EP0629828B1 - Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable - Google Patents
Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable Download PDFInfo
- Publication number
- EP0629828B1 EP0629828B1 EP94401213A EP94401213A EP0629828B1 EP 0629828 B1 EP0629828 B1 EP 0629828B1 EP 94401213 A EP94401213 A EP 94401213A EP 94401213 A EP94401213 A EP 94401213A EP 0629828 B1 EP0629828 B1 EP 0629828B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- liquid
- pressure
- flow rate
- vaporization
- heating fluid
- 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.)
- Expired - Lifetime
Links
Images
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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04103—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 using solely hydrostatic liquid head
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
- F25J3/04406—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
- F25J3/04763—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
- F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
-
- 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
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
-
- 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
- F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/939—Partial feed stream expansion, air
Definitions
- the present invention relates to the production of oxygen and / or nitrogen gas under pressure with variable flow. It primarily concerns a variable gas flow production process of at least one main constituent of pressurized air, of the type in which the component is drawn off in liquid form of an air distillation apparatus, we bring this liquid at spray pressure above the withdrawal pressure, and the liquid is vaporized under vaporization pressure by heat exchange with circulating fluid under high pressure. Such a process is known from document EP-A-0 422 974.
- the main application of the invention is production of gaseous oxygen under pressure at flow rate variable, and this is why we will explain below the invention with reference to this application.
- Air distillation devices are usually of the double column type and include a medium pressure column and a low pressure column coupled by a vaporizer-condenser.
- a medium pressure column and a low pressure column coupled by a vaporizer-condenser.
- pump liquid oxygen withdrawn from a tank the low pressure column is pumped up to a pressure relatively high, then is vaporized under this pressure, generally in the heat exchange line associated with the double column and by heat exchange with air being liquefied.
- characteristic curve There are for each component of the installation a relationship between the operating pressure and the flow, called the characteristic curve.
- the characteristic curve 1 links the compression ratio TC to the actual flow D aspirated ( Figure 2).
- the characteristic curve 5 is much more simple (Figure 3). It is a pressure P / flow D curve monotonous, increasing, passing through the origin.
- variable blades we can limit this loss by using a compressor equipped at its inlet with variable blades, which allows you to change characteristics. There is then no need to laminate on suction, and the point changes from A to C when moving to reduced flow.
- variable blades on an oxygen compressor is delicate and little widespread.
- US-A-3,214,925 also describes a system in which oxygen pumped liquid is vaporized against a flow of pressurized air, the air flow being thus liquefied.
- the invention aims to improve the overall performance of installation, both at reduced and nominal flow rates, without having use of variable blades, delicate to implement, for the final compressor.
- the invention relates to a process of the aforementioned type, characterized in that, when the demand for said gaseous component decreases, its flow rate is adjusted by modifying the flow rate of the liquid to be vaporized and said vaporization pressure and the flow of circulating fluid is reduced so balance the material balance and reduce the high pressure of circulating fluid to maintain the same temperature difference between the circulating fluid and the liquid that vaporizes.
- the invention also relates to an installation for the implementation work of such a process.
- This installation of the type known from document EP-A-0 422 974, comprising an apparatus for air distillation, means for withdrawing liquid from this apparatus, means for increasing the pressure of the liquid withdrawn to a pressure of vaporization, circulating fluid compressor, and heat exchanger for vaporizing the liquid under said vaporization pressure by exchange of heat with circulating fluid under high pressure, is characterized in that that it includes means for adjusting the flow rate of the liquid to be vaporized and for said vaporization pressure and means for reducing the flow rate of the fluid circulating in order to balance the material balance and to reduce the high pressure of the circulating fluid to maintain the same temperature difference between the fluid circulating and the fluid which vaporizes, when the demand of said constituent decreases.
- the installation shown in Figure 1 is intended to provide a flow variable gaseous oxygen under high pressure, for example under about 40 bars, via a product outlet pipe 6. It essentially comprises: an atmospheric air compressor 7; an apparatus 8 for purifying water and carbon dioxide by adsorption; a heat exchange line 9; a air blower 10 with variable blades; an expansion turbine 11; a double distillation column 12 itself comprising a medium column pressure 13 surmounted by a low pressure column 14, the head of the column 13 being coupled to the tank of column 14 by a vaporizer-condenser 15; a sub-cooler 16 a liquid oxygen pump 17 at rotational speed constant; a rolling valve 18 mounted in the discharge line 19 of this pump; and one oxygen compressor 20 without variable blades.
- the double column is equipped with pipes usual 21 "rich liquid” rise (air enriched in oxygen), 22 for the rise of “poor liquid” (almost pure nitrogen), these two pipes connecting the medium pressure column to the low pressure column and being equipped with respective expansion valves, and 23 exhaust gas W (impure nitrogen) from the top of column 14, the sub-cooling waste gas the rich liquid and the poor liquid in the subcooler 16.
- atmospheric air compressed in 7 at medium column pressure 13 and refined in 8 is divided into two streams: one first current which is cooled in 9 to the neighborhood from its dew point and introduced into the column tank 13; and a second current which is boosted in 10 to one high pressure adapted to the vaporization pressure of liquid oxygen.
- the compressed air is cooled in 9 up to an intermediate temperature T, at which it is divided into two fractions: a first fraction which continues to cool and is liquefied, and possibly sub-cooled, until the cold end of the heat exchange line and then is distributed among the columns 13 and 14 after expansion in gates of corresponding triggers; and a second fraction which is outlet of the heat exchange line, expanded at 11 at low pressure and introduced into column 14, this expansion ensuring that the installation is kept cold.
- the turbine could expand by air at medium pressure, the relaxed air then being introduced in column 13.
- Liquid oxygen is drawn off in a tank column 14 and brought by pump 17 to a pressure intermediate.
- the valve 18 is in the open position maximum, so this intermediate pressure is substantially the vaporization pressure of oxygen liquid in the heat exchange line. Oxygen vaporized leaving, near room temperature, the hot end of the heat exchange line is then compressed to production pressure by the compressor 20.
- the comparison can be done as follows: in the technique anterior, by playing on the variable blades of the booster 10, the operating point changes from A, for the nominal flow, at B, for reduced flow. By laminating the liquid, the operating point at reduced flow changes to C.
- a throttle valve on the discharge line pump 17 provides both a gain in energy at low flow rates and a gain in efficiency, and therefore in energy, at nominal flow.
- the oxygen pressure liquid withdrawn from the double column can be increased without the use of a pump, by a hydrostatic height created in a down pipe.
- the invention applies equally well to air distillers having their own medium pressure air compressor, as described more high, than devices integrated into a gas turbine.
- the invention also applies for the production of nitrogen under high pressure at flow rate variable. It brings the same advantage vis-à-vis the air blower (or, more generally, compressor cycle of circulating fluid ensuring vaporization), and allows the use of a final nitrogen compressor without variable blades, and therefore more economical.
- the invention applies also in case the installation does not include final compressor 20.
- the pressure of the oxygen produced is then a function of the flow rate of vaporized oxygen and is defined by the characteristic curve of the equipment consumer.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Structures Of Non-Positive Displacement Pumps (AREA)
Description
- la pression de vaporisation est intermédiaire entre la pression de soutirage et la pression de production, et on comprime jusqu'à la pression de production le gaz résultant de la vaporisation;
- on effectue ladite modification de manière à permettre au compresseur du gaz résultant de suivre sa courbe caractéristique;
- pour effectuer ladite modification, on lamine de manière variable le liquide à vaporiser;
- pour effectuer ladite modification, on pompe à vitesse variable le liquide envoyé dans l'échangeur de chaleur de vaporisation;
- pour effectuer ladite modification, on pompe un débit constant du liquide, et on en renvoie un débit variable vers l'appareil de distillation, le reste du liquide étant vaporisé.
- la figure 1 représente schématiquement une installation de production d'oxygène gazeux conforme à l'invention;
- la figure 2 est une courbe caractéristique du fonctionnement des compresseurs de cette installation;
- la figure 3 est une courbe caractéristique du fonctionnement des composants passifs de l'installation;
- la figure 4 illustre les avantages apportés par l'invention; et
- la figure 5 est une vue schématique partielle d'une variante.
Claims (12)
- Procédé de production à débit gazeux variable d'au moins un constituant principal de l'air sous pression, du type dans lequel on soutire le constituant sous forme liquide d'un appareil de distillation d'air (12), on amène ce liquide à une pression de vaporisation au dessus de la pression de soutirage, et on vaporise le liquide sous la pression de vaporisation par échange de chaleur (en 9) avec un fluide calorigène sous haute pression, caractérisé en ce que, lorsque la demande dudit constituant gazeux diminue, l'on règle son débit en modifiant le débit du liquide à vaporiser et ladite pression de vaporisation et on réduit le débit du fluide calorigène afin d'équilibrer le bilan matière et on réduit la haute pression du fluide calorigène pour maintenir le même écart de température entre le fluide calorigène et le liquide qui se vaporise.
- Procédé suivant la revendication 1 caractérisé en ce qu'on comprime jusqu'à la pression de production (en 20) le gaz résultant de la vaporisation.
- Procédé suivant la revendication 2, caractérisé en ce qu'on effectue ladite modification de manière à permettre au compresseur (20) du gaz résultant de suivre sa courbe caractéristique (1).
- Procédé suivant l'une quelconque des revendications 1 à 3, caractérisé en ce que, pour effectuer ladite modification, on lamine de manière variable (en 18) le liquide à vaporiser.
- Procédé suivant l'une quelconque des revendications 1 à 4, caractérisé en ce que, pour effectuer ladite modification, on pompe à vitesse variable (en 17) le liquide envoyé dans l'échangeur de chaleur de vaporisation (9).
- Procédé suivant l'une quelconque des revendications 1 à 4, caractérisé en ce que, pour effectuer ladite modification, on pompe un débit constant du liquide, et on en renvoie un débit variable (en 24) vers l'appareil de distillation (12), le reste du liquide étant vaporisé.
- Installation de production à débit variable d'au moins un constituant principal de l'air sous pression, du type comprenant un appareil de distillation d'air (12), des moyens pour soutirer un liquide de cet appareil, des moyens (17) pour augmenter la pression du liquide soutiré à une pression de vaporisation, un compresseur (10) de fluide calorigène, et un échangeur de chaleur (9) pour vaporiser le liquide sous ladite pression de vaporisation par échange de chaleur avec le fluide calorigène sous haute pression, caractérisée en ce qu'elle comprend des moyens (18;24) de réglage du débit du liquide à vaporiser et de ladite pression de vaporisation et des moyens (10) pour réduire le débit du fluide calorigène afin d'équilibrer le bilan matière et pour réduire la haute pression du fluide calorigène pour maintenir le même écart de température entre le fluide calorigène et le fluide qui se vaporise, lorsque la demande dudit constituant diminue.
- Installation suivant la revendication 7, caractérisée en ce qu'elle comprend un compresseur (20) pour amener le gaz résultant de ladite vaporisation à la pression de production.
- Installation suivant la revendication 8, caractérisée en ce que le compresseur (20) est dépourvu d'aubages variables à son entrée et/ou est entraíné par un moteur à vitesse constante.
- Installation suivant l'une quelconque des revendications 7 à 9, caractérisée en ce qu'elle comprend une pompe (17) à vitesse constante reliée en amont à l'appareil de distillation (12) et en aval à des passages de vaporisation du liquide de l'échangeur de chaleur (9), et en ce que les moyens de réglage comprennent une vanne d'étranglement (18) montée dans la conduite de refoulement de cette pompe.
- Installation suivant l'une quelconque des revendications 7 à 9, caractérisée en ce qu'elle comprend une pompe entraínée par un moteur à vitesse variable, reliée en amont à l'appareil de distillation (12) et en aval à des passages de vaporisation du liquide de l'échangeur de chaleur (9).
- Installation suivant la revendication 10 ou 11, caractérisée en ce qu'elle comporte une conduite de retour, équipée d'une vanne de réglage de débit (24), reliant le refoulement de la pompe (17) à l'appareil de distillation (12).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9307395 | 1993-06-18 | ||
FR9307395A FR2706595B1 (fr) | 1993-06-18 | 1993-06-18 | Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable. |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0629828A1 EP0629828A1 (fr) | 1994-12-21 |
EP0629828B1 true EP0629828B1 (fr) | 1998-04-15 |
Family
ID=9448298
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP94401213A Expired - Lifetime EP0629828B1 (fr) | 1993-06-18 | 1994-06-02 | Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable |
Country Status (6)
Country | Link |
---|---|
US (1) | US5437161A (fr) |
EP (1) | EP0629828B1 (fr) |
CA (1) | CA2125944C (fr) |
DE (1) | DE69409581T2 (fr) |
ES (1) | ES2117765T3 (fr) |
FR (1) | FR2706595B1 (fr) |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2721383B1 (fr) * | 1994-06-20 | 1996-07-19 | Maurice Grenier | Procédé et installation de production d'oxygène gazeux sous pression. |
US5501078A (en) * | 1995-04-24 | 1996-03-26 | Praxair Technology, Inc. | System and method for operating an integrated gas turbine and cryogenic air separation plant under turndown conditions |
US5802873A (en) * | 1997-05-08 | 1998-09-08 | Praxair Technology, Inc. | Cryogenic rectification system with dual feed air turboexpansion |
GB9807833D0 (en) * | 1998-04-09 | 1998-06-10 | Boc Group Plc | Separation of air |
US6000239A (en) * | 1998-07-10 | 1999-12-14 | Praxair Technology, Inc. | Cryogenic air separation system with high ratio turboexpansion |
US8429933B2 (en) * | 2007-11-14 | 2013-04-30 | Praxair Technology, Inc. | Method for varying liquid production in an air separation plant with use of a variable speed turboexpander |
FR2983287B1 (fr) * | 2011-11-25 | 2018-03-02 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et installation de separation d'air par distillation cryogenique |
Family Cites Families (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BE564694A (fr) * | 1957-02-13 | |||
DE1112997B (de) * | 1960-08-13 | 1961-08-24 | Linde Eismasch Ag | Verfahren und Einrichtung zur Gaszerlegung durch Rektifikation bei tiefer Temperatur |
FR1479561A (fr) * | 1966-03-25 | 1967-05-05 | Air Liquide | Procédé de preoduction d'un gaz en débit variable |
US3760596A (en) * | 1968-10-23 | 1973-09-25 | M Lemberg | Method of liberation of pure nitrogen and oxygen from air |
DE1907525A1 (de) * | 1969-02-14 | 1970-08-20 | Vnii Kriogennogo Masinostrojen | Verfahren zur Trennung von Stickstoff und Sauerstoff aus der Luft |
JPS5419165B2 (fr) * | 1973-03-01 | 1979-07-13 | ||
FR2461906A1 (fr) * | 1979-07-20 | 1981-02-06 | Air Liquide | Procede et installation cryogeniques de separation d'air avec production d'oxygene sous haute pression |
GB2061478B (en) * | 1979-10-23 | 1983-06-22 | Air Prod & Chem | Method and cryogenic plant for producing gaseous oxygen |
WO1987001185A1 (fr) * | 1985-08-23 | 1987-02-26 | Daidousanso Co., Ltd. | Unite de production d'oxygene a l'etat gazeux |
FR2610846A1 (fr) * | 1987-02-17 | 1988-08-19 | Air Liquide | Element filtrant pour dispositif d'event et dispositif comportant un tel element |
DE3913880A1 (de) * | 1989-04-27 | 1990-10-31 | Linde Ag | Verfahren und vorrichtung zur tieftemperaturzerlegung von luft |
FR2652887B1 (fr) * | 1989-10-09 | 1993-12-24 | Air Liquide | Procede et installation de production d'oxygene gazeux a debit variable par distillation d'air. |
US5129932A (en) * | 1990-06-12 | 1992-07-14 | Air Products And Chemicals, Inc. | Cryogenic process for the separation of air to produce moderate pressure nitrogen |
US5081845A (en) * | 1990-07-02 | 1992-01-21 | Air Products And Chemicals, Inc. | Integrated air separation plant - integrated gasification combined cycle power generator |
JP2909678B2 (ja) * | 1991-03-11 | 1999-06-23 | レール・リキード・ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | 圧力下のガス状酸素の製造方法及び製造装置 |
DE4126945A1 (de) * | 1991-08-14 | 1993-02-18 | Linde Ag | Verfahren zur luftzerlegung durch rektifikation |
FR2681415B1 (fr) * | 1991-09-18 | 1999-01-29 | Air Liquide | Procede et installation de production d'oxygene gazeux sous haute pression par distillation d'air. |
FR2689224B1 (fr) * | 1992-03-24 | 1994-05-06 | Lair Liquide | Procede et installation de production d'azote sous haute pression et d'oxygene. |
-
1993
- 1993-06-18 FR FR9307395A patent/FR2706595B1/fr not_active Expired - Fee Related
-
1994
- 1994-06-02 ES ES94401213T patent/ES2117765T3/es not_active Expired - Lifetime
- 1994-06-02 DE DE69409581T patent/DE69409581T2/de not_active Expired - Fee Related
- 1994-06-02 EP EP94401213A patent/EP0629828B1/fr not_active Expired - Lifetime
- 1994-06-06 US US08/257,691 patent/US5437161A/en not_active Expired - Fee Related
- 1994-06-15 CA CA002125944A patent/CA2125944C/fr not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
FR2706595B1 (fr) | 1995-08-18 |
DE69409581D1 (de) | 1998-05-20 |
CA2125944C (fr) | 2004-10-19 |
DE69409581T2 (de) | 1998-12-17 |
EP0629828A1 (fr) | 1994-12-21 |
ES2117765T3 (es) | 1998-08-16 |
CA2125944A1 (fr) | 1994-12-19 |
FR2706595A1 (fr) | 1994-12-23 |
US5437161A (en) | 1995-08-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0504029B1 (fr) | Procédé de production d'oxygène gazeux sous pression | |
EP0422974B1 (fr) | Procédé et installation de production d'oxygène gazeux à débit variable par distillation d'air | |
AU688218B2 (en) | Cooling a fluid stream | |
EP0848220B1 (fr) | Procédé et installation de fourniture d'un débit variable d'un gaz de l'air | |
EP0689019B1 (fr) | Procédé et installation de production d'oxygène gazeux sous pression | |
EP0024962A1 (fr) | Procédé cryogénique de séparation d'air avec production d'oxygène sous haute pression | |
EP1447634B1 (fr) | Procédé et installation de production sous forme gazeuse et sous haute pression d'au moins un fluide choisi parmi l'oxygène, l'argon et l'azote par distillation cryogénique de l'air | |
EP1352203A1 (fr) | Procede de refrigeration de gaz liquefie et installation mettant en oeuvre celui-ci | |
EP1118827B1 (fr) | Procédé de liquéfaction partielle d'un fluide contenant des hydrocarbures tel que du gaz naturel | |
EP0576314A1 (fr) | Procédé et installation de production d'oxygène gazeux sous pression | |
EP0694746B1 (fr) | Procédé de production d'un gaz sous pression à débit variable | |
EP0629828B1 (fr) | Procédé et installation de production d'oxygène et/ou d'azote sous pression à débit variable | |
EP0618415B1 (fr) | Procédé et installation de production d'oxygène gazeux et/ou d'azote gazeux sous pression par distillation d'air | |
FR2805339A1 (fr) | Procede de production d'oxygene par rectification cryogenique | |
FR2787560A1 (fr) | Procede de separation cryogenique des gaz de l'air | |
EP0914584B1 (fr) | Procede et installation de production d'un gaz de l'air a debit variable | |
EP0677713B1 (fr) | Procédé et installation pour la production de l'oxygène par distillation de l'air | |
EP0612967A1 (fr) | Procédé et installation de production d'oxygène et/ou d'azote sous pression | |
EP3695180B1 (fr) | Procede de separation d'air par distillation cryogenique | |
FR2943125A1 (fr) | Procede de liquefaction de gaz naturel a cycle combine | |
FR2929697A1 (fr) | Procede de production d'azote gazeux variable et d'oxygene gazeux variable par distillation d'air | |
CA2234435A1 (fr) | Procede et installation de separation d'air par distillation cryogenique | |
EP0422973A1 (fr) | Procédé et installation de réfrigeration utilisant un mélange réfrigerant | |
EP1007380A1 (fr) | Circuit de climatisation de vehicule muni d'un dispositif de predetente |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 19940615 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): BE DE ES FR IT NL |
|
17Q | First examination report despatched |
Effective date: 19960306 |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAG | Despatch of communication of intention to grant |
Free format text: ORIGINAL CODE: EPIDOS AGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAH | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOS IGRA |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): BE DE ES FR IT NL |
|
REF | Corresponds to: |
Ref document number: 69409581 Country of ref document: DE Date of ref document: 19980520 |
|
ITF | It: translation for a ep patent filed |
Owner name: ING. A. GIAMBROCONO & C. S.R.L. |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2117765 Country of ref document: ES Kind code of ref document: T3 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
26N | No opposition filed | ||
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: FR Payment date: 20060511 Year of fee payment: 13 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: NL Payment date: 20060515 Year of fee payment: 13 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20060523 Year of fee payment: 13 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: BE Payment date: 20060531 Year of fee payment: 13 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: ES Payment date: 20060606 Year of fee payment: 13 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: IT Payment date: 20060630 Year of fee payment: 13 |
|
BERE | Be: lapsed |
Owner name: S.A. L'*AIR LIQUIDE POUR L'ETUDE ET L'EXPLOITATION Effective date: 20070630 |
|
NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee |
Effective date: 20080101 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20070630 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST Effective date: 20080229 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080101 Ref country code: DE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20080101 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20070604 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20070702 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: ES Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20070604 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20070602 |