EP1746374A2 - Process and apparatus for the separation of air by cryogenic distillation - Google Patents

Process and apparatus for the separation of air by cryogenic distillation Download PDF

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Publication number
EP1746374A2
EP1746374A2 EP06117128A EP06117128A EP1746374A2 EP 1746374 A2 EP1746374 A2 EP 1746374A2 EP 06117128 A EP06117128 A EP 06117128A EP 06117128 A EP06117128 A EP 06117128A EP 1746374 A2 EP1746374 A2 EP 1746374A2
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EP
European Patent Office
Prior art keywords
air
heat exchanger
stream
purge
column system
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.)
Withdrawn
Application number
EP06117128A
Other languages
German (de)
French (fr)
Other versions
EP1746374A3 (en
Inventor
Tadeusz Pawulski
Michael A. Turney
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.)
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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Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP1746374A2 publication Critical patent/EP1746374A2/en
Publication of EP1746374A3 publication Critical patent/EP1746374A3/en
Withdrawn legal-status Critical Current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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—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
    • 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
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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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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/0423—Subcooling of liquid process streams
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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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
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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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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
    • 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
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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
    • F25J3/044—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 single pressure main column system only
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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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    • 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
    • F25J3/0446—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 the heat generated by mixing two different phases
    • F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
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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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
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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
    • 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.
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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
    • 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
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    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
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    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"

Definitions

  • the present invention relates to a process and apparatus for the separation of air by cryogenic distillation.
  • a cryogenic air separation unit has a distillation section where air is distilled into its heavy and light components. In this process, hydrocarbons become concentrated in the liquid oxygen stream and create a safety concern. Front-end adsorption beds of alumina and molecular sieve do not stop all these impurities from entering the distillation process.
  • This disclosure suggests installing a small purge vaporizer exchanger, which will provide recovery of most of the refrigeration of the purged liquid stream.
  • This exchanger vaporizes and warms the oxygen stream against a warm air stream.
  • the warm vaporized oxygen may be either vented or remixed with the gaseous oxygen exiting the main heat exchanger as product.
  • the warm air stream may come from the discharge of the absorbers, booster compressor, or other warm pressurized source.
  • the flow of air is adjusted to control the temperature of the air exiting the exchanger above a specified value (- -90°C) to avoid the deposit of hydrocarbons in the exchanger.
  • the low pressure column LP is placed above the mixing column M in a single structure with the high pressure column HP placed apart but thermally linked with the low pressure column, via condenser C.
  • a stream of compressed and purified air 1 substantially at the pressure of the high pressure column HP, is sent to the cold box. It is split into three streams.
  • the first stream 3 is not cooled, but sent to a booster compressor B, where it is compressed to a pressure substantially higher than that of the high pressure column. It is then divided into two portions 9 and 11 .
  • Portion 9 is sent to heat exchanger E2, whilst portion 11 is cooled in after-cooler A, and then sent to main heat exchanger E1 for further cooling.
  • Heat exchanger E2 may be of the shell and tube type, wound tube type, or any design capable of handling large temperature gradients, and avoiding potential plugging of the exchanger passages.
  • Portion 9 is used to vaporize a stream of purge oxygen 31 from the condenser of the high pressure column within the heat exchanger E2.
  • the air entering the heat exchanger E2 is at a temperature well above ambient, whereas the oxygen stream has been pumped at cryogenic temperatures. It is consequently necessary to adjust the air flow 9 so that the air leaving exchanger E2 is above a specified value ( ⁇ -90°C) to avoid the deposit of hydrocarbons therein.
  • a temperature indicator and controller TIC may be placed on the outlet air of exchanger E2 which controls a valve V used to change the airflow 9 .
  • Portion 11 is cooled to an intermediate temperature of the heat exchanger E1 and sent to turboexpander T along with the cooled air stream 9 from exchanger E2.
  • the expanded stream of air 13 is then sent to the low pressure column LP.
  • Air stream 5 is cooled to an intermediate temperature of the heat exchanger E1 and then sent to the bottom of the mixing column M.
  • Air stream 7 flows from the warm end to the cold end of heat exchanger E1 and is then sent to the bottom of the high pressure column HP.
  • the columns shown illustrate a conventional mixing column set up in which liquid oxygen 29 is sent from the condenser to the top of the mixing column M, liquid nitrogen 21 is sent from the high pressure column HP to the top of the low pressure column LP and oxygen enriched liquid 23 is sent from the bottom of the high pressure column to the low pressure column.
  • An intermediate liquid 17 and a bottom liquid 15 of the mixing column M are sent to the low pressure column LP.
  • the bottom liquid is preferably mixed with air stream 13 before entering the column LP.
  • the condenser C is fed with bottom liquid 25 from the LP column and produces vaporized gaseous oxygen 27 , which is sent back to the low pressure column.
  • Gaseous nitrogen 19 is removed from the top of the low pressure column and warmed in heat exchanger E1.
  • Gaseous oxygen 33 from the top of the mixing column M is sent to the heat exchanger E1, warmed up to the warm end, and mixed with vaporized oxygen 31 from heat exchanger E2 to form the product oxygen stream 35 . It is important to have sufficient pressure drop available for the air stream to go through the purge vaporizer E2, control valve V, and piping before mixing back into the process. If the available pressure drop is too low, it may not be possible to achieve enough air flow through the purge vaporizer and it will not work properly. On the other hand, if too much pressure drop is taken (e.g. by taking medium pressure air and returning to the low pressure circuit after the turbine) then the reduction in turbine flow will yield a loss of refrigeration and reduce the refrigeration benefit of the purge vaporizer.
  • the air is taken from the discharge of a booster compressor but before its aftercooler, it can be injected back into the inlet of the turbine, such that refrigeration is not lost (See Figure 1).
  • the air stream essentially bypasses the aftercooler and warm section of the main exchanger. This yields enough pressure drop for the purge vaporizer and control valve, since the booster aftercooler typically takes significant pressure drop.
  • the air stream is taken from upstream of the booster compressor (if any) it is typically returned to the air stream at the cold end of the main exchanger. In this case the vaporized purge stream is returned to the inlet of the waste oxygen expander to minimize refrigeration loss.
  • the air separation unit of Figure 2 uses a single column with a double top reboiler.
  • a compressed purified air stream 1 is divided in two forming air stream 9 and air stream 5 .
  • Air stream 5 is sent to heat exchanger E1 in which it cools, and is then sent to the bottom of the column HP.
  • Air stream 9 is sent to heat exchanger E2 without passing into heat exchanger E1. It is then mixed with cooled air stream 5 and sent to the column HP.
  • Oxygen enriched liquid 15 from the bottom of the column is subcooled in exchanger E3 and sent to condenser C1.
  • Condenser C1 serves to condense part of the gaseous nitrogen at the top of the column thereby vaporizing part of the oxygen enriched liquid.
  • the vaporized oxygen enriched liquid is sent to a booster B and returned to the column at a point below the entry point of stream 5 .
  • the oxygen enriched liquid which is not vaporized in C1 is sent to condenser C2 situated underneath condenser C1.
  • Condenser C2 also serves to condense part of the gaseous nitrogen at the top of the column, thereby vaporizing part of the rest of the oxygen enriched liquid.
  • the oxygen enriched liquid purge not vaporized in C2 is removed as stream 31 and is vaporized in exchanger E2 against the air stream 9 .
  • the vaporized purge stream is expanded in turbine T, which drives booster B, used to subcool the oxygen enriched liquid in exchanger E2, warmed in exchanger E1 and removed from the system as stream 53 .
  • Product nitrogen 33 is removed from the top of the column and warmed in heat exchanger E1.
  • Medium purity nitrogen 19 is removed from the middle of the column and warmed in heat exchanger E1.
  • Liquid nitrogen 51 is removed from the top of the column and sent to storage S.
  • the invention may be applied in other types of air separation unit, such as single column units, double column units, and double column units incorporating other columns, such as argon columns and triple column units.
  • this applies to any plant that needs to purge heavy components and recover the refrigeration and/or molecules of the purge stream.
  • the purge is taken from the sump of the vaporizer or column, which contains the highest concentration of heavy components (e.g. hydrocarbons).

Abstract

A cryogenic distillation apparatus for the separation of air using a column system comprises at least one column (HP,LP,M) a main heat exchanger (E1), a conduit (5,11,7) for sending cooled compressed air to the main heat exchanger and from the main heat exchanger to the column system, conduits (33,19) for sending oxygen enriched, and nitrogen enriched streams from the column system to the main heat exchanger, a purge vaporizer (E2), a conduit for removing a purge stream (31) from the column system and sending the purge stream to the purge vaporizer, a conduit (13) for sending compressed and purified air (9) to the purge vaporizer and a conduit for sending compressed and purified air from the purge vaporizer to the column system.

Description

  • The present invention relates to a process and apparatus for the separation of air by cryogenic distillation.
  • A cryogenic air separation unit has a distillation section where air is distilled into its heavy and light components. In this process, hydrocarbons become concentrated in the liquid oxygen stream and create a safety concern. Front-end adsorption beds of alumina and molecular sieve do not stop all these impurities from entering the distillation process.
  • Traditional methods of removing the remainder of impurities in the oxygen rich liquid streams include an additional adsorption step through a bed of silica gel. Another option is simply to purge a small portion of the hydrocarbon containing oxygen liquid stream to prevent accumulation of heavy impurities, and maintain its concentrations at sufficiently low levels. This option is typically only justified for small projects where the additional capital cost of the silica gel adsorption unit is high compared to the loss of refrigeration caused by purging liquid oxygen. Therefore, it is desirable to have a cost effective system, which will remove the hazardous hydrocarbons without a high loss of refrigeration caused by purging liquid oxygen. U.S. Patent 5,379,599 and US Patent 5,471,842 describe the case where the purge stream is pumped and vaporized in the main heat exchanger.
  • This disclosure suggests installing a small purge vaporizer exchanger, which will provide recovery of most of the refrigeration of the purged liquid stream. This exchanger vaporizes and warms the oxygen stream against a warm air stream. The warm vaporized oxygen may be either vented or remixed with the gaseous oxygen exiting the main heat exchanger as product. The warm air stream may come from the discharge of the absorbers, booster compressor, or other warm pressurized source. The flow of air is adjusted to control the temperature of the air exiting the exchanger above a specified value (- -90°C) to avoid the deposit of hydrocarbons in the exchanger.
  • For a further understanding of the nature and objects of the present invention, reference should be made to the following detailed description, taken in conjunction with the accompanying drawings, in which like elements are given the same or analogous reference numbers and wherein:
    • Figure 1 illustrates an air separation unit according to the invention for the production of oxygen using a side by side double column and a mixing column;
    • Figure 2 illustrates Figure 2 shows an air separation unit according to the invention for the production of nitrogen using a single column.
  • In Figure 1, the low pressure column LP is placed above the mixing column M in a single structure with the high pressure column HP placed apart but thermally linked with the low pressure column, via condenser C.
  • A stream of compressed and purified air 1, substantially at the pressure of the high pressure column HP, is sent to the cold box. It is split into three streams. The first stream 3 is not cooled, but sent to a booster compressor B, where it is compressed to a pressure substantially higher than that of the high pressure column. It is then divided into two portions 9 and 11. Portion 9 is sent to heat exchanger E2, whilst portion 11 is cooled in after-cooler A, and then sent to main heat exchanger E1 for further cooling.
  • Heat exchanger E2 may be of the shell and tube type, wound tube type, or any design capable of handling large temperature gradients, and avoiding potential plugging of the exchanger passages.
  • Portion 9 is used to vaporize a stream of purge oxygen 31 from the condenser of the high pressure column within the heat exchanger E2. The air entering the heat exchanger E2 is at a temperature well above ambient, whereas the oxygen stream has been pumped at cryogenic temperatures. It is consequently necessary to adjust the air flow 9 so that the air leaving exchanger E2 is above a specified value (~-90°C) to avoid the deposit of hydrocarbons therein. For example a temperature indicator and controller TIC may be placed on the outlet air of exchanger E2 which controls a valve V used to change the airflow 9.
  • Portion 11 is cooled to an intermediate temperature of the heat exchanger E1 and sent to turboexpander T along with the cooled air stream 9 from exchanger E2. The expanded stream of air 13 is then sent to the low pressure column LP.
  • Air stream 5 is cooled to an intermediate temperature of the heat exchanger E1 and then sent to the bottom of the mixing column M.
  • Air stream 7 flows from the warm end to the cold end of heat exchanger E1 and is then sent to the bottom of the high pressure column HP.
  • The columns shown illustrate a conventional mixing column set up in which liquid oxygen 29 is sent from the condenser to the top of the mixing column M, liquid nitrogen 21 is sent from the high pressure column HP to the top of the low pressure column LP and oxygen enriched liquid 23 is sent from the bottom of the high pressure column to the low pressure column. An intermediate liquid 17 and a bottom liquid 15 of the mixing column M are sent to the low pressure column LP. The bottom liquid is preferably mixed with air stream 13 before entering the column LP.
  • The condenser C is fed with bottom liquid 25 from the LP column and produces vaporized gaseous oxygen 27, which is sent back to the low pressure column.
  • Gaseous nitrogen 19 is removed from the top of the low pressure column and warmed in heat exchanger E1.
  • Gaseous oxygen 33 from the top of the mixing column M is sent to the heat exchanger E1, warmed up to the warm end, and mixed with vaporized oxygen 31 from heat exchanger E2 to form the product oxygen stream 35.
    It is important to have sufficient pressure drop available for the air stream to go through the purge vaporizer E2, control valve V, and piping before mixing back into the process. If the available pressure drop is too low, it may not be possible to achieve enough air flow through the purge vaporizer and it will not work properly. On the other hand, if too much pressure drop is taken (e.g. by taking medium pressure air and returning to the low pressure circuit after the turbine) then the reduction in turbine flow will yield a loss of refrigeration and reduce the refrigeration benefit of the purge vaporizer.
  • If the air is taken from the discharge of a booster compressor but before its aftercooler, it can be injected back into the inlet of the turbine, such that refrigeration is not lost (See Figure 1). For this case, the air stream essentially bypasses the aftercooler and warm section of the main exchanger. This yields enough pressure drop for the purge vaporizer and control valve, since the booster aftercooler typically takes significant pressure drop.
  • If the air stream is taken from upstream of the booster compressor (if any) it is typically returned to the air stream at the cold end of the main exchanger. In this case the vaporized purge stream is returned to the inlet of the waste oxygen expander to minimize refrigeration loss.
  • The air separation unit of Figure 2 uses a single column with a double top reboiler. In Figure 2, a compressed purified air stream 1 is divided in two forming air stream 9 and air stream 5. Air stream 5 is sent to heat exchanger E1 in which it cools, and is then sent to the bottom of the column HP. Air stream 9 is sent to heat exchanger E2 without passing into heat exchanger E1. It is then mixed with cooled air stream 5 and sent to the column HP.
  • Oxygen enriched liquid 15 from the bottom of the column is subcooled in exchanger E3 and sent to condenser C1. Condenser C1 serves to condense part of the gaseous nitrogen at the top of the column thereby vaporizing part of the oxygen enriched liquid. The vaporized oxygen enriched liquid is sent to a booster B and returned to the column at a point below the entry point of stream 5.
  • The oxygen enriched liquid which is not vaporized in C1 is sent to condenser C2 situated underneath condenser C1. Condenser C2 also serves to condense part of the gaseous nitrogen at the top of the column, thereby vaporizing part of the rest of the oxygen enriched liquid. The oxygen enriched liquid purge not vaporized in C2 is removed as stream 31 and is vaporized in exchanger E2 against the air stream 9. The vaporized purge stream is expanded in turbine T, which drives booster B, used to subcool the oxygen enriched liquid in exchanger E2, warmed in exchanger E1 and removed from the system as stream 53.
  • Product nitrogen 33 is removed from the top of the column and warmed in heat exchanger E1. Medium purity nitrogen 19 is removed from the middle of the column and warmed in heat exchanger E1. Liquid nitrogen 51 is removed from the top of the column and sent to storage S.
  • It will be appreciated that the invention may be applied in other types of air separation unit, such as single column units, double column units, and double column units incorporating other columns, such as argon columns and triple column units. In general, this applies to any plant that needs to purge heavy components and recover the refrigeration and/or molecules of the purge stream. The purge is taken from the sump of the vaporizer or column, which contains the highest concentration of heavy components (e.g. hydrocarbons). The essential characteristics of the present invention are described completely in the foregoing disclosure. One skilled in the art can understand the invention and make various modifications without departing from the spirit of the invention and without deviating from the scope and equivalents of the claims, which follow.

Claims (10)

  1. A cryogenic distillation air separation process using a column system comprising at least one column including the steps of:
    a) compressing feed air in a compressor to produce compressed air;
    b) purifying compressed air in a purification unit to produce compressed and purified air;
    c) sending compressed and purified air to a main heat exchanger to produce cooled, compressed and purified air;
    d) sending cooled, compressed and purified air to the column system;
    e) withdrawing nitrogen enriched and oxygen enriched fluids from the column system and warming the nitrogen enriched and oxygen enriched fluids in the main heat exchanger;
    f) withdrawing a liquid purge stream from the column system; and
    g) without having previously warming the liquid purge stream in the main heat exchanger, vaporizing the liquid purge stream by heat exchange with a stream of fluid at a temperature of above 0°C.
  2. Process according to Claim 1, wherein the stream of fluid at a temperature of above 0°C is an air stream.
  3. Process according to Claim 2, wherein the air stream is removed downstream of the compressor.
  4. Process according to Claim 3, wherein the air stream is removed downstream of the purification unit.
  5. Process according to Claim 4, wherein the air stream is removed downstream of a booster compressor.
  6. Process according to Claim 1, wherein the liquid purge stream is vaporized in a heat exchanger separate from the main heat exchanger.
  7. Process according to Claim 6, wherein the amount of air sent to the heat exchanger is controlled to maintain the temperature of the cooled air leaving the heat exchanger above a given temperature.
  8. Cryogenic distillation apparatus for the separation of air using a column system, comprising at least one column further comprising:
    a) a main heat exchanger;
    b) a conduit for sending cooled compressed air to the main heat exchanger, and from the main heat exchanger to the column system;
    c) conduits for sending oxygen enriched and nitrogen enriched streams from the column system to the main heat exchanger;
    d) a purge vaporizer;
    e) a conduit for removing a purge stream from the column system and sending the purge stream to the purge vaporizer;
    f) a conduit for sending compressed and purified air to the purge vaporizer; and
    g) a conduit for sending compressed and purified air from the purge vaporizer to the column system.
  9. Apparatus according to Claim 8, wherein the purge vaporizer is a heat exchanger of the wound type or of the shell and tube type.
  10. Apparatus according to Claim 8, wherein the main heat exchanger is of the plate fin type.
EP06117128A 2005-07-21 2006-07-13 Process and apparatus for the separation of air by cryogenic distillation Withdrawn EP1746374A3 (en)

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WO2012004241A2 (en) 2010-07-05 2012-01-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Apparatus and process for the separation of air by cryogenic distillation
WO2012127148A3 (en) * 2011-03-18 2014-12-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation
EP2614326A4 (en) * 2010-09-09 2018-03-28 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for separation of air by cryogenic distillation

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US5471842A (en) 1994-08-17 1995-12-05 The Boc Group, Inc. Cryogenic rectification method and apparatus

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012004241A2 (en) 2010-07-05 2012-01-12 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Apparatus and process for the separation of air by cryogenic distillation
EP2614326A4 (en) * 2010-09-09 2018-03-28 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and apparatus for separation of air by cryogenic distillation
WO2012127148A3 (en) * 2011-03-18 2014-12-04 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation
AU2012230171B2 (en) * 2011-03-18 2017-03-30 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Device and method for separating air by cryogenic distillation

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CN1904531B (en) 2010-06-23
CN1904531A (en) 2007-01-31
AU2005225027A1 (en) 2007-02-08

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