US3315477A - Cascade cycle for liquefaction of natural gas - Google Patents

Cascade cycle for liquefaction of natural gas Download PDF

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US3315477A
US3315477A US382774A US38277464A US3315477A US 3315477 A US3315477 A US 3315477A US 382774 A US382774 A US 382774A US 38277464 A US38277464 A US 38277464A US 3315477 A US3315477 A US 3315477A
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gas
stream
vapor
liquefied
pressure
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US382774A
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Jackson O Carr
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Conch International Methane Ltd
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Conch International Methane Ltd
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Priority to US382774A priority patent/US3315477A/en
Priority to FR23005A priority patent/FR1441863A/en
Priority to NL6509009A priority patent/NL6509009A/xx
Priority to OA52113A priority patent/OA01771A/en
Priority to DEC36403A priority patent/DE1256666B/en
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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
    • F25J1/0203—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
    • F25J1/0208—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 in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • F25J1/0209—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 in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop as at least a three level refrigeration cascade
    • F25J1/021—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 in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop as at least a three level refrigeration cascade using a deep flash recycle loop
    • 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
    • F25J1/003—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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0085—Ethane; 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
    • 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
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • 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
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • 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
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
    • 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

Definitions

  • This invention relates to the liquefaction of gas and more particularly to a method for the liquefaction of natural gas, which is normally composed mostly of methane but may contain relatively small proportions of both higher hydrocarbons and lower boiling-point components such as nitrogen.
  • the general system is similar, but represents an improvement over that disclosed in US. Patent No. 3,020,723 to De Lury et al.
  • the invention is particularly useful for liquefying natural gas that is lean in components which exhibit higher vapor pressures than methane (such as nitrogen, hydrogen and helium).
  • natural gas enters the plant at a high pressure and is cooled and liquefied by heat exchange in closed systems with an ethylene, propane and methane cascade refrigeration system, as is also done in the De Lury patent mentioned above.
  • the final cooling is achieved by flashing the liquefied natural gas, and the flash vapors are then re-cornpressed and recycled to the inlet feed gas stream, thereby eliminating the separate heat exchangers previously needed to cool and condense the methane refrigerant.
  • a portion of the liquefied gas is withdrawn from the main stream prior to subcooling for tempering the cold flash gases which are subsequently compressed for recycling to the inlet gas feed stream mentioned above to avoid feeding extremely cold gas to the compressors.
  • the use of flash drums in the low levels eliminates more costly heat exchangers.
  • the main object is to reduce the power requirement for liquefying natural gas, to simplify the process and reduce the equipment required.
  • the flow chart of the drawing shows in detail one system for the practice of the invention, with temperatures and pressures given for a typical type of gas at a particular initial pressure and temperature, it will be understood that this is merely exemplary, and that the operating conditions and subdivision of stages may be varied in accordance with known design considerations to suit particular conditions and materials.
  • the gas to he liquefied is assumed to be a lean natural gas relatively free of components that exhibit higher vapor pressure than methane, which is the principal ingredient, and which is assumed to enter the flow line 1 at a temperature of 70 F. and at a pressure of 600 p.s.i.a.
  • the refrigeration cycle for reducing the compressed gas to a liquefied state is a modified cascade system having a sequence of refrigeration steps including a propane refrigeration cycle, an ethylene refrigeration cycle, and a methane refrigeration cycle, as indicated in the drawing. Since the propane and ethylene cycles are generally similar to those employed in the De Lury Patent No. 3,020,- 723 mentioned above, they will be described only briefly. The temperatures and the significant pressures at various stages are as indicated in the drawing.
  • Gas entering at 1 is initially cooled to a temperature of approximately 30 F. in heat exchanger 2 and to a temperature of approximately -31 F. in heat exchanger 3, by heat exchange with evaporating propane from the propane cycle.
  • the propane is stored in container 4 at F. and at a pressure of p.s.i.a. This is taken in line 6 through throttle valve 7 to supply propane refrigerant to heat exchanger 2 and the pressure is reduced to produce the indicated temperature in the feed gas line .1, the propane being reduced in temperature to 25 F., at which temperature the propane vapor is conducted fromthe shell of heat exchanger 2 in line 8 into line 9, and hence to second stage compressor 11, where its pressure is raised from 60.6 p.s.i.a. to 140 p.s.i.a.
  • Propane from line 14 is similarly reduced in pressure by throttle valve 21 and evaporated in heat exchanger 22 prior to rejoining the stream from heat exchanger 3, for a second stage of cooling which reduces the temperature of the ethylene in line 23 to a temperature of 23 F., at which temperature it is condensed and is stored in ethylene container 24.
  • the natural gas in line 1 now continues through several similar stages of ethylene heat exchange in exchanges 25, 26, 27 and 28, with further temperature reductions at each stage as indicated lay the drawing.
  • the ethylene in turn is similarly compressed in a series of compressors (which may be a multi-stage compressor) as indicated in the flow chart, the number of stages and the temperatures for each stage being selected in accordance with known principles.
  • the various throttle valves e.g., valves 13, 17, 21, 16, etc., are part of conventional level control devices used to maintain the proper liquid level in their respective heat exchangers.
  • the feed gas After passing through heat exchanger 28, the feed gas is at a temperature of 144 F., and being still at a high pressure, it is now below its critical temperature and in liquid phase.
  • the main stream of now liquid natural gas continues through three more heat exchange stages in heat exchangers 31, 32 and 33 respectively, to reduce its temperature to approximately 195 F., at which point it is passed through throttle valve 35 into flash drum 36.
  • a portion of the stream is diverted between heat exchangers 28 and 31 in line 37 for heat exchange with the cold flash vapors from flash drums 36 and 38, to recover the refrigeration in these vapors, and to temper the gases going into the compressors, as will now be described.
  • the liquefied feed gas is flashed in flash drum 36 on reducing the pressure to 70 p.s.i.a. thus lowering its temperature to 216 F. It is then passed through throttle valve 39 into second flash drum 38, Where its pressure is reduced to 27 p.s.i.a., thus lowering the temperature to 242 F.
  • Liquefied feed gas from line 37 is heat exchanged in exchanger 41 with the flash vapors from flash drum 36 to raise the temperature of the flash vapor in line 42 to F., and correspondingly cool the liquid methane, which is then passed through throttle valve 43 to control the rate of flow returned to the main stream in line 1 and thence into flash drum 36, together with the main stream of liquefied feed gas in line 1.
  • liquefied feed gas in line 37 is withdrawn in line 44 for heat exchange in exchanger 46 with flash vapors from flash drum 38, and then passed through throttle valve 47 into flash drum 38.
  • the remaining liquefied feed gas in line 37 is used in heat exchanger 48 to temper the vapors in line 49, which are now substantially at atmospheric pressure.
  • Liquefied gas at 242 F. from flash drum 38 continues on main line 1 through final stage heat exchanger 51, where its temperature is reduced to 251 F. by heat exchange with evaporating liquid withdrawn from line 1 through throttle valve 52.
  • a final pressure reduction stage and throttle valve 53 reduces the pressure of the liquefied gas to slightly above atmospheric pressure, and a temperature of 25 8 F.-, for storage in a suitable storage facility 54, which may be an iu-ground large-scale storage tank, or any other suitable storage facility, in which it is stored essentially as a boiling liquid at slightly above atmospheric pressure.
  • vapors are removed on line 56 from the storage tank 54 and compressed by a low pressure blower 57 into line 58, where it joins the vapor stream in line 49 for the first stage of compression by methane compressors 59, 60, 61, which may be a multistage single compressor, for raising the pressure of the methane in lines 49, 45 and 42 respectively as indicated in the flow chart.
  • methane compressors 59, 60, 61 which may be a multistage single compressor, for raising the pressure of the methane in lines 49, 45 and 42 respectively as indicated in the flow chart.
  • methane compressors 59, 60, 61 which may be a multistage single compressor, for raising the pressure of the methane in lines 49, 45 and 42 respectively as indicated in the flow chart.
  • the methane now at 275 p.s.i.a. and above ambient temperature is cooled by cooling water heat exchange in exchanger 63 to 70 R, where some of it may be used on line 64 as plant fuel.
  • the method of liquefying a gas comprising (a) supplying the gas in a main feed stream at high pressure and essentially ambient temperature,
  • step (c) withdrawing from said main feed stream a portion of the liquefied gas from step (b) as a side stream,
  • step (e) throttling said subcooled liquid gas from step (d) into a flash drum at a reduced pressure to flash off part of the gas as a vapor and still further cool the residual liquid gas
  • step (f) heat exchanging liquefied gas from said side stream of step (c) with the flash vapor from step (e) to further subcool said liquefied side stream gas
  • step (e) throttling said subcooled liquid gas from step (d) into a flash drum at a reduced pressure to flash 011? part of the gas as a vapor and still further cool the residual liquid gas,
  • step (f) heat exchanging liquefied gas from said side stream of step (c) with the flash vapor from step (e) to further subcool said liquefied side stream gas
  • step (g) throttling said liquefied subcooled side stream gas of step (t) into the flash drum to rejoin the main 7 V I stream,
  • step (c) withdrawing'from said main feed stream a portion of the liquefied gas from step (b) as a side stream
  • step (e) throttling said subcooled liquid gas from step (d) into a flash drum at a reduced pressure to flash ofi part of the gas as a vapor and still further cool the residual liquid gas
  • step (f) heat exchanging liquefied gas from said stream of step (c) with the flash vapor from step (e) to further subcool said liquefied side stream gas
  • step (g) throttling said liquefied subcooled side stream gas of step (f) into the flash drum to rejoin the main stream
  • step (i) further throttling the residual liquid gas from step (e) into a second flash drum at a further reduced pressure to produce vapor at a lower pressure than in step (e) and to further subcool the residual liquid (j) heat exchanging liquefied gas from the side stream of step (c) with the flash vapor from the preceding step, and

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Description

United States Patent 3,315,477 CASCADE CYCLE FOR LIQUEFACTION OF NATURAL GAS Jackson 0. Carr, Shawnee Mission, Kans., assignor to Conch International Methane Limited, Nassau, Bahamas, a company of the Bahamas Filed July 15, 1964, Ser. No. 382,774 4 Claims. (Cl. 62-23) This invention relates to the liquefaction of gas and more particularly to a method for the liquefaction of natural gas, which is normally composed mostly of methane but may contain relatively small proportions of both higher hydrocarbons and lower boiling-point components such as nitrogen. The general system is similar, but represents an improvement over that disclosed in US. Patent No. 3,020,723 to De Lury et al. The invention is particularly useful for liquefying natural gas that is lean in components which exhibit higher vapor pressures than methane (such as nitrogen, hydrogen and helium).
According to the invention, natural gas enters the plant at a high pressure and is cooled and liquefied by heat exchange in closed systems with an ethylene, propane and methane cascade refrigeration system, as is also done in the De Lury patent mentioned above. However, instead of employing a closed system of pure methane refrigerant in the final refrigeration stages, the final cooling is achieved by flashing the liquefied natural gas, and the flash vapors are then re-cornpressed and recycled to the inlet feed gas stream, thereby eliminating the separate heat exchangers previously needed to cool and condense the methane refrigerant. In addition, a portion of the liquefied gas is withdrawn from the main stream prior to subcooling for tempering the cold flash gases which are subsequently compressed for recycling to the inlet gas feed stream mentioned above to avoid feeding extremely cold gas to the compressors. The use of flash drums in the low levels eliminates more costly heat exchangers.
As is apparent from the above, the main object is to reduce the power requirement for liquefying natural gas, to simplify the process and reduce the equipment required.
The specific nature of my invention, as Well as other objects and advantages thereof, will clearly appear from a description of a preferred embodiment as shown in the accompanying drawing in which the figure is a flow diagram illustrating the process of the invention for the liquefaction of natural gas.
While the flow chart of the drawing shows in detail one system for the practice of the invention, with temperatures and pressures given for a typical type of gas at a particular initial pressure and temperature, it will be understood that this is merely exemplary, and that the operating conditions and subdivision of stages may be varied in accordance with known design considerations to suit particular conditions and materials. In the example, the gas to he liquefied is assumed to be a lean natural gas relatively free of components that exhibit higher vapor pressure than methane, which is the principal ingredient, and which is assumed to enter the flow line 1 at a temperature of 70 F. and at a pressure of 600 p.s.i.a. The refrigeration cycle for reducing the compressed gas to a liquefied state is a modified cascade system having a sequence of refrigeration steps including a propane refrigeration cycle, an ethylene refrigeration cycle, and a methane refrigeration cycle, as indicated in the drawing. Since the propane and ethylene cycles are generally similar to those employed in the De Lury Patent No. 3,020,- 723 mentioned above, they will be described only briefly. The temperatures and the significant pressures at various stages are as indicated in the drawing.
Gas entering at 1 is initially cooled to a temperature of approximately 30 F. in heat exchanger 2 and to a temperature of approximately -31 F. in heat exchanger 3, by heat exchange with evaporating propane from the propane cycle. The propane is stored in container 4 at F. and at a pressure of p.s.i.a. This is taken in line 6 through throttle valve 7 to supply propane refrigerant to heat exchanger 2 and the pressure is reduced to produce the indicated temperature in the feed gas line .1, the propane being reduced in temperature to 25 F., at which temperature the propane vapor is conducted fromthe shell of heat exchanger 2 in line 8 into line 9, and hence to second stage compressor 11, where its pressure is raised from 60.6 p.s.i.a. to 140 p.s.i.a. and condensed at 70 F. by 'heat exchange with cooling water in exchanger 12 and returned to the storage container 4. Some of the propane is taken from the shell of heat exchanger 2 in line 14, further expanded through throttle valve 16 for the second heat exchange step in exchanger 3, and similarly returned to first stage compressor 17, where its pressure is raised from 16.4 p.s.i.a. to 60.6 p.s.i.a., at which pressure it joins the propane from line 9 for second stage compression at 11 as previously indicated. Some of the propane from line 6 is also passed through throttle valve 18 to reduce its pressure for use in heat exchanger 19 for cooling ethylene from the last compression stage of the ethylene cycle, from a temperature of 70 F., and then joins the stream from line 9 in line 9 as previously described. Propane from line 14 is similarly reduced in pressure by throttle valve 21 and evaporated in heat exchanger 22 prior to rejoining the stream from heat exchanger 3, for a second stage of cooling which reduces the temperature of the ethylene in line 23 to a temperature of 23 F., at which temperature it is condensed and is stored in ethylene container 24. The natural gas in line 1 now continues through several similar stages of ethylene heat exchange in exchanges 25, 26, 27 and 28, with further temperature reductions at each stage as indicated lay the drawing. The ethylene in turn is similarly compressed in a series of compressors (which may be a multi-stage compressor) as indicated in the flow chart, the number of stages and the temperatures for each stage being selected in accordance with known principles. It will be understood that the various throttle valves, e.g., valves 13, 17, 21, 16, etc., are part of conventional level control devices used to maintain the proper liquid level in their respective heat exchangers.
After passing through heat exchanger 28, the feed gas is at a temperature of 144 F., and being still at a high pressure, it is now below its critical temperature and in liquid phase. The main stream of now liquid natural gas continues through three more heat exchange stages in heat exchangers 31, 32 and 33 respectively, to reduce its temperature to approximately 195 F., at which point it is passed through throttle valve 35 into flash drum 36. However, a portion of the stream is diverted between heat exchangers 28 and 31 in line 37 for heat exchange with the cold flash vapors from flash drums 36 and 38, to recover the refrigeration in these vapors, and to temper the gases going into the compressors, as will now be described.
After passing through throttle valve 35, the liquefied feed gas is flashed in flash drum 36 on reducing the pressure to 70 p.s.i.a. thus lowering its temperature to 216 F. It is then passed through throttle valve 39 into second flash drum 38, Where its pressure is reduced to 27 p.s.i.a., thus lowering the temperature to 242 F.
Liquefied feed gas from line 37 is heat exchanged in exchanger 41 with the flash vapors from flash drum 36 to raise the temperature of the flash vapor in line 42 to F., and correspondingly cool the liquid methane, which is then passed through throttle valve 43 to control the rate of flow returned to the main stream in line 1 and thence into flash drum 36, together with the main stream of liquefied feed gas in line 1. Similarly, liquefied feed gas in line 37 is withdrawn in line 44 for heat exchange in exchanger 46 with flash vapors from flash drum 38, and then passed through throttle valve 47 into flash drum 38. The remaining liquefied feed gas in line 37 is used in heat exchanger 48 to temper the vapors in line 49, which are now substantially at atmospheric pressure.
Liquefied gas at 242 F. from flash drum 38 continues on main line 1 through final stage heat exchanger 51, where its temperature is reduced to 251 F. by heat exchange with evaporating liquid withdrawn from line 1 through throttle valve 52. A final pressure reduction stage and throttle valve 53 reduces the pressure of the liquefied gas to slightly above atmospheric pressure, and a temperature of 25 8 F.-, for storage in a suitable storage facility 54, which may be an iu-ground large-scale storage tank, or any other suitable storage facility, in which it is stored essentially as a boiling liquid at slightly above atmospheric pressure. Since it is in a boiling condition, vapors are removed on line 56 from the storage tank 54 and compressed by a low pressure blower 57 into line 58, where it joins the vapor stream in line 49 for the first stage of compression by methane compressors 59, 60, 61, which may be a multistage single compressor, for raising the pressure of the methane in lines 49, 45 and 42 respectively as indicated in the flow chart. After leaving compressor 61, the methane, now at 275 p.s.i.a. and above ambient temperature is cooled by cooling water heat exchange in exchanger 63 to 70 R, where some of it may be used on line 64 as plant fuel. The remainder of the methane is passed in line 66 through additional compressor stage 67 to line 68, and after further water cooling in exchanger 69, is returned on line 71 at a temperature of 70 F. and at the pressure of the incoming natural gas, to join the feed gas stream on line 1. It will be noted that any small amount of impurities of higher vapor pressure than methane (e.g., nitrogen) will ultimately be removed on line 64 with the feed gas stream, and therefore do not require special treatment. For high concentrations of high .vapor pressure impurities, the impurities may be removed by conventional means.
It will be apparent that the embodiments shown are only exemplary and that various modifications can be made in construction and arrangement within the scope of my invention as defined in the appended claims.
I claim:
1. The method of liquefying a gas comprising (a) supplying the gas in a main feed stream at high pressure and essentially ambient temperature,
(b) removing heat from the gas to cool the gas to a temperature at which it is in a liquid state at said high pressure, 7
(c) withdrawing from said main feed stream a portion of the liquefied gas from step (b) as a side stream,
(d) subcooling the rest of the gas in said main stream to a still lower tempearture than the gas in the side stream,
(e) throttling said subcooled liquid gas from step (d) into a flash drum at a reduced pressure to flash off part of the gas as a vapor and still further cool the residual liquid gas,
(f) heat exchanging liquefied gas from said side stream of step (c) with the flash vapor from step (e) to further subcool said liquefied side stream gas,
(g) throttling said liquefied subcooled side stream gas of step (t) into the flash drum to rejoin the main stream, 7
(h) throttling the subcooled main stream liquefied gas into a storage container as liquefied gas at substantially atmospheric pressure,
(i) withdrawing vapor from said storage container to maintain the pressure in said container at substantially atmospheric pressure,
(j) compressing said vapor in multi-stage compression and cooling said compressed vapor to ambient temperature,
(k) withdrawing part of said compressed vapor for use as product, and
(1) further compressing the remainder of said compressed vapor to about the initial pressure of the main feed stream, and returning it to the entry point (c) withdrawing from said main feed stream a portion of the liquefied gas from step (b) as a side stream,
(d) subcooling the rest of the gas in said main stream to a still lower temperature than the gas in the side stream,
(e) throttling said subcooled liquid gas from step (d) into a flash drum at a reduced pressure to flash 011? part of the gas as a vapor and still further cool the residual liquid gas,
(f) heat exchanging liquefied gas from said side stream of step (c) with the flash vapor from step (e) to further subcool said liquefied side stream gas,
(g) throttling said liquefied subcooled side stream gas of step (t) into the flash drum to rejoin the main 7 V I stream,
(h) throttling the subcooled main stream liquefied gas' into a storage container as liquefied gas at substantially atmospheric pressure,
(i) removing a small portion of the main fuel stream after said flash drum subcooling, (j) reducing the pressure of said removed small portion and passing it at substantially atmospheric pressure in heat-exchange relationship with the main stream to further subcool the main stream prior to storage, while expanding said small portion to a vapor condition,
(k) heat exchanging liquefied gas from said side stream with the vapor from the preceding step to further cool said side stream, and
(l) returning the further cooled side stream from the preceding step to the main stream.
4. The method of liquefying a gas comprising (a) supplying the gas in a main feed stream at high pressure and essentially ambient temperature,
(b) removing heat from the gas to cool the gas to a temperature at which it is in a liquid state at 'said high pressure,
(c) withdrawing'from said main feed stream a portion of the liquefied gas from step (b) as a side stream,
(d) subcooling the rest of the gas in said main stream to a still lower temperature than the gas in the side stream,
(e) throttling said subcooled liquid gas from step (d) into a flash drum at a reduced pressure to flash ofi part of the gas as a vapor and still further cool the residual liquid gas,
(f) heat exchanging liquefied gas from said stream of step (c) with the flash vapor from step (e) to further subcool said liquefied side stream gas,
(g) throttling said liquefied subcooled side stream gas of step (f) into the flash drum to rejoin the main stream,
(h) throttling the subcooled main stream liquefied gas into a storage container as liquefied gas at substantially atmospheric pressure,
(i) further throttling the residual liquid gas from step (e) into a second flash drum at a further reduced pressure to produce vapor at a lower pressure than in step (e) and to further subcool the residual liquid (j) heat exchanging liquefied gas from the side stream of step (c) with the flash vapor from the preceding step, and
(k) throttling said liquefied subcooled side stream from the main stream.
References Cited by the Examiner UNITED STATES PATENTS NORMAN YUDKOFF, Primary Examiner. the preceding step into the second flash drum to rejoin 10 V. W. PRETKA, Assistant Examin'er.

Claims (1)

1. THE METHOD OF LIQUEFYING A GAS COMPRISING (A) SUPPLYING THE GAS IN A MAIN FEED STREAM AT HIGH PRESSURE AND ESSENTIALLY AMBIENT TEMPERATURE, (B) REMOVING HEAT FROM THE GAS TO COOL THE GAS TO A TEMPERTURE AT WHICH IT IS IN A LIQUID STATE AT SAID HIGH PRESSURE, (C) WITHDRAWING FROM SAID MAIN FEED STREAM A PORTION OF THE LIQUEFIED GAS FROM STEP (B) AND A SIDE STREAM, (D) SUBCOOLING THE REST OF THE GAS IN SAID MAIN STREAM TO A STILL LOWER TEMPERATURE THAN THE GAS IN THE SIDE STREAM, (E) THROTTLING SAID SUBCOOLING LIQUID GAS FROM STEP (D) INTO A FLASH DRUM AT A REDUCED PRESSURE TO FLASH OFF PART OF THE GAS AS A VAPOR AND STILL FURTHER COOL THE RESIDUAL LIQUID GAS, (F) HEAT EXCHANGING LIQUEFIED GAS FROM SAID SIDE STREAM OF STEP (C) WITH THE FLASH VAPOR FRM STEP (E) TO FURTHER SUBCOOL SAID LIQUEFIED SIDE STEAM GAS, (G) THROTTLING SAID LIQUEFIED SUBCOOLED SIDE STREAM GAS OF STEP (F) INTO THE FLASH DRUM TO REJOIN THE MAIN STREAM, (H) THROTTLING THE SUBCOOLED MAIN STREAM LIQUEFIED GAS INTO A STORAGE CONTAINER AS LIQUEFIED GAS AT SUBSTANTIALLY ATMOSPHERIC PRESSURE, (I) WITHDRAWING VAPOR FROM SAID STORAGE CONTAINER TO MAINTAIN THE PRESSURE IN SAID CONTAINER AT SUBSTANTIALLY ATMOSPHERIC PRESSURE, (J) COMPRESSING SAID VAPOR IN MULTI-STAGE COMPRESSION AND COOLING SAID COMPRESSED VAPOR TO AMBIENT TEMPETATURE, (K) WITHDRAWING PART OF SAID COMPRESSED VAPOR FOR USE AS PRODUCT, AND (L) FURTHER COMPRESSING THE REMAINDER OF SAID COMPRESSED VAPOR TO ABOUT THE INITIAL PRESSURE OF THE MAIN FEED STREAM, AND RETURNING IT TO THE ENTRY POINT OF THE MAIN FEED STREAM.
US382774A 1964-07-15 1964-07-15 Cascade cycle for liquefaction of natural gas Expired - Lifetime US3315477A (en)

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GB1054489D GB1054489A (en) 1964-07-15
US382774A US3315477A (en) 1964-07-15 1964-07-15 Cascade cycle for liquefaction of natural gas
FR23005A FR1441863A (en) 1964-07-15 1965-06-30 Advanced cascade cycle for natural gas liquefaction
NL6509009A NL6509009A (en) 1964-07-15 1965-07-13
OA52113A OA01771A (en) 1964-07-15 1965-07-15 Advanced cascade cycle for natural gas liquefaction.
DEC36403A DE1256666B (en) 1964-07-15 1965-07-15 Process for the liquefaction of gases

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US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
US3408824A (en) * 1967-03-31 1968-11-05 Phillips Petroleum Co Gas liquefication employing thermosyphoned external liquid refrigerant
US3413817A (en) * 1964-04-10 1968-12-03 Lummus Co Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3413816A (en) * 1966-09-07 1968-12-03 Phillips Petroleum Co Liquefaction of natural gas
US3418819A (en) * 1965-06-25 1968-12-31 Air Liquide Liquefaction of natural gas by cascade refrigeration
US3440828A (en) * 1966-02-11 1969-04-29 Air Prod & Chem Liquefaction of natural gas employing cascade refrigeration
US3531943A (en) * 1965-10-23 1970-10-06 Aerojet General Co Cryogenic process for separation of a natural gas with a high nitrogen content
US3548606A (en) * 1968-07-08 1970-12-22 Phillips Petroleum Co Serial incremental refrigerant expansion for gas liquefaction
US3581510A (en) * 1968-07-08 1971-06-01 Phillips Petroleum Co Gas liquefaction by refrigeration with parallel expansion of the refrigerant
US3593535A (en) * 1965-06-29 1971-07-20 Air Prod & Chem Liquefaction of natural gas employing multiple-component refrigerants
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
US4150548A (en) * 1976-10-26 1979-04-24 Kemp Reduction Corporation Pollutant removal from pyrolytic gases by centrifuge and molecular sieves
US4229195A (en) * 1978-05-09 1980-10-21 Linde Aktiengesellschaft Method for liquifying natural gas
US20040182108A1 (en) * 2003-03-18 2004-09-23 Roberts Mark Julian Integrated multiple-loop refrigeration process for gas liquefaction
US20060162378A1 (en) * 2003-03-18 2006-07-27 Roberts Mark J Integrated multiple-loop refrigeration process for gas liquefaction
US20070193303A1 (en) * 2004-06-18 2007-08-23 Exxonmobil Upstream Research Company Scalable capacity liquefied natural gas plant
US20080006053A1 (en) * 2003-09-23 2008-01-10 Linde Ag Natural Gas Liquefaction Process
US20090095018A1 (en) * 2006-05-15 2009-04-16 Hillegonda Bakker Method for liquefying a hydrocarbon stream
US20120047943A1 (en) * 2009-03-31 2012-03-01 Keppel Offshore & Marine Technology Centre Pte Ltd Process for Natural Gas Liquefaction
FR2974167A1 (en) * 2011-04-14 2012-10-19 Air Liquide METHOD AND APPARATUS FOR LIQUEFACTING A GAS
EP3045849A3 (en) * 2015-01-14 2016-07-27 Luciano Ghergo A plant for liquefying methane gas
WO2016164556A1 (en) * 2015-04-07 2016-10-13 Conocophillips Company Quench system for a refrigeration cycle of a liquefied natural gas facility and method of quenching

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US3066492A (en) * 1959-05-15 1962-12-04 Air Liquide Process for the liquefaction of a gas
US3160489A (en) * 1961-02-06 1964-12-08 Fluor Corp Nitrogen removal from natural gas

Cited By (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3413817A (en) * 1964-04-10 1968-12-03 Lummus Co Liquefaction of natural gas at supercritical pressure employing a single refrigeration cycle
US3418819A (en) * 1965-06-25 1968-12-31 Air Liquide Liquefaction of natural gas by cascade refrigeration
US3593535A (en) * 1965-06-29 1971-07-20 Air Prod & Chem Liquefaction of natural gas employing multiple-component refrigerants
US3531943A (en) * 1965-10-23 1970-10-06 Aerojet General Co Cryogenic process for separation of a natural gas with a high nitrogen content
US3440828A (en) * 1966-02-11 1969-04-29 Air Prod & Chem Liquefaction of natural gas employing cascade refrigeration
US3407052A (en) * 1966-08-17 1968-10-22 Conch Int Methane Ltd Natural gas liquefaction with controlled b.t.u. content
US3413816A (en) * 1966-09-07 1968-12-03 Phillips Petroleum Co Liquefaction of natural gas
US3408824A (en) * 1967-03-31 1968-11-05 Phillips Petroleum Co Gas liquefication employing thermosyphoned external liquid refrigerant
US3548606A (en) * 1968-07-08 1970-12-22 Phillips Petroleum Co Serial incremental refrigerant expansion for gas liquefaction
US3581510A (en) * 1968-07-08 1971-06-01 Phillips Petroleum Co Gas liquefaction by refrigeration with parallel expansion of the refrigerant
US4112700A (en) * 1974-08-09 1978-09-12 Linde Aktiengesellschaft Liquefaction of natural gas
US4150548A (en) * 1976-10-26 1979-04-24 Kemp Reduction Corporation Pollutant removal from pyrolytic gases by centrifuge and molecular sieves
US4229195A (en) * 1978-05-09 1980-10-21 Linde Aktiengesellschaft Method for liquifying natural gas
US20060162378A1 (en) * 2003-03-18 2006-07-27 Roberts Mark J Integrated multiple-loop refrigeration process for gas liquefaction
US20040182108A1 (en) * 2003-03-18 2004-09-23 Roberts Mark Julian Integrated multiple-loop refrigeration process for gas liquefaction
US7086251B2 (en) * 2003-03-18 2006-08-08 Air Products And Chemicals, Inc. Integrated multiple-loop refrigeration process for gas liquefaction
US7308805B2 (en) 2003-03-18 2007-12-18 Air Products And Chemicals, Inc. Integrated multiple-loop refrigeration process for gas liquefaction
US20080006053A1 (en) * 2003-09-23 2008-01-10 Linde Ag Natural Gas Liquefaction Process
US20070193303A1 (en) * 2004-06-18 2007-08-23 Exxonmobil Upstream Research Company Scalable capacity liquefied natural gas plant
US20090095018A1 (en) * 2006-05-15 2009-04-16 Hillegonda Bakker Method for liquefying a hydrocarbon stream
US20120047943A1 (en) * 2009-03-31 2012-03-01 Keppel Offshore & Marine Technology Centre Pte Ltd Process for Natural Gas Liquefaction
US9657246B2 (en) * 2009-03-31 2017-05-23 Keppel Offshore & Marine Technology Centre Pte Ltd Process for natural gas liquefaction
FR2974167A1 (en) * 2011-04-14 2012-10-19 Air Liquide METHOD AND APPARATUS FOR LIQUEFACTING A GAS
CN104067078A (en) * 2011-04-14 2014-09-24 乔治洛德方法研究和开发液化空气有限公司 Method and apparatus for liquefying a gas or cooling a feed gas at supercritical pressure
WO2012140369A3 (en) * 2011-04-14 2015-01-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and apparatus for liquefying a gas or cooling a feed gas at supercritical pressure
US9435582B2 (en) 2011-04-14 2016-09-06 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Method and apparatus for liquefying a gas or cooling a feed gas at supercritical pressure
EP3045849A3 (en) * 2015-01-14 2016-07-27 Luciano Ghergo A plant for liquefying methane gas
WO2016164556A1 (en) * 2015-04-07 2016-10-13 Conocophillips Company Quench system for a refrigeration cycle of a liquefied natural gas facility and method of quenching
US11162732B2 (en) 2015-04-07 2021-11-02 Conocophillips Company Quench system for a refrigeration cycle of a liquefied natural gas facility and method of quenching

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OA01771A (en) 1970-01-14
DE1256666B (en) 1967-12-21
GB1054489A (en)
NL6509009A (en) 1966-01-17

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