EP2713128A1 - Verfahren zur Abscheidung von Luft durch kryogene Destillation - Google Patents

Verfahren zur Abscheidung von Luft durch kryogene Destillation Download PDF

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Publication number
EP2713128A1
EP2713128A1 EP12306195.4A EP12306195A EP2713128A1 EP 2713128 A1 EP2713128 A1 EP 2713128A1 EP 12306195 A EP12306195 A EP 12306195A EP 2713128 A1 EP2713128 A1 EP 2713128A1
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EP
European Patent Office
Prior art keywords
column
period
sent
during
nitrogen
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.)
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Application number
EP12306195.4A
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English (en)
French (fr)
Inventor
Benoit Davidian
Richard Dubettier-Grenier
Jean-Marc Peyron
Bernard Saulnier
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP12306195.4A priority Critical patent/EP2713128A1/de
Priority to EP13763036.4A priority patent/EP2904339A2/de
Priority to PCT/EP2013/068965 priority patent/WO2014053297A2/en
Priority to CN201380051043.6A priority patent/CN105431698A/zh
Priority to US14/431,918 priority patent/US20150253075A1/en
Publication of EP2713128A1 publication Critical patent/EP2713128A1/de
Withdrawn legal-status Critical Current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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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    • 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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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—Nitrogen
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
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    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • 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
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the present invention relates to a process for the separation of air by cryogenic distillation.
  • the Integrated Gasified Combined Cycle is usually selected to generate clean energy from coal. This clean energy production technique is especially suited for new coal-based power generation projects specified to operate efficiently and with minimal pollution to the environment.
  • the air separation unit ASU for the IGCC is a combination of an oxygen plant and a nitrogen generator plant.
  • the air separation process frequently used for this type of application is the elevated pressure process.
  • air separation units operating with this concept have good energy efficiency and reduced power consumption, it is not always possible to use this sort of ASU because the nitrogen/oxygen ratio is generally fixed at a value close to that found for air, ie close to 3.6. If the required ratio is lower than this value, for example about 2.5.
  • An object of the present invention is to provide an air separation unit with reduced energy consumption but which is capable of producing nitrogen and oxygen with a nitrogen/oxygen ratio of less than 3.6, preferably greater than 4.
  • a process for the separation of air by cryogenic distillation in which air is purified, cooled in a heat exchanger and separated in a column system including at least a first column and a second column, the first column operating at a higher pressure than the second column and the top of the first column being thermally linked to the bottom of the second column via a first reboiler-condenser, oxygen enriched liquid is removed from the first column and sent to the second column or liquid derived from the oxygen enriched liquid is sent to the second column, nitrogen enriched liquid is removed from the first column and sent to the second column, oxygen rich liquid is removed from the second column, pressurized and vaporized in the heat exchanger to form an oxygen rich gas, nitrogen rich fluid is removed from the column system and warmed in the heat exchanger to form a first nitrogen rich gas, wherein
  • Figure 1 shows a cryogenic air separation process using a standard double column, having a first column 11 and a second column 15, the first column operating at a higher pressure than the second column and being placed below the second column.
  • the top of the first column 11 is thermally linked to the bottom of the second column 15 by means of a vaporizer-condenser 13 placed at the bottom of the second column 15.
  • a vaporizer-condenser 13 placed at the bottom of the second column 15.
  • the second column it is also possible for the second column to use an intermediate vaporizer-condenser (not illustrated).
  • the process also uses an intermediate pressure column 17 having a bottom reboiler 65 and a top condenser.
  • the presence of the column 17 is not essential.
  • an air stream 1 compressed to the operating pressure of the first column 11 is divided into two parts.
  • One part 3 is cooled in heat exchanger 9 and sent in gaseous form to the first column 11.
  • the other part 5 is boosted to a higher pressure by booster compressor 7 and sent to the heat exchanger 7.
  • the boosted air 5 is cooled in the heat exchanger 9 and sent to the first column 11 after expansion in liquid or partially condensed form.
  • oxygen enriched liquid 19 from the bottom of the first column 11 is sent to subcooler 25 and then expanded into the column 17.
  • Liquid 67 from the bottom of column 17 is sent to the top condenser as stream 64, where it is partially evaporated, the liquid and gas streams formed being sent to the second column 15.
  • Part 71 of the liquid is sent from the bottom of column 17 to the second column 15.
  • a liquid stream 21 is removed from an intermediate region of the first column and expanded into the second column 15.
  • at least part of stream 5 can be sent directly to the second column 15.
  • a first nitrogen enriched liquid stream is sent as stream 23 from the first column to the second column, being removed a few trays below the top of the first column.
  • a nitrogen enriched gas stream 61 is removed at the top of the first column, condensed in bottom condenser 65 and mixed with stream 23 as stream 63.
  • a liquid stream 55 from the top of column 17 is sent to the top of column 15.
  • the column system produces a high pressure gaseous oxygen stream 53 by removing liquid oxygen 49 from the bottom of second column 15, pressurizing it via pump 51 and vaporizing the pumped liquid in exchanger 9.
  • the column system produces a high pressure gaseous nitrogen stream 47 by removing liquid nitrogen 43 from the top of first column 11, pressurizing it via pump 45 and vaporizing the pumped liquid in exchanger 9.
  • pressurized streams may be sent to a gasifier.
  • gaseous nitrogen 29, 37 is removed at the top of the second column 15, warmed in subcooler 25, partially warmed in heat exchanger 9 and sent as stream 75 to a turbine 73 having an inlet temperature which is an intermediate temperature of the heat exchanger 9.
  • the expanded nitrogen is sent to the cold end of the exchanger and warmed as far as the warm end.
  • the nitrogen 75 forms a waste stream.
  • Another part of the nitrogen 37 is warmed in the heat exchanger to the warm end, compressed in compressor 39 and sent to a gas turbine via conduit as stream 41.
  • the process uses two particular special operations during two periods.
  • the ratio between the amount of nitrogen rich gas produced 41 and the amount of oxygen rich gas 53 produced is greater than 2.5.
  • Nitrogen enriched liquid 57A is sent from a storage tank 27 to the column system 11,15 and nitrogen enriched gas 29, 31 from the second column 15 of the column system is compressed in a compressor 33 having an inlet temperature of less than -50°C and then sent to the cold end of the heat exchanger 9.
  • the compressor 33 only operates when nitrogen enriched liquid 57A is sent to the column.
  • the gas 31 is then warmed in the heat exchanger and mixed with the gas from compressor 39 to form stream 41. Either no nitrogen is sent to the turbine 73 or some nitrogen may be sent to the turbine 73.
  • the product ratio is less than 2.5 and a nitrogen rich gas removed from the column system is expanded in a turbine 73 having an inlet temperature lower than the ambient temperature and nitrogen enriched liquid 57 is sent to the storage tank 27 from the column system. No nitrogen is sent to the compressor 33 and all of stream 29 is removed as stream 37.
  • Figure 2 shows a variant of Figure 1 in which the cold turbine 73 is replaced by a liquefier.
  • the ratio between the amount of nitrogen rich gas produced 41 and the amount of oxygen rich gas 53 produced (known as the "product ratio"), is greater than 2.5.
  • Nitrogen enriched liquid 57A is sent from a storage tank 27 to the column system 11,15 and nitrogen enriched gas 29,31 from the second column 15 of the column system is compressed in a compressor 33 having an inlet temperature of less than -50°C and then sent to the cold end of the heat exchanger 9.
  • the compressor 33 only operates when nitrogen enriched liquid 57A is sent to the column.
  • the gas 31 is then warmed in the heat exchanger and mixed with the gas from compressor 39 to form stream 41.
  • the product ratio is less than 2.5 and a nitrogen rich gas removed from the column system 37 is warmed as far as the warm end of exchanger 9. Then part of the gas is sent to compressor 39 and the rest 75 is compressed by compressor 101 and divided into two. One part 79 is cooled and liquefied in exchanger 109 to form a partially condensed stream. This stream separates in a phase separator and the liquid formed serves as final product 83. The gas 85 is sent back to the exchanger, warmed and sent to the atmosphere. The other part of gas from compressor 101 is further compressed in boosters 103, 105, is cooled in exchanger 109 and is expanded in a turbine 73 having an inlet temperature lower than the ambient temperature.
  • the expanded gas is warmed in the exchanger 109 to an intermediate temperature and divided into two.
  • One part 81 is expanded at the intermediate temperature in turbine 173 and rewarmed in the exchanger before being sent to the atmosphere.
  • the rest 79 is warmed and recycled upstream of compressor 101.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP12306195.4A 2012-10-01 2012-10-01 Verfahren zur Abscheidung von Luft durch kryogene Destillation Withdrawn EP2713128A1 (de)

Priority Applications (5)

Application Number Priority Date Filing Date Title
EP12306195.4A EP2713128A1 (de) 2012-10-01 2012-10-01 Verfahren zur Abscheidung von Luft durch kryogene Destillation
EP13763036.4A EP2904339A2 (de) 2012-10-01 2013-09-13 Verfahren zur abscheidung von luft durch kryogene destillation
PCT/EP2013/068965 WO2014053297A2 (en) 2012-10-01 2013-09-13 Process for the separation of air by cryogenic distillation
CN201380051043.6A CN105431698A (zh) 2012-10-01 2013-09-13 通过低温蒸馏分离空气的方法
US14/431,918 US20150253075A1 (en) 2012-10-01 2013-09-13 Process for the separation of air by cryogenic distillation

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP12306195.4A EP2713128A1 (de) 2012-10-01 2012-10-01 Verfahren zur Abscheidung von Luft durch kryogene Destillation

Publications (1)

Publication Number Publication Date
EP2713128A1 true EP2713128A1 (de) 2014-04-02

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EP12306195.4A Withdrawn EP2713128A1 (de) 2012-10-01 2012-10-01 Verfahren zur Abscheidung von Luft durch kryogene Destillation
EP13763036.4A Withdrawn EP2904339A2 (de) 2012-10-01 2013-09-13 Verfahren zur abscheidung von luft durch kryogene destillation

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EP (2) EP2713128A1 (de)
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EP3438584B1 (de) * 2017-08-03 2020-03-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Verfahren und gerät zur trennung von luft durch kryogene destillation
WO2019127179A1 (en) 2017-12-28 2019-07-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Utilization of nitrogen-enriched streams produced in air separation units comprising split-core main heat exchangers
CN109059422A (zh) * 2018-07-12 2018-12-21 北京拓首能源科技股份有限公司 一种利用污氮冷能预冷空气的装置
US20220034584A1 (en) * 2020-07-30 2022-02-03 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Large liquid oxygen and liquefied natural gas production process
US20220252341A1 (en) * 2021-02-05 2022-08-11 Air Products And Chemicals, Inc. Method and system for decarbonized lng production
US20240035745A1 (en) * 2022-07-28 2024-02-01 Neil M. Prosser System and method for cryogenic air separation using four distillation columns including an intermediate pressure column
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

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WO2014053297A3 (en) 2015-11-19
WO2014053297A2 (en) 2014-04-10
EP2904339A2 (de) 2015-08-12
CN105431698A (zh) 2016-03-23
US20150253075A1 (en) 2015-09-10

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