EP1446622A1 - Procede de distillation d'air avec production d'argon at insallation de distillation d'air correspondante - Google Patents
Procede de distillation d'air avec production d'argon at insallation de distillation d'air correspondanteInfo
- Publication number
- EP1446622A1 EP1446622A1 EP02802662A EP02802662A EP1446622A1 EP 1446622 A1 EP1446622 A1 EP 1446622A1 EP 02802662 A EP02802662 A EP 02802662A EP 02802662 A EP02802662 A EP 02802662A EP 1446622 A1 EP1446622 A1 EP 1446622A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- argon
- fluid
- column
- enriched
- fluids
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
- F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
-
- 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
- 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
-
- 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04733—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction
- F25J3/04739—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction in combination with an auxiliary pure argon 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/58—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being argon or crude argon
Definitions
- the present invention relates to an air distillation process, of the type comprising the steps consisting in:
- the double distillation column comprising a higher pressure column and a pressure column lower
- the first oxygen-enriched fluid is, for example, impure oxygen used to gasify coal to form a fuel feeding a gas turbine.
- An object of the invention is therefore to provide an air distillation process of the aforementioned type which makes it possible to provide relatively large flow rates of first fluid enriched in oxygen and / or of first fluid enriched in nitrogen, and the implementation of which induce reduced costs.
- the subject of the invention is a process of the aforementioned type, characterized in that at least two double distillation columns and at least two argon columns are used which operate in parallel to distill air by forming at least two fluids enriched in argon, in that the fluids enriched in argon are mixed downstream of the two argon columns, and in that at least one element chosen from the group consisting of the compressor, the deoxygenation unit and the desiccation unit is a common element that is used to compress or deoxygenate or to desiccate mixed fluids in common.
- the method can include one or more of the following characteristics, taken alone or according to all technically possible combinations: -all of the mixed fluids are sent to a single common element chosen from the group consisting of by compressor, deoxygenation unit and desiccation unit
- - a common element is the deoxygenation unit where hydrogen is reacted with the mixed fluids to deoxygenate them in a common way by producing water
- - a common element is the desiccation unit where we pass the mixed fluids to draw them together
- the desiccation unit comprises a device for desiccation by adsorption
- the desiccation unit comprises a phase separator
- a common element is the compressor where the mixed fluids are compressed in common
- - the fluids mixed in a common heat exchanger are heated upstream of the compressor
- the fluids drawn down in a common heat exchanger are cooled downstream of the drying unit, - the mixed fluids are heated upstream of the compressor and cooled downstream of the drying unit , the fluids drawn in the same common heat exchanger,
- a dedicated denitrogenation column is used in which the respective deoxygenated and dessicated fluid is distilled.
- the invention further relates to an air distillation installation comprising:
- At least one double distillation column for distilling air by forming at least a first fluid enriched in oxygen and a first fluid enriched in nitrogen, the double distillation column comprising a column at higher pressure and a column at lower pressure,
- At least one argon column for distilling the fluid rich in argon by forming a fluid enriched in argon and a second fluid enriched in oxygen,
- deoxygenation unit for reacting hydrogen with the oxygen contained in the compressed fluid in order to deoxygenate it by producing water
- desiccation unit for passing the deoxygenated fluid therein in order to draw it out
- the installation comprises means for mixing fluids enriched in argon downstream of the two argon columns, and in that at least one element chosen from the group consisting of the compressor, the deoxygenation unit and the desiccation unit is a common element suitable for compressing or deoxygenating or desiccating in a manner common mixed fluids.
- the installation may include one or more of the following characteristics, taken alone or in any technically possible combination:
- the deoxygenation unit which is adapted to react hydrogen with the oxygen contained in the mixed fluids in order to deoxygenate them by producing water
- a common element is the desiccation unit which is adapted to pass the mixed fluids therein in order to desiccate them in a common manner
- the desiccation unit comprises a device for desiccation by adsorption
- the drying unit includes a phase separator
- a common element is the compressor which is adapted to compress the mixed fluids in common
- the installation comprises a common heat exchanger, placed upstream of the compressor, for jointly heating the mixed fluids,
- the installation comprises a common heat exchanger, arranged downstream of the desiccation unit, for jointly cooling the drawn fluids, - the installation comprises the same common heat exchanger for heating the mixed fluids upstream of the compressor and cool the mixed and drawn fluids downstream of the drying unit,
- the installation includes, for each double distillation column and each argon column, a dedicated denitrogenation column for distilling the respective deoxygenated and desiccated fluid therein.
- FIG. 1 is a schematic view of an air distillation installation according to a first embodiment
- FIG. 2 is a schematic partial view of an air distillation installation according to a second embodiment of the invention.
- FIG. 1 schematically illustrates an installation 1 for air distillation which essentially comprises:
- the distillation apparatus 2A essentially comprises:
- a double distillation column 6A which itself comprises an upper pressure column 8A, a lower pressure column 10A and a vaporizer-condenser 12A for connecting the heat exchange relationship of the head of the column 8A with the tank column 10A,
- auxiliary distillation column 14A generally called an argon column, this column 14A being provided with a top condenser-vaporizer 16A, - a second auxiliary column 18A generally called a denitrogenation column, this column being provided with a 20A vaporizer tank and a 22A head vaporizer-condenser, - a 24A air compressor,
- a unit 26A for air purification by adsorption a unit 26A for air purification by adsorption
- the air to be distilled is compressed by the 24A compressor, purified by the unit
- Row liquid" LR oxygen-enriched air
- withdrawn from the tank of column 8A is sub-cooled in the auxiliary exchanger 30A and then divided into two streams. A first of these flows is expanded in a valve 34A and then introduced at a first intermediate level of the column 10A.
- the second stream of the rich liquid LR is sent to the vaporizer-condenser 16A of the argon column 14A where it is vaporized.
- This vaporized rich liquid LR is returned to a second intermediate level of the lower pressure column 10A. This second intermediate level is arranged under the first intermediate level.
- Impure (or residual) nitrogen NR is taken off at the head of the lower pressure column 10A and then warmed up, firstly, through the auxiliary exchanger 30A and, secondly, through the main exchanger 28A.
- Lean liquid LP (approximately pure nitrogen), taken at the head of column 8A, is divided into two streams, the first of which is sub-cooled in the auxiliary exchanger 30A then expanded in a valve 36A and finally introduced into the top of the lower pressure column 10A.
- the second stream of lean liquid LP is sent to the evaporator-condenser 22A at the head of the denitrogenation column 18A where it is vaporized.
- the lean liquid LP vaporized and coming from the vaporizer-condenser 22A is mixed with the impure nitrogen NR upstream of the exchanger 30A.
- Gaseous oxygen OG is withdrawn from the bottom of the lower pressure column 10A and then reheated through the main exchanger 28A at the outlet of which it is distributed by a production line 38A, as a pre- mier distillation product. It may, for example, be pure oxygen, that is to say a purity of between 99 and 99.8%.
- a gas containing mainly oxygen and argon is drawn off via a pipe 39A of a third intermediate level of the lower pressure column 10A.
- This third intermediate level located below the second intermediate level, conventionally corresponds to the argon belly formed by the profile of the argon composition in the gas mixture inside the column 10A.
- the withdrawn gas contains for example about 90% of oxygen, 10% of argon and less than 2000 ppm of nitrogen. It is therefore a gas rich in argon compared to air which contains only about 0.9%.
- This argon-rich gas is introduced into the bottom of the argon column 14A.
- This column 14A ensures the distillation of this gas and produces in the tank a liquid mainly composed of oxygen which is returned, by a pipe 40A, to the third intermediate level of the column at lower pressure 10A.
- Column 14A produces at the head a gas enriched in argon which mainly contains argon, typically 95%, nitrogen, typically 3%, and oxygen, typically 2%.
- the gas enriched in argon coming from the argon column 14A is reheated in the auxiliary exchanger 32A then mixed at a point 41 with the gas enriched in argon coming from the argon column 14B and which has been previously reheated in an auxiliary exchanger 32B.
- the two gases thus mixed then form a single flow which is introduced into the apparatus 3 for deoxygenation and desiccation.
- This device 3 essentially comprises, connected in series: - a compressor 42,
- a desiccation unit 50 comprising a phase separator 51, and a device 52 for desiccation by adsorption.
- the gas mixture is compressed by the compressor 42 and then cooled in the device 44. Hydrogen is then added, by means of a single pipe 54, to the compressed and cooled mixture, before introduction into the deoxygenation unit 46.
- This deoxygenation unit 46 comprises a chemical reactor in the form of a metallic capacity containing a bed of catalyst. The oxygen in the compressed and cooled mixture reacts with the added hydrogen to form water.
- the mixture thus deoxygenated and containing water is then cooled in the device 48 and then sent to the separator 51, which is for example a separator pot, where the liquid water contained in the mixture is eliminated.
- the gas from the separator 51 is then sent to the device 52 for desiccation by adsorption which typically comprises bottles filled with alumina and connected in parallel to the separator 51.
- the single flow of gas from the separator 51 is sent alternately to one or the other of the bottles, the bottle in which the flow does not circulate being in the regeneration phase.
- the single gas flow from unit 50 therefore essentially contains argon and nitrogen, oxygen and water having been eliminated.
- This gas leaves the apparatus 3 and is then divided, at a point 54, into two streams, a first of which is sent to the distillation apparatus 2A and a second which is sent to the distillation apparatus 2B. It will be noted that the flow rate of the stream sent to the device 2A, respectively 2B, is substantially equal to the flow of argon and oxygen withdrawn from column 14A, respectively 14B, via the corresponding enriched gas.
- the gas flow returned to the device 2A is cooled in the heat exchanger 32A then condensed in the vaporizer 20A from the bottom of the denitrogenation column 18A.
- the liquid thus obtained is expanded in a valve 56A and finally introduced at an intermediate level of the column 18A.
- the aforementioned condensation ensures the vaporization, by the vaporizer 20A, of the tank liquid of the 18A denitrogenation column.
- the reflux in the column 18A is ensured by condensation of its overhead gas in the vaporizer-condenser 22A. This condensation is ensured by the vaporization of part of the lean liquid LP, as described above.
- Column 18A produces at the head a gas containing mainly nitrogen which is channeled through a line 57A to be mixed with the liquid vaporized by the vaporizer-condenser 22A, before the mixing of this liquid LP vaporized with impure nitrogen NR.
- a line 58A makes it possible to draw off pure liquid argon from the bottom of the denitrogenation and denitrogenation column 18A.
- this argon contains between 1 and 10 ppm of oxygen and / or nitrogen.
- Lines 58A and 58B are connected to a common production line 60 to mix the two liquids drawn from columns 18A and 18B and recover the argon as the second product of the distillation.
- a common production line 60 to mix the two liquids drawn from columns 18A and 18B and recover the argon as the second product of the distillation.
- the use of two double columns 6A and 6B in parallel makes it possible to produce a high flow rate of gaseous oxygen OG.
- each double distillation column 6A and 6B of a denitrogenation column 18A but especially of a dedicated argon column 14A makes it possible to limit the problems of regulating the operation of each of these columns.
- this regulation proves to be much simpler and less costly than if a single argon column and / or a single denitrogenation column were used in common for the two double distillation columns 6A and 6B.
- controllable valves (not shown) are provided, in particular upstream and downstream of the mixing points 41 and division 54. These valves allow ensure that the flow rates of the fluids supplying the columns 14 and 18 and withdrawn therefrom are such that the operations of the apparatuses 2A and 2B are substantially the same as if they each operated alone.
- the apparatus 3 being common to the two air distillation apparatuses 2A and 2B, the corresponding investments are therefore reduced.
- the method implemented by the installation 1 generates overall investments and relatively reduced regulation costs.
- the auxiliary heat exchangers 32A and 32B are replaced by a common exchanger 32 which belongs to the device 3.
- the exchanger 32 is located downstream of the mixing point 41 and upstream of division point 54.
- This heat exchanger 32 is crossed by, on the one hand, the enriched gases coming from the argon columns 14A and 14B and previously mixed to form a single flow, and, on the other hand, by the single flow of deoxygenated and drawn gas coming from of the desiccation unit 50.
- This second embodiment makes it possible to further reduce the investments required.
- the compressor 42, the cooling devices 44 and 48, the deoxygenation unit 46, the phase separator 51 and the device 52 can be replaced, respectively, by two corresponding elements, the l one is dedicated to device 2A and the other to device 2B.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Drying Of Gases (AREA)
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0114268 | 2001-11-05 | ||
FR0114268A FR2831953B1 (fr) | 2001-11-05 | 2001-11-05 | Procede de distillation d'air avec production d'argon et installation de distillation d'air correspondante |
PCT/FR2002/003449 WO2003040634A1 (fr) | 2001-11-05 | 2002-10-10 | Procede de distillation d'air avec production d'argon at insallation de distillation d'air correspondante |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1446622A1 true EP1446622A1 (fr) | 2004-08-18 |
EP1446622B1 EP1446622B1 (fr) | 2006-07-12 |
Family
ID=8869062
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP02802662A Revoked EP1446622B1 (fr) | 2001-11-05 | 2002-10-10 | Procede de distillation d'air avec production d'argon at insallation de distillation d'air correspondante |
Country Status (7)
Country | Link |
---|---|
US (1) | US20040261453A1 (fr) |
EP (1) | EP1446622B1 (fr) |
AT (1) | ATE333080T1 (fr) |
DE (1) | DE60213121T2 (fr) |
ES (1) | ES2268158T3 (fr) |
FR (1) | FR2831953B1 (fr) |
WO (1) | WO2003040634A1 (fr) |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2003087686A1 (fr) * | 2002-04-12 | 2003-10-23 | Linde Aktiengesellschaft | Procede de production d'argon par separation de l'air a basse temperature |
FR2853407B1 (fr) * | 2003-04-02 | 2012-12-14 | Air Liquide | Procede et installation de fourniture de gaz sous pression |
EP1544559A1 (fr) * | 2003-12-20 | 2005-06-22 | Linde AG | Procédé et dispositif pour la séparation cryogénique d'air |
US9714789B2 (en) * | 2008-09-10 | 2017-07-25 | Praxair Technology, Inc. | Air separation refrigeration supply method |
US8820115B2 (en) * | 2009-12-10 | 2014-09-02 | Praxair Technology, Inc. | Oxygen production method and apparatus |
US20140033762A1 (en) * | 2012-08-03 | 2014-02-06 | Air Products And Chemicals, Inc. | Heavy Hydrocarbon Removal From A Natural Gas Stream |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2990689A (en) * | 1954-11-19 | 1961-07-04 | Independent Engineering Compan | Method and apparatus for the production of argon |
FR2675567A1 (fr) * | 1991-04-16 | 1992-10-23 | Air Liquide | Procede et installation de production d'argon. |
FR2774753B1 (fr) * | 1998-02-06 | 2000-04-28 | Air Liquide | Installation de distillation d'air comprenant plusieurs unites de distillation cryogenique de meme nature |
US6212907B1 (en) * | 2000-02-23 | 2001-04-10 | Praxair Technology, Inc. | Method for operating a cryogenic rectification column |
-
2001
- 2001-11-05 FR FR0114268A patent/FR2831953B1/fr not_active Expired - Fee Related
-
2002
- 2002-10-10 EP EP02802662A patent/EP1446622B1/fr not_active Revoked
- 2002-10-10 US US10/494,697 patent/US20040261453A1/en not_active Abandoned
- 2002-10-10 WO PCT/FR2002/003449 patent/WO2003040634A1/fr not_active Application Discontinuation
- 2002-10-10 DE DE60213121T patent/DE60213121T2/de not_active Revoked
- 2002-10-10 AT AT02802662T patent/ATE333080T1/de not_active IP Right Cessation
- 2002-10-10 ES ES02802662T patent/ES2268158T3/es not_active Expired - Lifetime
Non-Patent Citations (1)
Title |
---|
See references of WO03040634A1 * |
Also Published As
Publication number | Publication date |
---|---|
ATE333080T1 (de) | 2006-08-15 |
FR2831953B1 (fr) | 2004-09-24 |
FR2831953A1 (fr) | 2003-05-09 |
DE60213121D1 (de) | 2006-08-24 |
EP1446622B1 (fr) | 2006-07-12 |
ES2268158T3 (es) | 2007-03-16 |
WO2003040634A1 (fr) | 2003-05-15 |
DE60213121T2 (de) | 2007-02-15 |
US20040261453A1 (en) | 2004-12-30 |
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