EP0718576B1 - Procédé de séparation d'un mélange gazeux par distillation cryogénique - Google Patents
Procédé de séparation d'un mélange gazeux par distillation cryogénique Download PDFInfo
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- EP0718576B1 EP0718576B1 EP95402924A EP95402924A EP0718576B1 EP 0718576 B1 EP0718576 B1 EP 0718576B1 EP 95402924 A EP95402924 A EP 95402924A EP 95402924 A EP95402924 A EP 95402924A EP 0718576 B1 EP0718576 B1 EP 0718576B1
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- refrigerant
- gas mixture
- flow
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- pressure
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
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- 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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04339—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air
- F25J3/04345—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of air and comprising a gas work expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
Definitions
- Climatic conditions are important in the design air separation devices and, more generally, in devices cryogenic. More particularly, the water for cooling the refrigerants of the various stages of compression of the air compressor can vary depending on the climate and even between day and night, so important in some countries so that one can save in these country temperature fluctuations on the water of the order of 15 ° C.
- the refrigeration unit has the disadvantage of being of a expensive investment and to use at least one rotating machine, which is unreliable and energy consuming.
- US-A-4,375,367 describes a system in which an air flow at distiller is cooled before being purified by recycling the air produced by the purification system.
- a refrigeration unit is essential in this case.
- EP-A-0.624.765A discloses a system which makes it possible to substitute the refrigeration unit by a heat exchange system with a flow of pressurized fluid from the air separation plant. Usage of a cycle fluid to cool the air upstream of the purification system is not described.
- This patent application also does not disclose a installation in which the air is precooled in an auxiliary exchanger with only one other fluid.
- JP-A-54103777 describes the use of a nitrogen flow coming from a distillation column to cool the air to be purified.
- EP-A-0.505.812 discloses that an air flow to be purified can be cooled with a purified air flow, before the expansion of the latter.
- the subject of the invention is a method as described above, characterized in that liquid is produced as the final product and at least part of the refrigerant is expanded in a expansion before it exchanges heat with the non-gas mixture refined.
- the proposed solution applies to all distillation apparatus a gaseous mixture containing oxygen and nitrogen and which, for this, use a refrigeration cycle, for example a gas or nitrogen mixture. It is well suited to liquid production devices.
- the invention applies in particular to small appliances for production of liquid by air distillation using a nitrogen cycle capable to supply the air with the necessary extra refrigeration for its refrigeration up to its purification temperature.
- the invention may consist in installing at the outlet of the final refrigerant from the air compressor an auxiliary exchanger allowing, for example, heat exchange between compressed air with a fraction of cycle nitrogen taken at an intermediate level of a main exchanger. Compressed air is thus cooled by the cycle nitrogen which is heated in this exchanger auxiliary, then remixed with the rest of the cycle nitrogen which continued to heating in the main exchanger.
- the invention also relates to a separation installation of a gaseous mixture containing nitrogen and oxygen by distillation cryogenic comprising a compressor, a purification system, a main exchanger, at least one distillation column, means constituting a refrigeration system and an auxiliary exchanger which puts the gas mixture compressed by the compressor in exchange relationship thermal with a refrigerant coming either from the column or from the feed downstream of the purification system, characterized in that it includes means for withdrawing a liquid product and a machine for expansion to relax at least part of the refrigerant upstream of the auxiliary exchanger.
- an air flow is compressed to 6 X 10 5 Pa by a compressor 1 and cooled to 40 ° C in a water cooler 3. Then the flow enters the auxiliary exchanger 5 where it cools down to 25 ° C by heat exchange with a nitrogen flow rate of 6 ⁇ 10 5 Pa.
- Separator pots (not shown) at the outlet of the refrigerant 3 and of the exchanger 5 make it possible to remove the condensed water from the treated air after cooling.
- the air is cooled in the main exchanger 9 near its dew point, then sent to a double tank conventional column 11 in which the air is separated into liquid oxygen, residual nitrogen at the pressure of the low pressure column (1.3 ⁇ 10 5 Pa) and gaseous and liquid nitrogen substantially pure at the pressure of the medium pressure column (6 ⁇ 10 5 Pa).
- the flow rate of substantially pure nitrogen gas is heated in the main exchanger 9 to a temperature of 22 ° C., from which the first flow rate 13A of pure nitrogen is drawn off by the draw-off valve 15 before passing into l auxiliary exchanger 5 where it cools the supply air to 25 ° C.
- the nitrogen of cycle 13A is thus heated to 37 ° C.
- a second flow of pure gaseous nitrogen 13B continues to heat up in the main exchanger 9 up to 35 ° C. and joins the first flow 13A after it has passed through the auxiliary exchanger 5.
- the combined flows are recompressed to 42 bar in the compressor 21 and cooled in the main exchanger 9.
- a third flow 13C of recompressed pure nitrogen is expanded in the turbine 23 of 42X 10 5 Pa up to 6 X 10 5 Pa and recycled with the nitrogen gas withdrawn from the column at 6X 10 5 Pa.
- the compressor 21 is coupled to the turbine 23.
- the residual nitrogen heats up in the main exchanger 9, is further heated in the electric heater 8 and is used to regenerate one of the beds of adsorbent he 7.
- the water temperature can reach 20-22 ° C. Under these conditions, the compressed air will come out of the final refrigerant of the compressor 1 at a temperature close to 25 ° C and valve 15 will be closed.
- the water temperature can reach 30-32 ° C and the air leaving the final refrigerant of compressor 1 will be at a temperature close to 40 ° C.
- Cycle nitrogen 13A will then be sent at a sufficient rate by valve 15 opens sufficiently for the temperature of the outlet air of the auxiliary exchanger 5 is close to 25 ° C.
- the system has no refrigeration units, the entire cooling capacity being provided by the nitrogen cycle.
- the system in Figure 2 differs from that in Figure 1 in that the nitrogen cycle is replaced by an air cycle (the gas mixture at distill).
- the equipment remains essentially the same.
- the air flow is compressed in the compressor 17 to 30 X 10 5 Pa, cooled in the exchanger 19 and recompressed by the compressor 21 to 42 X 10 5 Pa. Then, the air cools in the main exchanger 9.
- An air flow 13C is withdrawn after being partially cooled, the remaining part of the air therefore being liquefied and sent to column 11.
- the flow 13C is expanded to 6 X 10 5 Pa in the turbine 23. A part of this expanded air is sent to the column 11 as a gas supply and the rest of the air is heated in the exchanger 9.
- a flow 13A of this air is partially heated, drawn off by the valve 15 and sent to the auxiliary exchanger 5 where it cools all the supply air to 25 ° C.
- the flow 13A then joins the air to be compressed in the compressor 17.
- the air flow 13B continues to heat up and joins the supply air downstream of the purification system 7.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
- comprimer le mélange gazeux ;
- épurer le mélange gazeux comprimé en eau et en dioxyde de carbone ;
- refroidir le mélange gazeux épuré au voisinage de sa température de rosée ;
- distiller le mélange gazeux refroidi dans au moins une colonne de distillation ; et
- fournir la puissance frigorifique de l'appareil par un système de réfrigération autre qu'un groupe frigorifique, dans lequel on refroidit au moins une partie du mélange gazeux entre les étapes de compression et d'épuration par échange de chaleur indirect avec un débit de fluide frigorigène qui est un produit de la colonne de distillation ou qui constitue une partie du mélange gazeux à distiller.
- fournir un appoint de frigories moins coûteux en investissement et en énergie et de permettre une réfrigération de l'air à température constante (environ 25°C) avant son épuration par adsorption.
- le cycle frigorifique est un cycle d'azote ;
- le fluide frigorigène avec lequel le mélange gazeux échange de la chaleur est le fluide de cycle ;
- le débit de fluide frigorigène est réglé pour maintenir constante la température de la partie de mélange gazeux ;
- on épure le mélange gazeux en eau et en dioxyde de carbone par un système de perméation et/ou d'adsorption ;
- le débit de fluide est un débit d'azote produit par une colonne moyenne pression d'une double colonne de distillation ;
- toute la puissance frigorifique de l'appareil est fournie par au moins un cycle frigorifique ;
- après le refroidissement d'au moins une partie du mélange gazeux, le débit de fluide est liquéfié et injecté dans la colonne de distillation.
- une vanne de réglage pour contrôler la quantité de fluide frigorigène envoyé à l'échangeur auxiliaire ;
- le fluide frigorigène circule dans le cycle de réfrigération ;
- le fluide frigorigène est de l'azote gazeux provenant d'une colonne moyenne pression d'une double colonne ;
- le système d'épuration fonctionne par adsorption et/ou perméation ;
- des moyens pour liquéfier au moins une partie du fluide frigorigène en aval de l'échangeur auxiliaire et d'envoyer au moins une partie du fluide liquéfié à la colonne de distillation ;
- au moins un compresseur qui comprime le fluide frigorigène en aval de l'échangeur auxiliaire.
Claims (21)
- Procédé de séparation d'un mélange gazeux contenant de l'azote et de l'oxygène par distillation dans un appareil cryogénique comprenant les étapes de :comprimer le mélange gazeux;épurer le mélange gazeux comprimé en eau et en dioxyde de carbone ;refroidir le mélange gazeux épuré au voisinage de sa température de rosée ;distiller le mélange gazeux refroidi dans au moins une colonne de distillation (11) ; etfournir la puissance frigorifique de l'appareil par un système de réfrigération autre qu'un groupe frigorifique, dans lequel on refroidit au moins une partie du mélange gazeux entre les étapes de compression et d'épuration par échange de chaleur indirect avec un débit (13B) de fluide frigorigène qui est un produit de la colonne de distillation ou qui constitue une partie du mélange gazeux à distiller, caractérisé en ce que l'on produit du liquide comme produit final et on détend au moins une partie du fluide frigorigène dans une machine de détente avant qu'il échange de la chaleur avec le mélange gazeux non épuré.
- Procédé selon la revendication 1 dans lequel le système de réfrigération est un cycle frigorifique.
- Procédé selon la revendication 2 dans lequel le fluide frigorigène avec lequel le mélange gazeux échange de la chaleur est le fluide de cycle frigorifique.
- Procédé selon la revendication 2 ou 3, dans lequel le système de réfrigération est un cycle d'air ou un cycle d'azote.
- Procédé selon l'une des revendications précédentes dans lequel le débit (13B) de fluide frigorigène est réglé pour maintenir constante la température de la partie de mélange gazeux.
- Procédé selon l'une des revendications précédentes dans lequel on épure le mélange gazeux en eau et en dioxyde de carbone par un système de perméation et/ou d'adsorption (7).
- Procédé selon l'une des revendications précédentes dans lequel le débit (13B) de fluide frigorigène est un débit d'azote produit par une colonne moyenne pression d'une double colonne de distillation (11).
- Procédé selon l'une des revendications précédentes dans lequel au moins une partie du mélange gazeux ou du débit de fluide frigorigène est liquéfié et injecté dans la colonne de distillation (11).
- Procédé selon l'une des revendications précédentes dans lequel le système de réfrigération comprend l'injection d'un débit de liquide froid provenant d'une source extérieure dans la colonne de distillation (11).
- Procédé selon l'une des revendications précédentes, dans lequel au moins une partie du fluide frigorigène est surpressé avant d'être détendu.
- Procédé selon l'une des revendications précédentes, dans lequel le fluide frigorigène est partiellement réchauffé contre le mélange gazeux épuré après sa détente.
- Installation de séparation d'un mélange gazeux contenant de l'azote et de l'oxygène par distillation cryogénique comprenant un compresseur (1), un système d'épuration (7), un échangeur principal (9), au moins une colonne de distillation (11), des moyens (17, 21, 23) constituant un système de réfrigération et un échangeur auxiliaire (5) qui met le mélange gazeux comprimé par le compresseur (1) en relation d'échange thermique avec un fluide frigorigène provenant soit de la colonne (11), soit de l'alimentation en aval du système d'épuration (7), caractérisée en ce qu'elle comprend des moyens de soutirage d'un produit liquide et une machine de détente (23) pour détendre au moins une partie du fluide frigorigène en amont de l'échangeur auxiliaire.
- Installation selon la revendication 12, dans laquelle une vanne de réglage (15) contrôle la quantité de fluide frigorigène envoyé à l'échangeur auxiliaire (5).
- Installation selon la revendication 12 ou 13, dans laquelle le fluide frigorigène circule dans le cycle de réfrigération.
- Installation selon l'une des revendications 12 à 14, dans laquelle le fluide frigorigène est de l'azote gazeux provenant d'une colonne moyenne pression d'une double colonne (11) ou une partie du mélange gazeux.
- Installation selon l'une des revendications 12 à 15, dans laquelle le système d'épuration (7) fonctionne par adsorption et/ou perméation.
- Installation selon l'une des revendications 12 à 16 comprenant des moyens (17, 19, 21) pour liquéfier le fluide frigorigène en aval de l'échangeur auxiliaire (5) et d'en envoyer au moins une partie à la colonne de distillation (11).
- Installation selon l'une des revendications 12 à 17 comprenant au moins un compresseur (17, 21) qui comprime le fluide frigorigène en aval de l'échangeur auxiliaire (5).
- Installation selon l'une des revendications 12 à 18 comprenant des moyens pour injecter un débit de liquide provenant d'une source extérieure dans la colonne de distillation (11).
- Installation selon l'une des revendications 12 à 19 dans laquelle l'échangeur auxiliaire (5) met le mélange gazeux en relation d'échange thermique avec un seul fluide frigorigène.
- Installation selon l'une des revendications 12 à 20 comprenant des moyens (17, 21) pour surpresser la partie du fluide frigorigène destiné à être détendu.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9415608 | 1994-12-23 | ||
FR9415608A FR2728663B1 (fr) | 1994-12-23 | 1994-12-23 | Procede de separation d'un melange gazeux par distillation cryogenique |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0718576A1 EP0718576A1 (fr) | 1996-06-26 |
EP0718576B1 true EP0718576B1 (fr) | 1999-09-01 |
Family
ID=9470210
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP95402924A Expired - Lifetime EP0718576B1 (fr) | 1994-12-23 | 1995-12-22 | Procédé de séparation d'un mélange gazeux par distillation cryogénique |
Country Status (8)
Country | Link |
---|---|
US (1) | US5651271A (fr) |
EP (1) | EP0718576B1 (fr) |
JP (1) | JPH08254389A (fr) |
CN (1) | CN1133964A (fr) |
CA (1) | CA2165916A1 (fr) |
DE (1) | DE69511833T2 (fr) |
ES (1) | ES2138172T3 (fr) |
FR (1) | FR2728663B1 (fr) |
Families Citing this family (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2753394B1 (fr) * | 1996-09-13 | 1998-10-16 | Air Liquide | Procede de compression d'un gaz associe a une unite de separation d'un melange gazeux |
DE19720453A1 (de) * | 1997-05-15 | 1998-11-19 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung von Stickstoff durch Tieftemperaturzerlegung von Luft |
US5806342A (en) * | 1997-10-15 | 1998-09-15 | Praxair Technology, Inc. | Cryogenic rectification system for producing low purity oxygen and high purity oxygen |
US5968234A (en) * | 1998-04-14 | 1999-10-19 | Air Products And Chemicals, Inc. | Temperature swing adsorption with regeneration by elevated pressure ASU nitrogen-enriched gas |
FR2790823B1 (fr) * | 1999-03-12 | 2001-06-15 | Air Liquide | Procede et installation de purification et de separation d'air par voie cryogenique sans pre-refroidissement |
FR2807150B1 (fr) * | 2000-04-04 | 2002-10-18 | Air Liquide | Procede et appareil de production d'un fluide enrichi en oxygene par distillation cryogenique |
US6543253B1 (en) | 2002-05-24 | 2003-04-08 | Praxair Technology, Inc. | Method for providing refrigeration to a cryogenic rectification plant |
US7225637B2 (en) * | 2004-12-27 | 2007-06-05 | L'Air Liquide Société Anonyme á´ Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Integrated air compression, cooling, and purification unit and process |
CN100441990C (zh) * | 2006-08-03 | 2008-12-10 | 西安交通大学 | 利用空分制冷***的小型天然气液化装置 |
US8601833B2 (en) * | 2007-10-19 | 2013-12-10 | Air Products And Chemicals, Inc. | System to cold compress an air stream using natural gas refrigeration |
US9546814B2 (en) | 2011-03-16 | 2017-01-17 | 8 Rivers Capital, Llc | Cryogenic air separation method and system |
EP2505948B1 (fr) | 2011-03-30 | 2018-10-10 | General Electric Technology GmbH | Séparation cryogénique de CO2 au moyen d'un système de réfrigération |
FR2976059B1 (fr) * | 2011-05-31 | 2013-05-31 | Air Liquide | Appareil et procede integre de separation d'un melange de dioxyde de carbone et au moins un autre gaz et de separation d'air par distillation cryogenique |
CN102425574A (zh) * | 2011-10-20 | 2012-04-25 | 河北东明中硅科技有限公司 | 多晶硅***制氮制动风机用空气的处理方法 |
CN103438665B (zh) * | 2013-09-01 | 2015-06-17 | 杭州哲达科技股份有限公司 | 降低空分设备综合电单耗的装置及方法 |
CA3034454A1 (fr) | 2016-08-30 | 2018-03-08 | 8 Rivers Capital, Llc | Procede de separation d'air cryogenique pour produire de l'oxygene a des pressions elevees |
EP3769022A1 (fr) * | 2018-03-21 | 2021-01-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et appareil de separation d'un gaz de synthese par distillation cryogenique |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3327488A (en) * | 1964-04-17 | 1967-06-27 | Air Prod & Chem | Refrigeration system for gas liquefaction |
DE2544340A1 (de) * | 1975-10-03 | 1977-04-14 | Linde Ag | Verfahren zur luftzerlegung |
BR7606681A (pt) * | 1975-10-28 | 1977-11-16 | Linde Ag | Processo e instalacao para fracionamento de ar |
JPS54103777A (en) * | 1978-02-01 | 1979-08-15 | Hitachi Ltd | Pretreatment of air separator |
JPS576282A (en) * | 1980-06-14 | 1982-01-13 | Kobe Steel Ltd | Air separator |
US4375367A (en) | 1981-04-20 | 1983-03-01 | Air Products And Chemicals, Inc. | Lower power, freon refrigeration assisted air separation |
FR2661841B1 (fr) * | 1990-05-09 | 1992-07-17 | Air Liquide | Procede et appareil d'epuration par adsorption d'air destine a etre distille. |
DE4109945A1 (de) | 1991-03-26 | 1992-10-01 | Linde Ag | Verfahren zur tieftemperaturzerlegung von luft |
GB2274407B (en) * | 1993-01-22 | 1996-06-12 | Boc Group Plc | The separation of gas mixtures |
US5321953A (en) * | 1993-05-10 | 1994-06-21 | Praxair Technology, Inc. | Cryogenic rectification system with prepurifier feed chiller |
-
1994
- 1994-12-23 FR FR9415608A patent/FR2728663B1/fr not_active Expired - Fee Related
-
1995
- 1995-12-18 US US08/574,128 patent/US5651271A/en not_active Expired - Fee Related
- 1995-12-21 CA CA002165916A patent/CA2165916A1/fr not_active Abandoned
- 1995-12-22 EP EP95402924A patent/EP0718576B1/fr not_active Expired - Lifetime
- 1995-12-22 CN CN95113135.4A patent/CN1133964A/zh active Pending
- 1995-12-22 JP JP7335507A patent/JPH08254389A/ja active Pending
- 1995-12-22 ES ES95402924T patent/ES2138172T3/es not_active Expired - Lifetime
- 1995-12-22 DE DE69511833T patent/DE69511833T2/de not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
US5651271A (en) | 1997-07-29 |
FR2728663A1 (fr) | 1996-06-28 |
JPH08254389A (ja) | 1996-10-01 |
CA2165916A1 (fr) | 1996-06-24 |
CN1133964A (zh) | 1996-10-23 |
DE69511833T2 (de) | 2000-05-18 |
FR2728663B1 (fr) | 1997-01-24 |
EP0718576A1 (fr) | 1996-06-26 |
ES2138172T3 (es) | 2000-01-01 |
DE69511833D1 (de) | 1999-10-07 |
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