operate in a mode in oduction of liquid products will increase for increasing c manda. Alternatively, the nit liquefier could be used to increase the production of oxygen during periods in which electric current could become cheaper to allow With reference to Figure 2, the liquifier is illustrated that the nitrogen liquefier 2 will be adapted to discharge the separation plant., the vaporous vapor stream 130 combined with a ve-phase stream is expanded in an expansion valve 136 to the nitrogen-rich vapor pressure 130 and combined to form a nitrogen stream 138. The 138-stream is heated inside a heat exchanger then its pressure is reduced within a valve of 2. After the pressure reduction, the current of 8 is combined with an extraction current 144 which is cooled to the liqueur by fully heating the heat exchanger 140. This produces a current c 6 which is compressed within a recycle compressor after the heat removal of the rear fryer compression 150, a first portion 152 is introduced throttle compressor 154 to produce a co-current Tiprimide in the compressor 148 and then cooled by the rear fryer 150, the heat exchanger 140 is completely cooled and then expanded by the expansion valve 164 in a two-phase fluid that is a phase separator 166. The vapor phase is separated d from the phase separator 166 to produce nitrogen vapor stream 134. A liquid phase stream under pressure by means of an expansion valve of the upper pressure column 44 and a stream of nitrogen-rich liquid 132 is introduced. the lower pressure column 44.
As can be appreciated, other designs for ligorgen 2 could be used according to the expiration. For example, a nitrogen liquefier could be used where the nitro-rich vapor stream was compressed, expanded and liquefied by much higher energy. However, it was believed

Claims (8)

1. A method for adapting an existing separation plant to produce or increase production in a liquid product, comprising: separating the air within the separation plant stente having at least lower pressure columns operatively associated with each other in a heat transfer; adapting the nitrogen air separation plant to a pressure column its nitrogen carrier has no component in the existing components of the separation plant of the nitrogen liquefier that is connected to the top co-ion such that the liquefier of nitrogen receives a stream of nitrogen-rich vapor from a portion the column of higher pressure, the current of vap i the lower pressure column; Y withdrawing at least one liquid product from the air supply, at least one product liq > It shows a liquid stream rich in oxygen, liquid rich in oxygen.
2. The method of claim 1, wherein, nitrogen donor: a nitrogen vapor stream comprising nitrogen-rich vapor is heated to the heat exchanger, expanded to extract the fuel from a turbine exhaust stream, and the turbine extraction stream for combined product; the combined current is compressed in a cycling and after the removal of the heat of the co-divided in a stream of refrigerant fluid and current of the combined current; I heat exchanger and expands to the upper pressure pressure; Y the liquid stream rich in nitrogen forms part of the combined current.
3. The method of claim 2, wherein: the expansion work of the turboexpansor ac accelerator compressor; the expansion of the remaining part of the current produces a two-phase current; the liquid and vapor phases of the bif current stop to form a liquid phase current vapor phase current; the vapor phase current is combined with the cor for nitrogen rich to form the rheogen stream before its introduction into the exchanger the stream of liquid nitrogen consists of the
? Argon product; Y
The other part of the nitrogen-rich stream has a retivity that does not increase the oxygen concentration of the argon-rich current.
6. The method of claim 1, wherein: the air separation unit also has an argon connected to the lower pressure column for argon-rich current and thereby produce an argon product; The recovery of argon is increased by the supply of oxygen-rich liquid and the elimination of oxygen-rich liquid.
7. The method of claim 1, wherein the operation intermittently so that, in the case of liquid product, future ilization can be stored.
8. The method of claim 1, wherein the
MX2010013697A 2008-06-30 2009-05-12 Nitrogen liquefier retrofit for an air separation plant. MX2010013697A (en)

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ATE548620T1 (en) 2012-03-15

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