WO2012131277A2 - Method for producing a gas from pressurised air by means of cryogenic distillation - Google Patents

Method for producing a gas from pressurised air by means of cryogenic distillation Download PDF

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Publication number
WO2012131277A2
WO2012131277A2 PCT/FR2012/050701 FR2012050701W WO2012131277A2 WO 2012131277 A2 WO2012131277 A2 WO 2012131277A2 FR 2012050701 W FR2012050701 W FR 2012050701W WO 2012131277 A2 WO2012131277 A2 WO 2012131277A2
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WO
WIPO (PCT)
Prior art keywords
temperature
air
exchange line
booster
pressure
Prior art date
Application number
PCT/FR2012/050701
Other languages
French (fr)
Other versions
WO2012131277A3 (en
Inventor
Patrick Le Bot
Original Assignee
L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
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
Application filed by L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude filed Critical L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority to EP12717421.7A priority Critical patent/EP2691718B1/en
Priority to CN201280016757.9A priority patent/CN103827613B/en
Priority to US14/004,427 priority patent/US20140007617A1/en
Priority to ES12717421.7T priority patent/ES2675668T3/en
Publication of WO2012131277A2 publication Critical patent/WO2012131277A2/en
Publication of WO2012131277A3 publication Critical patent/WO2012131277A3/en

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • F25J3/04054—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 air
    • 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched stream
    • 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
    • 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
    • F25J3/04284—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—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.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • 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
    • 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
    • F25J2215/54—Oxygen production with multiple pressure 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel

Definitions

  • the present invention relates to a method and apparatus for producing pressurized air gas by cryogenic distillation.
  • An object of the invention is to propose an alternative for producing process diagrams making it possible to improve the installation costs of the air separation apparatus for oxygen production between 10 and 16 bar, preferably between 14 and 16 bar. 16 bars, so the order of 15 bars.
  • the state of the art for appliances producing oxygen under pressure of the order of 1 5 bar is constituted by "pump" devices, using a main air compressor at a pressure of about 6 bars, and an air booster compressing a portion of the air flow at a pressure of the order of 35-40 bar.
  • this solution is not available for devices of small sizes, for which the combination of a low flow to boost and a very high discharge pressure leads to a real output flow of the booster too small to be technologically feasible .
  • the proposed solution reduces costs for such devices by using a single air compressor at a moderately high discharge pressure, which offers a competitive advantage over the two previous solutions: compressor uniqueness and avoiding an expensive oxygen compressor.
  • US-A-20050126221 discloses an air separation method according to the preamble of claim 1.
  • two series boosters compress the air at intermediate temperatures of the main exchanger, the inlet temperature of the first booster being hotter than the outlet temperature of the second booster.
  • a refrigeration unit is used to lower the inlet temperature of the second booster, thus increasing the complexity of the process.
  • US-A-20060010912 discloses an air separation process in which medium pressure air is supercharged in two cold booster compressors in series.
  • the two boosters must not be coupled to a turbine, because the process turbines only work during a particular step to make liquid. In nominal operation, the process is kept cold by adding cryogenic liquid.
  • all the air is carried at high pressure (substantially higher than the pressure of the medium pressure column) and purified at this pressure, and then divided into at least two parts. Only a fraction of the air, the fraction subsequently liquefying at the cold end of the main exchange line, undergoes a succession of cryogenic compressions so as to bring this flow rate to a pressure sufficient to allow the vaporization of oxygen at the pressure desired.
  • the rest of the air is expanded in at least one turbine at the pressure of the medium pressure column. At least some of the work done by the air expansion is used for cryogenic compression.
  • a method of air separation by cryogenic distillation in an installation comprising a system of columns (31, 33), including a column (31) operating at the highest pressure called the medium pressure in which:
  • At least a portion of the air supercharged in the first booster is cooled in the exchange line, supercharged by means of at least a second booster to a single stage and sucking at a second intermediate temperature of the exchange line and is sent back to the exchange line where it cools, then liquefies, possibly at the cold end of the exchange line and is sent into the column system after expansion;
  • Another part of the purified air under the high pressure is cooled in the exchange line and then at least partially relaxed in at least two turbines having one or more inlet temperatures which is an intermediate temperature or which are intermediate temperatures of the exchange line and then sent to the column system for separation;
  • the work released by the expansion of the air is used at least partially for the cryogenic compression performed by the first and / or the second booster by coupling the first booster to one of the two turbines and the second booster to the other of the two. turbines;
  • the purified air in the purification unit is sent to the outlet temperature of the purification unit at an exchange line, the liquid oxygen pressurized at a pressure less than or equal to 1 6 bars, preferably between 10 and 16 bars, vaporizes in the exchange line, an energy dissipation device is coupled to at least one of the booster pumps, the first temperature differs from the second temperature by at most 10 ° C and the first and second temperatures are between -145 ° C and -165 ° C.
  • the two turbines have equal or different inlet temperatures constituted by the third intermediate temperature and a fourth intermediate temperature of the exchange line;
  • the third temperature is lower than the first temperature.
  • the third temperature differs from the fourth temperature by at most 20 ° C, or even at most 10 ° C;
  • the first temperature is greater than the second temperature
  • the first temperature is less than or equal to the second temperature
  • part of the air is liquefied at high pressure, preferably in the exchange line;
  • the air of at least one of the turbines is sent to the column operating at the highest pressure
  • the system comprises a double air separation column comprising a first column and a second column operating at a lower pressure than the first, the air expanded in the two turbines (17, 27) being sent to the first column;
  • the first temperature is colder than the outlet temperature of the second booster
  • the outlet temperature (s) of the first and / or second booster is / are between -1 10 ° C and -150 ° C;
  • the outlet temperature (s) of the first and / or second booster is / are between -125 ° C and -145 ° C.
  • an apparatus for separating air by cryogenic distillation comprising a system of columns, a column operating at the highest pressure called the medium pressure, a compressor for compressing all the air at a high pressure, at least 3 bar higher at medium pressure, a purification unit connected to the compressor to purify all the air at high pressure, a pipe to send a constituent part between 10% to 35% purified air under high pressure to cool in a line of exchange, a first booster to a single stage, a second booster to a single stage, a pipe to send the constituent part between 10 and 35% of the air to purify at the first booster at a first intermediate temperature of the exchange line, a pipe for sending at least a portion of the supercharged air into the first booster to cool in the exchange line, a pipe to send that cold part to the second booster at a second intermediate temperature of the exchange line, a conduit for sending air from the second booster to the exchange line to cool, a condu ite to send the cooled air from the second booster compressor of the
  • An air flow is compressed in a main compressor 3 to a pressure at least 3 bar above the pressure of the column 31, which is the medium pressure column of a double distillation air separation column cryogenic.
  • the compressed air is purified in a purification unit 7 to form the purified flow 9.
  • the purified flow is sent to the exchange line January 1 without having been cooled and in the exchange line it cools to a first intermediate temperature. At this temperature, the air is divided into a portion 13 and a portion 14.
  • the portion 13 enters a single first booster 15 having a single stage at the first intermediate temperature where it is supercharged.
  • the supercharged air is sent to the exchange line January 1 where it cools again to a second intermediate temperature, lower than the first intermediate temperature. At this second intermediate temperature, at least Part of the superpressed air in the booster 15 or all the air 13 is supercharged in a single second booster 25 having a single stage.
  • the first intermediate temperature differs from the second temperature by at most 10 ° C and the first and second temperatures range from -145 ° C to -165 ° C.
  • the first intermediate temperature may optionally be greater than or equal to the second intermediate temperature.
  • Each of the outlet temperatures of the boosters 15, 25 is between -10 ° C and -150 ° C, preferably between -125 ° C and -145 ° C.
  • the doubly supercharged flow 13 is returned to the exchange line at the pressure required for the vaporization of a flow of oxygen under pressure.
  • the supercharged flow 13 cools to this pressure to the cold end of the exchange line January 1 and condenses.
  • the flow is expanded, and is sent to the medium pressure column 31.
  • the rest of the air 14 is divided into two or three parts. According to a variant, all the air 14 is divided into two parts.
  • a part 19 is sent to a turbine 17 having an inlet temperature which is a third intermediate temperature of the exchange line, then is sent in gaseous form to the medium pressure column 31.
  • Another part 21 is sent to a turbine 27 having an inlet temperature which is a fourth intermediate temperature of the exchange line, greater than the third temperature, then is sent in gaseous form to the medium pressure column 31.
  • the parts 19, 21 are mixed to form a single flow 23.
  • a part 26 of the air at high pressure can possibly continue to cool down to the cold end of the heat exchanger 11 and condense.
  • the outlet of the exchanger it will be expanded in a valve and sent to the column system, for example to the medium pressure column 31.
  • the double column comprises a medium pressure column 31 and a low pressure column 33, thermally interconnected with reflux rates 39, 41 in a known manner.
  • the low pressure column 33 produces a nitrogen flow 43 which is heated in the exchange line 11. It also produces liquid oxygen 35 in vessel which is pressurized to a pressure between 10 and 16 bar and vaporizes in the exchange line to form gaseous oxygen under pressure.
  • part of the flow 13 can continue cooling to the cold end of the exchanger and not be overpressed by the booster 25. This fraction of flow will condense. At the outlet of the exchanger, it will be expanded in a valve and sent to the column system, for example to the medium pressure column 31.
  • the booster 1 5 is driven at least in part by one of the two turbines 17 or 25, and the booster 25 by the other turbine 25 or 17. In each case, there can also be a motor or a generator coupled to the compressor.
  • An energy dissipating device 22, 24, for example a brake, preferably an oil-brake system, will be integrated with at least one of the two turbine / compressor systems 15/17, 25/27.

Abstract

The invention relates to a method for separating air by means of cryogenic distillation in a system of columns, in which two single-stage air superchargers (15, 25) are connected in series and coupled to two turbines (17, 27) which expand the air that was not supercharged. The superchargers supercharge the cooled high-pressure air in an exchange line in which the oxygen from the system of columns is vaporised.

Description

Procédé de production d'un gaz de l'air  Process for producing an air gas
sous pression par distillation cryogénique La présente invention est relative à un procédé et à un appareil de production d'un gaz de l'air sous pression par distillation cryogénique.  The present invention relates to a method and apparatus for producing pressurized air gas by cryogenic distillation.
Un but de l'invention est de proposer une alternative pour réaliser des schémas de procédé permettant d'améliorer les coûts d'installation des appareil de séparation d'air pour une production d'oxygène entre 10 et 16 bars, de préférence entre 14 et 16 bars, donc de l'ordre de 15 bars.  An object of the invention is to propose an alternative for producing process diagrams making it possible to improve the installation costs of the air separation apparatus for oxygen production between 10 and 16 bar, preferably between 14 and 16 bar. 16 bars, so the order of 15 bars.
L'état de l'art industriel, pour des appareils produisant de l'oxygène sous pression de l'ordre de 1 5 bars est constitué par des appareils « à pompe », utilisant un compresseur d'air principal à une pression de l'ordre de 6 bars environ, et un surpresseur d'air comprimant une partie du débit d'air à une pression de l'ordre de 35-40 bars. Mais cette solution n'est pas disponible pour des appareils de petites tailles, pour lesquels la combinaison d'un faible débit à surpresser et d'une pression de refoulement très élevée amène à un débit réel en sortie du surpresseur trop petit pour être technologiquement réalisable.  The state of the art for appliances producing oxygen under pressure of the order of 1 5 bar is constituted by "pump" devices, using a main air compressor at a pressure of about 6 bars, and an air booster compressing a portion of the air flow at a pressure of the order of 35-40 bar. But this solution is not available for devices of small sizes, for which the combination of a low flow to boost and a very high discharge pressure leads to a real output flow of the booster too small to be technologically feasible .
Dès lors, pour les petits appareils, on doit avoir recours à l'utilisation de compresseurs d'oxygène, coûteux.  Therefore, for small appliances, we must resort to the use of expensive oxygen compressors.
La solution proposée permet de réduire les coûts pour de tels appareils, par l'utilisation d'un compresseur d'air unique, à une pression de refoulement modérément élevée, ce qui propose un avantage compétitif par rapport aux deux solutions précédentes : unicité du compresseur et évitement d'un compresseur d'oxygène coûteux.  The proposed solution reduces costs for such devices by using a single air compressor at a moderately high discharge pressure, which offers a competitive advantage over the two previous solutions: compressor uniqueness and avoiding an expensive oxygen compressor.
US-A-20050126221 décrit un procédé de séparation d'air selon le préambule de la revendication 1 . Pour produire de l'oxygène sous pression, deux surpresseurs en série compriment l'air à des températures intermédiaires de l'échangeur principal, la température d'entrée du premier surpresseur étant plus chaude que la température de sortie du deuxième surpresseur. Un groupe frigorifique est utilisé pour abaisser la température d'entrée du deuxième surpresseur, ainsi augmentant la complexité du procédé. US-A-20060010912 décrit un procédé de séparation d'air dans lequel de l'air à la moyenne pression est surpressé dans deux surpresseurs froids en série. US-A-20050126221 discloses an air separation method according to the preamble of claim 1. To produce pressurized oxygen, two series boosters compress the air at intermediate temperatures of the main exchanger, the inlet temperature of the first booster being hotter than the outlet temperature of the second booster. A refrigeration unit is used to lower the inlet temperature of the second booster, thus increasing the complexity of the process. US-A-20060010912 discloses an air separation process in which medium pressure air is supercharged in two cold booster compressors in series.
Les deux surpresseurs ne doivent pas être couplés à une turbine, car les turbines du procédé ne marchent que pendant une marche particulière permettant de fabriquer du liquide. En marche nominale, le procédé est tenu en froid par rajout de liquide cryogénique.  The two boosters must not be coupled to a turbine, because the process turbines only work during a particular step to make liquid. In nominal operation, the process is kept cold by adding cryogenic liquid.
Toutes les pressions sont des pressions absolues.  All pressures are absolute pressures.
Selon l'invention, tout l'air est porté à haute pression (sensiblement plus haute que la pression de la colonne moyenne pression) et épuré à cette pression, puis divisé en au moins deux parties. Seule une fraction de l'air, la fraction se liquéfiant ultérieurement au bout froid de la ligne d'échange principale, subit une succession de compressions cryogéniques de façon à porter ce débit à une pression suffisante pour permettre la vaporisation d'oxygène à la pression souhaitée. Le reste de l'air est détendu dans au moins une turbine à la pression de la colonne moyenne pression. Au moins une partie du travail dégagé par la détente de l'air est utilisée pour la compression cryogénique.  According to the invention, all the air is carried at high pressure (substantially higher than the pressure of the medium pressure column) and purified at this pressure, and then divided into at least two parts. Only a fraction of the air, the fraction subsequently liquefying at the cold end of the main exchange line, undergoes a succession of cryogenic compressions so as to bring this flow rate to a pressure sufficient to allow the vaporization of oxygen at the pressure desired. The rest of the air is expanded in at least one turbine at the pressure of the medium pressure column. At least some of the work done by the air expansion is used for cryogenic compression.
Selon un objet de l'invention, il est prévu un procédé de séparation d'air par distillation cryogénique dans une installation comprenant un système de colonnes (31 , 33), dont une colonne (31 ) opérant à la pression la plus élevée appelée la moyenne pression dans lequel :  According to one object of the invention, there is provided a method of air separation by cryogenic distillation in an installation comprising a system of columns (31, 33), including a column (31) operating at the highest pressure called the medium pressure in which:
- tout l'air est porté à une haute pression, supérieure d'au moins 3 bars à la moyenne pression, épuré à cette pression dans une unité d'épuration et de l'air est envoyé à la température de sortie de l'unité d'épuration à une ligne d'échange ;  - all the air is brought to a high pressure, at least 3 bar higher than the average pressure, purified at this pressure in a purification unit and air is sent to the outlet temperature of the unit purge on a line of exchange;
- tout l'air épuré est refroidi dans la ligne d'échange et une partie constituant entre 10% à 35% de l'air épuré est surpressée au moyen d'au moins un premier surpresseur à un seul étage et aspirant à une première température intermédiaire de la ligne d'échange ;  all the purified air is cooled in the exchange line and a portion constituting between 10% to 35% of the purified air is overpressed by means of at least a first single stage booster and sucking at a first temperature intermediary of the exchange line;
- au moins une partie de l'air surpressé dans le premier surpresseur est refroidie dans la ligne d'échange, surpressée au moyen d'au moins un deuxième surpresseur à un seul étage et aspirant à une deuxième température intermédiaire de la ligne d'échange et est renvoyée dans la ligne d'échange où elle se refroidit, puis se liquéfie, éventuellement au bout froid de la ligne d'échange et est envoyée dans le système de colonnes après détente ; - At least a portion of the air supercharged in the first booster is cooled in the exchange line, supercharged by means of at least a second booster to a single stage and sucking at a second intermediate temperature of the exchange line and is sent back to the exchange line where it cools, then liquefies, possibly at the cold end of the exchange line and is sent into the column system after expansion;
- une autre partie de l'air épuré sous la haute pression, constituant éventuellement entre 65% et 90% de l'air épuré sous la haute pression, est refroidie dans la ligne d'échange puis au moins en partie détendue dans au moins deux turbines ayant une ou des températures d'entrée qui est une température intermédiaire ou qui sont des températures intermédiaires de la ligne d'échange puis envoyée au système de colonnes pour être séparée ;  another part of the purified air under the high pressure, possibly constituting between 65% and 90% of the purified air under the high pressure, is cooled in the exchange line and then at least partially relaxed in at least two turbines having one or more inlet temperatures which is an intermediate temperature or which are intermediate temperatures of the exchange line and then sent to the column system for separation;
- le travail dégagé par la détente de l'air est utilisée au moins partiellement pour la compression cryogénique effectuée par le premier et/ou le deuxième surpresseur en couplant le premier surpresseur à une des deux turbines et le deuxième surpresseur à l'autre des deux turbines ;  the work released by the expansion of the air is used at least partially for the cryogenic compression performed by the first and / or the second booster by coupling the first booster to one of the two turbines and the second booster to the other of the two. turbines;
- de l'oxygène liquide se vaporise dans la ligne d'échange  - liquid oxygen vaporizes in the exchange line
caractérisé en ce que tout l'air épuré dans l'unité d'épuration est envoyé à la température de sortie de l'unité d'épuration à une ligne d'échange, l'oxygène liquide pressurisé à une pression inférieure ou égale à 1 6 bars, de préférence entre 1 0 et 1 6 bars, se vaporise dans la ligne d'échange, un dispositif de dissipation d'énergie est couplé à au moins un des surpresseurs, la première température diffère de la deuxième température d'au plus 10°C et les première et deuxième températures sont comprises entre -145°C et -165°C. characterized in that all the purified air in the purification unit is sent to the outlet temperature of the purification unit at an exchange line, the liquid oxygen pressurized at a pressure less than or equal to 1 6 bars, preferably between 10 and 16 bars, vaporizes in the exchange line, an energy dissipation device is coupled to at least one of the booster pumps, the first temperature differs from the second temperature by at most 10 ° C and the first and second temperatures are between -145 ° C and -165 ° C.
Selon d'autres caractéristiques optionnelles :  According to other optional features:
- les deux turbines ont des températures d'entrée égales ou différentes, constituées par la troisième température intermédiaire et une quatrième température intermédiaire de la ligne d'échange ;  the two turbines have equal or different inlet temperatures constituted by the third intermediate temperature and a fourth intermediate temperature of the exchange line;
- la troisième température est inférieure à la première température.  the third temperature is lower than the first temperature.
- la troisième température diffère de la quatrième température d'au plus 20°C, voire d'au plus 10°C ;  the third temperature differs from the fourth temperature by at most 20 ° C, or even at most 10 ° C;
- la première température est supérieure à la deuxième température ; the first temperature is greater than the second temperature;
- la prem ière température est inférieure ou égale à la deuxième température ; the first temperature is less than or equal to the second temperature;
- on dissipe une partie de l'énergie générée par au moins une des turbines ; - on dissipe une partie de l'énergie au moyen d'un système à frein d'huile relié à la turbine ; - Part of the energy generated by at least one of the turbines is dissipated; - Part of the energy is dissipated by means of an oil brake system connected to the turbine;
- une partie de l'air se liquéfié à la haute pression, de préférence dans la ligne d'échange ;  part of the air is liquefied at high pressure, preferably in the exchange line;
- l'air d'au moins une des turbines est envoyé à la colonne opérant à la pression la plus élevée ;  the air of at least one of the turbines is sent to the column operating at the highest pressure;
- tout l'air surpressé dans le premier surpresseur est envoyé au deuxième surpresseur ;  - all the supercharged air in the first booster is sent to the second booster;
- tout l'air épuré dans l'unité d'épuration est envoyé à la ligne d'échange à la pression de sortie de l'unité d'épuration ;  all the air purified in the purification unit is sent to the exchange line at the outlet pressure of the purification unit;
- le système comprend une double colonne de séparation d'air comprenant une première colonne et une deuxième colonne opérant à plus basse pression que la première, l'air détendu dans les deux turbines (1 7, 27) étant envoyé à la première colonne ;  the system comprises a double air separation column comprising a first column and a second column operating at a lower pressure than the first, the air expanded in the two turbines (17, 27) being sent to the first column;
- la première température est plus froide que la température de sortie du deuxième surpresseur ;  the first temperature is colder than the outlet temperature of the second booster;
- la/les température(s) de sortie du premier et/ou du deuxième surpresseur est/sont entre -1 10°C et -150°C ;  the outlet temperature (s) of the first and / or second booster is / are between -1 10 ° C and -150 ° C;
- la/les tem pératu re(s) de sortie du prem ier et/ou du deuxième surpresseur est/sont entre -125°C et -145°C.  the outlet temperature (s) of the first and / or second booster is / are between -125 ° C and -145 ° C.
Selon un autre objet de l'invention, il est prévu un appareil de séparation d'air par distillation cryogénique comprenant un système de colonnes, dont une colonne opérant à la pression la plus élevée appelée la moyenne pression, un compresseur pour comprimer tout l'air à une haute pression, supérieure d'au moins 3 bars à la moyenne pression, une unité d'épuration reliée au compresseur pour épurer tout l'air à la haute pression, une conduite pour envoyer une partie constituant entre 10% à 35% de l'air épuré sous la haute pression se refroidir dans une ligne d'échange, un premier surpresseur à un seul étage, un deuxième surpresseur à un seul étage, une conduite pour envoyer la partie constituant entre 10 et 35% de l'air épurer au premier surpresseur à une première température intermédiaire de la ligne d'échange, une conduite pour envoyer au moins une partie de l'air surpressé dans le premier surpresseur se refroidir dans la ligne d'échange, une conduite pour envoyer cette partie froidie au deuxième surpresseur à une deuxième température intermédiaire de la ligne d'échange, une conduite pour envoyer de l'air du deuxième surpresseur à la ligne d'échange pour se refroid ir, une condu ite pour envoyer l'air refroidi venant du deuxième surpresseur de la ligne d'échange à un moyen de détente et ensuite dans le système de colonnes, la ligne d'échange étant conçue de sorte que la première température diffère de la deuxième température d'au plus 10°C et les première et deuxième températures étant comprises entre -145°C et -165°C, au moins deux turbines, une conduite pour envoyer une autre partie de l'air épuré sous la haute pression, constituant éventuellement entre 65% et 90% de l'air épuré sous la haute pression, de la ligne d'échange aux deux turbines ayant une ou des températures d'entrée qui est une température intermédiaire ou qui sont des températures intermédiaires de la ligne d'échange, des conduites pour envoyer de l'air des deux turbines au système de colonnes, le premier surpresseur étant couplé à une des deux turbines et le deuxième surpresseur à l'autre des deux turbines, une conduite pour envoyer de l'oxygène liquide, pressurisé à une pression inférieure ou égale à 16 bars, de préférence entre 10 et 16 bars, se vaporise dans la ligne d'échange et un dispositif de dissipation d'énergie couplé à au moins un des surpresseurs. According to another object of the invention, there is provided an apparatus for separating air by cryogenic distillation comprising a system of columns, a column operating at the highest pressure called the medium pressure, a compressor for compressing all the air at a high pressure, at least 3 bar higher at medium pressure, a purification unit connected to the compressor to purify all the air at high pressure, a pipe to send a constituent part between 10% to 35% purified air under high pressure to cool in a line of exchange, a first booster to a single stage, a second booster to a single stage, a pipe to send the constituent part between 10 and 35% of the air to purify at the first booster at a first intermediate temperature of the exchange line, a pipe for sending at least a portion of the supercharged air into the first booster to cool in the exchange line, a pipe to send that cold part to the second booster at a second intermediate temperature of the exchange line, a conduit for sending air from the second booster to the exchange line to cool, a condu ite to send the cooled air from the second booster compressor of the exchange line to a means of expansion and then in the column system, the exchange line being designed so that the first temperature differs from the second temperature by at most 10 ° C and the first and second temperatures being included between -145 ° C and -165 ° C, at least two turbines, a pipe to send another part of the purified air under the high pressure, possibly constituting between 65% and 90% of the purified air under the high pressure , from the exchange line to the two turbines having one or more inlet temperatures which is an intermediate temperature or which are intermediate temperatures of the exchange line, conduits for sending air from the two turbines the column system, the first booster being coupled to one of the two turbines and the second booster to the other of the two turbines, a pipe for sending liquid oxygen, pressurized at a pressure of less than or equal to 16 bars, preferably between 10 and 16 bar, vaporizes in the exchange line and an energy dissipation device coupled to at least one of the boosters.
L'invention sera décrite en plus de détail en se référant à la figure qui illustre un procédé de séparation d'air selon l'invention.  The invention will be described in more detail with reference to the figure which illustrates an air separation method according to the invention.
Un débit d'air est comprimé dans un compresseur principal 3 jusqu'à une pression au moins 3 bars au-dessus de la pression de la colonne 31 , qui est la colonne moyenne pression d'une double colonne de séparation d'air par distillation cryogénique. L'air comprimé est épuré dans une unité d'épuration 7 pour former le débit épuré 9. Le débit épuré est envoyé à la ligne d'échange 1 1 sans avoir été refroidi et dans la ligne d'échange il se refroidit jusqu'à une première température intermédiaire. A cette température, l'air est divisé en une partie 13 et une partie 14. La partie 13 rentre dans un seul premier surpresseur 15 ayant un seu l étage à la première température intermédiaire où elle est surpressée. L'air surpressé est envoyé à la ligne d'échange 1 1 où il se refroidit de nouveau jusqu'à une deuxième température intermédiaire, inférieure à la première température intermédiaire. A cette deuxième température intermédiaire, au moins u ne partie de l 'a ir surpressé dans le surpresseur 15 voire tout l'air 13 est surpressé dans un seul deuxième surpresseur 25 ayant un seul étage. An air flow is compressed in a main compressor 3 to a pressure at least 3 bar above the pressure of the column 31, which is the medium pressure column of a double distillation air separation column cryogenic. The compressed air is purified in a purification unit 7 to form the purified flow 9. The purified flow is sent to the exchange line January 1 without having been cooled and in the exchange line it cools to a first intermediate temperature. At this temperature, the air is divided into a portion 13 and a portion 14. The portion 13 enters a single first booster 15 having a single stage at the first intermediate temperature where it is supercharged. The supercharged air is sent to the exchange line January 1 where it cools again to a second intermediate temperature, lower than the first intermediate temperature. At this second intermediate temperature, at least Part of the superpressed air in the booster 15 or all the air 13 is supercharged in a single second booster 25 having a single stage.
La première température intermédiaire diffère de la deuxième température d'au plus 10°C et les première et deuxième températures sont comprises entre -145°C et -165°C.  The first intermediate temperature differs from the second temperature by at most 10 ° C and the first and second temperatures range from -145 ° C to -165 ° C.
La première température intermédiaire peut éventuellement être supérieure ou égale à la deuxième température intermédiaire.  The first intermediate temperature may optionally be greater than or equal to the second intermediate temperature.
Chacune des températures de sortie des surpresseurs 15, 25 est entre - 1 10°C et -150°C, de préférence entre -125°C et -145°C.  Each of the outlet temperatures of the boosters 15, 25 is between -10 ° C and -150 ° C, preferably between -125 ° C and -145 ° C.
Le débit doublement surpressé 13 est renvoyé à la ligne d'échange à la pression requise pour la vaporisation d'un débit d'oxygène sous pression. Le débit surpressé 13 se refroidit à cette pression jusqu'au bout froid de la ligne d'échange 1 1 et se condense. En sortie d'échangeur, le débit est détendu, et est envoyé à la colonne moyenne pression 31 .  The doubly supercharged flow 13 is returned to the exchange line at the pressure required for the vaporization of a flow of oxygen under pressure. The supercharged flow 13 cools to this pressure to the cold end of the exchange line January 1 and condenses. At the outlet of the exchanger, the flow is expanded, and is sent to the medium pressure column 31.
Le reste de l'air 14 est divisé en deux ou trois parties. Selon une variante, tout l'air 14 est divisé en deux parties. Une partie 19 est envoyée à une turbine 17 ayant une température d'entrée qui est une troisième température intermédiaire de la ligne d'échange, puis est envoyée sous forme gazeuse à la colonne moyenne pression 31 . Une autre partie 21 est envoyée à une turbine 27 ayant une température d'entrée qui est une quatrième température intermédiaire de la ligne d'échange, supérieure à la troisième température, puis est envoyée sous forme gazeuse à la colonne moyenne pression 31 . De préférence les parties 19, 21 sont mélangées pour former un seul débit 23.  The rest of the air 14 is divided into two or three parts. According to a variant, all the air 14 is divided into two parts. A part 19 is sent to a turbine 17 having an inlet temperature which is a third intermediate temperature of the exchange line, then is sent in gaseous form to the medium pressure column 31. Another part 21 is sent to a turbine 27 having an inlet temperature which is a fourth intermediate temperature of the exchange line, greater than the third temperature, then is sent in gaseous form to the medium pressure column 31. Preferably the parts 19, 21 are mixed to form a single flow 23.
Autrement en plus des parties 1 9, 21 , une partie 26 de l'air à la haute pression peut éventuellement poursuivre son refroidissement jusqu'au bout froid de la l igne d 'échange 1 1 et se condenser. En sortie d'échangeur, elle sera détendue dans une vanne et envoyée au système de colonnes, par exemple à la colonne moyenne pression 31 .  Otherwise, in addition to the parts 19, 21, a part 26 of the air at high pressure can possibly continue to cool down to the cold end of the heat exchanger 11 and condense. At the outlet of the exchanger, it will be expanded in a valve and sent to the column system, for example to the medium pressure column 31.
La double colonne comprend une colonne moyenne pression 31 et une colonne basse pression 33, thermiquement reliées entre elles avec des débits de reflux 39, 41 de manière connue.  The double column comprises a medium pressure column 31 and a low pressure column 33, thermally interconnected with reflux rates 39, 41 in a known manner.
La colonne basse pression 33 produit un débit d'azote 43 qui se réchauffe dans la ligne d'échange 1 1 . Elle produit également de l'oxygène liquide 35 en cuve qui est pressurisé à une pression entre 10 et 16 bars et se vaporise dans la ligne d'échange pour former de l'oxygène gazeux sous pression. The low pressure column 33 produces a nitrogen flow 43 which is heated in the exchange line 11. It also produces liquid oxygen 35 in vessel which is pressurized to a pressure between 10 and 16 bar and vaporizes in the exchange line to form gaseous oxygen under pressure.
Il est envisageable de vaporiser de l'oxygène liquide à deux pressions différentes de cette manière ou de vaporiser de l'azote liquide ou de l'argon liquide, éventuellement pressurisé en même temps que l'oxygène liquide.  It is conceivable to vaporize liquid oxygen at two different pressures in this way or vaporize liquid nitrogen or liquid argon, possibly pressurized together with liquid oxygen.
Dans le cas où deux produits se vaporisent dans la ligne d'échange (ou un produit à deux niveaux de pression différentes), une partie du débit 13 pourra poursuivre son refroidissement jusqu'au bout froid de l'échangeur et ne pas être surpressé par le surpresseur 25. Cette fraction de débit se condensera. En sortie d'échangeur, elle sera détendue dans une vanne et envoyée au système de colonnes, par exemple à la colonne moyenne pression 31 .  In the case where two products vaporize in the exchange line (or a product with two different pressure levels), part of the flow 13 can continue cooling to the cold end of the exchanger and not be overpressed by the booster 25. This fraction of flow will condense. At the outlet of the exchanger, it will be expanded in a valve and sent to the column system, for example to the medium pressure column 31.
Le surpresseur 1 5 est entraîné au moins en partie par l'une des deux turbines 17 ou 25, et le surpresseur 25 par l'autre turbine 25 ou 17. Dans chaque cas, il peut également y avoir un moteur ou un générateur couplé au compresseur. Un dispositif de dissipation d'énergie 22, 24, par exemple un frein, préférablement un système à frein d'huile, sera intégré à au mois un des deux systèmes turbine/ compresseur 15/17, 25/27.  The booster 1 5 is driven at least in part by one of the two turbines 17 or 25, and the booster 25 by the other turbine 25 or 17. In each case, there can also be a motor or a generator coupled to the compressor. An energy dissipating device 22, 24, for example a brake, preferably an oil-brake system, will be integrated with at least one of the two turbine / compressor systems 15/17, 25/27.

Claims

Revendications claims
1 . Procédé de séparation d 'air par distillation cryogénique dans une installation comprenant un système de colonnes (31 , 33), dont une colonne (31 ) opérant à la pression la plus élevée appelée la moyenne pression dans lequel : 1. A method of separating air by cryogenic distillation in an installation comprising a system of columns (31, 33), including a column (31) operating at the highest pressure called the medium pressure in which:
- tout l'air est porté à une haute pression, supérieure d'au moins 3 bars à la moyenne pression, épuré à cette pression dans une unité d'épuration (7) et de l'air est envoyé à l a température de sortie de l'unité d'épuration à une ligne d'échange (1 1 ) ;  - all the air is brought to a high pressure, at least 3 bar higher than the average pressure, purified at this pressure in a purification unit (7) and air is sent to the outlet temperature of the purification unit at a exchange line (1 1);
- tout l'air épuré est refroidi dans la ligne d'échange (1 1 ) et une partie constituant entre 1 0% à 35% de l'air épuré est surpressée au moyen d'au moins un premier surpresseur (15) à u n seu l étag e et aspirant à une première température intermédiaire de la ligne d'échange ;  all the purified air is cooled in the exchange line (1 1) and a part constituting between 10% to 35% of the purified air is overpressed by means of at least a first booster (15) at a only the shelf and aspiring at a first intermediate temperature of the exchange line;
- au moins une partie de l'air surpressé dans le premier surpresseur est refroidie dans la ligne d'échange, surpressée au moyen d'au moins un deuxième surpresseur (25) à u n seu l étag e et aspirant à une deuxième température intermédiaire de la l igne d'échange et est renvoyée dans la ligne d'échange où elle se refroidit, puis se liquéfie, éventuellement au bout froid de la ligne d'échange et est envoyée dans le système de colonnes après détente ;  at least a portion of the air blown into the first booster is cooled in the exchange line, supercharged by means of at least one second booster (25) at a single shelf and sucking at a second intermediate temperature of the exchange line and is returned to the exchange line where it cools, then liquefies, possibly at the cold end of the exchange line and is sent into the column system after expansion;
- une autre partie de l'air épuré sous la haute pression, constituant éventuellement entre 65% et 90% de l'air épuré sous la haute pression, est refroidie dans la ligne d'échange puis au moins en partie détendue dans au moins deux turbines (17, 27) ayant une ou des températures d'entrée qui est une température intermédiaire ou qui sont des températures intermédiaires de la ligne d'échange puis envoyée au système de colonnes pour être séparée ;  another part of the purified air under the high pressure, possibly constituting between 65% and 90% of the purified air under the high pressure, is cooled in the exchange line and then at least partially relaxed in at least two turbines (17, 27) having one or more inlet temperatures which is an intermediate temperature or which are intermediate temperatures of the exchange line and then sent to the column system for separation;
- le trava i l d ég ag é pa r l a d éte nte de l'air est utilisée au moins partiellement pour la compression cryogénique effectuée par le premier et/ou le deuxième surpresseur en couplant le premier surpresseur à une des deux turbines et le deuxième surpresseur à l'autre des deux turbines ;  the air-cooled work is used at least partially for the cryogenic compression carried out by the first and / or second booster by coupling the first booster to one of the two turbines and the second booster to the booster. other of the two turbines;
- de l'oxygène liquide se vaporise dans la ligne d'échange  - liquid oxygen vaporizes in the exchange line
caractérisé en ce que tout l'air épuré dans l'unité d'épuration est envoyé à la température de sortie de l'un ité d'épuration à une l igne d'échange, l'oxygène liquide est pressurisé à une pression inférieure ou égale à 1 6 bars, de préférence entre 1 0 et 1 6 bars, pour se vaporiser dans la ligne d'échange, un dispositif de dissipation d'énergie (22, 24) est couplé à au moins un des surpresseurs, la première température diffère de la deuxième température d'au plus 10°C et les première et deuxième températures sont comprises entre -145°C et -165°C. characterized in that all the purified air in the purification unit is sent to the outlet temperature of the purification unit at an exchange temperature, the oxygen liquid is pressurized at a pressure of less than or equal to 16 bar, preferably between 10 and 16 bar, to vaporize in the exchange line, an energy dissipation device (22, 24) is coupled to minus one of the boosters, the first temperature differs from the second temperature by at most 10 ° C and the first and second temperatures are between -145 ° C and -165 ° C.
2. Procédé selon la revendication 1 dans lequel les deux turbines (17, 27) ont des températu res d'entrée différentes, constituées par une troisième température intermédiaire et une quatrième température intermédiaire de la ligne d'échange. 2. Method according to claim 1 wherein the two turbines (17, 27) have different inlet temperatures constituted by a third intermediate temperature and a fourth intermediate temperature of the exchange line.
3. Procédé selon la revendication 2 dans lequel la troisième température est inférieure à la première température. The method of claim 2 wherein the third temperature is lower than the first temperature.
4. P rocéd é sel on l a revend i cation 2 o u 3 d a n s l eq u el la troisième température diffère de la quatrième température d'au plus 20°C, voire d'au plus 10°C. 4. The method of claim 2 wherein the third temperature differs from the fourth temperature by not more than 20 ° C, or even not more than 10 ° C.
5. Procédé selon l'une des revendications précédentes dans lequel la première température est supérieure à la deuxième température. 5. Method according to one of the preceding claims wherein the first temperature is greater than the second temperature.
6. Procédé selon l'une des revendications 1 à 4 dans lequel la première température est inférieure ou égale à la deuxième température. 6. Method according to one of claims 1 to 4 wherein the first temperature is less than or equal to the second temperature.
7. Procédé selon l'une des revendications précédentes dans lequel on dissipe une partie de l'énergie générée par au moins une des turbines. 7. Method according to one of the preceding claims wherein dissipates a portion of the energy generated by at least one of the turbines.
8. Procédé selon la revendication 7 dans lequel on dissipe une partie de l'énergie au moyen d'un système à frein d'huile (22, 24) relié à la turbine. 8. The method of claim 7 wherein dissipating a portion of the energy by means of an oil brake system (22, 24) connected to the turbine.
9. Procédé selon l'une des revendications précédentes dans lequel tout l'air s u rp res sé d a n s l e p re m i e r surpresseur (15) est envoyé au deuxième surpresseur (25). 9. Method according to one of the preceding claims wherein all the air su rp res séle in the second surpresseur (15) is sent to the second booster (25).
10. Procédé selon l'une des revendications précédentes dans lequel tout l'air épuré dans l'un ité d'épuration (7) est envoyé à la ligne d'échange à la pression de sortie de l'unité d'épuration. 10. Process according to one of the preceding claims, in which all the purified air in the purification unit (7) is sent to the exchange line at the outlet pressure of the purification unit.
1 1 . Procédé selon l'une des revendications précédentes dans lequel le système comprend une double colonne de séparation d'air comprenant une première colonne (31 ) et une deuxième colonne (33) opérant à plus basse pression que la première et dans lequel l'air détendu dans les deux turbines (17, 27) est envoyé à la première colonne. 1 1. Method according to one of the preceding claims wherein the system comprises a double air separation column comprising a first column (31) and a second column (33) operating at a lower pressure than the first and in which the air relaxed in both turbines (17, 27) is sent to the first column.
12. Procédé selon l'une des revendications précédentes dans lequel tout l'air destiné à la séparation est envoyé au bout chaud de la ligne d'échange (1 1 ). 12. Method according to one of the preceding claims wherein all the air for separation is sent to the hot end of the exchange line (1 1).
1 3. Procédé selon l 'une des revendications précédentes dans lequel la première température est plus froide que la température de sortie du deuxième surpresseur (25). 3. Method according to one of the preceding claims wherein the first temperature is colder than the outlet temperature of the second booster (25).
14. Procédé selon l'une des revendications précédentes dans lequel la/les température(s) de sortie du prem ier et/ou du deuxième surpresseur (15, 25) est/sont entre -1 10°C et -150°C. 14. Method according to one of the preceding claims wherein the (s) outlet temperature (s) of the first and / or second booster (15, 25) is / are between -1 10 ° C and -150 ° C.
15. Procédé selon la revendication 14 dans lequel la/les température(s) de sortie du premier et/ou du deuxième surpresseur (15, 25) est/sont entre -125°C et -145°C. 15. The method of claim 14 wherein the (s) outlet temperature (s) of the first and / or second booster (15, 25) is / are between -125 ° C and -145 ° C.
PCT/FR2012/050701 2011-03-31 2012-03-30 Method for producing a gas from pressurised air by means of cryogenic distillation WO2012131277A2 (en)

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CN201280016757.9A CN103827613B (en) 2011-03-31 2012-03-30 For producing the method for gas-pressurized by low temperature distillation
US14/004,427 US20140007617A1 (en) 2011-03-31 2012-03-30 Method for producing a pressurised air gas by means of cryogenic distillation
ES12717421.7T ES2675668T3 (en) 2011-03-31 2012-03-30 Production process of a pressurized air gas by cryogenic distillation

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FR2973487A1 (en) 2012-10-05
FR2973487B1 (en) 2018-01-26
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EP2691718A2 (en) 2014-02-05
ES2675668T3 (en) 2018-07-11

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