CN101711336A - Method an apparatus for providing nitrogen - Google Patents
Method an apparatus for providing nitrogen Download PDFInfo
- Publication number
- CN101711336A CN101711336A CN200880006178A CN200880006178A CN101711336A CN 101711336 A CN101711336 A CN 101711336A CN 200880006178 A CN200880006178 A CN 200880006178A CN 200880006178 A CN200880006178 A CN 200880006178A CN 101711336 A CN101711336 A CN 101711336A
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- CN
- China
- Prior art keywords
- nitrogen
- user
- threshold value
- equipment
- gaseous
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 217
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 109
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 238000001704 evaporation Methods 0.000 claims description 15
- 230000008020 evaporation Effects 0.000 claims description 15
- 238000004821 distillation Methods 0.000 claims description 9
- 230000005611 electricity Effects 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 238000009834 vaporization Methods 0.000 abstract 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 1
- 239000001257 hydrogen Substances 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 9
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 230000004913 activation Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Images
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
-
- 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
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- 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
-
- 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
-
- 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
-
- 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
The invention relates to a method for providing hydrogen using a gaseous-nitrogen production apparatus (9) by air separation and vaporisation of liquid nitrogen from a feedstock (1), wherein if the needs of a client for gaseous nitrogen are lower than a first threshold, the client is supplied with nitrogen exclusively by vaporisation of liquid nitrogen, and if the needs of a client for gaseous nitrogen are higher than a second threshold, the second threshold being higher than the first threshold, the client is supplied with nitrogen at least partially by the nitrogen production apparatus.
Description
Technical field
The present invention relates to a kind of method and apparatus that is used to provide nitrogen.Usually by gas generating equipment, cryogenic distillation of air equipment for example, and the nitrogen storage device of supplying gaseous nitrogen to the user when Cryo Equipment is not worked and/or can not produce whole required flow rate is supplied nitrogen to the user.
According to the present invention, only just open gas generating equipment when being supplied to the user more economical at using gases storage device (with gaseous state or liquid form).
Background technology
As shown in Figure 1, according to prior art, the gas generator A that is used in particular for the unit on the user place is connected in the urgent/emergent feeding mechanism B of " (vrac) in bulk " type (liquid or gas with evaporimeter) usually.
This generator always is in via pipeline C, E and is supplied under user's the condition.When the user consumed above rated capacity (100%), the emergency service device started, and via pipeline D, E transmission nitrogen.
Equally, when generator was not worked, the emergency service device was just taken over (work).
In this operational mode, all start generator no matter how much consumption of user is.In comparing user's consumption stage low with the rated capacity of generator, energy consumption and therefore production cost be not the best.
Fig. 3 illustrates this method of operation according to prior art.At the moment 0 place, the nitrogen that the user consumes is 20Nm
3/ h, this flow supply by having the airdistillation that simple liquid injects the separation equipment of tower fully.When user's consumption increased, the output of this equipment was increased to the 40Nm that located at 10 hours
3/ h also is increased to the 100Nm that located at 20 hours subsequently
3/ h.Now, the consumption as the user reaches 150Nm
3During/h, separation equipment is with its maximum flow rate 100Nm
3/ h continues to produce, and remaining flow rate provides by the evaporation of the nitrogen of storage, to produce 50Nm
3The flow rate of/h.
Be reduced to 80Nm when locating at 50 hours to consume
3During/h, stop to produce nitrogen, and reduce to 80Nm by the nitrogen of distillation equipment production by evaporation
3/ h.Subsequently, in order to follow user's consumption, the level of production of equipment reduces to 40Nm
3/ h and reduce to 20Nm then
3/ h.
Summary of the invention
According to one object of the present invention, provide a kind of being used for to produce the equipment of gaseous nitrogen and the method for supplying nitrogen by the evaporation of liquid nitrogen by air separation, wherein:
If a) user is lower than first threshold to the demand of gaseous nitrogen, so only supply nitrogen to the user by the evaporation of liquid nitrogen,
B) if the user is higher than second threshold value to the demand of gaseous nitrogen, this second threshold value is greater than first threshold, supplies nitrogen by the described equipment that is used to produce nitrogen to the user so at least in part.
According to other purpose of the present invention:
If-user surpasses the 3rd threshold value to the demand of nitrogen, the 3rd threshold value is greater than second threshold value, so partly by describedly being used to produce the equipment of nitrogen, partly supplying the user by the evaporation of liquid nitrogen;
If-user's demand is between second threshold value and the 3rd threshold value, so only by the described supply of equipment user who is used to produce nitrogen;
If-user greater than second threshold value, so only supplies nitrogen by the described equipment that is used to produce nitrogen to the user to the demand of gaseous nitrogen;
In-first threshold, second threshold value, the 3rd threshold value at least one is according to the price of the price of electricity and/or liquid nitrogen and/or be connected in the amount of the liquid nitrogen in the storage container of vaporising device and/or the rate of change of the amount of the liquid nitrogen in the described storage container changes;
If greater than second threshold value or greater than second threshold value but less than the 3rd threshold value, the then described equipment that is used to produce nitrogen is produced gaseous nitrogen with constant substantially flow rate to-user to the demand of gaseous nitrogen, and
If a) user is lower than this constant substantially flow rate to the demand of gaseous nitrogen, then with gaseous nitrogen unnecessary/exceed partial discharge in atmosphere, and remaining gaseous nitrogen is transferred to the user;
B) if the user to the demand of gaseous nitrogen more than or equal to this constant substantially flow rate, then whole gaseous nitrogen flows are flowed to the user;
-described the equipment that is used to produce gaseous nitrogen is cryogenic distillation of air equipment, liquid nitrogen can be transferred to if necessary/when needed describedly to be used to produce the equipment of gaseous nitrogen so that participate in keeping this equipment colder.
According to other purpose of the present invention, a kind of equipment that is used to supply gaseous nitrogen is provided, and this equipment comprises the equipment that is used for producing by air separation gaseous nitrogen, the liquid nitrogen evaporimeter, storage container, be used for to supply to the device of evaporimeter from the liquid nitrogen of storage container, be used for gaseous nitrogen is transferred to from production equipment user's device, be used for gaseous nitrogen is transferred to from evaporimeter user's device, and be used for regulating one device at least in the gaseous nitrogen stream that is transferred to the user according to the rate of change of the amount of liquid nitrogen in the amount of the liquid nitrogen of the price of the price of electricity and/or liquid nitrogen and/or storage container and/or the storage container.
When needed, the described equipment that is used to produce gaseous nitrogen is cryogenic distillation of air equipment.
Description of drawings
Describe the present invention in detail below in conjunction with accompanying drawing.
Fig. 2 is the equipment that is used to supply nitrogen according to of the present invention.Fig. 4 is the schematic diagram of operational mode that utilizes this equipment of the method according to this invention.
The specific embodiment
According to this invention, propose to put upside down existing basic principle.Substantially supply with the user by " in bulk " emergency service device.When user's demand surpassed particular value, generator replaced " in bulk " supply.This particular value is defined as and makes the production cost of generator supply more economically than " in bulk ".This depends on the cost of energy and the cost of supply in bulk.
When surpassing the production capacity of generator, " in bulk " supply replenishes the production of generator to be supplied to the user.
Like this, as can be seen from Figure 4, at the moment 0 place, the nitrogen that the user consumes is 20Nm
3/ h, this flow provide by making from the nitrogen of storage container evaporation (perhaps can by the inflow from the gaseous nitrogen of pipe network/network (r é seau)) fully.Then, user's consumption located to increase to 40Nm at 10 hours
3/ h, nitrogen evaporate full cut-off to be ended, and the production of distillation equipment is with 40Nm
3/ h begins, and reaches 100Nm after 20 hours
3/ h.Now, the consumption as the user reaches 150Nm
3During/h, separation equipment continues to produce its 100Nm
3The maximum stream flow of/h.All the other evaporations by the nitrogen that stores provide to produce 50Nm
3The flow rate of/h.
Reduce to 80Nm when consuming 50 hours the moment
3During/h, stop to produce nitrogen by evaporation, the production of the nitrogen by distillation equipment is reduced to 80Nm
3/ h.Subsequently, in order to follow user's consumption, the level of production of this equipment is decreased to 40Nm
3/ h.Surpass this value, airdistillation stops, and for 20Nm
3/ h provides user's basic consumption, the evaporation of restarting liquid nitrogen.
According to the present invention, for 40Nm
3/ h and 100Nm
3Value between the/h, air separation equipment can accurately be produced the consumption of needs according to the present invention.As shown in Figure 2, complete assembly 6 comprises at least one ice chest 9 of liquid nitrogen storage container 1 and cryogenerator.
Gas generator comprises the simple air separation of ice chest 9 inside, produces gaseous nitrogen 11 at the place, top of this tower.
The ice chest 9 that liquid nitrogen 8 is connected to alternatively cryogenerator guarantees that at least in part generator keeps colder by the liquid injection.
Storage container also is connected in evaporimeter 5 by pipeline 3.
This evaporimeter is connected in the user by pipeline 18.
Between 0 hour and 10 hours, liquid 3 is extracted from storage container 1 in Fig. 4, expands in expansion valve 7, then evaporation in vapo(u)rization system 5 (and being heated to environment temperature again).Ice chest 9 does not move.
Between 10 hours and 30 hours, be transferred to user's pipe network by pipeline 11 from the gas of ice chest 9.In evaporimeter 5, do not evaporate from the liquid flow of storage container.
Between 30 hours and 40 hours, by producing nitrogen simultaneously from the evaporation of the nitrogen of storage container with by distillation, this two plume is in the mixed downstream of evaporimeter 5 (or describe among the patent application FR 0752579 that also can submit to as on January 9th, 2007 in combined upstream).
Between 40 hours and 60 hours, be transferred to user's pipe network by pipeline 11 from the gas of ice chest 9.The liquid stream from storage container does not evaporate in evaporimeter 5.
Between 60 hours and 70 hours in Fig. 4, liquid 3 is extracted from storage container 1 once more, and the pressure of this liquid reduces in expansion valve 7, then evaporation in vapo(u)rization system 5 (and being heated to environment temperature again).Ice chest 9 is not worked.
According to modification of the present invention, it is the 8.3barg firm discharge of (being 8.6barg to the maximum) that air separation equipment produces nominal pressure.Be not speed operation, and the air compressor of air distillation installation is in fixing speed to reduce.
All nitrogen that this equipment is produced if the user does not use up, then a part of nitrogen is discharged in the atmosphere by dump valve or control valve FV.This makes it possible to the pressure of this tower (ductwork pressure N2) is restricted to a limiting value (PSH, about 7.9barg), and needn't discharge compressor.
If the user has peak value consumption, from storage container 1, this makes it possible to keep the pressure in user's pipe network to superfluous flow via liquid pressure reducer 7 (opening when about 7.4barg).
Start: give user's feed fluid.
Generator starting when if the liquid level among the storage container LT descends with the speed that is judged to be economic equivalent throughput rate (for example 20% of crest speed) greater than the cost according to liquid nitrogen and electric energy.This activation threshold parameter can be set up by IHM.Can set up moving average during several hours so that estimation/estimation mean consumption speed at one, thereby obtain the clear and reliable reading that liquid level descends.
If user's consumption sharply reduces, generator will stop when the flow that is offered the user by generator is judged to be uneconomic flow threshold (for example 20% of crest speed) less than the cost according to liquid nitrogen and electric energy.This outage threshold parameter can be set up by IHM.
The flow that is discharged into atmosphere is estimated by such fact: this flow depends on the Cv value of valve and aperture, pressure P T and the gas temperature of valve.Then, the actual flow that is offered the user by generator is known by inference with the difference that is discharged into the flow in the atmosphere by the specified production flow from generator.
Even under low consumed situation, when storage container only holds seldom liquid (for example 10% of maximum level), also need to start generator, so that (via generator) increases the duration of user's supply.So, the consumption of liquid nitrogen is confined to liquid injection (if any).
Claims (7)
1. one kind is used for producing the method that nitrogen is supplied in the evaporation of the equipment (9) of gaseous nitrogen and liquid nitrogen by air separation, wherein:
If a) user is lower than first threshold to the demand of gaseous nitrogen, so only supply nitrogen to the user by the evaporation of liquid nitrogen,
B) if the user is higher than second threshold value to the demand of gaseous nitrogen--this second threshold value is greater than described first threshold, supplies nitrogen by the described equipment that is used to produce nitrogen to the user so at least in part.
2. the method for supply nitrogen according to claim 1, it is characterized in that, if the user surpasses the 3rd threshold value to the demand of nitrogen, the 3rd threshold value is greater than described second threshold value, so partly by the described equipment (9) that is used to produce nitrogen, partly supply the user by the evaporation of liquid nitrogen.
3. method according to claim 2 is characterized in that, user's demand is between described second threshold value and the 3rd threshold value, and only by described equipment (9) the supply user who is used to produce nitrogen.
4. method according to claim 1 is characterized in that, if the user to the demand of gaseous nitrogen greater than described second threshold value, so only supply nitrogen to the user by the described equipment (9) that is used to produce nitrogen.
5. according to the described method of one of aforementioned claim, it is characterized in that at least one in described first threshold, second threshold value, the 3rd threshold value is according to the price of the price of electricity and/or liquid nitrogen and/or be connected in the amount of the liquid nitrogen in the storage container (1) of vaporising device (5) and/or the rate of change of the amount of the liquid nitrogen in the described storage container changes.
6. according to the described method of one of aforementioned claim, it is characterized in that, if greater than described second threshold value and when needed less than described the 3rd threshold value, the then described equipment that is used to produce nitrogen is produced gaseous nitrogen with constant substantially flow rate to the user to the demand of gaseous nitrogen, and
If a) user is lower than this constant substantially flow rate to the demand of gaseous nitrogen, then the redundance with gaseous nitrogen is discharged in the atmosphere, and remaining gaseous nitrogen is transferred to the user;
B) if the user to the demand of gaseous nitrogen more than or equal to this constant substantially flow rate, then whole gaseous nitrogen flows are flowed to the user.
7. according to the described method of one of aforementioned claim, it is characterized in that, the described equipment that is used to produce gaseous nitrogen is cryogenic distillation of air equipment (9), and liquid nitrogen can be transferred to when needed and describedly be used to produce the equipment of gaseous nitrogen so that keep this equipment colder.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0753567A FR2913104B1 (en) | 2007-02-28 | 2007-02-28 | PROCESS AND APPARATUS FOR SUPPLYING NITROGEN. |
| FR0753567 | 2007-02-28 | ||
| PCT/FR2008/050262 WO2008113928A2 (en) | 2007-02-28 | 2008-02-18 | Method an apparatus for providing nitrogen |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101711336A true CN101711336A (en) | 2010-05-19 |
| CN101711336B CN101711336B (en) | 2012-09-05 |
Family
ID=38752525
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200880006178XA Expired - Fee Related CN101711336B (en) | 2007-02-28 | 2008-02-18 | Method an apparatus for providing 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) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110958989A (en) * | 2017-07-19 | 2020-04-03 | 气体运输技术公司 | Device for producing and distributing nitrogen, in particular for a liquefied gas vessel |
Families Citing this family (2)
| 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 |
| 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 |
Family Cites Families (13)
| 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 |
| FR2660741A1 (en) * | 1990-04-10 | 1991-10-11 | Air Liquide | PROCESS AND PLANT FOR GENERATING GASEOUS NITROGEN AND CORRESPONDING NITROGEN SUPPLY SYSTEM THEREFOR. |
| JP3220755B2 (en) * | 1991-09-27 | 2001-10-22 | 日本酸素株式会社 | Air liquefaction separation method and apparatus |
| DE4135302A1 (en) * | 1991-10-25 | 1993-04-29 | Linde Ag | DEVICE FOR LOW TEMPERATURE DISPOSAL OF AIR |
| JPH0829055A (en) * | 1994-07-13 | 1996-02-02 | Toshiba Corp | Operation controller for oxygen manufacturing plant |
| JPH1144470A (en) * | 1997-07-24 | 1999-02-16 | Mitsui Eng & Shipbuild Co Ltd | Distilled water and method of supplying distilled water and cool water simultaneously |
| FR2784308B1 (en) * | 1998-10-09 | 2001-11-09 | Air Liquide | GAS SEPARATION PROCESS AND PLANT WITH PRODUCTION OF A VARIABLE GAS FLOW |
| JP4450503B2 (en) * | 2000-12-14 | 2010-04-14 | 日本エア・リキード株式会社 | Product gas backup device |
| FR2842124B1 (en) * | 2002-07-09 | 2005-03-25 | Air Liquide | METHOD FOR CONDUCTING AN ELECTRIC POWER GAS-GENERATING PLANT AND THIS PRODUCTION PLANT |
| CN1223786C (en) * | 2002-12-20 | 2005-10-19 | 中国科学院理化技术研究所 | Gasifier of 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 CN CN200880006178XA patent/CN101711336B/en not_active Expired - Fee Related
- 2008-02-18 EP EP08762110A patent/EP2129983A2/en not_active Withdrawn
- 2008-02-18 WO PCT/FR2008/050262 patent/WO2008113928A2/en active Application Filing
- 2008-02-18 JP JP2009551936A patent/JP2010521642A/en active Pending
- 2008-02-18 US US12/528,713 patent/US20110132035A1/en not_active Abandoned
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110958989A (en) * | 2017-07-19 | 2020-04-03 | 气体运输技术公司 | Device for producing and distributing nitrogen, in particular for a liquefied gas vessel |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2913104B1 (en) | 2009-11-27 |
| EP2129983A2 (en) | 2009-12-09 |
| CN101711336B (en) | 2012-09-05 |
| WO2008113928A3 (en) | 2010-03-11 |
| JP2010521642A (en) | 2010-06-24 |
| WO2008113928A2 (en) | 2008-09-25 |
| US20110132035A1 (en) | 2011-06-09 |
| FR2913104A1 (en) | 2008-08-29 |
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