FR2913104A1 - Nitrogen supplying method, involves supplying nitrogen to client by vaporization of liquid nitrogen and by gaseous nitrogen producing apparatus when need of client for gaseous nitrogen is less than and greater than threshold, respectively - Google Patents
Nitrogen supplying method, involves supplying nitrogen to client by vaporization of liquid nitrogen and by gaseous nitrogen producing apparatus when need of client for gaseous nitrogen is less than and greater than threshold, respectively Download PDFInfo
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- FR2913104A1 FR2913104A1 FR0753567A FR0753567A FR2913104A1 FR 2913104 A1 FR2913104 A1 FR 2913104A1 FR 0753567 A FR0753567 A FR 0753567A FR 0753567 A FR0753567 A FR 0753567A FR 2913104 A1 FR2913104 A1 FR 2913104A1
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- nitrogen
- customer
- threshold
- nitrogen gas
- liquid
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 206
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 83
- 239000007788 liquid Substances 0.000 title claims abstract description 43
- 238000009834 vaporization Methods 0.000 title claims abstract description 19
- 230000008016 vaporization Effects 0.000 title claims abstract description 18
- 238000000034 method Methods 0.000 title claims abstract description 12
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 40
- 238000004519 manufacturing process Methods 0.000 claims description 16
- 238000004821 distillation Methods 0.000 claims description 12
- 239000006200 vaporizer Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 10
- 230000005611 electricity Effects 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 238000012423 maintenance Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 10
- 230000004913 activation Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
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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
- F25J3/04248—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
- F25J3/04763—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
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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
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/42—One fluid being 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
2913104 La présente invention est relative à un procédé et à un appareilThe present invention relates to a method and apparatus
de fourniture d'azote. Il est commun de fournir un client en azote au moyen d'un appareil générateur de gaz, tel qu'un appareil cryogénique de distillation d'air, ainsi qu'un stockage d'azote qui fournit de l'azote gazeux qui fournit le client quand l'appareil cryogénique est en panne et/ou n'arrive pas à produire tout le débit requis. Selon l'invention l'appareil générateur de gaz est mis en marche uniquement lorsque cela est plus économique que d'utiliser un stockage de gaz (sous forme gazeuse ou liquide) pour fournir un client. io Comme montré à la Figure 1, selon l'art antérieur, un générateur de gaz A, en particulier pour les unités présentes sur le site d'un client, est généralement couplé à un moyen de fourniture de secours B de type vrac (liquide avec évaporateur ou gaz). Le générateur est toujours en état de fournir le client via les conduites 15 C,E. Lorsque le client consomme plus que le nominal (100 %), le moyen de fourniture de secours se met en route et transfère de l'azote via les conduites D,E. De même, lorsque le générateur est en panne, le moyen de fourniture de secours prend le relais. nitrogen supply. It is common to provide a nitrogen customer by means of a gas generating apparatus, such as a cryogenic air distillation apparatus, as well as a storage of nitrogen which provides nitrogen gas which supplies the customer. when the cryogenic apparatus is out of order and / or fails to produce all the required flow rate. According to the invention the gas generator apparatus is operated only when it is more economical than using a gas storage (in gaseous or liquid form) to provide a customer. As shown in FIG. 1, according to the prior art, a gas generator A, in particular for the units present on the site of a customer, is generally coupled to an emergency supply means B of the bulk type (liquid with evaporator or gas). The generator is still able to supply the customer via lines 15 C, E. When the customer consumes more than the nominal (100%), the means of emergency supply starts up and transfers nitrogen via lines D, E. Similarly, when the generator is down, the emergency supply means takes over.
20 Dans ce mode de fonctionnement, le générateur est en marche quelle que soit la consommation du client. Dans les phases de faible consommation du client par rapport au nominal du générateur, la consommation énergétique et donc le coût de production ne sont pas optimaux. Ce fonctionnement selon l'art antérieur est illustré à la Figure 3. Au 25 temps 0, le client consomme 20 Nm3/h d'azote, ce débit étant fourni entièrement par distillation d'air dans un appareil de séparation à simple colonne biberonné. Au fur et à mesure que la consommation du client augmente, la production de l'appareil augmente en conséquence à 40 et ensuite 100 Nm3/h aux temps 10 heures et 20 heures respectivement. Or, 30 quand la consommation du client atteint 150 Nm3/h, l'appareil de séparation continue de produire son débit maximal de 100 Nm3/h, le reste étant fourni par vaporisation d'azote stocké pour produire un débit de 50 Nm3/h.In this mode of operation, the generator is running regardless of the customer's consumption. In the phases of low consumption of the customer compared to the nominal of the generator, the energy consumption and therefore the production cost are not optimal. This operation according to the prior art is illustrated in FIG. 3. At time 0, the customer consumes 20 Nm.sup.3 / hr of nitrogen, this flow being supplied entirely by air distillation in a single-column, boiling-off separation apparatus. As the customer's consumption increases, the output of the device increases accordingly to 40 and then 100 Nm3 / h at 10 hours and 20 hours respectively. However, when the customer's consumption reaches 150 Nm3 / h, the separation apparatus continues to produce its maximum flow rate of 100 Nm3 / h, the remainder being supplied by nitrogen spraying stored to produce a flow rate of 50 Nm3 / h. .
2 2913104 Quand la consommation réduit à 80 Nm3/h à l'instant 50 heures, la production d'azote par vaporisation s'arrête et la production d'azote par l'appareil de distillation est rabaissée à 80 Nm3/h. Ensuite pour suivre la consommation du client, le niveau de production de l'appareil est réduit à 40 5 et ensuite 20 Nm3/h. Selon un objet de l'invention, il est prévu un procédé de fourniture d'azote au moyen d'un appareil de production d'azote gazeux par séparation d'air et par vaporisation d'azote liquide dans lequel : a) si les besoins du client en azote gazeux sont inférieurs à un io premier seuil, le client est fourni en azote exclusivement par vaporisation d'azote liquide b) si les besoins du client en azote gazeux sont supérieurs à un deuxième seuil, le deuxième seuil étant supérieur au premier seuil, le client est fourni en azote au moins partiellement par l'appareil de production 15 d'azote. Selon d'autres objets de l'invention : - si les besoins du client en azote dépassent un troisième seuil, supérieur au deuxième seuil, le client est fourni partiellement par l'appareil de production d'azote et partiellement par vaporisation d'azote liquide ; 20 - les besoins du client sont entre le deuxième et le troisième seuil et le client est fourni uniquement par l'appareil de production d'azote ; - si les besoins du client en azote gazeux sont supérieurs au deuxième seuil, le client est fourni en azote uniquement par l'appareil de production d'azote ; 25 - au moins un des premier, deuxième et troisième seuils est variable selon le prix de l'électricité et/ou le prix de l'azote liquide et/ou la quantité d'azote liquide dans un stockage relié au moyen de vaporisation et/ou la vitesse de modification de la quantité d'azote liquide dans le stockage ; - si les besoins du client en azote gazeux sont supérieurs au 30 deuxième seuil ou supérieurs au deuxième seuil mais inférieurs au troisième seuil, l'appareil de production d'azote produit de l'azote gazeux avec un débit sensiblement constant et 3 2913104 a) si les besoins du client en azote gazeux sont inférieurs au débit sensiblement constant, la partie excédentaire d'azote gazeux est rejetée à l'atmosphère et le reste d'azote gazeux est envoyé au client b) si les besoins du client en azote gazeux sont supérieurs ou 5 égaux au débit sensiblement constant, tout le débit d'azote gazeux est envoyé au client - l'appareil de production d'azote gazeux est un appareil de distillation cryogénique d'air et éventuellement de l'azote liquide est envoyé à l'appareil de production d'azote gazeux pour participer à son maintien en froid. io Selon un autre objet de l'invention, il est prévu un appareil de fourniture d'azote gazeux comprenant un appareil de production d'azote gazeux par séparation d'air, un vaporiseur d'azote liquide, un stockage, des moyens pour alimenter le vaporiseur en azote liquide par le stockage, des moyens pour envoyer de l'azote gazeux de l'appareil de production au client, 15 des moyens pour envoyer de l'azote gazeux du vaporiseur au client et des moyens pour réguler au moins un des débits d'azote gazeux envoyé au client en fonction du prix de l'électricité et/ou du prix de l'azote liquide et/ou de la quantité d'azote liquide dans le stockage et/ou de la vitesse de modification de la quantité d'azote liquide dans le stockage.When the consumption reduces to 80 Nm3 / h at the instant 50 hours, the nitrogen production by vaporization stops and the production of nitrogen by the distillation apparatus is lowered to 80 Nm3 / h. Then to track the customer's consumption, the production level of the device is reduced to 40 5 and then 20 Nm3 / h. According to one object of the invention, there is provided a method of supplying nitrogen by means of an apparatus for producing nitrogen gas by separation of air and by vaporization of liquid nitrogen in which: a) if the needs the customer's nitrogen gas is below a first threshold, the customer is provided with nitrogen exclusively by vaporization of liquid nitrogen b) if the customer's nitrogen gas requirements are greater than a second threshold, the second threshold being greater than the first threshold; At the threshold, the customer is provided with nitrogen at least partially by the nitrogen production apparatus. According to other objects of the invention: - if the nitrogen requirements of the customer exceed a third threshold, higher than the second threshold, the customer is supplied partially by the nitrogen production apparatus and partly by vaporization of liquid nitrogen ; The customer's needs are between the second and the third threshold and the customer is supplied solely by the nitrogen production apparatus; - if the customer's nitrogen gas requirements are higher than the second threshold, the customer is provided with nitrogen only by the nitrogen generator; 25 - at least one of the first, second and third thresholds is variable according to the price of electricity and / or the price of liquid nitrogen and / or the amount of liquid nitrogen in a storage connected to the vaporization means and / or the rate of change of the amount of liquid nitrogen in the storage; - if the customer's nitrogen gas requirements are greater than the second threshold or greater than the second threshold but lower than the third threshold, the nitrogen generating apparatus produces nitrogen gas with a substantially constant flow rate and 3 2913104 a) if the customer's nitrogen gas requirements are lower than the substantially constant flow rate, the excess nitrogen gas is released to the atmosphere and the remaining nitrogen gas is sent to the customer b) if the customer's nitrogen gas requirements are met greater than or equal to the substantially constant flow rate, the entire flow of nitrogen gas is sent to the customer - the apparatus for producing nitrogen gas is a cryogenic distillation apparatus of air and possibly liquid nitrogen is sent to the apparatus for producing nitrogen gas to participate in keeping it cold. According to another object of the invention, there is provided a device for supplying nitrogen gas comprising an apparatus for producing nitrogen gas by separation of air, a liquid nitrogen vaporizer, a storage, means for feeding the liquid nitrogen vaporizer by storage, means for supplying nitrogen gas from the production apparatus to the customer, means for sending nitrogen gas from the vaporizer to the customer and means for regulating at least one of the flow rates of nitrogen gas to the customer based on the price of electricity and / or the price of liquid nitrogen and / or the amount of liquid nitrogen in the storage and / or rate of change in quantity of liquid nitrogen in the storage.
20 Eventuellement l'appareil de production d'azote gazeux est un appareil de distillation cryogénique d'air. L'invention sera maintenant décrite en plus de détail en se référant aux figures. La figure 2 illustre un appareil de fourniture d'azote selon l'invention.Optionally, the apparatus for producing nitrogen gas is a cryogenic air distillation apparatus. The invention will now be described in more detail with reference to the figures. Figure 2 illustrates a nitrogen supply apparatus according to the invention.
25 La figure 4 est un graphique illustrant la mode d'opération de cet appareil avec le procédé selon l'invention. Selon cette invention, il est proposé d'inverser la philosophie actuelle. Le client est en base fourni par le moyen de fourniture de secours vrac . Lorsque sa demande dépasse une certaine valeur, le générateur efface la 30 fourniture vrac . Cette valeur est définie de façon à ce que le coût de production par le générateur devienne plus économique que la fourniture vrac . Elle dépend du coût de l'énergie et du coût du vrac.Figure 4 is a graph illustrating the mode of operation of this apparatus with the method of the invention. According to this invention, it is proposed to reverse the current philosophy. The customer is in base provided by the bulk emergency supply means. When its demand exceeds a certain value, the generator clears the bulk supply. This value is defined so that the cost of production by the generator becomes more economical than the bulk supply. It depends on the cost of energy and the cost of bulk.
4 2913104 Au delà de la capacité de production du générateur, le vrac vient compléter la production du générateur pour fournir le client. Ainsi comme on voit sur la figure 4, au temps 0, le client consomme 20 Nm3/h d'azote, ce débit étant fourni entièrement par vaporisation d'azote 5 provenant d'un stockage (ou éventuellement par arrivée d'azote gazeux provenant d'un réseau). La consommation du client augmente ensuite à 40 Nm3/h à 10 heures, la vaporisation d'azote s'arrête complètement, la production de l'appareil de distillation commence en conséquence à 40 Nm3/h et atteint 100 Nm3/h après 20 heures. Or, quand la consommation du io client atteint 150 Nm3/h, l'appareil de séparation continue de produire son débit maximal de 100 Nm3/h, le reste étant fourni par vaporisation d'azote stocké pour produire un débit de 50 Nm3/h. Quand la consommation réduit à 80 Nm3/h à l'instant 50 heures, la production d'azote par vaporisation s'arrête et la production d'azote par 15 l'appareil de distillation est rabaissée à 80 Nm3/h. Ensuite pour suivre la consommation du client, le niveau de production de l'appareil est réduit à 40 Nm3/h. Au-delà de cette valeur, la distillation d'air est arrêtée et pour fournir la consommation basse du client à 20 Nm3/h, la vaporisation d'azote liquide est remise en marche.4 2913104 Beyond the generating capacity of the generator, the bulk is used to supplement the generator's production to provide the customer. Thus, as can be seen in FIG. 4, at time 0, the customer consumes 20 Nm 3 / h of nitrogen, this flow being supplied entirely by nitrogen vaporisation from a storage (or possibly by the arrival of nitrogen gas from network). The customer's consumption then increases to 40 Nm3 / h at 10 hours, the nitrogen vaporization stops completely, the production of the distillation apparatus consequently starts at 40 Nm3 / h and reaches 100 Nm3 / h after 20 hours. . However, when the consumption of the customer reaches 150 Nm3 / h, the separation apparatus continues to produce its maximum flow rate of 100 Nm3 / h, the remainder being supplied by vaporization of nitrogen stored to produce a flow rate of 50 Nm3 / h. . When the consumption reduces to 80 Nm3 / h at the instant 50 hours, the nitrogen production by vaporization stops and the production of nitrogen by the distillation apparatus is lowered to 80 Nm3 / h. Then to track the customer's consumption, the production level of the device is reduced to 40 Nm3 / h. Beyond this value, the air distillation is stopped and to provide the low consumption of the customer at 20 Nm3 / h, the vaporization of liquid nitrogen is restarted.
20 Selon l'invention, l'appareil de séparation d'air peut produire, pour des valeurs entre 40 et 100 Nm3/h, la consommation exacte souhaitée selon l'invention. Comme illustré à la Figure 2, un ensemble complet 6 comprend un stockage d'azote liquide 1 et au moins la boite froide 9 du générateur cryogénique.According to the invention, the air separation apparatus can produce, for values between 40 and 100 Nm3 / h, the exact consumption desired according to the invention. As illustrated in FIG. 2, a complete set 6 comprises a storage of liquid nitrogen 1 and at least the cold box 9 of the cryogenic generator.
25 Le générateur de gaz est constitué par une simple colonne de séparation d'air, à l'intérieur d'une boîte froide 9, produisant de l'azote gazeux 11 en tête de colonne. Un détendeur 7 placé sur la conduite 3 de liquide détend le liquide destiné au vaporiseur 5.The gas generator is constituted by a simple air separation column, inside a cold box 9, producing nitrogen gas 11 at the top of the column. An expander 7 placed on the pipe 3 of liquid expands the liquid intended for the vaporizer 5.
30 Une connexion optionnelle d'azote liquide 8 vers la boîte froide 9 du générateur cryogénique assure au moins partiellement le maintien en froid du générateur par biberonnage. Le stockage est également relié au vaporiseur 5 par la conduite 3.An optional connection of liquid nitrogen 8 to cold box 9 of the cryogenic generator at least partially ensures that the generator is kept cold by bins. The storage is also connected to the vaporizer 5 via line 3.
5 2913104 Le vaporiseur est relié au client via une conduite 18. Entre les temps 0 et 10 heures de la Figure 4, du liquide 3 est soutiré du stockage 1, est détendu dans le détendeur 7, puis vaporisé (et réchauffé à la température ambiante) dans le système de vaporisation 5. La boîte 5 froide 9 ne fonctionne pas. Entre les temps 10 et 30 heures, le gaz provenant de la boîte froide 9 est envoyé dans le réseau client à travers la conduite 11. Aucun débit liquide provenant du stockage n'est vaporisé dans le vaporiseur 5. Entre les temps 30 et 40 heures, le gaz est produit à la fois par io vaporisation d'azote du stockage et par distillation, les deux débits étant mélangés en aval du vaporiseur 5 (ou éventuellement en amont comme décrit dans la demande de brevet FR0752579 déposée le 9 janvier 2007). Entre les temps 40 et 60 heures, le gaz provenant de la boîte froide 9 est envoyé dans le réseau client à travers la conduite 11. Aucun débit liquide 15 provenant du stockage n'est vaporisé dans le vaporiseur 5. Entre les temps 60 et 70 heures de la Figure 4, du liquide 3 est de nouveau soutiré du stockage 1, détendu dans le détendeur 7, puis vaporisé (et réchauffé à la température ambiante) dans le système de vaporisation 5. La boîte froide 9 ne fonctionne pas.The vaporizer is connected to the customer via line 18. Between the times 0 and 10 hours of Figure 4, liquid 3 is withdrawn from storage 1, is expanded in the expander 7, and then vaporized (and warmed to room temperature). ) in the vaporization system 5. The cold box 9 does not work. Between 10 and 30 hours, the gas from the cold box 9 is sent into the customer network through line 11. No liquid flow from the storage is vaporized in the vaporizer 5. Between 30 and 40 hours , the gas is produced by both vaporization of nitrogen from the storage and by distillation, the two flow rates being mixed downstream of the vaporizer 5 (or possibly upstream as described in the patent application FR0752579 filed January 9, 2007). Between times 40 and 60 hours, the gas from the cold box 9 is sent into the customer network through line 11. No liquid flow 15 from the storage is vaporized in the vaporizer 5. Between times 60 and 70 hours of Figure 4, the liquid 3 is again withdrawn from the storage 1, expanded in the expander 7, and then vaporized (and warmed to room temperature) in the vaporization system 5. The cold box 9 does not work.
20 Selon une variante de l'invention, l'appareil de séparation d'air produit un débit fixe avec une pression nominale de 8.3 barg (8.6 barg maxi). Il n'y a pas de marche réduite et le compresseur d'air de l'appareil de distillation est à vitesse fixe). Si le client ne prend pas tout l'azote produit par l'appareil, une partie 25 de l'azote est jetée à l'atmosphère, via un déverseur ou une vanne de régulation FV. Ceci permet de limiter la pression de la colonne (pression réseau N2) à une valeur limite (PSH, autour de 7.9 barg), sans devoir décharger le compresseur. Si le client a une consommation en pic, le surplus de débit vient du 30 stockage 1 via un détendeur de liquide 7 (ouverture vers 7.4 barg), ce qui permet de maintenir la pression dans le réseau client. • Mise en route : le client est fourni en liquide. 6 2913104 • Si la baisse de niveau du stockage LT s'effectue à une vitesse supérieure à un équivalent de débit de production jugé économique en fonction du coût de l'azote liquide et de l'énergie électrique (par exemple, 20% du débit nominal), le générateur est mis en route. Ce seuil de mise en 5 route pourra être paramétré via l'IHM. On pourra faire une moyenne glissante sur une à quelques heures pour estimer le débit moyen de consommation, de façon à obtenir une lecture lisible et fiable de la baisse de niveau. • Si la consommation du client baisse fortement, le générateur sera arrêté si le débit effectivement fourni au client par le générateur est inférieur io à un seuil de débit jugé non économique en fonction du coût de l'azote liquide et de l'énergie électrique (par exemple, 20% du débit nominal). Ce seuil d'arrêt pourra être paramétrable via IHM. On estime le débit rejeté à l'atmosphère en utilisant le fait que celui-ci est fonction du Cv de la vanne, de son ouverture, de la pression PT, et de la 15 température du gaz. On en déduit alors le débit effectivement fourni par le générateur au client, par différence du débit nominal de production du générateur et du débit rejeté à l'atmosphère. La mise en route du générateur, même en cas de consommation basse, peut être rendue nécessaire quand le stockage ne contient que peu 20 de liquide (par exemple 10% du niveau maximal) dans le stockage pour augmenter la durée de fourniture au client (via le générateur). La consommation d'azote liquide est alors limitée au biberonnage (s'il y en a). 7According to a variant of the invention, the air separation apparatus produces a fixed flow rate with a nominal pressure of 8.3 barg (8.6 barg max). There is no reduced running and the air compressor of the distillation apparatus is at a fixed speed). If the customer does not take all the nitrogen produced by the apparatus, a portion of the nitrogen is vented to the atmosphere via an overflow or FV control valve. This makes it possible to limit the pressure of the column (mains pressure N2) to a limit value (PSH, around 7.9 barg), without having to unload the compressor. If the client has a peak consumption, the excess flow comes from the storage 1 via a liquid expander 7 (opening to 7.4 barg), which maintains the pressure in the customer network. • Getting started: the customer is supplied with cash. 6 2913104 • If the level of LT storage declines at a rate greater than a production flow equivalent deemed economically based on the cost of liquid nitrogen and electrical energy (eg, 20% of nominal), the generator is started. This activation threshold can be parameterized via the HMI. A sliding average of one to a few hours can be used to estimate the average rate of consumption, so as to obtain a readable and reliable reading of the level drop. If the customer's consumption drops sharply, the generator will be shut down if the flow actually supplied to the customer by the generator is less than a threshold of flow deemed uneconomical according to the cost of the liquid nitrogen and the electrical energy ( for example, 20% of the nominal flow). This stop threshold can be parameterized via HMI. The discharge rate to the atmosphere is estimated using the fact that it is a function of the CV of the valve, its opening, the pressure PT, and the temperature of the gas. We then deduce the actual flow supplied by the generator to the customer, by difference of the nominal output rate of the generator and the discharge rate to the atmosphere. The start-up of the generator, even in the case of low consumption, may be necessary when the storage contains little liquid (for example 10% of the maximum level) in the storage to increase the duration of supply to the customer (via the generator). The consumption of liquid nitrogen is then limited to the bottle-feeding (if there is one). 7
Claims (9)
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0753567A FR2913104B1 (en) | 2007-02-28 | 2007-02-28 | PROCESS AND APPARATUS FOR SUPPLYING NITROGEN. |
| CN200880006178XA CN101711336B (en) | 2007-02-28 | 2008-02-18 | Method an apparatus for providing nitrogen |
| US12/528,713 US20110132035A1 (en) | 2007-02-28 | 2008-02-18 | Method And Apparatus For Providing Nitrogen |
| JP2009551936A JP2010521642A (en) | 2007-02-28 | 2008-02-18 | Method and apparatus for providing nitrogen |
| EP08762110A EP2129983A2 (en) | 2007-02-28 | 2008-02-18 | Method an apparatus for providing nitrogen |
| PCT/FR2008/050262 WO2008113928A2 (en) | 2007-02-28 | 2008-02-18 | Method an apparatus for providing nitrogen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0753567A FR2913104B1 (en) | 2007-02-28 | 2007-02-28 | PROCESS AND APPARATUS FOR SUPPLYING NITROGEN. |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| FR2913104A1 true FR2913104A1 (en) | 2008-08-29 |
| FR2913104B1 FR2913104B1 (en) | 2009-11-27 |
Family
ID=38752525
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| FR0753567A Expired - Fee Related FR2913104B1 (en) | 2007-02-28 | 2007-02-28 | PROCESS AND APPARATUS FOR SUPPLYING NITROGEN. |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20110132035A1 (en) |
| EP (1) | EP2129983A2 (en) |
| JP (1) | JP2010521642A (en) |
| CN (1) | CN101711336B (en) |
| FR (1) | FR2913104B1 (en) |
| WO (1) | WO2008113928A2 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5425612B2 (en) * | 2009-12-24 | 2014-02-26 | 住友重機械工業株式会社 | Ozone gas concentrator |
| FR3069237B1 (en) * | 2017-07-19 | 2019-08-23 | Gaztransport Et Technigaz | DEVICE FOR THE PRODUCTION AND DISTRIBUTION OF NITROGEN, PARTICULARLY FOR A TRANSPORT VESSEL OF LIQUEFIED GAS |
| CN116105074B (en) * | 2022-12-07 | 2024-03-08 | 北京航天试验技术研究所 | High-pressure nitrogen gas supply device and control method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5157927A (en) * | 1990-04-10 | 1992-10-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the production of gaseous nitrogen and system for supplying corresponding nitrogen |
| EP0538857A1 (en) * | 1991-10-25 | 1993-04-28 | Linde Aktiengesellschaft | Installation for the low temperature separation |
| US6273936B1 (en) * | 1998-10-09 | 2001-08-14 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for producing a variable gas output |
| US20050172666A1 (en) * | 2002-07-09 | 2005-08-11 | Alain Guillard | Method of operating a production plant and production plant |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2129115B (en) * | 1982-10-27 | 1986-03-12 | Air Prod & Chem | Producing gaseous nitrogen |
| JP2873473B2 (en) * | 1989-11-07 | 1999-03-24 | 株式会社大分サンソセンター | Air liquefaction separation method |
| JP3220755B2 (en) * | 1991-09-27 | 2001-10-22 | 日本酸素株式会社 | Air liquefaction separation method and apparatus |
| JPH0829055A (en) * | 1994-07-13 | 1996-02-02 | Toshiba Corp | Operation control device for oxygen production plant |
| JPH1144470A (en) * | 1997-07-24 | 1999-02-16 | Mitsui Eng & Shipbuild Co Ltd | Simultaneous supply of fresh water and cold water |
| JP4450503B2 (en) * | 2000-12-14 | 2010-04-14 | 日本エア・リキード株式会社 | Product gas backup device |
| CN1223786C (en) * | 2002-12-20 | 2005-10-19 | 中国科学院理化技术研究所 | Gasification device for cold storage type low-temperature liquid |
| FR2872262B1 (en) * | 2004-06-29 | 2010-11-26 | Air Liquide | METHOD AND INSTALLATION FOR PROVIDING SUPPORT OF A PRESSURIZED GAS |
| US7249470B2 (en) * | 2005-04-07 | 2007-07-31 | Praxair Technology, Inc. | Method of controlling liquid production utilizing an expert system controller |
-
2007
- 2007-02-28 FR FR0753567A patent/FR2913104B1/en not_active Expired - Fee Related
-
2008
- 2008-02-18 EP EP08762110A patent/EP2129983A2/en not_active Withdrawn
- 2008-02-18 JP JP2009551936A patent/JP2010521642A/en active Pending
- 2008-02-18 US US12/528,713 patent/US20110132035A1/en not_active Abandoned
- 2008-02-18 WO PCT/FR2008/050262 patent/WO2008113928A2/en not_active Ceased
- 2008-02-18 CN CN200880006178XA patent/CN101711336B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5157927A (en) * | 1990-04-10 | 1992-10-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the production of gaseous nitrogen and system for supplying corresponding nitrogen |
| EP0538857A1 (en) * | 1991-10-25 | 1993-04-28 | Linde Aktiengesellschaft | Installation for the low temperature separation |
| US6273936B1 (en) * | 1998-10-09 | 2001-08-14 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for producing a variable gas output |
| US20050172666A1 (en) * | 2002-07-09 | 2005-08-11 | Alain Guillard | Method of operating a production plant and production plant |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101711336A (en) | 2010-05-19 |
| JP2010521642A (en) | 2010-06-24 |
| CN101711336B (en) | 2012-09-05 |
| WO2008113928A2 (en) | 2008-09-25 |
| EP2129983A2 (en) | 2009-12-09 |
| US20110132035A1 (en) | 2011-06-09 |
| WO2008113928A3 (en) | 2010-03-11 |
| FR2913104B1 (en) | 2009-11-27 |
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