NO333065B1 - Apparatus and method for keeping tanks for storing or transporting a liquid gas cold - Google Patents
Apparatus and method for keeping tanks for storing or transporting a liquid gas coldInfo
- Publication number
- NO333065B1 NO333065B1 NO20001980A NO20001980A NO333065B1 NO 333065 B1 NO333065 B1 NO 333065B1 NO 20001980 A NO20001980 A NO 20001980A NO 20001980 A NO20001980 A NO 20001980A NO 333065 B1 NO333065 B1 NO 333065B1
- Authority
- NO
- Norway
- Prior art keywords
- liquid
- gas
- heat exchanger
- tank
- liquefied
- Prior art date
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 79
- 238000000034 method Methods 0.000 title claims description 23
- 239000007789 gas Substances 0.000 claims abstract description 82
- 239000000203 mixture Substances 0.000 claims abstract description 24
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000003915 liquefied petroleum gas Substances 0.000 claims abstract description 10
- 239000012530 fluid Substances 0.000 claims abstract description 7
- 239000012809 cooling fluid Substances 0.000 claims abstract description 6
- 238000012432 intermediate storage Methods 0.000 claims abstract description 6
- 239000001257 hydrogen Substances 0.000 claims abstract description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000001816 cooling Methods 0.000 claims description 8
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 239000013526 supercooled liquid Substances 0.000 abstract 2
- 239000004743 Polypropylene Substances 0.000 abstract 1
- 239000000110 cooling liquid Substances 0.000 abstract 1
- -1 polypropylene Polymers 0.000 abstract 1
- 229920001155 polypropylene Polymers 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 14
- 238000003860 storage Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
- F17C13/02—Special adaptations of indicating, measuring, or monitoring equipment
- F17C13/025—Special adaptations of indicating, measuring, or monitoring equipment having the pressure as the parameter
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C5/00—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures
- F17C5/02—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures for filling with liquefied gases
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0005—Light or noble gases
- F25J1/001—Hydrogen
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2221/00—Handled fluid, in particular type of fluid
- F17C2221/03—Mixtures
- F17C2221/032—Hydrocarbons
- F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
- F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
- F17C2223/0146—Two-phase
- F17C2223/0153—Liquefied gas, e.g. LPG, GPL
- F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
- F17C2250/03—Control means
- F17C2250/032—Control means using computers
-
- 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
- F25J2210/04—Mixing or blending of fluids with the feed stream
-
- 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
- F25J2210/90—Boil-off gas from storage
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
-
- 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
- F25J2290/34—Details about subcooling of liquids
-
- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/32—Hydrogen storage
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/34—Hydrogen distribution
Abstract
Description
Den foreliggende oppfinnelsen vedrører generelt område med lagring og transport av flytendegjort eller kondensert gass, og vedrører mer spesielt en fremgangsmåte for å holde tanker som inneholder flytende gass kalde og til en samsvarende anordning for implementering av fremgangsmåten. The present invention generally relates to the area of storage and transport of liquefied or condensed gas, and relates more particularly to a method for keeping tanks containing liquefied gas cold and to a corresponding device for implementing the method.
KJENT TEKNIKK PRIOR ART
Det er kjent å lagre og transportere visse gasser i form av en væske ved svært lave temperaturer og ved trykk som er nær atmosfæretrykk. Uheldigvis, kan ikke tanker der slike flytende gasser lagres og transporterer, bli fullstendig og perfekt isolert, og blir derfor utsatt for varmelekkasje. Dette gjør at væske for-damper, og følgelig øker trykket innvendig i en slik tank slik at det kan raskt bli uakseptabelt høyt, og gjør det nødvendig å slippe ut fordampet gass. It is known to store and transport certain gases in the form of a liquid at very low temperatures and at pressures close to atmospheric pressure. Unfortunately, tanks where such liquefied gases are stored and transported cannot be completely and perfectly insulated, and are therefore exposed to heat leakage. This causes liquid to evaporate, and consequently increases the pressure inside such a tank so that it can quickly become unacceptably high, and makes it necessary to release evaporated gas.
Forskjellige løsninger på problemet med fordampning har følgelig blitt laget, særlig for transport av slik væskeformig gass. Følgelig, blir på metan-tankbåter utstyrt med dampdrift, den fordampede gassen tatt fra lagringstankene, varmet og brent i kjeler som leverer energi direkte til en dampkrets for å drive skipets propeller via passende giring. Various solutions to the problem of evaporation have consequently been devised, particularly for the transport of such liquefied gas. Accordingly, on methane tankers equipped with steam propulsion, the vaporized gas is taken from the storage tanks, heated and burned in boilers which supply energy directly to a steam circuit to drive the ship's propellers via suitable gearing.
Uheldigvis, blir dampdrift byttet ut i større og større grad med driftsmetoder som gir større energivirkningsgrad, eksempelvis dieseldrift. I tillegg finnes det forskjellige prosjekter som har som formål å prosessere unnsluppet gass uavhengig av skipsdriften ved hjelp av anordninger som tar sikte på å eliminere slik fordampning på andre måter. Unfortunately, steam operation is being replaced to a greater and greater extent by operating methods that provide greater energy efficiency, for example diesel operation. In addition, there are various projects whose purpose is to process escaped gas independently of the ship's operation using devices that aim to eliminate such evaporation in other ways.
Eksempelvis er det kjent å på ny gjøre dampen om til væske og på ny sprøyte den tilbake inn i tanken den kom fra. Imidlertid foreskriver denne teknikken bruk av en enhet som på ny flytendegjør eller kondenserer gassen som er svært kompleks og kostbar når de lagrede og transporterte flytendegjorte gasser ikke er rene, hvilket vanligvis er tilfelle, slik at gassen inneholder ukondenserbare komponenter som må bli utsatt for spesiell prosessering og må bli sluppet ut til atmosfæren, hvilket representerer ulemper i forbindelse med sikkerhet og miljø-beskyttelse. For example, it is known to re-convert the vapor into liquid and re-inject it back into the tank it came from. However, this technique prescribes the use of a device that re-liquefies or condenses the gas which is very complex and expensive when the stored and transported liquefied gases are not pure, which is usually the case, so that the gas contains non-condensable components that must be subjected to special processing and must be released into the atmosphere, which represents disadvantages in connection with safety and environmental protection.
En annen løsning består å ikke på ny flytendegjøre den fordampede gassen, men i en lett kjøling av den væskeformige gassen direkte. US patent 3 918 265 illustrerer anordninger som er passende for å holde tanker kalde på denne måten, som vist på figur 3. Med henvisning til figur 3, fremgår det et system der væskeformig gass blir pumpet ut fra en tank 50 og den væskeformige gassen blir ekstrahert på denne måten blir underkjølt i én eller flere varmevekslere 54 og 56, etter hvilket den blir på ny sprøytet inn i tanken 50 og muligens inn i andre tanker 52. Ventilene 58, 60, 62 og 64 tjener til å regulere de forskjellige fluidene som strømmer gjennom anordningen. Another solution consists in not re-liquefying the evaporated gas, but in a slight cooling of the liquid gas directly. US patent 3,918,265 illustrates devices suitable for keeping tanks cold in this way, as shown in figure 3. With reference to figure 3, there appears a system in which liquefied gas is pumped out from a tank 50 and the liquefied gas is extracted in this way is subcooled in one or more heat exchangers 54 and 56, after which it is re-injected into the tank 50 and possibly into other tanks 52. The valves 58, 60, 62 and 64 serve to regulate the various fluids which flows through the device.
Den løsningen kan være tilfredsstillende for styring av saktegående økninger i trykket av væskeformig gass, dvs. i det lange løp (der slike trykkhevninger kan evalueres i omtrent 10 mbar/time for LNG). Imidlertid viser dette seg å være utilstrekkelig for å imøtekomme mot raske økninger i trykk, pga. at den væskeformige gassen glir satt inn i tanken som i utgangspunktet har en dårlig tilstand i forbindelse med termodynamisk likevekt, eller at tanken ikke er skikkelig kjølt. Særlig, ved transportering av flytende gass på sjøen (for eksempel om bord på en LNG metan-tankbåt) kan vanskelige seilingsforhold føre til øyeblikkelig fordampning og forårsake at trykket øker med kanskje så mye som 10 mbar/min. i varigheter som varer opp til flere minutter. That solution can be satisfactory for managing slow increases in the pressure of liquefied gas, i.e. in the long run (where such pressure increases can be evaluated at approximately 10 mbar/hour for LNG). However, this proves to be insufficient to accommodate rapid increases in pressure, due to that the liquefied gas slips into the tank, which initially has a bad state in connection with thermodynamic equilibrium, or that the tank is not properly cooled. In particular, when transporting liquefied gas at sea (for example on board an LNG methane tanker), difficult sailing conditions can lead to instantaneous evaporation and cause the pressure to increase by perhaps as much as 10 mbar/min. for durations lasting up to several minutes.
FORMÅL OG DEFINISJON AV OPPFINNELSEN PURPOSE AND DEFINITION OF THE INVENTION
Den foreliggende oppfinnelsens forhold smelter sammen med de ovenfor nevnte ulempene ved å foreslå en fremgangsmåte for å holde tanker kalde for lagring og transport av flytendegjort gass, hvilken fremgangsmåte fremskaffer god styring av trykkøkinger, både raske og trege. Et formål med oppfinnelsen er også å foreslå en anordning for å implementere fremgangsmåten, hvilken anordning er enkelt og har lav kostnad og samsvarer bedre med dagens standarder i forbindelse med forurensning enn dagens kjente anordninger. The conditions of the present invention merge with the above-mentioned disadvantages by proposing a method for keeping tanks cold for the storage and transport of liquefied gas, which method provides good control of pressure increases, both fast and slow. An object of the invention is also to propose a device for implementing the method, which device is simple and has low cost and corresponds better to today's standards in connection with pollution than today's known devices.
Foreliggende oppfinnelse tilveiebringer en fremgangsmåte for å holde kaldt The present invention provides a method for keeping cold
i det minste én tank for lagring eller transport av flytende gass, i hvilket fremgangsmåten omfatter ekstrahering av en del av flytende gass i tanken ved å pumpe den og så blir den flytende gassen som blir ekstrahert på denne måten underkjølt i et varmevekslersystem og den flytendegjorte gassen som blir underkjølt på denne måten blir selektivt på ny innsprøytet inn i tanken, der fremgangsmåten erkarakterisert vedat en andel av dampen i tanken også blir ekstrahert intermittent, at least one tank for storing or transporting liquefied gas, in which the method comprises extracting a portion of liquefied gas in the tank by pumping it and then the liquefied gas thus extracted is subcooled in a heat exchanger system and the liquefied gas which is subcooled in this way is selectively re-injected into the tank, where the method is characterized by the fact that a proportion of the steam in the tank is also extracted intermittently,
der dampen som blir ekstrahert på denne måten blir komprimert i en kompressor, og den ekstraherte dampen som blir komprimert på denne måten blir sprøytet inn i den ekstraherte flytende gassen for å danne en blanding som så er gjort fullstendig flytende og underkjølt i varmevekslersystemet. wherein the vapor thus extracted is compressed in a compressor, and the extracted vapor thus compressed is injected into the extracted liquefied gas to form a mixture which is then completely liquefied and subcooled in the heat exchanger system.
I oppfinnelsen, blir det brukt en varmeveksler som er konstruert for å motta et fluid for kjøling som hovedsakelig er i væskeform. In the invention, a heat exchanger is used which is designed to receive a fluid for cooling which is mainly in liquid form.
Den komprimerte flytende gassblandingen som blir sprøytet inn i varmevekslersystemet har et væskeinnhold som er i området fra 50% til 100% molar og fortrinnsvis i området fra 70% til 100% molar. The compressed liquid gas mixture which is injected into the heat exchanger system has a liquid content which is in the range from 50% to 100% molar and preferably in the range from 70% to 100% molar.
Innsprøytning av gassen etter at den har blitt komprimert inn i strømmen av flytendegjort gass forbedrer styring over trykkhevninger, uavhengig av om de er raske eller trege. Injecting the gas after it has been compressed into the liquefied gas stream improves control over pressure surges, regardless of whether they are rapid or slow.
Fremgangsmåten i henhold til oppfinnelsen kan bli brukt til et sett som omfatter en rekke tanker. Under slike forhold eller omstendigheter, blir den komprimerte væske/gassblandingen tatt fra minst én av tankene, og etterpå blir den fullstendig væskegjort og underkjølt i varmevekslersystemet der det blir gjeninn-sprøytet inn i minst én av tankene. The method according to the invention can be used for a set comprising a number of tanks. Under such conditions or circumstances, the compressed liquid/gas mixture is taken from at least one of the tanks, and thereafter it is completely liquefied and subcooled in the heat exchanger system where it is re-injected into at least one of the tanks.
Oppfinnelsen fremskaffer også en anordning for implementering av fremgangsmåten som omfatter for det første minst én tank for flytende gass som inneholder en væske (LIQ) og en gass (BOG) og for det andre et varmevekslersystem hvis innløp kommuniserer med væskenivået i tanken via et pumpesystem og et væskeavsugningsrør (draw-off pipe) og hvis utløp kommuniserer med tanken etter at den har passert gjennom en styringsventil, der anordningen erkarakterisert vedat den ytterligere omfatter en kompressor med et innløp som kommuniserer med tanken i sitt gassnivå og hvis utløp kommuniserer med væskeavtrek-ningsrøret via et innsprøytningssystem via innløpet til varmeveksleren, på en slik måte at en fullstendig flytende og underkjølt blanding blir på ny satt inn i tanken for å kjøle dens innhold, og for derved styring av trykkøkninger. The invention also provides a device for implementing the method comprising firstly at least one tank for liquefied gas containing a liquid (LIQ) and a gas (BOG) and secondly a heat exchanger system whose inlet communicates with the liquid level in the tank via a pump system and a liquid suction pipe (draw-off pipe) and whose outlet communicates with the tank after it has passed through a control valve, where the device is characterized in that it further comprises a compressor with an inlet which communicates with the tank in its gas level and whose outlet communicates with the liquid draw-off pipe via an injection system via the inlet to the heat exchanger, in such a way that a completely liquid and subcooled mixture is reintroduced into the tank to cool its contents, thereby controlling pressure increases.
Fortrinnsvis omfatter varmevekslersystemet en varmeveksler som er konstruert for å motta et fluid for kjøling som hovedsakelig er i væskeform. Preferably, the heat exchanger system comprises a heat exchanger which is designed to receive a fluid for cooling which is mainly in liquid form.
Fortrinnsvis har den komprimerte væske gassblandingen som blir sprøytet inn i varmevekslersystemet et væskeinnhold som ligger i området fra 50% til 100% molar, og fortrinnsvis i området 70% til 100% molar. Preferably, the compressed liquid-gas mixture that is injected into the heat exchanger system has a liquid content that lies in the range from 50% to 100% molar, and preferably in the range 70% to 100% molar.
Varmevekslersystemet kan ha et kjølende fluid som passerer gjennom det eksempelvis et gassformig nitrogen eller en blanding av substanser som kommer fra tanken. Fortrinnsvis er den konfigurert for å kjøle den innsprøytede sammen-pressede væske/gassblandingen ved 1°C til 20°C, og fortrinnsvis ved 3°C til 17°C. Den fullstendige væskeformige og underkjølte blandingen som kommer fra varmeveksler-systemet blir gjeninnsprøytet inn i tanken i gassen (BOG) som/eller i væsken (LIQ). The heat exchanger system can have a cooling fluid that passes through it, for example gaseous nitrogen or a mixture of substances coming from the tank. Preferably, it is configured to cool the injected compressed liquid/gas mixture at 1°C to 20°C, and preferably at 3°C to 17°C. The complete liquid and subcooled mixture coming from the heat exchanger system is re-injected into the tank in the gas (BOG) and/or in the liquid (LIQ).
I en fordelaktig variant av anordningen i henhold til oppfinnelsen omfatter anordningen videre et mellomlagringsvolum plassert på et retur-rør for returnering av fullstendig flytende og underkjølt blanding til tanken, der hvor volumet er plassert mellom utløpet fra varmevekslersystemet og styringsventilen. In an advantageous variant of the device according to the invention, the device further comprises an intermediate storage volume placed on a return pipe for returning completely liquid and subcooled mixture to the tank, where the volume is placed between the outlet from the heat exchanger system and the control valve.
Man skal merke seg at den flytende gassen til hvilket oppfinnelsen kan bli brukt kan bli omfattet av en gass som er tilgjengelig i væskeform lavere enn omgivende temperatur, eksempelvis flytende naturgass (LNG), flytende petroleumsgass (LPG), ammoniakk, hydrogen, etc. Oppfinnelsen kan brukes på en spesiell fordelaktig måte for gasser som ikke finnes i væskeform ved standard-temperaturen på 15°C og hvilket som helst trykk, eksempelvis naturgass eller hydrogen. Når den flytende gassen består av en flytende petroleumsgass (LPG), kan varmevekslersystemet ha et kjølende fluid som passerer derigjennom eksempelvis propylen, freon, en HCFC, eller substanser som kommer fra tanken. It should be noted that the liquefied gas for which the invention can be used can be comprised of a gas that is available in liquid form lower than ambient temperature, for example liquefied natural gas (LNG), liquefied petroleum gas (LPG), ammonia, hydrogen, etc. The invention can be used in a particularly advantageous way for gases that do not exist in liquid form at the standard temperature of 15°C and any pressure, for example natural gas or hydrogen. When the liquefied gas consists of liquefied petroleum gas (LPG), the heat exchanger system can have a cooling fluid that passes through it, for example propylene, freon, an HCFC, or substances coming from the tank.
KORT BESKRIVELSE AV TEGNINGENE BRIEF DESCRIPTION OF THE DRAWINGS
Egenskapene og fordelene med den foreliggende oppfinnelsen vil oppfinnelsen fremgå klarere fra den etterfølgende beskrivelsen gitt av et ikke-be-grensende eksempel og med henvisning til de vedlagte tegninger, der: Fig. 1 er et diagram som viser anordningens prinsipper for lagring og transport av væskeformig gass i samsvar med oppfinnelsen; The properties and advantages of the present invention will appear more clearly from the following description given by a non-limiting example and with reference to the attached drawings, where: Fig. 1 is a diagram showing the principles of the device for storing and transporting liquid gas according to the invention;
Fig. 2 viser en utførelsesvariant av anordningen på fig. 1; og Fig. 2 shows an embodiment variant of the device in fig. 1; and
Fig. 3 viser en anordning i henhold til kjent teknikk som egner seg for styring av trege trykkøkninger i gasstanker for væskeformig gass. Fig. 3 shows a device according to known technology which is suitable for controlling slow pressure increases in gas tanks for liquefied gas.
DETALJERT BESKRIVELSE AV EN FORETRUKKET UTFØRELSESFORM DETAILED DESCRIPTION OF A PREFERRED EMBODIMENT
Fig. 1 viser en anordning i henhold til oppfinnelsen for lagring og transport av flytende gass eksempelvis flytende naturgass (LNG). Anordningen omfatter en tank 10 som inneholder en væske (LIQ) 12 og en gass. På vanlig måte er tanken anbrakt med forskjellige termiske isoleringskonstruksjoner for å begrense varmelekkasjene til hvilket væsken og gassen som er lagret deri er uttatt for. Over væskeseparasjonsoverflaten 14 finnes det et tilleggsrom 16 som inneholder gassen fra lagringen som består av damp eller "avkok-gass" (BOG). Et pumpesystem 18 er plassert innvendig i tanken i væsken 12 og hovedsakelig ved den nedre delen av denne, (bunnen av tanken), men den kunne også være plassert et annet sted, inkludert utsiden av tanken 10, og er forbundet til en første ende av et gå-rør 20 (go pipe) 20 for å trekke av væsker, hvis andre ende er forbundet til et første innløp på en varmeveksler 22 som også har et kjølefluid som passerer derigjennom mellom et andre innløp og et andre utløp, dvs. gassformig nitrogen eller en blanding av substanser som kommer fra tanken. Et første utløp fra varmeveksler 22 er forbundet med den første ende av et retur-rør 24 hvis andre ende stikker inn i tank 10 (inn i væsken og/eller inn i den avkokte gassen, avhengig av nivået som tanken er fylt til) etter at det har passert gjennom en reguleringsventil 26. Fig. 1 shows a device according to the invention for storing and transporting liquefied gas, for example liquefied natural gas (LNG). The device comprises a tank 10 which contains a liquid (LIQ) 12 and a gas. In the usual way, the tank is fitted with various thermal insulation constructions to limit the heat leaks to which the liquid and gas stored therein is withdrawn. Above the liquid separation surface 14 there is an additional space 16 which contains the gas from the storage consisting of steam or "boil-off gas" (BOG). A pump system 18 is located inside the tank in the liquid 12 and mainly at the lower part thereof, (the bottom of the tank), but it could also be located elsewhere, including the outside of the tank 10, and is connected to a first end of a go pipe 20 (go pipe) 20 for withdrawing liquids, the other end of which is connected to a first inlet of a heat exchanger 22 which also has a cooling fluid passing through it between a second inlet and a second outlet, i.e. gaseous nitrogen or a mixture of substances coming from the tank. A first outlet from the heat exchanger 22 is connected to the first end of a return pipe 24, the other end of which protrudes into the tank 10 (into the liquid and/or into the boiled-off gas, depending on the level to which the tank is filled) after it has passed through a control valve 26.
Oppfinnelsen omfatter ytterligere et andre rør 34 med en ende i kommuni-kasjon med det innvendige av tanken 10 i sin gass 16, hovedsakelig i de øvre deler av denne (toppen av tanken), og med sin andre ende forbundet med innløpet på en kompressor 36 etter at det har passert gjennom en ventil 31. Kompressor 36 kan være tilknyttet kjølingssystemet. Utløpet fra kompressoren 36 kommuniserer via et innsprøytningssystem med røret 20 for å trekke av væske. The invention further comprises a second pipe 34 with one end in communication with the interior of the tank 10 in its gas 16, mainly in the upper parts thereof (the top of the tank), and with its other end connected to the inlet of a compressor 36 after it has passed through a valve 31. Compressor 36 may be connected to the cooling system. The outlet from the compressor 36 communicates via an injection system with the pipe 20 to draw off liquid.
Reguleringsventiler 26 og 31, og kompressoren 36 blir alle styrt av en passende styringsenhet 28 slik at væsken som på ny blir ført inn i tanken og slik at den periodiske avsugningen av gassen 16 gjør det mulig at trykket innvendig i tanken blir styrt i sanntid, med underkjøling av den på ny innsatte væsken som møter varmelekkasjen som motvirker varmelekkasjen og som er årsaken til at væsken 12 og gassen 16 varmes opp. Et mellomlagringsvolum 30 kan bli plassert ved retur-rør 24 på vei tilbake til tanken 10 mellom utløpet fra varmeveksler 22 og reguleringsventil 26 for å fremskaffe større fleksibilitet under drift av anordningen ved å fremskaffe en reservetilførsel av kjølt væske. Naturligvis, gjør tilveiebringelsen av en ventil 32 det mulig, skulle det være nødvendig, å trekke ut eller ekstrahere gassen som mellomlagringsvolumet 30 inneholder. Control valves 26 and 31, and the compressor 36 are all controlled by a suitable control unit 28 so that the liquid which is re-introduced into the tank and so that the periodic suction of the gas 16 makes it possible for the pressure inside the tank to be controlled in real time, with subcooling of the reinserted liquid which meets the heat leak which counteracts the heat leak and which causes the liquid 12 and the gas 16 to heat up. An intermediate storage volume 30 can be placed at the return pipe 24 on the way back to the tank 10 between the outlet from the heat exchanger 22 and the control valve 26 to provide greater flexibility during operation of the device by providing a reserve supply of cooled liquid. Naturally, the provision of a valve 32 makes it possible, should it be necessary, to withdraw or extract the gas which the intermediate storage volume 30 contains.
Fremgangsmåten implementert i anordningen i henhold til oppfinnelsen består i utgangspunktet i å bruke pumpe 18 til å ekstrahere en del av væsken LIQ 12 som blir levert til går-rør 20 til varmeveksler 22 der det blir underkjølt ved hjelp av kjølevæsken som kommer fra et eksternt kjølingssystem. Ved utløpet av varmeveksleren, blir den underkjølte væsken levert i retur-rør 24 mot tank 10 inn i hvilket det blir på ny innsprøytet selektivt, enten direkte eller etter alternativ mellomlagring i volumet 30. I seg selv, tjener denne sirkulasjonen av kjølt væske på en svært enkel måte til å styre trege eller saktegående trykkøkninger. Følgelig, kan eksempelvis for en metantanker med en kapasitet på 135 000 m og for transportering av LNG ha et relativt høyt nitrogeninnhold (omtrent 1,2 % molar i væsken), og tankene holdes kalde av en strøm av flere hundre m<3>/time LNG som er underkjølt av en mengde som ligger i området 1°C til 20°C (fortrinnsvis i området fra 3°C til 17°C). Mer presist, for 150 m<3>/time av LNG underkjølt med 11°C før gjeninnsprøyting i væsken inn i tanken utføres denne funksjonen å holde tanken kald på lang sikt i tillegg godt og uten at noe slippes ut i atmosfæren. Denne sirkuleringshastigheten av LNG kan oppnås rett og slett ved hjelp av en eller flere resirkuleringspumper (spray pumps) eller muligens ved bruk av av-blåsningspumper som metantanker vanligvis er utstyrt med. The method implemented in the device according to the invention basically consists in using pump 18 to extract part of the liquid LIQ 12 which is delivered to the flow pipe 20 to the heat exchanger 22 where it is subcooled by means of the coolant coming from an external cooling system . At the outlet of the heat exchanger, the subcooled liquid is delivered in the return pipe 24 towards the tank 10 into which it is re-injected selectively, either directly or after alternative intermediate storage in the volume 30. In itself, this circulation of cooled liquid serves a very simple way to control slow or slow pressure increases. Consequently, for example, a methane tanker with a capacity of 135,000 m and for transporting LNG can have a relatively high nitrogen content (about 1.2% molar in the liquid), and the tanks are kept cold by a flow of several hundred m<3>/ hour LNG that is subcooled by an amount in the range of 1°C to 20°C (preferably in the range of 3°C to 17°C). More precisely, for 150 m<3>/hour of LNG subcooled by 11°C before re-injection into the liquid into the tank, this function is performed to keep the tank cold in the long term in addition well and without anything being released into the atmosphere. This circulation rate of LNG can be achieved simply by means of one or more recirculation pumps (spray pumps) or possibly by the use of blow-off pumps that methane tanks are usually equipped with.
Uheldigvis, er ikke denne resirkulasjonen av væske tilstrekkelig i seg selv til å styre raske trykkøkninger. Fremgangsmåten beskrevet over blir forbedret ved at en del av avkok-gass BOG 16 kan bli ekstrahert i perioder, og etterfølgende sprøytet inn etter at det blir komprimert (i kompressor 36) via innsprøytnings-systemet 35 inn i LNG-strømmen som sirkulerer i gå-røret 20 etter hvilket det blir utsatt for kjøling i varmeveksler 22. Strømmen som går inn i varmeveksleren er enten en strøm væske i BOG-strømmen hvis BOG-strømmen er fullstendig opp-løst i LNG-strømmen eller ellers mer generelt en strøm væske og damp med en hoveddel væskeinnhold som ligger i området 50% til 100%, og fortrinnsvis i området 70% til 100% molar. Under slike forhold, er varmeveksleren naturligvis en tofase-varmeveksler skjønt av en forenklet struktur-konstruksjon på grunn av tilstedeværelsen av en liten mengde damp. Følgelig, tilbake til det ovenfor gitte eksempel for en metan-tanker, kan det ble vist at håndtering av en trykkhevning på 10 mbar/minutt tilsvarer innsprøytning av en strøm på 2800 kg/time av BOG inn i strømmen på 150 m Vtime væske. Denne blandingen, hvis væskeinnhold i dette tilfelle er 98% molar blir sprøytet inn i varmeveksleren når den blir fullstendig væskeformig og kjølt ved 13°C, etter hvilket den blir på ny sprøytet inn i tanken ved en temperatur på -177°C, dvs. en temperatur som er høyere enn krystalli-sasjonstemperaturen for metan ved atmosfæretrykk, hvilket temperatur er omtrent -182,6°C. Unfortunately, this recirculation of fluid is not sufficient by itself to control rapid pressure increases. The procedure described above is improved by the fact that a part of the boil-off gas BOG 16 can be extracted in periods, and subsequently injected after it is compressed (in the compressor 36) via the injection system 35 into the LNG stream which circulates in the pipe 20 after which it is exposed to cooling in the heat exchanger 22. The stream that enters the heat exchanger is either a stream of liquid in the BOG stream if the BOG stream is completely dissolved in the LNG stream or else more generally a stream of liquid and steam with a main liquid content in the range 50% to 100%, and preferably in the range 70% to 100% molar. Under such conditions, the heat exchanger is naturally a two-phase heat exchanger albeit of a simplified structural design due to the presence of a small amount of steam. Accordingly, returning to the example given above for a methane tanker, it can be shown that handling a pressure rise of 10 mbar/minute is equivalent to injecting a flow of 2800 kg/hour of BOG into the flow of 150 m Vhour of liquid. This mixture, whose liquid content in this case is 98% molar, is injected into the heat exchanger when it becomes completely liquid and cooled at 13°C, after which it is re-injected into the tank at a temperature of -177°C, i.e. a temperature which is higher than the crystallization temperature of methane at atmospheric pressure, which temperature is approximately -182.6°C.
Med konstruksjonen i henhold til oppfinnelsen oppnås utmerket varme-veksling med den kombinerte væske og den fordampede gassen i tanken ("bulk") uten skadelig dumpning ut i atmosfæren. I tillegg, og i denne sammenheng for bruk om bord i skip, er utstyret som foreskrives av liten kostnad, fordi som nevnt over, er det mulig å bruke eksisterende utstyr på skipet, og spesielt dens pumper eller kompressorer. With the construction according to the invention, excellent heat exchange is achieved with the combined liquid and the vaporized gas in the tank ("bulk") without harmful dumping into the atmosphere. In addition, and in this context for use on board ships, the equipment prescribed is of little cost, because as mentioned above, it is possible to use existing equipment on the ship, and especially its pumps or compressors.
Figur 2 viser en variant av anordningen på figur 1 som demonstrerer at fremgangsmåten i henhold til oppfinnelsen også kan bli brukt til ett sett tanker. Etter den første tank 10, som er svært full (for eksempel 98%), kan det ses en andre tank 40 som er nesten tom, og med en sone 42 som inneholder en væske eller LIQ, en væske/dampseparasjonsoverflate 44 og en sone 46 som inneholder gass eller BOG. Mellom de to tankene tillater en kanal 48 at de to sonene som inneholder gassen kommuniserer. Det skal bemerkes at på grunn av at den andre tanken er nesten tom, blir nødvendigvis den underkjølte komprimerte væske/- gassblandingen gjeninnsprøytet i gassen i denne tanken 40. Figure 2 shows a variant of the device in Figure 1 which demonstrates that the method according to the invention can also be used for one set of tanks. After the first tank 10, which is very full (eg 98%), a second tank 40 can be seen which is almost empty, and with a zone 42 containing a liquid or LIQ, a liquid/vapor separation surface 44 and a zone 46 which contains gas or BOG. Between the two tanks, a channel 48 allows the two zones containing the gas to communicate. It should be noted that because the second tank is almost empty, the subcooled compressed liquid/gas mixture is necessarily re-injected into the gas in this tank 40.
Det skal også bemerkes at selv om begge utførelsesformene som vist ved-rører spesielt lagring av væskeformig naturgass (LNG) er det åpenbart at oppfinnelsen kan bli implementert for hvilken som helst annen type gass som er tilgjengelig i væskeform ved lavere enn omgivende temperaturer, eksempelvis flytende petroleumsgass (LPG), ammoniakk, hydrogen, etc. It should also be noted that although both embodiments shown relate in particular to the storage of liquefied natural gas (LNG), it is obvious that the invention can be implemented for any other type of gas that is available in liquid form at lower than ambient temperatures, for example liquid petroleum gas (LPG), ammonia, hydrogen, etc.
Claims (14)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| FR9904949A FR2792707B1 (en) | 1999-04-20 | 1999-04-20 | METHOD AND DEVICE FOR THE COLD HOLDING OF TANKS FOR STORING OR TRANSPORTING LIQUEFIED GAS |
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| NO20001980D0 NO20001980D0 (en) | 2000-04-14 |
| NO20001980L NO20001980L (en) | 2000-10-23 |
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| NO20001980A NO333065B1 (en) | 1999-04-20 | 2000-04-14 | Apparatus and method for keeping tanks for storing or transporting a liquid gas cold |
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| EP (1) | EP1046858B1 (en) |
| JP (1) | JP4662602B2 (en) |
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Families Citing this family (27)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| MY123311A (en) * | 1999-01-15 | 2006-05-31 | Exxon Production Research Co | Process for producing a pressurized methane-rich liquid from a methane-rich gas |
| FR2792707B1 (en) * | 1999-04-20 | 2001-07-06 | Gaz De France | METHOD AND DEVICE FOR THE COLD HOLDING OF TANKS FOR STORING OR TRANSPORTING LIQUEFIED GAS |
| US6336331B1 (en) * | 2000-08-01 | 2002-01-08 | Praxair Technology, Inc. | System for operating cryogenic liquid tankage |
| JP4255269B2 (en) * | 2002-11-25 | 2009-04-15 | 昭和炭酸株式会社 | Ultra-low temperature nitrogen gas supply device |
| GB0320474D0 (en) * | 2003-09-01 | 2003-10-01 | Cryostar France Sa | Controlled storage of liquefied gases |
| JP4408211B2 (en) * | 2003-11-04 | 2010-02-03 | 株式会社神戸製鋼所 | Pressure adjusting device for liquefied natural gas tank and pressure adjusting method thereof |
| KR100613430B1 (en) * | 2005-07-27 | 2006-08-17 | 삼성중공업 주식회사 | Process and apparatus for boil-off gas treatment |
| US20080190352A1 (en) | 2007-02-12 | 2008-08-14 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Lng tank ship and operation thereof |
| KR100834273B1 (en) * | 2007-03-20 | 2008-05-30 | 대우조선해양 주식회사 | Membrane type lng cargo tank, lng carrier with it, and lng carrying method |
| US20090199591A1 (en) | 2008-02-11 | 2009-08-13 | Daewoo Shipbuilding & Marine Engineering Co., Ltd. | Liquefied natural gas with butane and method of storing and processing the same |
| KR20090107805A (en) | 2008-04-10 | 2009-10-14 | 대우조선해양 주식회사 | Method and system for reducing heating value of natural gas |
| DE102010020476B4 (en) | 2010-05-14 | 2023-05-04 | Air Liquide Deutschland Gmbh | Use of a device for storing, decanting and/or transporting cryogenic liquefied combustible gas in a vehicle |
| DE202010012886U1 (en) | 2010-11-15 | 2011-01-05 | Marine Service Gmbh | Container for the transport or storage of liquid natural gas |
| RU2446344C1 (en) * | 2011-01-24 | 2012-03-27 | ФЕДЕРАЛЬНОЕ ГОСУДАРСТВЕННОЕ ВОЕННОЕ ОБРАЗОВАТЕЛЬНОЕ УЧРЕЖДЕНИЕ ВЫСШЕГО ПРОФЕССИОНАЛЬНОГО ОБРАЗОВАНИЯ "ВОЕННАЯ АКАДЕМИЯ ТЫЛА И ТРАНСПОРТА имени генерала армии Хрулева А.В." | Condensed natural gas storage complex |
| RU2451872C1 (en) * | 2011-02-14 | 2012-05-27 | ФЕДЕРАЛЬНОЕ ГОСУДАРСТВЕННОЕ ВОЕННОЕ ОБРАЗОВАТЕЛЬНОЕ УЧРЕЖДЕНИЕ ВЫСШЕГО ПРОФЕССИОНАЛЬНОГО ОБРАЗОВАНИЯ "ВОЕННАЯ АКАДЕМИЯ ТЫЛА И ТРАНСПОРТА имени генерала армии Хрулева А.В." | Complex for long-term storage of liquefied natural gas |
| FR2986061B1 (en) * | 2012-01-19 | 2019-12-06 | L'air Liquide, Societe Anonyme Pour L'etude Et L’Exploitation Des Procedes Georges Claude | INSTALLATION AND METHOD FOR PROVIDING LIQUID XENON |
| CN103343884B (en) * | 2013-06-19 | 2015-04-15 | 北京航空航天大学 | Liquid helium conveying system used for large-size multi-section liquid helium heat sinks and class converting method for large-size multi-section liquid helium heat sinks |
| CN104110938A (en) * | 2014-06-24 | 2014-10-22 | 中国石油大学(北京) | Pipeline gas differential pressure refrigeration liquefying device and technology by combining nitrogen to achieve expansion refrigeration |
| CN104315802A (en) * | 2014-10-27 | 2015-01-28 | 中国海洋石油总公司 | Method and equipment for dynamically recycling evaporated gas of liquefied natural gas |
| CN104677000B (en) * | 2015-03-19 | 2017-05-17 | 中国工程物理研究院材料研究所 | Liquid nitrogen cooling cryogenic device and implementation method for same |
| CN105486031A (en) * | 2016-01-07 | 2016-04-13 | 惠生（南通）重工有限公司 | Natural gas liquefying system used for FLNG (floating liquefied natural gas) and liquefying method thereof |
| DE102016002316A1 (en) * | 2016-02-29 | 2017-08-31 | Tge Marine Gas Engineering Gmbh | Method for operating a liquefied gas tank and liquid gas tank for receiving LNG and boil-off gas |
| RU2649510C2 (en) * | 2016-07-25 | 2018-04-03 | Николай Геннадьевич Кириллов | Complex of long-term storage and use of cryogenic fuel components |
| JP6834999B2 (en) * | 2018-01-29 | 2021-02-24 | Ｊｆｅエンジニアリング株式会社 | Evaporative gas suppression device and evaporative gas suppression method for LNG tanks |
| FR3088407B1 (en) * | 2018-11-13 | 2023-04-14 | Engie | DEVICE FOR COOLING AN EVAPORATION GAS |
| US11686434B1 (en) * | 2022-02-22 | 2023-06-27 | China Energy Investment Corporation Limited | Submerged multi-mode cryopump for refueling hydrogen, system having the same, and method of using the same |
| CN115388615B (en) * | 2022-04-19 | 2023-11-24 | 北京师范大学 | Argon liquefaction system |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3733838A (en) * | 1971-12-01 | 1973-05-22 | Chicago Bridge & Iron Co | System for reliquefying boil-off vapor from liquefied gas |
| DE2260516A1 (en) * | 1972-12-11 | 1974-06-12 | Linde Ag | PROCESS FOR COMPENSATING COLD LOSS DURING STORAGE OF LOW-BOILING LOW-BOILING GAS MIXTURES |
| GB1472533A (en) * | 1973-06-27 | 1977-05-04 | Petrocarbon Dev Ltd | Reliquefaction of boil-off gas from a ships cargo of liquefied natural gas |
| US4249387A (en) * | 1979-06-27 | 1981-02-10 | Phillips Petroleum Company | Refrigeration of liquefied petroleum gas storage with retention of light ends |
| JPS6465394A (en) * | 1987-09-03 | 1989-03-10 | Osaka Gas Co Ltd | Manufacture of fuel gas |
| US5243821A (en) * | 1991-06-24 | 1993-09-14 | Air Products And Chemicals, Inc. | Method and apparatus for delivering a continuous quantity of gas over a wide range of flow rates |
| US5687776A (en) * | 1992-12-07 | 1997-11-18 | Chicago Bridge & Iron Technical Services Company | Method and apparatus for fueling vehicles with liquefied cryogenic fuel |
| JPH06185699A (en) * | 1992-12-15 | 1994-07-08 | Tokyo Gas Co Ltd | Device for restraining bog generated in liquefied gas storage tank |
| JPH06341598A (en) * | 1993-05-31 | 1994-12-13 | Chiyoda Corp | Evaporated gas treating method of low temperature liquefied gas storage tank |
| US5456084A (en) * | 1993-11-01 | 1995-10-10 | The Boc Group, Inc. | Cryogenic heat exchange system and freeze dryer |
| JPH07218033A (en) * | 1994-02-03 | 1995-08-18 | Nkk Corp | Cooling device for lng tank |
| JPH08159396A (en) * | 1994-12-09 | 1996-06-21 | Tokyo Gas Co Ltd | Method for suppressing bog generated in liquefied gas storage tank, and device therefor |
| JPH08285194A (en) * | 1995-04-11 | 1996-11-01 | Ishikawajima Harima Heavy Ind Co Ltd | Cryogenic liquid storage equipment |
| FR2792707B1 (en) * | 1999-04-20 | 2001-07-06 | Gaz De France | METHOD AND DEVICE FOR THE COLD HOLDING OF TANKS FOR STORING OR TRANSPORTING LIQUEFIED GAS |
-
1999
- 1999-04-20 FR FR9904949A patent/FR2792707B1/en not_active Expired - Lifetime
-
2000
- 2000-04-14 NO NO20001980A patent/NO333065B1/en not_active IP Right Cessation
- 2000-04-17 AT AT00401063T patent/ATE332474T1/en active
- 2000-04-17 ES ES00401063T patent/ES2267473T3/en not_active Expired - Lifetime
- 2000-04-17 EP EP00401063A patent/EP1046858B1/en not_active Expired - Lifetime
- 2000-04-17 DE DE60029162T patent/DE60029162T2/en not_active Expired - Lifetime
- 2000-04-18 KR KR1020000020390A patent/KR100696079B1/en active IP Right Grant
- 2000-04-20 JP JP2000119921A patent/JP4662602B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JP2000337597A (en) | 2000-12-05 |
| JP4662602B2 (en) | 2011-03-30 |
| EP1046858A1 (en) | 2000-10-25 |
| DE60029162D1 (en) | 2006-08-17 |
| KR20010049264A (en) | 2001-06-15 |
| FR2792707B1 (en) | 2001-07-06 |
| FR2792707A1 (en) | 2000-10-27 |
| EP1046858B1 (en) | 2006-07-05 |
| ES2267473T3 (en) | 2007-03-16 |
| KR100696079B1 (en) | 2007-03-16 |
| NO20001980D0 (en) | 2000-04-14 |
| ATE332474T1 (en) | 2006-07-15 |
| DE60029162T2 (en) | 2007-07-05 |
| NO20001980L (en) | 2000-10-23 |
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| Date | Code | Title | Description |
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| MK1K | Patent expired |