WO2012136939A2 - Procede et appareil de separation d'air par distillation cryogenique - Google Patents
Procede et appareil de separation d'air par distillation cryogenique Download PDFInfo
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- WO2012136939A2 WO2012136939A2 PCT/FR2012/050742 FR2012050742W WO2012136939A2 WO 2012136939 A2 WO2012136939 A2 WO 2012136939A2 FR 2012050742 W FR2012050742 W FR 2012050742W WO 2012136939 A2 WO2012136939 A2 WO 2012136939A2
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- column
- oxygen
- liquid
- air
- vaporizer
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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
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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
- F25J3/04006—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
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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- 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
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Definitions
- the present invention relates to a method and apparatus for air separation by cryogenic distillation.
- the invention particularly provides a method of producing pure oxygen using a dual vaporizer air separation unit.
- the method according to the invention allows the production of pure liquid oxygen (containing at least 99 mol%, or even at least 99.6 mol% of oxygen) on an apparatus producing impure oxygen gas (less than 97 mol%, or even 96 mol%) at low pressure, for example in the context of an apparatus for oxycombustion.
- the oxygen-generating air separation (ASU) schemes for an oxy-fuel coal plant generally comprise two (or three) vaporizers located between the medium pressure column (MP column) and the low pressure column. (BP column).
- MP column medium pressure column
- BP column low pressure column
- the purity of the oxygen produced by this type of plant is typically between 95 and 97 mol%. O 2 .
- the vaporisation of the oxygen is ensured in a dedicated vaporizer.
- the vaporization frigories of liquid oxygen are used to condense gaseous air.
- a method of this kind is known from US-A-4936099 and EP-A-0547946.
- the pressure of the column MP is so low that it is not possible to use one of the gaseous flows entering or leaving the column MP or the column LP to condense in the bottom vaporizer of the column of Additional pure LOX (their condensing temperature is too low).
- the invention described here proposes to use as condensing fluid, a fraction of the gaseous air leaving the exchange line and which will subsequently enter the dedicated exchanger ensuring the vaporization of pure oxygen production. (which is referred to as HP air).
- HP air a fraction of the gaseous air leaving the exchange line and which will subsequently enter the dedicated exchanger ensuring the vaporization of pure oxygen production.
- This air flow is compressed upstream of the main exchange line by the blower (BAC) of the unit.
- the pressure of this flow rate is of the order of 4.5 bar abs, higher than that of the MP column, and such that its bubble temperature is higher than the equilibrium temperature of the pure liquid oxygen.
- the temperature difference between the air flow rate considered and the pure oxygen is of the order of 2 to 3 ° C, a fairly high value, which makes it possible to install a small vaporizer.
- the production of pure liquid oxygen is free in terms of separation energy and does not play on the separation energy of the production of impure oxygen gas. You just have to pay for the liquefaction energy.
- the additional refrigeration can be carried out by a liquefaction system independent of the ASU.
- the invention provides a method for producing pure oxygen (Purity> 99.6%) on a dual vaporizer air separation unit, typically used for oxy-fuel combustion, the majority of which is oxygen produced. at a purity of the order of 95 to 97%. Indeed, on this type of process, apart from HP air, there is no fluid available at sufficiently high condensation temperature to achieve the reboiling of the pure oxygen column.
- Air separation units are frequently found in a single vaporizer, where a small column producing ultra-pure oxygen is added to the bottom of the LP column.
- the pressure of the MP column is of the order of 5 to 6 bar and the reboiling of the ultra pure LOX column is provided by a fraction of the flow of gaseous air supplying the MP column.
- EP-A-0793069 discloses a method according to the preamble of claim 1.
- air at a first pressure is used to vaporize oxygen in a vaporizer and air at a second pressure, higher than the first one, is used for reboiling a column of pure oxygen.
- US-A-5916262 discloses a dual purity oxygen production process using an oxygen scrubber heated in tank by air. Pump-pressurized liquid oxygen is also vaporized in the main exchange line by heat exchange with pressurized air.
- the present invention proposes to produce pure oxygen in a double vaporizer scheme by installing an additional pure oxygen column, the pressure of which is equal to the pressure of the LP column.
- a method for separating air by cryogenic distillation in a separation unit comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a reboiler vessel and an intermediate reboiler, and a pure oxygen column in which
- purified air gas is sent and then cooled to a first pressure in an exchange line at the medium pressure column, ii) an oxygen-enriched liquid and a nitrogen-enriched liquid are sent from the medium-pressure column to the low-pressure column,
- a second flow of oxygen-rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%. oxygen
- a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
- vessel liquid is withdrawn from the pure oxygen column as product and superpressed air is supplied to the second vaporizer pressure to vaporize the first oxygen-rich liquid flow.
- the first flow of oxygen-rich liquid is pressurized upstream of the vaporizer.
- the first flow of oxygen-rich liquid and the second flow of oxygen-rich liquid have the same purity.
- air pressure is divided at the second pressure in two parts, a first portion of superpressed air is sent at the second pressure to the reboiler of the pure oxygen column and a second part of compressed air is sent to the second pressure to the vaporizer.
- air is sent at the first pressure to the bottom reboiler of the low pressure column to heat it. all the air is divided into a flow at the first pressure and a flow at the second pressure upstream of the exchange line.
- the first flow of oxygen-rich liquid is less oxygen-rich than the second oxygen-rich flow of oxygen.
- the first flow of oxygen-rich liquid is vaporized partially in the vaporizer, the formed liquid constituting the second flow of oxygen-rich liquid.
- the compressed air flow at the second pressure first heats the bottom reboiler of the pure oxygen column and then the vaporizer.
- Air at the first pressure cools in the exchange line and is sent in gaseous form to the medium pressure column.
- a cryogenic liquid from an auxiliary source is sent to the double column.
- medium pressure and low pressure simply mean that the medium pressure column operates at a higher pressure than the low pressure column. These terms are common in the art and clear to those skilled in the art.
- a cryogenic distillation air separation apparatus comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a bottom reboiler and a reboiler intermediate, and a pure oxygen column, an exchange line, a vaporizer, means for sending purified air gas and then cooled at a first pressure of the exchange line to the medium pressure column, means for supplying an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 mol% of oxygen in the tank of the low pressure column, means for sending a first flow of oxygen-rich liquid to the vaporizer, a pipe for sending the gaseous oxygen thus formed to the exchange line, means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a
- a booster a line for sending a superpressed air flow at a second pressure higher than the first pressure to the reboiler of the pure oxygen column, lines for withdrawing a nitrogen-rich gas at the top of the medium pressure column , to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a nitrogen-rich gas or air to the bottom column reboiler pressure and to send the liquid which condenses thereon to the medium pressure column characterized in that it comprises a pipe for drawing liquid from the column of the pure oxygen column as product and means for sending compressed air at the second pressure of the booster to the vaporizer.
- the apparatus comprises:
- the means for sending the supercharged air from the booster to the vaporizer are connected to the bottom reboiler of the pure oxygen column so that the air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
- the means for sending a second flow of oxygen-rich liquid at the top of the pure oxygen column are constituted by the conduit for sending a bottom liquid from the low pressure column to the top of the pure oxygen column.
- the vaporizer is not part of a distillation or exhaustion column.
- a method for separating air by cryogenic distillation in a separation unit comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a reboiler vessel and an intermediate reboiler and a column of pure oxygen in which
- a second flow of oxygen rich liquid is fed to the top of the pure oxygen column, having a bottom reboiler, where it purifies to form a bottom liquid containing at least 98 mol%,
- a nitrogen rich gas is withdrawn at the top of the medium pressure column, it is sent to the intermediate reboiler of the low pressure column and the condensed gas is sent to the head of the medium pressure column, and
- a nitrogen-rich gas or air is sent to the bottom reboiler of the low-pressure column and the liquid which condenses therein is sent to the medium-pressure column, characterized in that the liquid from the bottom of the vessel is withdrawn. pure oxygen column as product and in that the first flow of oxygen-rich liquid is less oxygen-rich than the second flow of oxygen-rich liquid.
- the first flow of oxygen-rich liquid is pressurized upstream of the vaporizer.
- a second superpressed air flow is sent at the second pressure to the vaporizer.
- the first flow of oxygen-rich liquid partially vaporizes in the vaporizer, the formed liquid constituting the second flow of oxygen-rich liquid.
- the supercharged air flow first heats the vessel reboiler of the pure oxygen column and then the vaporizer.
- a cryogenic liquid from an auxiliary source is sent to the double column.
- the medium pressure column operates at between 2.5 and 4.5 bar abs.
- a cryogenic distillation air separation apparatus comprising a medium pressure column and a low pressure column, thermally connected to each other, the low pressure column comprising a bottom reboiler and a reboiler intermediate and a pure oxygen column, an exchange line, a vaporizer, means for sending purified air gas and then cooled to a first pressure of the exchange line to the medium pressure column, means for sending an oxygen enriched liquid and a nitrogen enriched liquid from the medium pressure column to the low pressure column, means for withdrawing a nitrogen rich gas from the low pressure column, means for withdrawing an oxygen rich liquid containing at most 97 % mol.
- a booster a line for sending a superpressed air flow at a second pressure higher than the first tank reboiler pressure of the pure oxygen column, lines for drawing a nitrogen-rich gas at the top of the the medium pressure column, to send it to the intermediate reboiler of the low pressure column and to send the condensed gas to the head of the medium pressure column and lines to send a nitrogen-rich gas or air to the reboiler of the low pressure column and to send the liquid that is condensed in the medium pressure column characterized in that it comprises a pipe for withdrawing liquid from the column of the pure oxygen column as product and a pipe for sending a liquid (53) of the vaporizer (51) at the top pure oxygen column (49).
- the apparatus may also include a conduit for supplying a bottom liquid from the low pressure column to the top of the pure oxygen column.
- the means for supplying the blower pressurized air to the vaporizer can be connected to the bottom reboiler of the pure oxygen column so that the air for the vaporizer passes through the bottom reboiler of the pure oxygen column.
- the means for sending a second flow of oxygen-rich liquid to the top of the pure oxygen column may be constituted by the conduit for sending a bottom liquid from the low pressure column to the top of the pure oxygen column.
- the apparatus may comprise means for dividing the supercharged air at the second pressure into two parts, the means for supplying superpressed air at the second pressure of the booster to the vaporizer and the duct for sending a pressurized air flow to the booster.
- the second tank reboiler pressure of the pure oxygen column being connected so that a portion of pressurized air is sent to the bottom reboiler of the pure oxygen column and another portion of pressurized air is sent to the vaporizer.
- the apparatus may include means for supplying a cryogenic liquid to the low pressure column of an external source.
- the apparatus may include a conduit for supplying the pressurized air flow from the reboiler of the pure oxygen column to the vaporizer and a conduit for supplying the air from the vaporizer to the medium pressure column and / or the lower column. pressure.
- the apparatus comprises a pipe for sending the supercharged air flow of the tank reboiler of the pure oxygen column directly to the medium pressure column and / or the low pressure column.
- the main innovative feature of the invention presented here is that the reboiling of the pure oxygen column is achieved by a fraction of the flow of gaseous air leaving the main exchange line, compressed by a booster at the pressure required for the vaporization of oxygen in the vaporizer (HP air). This fraction of air HP condenses partially or totally in the condenser of the pure oxygen column.
- the partially condensed compressed air flow possibly after having separated the condensed part (which is then sent into the MP column), is then sent into the product vaporizer where it finishes to condense completely.
- the partial condensation of the supercharged air allows, with a quasi-nominal flow of GOX production and the same pressure, to operate the vaporizer in pure column vat, then that of the vaporizer produced.
- the reboiling of the pure liquid oxygen column is therefore free compared to the energy required to vaporize the production.
- the pressure of this air flow is greater than the pressure of the MP column (typically of the order of 4.5 bar abs against 3.2 bar abs.).
- Part of the impure liquid is removed from the vaporizer produced (at the same level and instead of the purge of the evaporator), and the pure liquid is sent to the column of oxygen which is a distillation column which is substantially distilled off. same pressure as the vaporizer produces ..
- the impure gas reflux from the pure oxygen column is mixed with the gas stream from the product vaporizer, the two flows constituting the nominal output flow of the impure GOX.
- the pure liquid is taken from the vat of the pure oxygen column. It also serves as a purge of deconcentration of the entire device.
- the addition of frigories can be provided by an independent liquefier, for example by producing liquid nitrogen, from pure nitrogen (from a minaret), which would then be added in liquid form in the apparatus. If there is no pure nitrogen production, it is possible to liquefy residual nitrogen in an independent liquefier.
- FIG. 1 illustrate air separation methods according to the invention.
- the air is separated in an ASU comprising a double air separation column, comprising a medium pressure column 23 and a low pressure column 25. Frigories for the separation are provided by expansion of medium pressure nitrogen. in a turbine 47.
- the apparatus comprises a column of pure liquid oxygen 49, a pump 57, a vaporizer 51 and an exchange line 63.
- Air 1 is pressurized by a compressor 3 at a pressure between 2.5 and 4.5 bar abs.
- the air is then purified in a purification unit 5 by adsorption.
- the air fresh 7 is divided into two parts.
- Part 9 is overpressed in a booster 13 to a pressure of between 4 and 20 bar abs and then cooled in the exchange line 63 to the cold end.
- the air 9 is divided into two fractions 15, 17.
- a fraction 1 5 is sent to the vaporizer 51 where it serves to partially vaporize liquid oxygen comprising at most 97 mol%. oxygen, to produce gaseous oxygen 59 which is heated in the exchange line 63. This gas 59 is sent to an oxyfuel unit.
- An oxygen-rich liquid 53 is withdrawn from the vaporizer 51 as a purge.
- the air is condensed.
- the other fraction of the air 17 is sent to the reboiler 61 of the pure oxygen column 49.
- This column comprises the reboiler vessel and means for exchanging heat and material above the reboiler.
- Liquid oxygen 65 comprising at most 97 mol%. oxygen is sent to the top of the column 49 and is enriched to form the liquid product 71 withdrawn into the tank and containing at least 98 mol%. oxygen.
- the gaseous oxygen at the top of the column 49 is sent to the bottom of the low pressure column 25.
- the condensed air 17 mixes with the condensed air coming from the vaporizer 51 and, after expansion in a valve 21, is sent to the MP 23 column, which operates at between 2.5 and 4.5 bar abs.
- Another part 1 1 of the air is cooled in the exchange line 63, is sent to the bottom reboiler 35 of the column BP 25, condenses at least partially and is sent to the bottom of the column MP 23, below the point of arrival of liquid air 19.
- Oxygen-enriched liquid 27 is withdrawn from the tank of the MP column
- Low pressure nitrogen 39 is withdrawn at the top of the LP column, reheated in the subcooler 33 and reheated in the exchange line 63.
- Medium pressure nitrogen 41 is divided in two to form a part
- the portion 43 serves to heat the intermediate reboiler 37 of the low pressure column 25.
- the portion 45 is heated in the exchange line 63, is expanded in the turbine 47 and is returned to the line of exchange 63.
- Liquid oxygen is withdrawn from the tank of the LP column and divided in two.
- a portion 55 is pressurized in the pump 57 upstream of the vaporizer 51 and the remainder 65 is sent to the top of the pure oxygen column 49 without having been pressurized.
- the head of the pure oxygen column 49 is therefore at the same pressure as the tank of the low pressure column 25. All or part of the purge liquid 53 can also feed the head of the column 49.
- a flow of cryogenic liquid 69 for example liquid nitrogen, is sent to the top of the LP column to keep the process cold.
- the method of FIG. 1 bis differs from that of FIG. 1 in that the column 49 is fed exclusively at the top by the purge 53 of the vaporizer 51, following a step of expansion in a valve.
- the reboiler 61 of the column 49 is still heated by the pressurized air 17, the air thus condensed being mixed with the pressurized air 15 which was used to heat the vaporizer 51. It is also possible to feed the column with purge liquid 53 and liquid oxygen 65 from the bottom of the low pressure column 25.
- the method of Figure 2 differs from that of Figure 1 in that the air flow 9 is first sent to the vessel vaporizer 61 of the pure oxygen column 49 and then to the vaporizer 51 where it condenses.
- the air thus formed is expanded in the valve 21 and sent to the medium pressure column 23.
- the air fraction 1 1 cools in the exchange line January 1 and is sent to the tank of the medium pressure column 23 without have been relaxed or compressed downstream of the compressor 3.
- Intermediate reboiler 37 is still heated by medium pressure nitrogen 43 but another part of medium pressure nitrogen 73 is compressed in a cold booster 71 from a cryogenic temperature and sent
- the condensed nitrogen is expanded in a valve 36 and sent to the top of the MP column 23.
- the vessel oxygen 55 of the low pressure column is fully pressurized in the pump 57 sent to the vaporizer 51 where it partially vaporizes.
- the vaporized gas is the gaseous oxygen product 59 containing less than 97 mol%. oxygen.
- the non-vaporized liquid 53 feeds the top of the column 49.
- the gaseous oxygen 67 at the top of the column 49 is mixed with the oxygen gas 59.
- the liquid oxygen 71 constitutes the liquid product. In this case, the pure oxygen column 49 does not operate at the same pressure as the BP column 25.
- the process of Figure 1 or 1a may use nitrogen to heat the bottom reboiler 35 and the method of Figure 2 may use air to heat the bottom reboiler 35.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
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- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US14/110,356 US9696087B2 (en) | 2011-04-08 | 2012-04-05 | Method and apparatus for separating air by cryogenic distillation |
EP12720248.9A EP2694898B1 (fr) | 2011-04-08 | 2012-04-05 | Procédé et appareil de séparation d'air par distillation cryogénique |
AU2012238460A AU2012238460B2 (en) | 2011-04-08 | 2012-04-05 | Method and apparatus for separating air by cryogenic distillation |
CA2830826A CA2830826C (fr) | 2011-04-08 | 2012-04-05 | Procede et appareil de separation d'air par distillation cryogenique |
CN201280027982.2A CN103842753B (zh) | 2011-04-08 | 2012-04-05 | 用于通过低温蒸馏分离空气的方法和设备 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1153070A FR2973865B1 (fr) | 2011-04-08 | 2011-04-08 | Procede et appareil de separation d'air par distillation cryogenique |
FR1153070 | 2011-04-08 |
Publications (2)
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WO2012136939A2 true WO2012136939A2 (fr) | 2012-10-11 |
WO2012136939A3 WO2012136939A3 (fr) | 2015-01-22 |
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PCT/FR2012/050742 WO2012136939A2 (fr) | 2011-04-08 | 2012-04-05 | Procede et appareil de separation d'air par distillation cryogenique |
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Country | Link |
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US (1) | US9696087B2 (fr) |
EP (1) | EP2694898B1 (fr) |
CN (1) | CN103842753B (fr) |
AU (1) | AU2012238460B2 (fr) |
CA (1) | CA2830826C (fr) |
FR (1) | FR2973865B1 (fr) |
WO (1) | WO2012136939A2 (fr) |
Families Citing this family (5)
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CN104251599A (zh) * | 2014-07-12 | 2014-12-31 | 孙竟成 | 超低压空分设备工艺流程 |
FR3044747B1 (fr) * | 2015-12-07 | 2019-12-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede de liquefaction de gaz naturel et d'azote |
WO2018005540A1 (fr) | 2016-06-27 | 2018-01-04 | Texas Tech Universtiy System | Appareil et procédé pour séparer l'oxygène liquide de l'air liquéfié |
CN111406191B (zh) * | 2017-12-25 | 2021-12-21 | 乔治洛德方法研究和开发液化空气有限公司 | 具有反向主热交换器的单封装空气分离设备 |
CN112781321B (zh) * | 2020-12-31 | 2022-07-12 | 乔治洛德方法研究和开发液化空气有限公司 | 一种具有氮液化器的空气分离装置和方法 |
Citations (4)
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US4936099A (en) | 1989-05-19 | 1990-06-26 | Air Products And Chemicals, Inc. | Air separation process for the production of oxygen-rich and nitrogen-rich products |
EP0547946A1 (fr) | 1991-12-18 | 1993-06-23 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et installation de production d'oxygène impur |
EP0793069A1 (fr) | 1996-03-01 | 1997-09-03 | Air Products And Chemicals, Inc. | Générateur d'oxygène à deux degrés de pureté avec compresseur pour le rebouilleur |
US5916262A (en) | 1998-09-08 | 1999-06-29 | Praxair Technology, Inc. | Cryogenic rectification system for producing low purity oxygen and high purity oxygen |
Family Cites Families (7)
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US5546767A (en) * | 1995-09-29 | 1996-08-20 | Praxair Technology, Inc. | Cryogenic rectification system for producing dual purity oxygen |
US5669236A (en) * | 1996-08-05 | 1997-09-23 | Praxair Technology, Inc. | Cryogenic rectification system for producing low purity oxygen and high purity oxygen |
EP0908689A3 (fr) * | 1997-08-20 | 1999-06-23 | AIR LIQUIDE Japan, Ltd. | Procédé et dispositif de distillation d'air |
US5839296A (en) * | 1997-09-09 | 1998-11-24 | Praxair Technology, Inc. | High pressure, improved efficiency cryogenic rectification system for low purity oxygen production |
FR2787561A1 (fr) * | 1998-12-22 | 2000-06-23 | Air Liquide | Procede de separation d'air par distillation cryogenique |
FR2930330B1 (fr) * | 2008-04-22 | 2013-09-13 | Air Liquide | Procede et appareil de separation d'air par distillation cryogenique |
FR2943772A1 (fr) * | 2009-03-27 | 2010-10-01 | Air Liquide | Appareil et procede de separation d'air par distillation cryogenique |
-
2011
- 2011-04-08 FR FR1153070A patent/FR2973865B1/fr not_active Expired - Fee Related
-
2012
- 2012-04-05 CN CN201280027982.2A patent/CN103842753B/zh not_active Expired - Fee Related
- 2012-04-05 AU AU2012238460A patent/AU2012238460B2/en not_active Ceased
- 2012-04-05 US US14/110,356 patent/US9696087B2/en not_active Expired - Fee Related
- 2012-04-05 WO PCT/FR2012/050742 patent/WO2012136939A2/fr active Application Filing
- 2012-04-05 CA CA2830826A patent/CA2830826C/fr not_active Expired - Fee Related
- 2012-04-05 EP EP12720248.9A patent/EP2694898B1/fr active Active
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4936099A (en) | 1989-05-19 | 1990-06-26 | Air Products And Chemicals, Inc. | Air separation process for the production of oxygen-rich and nitrogen-rich products |
EP0547946A1 (fr) | 1991-12-18 | 1993-06-23 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procédé et installation de production d'oxygène impur |
EP0793069A1 (fr) | 1996-03-01 | 1997-09-03 | Air Products And Chemicals, Inc. | Générateur d'oxygène à deux degrés de pureté avec compresseur pour le rebouilleur |
US5916262A (en) | 1998-09-08 | 1999-06-29 | Praxair Technology, Inc. | Cryogenic rectification system for producing low purity oxygen and high purity oxygen |
Also Published As
Publication number | Publication date |
---|---|
CN103842753A (zh) | 2014-06-04 |
AU2012238460A1 (en) | 2013-10-31 |
FR2973865A1 (fr) | 2012-10-12 |
CA2830826A1 (fr) | 2012-10-11 |
AU2012238460B2 (en) | 2016-12-22 |
US9696087B2 (en) | 2017-07-04 |
FR2973865B1 (fr) | 2015-11-06 |
CN103842753B (zh) | 2016-12-07 |
EP2694898A2 (fr) | 2014-02-12 |
CA2830826C (fr) | 2018-10-16 |
WO2012136939A3 (fr) | 2015-01-22 |
EP2694898B1 (fr) | 2020-06-17 |
US20140053601A1 (en) | 2014-02-27 |
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