US20090320520A1 - Nitrogen liquefier retrofit for an air separation plant - Google Patents

Nitrogen liquefier retrofit for an air separation plant Download PDF

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Publication number
US20090320520A1
US20090320520A1 US12/164,269 US16426908A US2009320520A1 US 20090320520 A1 US20090320520 A1 US 20090320520A1 US 16426908 A US16426908 A US 16426908A US 2009320520 A1 US2009320520 A1 US 2009320520A1
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Prior art keywords
stream
nitrogen
liquid
rich
pressure column
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US12/164,269
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English (en)
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David Ross Parsnick
Todd Alan Skare
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Praxair Technology Inc
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Praxair Technology Inc
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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=US20090320520(A1) "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
Priority to US12/164,269 priority Critical patent/US20090320520A1/en
Assigned to PRAXAIR TECHNOLOGY, INC. reassignment PRAXAIR TECHNOLOGY, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: PARSNICK, DAVID ROSS, SKARE, TODD ALAN
Priority to AT09773952T priority patent/ATE548620T1/de
Priority to MX2010013697A priority patent/MX2010013697A/es
Priority to BRPI0914327A priority patent/BRPI0914327A2/pt
Priority to KR1020107029373A priority patent/KR20110026435A/ko
Priority to PCT/US2009/043558 priority patent/WO2010002500A2/en
Priority to EP09773952A priority patent/EP2307835B1/en
Priority to ES09773952T priority patent/ES2383781T3/es
Priority to CN200910151331A priority patent/CN101619917A/zh
Publication of US20090320520A1 publication Critical patent/US20090320520A1/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—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"
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    • 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
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    • 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
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    • 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
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    • 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
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    • 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
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    • 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
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    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
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    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods

Definitions

  • the present invention relates to a method of retrofitting an existing air separation plant with a nitrogen liquefier in which nitrogen-rich vapor produced in a higher pressure column operatively associated with a lower pressure column in a heat transfer relationship is liquefied and reintroduced into the higher pressure column to increase reflux in the higher pressure column and the production of an oxygen-rich liquid column bottoms of the lower pressure column, thereby to allow or to increase liquid production of liquid oxygen products and possibly other liquid products of air separation plants.
  • Air can be separated into oxygen and nitrogen products within an air separation plant in which the air is cryogenically rectified into oxygen and nitrogen-rich products and also possibly an argon product.
  • the air is compressed, purified of higher boiling impurities such as carbon dioxide, carbon monoxide and water vapor and then cooled in a main heat exchanger to a temperature suitable for the rectification of air.
  • the air after having been cooled is introduced into a higher pressure column in which an ascending vapor phase is produced that becomes evermore rich in nitrogen.
  • the resulting nitrogen-rich column overhead is condensed to produce a descending liquid phase that becomes evermore rich in oxygen.
  • the liquid and vapor phases are contacted by mass transfer contacting elements that can be trays or structured packing or possibly, random packing. In any event, the contact produces a crude-rich liquid column bottoms in the higher pressure column that is rich in oxygen.
  • a stream of the crude-rich liquid column bottoms is then introduced in the lower pressure to be further refined into an oxygen-rich liquid column bottoms that collects in the lower pressure column and a nitrogen-rich column overhead that is formed in the lower pressure column.
  • the higher pressure column and the lower pressure column are operatively associated in a heat transfer relationship by a condenser reboiler or a main condenser that is typically located within the base of the lower pressure column.
  • the oxygen-rich liquid is in part vaporized with a stream of nitrogen-rich vapor produced from the nitrogen-rich vapor column overhead.
  • the stream of nitrogen-rich vapor is condensed in the condenser against the vaporization of the oxygen-rich liquid to produce a nitrogen-rich liquid stream that is used in refluxing both the higher pressure column and the lower pressure column. Part of such nitrogen-rich liquid stream can be taken as a product. Oxygen and nitrogen products can be removed from the higher and lower pressure columns and pass through the main heat exchanger to help cool the incoming air.
  • An argon product can also be produced by extracting an argon-rich stream from the lower pressure column and rectifying such stream in an argon column.
  • the argon-rich product collects as tower overhead and a stream of the same can be extracted.
  • the argon column is refluxed by condensing some of the argon-rich product with the crude liquid oxygen stream extracted from the higher pressure column.
  • the purity of the argon can be such that a large fraction of the oxygen is separated from the argon.
  • argon products can also be produced that are further refined to remove oxygen and residual nitrogen within such an argon product.
  • refrigeration has to be imparted into the cryogenic rectification plant to overcome warm end heat exchanger losses as well as heat leakage through the insulation of a cold box that is used to house the column such as described above.
  • This refrigeration can be imparted by partially cooling part of the air to be rectified within the main heat exchanger and expanding the same in a turboexpander. The work of expansion is extracted from the plant and the resultant cooled air is introduced into the bottom of a higher pressure column.
  • refrigeration can be imparted by an expander connected to the lower pressure column. The degree to which refrigeration is imparted to the air separation plant will determine the amount of liquid products that can be produced, typically from the oxygen-rich liquid column bottoms produced in the lower pressure column, but also possibly from the nitrogen-rich liquid stream.
  • nitrogen vapor is removed from the higher pressure column and split into two streams, one stream passes through the heat exchangers of a nitrogen liquefier and the other stream passes through the main heat exchangers.
  • the two nitrogen vapor streams are introduced into a recycle compressor and then through dual turbine-booster compressor arrangements to produce a liquid nitrogen stream that is reintroduced into the higher pressure column to produce liquid nitrogen and oxygen products.
  • the present invention provides a method of retrofitting an existing air separation plant with a nitrogen liquefier that either allows or increases the ability to withdraw a liquid oxygen product and optionally, a liquid nitrogen product and can increase argon production when such a plant is outfitted with an argon column.
  • the liquefier is integrated in a manner that does not involve the high degree of integration in the prior art.
  • the present invention provides a method of retrofitting an existing air separation plant to produce or to increase production of at least one liquid product.
  • air is separated within the existing air separation plant.
  • the existing air separation plant has at least higher and lower pressure columns operatively associated with one another in a heat transfer relationship.
  • the existing air separation plant is retrofitted by connecting a nitrogen liquefier to the higher pressure column.
  • the nitrogen liquefier has no components in common with existing components of said existing air separation plant.
  • the nitrogen liquefier is connected to the higher pressure column such that the nitrogen liquefier only receives a nitrogen-rich vapor stream from a top portion of the higher pressure column.
  • the nitrogen-rich vapor stream is liquefied in the nitrogen liquefier to produce a nitrogen-rich liquid stream and at least a portion of the nitrogen-rich liquid stream is introduced into the higher pressure column. This increases liquid nitrogen reflux to the higher pressure column, production of a crude liquid oxygen column bottoms formed in the higher pressure column and therefore, an oxygen-rich liquid formed in a bottom region of the lower pressure column.
  • the at least one liquid product is withdrawn from the air separation unit and it comprises an oxygen-rich liquid stream composed of the oxygen-rich liquid.
  • a nitrogen vapor stream comprising the nitrogen-rich vapor stream is warmed within a heat exchanger, expanded to exhaust stream pressure of a turbine exhaust stream and combined with the turbine exhaust stream to produce a combined stream.
  • the combined stream is compressed in a recycle compressor and after removal of the heat of compression, is divided into a refrigerant fluid stream and a remaining part of the combined stream.
  • the refrigerant fluid stream is compressed in a booster compressor, partially cooled in the heat exchanger and then introduced into the turboexpander to generate the turbine exhaust stream.
  • the turbine exhaust stream is warmed within the heat exchanger and combined with the nitrogen-rich vapor stream.
  • the remaining part of the combined stream is cooled within the heat exchanger and is expanded to higher pressure column pressure.
  • the nitrogen-rich liquid stream is formed from at least part of the combined stream.
  • the work of expansion of the turboexpander powers the booster compressor.
  • the expansion of the remaining part of the combined stream produces a two-phase stream and the liquid and vapor phases of the two-phase stream are disengaged to form a vapor phase stream and a liquid phase stream.
  • the vapor phase stream is combined with a nitrogen-rich vapor stream to form the nitrogen vapor stream prior to its introduction into the heat exchanger.
  • the liquid nitrogen stream is composed of the liquid phase stream.
  • a liquid nitrogen product stream can be withdrawn that is made up of a further part of the nitrogen-rich liquid stream.
  • the air separation unit can also be provided with an argon column connected to the lower pressure column to purify an argon-rich stream and thereby to produce an argon product stream.
  • the further part of the nitrogen-rich stream is withdrawn at a rate that does not increase oxygen concentration within the argon-rich stream. Where, the further part of the nitrogen-rich stream is not produced, argon recovery can be increased by increased production of the oxygen-rich liquid and removal of the oxygen-rich liquid stream.
  • the nitrogen liquefier can be operated intermittently so that the at least one liquid product stream is able to be stored for future utilization.
  • the existing air separation plant can be configured such that attachment points exist within the higher pressure column of the existing air separation plant for connection to the nitrogen liquefier if the same is to be retrofitted.
  • FIG. 1 is a schematic process flow diagram of an existing air separation plant that is used in carrying out a method in accordance with the present invention.
  • FIG. 2 is a schematic process flow diagram of a nitrogen-rich liquefier that is to be retrofitted and connected to the higher pressure column of the air separation plant illustrated in FIG. 1 .
  • an existing air separation plant 1 is illustrated for exemplary purposes. As will be discussed, it includes a higher and lower pressure column, an ultra high purity oxygen column and argon columns to produce liquid argon as a product. However, this is for exemplary purposes only and the present invention has applicability to an air separation plant that has solely a higher pressure column and a lower pressure column or one that also includes an argon column.
  • Prepurification unit 18 typically contains beds of adsorbents that are operated in an out of phase cycle to purify the air stream of higher boiling contaminants such as carbon monoxide, carbon dioxide and water vapor.
  • the cycle can be pressure swing adsorption cycle or a temperature swing adsorption cycle.
  • the resulting compressed and purified air stream 20 is then divided into a first portion 22 and a second portion 24 .
  • First portion 22 is utilized in generating refrigeration for the plant.
  • An exhaust stream 26 is combined with first portion 22 and introduced into a recycle compressor 28 .
  • the resultant compressed stream is divided into a first subsidiary stream 32 and a second subsidiary stream 34 .
  • First subsidiary stream 32 is fully cooled within the main heat exchanger 36 and second subsidiary stream 34 is introduced into a turbine booster compressor 38 .
  • the resulting compressed stream is cooled within main heat exchanger 36 and introduced into a turbine 42 in which the work of expansion can be utilized to drive the turbine booster compressor 38 .
  • the expansion occurring within turbine 42 produces the cooled exhaust stream 26 which is warmed within main heat exchanger 36 to impart the refrigeration into the air separation plant 1 .
  • Air separation plant 1 is provided with a higher pressure column 44 that is operatively associated with a lower pressure column 46 in a heat transfer relationship by means of a condenser reboiler 48 .
  • air separation plant 1 is also provided with a low ratio column 50 associated with a superstage column 52 to separate argon in a manner that will be discussed.
  • an ultra high purity oxygen column 54 is provided to produce an ultra high purity oxygen product that will also be discussed.
  • Each of the higher pressure column 44 , the lower pressure column 46 , the low ratio column 50 , the superstage column 52 and the ultra high purity liquid oxygen column 54 contain mass transfer elements such as structured packing or trays to bring liquid and vapor phases of the mixtures that are introduced therein to be separated into intimate contact and thereby to rectify such mixtures.
  • Second portion 24 of the compressed air stream is fully cooled within main heat exchanger 36 and divided into a first subsidiary stream 60 that is introduced directly into the higher pressure column 44 and a second subsidiary stream 62 that is introduced into a reboiler 64 placed in the bottom of ultra high purity oxygen column 54 to produce a liquid stream 66 .
  • First subsidiary stream 32 is fully cooled within the main heat exchanger 36 and is divided into first and second portions 68 and 70 .
  • First portion 68 is introduced directly into the lower pressure column 46 and second portion 70 is combined with the liquid stream 66 to form a combined stream 72 that is introduced into the higher pressure column 44 .
  • the introduction of combined stream 72 along with first portion 60 initiate the formation of an ascending vapor phase within higher pressure column 44 that becomes evermore lean in nitrogen to produce a nitrogen-rich vapor column overhead.
  • a stream of the nitrogen-rich column overhead as a stream 74 is condensed within a condenser reboiler 48 .
  • a first portion 76 is returned as a reflux stream to higher pressure column 44 and a second portion 78 is subcooled within main heat exchanger 36 and used to reflux the lower pressure column 46 .
  • a portion 80 can be optionally taken as a liquid nitrogen product and the remaining portion 82 can then be introduced as a reflux stream into the lower pressure column 46 .
  • a crude liquid oxygen stream 84 composed of the crude liquid oxygen column bottoms can be introduced into a heat exchanger 86 that is used in generating reflux for the superstage argon separation column 52 . This partially vaporizes crude liquid oxygen stream 84 to produce a liquid phase stream 88 and a vapor phase stream 89 that is introduced into the lower pressure column 46 for further refinement. Additionally, another crude liquid oxygen stream 87 can be introduced into the lower pressure column 46 . Although not illustrated, but as known in the art, both crude liquid oxygen streams 84 and 87 would be valve expanded prior to their introduction into the lower pressure column so that the streams are at a pressure suitable for introduction into such column.
  • the descending liquid phase within lower pressure column 46 produces an oxygen-rich liquid that is vaporized by condenser reboiler 48 .
  • Residual liquid can be taken as a liquid oxygen product stream 90 .
  • the resulting nitrogen-rich vapor can be taken as a nitrogen vapor product stream 92 .
  • Nitrogen vapor product stream 92 can have a concentration of less than about 2 ppm.
  • a waste nitrogen stream 94 can also be removed. Waste nitrogen stream 94 can be used in regenerating adsorbents within prepurification unit 18 . Both nitrogen vapor product stream 92 and waste nitrogen stream are first warmed in a superheater and then in the main heat exchanger 36 to near ambient temperatures.
  • a gaseous oxygen product stream 96 can also be removed from lower pressure column 46 that consists of vaporized oxygen-rich liquid that is produced by the vaporization of the liquid phase at the bottom of lower pressure column 46 by condenser reboiler 48 .
  • Both gaseous oxygen product stream 96 and liquid oxygen product stream 90 can have a purity of about 99.5 percent by volume.
  • An argon containing vapor stream 98 that can contain greater than about 10 percent by volume argon and less than 1 ppm nitrogen can be removed from the lower pressure column 46 and introduced into the low ratio column 50 .
  • the oxygen-rich column bottoms can be returned as an oxygen-rich liquid stream 100 back to the lower pressure column 46 .
  • the argon-rich column overhead can be taken as an argon-rich stream 102 and introduced into superstage column 52 for separation of oxygen to very low levels to thereby produce an oxygen-rich column bottoms that can be removed as an oxygen-rich stream 106 that is pumped by a pump 108 back to the low ratio column 50 as a pumped stream 110 .
  • An argon-rich stream 112 can be introduced into heat exchanger 86 to produce an argon reflux stream 114 , an argon vent stream 116 is taken to prevent build up of non-condensable nitrogen and a liquid argon product stream 120 can be removed from the superstage argon column 52 as a liquid argon product stream that can contain less than about 1 ppm nitrogen and about 1 ppm oxygen.
  • An oxygen liquid stream 122 that is essentially hydrocarbon and nitrogen free can be removed from the low ratio argon column 50 and introduced into the ultra high purity oxygen column 54 as feed to produce an ultra high purity liquid oxygen product stream 124 from residual liquid that is not reboiled by reboiler 64 that has a purity of about 99.99999 percent oxygen.
  • the vapor overhead within ultra high purity oxygen column 54 can be removed as a vapor stream 126 that is reintroduced into the low ratio column 50 .
  • the air separation plant 1 produces an ultra high purity liquid oxygen product 124 , a liquid oxygen product 90 and potentially a liquid nitrogen product stream 80 .
  • the degree to which liquids are produced is dependent upon the total refrigeration that is imparted into air separation plant 1 .
  • the aforesaid liquid products are produced at a lower rate.
  • a liquefier 2 can be retrofitted into air separation plant 1 . Liquefier 2 is illustrated in FIG. 2 .
  • a nitrogen-rich vapor stream 130 is introduced into liquefier 2 that liquefies the nitrogen-rich vapor stream 130 and returns the resulting nitrogen-rich liquid stream 132 back to the higher pressure column 44 . It is to be noted that it is solely that nitrogen-rich vapor stream 130 that is removed and the nitrogen-rich liquid stream 132 that is reintroduced into the lower pressure column 44 .
  • liquid nitrogen product stream 80 and ultra high purity liquid oxygen stream 124 can also be withdrawn at a greater rate.
  • liquid nitrogen product stream 80 should not be withdrawn in an excessive rate that would affect the purity of argon-rich stream 98 .
  • the increased amount of liquid nitrogen that is being introduced into the lower pressure column 46 without any production of liquid nitrogen product stream 80 will increase the argon concentration within argon-rich stream 98 and thereby increase the recovery and rate at which liquid argon product stream 120 can be removed from superstage column 52 . Consequently, in one mode of operation, liquid nitrogen stream 80 is removed at a rate that will not effect the argon concentration of argon-rich stream 98 or alternatively can be removed at a lesser rate or not removed at all to increase the argon concentration of argon-rich stream 98 . It is to be noted that it is also possible to take a liquid nitrogen product stream from part of the nitrogen-rich liquid stream 132 and the same discussion as above would apply to removal of such a stream as a product.
  • air separation plant 1 can be constructed with standard attachment points 128 and 129 that allow for the simple connection of the nitrogen liquefier 2 to such a plant.
  • attachment points 128 and 129 could be capped pipes or closed and capped valves that would be built into a standard plant design.
  • a product line of plants could thereby be designed with such attachment points 128 and 129 . This would allow the retrofit of nitrogen liquefier 2 to be carried out in an expeditious and cost effective manner if the same were desired on any such plant within the product line.
  • the air separation plant 1 could be utilized to operate in a mode in which liquid production of products were increased to meet an increased demand.
  • the nitrogen liquefier 2 could be employed to increase oxygen production during periods in which electrical power could be obtained at lower cost to allow the liquid products produced at the enhanced rate to be stored for later use during periods of higher cost electrical power.
  • the nitrogen liquefier could also be employed during turn-down conditions of the plant to produce liquid products at such time.
  • a yet further mode of operation is to employ nitrogen liquefier 2 in connection with a plant not designed to produce liquid products and retrofit such plant to produce liquid products.
  • nitrogen liquefier 2 to be retrofitted to air separation plant 1 is illustrated.
  • nitrogen-rich vapor stream 130 combined with a vapor phase stream 134 that is expanded in an expansion valve 136 to the pressure of nitrogen-rich vapor stream 130 and combined therewith to form a nitrogen stream 138 .
  • Nitrogen stream 138 is warmed within a heat exchanger 140 and is then reduced in pressure within an expansion valve 142 . After the reduction in pressure, the nitrogen stream 138 is combined with an exhaust stream 144 which imparts refrigeration to the liquefier by being fully warmed within the heat exchanger 140 . This produces a combined stream 146 that is compressed within a recycle compressor 148 .
  • a first portion 152 is introduced into a booster compressor 154 to produce a compressed stream 156 .
  • compressed stream 156 is partially cooled within heat exchanger 140 , reduced in pressure by means of an expansion valve 158 and is then introduced into turbine 160 to produce exhaust stream 144 .
  • the work of expansion provided by turbine 160 can be applied to the compression within booster compressor 154 .
  • the other portion 162 of combined stream 146 after having been compressed in compressor 148 and cooled within after cooler 150 , is fully cooled in heat exchanger 140 and then expanded by means of an expansion valve 164 into a two-phase fluid that is introduced into a phase separator 166 .
  • the vapor phase is disengaged from the liquid within phase separator 166 to produce nitrogen vapor phase stream 134 .
  • a liquid phase stream 168 is reduced in pressure by means of an expansion valve 170 to a pressure of the higher pressure column 44 and introduced as the nitrogen-rich liquid stream 132 back into lower pressure column 44 .
  • nitrogen liquefier 2 could be utilized in accordance with the present invention.
  • a very simple nitrogen liquefier could be used in which the nitrogen-rich vapor stream 130 alone was compressed, expanded and liquefied at of course a much higher energy cost.
  • nitrogen liquefier 2 is a particularly advantageous design in its simplicity and strikes a balance between simplicity and efficiency for retrofit applications.

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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)
  • Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)
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US12/164,269 2008-06-30 2008-06-30 Nitrogen liquefier retrofit for an air separation plant Abandoned US20090320520A1 (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US12/164,269 US20090320520A1 (en) 2008-06-30 2008-06-30 Nitrogen liquefier retrofit for an air separation plant
ES09773952T ES2383781T3 (es) 2008-06-30 2009-05-12 Reacondicionamiento de licuador de nitrógeno para una planta de separación de aire
EP09773952A EP2307835B1 (en) 2008-06-30 2009-05-12 Nitrogen liquefier retrofit for an air separation plant
BRPI0914327A BRPI0914327A2 (pt) 2008-06-30 2009-05-12 método para reequipar uma instalação de separação de ar existente
MX2010013697A MX2010013697A (es) 2008-06-30 2009-05-12 Adaptacion de licuador de nitrogeno para una planta de separacion de aire.
AT09773952T ATE548620T1 (de) 2008-06-30 2009-05-12 Stickstoffverflüssigernachrüstung für eine lufttrennanlage
KR1020107029373A KR20110026435A (ko) 2008-06-30 2009-05-12 공기 분리 플랜트를 위한 질소 액화기 개장
PCT/US2009/043558 WO2010002500A2 (en) 2008-06-30 2009-05-12 Nitrogen liquefier retrofit for an air separation plant
CN200910151331A CN101619917A (zh) 2008-06-30 2009-06-30 空气分离装置的氮液化器改造

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US12/164,269 US20090320520A1 (en) 2008-06-30 2008-06-30 Nitrogen liquefier retrofit for an air separation plant

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EP (1) EP2307835B1 (es)
KR (1) KR20110026435A (es)
CN (1) CN101619917A (es)
AT (1) ATE548620T1 (es)
BR (1) BRPI0914327A2 (es)
ES (1) ES2383781T3 (es)
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WO (1) WO2010002500A2 (es)

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ES2383781T3 (es) 2012-06-26
ATE548620T1 (de) 2012-03-15
CN101619917A (zh) 2010-01-06
EP2307835B1 (en) 2012-03-07
WO2010002500A2 (en) 2010-01-07
KR20110026435A (ko) 2011-03-15
EP2307835A2 (en) 2011-04-13
MX2010013697A (es) 2010-12-21
BRPI0914327A2 (pt) 2015-10-13
WO2010002500A3 (en) 2010-09-30

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