CN101619917A - Nitrogen liquefier retrofit for air separation plant - Google Patents

Nitrogen liquefier retrofit for air separation plant Download PDF

Info

Publication number
CN101619917A
CN101619917A CN200910151331A CN200910151331A CN101619917A CN 101619917 A CN101619917 A CN 101619917A CN 200910151331 A CN200910151331 A CN 200910151331A CN 200910151331 A CN200910151331 A CN 200910151331A CN 101619917 A CN101619917 A CN 101619917A
Authority
CN
China
Prior art keywords
stream
nitrogen
liquid
oxygen
rich
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN200910151331A
Other languages
Chinese (zh)
Inventor
D·R·帕斯尼克
T·A·斯科尔
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Praxair Technology Inc
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=CN101619917(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 CN101619917A publication Critical patent/CN101619917A/en
Pending legal-status Critical Current

Links

Images

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

Landscapes

  • 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

The present invention relates to the nitrogen liquefier retrofit for an air separation plant, in particular discloses a method for increasing liquid production and involving retrofitting an existing air separation plant with a nitrogen liquefier. The nitrogen liquefier liquefies a nitrogen-rich vapor stream withdrawn from the higher pressure column to return a nitrogen-rich liquid stream 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 in the lower pressure column. 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 as a result of the retrofit.

Description

The nitrogen liquefier of air-separating plant is transformed
Technical field
The present invention relates to method with the existing air-separating plant of nitrogen liquefier transformation, wherein, but with the lower pressure column high-pressure tower related with heat exchange relationship runnability ground in the nitrogen rich vapor that produces be liquefied and import again in the described high-pressure tower increasing the production of oxygen enriched liquid bottom backflow in the high-pressure tower and the lower pressure column, thereby can allow or promote the liquid oxygen product of air-separating plant and the liquid production of possible other liquid form products.
Background technology
Air can be separated into oxygen and nitrogen product in air-separating plant, wherein air low temperature rectifying is oxygen enriched product and rich nitrogen product, and also has the argon product.
In such device, air is compressed, and purifying is removed impurity such as carbon dioxide, carbon monoxide and the water vapour of higher, is cooled to the temperature of suitable air rectifying then in main heat exchanger.Chilled air imports high-pressure tower, wherein produces the more and more rising gas phase of enrichment of nitrogen.The condensation of the rich nitrogen overhead product of gained produces the more and more decline liquid phase of enrichment of oxygen.Liquid and gas contact by the mass transfer contact element, and described mass transfer contact element can be column plate or structuring filling, perhaps may be fillers at random.Under any circumstance, described contact produces the rough enrichment liquid bottoms product of oxygen enrichment in high-pressure tower.
Then rough enrichment liquid bottoms product steam is imported in the lower pressure column and be oxygen enrichment tower bottom product of in lower pressure column, collecting and the rich nitrogen overhead product that in lower pressure column, forms with further rectifying.But high-pressure tower is related with heat exchange relationship runnability ground by the condenser reboiler or the main condenser that are usually located at the lower pressure column substrate with lower pressure column.Described oxygen enriched liquid partly evaporates with the nitrogen rich vapor that is produced by the nitrogen rich vapor overhead product.With respect to the steam of oxygen enriched liquid and condensation produces nitrogen-rich liquid, this nitrogen-rich liquid is used for refluxing at high-pressure tower and lower pressure column nitrogen enriched vapor stream in condenser.The part of this nitrogen-rich liquid stream can be used as product.Can from high-pressure tower and lower pressure column, take out oxygen and nitrogen product and help cool off the air of introducing through main heat exchanger.
Thereby also can be by from lower pressure column, taking out stream with rich argon and this air-flow production argon product of rectifying in argon column.Rich argon product can be collected as overhead product and can take out and be identical air-flow.By some rich argon products are carried out the argon air tower backflow with flowed condensation by the crude liquid oxygen of taking out in the high-pressure tower.According to the separation tray number that exists in one or more argon column, the purity of argon can be to make most of oxygen separate from argon.Yet, thereby also further rectifying remove oxygen in this argon product and residual nitrogen is made the argon product.
In the art widely known to, refrigeration can be incorporated in the hypothermia distillation device to overcome the hot-side heat exchanger loss and to see through the heat that is used to hold such as the heat insulation layer of the ice chest of above-mentioned tower and reveal.Thereby can will in described main heat exchanger, carry out the portion of air of rectifying and in turbine expander, make its expansion introduce refrigeration by partly cooling off.From device, take out the acting of expanding, and gained imports the bottom of high-pressure tower through the air of cooling.In addition, can introduce refrigeration by the expander that links to each other with lower pressure column.The cooling degree that is incorporated in the air-separating plant will determine fertile fluid product amount, and described fluid product produces in the oxygen enriched liquid tower bottom product that is produced by lower pressure column usually, but also may be by producing in the nitrogen-rich liquid stream.
It is also known that to provide refrigeration to air-separating plant by the nitrogen cycle liquefier.The example of such liquefier can be at United States Patent (USP) 5,231, finds in 845.In this patent, add twin turbocharged compressor in the liquefier of description, thereby described compressor is through arranging Machine Design parameter and the effective cooling curve feature that provides favourable especially.From the middle pressure nitrogen of high-pressure tower, also from high-pressure tower and at its middle pressure nitrogen that heats fully in the heat-exchange system of air-separating plant, and the low pressure nitrogen product that obtains from lower pressure column all is fed in the nitrogen liquefier.Thereby the gained liquid nitrogen also can turn back to the high-pressure tower top and produce the subcooled liquid product so that refrigeration to be provided by air-separating plant.At United States Patent (USP) 4,883, in 518, from high-pressure tower, take out nitrogen and be divided into two strands of air-flows, the heat exchanger of one airflow passes nitrogen liquefier and another burst airflow passes main heat exchanger.Two strands of nitrogen conductances are gone into recycle compressor, thereby produce liquid nitrogen stream by twin turbocharged compressor preparation then, produce liquid nitrogen and liquid oxygen product thereby it is imported high-pressure tower again.
By seeing that the discussion of above two existing patents may be obvious that, owing to adopt the necessary high integration of disclosed liquefier in these inventions, thereby none particularly suitable is done the transformation of existing air-separating plant.Just as will be discussed, except that other advantages, the invention provides method with the existing air-separating plant of nitrogen liquefier transformation, thereby or enable or improve the taking-up liquid oxygen product, the perhaps ability of optional liquid nitrogen product, and raising argon production when this device is equipped with argon column.In addition, described liquefier carries out integrated in the mode that does not involve high integration in the prior art.
Summary of the invention
Thereby the production that the method that the invention provides the existing air-separating plant of transformation is produced at least a fluid product or improved at least a fluid product.
According to described method, air separates in existing air-separating plant.Existing air-separating plant has the high-pressure tower and the lower pressure column that can be associated mutually with heat exchange relationship at least with moving.Thereby existing air-separating plant is transformed by the nitrogen liquefier being connected to high-pressure tower.Described nitrogen liquefier does not have the parts of (or identical) with described existing air-separating plant.
The nitrogen liquefier links to each other with high-pressure tower and makes described nitrogen liquefier only receive the nitrogen enriched vapor stream from the high-pressure tower head portion.Described nitrogen enriched vapor stream liquefies in the nitrogen liquefier and flows to produce rich nitrogen liquid, and the described rich nitrogen liquid stream of at least a portion imports in the high-pressure tower.The backflow that this has increased high-pressure tower has increased the production of the crude liquid oxygen column bottoms that forms in the high-pressure tower, and has therefore increased the production of the oxygen enriched liquid that forms at the lower pressure column bottom section.
From air gas separation unit, take out at least a fluid product, and it comprises the stream of oxygen-enriched liquid that is made of oxygen enriched liquid.
Be preferably, in described nitrogen liquefier, the nitrogen vapor stream that comprises nitrogen enriched vapor stream is warm in heat exchanger, is expanded to the exhaust flowing pressure of turbine exhaust stream, and merges formation merging stream with turbine exhaust stream.Described merging is flowed in recycle compressor and is compressed, and after removing the heat of compression, splits into refrigeration stream and merge stream remainder (remaining part).Described refrigeration stream is compressed in booster compressor, and part cooling in heat exchanger imports in the turbine expander then to form turbine exhaust stream.Turbine exhaust stream is warm and merge with nitrogen enriched vapor stream in heat exchanger.Described merging stream remainder cools off in heat exchanger and is expanded to high-pressure tower pressure.Merge stream by at least a portion and form rich nitrogen liquid stream.
Be preferably, the turbine expander acting provides power for booster compressor.The expansion that merges the stream remainder forms two phase flow, and the liquid and gas of described two phase flow are separately to form vapor phase stream and liquid phase stream.Described vapor phase stream merged to form nitrogen vapor stream with nitrogen enriched vapor stream before delivery heat exchanger.Liquid nitrogen stream is made of liquid phase stream.
Can take out the liquid nitrogen product stream that constitutes by a part of richer nitrogen liquid stream.Described air gas separation unit also can be equipped with the argon air tower that links to each other with lower pressure column with the purifying stream with rich argon, and produces argon product stream therefrom.Take out the nitrogen-enriched stream of a part again with the speed that does not improve the oxygen concentration in the stream with rich argon.When not producing described a part of nitrogen-enriched stream again, thus production that can be by improving oxygen enriched liquid and remove stream of oxygen-enriched liquid and increase argon gas and reclaim.
Thereby the nitrogen liquefier can intermittently turn round and make at least a liquid form product stream can be stored in order to further using.
In addition, existing air-separating plant can be configured to, if transform, the mounting points that then is used for connecting the nitrogen liquefier is positioned at the high-pressure tower of existing air-separating plant.
Description of drawings
When specification with claims of spelling out the inventor and being considered as its subject matter of an invention when finishing, will be understood that connection with figures can understand the present invention better.Wherein
Fig. 1 is the exemplary process flow figure that realizes the existing air-separating plant of method of the present invention; And
Fig. 2 is the exemplary process flow figure of rich nitrogen liquefier that is used to transform and be connected to the high-pressure tower of the air-separating plant described in Fig. 1.
The specific embodiment
With reference to figure 1, existing air-separating plant has been described for exemplary purposes.As the discussion that will carry out, it comprises high-pressure tower and lower pressure column, and ultra-high purity oxygen column and argon column are to produce the liquid argon product.Yet this only is an illustrative purpose, and the present invention can be applicable to have separately the air-separating plant of high-pressure tower and lower pressure column, perhaps also comprises the air-separating plant of argon column.
Air stream 10 after filtering in filter element 12 compresses in main air compressor 14.Remove the heat of compression in aftercooler 16 after, air stream 10 carries out purifying in pre-purification unit 18.Pre-purification unit 18 contains absorbent bed usually, and described absorbent bed is removed high-boiling-point impurity such as carbon monoxide, carbon dioxide and water vapour with the operation of out-phase endless form with the described air stream of purifying.Usually, described circulation can be transformation sorption cycle or alternating temperature sorption cycle.
Gained air stream 20 compressed and purifying splits into first 22 and second portion 24 subsequently.First 22 is used for the refrigeration of described device.Exhaust stream 26 merges with first 22, and imports recycle compressor 28.Remove the heat of compression in aftercooler 30 after, the compressed airflow diversion of gained is the first son stream, the 32 and second son stream 34.The cooling fully in main heat exchanger 36 of the first son stream 32, the second son stream 34 imports in the turbocharger compressor 38.Remove the heat of compression in aftercooler 40 after, the compressed air-flow of gained cools off in main heat exchanger 36 and imports turbine 42, and the acting of wherein expanding can be used for driving turbocharger compressor 38.The expansion of carrying out in turbine 42 forms the exhaust stream 26 through cooling, thereby described exhaust stream 26 heating in main heat exchanger 36 makes air-separating plant 1 refrigeration.
Air-separating plant 1 is equipped with high-pressure tower 44, and it is related that the mode of described high-pressure tower 44 by condenser reboiler 48 can be moved ground with the relation of heat exchange and lower pressure column 46.In addition, air-separating plant 1 also is equipped with the mode separation of argon of low ratio tower 50 to be about to discuss that links to each other with superstage tower 52.In addition, be equipped with ultra-high purity oxygen column 54 to produce the ultra-high purity oxygen product that also is about to discussion.Contact closely thereby include the liquid and gas that mass transfer component such as structuring filling or column plate will import the mixture that wherein separates in described high-pressure tower 44, lower pressure column 46, low ratio tower 50, superstage tower 52 and the ultra high purity liquid oxygen column 54 separately, and this mixture of rectifying thus.
The second portion 24 of compressed air stream is cooling fully in main heat exchanger 36, and split into the first son stream 60 directly import high-pressure towers 44 and the second son stream 62 import be positioned over ultra-high purity oxygen column 54 bottoms reboiler 64 to form liquid stream 66.
The cooling fully in main heat exchanger 36 of the first son stream 32, and split into first 68 and second portion 70.First 68 directly imports lower pressure column 46, and second portion 70 merges formation merging stream 72 mutually with liquid stream 66 and imports high-pressure tower 44.Nitrogen rising gas phase less and less forms the nitrogen rich vapor overhead product in high-pressure tower 44 thereby the importing that merges stream 72 and first 60 begins to have formed.
Rich nitrogen overhead stream is as stream 74 condensations in condenser reboiler 48.First 76 returns high-pressure tower 44 as backflow, and second portion 78 is crossed cold in main heat exchanger 36 and is used for low pressure return tower 46.Part 80 can randomly be got and be made liquid nitrogen product, and remainder 82 can import lower pressure column 46 as refluxing subsequently.
In high-pressure tower 44, along with liquid phase descends, thereby oxygen more and more enrichment form crude liquid oxygen column bottoms.But flowed in 84 delivery heat exchangers 86 by the crude liquid oxygen that described crude liquid oxygen column bottoms constitutes, described heat exchanger 86 is used to form the backflow in the superstage argon gas knockout tower 52.Crude liquid oxygen stream 84 forms liquid phase stream 88 and vapor phase stream 89 thereby this part ground has gasified, and vapor phase stream 89 imports further rectifying in the lower pressure column 46.In addition, another crude liquid oxygen stream 87 can import lower pressure column 46.Although be not described, be known in the art, thereby crude liquid oxygen stream 84 and 87 before importing lower pressure column, it makes air-flow be in the suitable pressure that imports this tower the valve expansion.
Decline liquid phase in lower pressure column 46 forms the oxygen enriched liquid of device reboiler 48 gasifications that are condensed.The desirable liquid oxygen product stream 90 of doing of residual liquid.The desirable nitrogen vapor product stream 92 of doing of gained nitrogen rich vapor.Nitrogen vapor product stream 92 can have the concentration that is lower than about 2ppm.In addition, useless nitrogen stream 94 also can be removed.Useless nitrogen stream 94 can be used for regenerating and is arranged in the adsorbent of pre-purification unit 18.Nitrogen vapor product stream 92 and useless nitrogen stream at first in superheater, are heated in main heat exchanger 36 near the environment temperature of determining then.In addition, the gaseous oxygen product stream 96 that is made of the oxygen enriched liquid through gasification also can take out from lower pressure column 46, and described oxygen enriched liquid through gasification forms by the gasification of condenser reboiler 48 by the liquid phase that is positioned at lower pressure column 46 bottoms.Gaseous oxygen product stream 96 and liquid oxygen product stream 90 all can have the purity of about 99.5 volume %.
Can contain the argon gas that surpasses about 10 volume % and be less than containing argon stream 98 and can from lower pressure column 46, taking out of 1ppm nitrogen, and import and hang down ratio tower 50.This has formed rich argon column top product and oxygen enrichment tower bottom product among low ratio tower 50.The oxygen enrichment tower bottom product can be used as stream of oxygen-enriched liquid 100 and is back to lower pressure column 46.Rich argon column top product is desirable make stream with rich argon 102 and import superstage tower 52 be used for oxygen separate to the utmost point low-level, thereby form the oxygen enrichment tower bottom product, described oxygen enrichment tower bottom product can be used as oxygen-rich stream 106 and takes out, and flows 110 blowbacks to low ratio tower 50 by pump 108 as pump.The removal of oxygen forms rich argon column top product.But reflux 114 to form argon in stream with rich argon 112 delivery heat exchangers 86, argon exhaust stream 116 is used to prevent the accumulation of uncondensable nitrogen, and can take out liquid argon product stream 120 as liquid argon product stream from superstage argon column 52, it can contain the oxygen of the nitrogen that is less than about 1ppm and about 1ppm.
Substantially the oxygen liquid stream 122 that does not contain hydrocarbon and nitrogen can take out from low ratio argon column 50, thereby and as flowing 124 by not produced the ultra high purity liquid oxygen product by the residual liquid with about 99.99999% oxygen purity that reboiler 64 heavily boils in the charging importing ultra-high purity oxygen column 54.Gas overhead product in ultra-high purity oxygen column 54 can be used as air-flow 126 and is removed, and imports low ratio tower 50 again.
Air-separating plant 1 produces ultra high purity liquid oxygen product 124, liquid oxygen product 90 and possible liquid nitrogen product stream 80.The degree of liquid production depends on the total refrigeration that imports air-separating plant.Under the lower-speed state of air-separating plant, the aforesaid liquid product is to produce than low rate.In order to improve the production of fluid product,, liquefier 2 can be transformed in the air-separating plant 1 at the lower-speed state of air-separating plant with when running well.Liquefier 2 is described in Fig. 2.Nitrogen enriched vapor stream 130 imports in the liquefier, and described liquefier 2 is back to high-pressure tower 44 with nitrogen enriched vapor stream 130 liquefaction and with the rich nitrogen liquid stream 132 of gained.It should be noted that it only is that nitrogen enriched vapor stream 130 is removed, and rich nitrogen liquid stream 132 imports to again in the lower pressure column 44.
Liquid nitrogen imports as rich nitrogen liquid stream 132 and improved the liquid oxygen amount of collecting in crude liquid oxygen column bottoms, and has improved the oxygen amount that imports lower pressure column 46 thus.This has the effect that can allow liquid oxygen product stream 90 to take out with faster rate, thereby produces more oxygen enriched liquid.In addition, liquid nitrogen product stream 80 and ultra high purity liquid oxygen flow 124 also can take out with faster rate.
Accessible as those skilled in the art, liquid nitrogen product stream 80 should not take out with too fast speed, and this will influence the purity of stream with rich argon 98.Yet, import lower pressure column 46 and the liquid nitrogen that do not produce the recruitment of liquid nitrogen product stream 80 will improve the argon concentration in the stream with rich argon 98, and therefore improve the yield and the speed of the liquid argon product stream 120 of taking-up from superstage tower 52.Therefore, under a kind of operation mode, liquid nitrogen stream 80 is taken out with the speed of the argon concentration that do not influence stream with rich argon 98, thereby perhaps takes out with lower speed or even take out the argon concentration that improves stream with rich argon 98.Should be noted in the discussion above that also and may obtain liquid nitrogen product stream from the rich nitrogen liquid stream 132 of a part, discussion same as described above also can be applicable to the place to go of such stream as product.
Preferably, air-separating plant 1, and other air-separating plant available standards mounting points 128 and 129 of transforming with nitrogen liquefier of the present invention 2 make up, and described standard mounting points 128 and 129 allows described nitrogen liquefier 2 to be connected to such device simply.For example, mounting points 128 and 129 can be the tool capped pipe road or valve sealing or the tool cap that can be building up among the standard set-up design.Therefore the device production line can have such mounting points 128 and 129 through design.If in any such device on production line identical demand is arranged, this will make the transformation of nitrogen liquefier 2 carry out in fast and cost-effective mode.The liquid production of product improves with under the pattern that satisfies the demand that increases in case employing, air-separating plant 1 can be used for operating in wherein.Another mode, thus can allow to produce fluid product and lay in to improve oxygen production to adopt nitrogen liquefier 2 period of more low-cost acquisition electric power in order to using cost period in higher power with the speed that improves.In addition, thus can during the device lower-speed state, adopt the nitrogen liquefier produce fluid product during this period.Another pattern of running is to adopt nitrogen liquefier 2 and link to each other without being designed for the device of producing liquid form product, and such device is transformed to produce liquid form product.
With reference to figure 2, the nitrogen liquefier of transforming on the air-separating plant 12 has been described.In nitrogen liquefier 2, nitrogen enriched vapor stream 130 merges mutually with the vapor phase stream 134 of the pressure that is expanded to nitrogen enriched vapor stream 130 in expansion valve 136, and forms nitrogen stream 138.Nitrogen stream 138 heating in heat exchanger 140 also reduces pressure subsequently in expansion valve 142.After pressure reduced, nitrogen stream 138 merged with exhaust stream 144, thus described exhaust stream 144 by in heat exchanger 140 fully heating make the liquefier refrigeration.This has produced the merging stream 146 that compresses in recycle compressor 148.Utilizing after aftercooler 150 removes the heat of compression, first 152 imports and forms compressive flow 156 in the booster compressors 154.Remove the heat of compression in aftercooler 157 after, compressive flow 156 is partly cooling in heat exchanger 140, and the mode by expansion valve 158 reduces pressure, and imports turbine 160 subsequently to produce exhaust stream 144.The expansion acting that is provided by turbine 160 can be used for the compression in the booster compressor 154.In compressor 148, carry out other parts 162 cooling fully in heat exchanger 140 of the merging stream 146 that ship cake cools off in aftercooler 150, and the mode by expansion valve 164 is expanded to two-phase fluid subsequently, and described two-phase fluid imports phase separator 166.Thereby gas phase and liquid phase separation form nitrogen vapor phase stream 134 in phase separator.Mode by expansion valve 170 reduces the pressure of the pressure of liquid phase stream 168 to high-pressure tower 44, and leads as rich nitrogen liquid stream 132 and to be back to high-pressure tower 44.
Accessible is also to adopt the design of other nitrogen liquefiers 2 according to the present invention.For example, can use very simple nitrogen liquefier, wherein nitrogen enriched vapor stream 130 is compressed alone, expands and liquefy in very energy-conservation mode.Yet, it is believed that nitrogen liquefier 2 is very favorable design on its simplification, and between the simplification of retrofit applications and high efficiency, average out.
Although invention has been described with reference to preferred implementation, will run into as those skilled in the art, do not deviate from appended claims in can carry out a large amount of variations, increase and delete under the situation of the spirit and scope of the present invention set forth.

Claims (8)

1. transform existing air-separating plant to produce at least a fluid product or to improve the method that at least a fluid product is produced for one kind, described method comprises:
Separation of air in the existing air-separating plant that has the high-pressure tower that can be associated mutually and lower pressure column at least with heat exchange relationship with turning round;
Thereby existing air-separating plant is transformed the parts that described nitrogen liquefier is not total with described existing air-separating plant by the nitrogen liquefier being connected to high-pressure tower;
Described nitrogen liquefier links to each other with high-pressure tower and makes described nitrogen liquefier only receive the nitrogen enriched vapor stream from the high-pressure tower head portion, described nitrogen enriched vapor stream liquefies in the nitrogen liquefier to produce rich nitrogen liquid stream, and the described rich nitrogen liquid stream of at least a portion imports in the high-pressure tower, thereby increased the liquid nitrogen reflux of high-pressure tower, increase the production of the crude liquid oxygen column bottoms that forms in the high-pressure tower, and therefore increased the production of the oxygen enriched liquid that forms at the lower pressure column bottom section; With
Take out at least a fluid product from air gas separation unit, described at least a fluid product comprises the stream of oxygen-enriched liquid that is made of oxygen enriched liquid.
2. the method for claim 1, wherein in described nitrogen liquefier:
The nitrogen vapor stream that comprises nitrogen enriched vapor stream is warm in heat exchanger, is expanded to the exhaust flowing pressure of turbine exhaust stream, and merges formation merging stream with turbine exhaust stream;
Described merging is flowed in recycle compressor and is compressed, and after removing the heat of compression, splits into refrigeration stream and merge the stream remainder;
Described refrigeration stream is compressed in booster compressor, and part cooling in heat exchanger imports in the turbine expander then to form turbine exhaust stream;
Turbine exhaust stream is warm and merge with nitrogen enriched vapor stream in heat exchanger;
Described merging stream remainder cools off in heat exchanger and is expanded to high-pressure tower pressure; With
Merge stream by at least a portion and form rich nitrogen liquid stream.
3. method as claimed in claim 2, wherein:
The turbine expander acting provides power for booster compressor;
The expansion that merges the stream remainder forms two phase flow;
The liquid and gas of described two phase flow are separately to form vapor phase stream and liquid phase stream;
Described vapor phase stream merged to form nitrogen vapor stream with nitrogen enriched vapor stream before delivery heat exchanger; With
Liquid nitrogen stream is made of liquid phase stream.
4. the method for claim 1 is wherein taken out the liquid nitrogen product stream that the rich nitrogen liquid stream by another part constitutes.
5. method as claimed in claim 4, wherein:
Described air gas separation unit also has the argon column that links to each other with lower pressure column and also forms argon product stream thus with the purifying stream with rich argon; With
The described nitrogen-enriched stream of a part again is removed with the speed that does not increase the oxygen concentration in the described stream with rich argon.
6. the method for claim 1, wherein:
Described air gas separation unit also has the argon column that links to each other with lower pressure column and also forms argon product stream thus with the purifying stream with rich argon;
Improved the argon recovery by the increase of oxygen-rich stream production and the removal of stream of oxygen-enriched liquid.
7. the method for claim 1 is used in order to later thereby wherein said liquefier intermitten service can store at least a liquid product flow.
8. the method for claim 1, wherein existing air-separating plant be configured make mounting points be arranged in existing air-separating plant high-pressure tower to connect the nitrogen liquefier.
CN200910151331A 2008-06-30 2009-06-30 Nitrogen liquefier retrofit for air separation plant Pending CN101619917A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US12/164269 2008-06-30
US12/164,269 US20090320520A1 (en) 2008-06-30 2008-06-30 Nitrogen liquefier retrofit for an air separation plant

Publications (1)

Publication Number Publication Date
CN101619917A true CN101619917A (en) 2010-01-06

Family

ID=41445836

Family Applications (1)

Application Number Title Priority Date Filing Date
CN200910151331A Pending CN101619917A (en) 2008-06-30 2009-06-30 Nitrogen liquefier retrofit for air separation plant

Country Status (9)

Country Link
US (1) US20090320520A1 (en)
EP (1) EP2307835B1 (en)
KR (1) KR20110026435A (en)
CN (1) CN101619917A (en)
AT (1) ATE548620T1 (en)
BR (1) BRPI0914327A2 (en)
ES (1) ES2383781T3 (en)
MX (1) MX2010013697A (en)
WO (1) WO2010002500A2 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102620520A (en) * 2012-04-09 2012-08-01 开封黄河空分集团有限公司 Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation
CN103375968A (en) * 2012-04-27 2013-10-30 林德股份公司 Piping module for air fractionation plant
TWI832872B (en) * 2019-04-08 2024-02-21 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 Cryogenic air separation device

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010056560A1 (en) * 2010-08-13 2012-02-16 Linde Aktiengesellschaft Method for recovering compressed oxygen and compressed nitrogen by low temperature degradation of air in e.g. classical lime dual column system, for nitrogen-oxygen separation, involves driving circuit compressor by external energy
EP2980514A1 (en) * 2014-07-31 2016-02-03 Linde Aktiengesellschaft Method for the low-temperature decomposition of air and air separation plant
US10314249B2 (en) * 2014-12-10 2019-06-11 The Boeing Company Systems and methods of inducing rainfall
CN110869687B (en) 2017-05-16 2021-11-09 特伦斯·J·埃伯特 Apparatus and process for liquefied gas
CN112781321B (en) * 2020-12-31 2022-07-12 乔治洛德方法研究和开发液化空气有限公司 Air separation device with nitrogen liquefier and method
WO2023083488A1 (en) * 2021-11-10 2023-05-19 Linde Gmbh Method and arrangement for producing an argon product and an oxygen product, and method for retrofitting one or more air fractionation plants
US11959701B2 (en) * 2022-07-28 2024-04-16 Praxair Technology, Inc. Air separation unit and method for production of high purity nitrogen product using a distillation column system with an intermediate pressure kettle column

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS62194176A (en) * 1986-02-19 1987-08-26 株式会社日立製作所 Method of supplying nitrogen liquefier with nitrogen gas
US4894076A (en) * 1989-01-17 1990-01-16 Air Products And Chemicals, Inc. Recycle liquefier process
JPH0328681A (en) * 1989-06-27 1991-02-06 Kobe Steel Ltd Air separator
US5582033A (en) * 1996-03-21 1996-12-10 Praxair Technology, Inc. Cryogenic rectification system for producing nitrogen having a low argon content
CN1163386A (en) * 1995-12-18 1997-10-29 波克股份有限公司 Process and device for producing nitrogen
CN1191600A (en) * 1995-07-21 1998-08-26 林德股份公司 Method and device for production of variable amounts of pressurized gaseous product
US6779361B1 (en) * 2003-09-25 2004-08-24 Praxair Technology, Inc. Cryogenic air separation system with enhanced liquid capacity
CN101097112A (en) * 2006-06-30 2008-01-02 气体产品与化学公司 System to increase capacity of lng-based liquefier in air separation process

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4433990A (en) * 1981-12-08 1984-02-28 Union Carbide Corporation Process to recover argon from oxygen-only air separation plant
US4778497A (en) * 1987-06-02 1988-10-18 Union Carbide Corporation Process to produce liquid cryogen
DE3738559A1 (en) * 1987-11-13 1989-05-24 Linde Ag METHOD FOR AIR DISASSEMBLY BY DEEP TEMPERATURE RECTIFICATION
US5345773A (en) * 1992-01-14 1994-09-13 Teisan Kabushiki Kaisha Method and apparatus for the production of ultra-high purity nitrogen
US5231835A (en) * 1992-06-05 1993-08-03 Praxair Technology, Inc. Liquefier process
US5730003A (en) * 1997-03-26 1998-03-24 Praxair Technology, Inc. Cryogenic hybrid system for producing high purity argon
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion
GB9711258D0 (en) * 1997-05-30 1997-07-30 Boc Group Plc Air separation
US5799505A (en) * 1997-07-28 1998-09-01 Praxair Technology, Inc. System for producing cryogenic liquefied industrial gas
US6543253B1 (en) * 2002-05-24 2003-04-08 Praxair Technology, Inc. Method for providing refrigeration to a cryogenic rectification plant
US7090816B2 (en) * 2003-07-17 2006-08-15 Kellogg Brown & Root Llc Low-delta P purifier for nitrogen, methane, and argon removal from syngas
US9714789B2 (en) * 2008-09-10 2017-07-25 Praxair Technology, Inc. Air separation refrigeration supply method

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS62194176A (en) * 1986-02-19 1987-08-26 株式会社日立製作所 Method of supplying nitrogen liquefier with nitrogen gas
US4894076A (en) * 1989-01-17 1990-01-16 Air Products And Chemicals, Inc. Recycle liquefier process
JPH0328681A (en) * 1989-06-27 1991-02-06 Kobe Steel Ltd Air separator
CN1191600A (en) * 1995-07-21 1998-08-26 林德股份公司 Method and device for production of variable amounts of pressurized gaseous product
CN1163386A (en) * 1995-12-18 1997-10-29 波克股份有限公司 Process and device for producing nitrogen
US5582033A (en) * 1996-03-21 1996-12-10 Praxair Technology, Inc. Cryogenic rectification system for producing nitrogen having a low argon content
US6779361B1 (en) * 2003-09-25 2004-08-24 Praxair Technology, Inc. Cryogenic air separation system with enhanced liquid capacity
CN101097112A (en) * 2006-06-30 2008-01-02 气体产品与化学公司 System to increase capacity of lng-based liquefier in air separation process

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102620520A (en) * 2012-04-09 2012-08-01 开封黄河空分集团有限公司 Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation
CN102620520B (en) * 2012-04-09 2014-09-17 开封黄河空分集团有限公司 Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation
CN103375968A (en) * 2012-04-27 2013-10-30 林德股份公司 Piping module for air fractionation plant
CN103375968B (en) * 2012-04-27 2017-04-12 林德股份公司 Piping module for air fractionation plant
TWI832872B (en) * 2019-04-08 2024-02-21 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 Cryogenic air separation device

Also Published As

Publication number Publication date
EP2307835B1 (en) 2012-03-07
US20090320520A1 (en) 2009-12-31
ES2383781T3 (en) 2012-06-26
WO2010002500A3 (en) 2010-09-30
EP2307835A2 (en) 2011-04-13
WO2010002500A2 (en) 2010-01-07
MX2010013697A (en) 2010-12-21
ATE548620T1 (en) 2012-03-15
KR20110026435A (en) 2011-03-15
BRPI0914327A2 (en) 2015-10-13

Similar Documents

Publication Publication Date Title
CN101619917A (en) Nitrogen liquefier retrofit for air separation plant
CN101479550B (en) Cryognic air separation system
US20160025408A1 (en) Air separation method and apparatus
CN101266095A (en) Air separation method
JP4057668B2 (en) Method and apparatus for producing nitrogen by separating air components
CN1057380C (en) Cryogenic air separation system with dual temperature feed turboexpansion
CN101925790A (en) Method and device for low-temperature air separation
CN204115392U (en) With the full air separation units producing liquids of air supply compressor
CN103827612A (en) Air separation method and apparatus
CN102155841A (en) Cryogenic separation method and apparatus
JPH05157448A (en) Cryogenic method separating supply air flow into component
CN102047057A (en) Method and apparatus for separating air
CN104755360A (en) Method and apparatus for air separation by cryogenic distillation
CN102192637B (en) Air separation method and apparatus
CN103292576A (en) Process and apparatus for the separation of air by cryogenic distillation
CN101509722A (en) Distillation method and apparatus
CN104185767B (en) For the method and apparatus producing two strands of partial air flow purified
JP2007147113A (en) Nitrogen manufacturing method and device
CN104685310A (en) Air separation method and apparatus
TW202108222A (en) Method and system for low-temperature air separation
CN109883139B (en) Efficient argon extraction process based on oxygen-enriched air separation
CN1038514A (en) Produce the air separating technological of hyperbaric oxygen and elevated pressure nitrogen
CN2898737Y (en) Liquefier containing coal-seam gas
CN104364597B (en) Air separating method and equipment
CN103038589A (en) Krypton xenon recovery from pipeline oxygen

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C02 Deemed withdrawal of patent application after publication (patent law 2001)
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20100106