NO137565B - PROCEDURE AND AIR SEPARATION APPLIANCE - Google Patents
PROCEDURE AND AIR SEPARATION APPLIANCE Download PDFInfo
- Publication number
- NO137565B NO137565B NO741307A NO741307A NO137565B NO 137565 B NO137565 B NO 137565B NO 741307 A NO741307 A NO 741307A NO 741307 A NO741307 A NO 741307A NO 137565 B NO137565 B NO 137565B
- Authority
- NO
- Norway
- Prior art keywords
- air
- nitrogen
- oxygen
- rectification column
- heat exchanger
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims description 13
- 238000000926 separation method Methods 0.000 title description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 87
- 229910052757 nitrogen Inorganic materials 0.000 claims description 42
- 239000007788 liquid Substances 0.000 claims description 31
- 229910052760 oxygen Inorganic materials 0.000 claims description 24
- 239000001301 oxygen Substances 0.000 claims description 24
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 23
- 238000001816 cooling Methods 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000011261 inert gas Substances 0.000 description 6
- 238000010992 reflux Methods 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 3
- 239000002360 explosive Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 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
-
- 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
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04975—Construction and layout of air fractionation equipments, e.g. valves, machines adapted for special use of the air fractionation unit, e.g. transportable devices by truck or small scale use
- F25J3/04987—Construction and layout of air fractionation equipments, e.g. valves, machines adapted for special use of the air fractionation unit, e.g. transportable devices by truck or small scale use for offshore use
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
-
- 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
- F25J2250/40—One fluid being air
-
- 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
- F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
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)
- Percussion Or Vibration Massage (AREA)
- Separating Particles In Gases By Inertia (AREA)
Description
Oppfinnelsen vedrører en fremgangsmåte for separering av luft hvor luft komprimeres, avkjøles i en varmeveksler og føres til en rektifiseringskdlonne, i hvilken trykket er i det vesentlige det samme som det trykk til hvilket den innkomne luft komprimeres, og i hvilken den innkomne luft separeres til nitrogendamp og en oksygenanriket væske, og hvor oksygenanriket væske føres gjennom en ekspansjonsventil (Joule-Thomson-ventil) og bringes i varmeutveksling med en del av nitrogendampen for å tilveiebringe en tilbakestrømning som innføres i rektifiseringskolonnen. Oppfinnelsen vedrører også et apparat for gjennomfør-ing av fremgangsmåten. The invention relates to a process for separating air where air is compressed, cooled in a heat exchanger and fed to a rectification boiler, in which the pressure is substantially the same as the pressure to which the incoming air is compressed, and in which the incoming air is separated into nitrogen vapor and an oxygen-enriched liquid, and wherein the oxygen-enriched liquid is passed through an expansion valve (Joule-Thomson valve) and brought into heat exchange with a portion of the nitrogen vapor to provide a reflux which is introduced into the rectification column. The invention also relates to an apparatus for carrying out the method.
Hensikten med en slik separering av luft er å tilføre nitrogen til bruk f. eks. til reduksjon av brennbarheten av en gassblanding i slike beholdere som lasterom, rom eller andre deler av skip, særlig oljetanker eller naturgasstanker, og på land anordnede installasjoner, såsom oljetanker. The purpose of such a separation of air is to supply nitrogen for use, e.g. to reduce the flammability of a gas mixture in such containers as holds, rooms or other parts of ships, in particular oil tanks or natural gas tanks, and land-based installations, such as oil tanks.
Hydrokarbondamper i slike tankskip og lagringstanker har en tendens til å blande seg med oksygen i luften og gi eksplosive blandinger. Den vanlige måte å forhindre en slik eksplosjon er å sikre at det ikke oppnås eksplosive konsentrasjoner. Hydrocarbon vapors in such tankers and storage tanks tend to mix with oxygen in the air and form explosive mixtures. The usual way to prevent such an explosion is to ensure that explosive concentrations are not reached.
En fremgangsmåte har vært å opprettholde en inert atmosfære i tankene ved dannelsen av en inert gass og innføre den i tanken når op<p>byggingen av en eksplosiv blanding enten er ventet eller vist av en registreringsinnretning. One method has been to maintain an inert atmosphere in the tanks by the formation of an inert gas and introduce it into the tank when the build-up of an explosive mixture is either expected or shown by a recording device.
I et skjent system fremstilles flytende nitrogen enten ombord på skip eller det oppnås fra på land anordnede forråd og fordampes ved behov. Denne metode har den. ulempe at flytende nitrogen som produseres ombord på skip krever et relativt høyt energiforbruk, og forrås på land medfører vanligvis høye tran-sportkostnader og lagringsvanskeligheter. I et annet kjent sy-stem blir inert gass fremstilt i store mengder av forbrennings-produktene til skipsmotorer eller fra spesielt utformede brenne-re. Inert gass fra slike kilder inneholder en stor andel karbondioksyd som kan reagere med visse laster og kan inneholde korrosive oksyder, f. eks. av svovel eller vanadium. Et annet potensielt problem er at en kontinuerlig krets eksisterer mellom forbrenningssonen og den del av beholderen hvor man vil hindre en eksplosjon. Foreliggende oppfinnelse vedrører en fremgangsmåte og et apparat for dannelse av nitrogen, som er særlig egnet for anvendelse ombord på skip. In a conventional system, liquid nitrogen is produced either on board a ship or it is obtained from stores arranged on land and vaporized when needed. This method has it. disadvantage is that liquid nitrogen produced on board ships requires a relatively high energy consumption, and supply on land usually entails high transport costs and storage difficulties. In another known system, inert gas is produced in large quantities from the combustion products of ship engines or from specially designed burners. Inert gas from such sources contains a large proportion of carbon dioxide which can react with certain loads and can contain corrosive oxides, e.g. of sulfur or vanadium. Another potential problem is that a continuous circuit exists between the combustion zone and the part of the container where an explosion is to be prevented. The present invention relates to a method and an apparatus for the formation of nitrogen, which is particularly suitable for use on board ships.
Ifølge oppfinnelsen er det tilveiebragt en fremgangsmåte for separering av luft hvor luft komprimeres, avkjøles i en varmeveksler og føres til en rektifiseringskoionne, i hvilken trykket er i det vesentlige det samme som det trykk til hvilket den■innkomne luft komprimeres, og i hvilken den innkomne luft separeres til nitrogendamp og. en oksygenanriket væske, og hvor oksygenanriket væske føres gjennom en ekspansjonsventil (Joule-Thomson-ventil)- og bringes i varmeutveksling med en del av nitrogendampen for å tilveiebringe en tilbakestrømning som innføres i rektifiseringskolonnen. Fremgangsmåten er kjennetegnet ved at flytende nitrogen fra et forråd innføres i rektifiseringskolonnen for å tilveiebringe en kjøling i denne. According to the invention, a method for separating air is provided in which air is compressed, cooled in a heat exchanger and led to a rectification coionne, in which the pressure is essentially the same as the pressure to which the incoming air is compressed, and in which the incoming air air is separated into nitrogen vapor and. an oxygen-enriched liquid, and where the oxygen-enriched liquid is passed through an expansion valve (Joule-Thomson valve) - and brought into heat exchange with part of the nitrogen vapor to provide a reflux which is introduced into the rectification column. The method is characterized by the fact that liquid nitrogen from a supply is introduced into the rectification column to provide cooling in it.
Oppfinnelsen vedrører også et apparat for gjennomfør-ing av fremgangsmåtén, hvilket apparat innbefatter en luftkompressor, en varmeveksler for kjølin<q> av den komprimerte luft, en rektifiseringskoionne som drives ved i det vesentlige det samme trykk som trykket for den komprimerte luft for å separere den komprimerte luft til nitrogendamp og en oksygenanriket væske, en ekspansjonsventil som ekspanderer den oksygenanrikede væske og en varmeveksler for indirekte kontakt mellom den ekspanderte-oksygenanrikede væske , og en del av nitrogendampen for å frembringe en tilbakestrømning av nitrogen som blir gjeninnført i rektifiseringskolonnen. Apparatet er kjennetegnet ved en lagringstank for flytende nitrogen, tilknyttet rektifiseringskolonnen for inn-føring av flytende nitrogen i rektifiseringskolonnen. The invention also relates to an apparatus for carrying out the method, which apparatus includes an air compressor, a heat exchanger for cooling <q> of the compressed air, a rectification ion which is operated at essentially the same pressure as the pressure of the compressed air to separate the compressed air to nitrogen vapor and an oxygen-enriched liquid, an expansion valve that expands the oxygen-enriched liquid and a heat exchanger for indirect contact between the expanded-oxygen-enriched liquid, and part of the nitrogen vapor to produce a return flow of nitrogen that is reintroduced into the rectification column. The device is characterized by a storage tank for liquid nitrogen, connected to the rectification column for introducing liquid nitrogen into the rectification column.
Den innkomne luft er fordelaktig komprimert til et lavt trykk, typisk i området 2-4 bar. En etterkjøler, f. eks. en varmeveksler, i hvilken komprimert luft blir bragt i indirekte kontakt med kjølevann kan hvis ønsket anordnes for å fjerne var-men fra kompresjonen, men i mange tilfeller, særlig hvis kompresjonen er mindre enn 4 bar, gir dette små fordeler. The incoming air is advantageously compressed to a low pressure, typically in the range of 2-4 bar. An aftercooler, e.g. a heat exchanger in which compressed air is brought into indirect contact with cooling water can, if desired, be arranged to remove heat from the compression, but in many cases, especially if the compression is less than 4 bar, this gives little advantage.
Luftkompresjonen kan utføres i en kompressor som også kan benyttes til andre formål, f. eks. til å pumpe frisk luft inn i en beholder for å blåse ut inert gass..-'fra denne. I et slikt tilfelle benyttes luftkompressoren alternativt til drift av systemet for å tilveiebringe nitrogen for å gjøre beholderen inert og ved den etterfølgende fjerning av inert gass. The air compression can be carried out in a compressor which can also be used for other purposes, e.g. to pump fresh air into a container to blow out inert gas..-'from this. In such a case, the air compressor is used alternatively to operate the system to provide nitrogen to make the container inert and in the subsequent removal of inert gas.
Slik alternativ drift kan være nødvendig når det må utøves reparasjoner i det indre av beholderen. Such alternative operation may be necessary when repairs have to be carried out in the interior of the container.
Hovedvarmeveksleren for kjøling av den innkomne luft er fordelaktig en omvendt varmeveksler. Denne vil vanligvis bli avkjølt såvel av den oksygenanrikede strøm og en annen del av nitrogendampstrømmen, hvilken del ikke er returnert til rektifiseringskolonnen som tilbakestrømning, men fordeles på en ønsket måte. Den oksygenanrikede strøm som forlater hovedvarmeveksleren vil vanligvis bli kassert. The main heat exchanger for cooling the incoming air is advantageously a reverse heat exchanger. This will usually be cooled both by the oxygen-enriched stream and another part of the nitrogen vapor stream, which part is not returned to the rectification column as reflux, but is distributed in a desired way. The oxygen-enriched stream leaving the main heat exchanger will usually be discarded.
Den avkjølte luft som forlater hovedvarmeveksleren føres direkte til rektifiseringskolonnen uten å gå gjennom noe ekspansjonstrinn. The cooled air leaving the main heat exchanger is fed directly to the rectification column without going through any expansion stage.
Selv om det kan benyttes en dobbelt rektifiseringskoionne, er en enkel kolonne velegnet for de fleste formål, da det vanligvis bare er nødvendig å konsentrere den oksygenanrikede væske til et oksygeninnhold i området 35 - 40 %. En enkelt kolonne kan lett drives til å gi meget ren nitrogendamp, vanligvis bedre enn 99,5 % renhet. Although a double rectifier column can be used, a single column is suitable for most purposes, as it is usually only necessary to concentrate the oxygenated liquid to an oxygen content in the range of 35 - 40%. A single column can easily be operated to provide very pure nitrogen vapor, usually better than 99.5% purity.
Hvis hovedvarmeveksleren er av den reverserende type, vil den bevirke fjerningen av vanndamp og karbondioksyd fra den innkomne luft. Hvis det benyttes en annen type varmeveksler, er det fordelaktig anordnet et adsorbsjons- eller absorbsjonssystem for å fjerne vanndamp og karbondioksyd enten før den innkomne luft når hovedvarmeveksleren eller på et sted på denne. If the main heat exchanger is of the reversing type, it will effect the removal of water vapor and carbon dioxide from the incoming air. If another type of heat exchanger is used, an adsorption or absorption system is advantageously arranged to remove water vapor and carbon dioxide either before the incoming air reaches the main heat exchanger or somewhere on it.
I noen tilfeller er det nødvendig å oppvarme en eller begge strømmer av oksygenanriket væske og nitrogendamp før de går inn i hovedvarmeveksleren for å hindre kjøling av den innkomne luft til en for lav temperatur før inngangen til rektifiseringskolonnen. Varmingen kan utøves med en varmeveksler i hvilken den oksygenanrikede strøm og nitrogendampen bringes i indirekte kontakt med relativt varm luft som tas fra den komprimerte strøm som går inn i rektifiseringskolonnen. Den således avkjølte luft blir så ført tilbake til rektifiseringskolonnen ved et nivå nær det hvor resten av den komprimerte strøm innføres. In some cases, it is necessary to heat one or both streams of oxygen-enriched liquid and nitrogen vapor before entering the main heat exchanger to prevent cooling of the incoming air to too low a temperature before entering the rectification column. The heating may be effected with a heat exchanger in which the oxygen-enriched stream and nitrogen vapor are brought into indirect contact with relatively hot air taken from the compressed stream entering the rectification column. The thus cooled air is then returned to the rectification column at a level close to that where the rest of the compressed stream is introduced.
Flytende nitrogen innføres fra forrådet til rektifiseringskolonnen og utgjør størstedelen av kuldebehovet til pro-■ sessen. Mengden av flytende nitrogen som er nødvendig avhenger av forskjellige faktorer, innbefattende effektiviteten til utsty-ret, men er vanligvis ved jevn drift mellom 5 og 10 % (målt som damp) av volumet av oppnådd nitrogengass i tidsenheten for rektifiseringskolonnen. Liquid nitrogen is introduced from the supply to the rectification column and makes up the majority of the cooling requirement for the process. The amount of liquid nitrogen required depends on various factors, including the efficiency of the equipment, but is usually at steady operation between 5 and 10% (measured as vapor) of the volume of nitrogen gas obtained in the unit time of the rectification column.
Det lagrede flytende nitrogen kan hvis ønsket bli fremstilt i et lite luftsepareringsanlegg som kjører over lengre perioder i forhold til driftsperioden for luftsepareringsanleg-get ifølge oppfinnelsen. For inertgjøring av en~tank med et slikt system kan det lille anlegg benyttes til å bygge opp over en lengre periode det volum av lagret flytende nitrogen-som så trekkes ut når det er nødvendig å drive det større luftsepareringsanlegg for å gi en høy hastighet"for nitrogenutlevering over en kort periode. The stored liquid nitrogen can, if desired, be produced in a small air separation plant which runs for longer periods in relation to the operating period of the air separation plant according to the invention. For the inerting of a tank with such a system, the small plant can be used to build up over a longer period the volume of stored liquid nitrogen - which is then withdrawn when it is necessary to operate the larger air separation plant to give a high speed" for nitrogen delivery over a short period.
Oppfinnelsen er særlig . fordelaktig ved anvendelse ombord på skip. Det benyttes et lavere lufttrykk enn ved de kon-vensjonelle luftsepareringsanlegg og apparatet er betydelig enklere og således mer pålitelig enn de kjente anlegg. Det gir 15 - 20 ganger det volum av nitrogengass som ville bli utviklet ved fordampning av et volum av flytende nitrogen svarende til det som er innført i apparatet. Ved anvendelse av flytende nitrogen tillater det en meget hurtig' start og således fremstill-ingen av store mengder gass over en relativt kort periode. Dette er særlig verdifullt når beholdere skal gjøres inerte, da sikker-hetsbestemmelsene krever en stor hastighet for inert-gassforsyn-ingen. Det produserer lett nitrogen med en renhet høyere enn The invention is particularly . beneficial when used on board ships. A lower air pressure is used than with conventional air separation systems and the device is considerably simpler and thus more reliable than the known systems. It gives 15 - 20 times the volume of nitrogen gas that would be developed by evaporating a volume of liquid nitrogen corresponding to that introduced into the apparatus. When liquid nitrogen is used, it allows a very quick start and thus the production of large quantities of gas over a relatively short period. This is particularly valuable when containers are to be made inert, as the safety regulations require a high speed for the inert gas supply. It easily produces nitrogen with a purity higher than
99,5 %. 99.5%.
Oppfinnelsen skal i det følgende nærmere beskrives ved hjelp av et utførelseseksempel som skjematisk er vist på tegnin-gen i form av et strømningsdiagråm. In the following, the invention will be described in more detail with the help of an embodiment which is schematically shown in the drawing in the form of a flow diagram.
Luft komprimeres i en'luftkompressor 1 til ca. 3 bar og avkjøles i en reversert varmeveksler 2. Den avkjølte luft går inn i en enkel rektifiseringskoionne 3 i hvilken den separeres i nitrogendamp og en oksygenanriket væske med et oksygeninnhold i området 35 - 40 % oksygen. Oksygenanriket væske trekkes ut fra bunnen av kolonnen, ekspanderes i en ekspansjonsventil 4 og benyttes i en varmeveksler 5 for å kondensere en del av nitro-gendampproduktet som trekkes ut fra -toppen av kolonnen. Det kon-denserte nitrogen føres tilbake til toppen av kolonnen for å virke som tilbakestrømning. Resten av nitrogenproduktet og ok-.sygenanriket luft forlater varmeveksleren 5 og føres gjennom en varmeveksler 6, i hvilken det foretas en oppvarming ved indirekte kontakt med en luftstrøm som trekkes ut fra den komprimerte luft-strøm like foran hovedluftinntaket i kolonnen 3, og den således kjølte luft blir returnert til kolonnen 3 ved et nivå nær hoved-luf tinnløpet . Nitrogenstrømmen og den oksygenanrikede strøm fra varmeveksleren 6 blir så ført gjennom den reverserte varmeveksler 2 for å kjøle den innkomne luft til en temperatur nær met-ningstemperaturen. Air is compressed in an air compressor 1 to approx. 3 bar and is cooled in a reversed heat exchanger 2. The cooled air enters a simple rectification cone 3 in which it is separated into nitrogen vapor and an oxygen-enriched liquid with an oxygen content in the range of 35 - 40% oxygen. Oxygen-enriched liquid is extracted from the bottom of the column, expanded in an expansion valve 4 and used in a heat exchanger 5 to condense part of the nitrogen vapor product that is extracted from the top of the column. The condensed nitrogen is fed back to the top of the column to act as reflux. The rest of the nitrogen product and oxygen-enriched air leave the heat exchanger 5 and are passed through a heat exchanger 6, in which heating is carried out by indirect contact with an air stream which is extracted from the compressed air stream just in front of the main air intake in the column 3, and thus cooled air is returned to column 3 at a level near the main air inlet. The nitrogen stream and the oxygen-enriched stream from the heat exchanger 6 are then passed through the reversed heat exchanger 2 to cool the incoming air to a temperature close to the saturation temperature.
Ved fremgangsmåten blir flytende nitrogen innført ved toppen av rektifiseringskolonnen 3 fra en lagertank 7. Dette sørger for å opprettholde de kolde driftsforhold for rektifiseringskolonnen , og graden av nitrogeninnføring innstilles for å holde systemet i likevekt. Den nitrogengass som oppnås fra en slik enhet har vanligvis et trykk på 2,5 bar, som er et særlig egnet trykk for vanlig fordeling ombord på skip. In the method, liquid nitrogen is introduced at the top of the rectification column 3 from a storage tank 7. This ensures that the cold operating conditions for the rectification column are maintained, and the degree of nitrogen introduction is set to keep the system in equilibrium. The nitrogen gas obtained from such a unit usually has a pressure of 2.5 bar, which is a particularly suitable pressure for normal distribution on board ships.
Claims (2)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB1804273A GB1463075A (en) | 1973-04-13 | 1973-04-13 | Air separation |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| NO741307L NO741307L (en) | 1974-10-15 |
| NO137565B true NO137565B (en) | 1977-12-05 |
| NO137565C NO137565C (en) | 1978-03-15 |
Family
ID=10105649
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO741307A NO137565C (en) | 1973-04-13 | 1974-04-08 | PROCEDURE AND APPARATUS FOR AIR SEPARATION |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JPS5047882A (en) |
| DE (1) | DE2417766A1 (en) |
| FR (1) | FR2225705A1 (en) |
| GB (1) | GB1463075A (en) |
| NO (1) | NO137565C (en) |
Families Citing this family (28)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6041587B2 (en) * | 1979-11-27 | 1985-09-18 | 北里研究所（社団法人） | Antibiotic production medium |
| JPS59129372A (en) * | 1983-01-14 | 1984-07-25 | 大同酸素株式会社 | Device for manufacturing nitrogen gas |
| JPS59164874A (en) * | 1983-03-08 | 1984-09-18 | 大同酸素株式会社 | Device for manufacturing nitrogen gas |
| JPS60147086A (en) * | 1984-01-11 | 1985-08-02 | 大同酸素株式会社 | Method and device for manufacturing high-purity nitrogen gas |
| DE3476114D1 (en) * | 1983-03-08 | 1989-02-16 | Daido Oxygen | Apparatus for producing high-purity nitrogen gas |
| JPS59142220U (en) * | 1983-03-15 | 1984-09-22 | 株式会社ダイフク | Chain drive device with load detection |
| JPS60232472A (en) * | 1984-05-02 | 1985-11-19 | 大同酸素株式会社 | Manufacture of high-purity nitrogen gas |
| JPS60232471A (en) * | 1984-05-02 | 1985-11-19 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6115070A (en) * | 1984-07-02 | 1986-01-23 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6115068A (en) * | 1984-07-02 | 1986-01-23 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6115066A (en) * | 1984-07-02 | 1986-01-23 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6124967A (en) * | 1984-07-13 | 1986-02-03 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6124971A (en) * | 1984-07-13 | 1986-02-03 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS6124968A (en) * | 1984-07-13 | 1986-02-03 | 大同酸素株式会社 | Production unit for high-purity nitrogen gas |
| JPS61217670A (en) * | 1985-12-10 | 1986-09-27 | 大同酸素株式会社 | Production unit for nitrogen gas |
| JPS61211688A (en) * | 1985-12-10 | 1986-09-19 | 大同酸素株式会社 | Production unit for nitrogen gas |
| JPS62116887A (en) * | 1986-08-12 | 1987-05-28 | 大同ほくさん株式会社 | Production unit for high-impurity nitrogen gas |
| JPH0587447A (en) * | 1987-11-20 | 1993-04-06 | Daido Sanso Kk | Producing apparatus for nitrogen gas |
| JPS63148080A (en) * | 1987-11-20 | 1988-06-20 | 大同酸素株式会社 | Production unit for nitrogen gas |
| JP2755953B2 (en) * | 1988-05-19 | 1998-05-25 | テイサン株式会社 | Nitrogen gas production method |
| US4966002A (en) * | 1989-08-11 | 1990-10-30 | The Boc Group, Inc. | Process and apparatus for producing nitrogen from air |
| FR2660741A1 (en) * | 1990-04-10 | 1991-10-11 | Air Liquide | PROCESS AND PLANT FOR GENERATING GASEOUS NITROGEN AND CORRESPONDING NITROGEN SUPPLY SYSTEM THEREFOR. |
| JPH0763476A (en) * | 1992-01-31 | 1995-03-10 | Daido Hoxan Inc | High-purity nitrogen gas production apparatus |
| JP2672251B2 (en) * | 1993-08-10 | 1997-11-05 | 大同ほくさん 株式会社 | Nitrogen gas production equipment |
| JP2672250B2 (en) * | 1993-08-10 | 1997-11-05 | 大同ほくさん 株式会社 | High-purity nitrogen gas production equipment |
| DE19617377A1 (en) * | 1996-04-30 | 1997-11-06 | Linde Ag | Process for restarting a plant for the low-temperature separation of air and plant for the low-temperature separation of air |
| US5740683A (en) * | 1997-03-27 | 1998-04-21 | Praxair Technology, Inc. | Cryogenic rectification regenerator system |
| EP2916089A1 (en) | 2014-03-05 | 2015-09-09 | Linde Aktiengesellschaft | Buoyant low temperature gas decomposition plant and method for low temperature gas decomposition |
-
1973
- 1973-04-13 GB GB1804273A patent/GB1463075A/en not_active Expired
-
1974
- 1974-04-08 NO NO741307A patent/NO137565C/en unknown
- 1974-04-10 JP JP49040634A patent/JPS5047882A/ja active Pending
- 1974-04-11 DE DE2417766A patent/DE2417766A1/en not_active Withdrawn
- 1974-04-12 FR FR7413098A patent/FR2225705A1/fr not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| GB1463075A (en) | 1977-02-02 |
| FR2225705A1 (en) | 1974-11-08 |
| NO137565C (en) | 1978-03-15 |
| NO741307L (en) | 1974-10-15 |
| JPS5047882A (en) | 1975-04-28 |
| DE2417766A1 (en) | 1974-10-24 |
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