US3877240A - Process and apparatus for the storage and transportation of liquefied gases - Google Patents

Process and apparatus for the storage and transportation of liquefied gases Download PDF

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US3877240A
US3877240A US354925A US35492573A US3877240A US 3877240 A US3877240 A US 3877240A US 354925 A US354925 A US 354925A US 35492573 A US35492573 A US 35492573A US 3877240 A US3877240 A US 3877240A
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Prior art keywords
gas
cryogenic tank
liquefied
liquefied gas
tank means
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US354925A
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English (en)
Inventor
Ludwig Kniel
Frederick Fussman
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CB&I Technology Inc
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Lummus Co
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Priority to US354925A priority Critical patent/US3877240A/en
Priority to JP48099798A priority patent/JPS502211A/ja
Priority to NO741457A priority patent/NO741457L/no
Priority to NL7405659A priority patent/NL7405659A/xx
Priority to FR7414740A priority patent/FR2227505B1/fr
Priority to DE2420525A priority patent/DE2420525A1/de
Priority to GB1871074A priority patent/GB1413456A/en
Application granted granted Critical
Publication of US3877240A publication Critical patent/US3877240A/en
Priority to JP12248680A priority patent/JPS5694094A/ja
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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
    • 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
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0277—Offshore use, e.g. during shipping
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63J—AUXILIARIES ON VESSELS
    • B63J2/00—Arrangements of ventilation, heating, cooling, or air-conditioning
    • B63J2/12—Heating; Cooling
    • B63J2/14—Heating; Cooling of liquid-freight-carrying tanks
    • 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
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • 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
    • F25J1/02—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
    • F25J1/0221—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 using the cold stored in an external cryogenic component in an open refrigeration loop
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
    • B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
    • B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
    • B63B2025/087—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid comprising self-contained tanks installed in the ship structure as separate units
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • 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
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • 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

Definitions

  • ABSTRACT There is disclosed a vessel having a plurality of cryogenic tanks for the storage of liquefied gases wherein the cryogenic tanks are provided with conduit means and a heat exchange means whereby the unavoidable boil-Off from a lower boiling liquefied gas stored in a first cryogenic tank means, is passed in indirect heat transfer relationship with the unavoidable boil-off from a higher boiling liquefied gas stored in a second cryogenic tank means, to re-liquefy the vapors Of the higher boiling liquefied gas. Additional conduit means are provided to permit alteration of the gaseous atmosphere in the second cryogenic tank means (after unloading its content) to the atmosphere of the liquefied gas to be subsequently stored and transported therein.
  • This invention relates to the storage of liquefied gases, and more particularly to novel processes and apparatus for the storage and transportation of liquefied gases at about atmospheric pressure in a vessel, such as a ship. barge or the like.
  • An object of the present invention is to provide novel processes and apparatus for the storage of liquefied gases.
  • Another object of the present invention is to provide novel processes and apparatus for the storage and transportation of liquefied gases by a vessel.
  • a further object of the present invention is to provide a novel process and apparatus for the storage and transportation of liquefied gases by a vessel wherein the vapors evolving from the lower boiling liquefied gas being transported as a result mainly of heat leakage and varying sea and weather conditions (hereinafter sometimes referred to as the unavoidable boil-off"), is utilized as a means to liquefy the vapors (i.e., unavoidable boiloff) evolving from the higher boiling liquefied gas being transported.
  • a still further object of the present invention is to provide novel processes and apparatus for the en route preparation of a cryogenic tank of any such vessel for the storage and transportation of a liquefied gas different than the liquefied gas previously transported therein.
  • Another object of the present invention is to provide a novel process and apparatus for modifying an existing liquefied natural gas ship having cryogenic tanks for the storage and transportation of LNG and a liquefied gas having a higher boiling point than LNG.
  • Still another object of the present invention is to provide a novel process and apparatus to be utilized on new liquefied gas ships having cryogenic tanks for the storage and transportation at about atmospheric pressure of diverse liquefied gases.
  • a still further object of the present invention is to provide a novel system for transporting liquefied natural gas and ethylene from a source thereof to a user location.
  • a vessel having a plurality of cryogenic tanks for the storage of liquefied gases by providing the cryogenic tanks with conduit means and heat exchange means whereby the unavoidable boil-off from the lower boiling liquefied gas stored in a first cryogenic tank means thereof, is passed in indirect heat transfer relationship with the unavoidable boil-off from the higher boiling liquefied gas stored in a second cryogenic tank means, to re-liquefy the vapors of the higher boiling liquefied gas.
  • Additional conduit means and other apparatus are provided to permit alteration of the atmosphere in the cryogenic tank (after un-loading its contents) to the atmosphere of the liquefied gas to be subsequently stored and transported therein (as more fully hereinafter discussed).
  • the vessels in service at the present day for transportation of liquefied gases are generally designed to carry from 5 to 7 similarly sized tanks of the spherical or prismatic type, although other shapes of cryogenic tank may be employed.
  • a preferred emstoring the liquefied ethylene regardless of the size and number of such tanks, it being understood that volumetric ratios will vary depending upon the liquefied gases being transported. While the drawing includes fluid communication equipment, such as valves, pumps, and the like, it is understood that additional such equipment has been omitted from the drawing to facilitate the description thereof and the placing of such equipment at appropriate places are deemed to be within the scopeof those skilled in the art.
  • FIG. 1 is a schematic elevational view of a vessel illustrating the general arrangement of the various tanks and associated apparatus
  • FIG. 2 is a schematic flow diagram of a preferred embodiment of the invention.
  • FIG. 1 there is illustrated a vessel, generally indicated as 10, provided with five spherical cryogenic tanks T including a re-liquefaction assembly, a cargo control station, and an off-loading station, generally indicated as 12, 14 and 16, respectively, with the reliquefaction assembly 12 being disposed between the first and second tank proximate to the super structure of the vessel 10.
  • a vessel may have a capacity of, for example, 125,0Om of LNG, with principal characteristics being an overall length of about 900-1,000 feet, a draft of 36 feet or more, and a displacement of 94,600 long tons at speeds of about 20 knots or more.
  • one tank T(LE) to store liquefied ethylene and the remaining tanks T(LNG) to store liquefied natural gas will be provided with piping or conduit configuration in fluid communication with the re-liquefaction apparatus 12 as more fully hereinafter described.
  • a preferred placement of the liquefied ethylene storage tank T(LE) to minimize piping expenses is to position the liquefied ethylene tank proximate to the stern of the ship, however it is understood that other consideration, e.g., partial loading conditions, order of loading and unloading of liquefied ethylene and LNG, etc., may make it desirable to position the liquefied ethylene storage tank T(LE) amidships. All of the cryogenic tanks of the vessel 10 are usually of the same constructions and heavily insulated.
  • FIG. 2 there is illustrated the reliquefaction apparatus 12 with a piping configuration associated with the tank T( LE) for the storage of liquefied ethylene.
  • a line for the loading and off-loading of liquefied ethylene is provided with a suitable fitting (not shown) for connecting the line 20 to an appropriate dock side facilities (not shown).
  • the line 20 is in fluid communication with loading line 22 under the control of valve 24, and with an unloading pump 28 by line 30 under the control valve 32.
  • Unloading pump 28 may be located inside the tank, i.e., submerged, or externally of the tank.
  • a line 34 is provided on the top portion of the liquefied ethylene tank T( LE) under the control of valve 36 in fluid communication via lines 38 and 40 under the control of valves 42 and 44 with a fractionating condenser, generally indicated as 46.
  • the tank T(LE) is provided with safety vent line 26 under the control of a safety relief valve 18 by line 34.
  • Line 34 is in fluid communication with a line 48 under the control of valve 50 with a compressor 52 and thence with line 40 by line 54 under the control of valve 56.
  • a line 58 under the control of valve 60 is in fluid communication with a reboiler coil 63 positioned in the lower portion of the fractionating condenser 46 (as more fully hereinafter discussed) and with line 40 by line 62 under the control of valve 64.
  • a vapor header or manifold, generally indicated as 66, is in fluid communication by conduits 68 with the remaining tanks of the vessel 10 containing LNG.
  • the header 66 is in fluid communication by line 70 under the control of valve 72 with a heat exchange coil 74 disposed within the upper portion of the fractionating condenser 46;
  • the outlet of the coil 74 is in fluid communication by line 76 under the control of valve 78 via a booster compressor 80 with a fuel manifold 82.
  • the top of the condenser 46 is in fluid communication by line 84 under the control of valve 86 with a heat exchange coil 88 disposed within the upper portion of the fractionating condenser 46 proximate to the coil 74 and thence with line 76 by line 90 under the control of valve 92.
  • the header 66 is in fluid communication by line 94 under the control of valve 96 with the suction side of a compressor 98 with the outlet therefrom being in fluid communication with line 100.
  • Line 100 is in fluid communication with line 102 and 104 under the control of valves 106 and 108, respectively.
  • Line 102 is in fluid communication with line 70, and line 104 is in fluid communication with lines 110 and 112 under the control of valves 114 and 116, respectively, with line 110 being in fluid communication with the liquefied ethylene tank T(LE).
  • the bottom of the fractionating tower 46 is in fluid communication by line via pump 122 with lines 124 and 126 under the control of valves 128 and 130, respectively.
  • Line 124 is in fluid communication with the liquefied ethylene tank T(LE) whereas the line 126 is in fluid communication with liquefied ethylene holding tank 132.
  • the liquefied ethylene holding tank 132 is provided with a line 134 under the control of valve 136 for the fluid communication with dock side facilities, as more fully hereinafter discussed.
  • the bottom of the ethylene holding tank 132 is provided with a conduit 138 in fluid communication by a pump 140 with line 142 under the control of valve 144.
  • Line 142 is in fluid communication with line 146 and 148 under the control of valves 150 and 152, respectively.
  • Line 146 is in fluid communication with a line 154 positioned within the tank T(LE) and through line 156 under the control of valve 158 with line 34.
  • Line 148 is in fluid communication with tank T(LE) via heat exchanger 160 through line 162 under the control of valve 164.
  • this invention relates to the storage of liquefied gases in a plurality of cryogenic tanks positioned on a vessel, however, for the transportation of LNG and liquefied ethylene the volumetric capacity of the tank(s) storing LNG is in a ratio of at least 4:1 with respect to the volumetric capacity of the tank(s) storing liquefied ethylene. Therefore, with regard to the vessel of FIG. 1, one tank of the five cryogenic tanks would be provided with conduit means and ancillary equipment necessary to permit the storage of the liquefied ethylene, and re-liquefaction of the unavoidable boil-off, as hereinabove discussed.
  • the tank T(LE) of the vessel is filled with liquefied ethylene and the remaining tanks T(LNG) of the vessel 10 are filled with LNG at pressures slightly above atmospheric.
  • the ethylene vapors resulting from unavoidable boil-off are withdrawn from tank T( LE) by line 34 and passed by line 38 and 40 into the fractionating condenser 46.
  • the ethylene vapors are passed in indirect heat transfer relationship to natural gas (unavoidable boil-off) introduced into the coil 74 of the condenser 46 from line 70 collected in manifold 66 from the tanks T( LNG) by lines 68.
  • valve 72 will be opened at this time whereas the valves 96, 106 and 116 will be closed.
  • the amount of unavoidable boil-off from the LNG in the tanks T( LNG) is sufficient to provide the cooling requirements to re-liquefy the unavoidable boil-off from the tank T( LE) in fractionating condenser 46 with liquefied ethylene being returned by line 124 to the tank T(LE) by pump 122 in fluid communication with the bottom of the fractionating condenser 46 through line 120.
  • the natural gas withdrawn from the coil by line 76 is passed as fuel by booster compressor 80 through line 82 to the propulsion system of the vessel (not shown).
  • the compressor S2 is preferably of the non-lubricated reciprocating type with the suction volume thereof being regulated either by a variable speed transmission or by clearance pockets and valve lifters, or through a combination of such devices actuated by a pressure controller 170 in communication with the tank T(LE) by line 172.
  • the compressor 98 may be a compressor similar to the compressor 52. It is contemplated that in some instances it may be necessary to utilize a plurality of such compressors in parallel. It is noted that in this operation the ethylene vapors are not passed by line 58 through the reboiler coil 63 in the fractionating condenser 46, the use thereof being hereinafter discussed. It will be further understood that pump 122 may not be necessary since the liquefied ethylene may usually be readily passed by gravity to the liquefied ethylene tank T( LE). Upon the vessel reaching its destination, the liquefied ethylene and/or LNG are unloaded in a manner known to those skilled in the art. Liquefied ethylene, for example, is withdrawn by the pump 28 from the tank T(LE) by line 30 and is passed through lines 30 and to dock side facilities (not shown) with lines 34 and 174 being in fluid communication with the facilities to provide for pressure equalization.
  • Preparation of the tank T(LE) for the cargo switch involves two operations, i.e., (a) the replacement of the tanks atmosphere with an atmosphere of the material to be transported, and (b) the cooling or heating of the tank to a temperature compatible with that of the boiling point of the material to be stored to thereby reduce or avoid the so-called load flash or a negative pressure which arises when the cryogenic tank is either too warm to too cold, respectively, to receive the new material.
  • Unloading liquefied ethylene in a manner known to those skilled in the art includes the introduction of gaseous ethylene from a shore side source in fluid communication with storage tanks into the space in the tank T(LE) created by the withdrawn liquefied ethylene. After unloading liquefied ethylene from, for example, a 25,000 cubic meter tank, there will remain about 50 metric tons of ethylene vapors at a temperature of about l40F, at a pressure of about 0.5 psig. as well as a residual amount of liquefied ethylene. A predetermined amount of LNG remains in the LNG tanks to maintain the tanks at proper pressure and temperature conditions during the return voyage, as is known to those skilled in the art.
  • the unavoidable boil-off from the LNG tanks is collected in the manifold 66 and a minor portion thereof is introduced into tank T(LE) through line 112 and under the control of valves 116 and 114, respectively, or alternately, through line 94, 100, 104 and 110 via the compressor 98 if the pressure in T(LNG). is insufficient.
  • the remaining portion of the unavoidable boil-off from the LNG tanks is passed to the coil 74 in the fractionating condenser 46 through line 70 under the control of valve 72.
  • Ethylene vapors are gradually downwardly displaced by the natural gas introduced into thetank T(LE) with only limited amount'of cross mixing effected at the interface since natural gas which is essentially methane (with limited amounts of nitrogen) is considerably lighter than the ethylene vapors contained in the tank especially upon being warmed-up by the walls of the tank.
  • the displaced ethylene vapors are withdrawn from tank T(LE) through line 154 under the control of valve 158, line 156, line 34 and line 48 under the control of valve 50 by the compressor 52.
  • Compressed ethylene vapors are then introduced by lines 54 and 40 into the condenser 46 wherein the ethylene vapors are passed in indirect heat transfer relationship with natural gas in coil 74 to liquefy thereby the ethylene vapors.
  • Liquefied ethylene collected in the bottom of the condenser 46 is withdrawn from condenser 46 by pump 122 through line and is passed by line 126 under the control of valve 130 to the liquefied ethylene holding tank 132. Ethylene vapors'in the liquefied ethylene holding tank 132 are returned to the compressor 52 through lines 134, 34 and 48.
  • essentially pure ethylene vapors from the liquefied ethylene tank T(LE) are introduced into the fractionating condenser 46.
  • Trace impurities, such as methane and hydrogen in the ethylene vapors are withdrawn as condenser overhead in line 84 and are passed through coil 88 in condenser 46 to heat the gas prior to introduction into the fuel gas header 82.
  • the gaseous stream in line 154 will contain increasing amounts of methane which necessitates the use of the reboiler coil 63 in condenser 46 to strip the methane from condensed liquefied ethylene accumulating in the bottom of the condenser 46.
  • the liquefied ethylene stored in liquefied ethylene. holding tank 132 will be contaminated with a little methane which is of no consequence in view of the subsequent use of the liquefied ethylene in the tank 132, as more fully hereinafter discussed.
  • a tank may be cooled only a limited number of degrees regardless of the length of time of such procedure. If there were no heat losses, the tank could be cooled to within a few degrees of the temperature of the natural gas introduced into the coil 74 in the condenser 46.
  • the temperature of the tank T( LE) is lowered to a temperature of about 95 to 2()()F.
  • To further reduce the temperature of the tank to about the temperature of the boiling point of LNG would require the introduction of LNG at a controlled rate of injection such as is the normal practice when cooling LNG tanks at the loading terminal.
  • the amount of LNG required to cool the tank is in the order of about 26 metric tons depending upon the heat capacity of the materials of construction of the tank walls and the amount of insulation.
  • Such an amount of LNG to be vaporized is equal to the propulsion fuel requirement of about 2 V2 to 3 hours of a tank ship designed in accordance with the above specification. Consequently, it is thus advantageous to effect such purge procedure during the return voyage of the vessel since vaporizing LNG may be passed to the propulsion unit of the vessel rather than effecting the purge procedure at the loading terminal and burning the purged vapors in a flare stack included in the loading terminal facilities, thereby losing the fuel value thereof.
  • gaseous ethylene Upon introduction into the tank T(LE), gaseous ethylene is condensed in the colder atmosphere and against the colder tank walls thereby warming up both the atmosphere and tank walls. As the pressure tends to increase, gases are withdrawn by line 34 and passed to the fuel gas header 82 via the condenser 46 and the coil 88 through lines 38, 40, 84, 90 and 76. Upon reaching a temperature of about l70F, introduction of gaseous ethylene in line 162 is discontinued and the tank T(LE) permitted to warm up further by natural conduction ('i.e., normal heat leakage).
  • natural conduction 'i.e., normal heat leakage
  • the remaining portion of liquefied ethylene in the holding tank 132 is withdrawn at a controlled rate through line 138 by pump 140 and passed through line 142 and 146 under the control of valves 144 and 150, respectively, and by line 154 into the tank T(LE).
  • the tank T(LE) becomes further warmed by heat transfer from the surrounding environment, a portion of the liquefied ethylene in the tank T(LE) becomes vaporized thereby gradually driving-off the residual amounts of natural gas through line 34 and into the fuel gas header 82, as hereinabove discussed.
  • Liquefied ethylene is introduced into the liquefied ethylene holding tank 132 at the outset of the contemplation of ethylene transportation in an amount or inventory sufficient to replace the natural gas atmosphere in the tank T( LE) by an ethylene atmosphere of relativelyhigh purity. Moreover, the atmosphere will constantly be further purified by continued operation of compressor 52 to maintain the pressure in the tank T( LE) at a constant value upon arrival of the vessel at the on-loading facilities whereat the vapor space of the tank T( LE) is placed in fluid communication by lines 34 and 174 with shore side liquefied ethylene storage tanks without endangering or impairing the quality of liquefied ethylene stored therein.
  • liquefied ethylene may be taken on board without any appreciable load flash loss" occasioned by the tank T(LE) not being in temperature equilibrium with the liquefied ethylene being loaded.
  • a system would require a fleet of six tank ships having the specifications hereinabove described with at least three tank ships modified with the hereinabove discussed reliquefaction system, although it is contemplated that all of the tank ships of the fleet may be so equipped.
  • the ships could carry LNG alone, or LNG and liquefied ethylene depending upon the quantity of liquefied ethylene available to be transported upon arrival of any one of the ships of the fleet at the loading terminal.
  • the captain of the vessel would be accordingly notified and the tank T( LE) would be subjected during the return voyage to the hereinabove discussed purge procedure to change the atmosphere in the tank T(LE) to permit LNG loading.
  • the tank T(LE) had stored LNG and a sufficient quantity of liquefied ethylene is available to fill the tank, the tank T(LE) could be converted to liquefied ethylene handling duty as also hereinabove discussed.
  • the liquefied ethylene would be transported without loss thereof by utilizing the cold potential in the unavoidable boil-off from the LNG tanks during transportation as a result of heat leakage as well as the effects of sea conditions.
  • the storage facilities at the terminals would depend on the capacity of the vessels, and would be nominally sized to store a multiple of about 1.2 to 2.0 times the volume of a vessel.
  • the system of the present invention would be to employ a fleet of vessels equipped with the hereinabove disclosed re-liquefaction facilities, which vessels are in continuous operation between terminals wherein one cryogenic tank of each vessel is capable of handling LNG or liquefied ethylene with provisions to eliminate or minimize ethylene losses and wherein the tank so equipped may be converted to the storage of another liquefied gas during transit of the vessel.
  • the present invention is applicable to the transportation of other combinations of liquefied gas, e.g., LNG-ethane; LNG-LPG; LNG- propane; LNG-ammonia, etc., wherein the liquefied gases have substantially different boiling points. It is particularly advantageously applicable to the transportation of a combination of liquefied gases wherein the lower boiling liquefied gas may be used as fuel for the vessel.
  • the lower boiling gas should be present in an amount to provide the refrigeration potential to condense the unavoidable boil-off of the higher boiling liquefied gas.
  • the respective volumetric capacity of the tank(s) should be in a ratio of at least 4:1 as hereinabove discussed, whereas with other combinations of liquefied gas, the ratios will differ.
  • the transportation of LNG-liquefied ethane would require volumetric ratios of between about 3.0:1 to 3.511 whereas for an LNG-LPG system, a volumetric ratio of as low as 2:1 would be satisfactory.
  • Apparatus for the re-liquefaction of a gas evolved from a first liquefied gas stored in first cryogenic tank means proximate to a second cryogenic tank means storing a second liquefied gas wherein said liquefied gases are stored at about atmospheric pressure and wherein said liquefied gas have different boiling points which comprises:
  • first conduit means for withdrawing a gas from said first cryogenic tank means
  • heat transfer means for passing said gases in indirect heat transfer relationship to re-liquefy the gas withdrawn from the cryogenic tank means storing the higher boiling liquefied gas.
  • the apparatus as defined in claim 10 including a third conduit means for passing said liquefied gas from said heat transfer means to said cryogenic tank means storing said higher boiling liquefied gas.
  • the apparatus as defined in claim 12 including compressor means disposed in said first and second conduit means.
  • the apparatus as defined in claim 12 including a fourth conduit means for the gas withdrawn from said cryogenic tank means storing a lower boiling liquefied gas to .propulsion means for said vessel.
  • Apparatus for modifying a cryogenic tank on a vessel having a plurality of cryogenic tanks for storing at about atmospheric pressure liquefied gases having different boiling points wherein said modified tank is to store a higher boiling liquefied gas which comprises:
  • the apparatus as defined in claim 15 including a third conduit means disposed between said heat transfer means and said one of said plurality of tanks.
  • the apparatus as defined in claim 16 including a fourth conduit means disposed between said heat transfer means and a liquefied gas holding tank.
  • the apparatus as defined in claim 17 including a fifth conduit means disposed between said holding tank and said one of said plurality of cryogenic tanks, and wherein a second heat transfer means is provided in said fifth conduit means.
  • a method for modifying a cryogenic tank on a vessel having a plurality of cryogenic tanks to store at about atmospheric pressure liquefied gases having different boiling points wherein said modified tank is to store a higher boiling liquefied gas of said liquefied gases which comprises:
  • step (a) introducing a portion of said evolved gas of step (a) into said first cryogenic tank means;
  • step (d) passing said liquefied gas recovered from step (d) to a storage holding zone.
  • Apparatus for the preparation of a first cryogenic means for the storage of a first liquefied gas on a vessel having a second cryogenic tank means for the storage of said first liquefied gas wherein said first cryogenic tank means previously stored a second liquefied gas having a boiling point higher than said first liquefied gas which comprises:
  • heat transfer means for passing in indirect heat transfer relationship the gas in said first conduit means and the remaining portion of gas in said second conduit means to liquefy said gas in said first conduit means.
  • the apparatus as defined in claim 28 including a fourth conduit means for passing liquefied gas to a storage tank.
  • introducing into said first cryogenic tank means a gas formed from said first liquefied gas
  • Apparatus for the preparation of a first cryogenic tank means for the storage of a first liquefied gas on a vessel having a second cryogenic tank means for the storage of a second liquefied gas having a lower boiling point than said first liquefied gas and wherein said first cryogenic tank means previously stored said second liquefied gas which comprises:
  • a heat transfer means for passing in indirect heat transfer relationship the gas in each of said second and third conduit means to condense any higher boiling gas in said second conduit means.
  • a method of transporting a first liquefied gas from a loading terminal to an unloading terminal utilizing a plurality of vessels having a first cryogenic tank means for said first liquefied gas and a second cryogenic tank means for a second liquefied gas having a boiling point higher than said first liquefied gas which comprises:
  • a method of transporting a first liquefied gas and a second liquefied gas having a boiling point higher than said first liquefied gas from a loading terminal to an unloading terminal utilizing a plurality of vessels having a first cryogenic tank means for said first liquefied gas and a second cryogenic tank means for said second liquefied gas wherein said cryogenic tank means previously stored said first liquefied gas which comprises:

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Ocean & Marine Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
US354925A 1973-04-27 1973-04-27 Process and apparatus for the storage and transportation of liquefied gases Expired - Lifetime US3877240A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US354925A US3877240A (en) 1973-04-27 1973-04-27 Process and apparatus for the storage and transportation of liquefied gases
JP48099798A JPS502211A (no) 1973-04-27 1973-09-06
NO741457A NO741457L (no) 1973-04-27 1974-04-23 Fremgangsmåte for kondensasjon av gasser
FR7414740A FR2227505B1 (no) 1973-04-27 1974-04-26
NL7405659A NL7405659A (no) 1973-04-27 1974-04-26
DE2420525A DE2420525A1 (de) 1973-04-27 1974-04-27 Verfahren und vorrichtung fuer die lagerung und den transport verfluessigter gase
GB1871074A GB1413456A (en) 1973-04-27 1974-04-29 Re-liquefaction of gas evolved from a cryogenic tank
JP12248680A JPS5694094A (en) 1973-04-27 1980-09-05 Method and device for storing and transporting liquefied gas

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US354925A US3877240A (en) 1973-04-27 1973-04-27 Process and apparatus for the storage and transportation of liquefied gases

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US3877240A true US3877240A (en) 1975-04-15

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JP (2) JPS502211A (no)
DE (1) DE2420525A1 (no)
FR (1) FR2227505B1 (no)
GB (1) GB1413456A (no)
NL (1) NL7405659A (no)
NO (1) NO741457L (no)

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WO1994025541A1 (en) * 1993-05-03 1994-11-10 Den Norske Stats Oljeselskap A.S. Device for recovering excess gas in a plant for the treatment of oil and gas
WO1998059206A1 (en) * 1997-06-20 1998-12-30 Exxon Production Research Company Improved multi-component refrigeration process for liquefaction of natural gas
US6112528A (en) * 1998-12-18 2000-09-05 Exxonmobil Upstream Research Company Process for unloading pressurized liquefied natural gas from containers
US6202707B1 (en) 1998-12-18 2001-03-20 Exxonmobil Upstream Research Company Method for displacing pressurized liquefied gas from containers
US6237347B1 (en) 1999-03-31 2001-05-29 Exxonmobil Upstream Research Company Method for loading pressurized liquefied natural gas into containers
US6257017B1 (en) 1998-12-18 2001-07-10 Exxonmobil Upstream Research Company Process for producing a displacement gas to unload pressurized liquefied gas from containers
US20040068993A1 (en) * 1999-11-05 2004-04-15 Toshikazu Irie Device and method for pressure control of cargo tank of liquefied natural gas carrier
US6729145B1 (en) * 1998-04-17 2004-05-04 Norsk Hydro Asa Process plant
US6810832B2 (en) 2002-09-18 2004-11-02 Kairos, L.L.C. Automated animal house
WO2006128470A2 (en) * 2005-06-02 2006-12-07 Lauritzen Kozan A/S Equipment for a tanker vessel carrying a liquefield gas
US20070193282A1 (en) * 2006-02-22 2007-08-23 The Boeing Company Thermally coupled liquid oxygen and liquid methane storage vessel
US20080110181A1 (en) * 2006-11-09 2008-05-15 Chevron U.S.A. Inc. Residual boil-off gas recovery from lng storage tanks at or near atmospheric pressure
CN100429452C (zh) * 2005-11-03 2008-10-29 常州东昊科技开发有限公司 一种常压中压联合的液相乙烯储存方法
US20110041518A1 (en) * 2009-08-18 2011-02-24 Synfuels International, Inc. method of storing and transporting light gases
US20110132033A1 (en) * 2009-12-07 2011-06-09 Alkane, Llc Conditioning an Ethane-Rich Stream for Storage and Transportation
US20110179810A1 (en) * 2007-11-12 2011-07-28 Sipilae Tuomas Method for operating a lng fuelled marine vessel
US20120017639A1 (en) * 2010-07-21 2012-01-26 Synfuels International, Inc. Methods and systems for storing and transporting gases
EP2540611B1 (en) 2010-02-24 2015-09-30 Samsung Heavy Ind. Co., Ltd. Floating type lng station
US20150330572A1 (en) * 2012-12-14 2015-11-19 Wartsila Finland Oy Method of filling a fuel tank with liquefied gas and liquefied gas system
US20210088185A1 (en) * 2019-09-24 2021-03-25 Exxonmobil Upstream Research Company Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for lng and liquid nitrogen

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US10351111B2 (en) 2017-04-20 2019-07-16 Toyota Motor Engineering & Manufacturing North America, Inc. Automatic brake application for one pedal driving

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Cited By (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2293000A (en) * 1993-05-03 1996-03-13 Norske Stats Oljeselskap Device for recovering excess gas in a plant for the treatment of oil and gas
GB2293000B (en) * 1993-05-03 1997-05-28 Norske Stats Oljeselskap Device for recovering excess gas in a plant for the treatment of oil and gas
US6045659A (en) * 1993-05-03 2000-04-04 Den Norske Stats Oijeselkap A.S. Device for recovery of excess gas in an oil/gas treatment plant
WO1994025541A1 (en) * 1993-05-03 1994-11-10 Den Norske Stats Oljeselskap A.S. Device for recovering excess gas in a plant for the treatment of oil and gas
GB2344641B (en) * 1997-06-20 2001-07-25 Exxon Production Research Co Improved multi-component refrigeration process for liquefaction of natural gas
WO1998059206A1 (en) * 1997-06-20 1998-12-30 Exxon Production Research Company Improved multi-component refrigeration process for liquefaction of natural gas
US5950453A (en) * 1997-06-20 1999-09-14 Exxon Production Research Company Multi-component refrigeration process for liquefaction of natural gas
GB2344641A (en) * 1997-06-20 2000-06-14 Exxon Production Research Co Improved multi-component refrigeration process for liquefaction of natural gas
AT413599B (de) * 1997-06-20 2006-04-15 Exxonmobil Upstream Res Co Verbessertes multikomponenten-kühlungsverfahren zur verflüssigung von erdgas
US6729145B1 (en) * 1998-04-17 2004-05-04 Norsk Hydro Asa Process plant
US6202707B1 (en) 1998-12-18 2001-03-20 Exxonmobil Upstream Research Company Method for displacing pressurized liquefied gas from containers
US6257017B1 (en) 1998-12-18 2001-07-10 Exxonmobil Upstream Research Company Process for producing a displacement gas to unload pressurized liquefied gas from containers
US6112528A (en) * 1998-12-18 2000-09-05 Exxonmobil Upstream Research Company Process for unloading pressurized liquefied natural gas from containers
US6237347B1 (en) 1999-03-31 2001-05-29 Exxonmobil Upstream Research Company Method for loading pressurized liquefied natural gas into containers
US20040068993A1 (en) * 1999-11-05 2004-04-15 Toshikazu Irie Device and method for pressure control of cargo tank of liquefied natural gas carrier
US6901762B2 (en) * 1999-11-05 2005-06-07 Osaka Gas Co., Ltd. Device and method for pressure control of cargo tank of liquefied natural gas carrier
US6810832B2 (en) 2002-09-18 2004-11-02 Kairos, L.L.C. Automated animal house
WO2006128470A2 (en) * 2005-06-02 2006-12-07 Lauritzen Kozan A/S Equipment for a tanker vessel carrying a liquefield gas
WO2006128470A3 (en) * 2005-06-02 2007-10-18 Lauritzen Kozan As Equipment for a tanker vessel carrying a liquefield gas
CN100429452C (zh) * 2005-11-03 2008-10-29 常州东昊科技开发有限公司 一种常压中压联合的液相乙烯储存方法
US20070193282A1 (en) * 2006-02-22 2007-08-23 The Boeing Company Thermally coupled liquid oxygen and liquid methane storage vessel
US7568352B2 (en) * 2006-02-22 2009-08-04 The Boeing Company Thermally coupled liquid oxygen and liquid methane storage vessel
US20080110181A1 (en) * 2006-11-09 2008-05-15 Chevron U.S.A. Inc. Residual boil-off gas recovery from lng storage tanks at or near atmospheric pressure
US20110179810A1 (en) * 2007-11-12 2011-07-28 Sipilae Tuomas Method for operating a lng fuelled marine vessel
US20110041518A1 (en) * 2009-08-18 2011-02-24 Synfuels International, Inc. method of storing and transporting light gases
US9683703B2 (en) 2009-08-18 2017-06-20 Charles Edward Matar Method of storing and transporting light gases
US20110132033A1 (en) * 2009-12-07 2011-06-09 Alkane, Llc Conditioning an Ethane-Rich Stream for Storage and Transportation
US8707730B2 (en) 2009-12-07 2014-04-29 Alkane, Llc Conditioning an ethane-rich stream for storage and transportation
EP2540611B1 (en) 2010-02-24 2015-09-30 Samsung Heavy Ind. Co., Ltd. Floating type lng station
US9764802B2 (en) 2010-02-24 2017-09-19 Samsung Heavy Ind. Co., Ltd. Floating type LNG station
US20120017639A1 (en) * 2010-07-21 2012-01-26 Synfuels International, Inc. Methods and systems for storing and transporting gases
US20150330572A1 (en) * 2012-12-14 2015-11-19 Wartsila Finland Oy Method of filling a fuel tank with liquefied gas and liquefied gas system
US10088108B2 (en) * 2012-12-14 2018-10-02 Wärtsilä Finland Oy Method of filling a fuel tank with liquefied gas and liquefied gas system
US20210088185A1 (en) * 2019-09-24 2021-03-25 Exxonmobil Upstream Research Company Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for lng and liquid nitrogen
US11808411B2 (en) * 2019-09-24 2023-11-07 ExxonMobil Technology and Engineering Company Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for LNG and liquid nitrogen

Also Published As

Publication number Publication date
JPS5694094A (en) 1981-07-30
GB1413456A (en) 1975-11-12
NO135880B (no) 1977-03-07
NO741457L (no) 1974-10-29
JPS502211A (no) 1975-01-10
NO135880C (no) 1977-06-15
FR2227505A1 (no) 1974-11-22
DE2420525A1 (de) 1974-11-14
FR2227505B1 (no) 1979-05-25
NL7405659A (no) 1974-10-29

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