US3285719A - Ofw xx - Google Patents

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US3285719A
US3285719A US3285719DA US3285719A US 3285719 A US3285719 A US 3285719A US 3285719D A US3285719D A US 3285719DA US 3285719 A US3285719 A US 3285719A
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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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
    • F25J1/0255—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature controlling the composition of the feed or liquefied gas, e.g. to achieve a particular heating value of natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/06—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by mixing with gases
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17B—GAS-HOLDERS OF VARIABLE CAPACITY
    • F17B1/00—Gas-holders of variable capacity
    • F17B1/02—Details
    • F17B1/12—Gas admission or discharge arrangements
    • 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
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return 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
    • 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
    • F25J1/0203—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0205—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a dual level SCR refrigeration cascade
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied gas
    • 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
    • F17C2260/00—Purposes of gas storage and gas handling
    • F17C2260/05—Improving chemical properties
    • F17C2260/056—Improving fluid characteristics
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • 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
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • This invention relates to natural gas storage and transmission equipment, and particularly to an improved process and apparatus for liquefying and maintaining in storage, at least a portion of the natural gas iiowing through the transmission equipment, with the B.t.u. value of the inlet gas and the outlet gas being maintained in substantial balance as gas is directed to a user from the outlet line in conjunction with supply of fresh gas to the inlet.
  • the nitrogen and methane which have been liquefied tend to ⁇ boil out of the liquefied gas storage facility first, thereby leaving the higher hydrocarbons in liquefied condition, and causing the output gas from the storage unit to have a lower B.t.u. value per standard cubic foot than the corresponding B.t.u. value of the gas fiowing into the liquefaction plant and thus causing the remaining liquid in the storage unit to have a 3,285,719 Patented Nov. 15, 1966 higher B.t.u. value.
  • a further important object of the invention is to provide an improved method and apparatus for liquefying and storing natural gas, wherein calorimeter controlled structure is employed for continuously measuring the B.t.u. value of the outlet gas from the facility and operably coupled to higher hydrocarbon fortification mechanism for adjusting the amount of higher hydrocarbons intro ⁇ quizd into the outlet gas, to thereby maintain the B.t.u. value thereof at the same level as the B.t.u. value of the inlet gas.
  • Another significant object of the invention is the provision of a method and apparatus for liquefying and storing natural gas, wherein the B.t.u. value of the outlet gas is accurately controlled to maintain the same substantially equal to the B.t.u. value of the inlet gas, thereby necessarily resulting in liquefaction and storage of a product having a B.t.u. value in standard cubic feet as a gas, equal to the inlet and outlet B.t.u. gas values.
  • FIGURE 1 is a schematic representation of preferred apparatus for liquefying and storing natural gas, employed in practicing the novel process of this invention, and adapted to maintain the B.t.u. value of the outlet gas balanced with the B.t.u. value of the inlet gas;
  • FIG. 2 is a schematic representation of a modified form of apparatus for carrying out another method which also is effective in maintaining the B.t.u. values of the inlet and outlet gases substantially equal.
  • the gas inlet line 12 is coupled to a liquid separator vessel 14. Gas supplied to line 12 is first cooled in chiller 85 to a suitably low temperature. The gaseous phase outlet port at the top of vessel 14 is coupled to the inlet 16 of a first heat exchanger 18 by a line 20. The liquid outlet port of vessel 14 is connected to gas outlet line 22 by a line 24. One extremity of line 22 is joined to the outlet 26 of heat exchanger 18. A pneumatically or electrically controlled variable orifice control valve 28 is interposed in line 24 and is operated by a calorimeter 30 operably associated with the gas outlet line by the control line 31.
  • a chiller 32 interposed in line 20, is adapted to be operably coupled to an external refrigeration system not shown, and preferably having a material such as ethylene or Freon therein as the refrigerant medium.
  • the outlet 34 of heat exchanger 18 is coupled to the inlet 36 of a second heat exchanger 38 by line 40, while the outlet 42 of exchanger 38 associated with inlet 36, is connected to an underground storage unit 44 through line 46.
  • a pressure controlled. variable orifice expansion valve 48 is located in line 46 for reducing the pressure on the liquefied gas flowing through line 46, immediately prior to direction of the same into storage unit 44.
  • this structure may take various forms, such as an underground cavern in rock, a metal walled receiver above or below ground, or an underground compartment defined at least in part by a frozen wall of earth and capped by a suitable cover to protect the liquefied natural gas product and to confine vapors therefrom within the storage facility.
  • a bleed line 50 communicating with line 40 between heat exchangers 18 and 38, is operably coupled to the inlet 52 of the heat exchanger 18, and has a temperature controlled, variable orifice expansion valve 54 interposed therein.
  • Another bleed line 56 communicates line 46 with the inlet 58 of heat exchanger 38 and is provided with a temperature controlled, variable orifice expansion valve 60 therein.
  • Control line 62 between valve 48 and line 46 permits the control structure for valve 48 to sense the pressure in line 46, while control line 64 between valve 54 and line 40 and control line 66 between valve 60 and line 46 permit the control units for valves 54 and 60 to sense the temperature of the streams in respective lines 40 and 46.
  • Line 68 interconnecting the outlet 70 of heat exchanger 38 with the inlet 72 of heat exchanger 18, has a T therein communicating line 68 with the storage unit 44 through the line 74.
  • Blower 76 interposed in line 74 directs vapor above the level of liquid in storage unit 44 directly to line 68.
  • the outlet 78 of heat exchanger 18 is connected to line 100 by line 80 having a compressor 82 therein.
  • both of the lines 22 and 80 preferably extend through heat exchangers represented schematicallyy in the drawing and designated broadly by the numeral 85 which serve to raise the temperature of the gaseous product ultimately discharged through the terminus of the outlet line 100, while utilizing the refrigeration available in these cold streams for a useful purpose such as cooling feed gas to the liquefaction unit before it arrives at separator 14 through line 12.
  • the dotted lines in heat exchanger 18 and 38 represent the effective connection of the inlet and outlet ports rather than the actual arrangement of components therein, with line 84 representing the path of iiuid between inlet 52 and outlet 26, while line 86 shows the effective connection between inlet 16 and outlet 34 and line 88 schematically represents the effective intercommunication of inlet 72 with outlet 78. Similarly, the dotted line 90 represents the communication between inlet 36 and outlet 42, with the line 92 representing the connection of inlet 58 with outlet 70.
  • the gaseous stream emanating from the outlet 78 of heat exchanger 18 is directed via line 80 into outlet line 10() with the compressor 82 serving to increase the pressure of the gas.
  • the heat exchange and expansion operations explained above, are effective to lower the temperature of the liquefied product to a level where the same will be obtained in a substantially liquid condition for storage at atmospheric pressure. Therefore, the product should be discharged into storage unit 44 at a temperature of about A--257" F.
  • a certain proportion of the liquefied gas is permitted to boil off and which is directed in vapor form by blower 76 through line 74 directly into line 68.
  • suitable control mechanism is provided in operable association with vessel 14 for assuring collection of sufficient liquefied higher hydrocarbons in vessel 14 to provide the necessary amounts thereof for fortification of gas in line 22 under the demands of calorimeter 30 controlling the size of the orifice of valve 28. This is done by adjusting, as required, the temperature of the inlet stream to vessel 14 to liquefy more or less of the higher hydrocarbons as needed to maintain a quantity thereof in vessel 14.
  • the composition of the natural gas is such that 0.0943 m.m.s.e.f.d. of product comprising mainly higher hydrocarbons in the original natural gas stream, will be liquefied at the temperature and pressure stated and removed from vessel 14 via line 24 under the control of calorimeter 30.
  • the composition is also such that the higher hydrocarbons thus condensed will have a value of 1,700 B.t.u.s per standard cubic foot.
  • the liquefied higher hydrocarbons will actually collect to a certain level in the lower portion of vessel 14, and that the quantity parameter set forth above represents the average amount of the liquefied hydrocarbons which are removed from the separator under the control of valve 28 during continuous operation of the apparatus.
  • the gaseous stream discharged from vessel 14 via line 20 is then passed through the ethylene chiller to effect nearly complete liquefaction of methane, nitrogen and other components which remain in the natural gas stream.
  • the gaseous discharge from vessel 14 will have a B.t.u. value of 1,020 B.t.u.s per standard cubic foot, and it is to be preferred that the liquefied ethylene directed through chiller 32 in heat exchange relationship to the product flowing through line 20, be at a temperature of about 148 F., thereby lowering the natural gas in liquefied condition to a temperature level of about 143 F.
  • the pressure at this point will remain at 600 p.s.i.a.
  • the liquefied product discharged from heat exchanger 18 at outlet 34 will be at a temperature of about 205 F. because of thermal interchange between the liquefied gas flowing along path 86 in heat exchanger 18, and the streams at lower temperatures flowing in countercurrent relationship along paths 84 and 88. It can therefore, be appreciated that the product introduced into heat exchanger 38 at inlet 36 ⁇ is substantially colder than the product entering exchanger 18 at inlet 16. A portion of the product in line 40 is bled therefrom through line 50, with the pressure on the liquefied gas being lowered to about 80 p.s.i.a. across the expansion valve 54.
  • the product remains mainly in liquid form, and is introduced into the heat exchanger 18 for flow along path 84 to cool the liquefied gas flowing along path 86. Because of the difference in temperatures between the products flowing along paths 84 and 86, the product from line 50 will be converted to gaseous form during heating thereof, while the temperature of the liquefied gas from line 20 is lowered to the 205 F. level found in line 40. Sufficient product is diverted from line 40 through bleed line 50, to provide 1.7 m.m.s.c.f.d. of gas at 140 F. at outlet 26 and having a B.t.u. value of 1,020 B.t.u.s per standard cubic foot.
  • the temperature thereof is again substantially lowered by virtue of the fact that a selected proportion of the product is bled from line 46 through line 56 for passage in countercurrent relationship along path 92 between inlet 58 and outlet 70 of heat exchanger 38.
  • the temperature of the liquefied gas discharged from outlet 42 of heat exchanger 38 will be about 240 F., with the temperature of the liquefied gas bled from line 46 through line 56, being lowered to about 254 F. across expansion valve 60.
  • the liquefied product entering heat exchanger 38 through inlet 58, for flow along path 92 undergoes heating in heat exchanger 38, so that the temperature of the product passing out of outlet 7l) will be about 210 F.
  • the contuoller for expansion valve 60 sensing the temperature of the product in line 46, maintains the quantity of the liquefied gas for flow along path 92 of heat exchanger 38, at the proper level to give the cooling required.
  • the expansion valve 60 is also effective to lower the pressure on the product to about 17.7 p.s.i.a., with the pressure drop in the product occurring through the remainder of the line leading to outlet line finally dropping the pressure of the gas down to about 14.7 p.s.i.a. at the inlet of compressor 82.
  • the mixture of gas from line 74 and the product discharged from heat exchanger 38 at outlet 70, is directed into heat exchanger 18 for flow along path 88 in thermal interchange relationship with the liquefied product flowing along path 86.
  • the gaseous product discharged from heat exchanger 18 at outlet 78 will have a temperature of 148 F. Since 0.5 m.m.s.c.f.d. of product having a B.t.u. value of 1,020 B.t.u.s per standard cubic foot is removed from line 46 via line 56, this quantity of gas will be mixed with the proportion introduced into line 68 via line 74, resulting in a total of 3.1943 m.m.s.c.f.d. of gas of a B.t.u.
  • the higher hydrocarbons removed from the natural gas stream within separator 14, are introduced into the gas stream flowing through line 22 by line 24, with the 1,700 B.t.u.s per standard cubic foot product in line 24 enriching the 1,020 B.t u.s per standard cubic foot gas in line 22 to thereby bring the combined gas in outlet line 100 to the required level of 1,035 B.t.u.s per standard cubic foot, equal to the B.t.u. content of the inlet gas in line 12.
  • the calorimeter 30 operably coupled to valve 28 accurately determines the B.t.u. content of the outlet gas and varies the amount of higher hydrocarbons delivered thereto in accordance with the needs of the system.
  • FIG. 2 An alternative arrangement for liquefying and storing natural gas while maintaining the B.t.u. value of the outlet gas from the facility equal to the B.t.u. value of the inlet gas, is illustrated in FIG. 2 with the arrangement and components illustrated in FIG. 1 being preferred only because a greater quantity of the gas product may be stored in liquefied condition than is the case with the FIG. 2 arrangement.
  • the natural gas liquefying and storage apparatus broadly designated in FIG. 2 also has a natural gas inlet line 112 which leads to a liquid separator vessel 114.
  • the gas exhaust port of separator vessel 114 is coupled to the inlet 116 of heat exchanger 118 by line 120.
  • the gas outlet line 200 of apparatus 110 is connected by line 122 to the outlet 126 of heat exchanger 118- while a liquid higher hydrocarbon line 124 extends between the liquid outlet of separator vessel 114 and line 122.
  • a variable oritlce calorimeter controlled valve 128 is interposed in line 124, so that the amount of higher hydrocarbon liquid delivered to line 122 may be selectively controlled.
  • the calorimeter 130 is coupled to valve 128 through the control line 131 and is operable to continuously sense the B.t.u. value of the gas flowing through outlet line 200.
  • the gas outlet line 120 from separator 114 passes through a heat exchanger 132 comprising the chiller portion of an ethylene refrigeration system which is not illustrated in detail in the drawing.
  • the outlet 134 of heat exchanger 118 is connected to the inlet 136 of a liquid separator vessel 139 by a line 140 having a pressure controlled expansion valve 154 interposed therein.
  • the control line 164 for valve 154 senses the pressure of the liquid in line 140 upstream of valve 154.
  • the gas exhaust port at the upper extremity' of separator vessel 139 is connected ⁇ to the inlet 152 of heat exchanger 118 by a line 150, while the liquid outlet line 141 leading from the lower portion of vessel 139A is coupled to the inlet 143 of heat exchanger 138.
  • the outlet 142 of heat exchanger 138 is joined to the inlet of another separator vessel 145 by line 147 having a level control expansion valve therein.
  • the control line 166 for valve 160 extends to a liquid level sensing device within separator vessel 139.
  • the gas exhaust port of separator 145 is joined to the inlet 158 of heat exchanger 138 by a line 149, while the outlet of ⁇ heat exchanger 138 is joined to vapor line 174 by line 168.
  • the liquid outlet at the lower extremity of separator vessel 145 is connected directly to the liquefied gas storage unit 144 by a line 146 having a level control expansion valve 148 therein which is provided with a control line 162 which extends to a level sensing device within separator vessel 145.
  • the storage unit 144 is of the same type as outlined with respect to unit 44 of FIG. 1 and is preferably, although not necessarily, recessed in the ground as previously described. from the upper extremity of storage unit 144 to the inlet 172 of heat exchanger 118 and is provided with a blower 176 therein downstream of the point of connection of the line 168 to line 174.
  • Line 180 joined to the outlet 178 of heat exchanger 118, is coupled to gas outlet line 280, and has a compressor 182 interposed therein downstream of the heat exchangers 184 which are similar in construction and operation to previously described heat exchangers 85.
  • ] is connected to both of the lines 122 and 180 to direct outlet gas to a point of use.
  • the llow path of product between inlet 152 and outlet 126 of heat exchanger 118 is represented schematically by the dotted line 185 while the dotted lines 186 and 188 represent the ow paths between inlet 116 and outlet 134, and inlet 172 and outlet 180 respectively.
  • dotted line represents the flow path between inlet 143 and outlet 142 of heat exchanger 138 and line 192 illustrates the fluid flow path between inlet 158 and Outlet 170.
  • Apparatus 110 operates in a manner similar to the operation of apparatus 10, with the exception of the way in which the product is permitted to expand within separators 139 and 145 and which is not the case in the equivalent lines 50 and 56 of apparatus 10. Since the Vapor line 174 extends Llll] previously cooled natural gas entering separator vessel 114 contains both gaseous and liquid components, the liquid fraction is collected in the lower portion of the vessel for ultimate discharge therefrom through line 124. Fortiiication liquid from vessel 114 is directed to the gas in line 122 under the control of valve 128.
  • the gas from the outlet of separator 114 will thereby have a B.t.u. value of 1,013 B.t.u.s per standard cubic foot.
  • the gas passing out of the Lipper end of vessel 114 flows through Chiller 132 and is lowered to a temperature of 143 F. by liquefied ethylene passing through the chiller at an inlet temperature of 148 F.
  • the liquelied product flowing along path 186 in heat exchanger 118 is reduced in temperature from the inlet level of 143 F., to 162 F. Expansion ofthe liquefied gas across valve 154 and into separator 139, further lowers the temperature of the product to 210 F. with the liqueed material flowing into heat exchanger 138 through line 141.
  • the gas collected at the top of vessel 139 is returned to heat exchanger 18 via line 150.
  • Gas flowing out of outlet 126 of heat exchanger 118 will have a temperature of 148 F. and the pressure of liquefied product flowing through expansion valve 154 is preferably lowered to a level of about 80 p.s.i.a.
  • the liquefied natural gas flowing along path 190 in heat exchanger 138 will be decreased in temperature from 210 F. to about 216 F., whereby further lowering of the pressure of the liquid across expansion valve 160 to about 17.7 p.s.i.a., decreases the temperature ofthe product to about 254 F.
  • the liquid in the lower portion of separator vessel 145 flows through the expansion valve 148 into storage unit 144.
  • Valve 148 lowers the pressure of the liquid to atmospheric level, and effects further lowering ofthe temperature of the liquefied gas to 257 F.
  • the gas from the overhead of separator vessel 154 flows via line 149 into exchanger 138 for tlow along path 192 into line 168 leading to line 174.
  • the temperature of the product flowing along path 192 is increased to about 215 F. from the level of 254 F. in vessel 145.
  • the product flowing through line 168 combines with vapor from the top of the liquefied natural gas in storage unit 144, which is directed to heat exchanger 118 via line 174, whereby the gas is brought into thermal interchange relationship with the liquefied gas flowing along path 186, and resulting in the gas emanating from the outlet 178 of heat exchanger 118 and flowing in line 180, having a temperature of about 148 F.
  • the quantity of gas discharged from the overheads of separator vessels 139 and 14S and storage unit 144 results in 2.5 m.m.s.c.f.d. of product being introduced into the unit 144 while 3.318 m.rn.s.c.f.d. of gas is discharged from the outlet line 200l and representing the combination of gas from lines 122 and 180.
  • the final quantity of outlet gas in line 200 is made up of this 1,500 B.t.u. stream plus 1.7 m.m.s.c.f.d. of 1,000 B.t.u.s per standard cubic foot gas owing through line 122, and 1.4 m.m.s.c.f.d. of 1,005 B.t.u.s per standard cubic foot gas flowing through line 180.
  • the heat exchangers 184 and compressor 182 serve to increase the temperature of the final gas to +50 F. and at a pressure of 50 p.s.i.a.
  • apparatus 10 as well as apparatus 110, operate to maintain the B.t.u. values of the inlet and outlet gas streams equal, but with a somewhat greater proportion of the gas being liquefied for storage in apparatus 10 than is the case with apparatus 110.
  • a process as set forth in claim 1 wherein the amount of said liquid product permitted to vaporize is the quantity which thermally maintains the temperature of the liquid product at said second temperature level.
  • Gas transmission apparatus for natural gas having nitrogen, a major proportion of methane and C2 and higher hydrocarbons therein, comprising: a gas inlet line; a gas outlet line; structure coupled to said inlet line for cooling the natural gas owing therethrough to a first temperature level to effect liquefaction of ⁇ a certain proportion of the higher hydrocarbons in the gas without effecting liquefaction of the bulk of the methane therein; said structure including means for separating the gaseous phase from the liquid phase of the natural gas product; components operably connected to said structure for cooling the gaseous phase of the natural gas emanating from said structure to a second temperature level to effect liquefaction thereof and producing a liquefied gas product; a storage unit coupled to said components for ⁇ receiving the liquefied gas product therefrom', pipe means coupling the storage unit to said outlet line for directing vapor from the liquefied gas product in the storage unit to the outlet line; and means operably associated with said outlet line and the separating means of said structure for adding a
  • said components include conduit means between said structure and the storage unit, heat exchange means operably associated with said conduit for lowering the temperature of the gas emanating from said structure to a level to liquefy the same, a pair of expansion valves interposed in said conduit downstream of said heat exchange means, a liquid separator in the conduit downstream of each of the expansion valves, and fluid conveying means coupled to said liquid separators and the outlet line for conveying the gaseous phase product from said separators to the outlet line.
  • said components include conduit means between the structure and said storage unit, a pair of heat exchangers in series relationship in said conduit means, a rst line communicating the conduit means at a point between said heat exchangers with the outlet line and operably coupled with the first heat exchanger downstream of said structure for bringing the liquefied gas product removed from the conduit means into heat exchange relationship with the liquefied gas product flowing through the conduit means in countercur- ⁇ rent relationship, an expansion valve in said first line between the conduit means and said first heat exchanger, and a second line communicating the conduit means to a point downstream of the second heat exchanger with the outlet line and operably coupled t0 said second heat exchanger for bringing the liquefied gas product removed from the conduit means into heat exchange relationship with the liquefied gas product flowing through the conduit means in countercurrent relationship.

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  • General Chemical & Material Sciences (AREA)
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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3331214A (en) * 1965-03-22 1967-07-18 Conch Int Methane Ltd Method for liquefying and storing natural gas and controlling the b.t.u. content
US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
US3407613A (en) * 1966-09-13 1968-10-29 Nat Distillers Chem Corp Enrichment of natural gas in c2+ hydrocarbons
US3419369A (en) * 1965-03-19 1968-12-31 Phillips Petroleum Co Manufacturing town gas from liquefied natural gas
US3469956A (en) * 1966-06-08 1969-09-30 E Sam Dick Co Inc Standby liquefied petroleum gas unit
DE1933080A1 (de) * 1968-07-03 1970-01-22 Air Liquide Verfahren zur Herstellung eines methanreichen Gases
US3527585A (en) * 1967-12-01 1970-09-08 Exxon Research Engineering Co Method and apparatus for the control of the heating value of natural gas
US3607153A (en) * 1968-09-20 1971-09-21 Selas Corp Of America Quench arrangement
US3658499A (en) * 1970-10-28 1972-04-25 Chicago Bridge & Iron Co Method of diluting liquefied gases
US3837821A (en) * 1969-06-30 1974-09-24 Air Liquide Elevating natural gas with reduced calorific value to distribution pressure
WO2011073931A1 (fr) * 2009-12-18 2011-06-23 Total S.A. Procede de production de gaz naturel liquefie ayant un pouvoir calorifique superieur ajuste

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2541569A (en) * 1945-04-02 1951-02-13 Paul L Born Liquefying and regasifying natural gases

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3419369A (en) * 1965-03-19 1968-12-31 Phillips Petroleum Co Manufacturing town gas from liquefied natural gas
US3331214A (en) * 1965-03-22 1967-07-18 Conch Int Methane Ltd Method for liquefying and storing natural gas and controlling the b.t.u. content
US3469956A (en) * 1966-06-08 1969-09-30 E Sam Dick Co Inc Standby liquefied petroleum gas unit
US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
US3407613A (en) * 1966-09-13 1968-10-29 Nat Distillers Chem Corp Enrichment of natural gas in c2+ hydrocarbons
US3527585A (en) * 1967-12-01 1970-09-08 Exxon Research Engineering Co Method and apparatus for the control of the heating value of natural gas
DE1933080A1 (de) * 1968-07-03 1970-01-22 Air Liquide Verfahren zur Herstellung eines methanreichen Gases
US3607153A (en) * 1968-09-20 1971-09-21 Selas Corp Of America Quench arrangement
US3837821A (en) * 1969-06-30 1974-09-24 Air Liquide Elevating natural gas with reduced calorific value to distribution pressure
US3658499A (en) * 1970-10-28 1972-04-25 Chicago Bridge & Iron Co Method of diluting liquefied gases
WO2011073931A1 (fr) * 2009-12-18 2011-06-23 Total S.A. Procede de production de gaz naturel liquefie ayant un pouvoir calorifique superieur ajuste
FR2954345A1 (fr) * 2009-12-18 2011-06-24 Total Sa Procede de production de gaz naturel liquefie ayant un pouvoir calorifique superieur ajuste

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DE1245396C2 (de) 1973-07-19
ES293448A1 (es) 1964-01-16
AT263729B (de) 1968-08-12

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