US20140283548A1 - System and method for liquefying natural gas using single mixed refrigerant as refrigeration medium - Google Patents

System and method for liquefying natural gas using single mixed refrigerant as refrigeration medium Download PDF

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US20140283548A1
US20140283548A1 US14/354,964 US201214354964A US2014283548A1 US 20140283548 A1 US20140283548 A1 US 20140283548A1 US 201214354964 A US201214354964 A US 201214354964A US 2014283548 A1 US2014283548 A1 US 2014283548A1
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gas
heat exchange
stage
heat exchanger
mixed refrigerant
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US14/354,964
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Zhenyong He
Long Yu
Sheng Zhang
Jianqing Fu
Xiaozhe Zhang
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Xindi Energy Engineering Technology Co Ltd
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Xindi Energy Engineering Technology Co Ltd
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Assigned to XINDI ENERGY ENGINEERING TECHNOLOGY CO., LTD. reassignment XINDI ENERGY ENGINEERING TECHNOLOGY CO., LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FU, Jianqing, HE, Zhenyong, YU, LONG, ZHANG, SHENG, ZHANG, Xiaozhe
Publication of US20140283548A1 publication Critical patent/US20140283548A1/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
    • F25J1/0002—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
    • F25J1/0047—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
    • F25J1/0055—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 originating from an incorporated cascade
    • 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
    • F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • 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
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
    • 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

Definitions

  • the present invention relates to the liquefaction of a hydrocarbon-rich gas, and particularly to a system and a method for liquefying natural gas using single mixed refrigerant as refrigeration medium.
  • Natural gas is becoming the best material to replace other fuels because of its environmental friendliness, and its fields of application has gradually expanded to power generation, automotive gas, industrial gas, domestic gas, chemical gas etc.
  • the relatively well-established techniques for liquefying natural gas mainly comprise: cascade refrigeration technology, expansion refrigeration technology and mixed refrigerant refrigeration process.
  • single mixed refrigerant refrigeration process is more preferable for medium-sized LNG plant.
  • the refrigerant compressor system comprises two compressor stages, and liquefaction of natural gas uses one-stage heat exchange.
  • the system comprises a two-stage mixed refrigerant compressor driven by a motor, two coolers, two gas-liquid separators, two liquid pumps, a plate-fin heat exchanger and a LNG storage tank.
  • the mixed refrigerant composed of C1 ⁇ C5 alkanes and N 2 in a reasonable proportion is fed into the inlet of the compressor, compressed to 0.6 ⁇ 1 MPa by first stage compression, entered into the first stage cooler and cooled to 30 ⁇ 40° C., and then introduced into the first stage gas-liquid separator for gas-liquid separation.
  • the gas separated from the top of the first stage gas-liquid separator is fed to the inlet of the second stage compressor, compressed to 1.6 ⁇ 2.5 MPa by the second stage compression; and the liquid obtained at the bottom of the first stage gas-liquid separator is pressurized by the first liquid pump, mixed with the gas from the outlet of the second stage compressor, further introduced to the second stage cooler and cooled to 30 ⁇ 40° C., and then the mixed refrigerant after cooling is fed to the second stage gas-liquid separator for gas-liquid separation.
  • the separated liquid is pressurized by the second liquid pump and mixed with the gas obtained at the top of the second stage gas-liquid separator.
  • the resulting mixture is fed to the plate-fin heat exchanger, precooled to the determined temperature, throttled after exiting from the heat exchanger, and returned to the plate-fin heat exchanger again for providing cold energy for the overall heat exchanging process.
  • the natural gas is supplied to the LNG storage tank after passing through the plate-fin heat exchanger.
  • the liquid obtained at the bottom of the final stage gas-liquid separator needs to be pressurized to overcome the liquid column pressure resulted from the height difference from the liquid outlet of the bottom of the gas-liquid separator to the refrigerant inlet of the top of the plate-fin heat exchanger, which is achieved by providing the final stage liquid pump.
  • the heat exchange process between the refrigerant and natural gas in the plate-fin heat exchanger is the first stage heat exchange, the optimization of the temperature difference for heat exchange between the streams is limited to some extent, and the energy consumption of the apparatus is high. Further, there is no good adaptability to load-variable operation of the apparatus.
  • the present invention relates to a process for liquefying natural gas by using single mixed refrigerant as refrigeration medium.
  • the present invention provides a system for liquefying natural gas using single mixed refrigerant as refrigeration medium, comprising a mixed refrigerant compressor system and a cold box system (heat exchanger),
  • the system for liquefying natural gas using single mixed refrigerant as refrigeration medium in the present invention has a natural gas cycle and a mixed refrigerant refrigeration cycle.
  • the mixed refrigerant refrigeration cycle the mixed refrigerant is compressed by two-stage compression, the stage-by-stage compression is accompanied by stage-by-stage gas-liquid separation, and the liquid phase stream separated from the first stage compression does not participate in the subsequent compression process, which effectively reduces the power consumption of the subsequent gas compression.
  • the gas phase and liquid phase mixed refrigerant streams obtained by compression are fed respectively to different passages of the heat exchanger group for throttling and heat exchanging, the final stage liquid pump is omitted (i.e., only one liquid pump is used) compared to the existing process, and the heat exchange curves of cold fluid and hot fluid in the whole heat exchange process match with each other better by using two-stage heat exchange.
  • the system for liquefying natural gas using single mixed refrigerant as refrigeration medium in the present invention comprises a two-stage mixed refrigerant compressor, coolers, gas-liquid separators, throttling devices, a plate-fin heat exchanger group and a LNG storage tank.
  • the mixed refrigerant compressor system comprises: a two-stage mixed refrigerant compressor, two coolers, two gas-liquid separators, and a liquid pump, and the cold box system comprises a plate-fin heat exchanger group (two-stage heat exchange), a heavy hydrocarbon separator (i.e., a gas-liquid separator) and two throttling devices.
  • the overall heat exchange of the mixed refrigerant and natural gas is conducted in the cold box system.
  • the outlet of the first stage compressor is connected to the first cooler, and the latter is connected to the first gas-liquid separator.
  • the gas phase port of the first gas-liquid separator is connected to the second stage compressor, the liquid phase port at the bottom of the first gas-liquid separator is connected to a liquid pump, and the output line of the liquid pump is converged with the output line of the second stage compressor and then connected to the second cooler.
  • the second cooler is then connected to the second gas-liquid separator.
  • the gas phase port of the top of the second gas-liquid separator is connected to the first heat exchange passage (the gas phase passage) of the heat exchanger group, and the liquid phase port of the bottom of the second gas-liquid separator is connected to the second heat exchange passage of the heat exchanger group.
  • the liquid phase port at the bottom of the second gas-liquid separator is in fluid communication with an end of the first throttling device via the second heat exchange passage of the heat exchanger group, and another end of the first throttling device is connected to the third heat exchange passage of the heat exchanger group.
  • the gas phase port at the top of the second gas-liquid separator is connected to the first heat exchange passage (the gas phase passage) of the heat exchanger group for precooling, and then connected to an end of the second throttling device, and another end of the second throttling device is connected to the third heat exchange passage of the heat exchanger group and then connected to the first stage compressor.
  • a natural gas line is connected to the fourth heat exchange passage of the heat exchanger group and then to the heavy hydrocarbon separator.
  • the gas phase port at the top the heavy hydrocarbon separator is in fluid communication with the LNG storage tank via subsequent stages of the heat exchanger (such as a fifth heat exchange passage).
  • the present invention provides a system for liquefying natural gas using single mixed refrigerant as refrigeration medium, comprising a mixed refrigerant compressor system and a cold box system (heat exchanger),
  • the gas phase port at the top of the heavy hydrocarbon separator is connected to the LNG storage tank after passing through the fifth and sixth heat exchange passages of the plate-fin heat exchanger successively.
  • first compressor stage and “first stage compressor” as described herein can be used interchangeably, and so on.
  • the gas exited from the first compressor stage in the mixed refrigerant compressor system is passed through the first cooler and cooled, and then entered into the first gas-liquid separator for gas-liquid separation; the gas phase after separation is passed through the second compressor stage, and the liquid phase after separation is pressurized by a liquid pump, converged with the hot gas obtained after the second stage compression, cooled by the second cooler, and introduced to the second gas-liquid separator for gas-liquid separation; and the gas phase obtained at the top of the second gas-liquid separator is passed through the first heat exchange passage (i.e.
  • the liquid phase passage) of the downstream heat exchanger and the liquid phase obtained at the bottom of the second gas-liquid separator is passed through the second, liquid phase heat exchange passage of the downstream heat exchanger.
  • the liquid refrigerant from the bottom of the second gas-liquid separator in the mixed refrigerant compressor system is passed through the second, liquid phase heat exchange passage of the heat exchanger group, precooled and then throttled by the first throttling device; the throttled stream is returned to the third heat exchange passage of the heat exchanger group for providing cold energy;
  • the gas refrigerant from the top of the second gas-liquid separator is passed through the first heat exchange passage of the heat exchanger group, precooled and then throttled by the second throttling device; the throttled gas stream is reversely passed through the third heat exchange passage of the heat exchanger group for providing cold energy.
  • the mixed refrigerant exited from the third heat exchange passage is fed to the first stage compressor. Natural gas is firstly passed through the fourth heat exchange passage, cooled to a given temperature and then entered into the heavy hydrocarbon separator for separation. The heavy hydrocarbon component is obtained at the bottom of the heavy hydrocarbon separator. The gas phase component obtained at the top of heavy hydrocarbon separator is further passed through the other stages (such as the fifth heat exchange passage) of the heat exchanger group for heat exchanging, cooled to supercooled state, and thus obtained LNG is delivered to the LNG storage tank for storing.
  • Natural gas is firstly passed through the fourth heat exchange passage, cooled to a given temperature and then entered into the heavy hydrocarbon separator for separation.
  • the heavy hydrocarbon component is obtained at the bottom of the heavy hydrocarbon separator.
  • the gas phase component obtained at the top of heavy hydrocarbon separator is further passed through the other stages (such as the fifth heat exchange passage) of the heat exchanger group for heat exchanging, cooled to supercooled state, and thus obtained LNG is delivered to the LNG storage tank for
  • the method for liquefying natural gas using single mixed refrigerant as refrigeration medium comprises:
  • Purified natural gas as a raw material is firstly passed through the fourth heat exchange passage of a plate-fin heat exchanger group, cooled to ⁇ 30° C. ⁇ 60° C. and then entered into the heavy hydrocarbon separator for separation,
  • the gas phase component separated from the top of heavy hydrocarbon separator is further passed through the other stages (such as the fifth heat exchange passage) of the heat exchanger group for heat exchanging, cooled to ⁇ 130° C. ⁇ 166° C., and thus obtained LNG is delivered to the LNG storage tank for storing;
  • the mixed refrigerant composed of C1 ⁇ C5 alkanes and N 2 (usually four or five or six components selected from C1, C2, C3, C4, C5 alkanes and N 2 , and these components are mixed in any volume ratio or in substantially equal ratio) is fed into the inlet of the compressor, compressed to 0.6 ⁇ 1.8 MPa by first stage compression, entered into the first cooler and cooled to 30 ⁇ 40° C., and then introduced into the first gas-liquid separator for gas-liquid separation;
  • the gas separated from the top of the first gas-liquid separator is fed to the inlet of the second stage compressor, compressed to 1.2 ⁇ 5.4 MPa by the second stage compression;
  • the liquid separated from the liquid phase port at the bottom of the first gas-liquid separator is pressurized by the liquid pump, mixed with the hot gas from the outlet of the second stage compressor, further introduced to the second cooler and cooled to 30 ⁇ 40° C., and then the mixed refrigerant after cooling is fed to the second gas-liquid separator for gas-liquid separation;
  • the gas obtained at the top of the second gas-liquid separator is passed through the first heat exchange passage of the main heat exchanger group for heat exchanging, and the liquid separated from the bottom of the second gas-liquid separator is passed through the second heat exchange passage of the main heat exchanger group for heat exchanging;
  • the liquid separated from the bottom of the second gas-liquid separator is precooled to about ⁇ 30° C. ⁇ 80° C. in the second heat exchange passage of the heat exchanger group, throttled to 0.25 ⁇ 0.75 MPaA by the first throttling device, converged with the mixed refrigerant stream, which is passed through the first heat exchange passage of the main heat exchanger group and returned via the second throttling device (into the third heat exchange passage), and reversely entered into the third heat exchange passage for providing cold energy for the heat exchanger group and then returned to the first compressor stage;
  • the gas stream of the mixed refrigerant separated from the top of the second gas-liquid separator is cooled to ⁇ 135 ° C. ⁇ 169 ° C. in the gas phase passage (the first heat exchange passage) of the heat exchanger group, throttled to 0.25 ⁇ 0.75 MPaA by the second throttling device, and reversely entered into the third heat exchange passage for providing cold energy for the heat exchanger group.
  • the pressure unit “MPaA” as described herein refers to Megapaskal, absolute pressure.
  • connection of one device to another device is achieved through a pipeline.
  • the system of the present invention uses a two-stage mixed refrigerant compressor, compresses and separates the mixed refrigerant stage by stage, which reduces the power consumption for gas compression.
  • the liquid stream obtained at the bottom of the first gas-liquid separator does not participate in the subsequent stream compression process, which to some extent reduces the influence of the fluctuation of the mixed refrigerant ratio on the compressor running conditions, making the system easier to operate.
  • the gas phase and liquid phase mixed refrigerant streams obtained by compression using the mixed refrigerant compressor are fed to different passages of the heat exchanger group, and the final stage liquid pump is omitted (i.e., only one liquid pump is used), which may decrease the energy consumption. Furthermore, the heat exchange curves of cold fluid and hot fluid in the total heat exchange process match with each other better by the aid of using two-stage heat exchange, which can reduce the flow of the mixed refrigerant.
  • the system of the present invention has a good adaptability to load-variable operation of the apparatus, which can effectively avoid abnormal liquid-flooding at the bottom of the cold box, thus ensuring energy consumption under low load conditions, is close to energy consumption at normal operating conditions.
  • FIG. 1 shows a system for liquefying natural gas in the prior art.
  • FIG. 2 shows the system for liquefying natural gas using two-stage mixed refrigerant compressor system in the present invention.
  • the mixed refrigerant compressor system as shown in FIG. 2 comprises a two-stage mixed refrigerant compressor 1 , a first cooler 21 , a second cooler 22 , a first gas-liquid separator 31 , a second gas-liquid separator 32 , a heavy hydrocarbon separator 6 (gas-liquid separator), a liquid pump 4 , a first throttling device 51 , a second throttling device 52 , a plate-fin heat exchanger group 7 (i.e. the main heat exchanger group) and a LNG storage tank 8 .
  • Its mixed refrigerant compressor system comprises the two-stage mixed refrigerant compressor 1 , two cooler 21 and 22 , two gas-liquid separator 31 and 32 , one liquid pump 4 , and the cold box system comprises the plate-fin heat exchanger group 7 (two-stage heat exchange), the heavy hydrocarbon separator 6 (i.e., a gas-liquid separator) and two throttling devices 51 and 52 . Heat exchange of the mixed refrigerant and natural gas is conducted in the cold box system.
  • the outlet of the first stage of the compressor 1 is connected to the first cooler 21 , and the latter is connected to the first gas-liquid separator 31 .
  • the gas phase port of the first gas-liquid separator 31 is connected to the second stage compressor, the liquid phase port at the bottom of the first gas-liquid separator 31 is connected to the liquid pump 4 , and the output line of the liquid pump 4 is converged with the output line of the second stage compressor and then connected to the second cooler 22 .
  • the second cooler 22 is then connected to the second gas-liquid separator 32 .
  • the gas phase port at the top of the second gas-liquid separator 32 is in fluid communication with the first heat exchange passage (the gas phase passage) of the heat exchanger group 7
  • the liquid phase port at the bottom of the second gas-liquid separator 32 is in fluid communication with the second heat exchange passage of the heat exchanger group 7 .
  • the liquid phase port at the bottom of the second gas-liquid separator 32 is passed through the second heat exchange passage of the heat exchanger group 7 and then connected to one end of the first throttling device 51 , and another end of the first throttling device 51 is connected to the third heat exchange passage of the heat exchanger group 7 .
  • the gas phase port at the top of the second gas-liquid separator 32 is connected to the first heat exchange passage (the gas phase passage) of the heat exchanger group 7 for precooling, and then connected to one end of the second throttling device 52 , and another end of the second throttling device 52 is connected to the third heat exchange passage of the heat exchanger group 7 and then connected to the first stage compressor.
  • a natural gas line passes through the fourth heat exchange passage of the heat exchanger group and then is connected to the heavy hydrocarbon separator 6 .
  • the gas phase port at the top of the heavy hydrocarbon separator 6 passes through subsequent stages (such as a fifth heat exchange passage) of the heat exchanger and then is connected to the LNG storage tank 8 .
  • the method for liquefying natural gas using the system as shown in FIG. 2 comprises:
  • Purified natural gas as a raw material is firstly passed through the fourth heat exchange passage of the plate-fin heat exchanger group 7 (two-stage heat exchange), cooled to ⁇ 30° C. ⁇ 60° C. and then entered to the heavy hydrocarbon separator 6 for gas-liquid separation,
  • the gas phase component separated from the top of heavy hydrocarbon separator 6 is further passed through the other stages (such as the fifth heat exchange passage) of the heat exchanger group 7 for heat exchanging, cooled to ⁇ 130° C. ⁇ 166° C., and thus obtained Liquefied natural gas (LNG) is delivered to the LNG storage tank 8 for storing.
  • Liquefied petroleum gas (LPG) is obtained at the bottom of the heavy hydrocarbon separator 6 .
  • the mixed refrigerant composed of C1 ⁇ C5 alkanes and N 2 (usually four or five or six components selected from C1, C2, C3, C4, C5 alkanes and N 2 , and these components are mixed in any volume ratio or in substantially equal ratio) is fed into the inlet of the compressor 1 , compressed to 0.6 ⁇ 1.8 MPa by first stage compression, entered into the first stage cooler 21 and cooled to 30 ⁇ 40° C., and then introduced into the first stage gas-liquid separator 31 for gas-liquid separation;
  • the gas separated from the top of the first stage gas-liquid separator 31 is fed to the inlet of the second stage compressor, compressed to 1.2 ⁇ 5.4 MPa by the second stage compression;
  • the liquid separated from the liquid phase port at the bottom of the first stage gas-liquid separator 31 is pressurized by the liquid pump 4 , mixed with the hot gas from the outlet of the second stage compressor, further introduced to the second cooler 22 and cooled to 30 ⁇ 40° C., and then the mixed refrigerant after cooling is fed to the second stage gas-liquid separator 32 for gas-liquid separation;
  • the gas obtained at the top of the second stage gas-liquid separator 32 is passed through the first heat exchange passage of the main heat exchanger group 7 for heat exchanging, and the liquid separated from the bottom of the second stage gas-liquid separator 32 is passed through the second heat exchange passage of the main heat exchanger group 7 for heat exchanging;
  • the liquid separated from the bottom of the second stage gas-liquid separator 32 is precooled to about ⁇ 30° C. ⁇ 80° C. in the second heat exchange passage of the heat exchanger group, throttled to 0.25 ⁇ 0.75 MPaA by the first throttling device 51 , converged with the mixed refrigerant stream returned from the latter stage of the heat exchanger group 7 (i.e., via the first heat exchange passage and the second throttling device), and reversely entered into the former stage heat exchanger (i.e., the third heat exchange passage) for providing cold energy for the heat exchanger group 7 and then returned to the first compressor stage;
  • the gas stream of the mixed refrigerant separated from the top of the second stage gas-liquid separator 32 is cooled to ⁇ 135° C. ⁇ 169° C. in the gas phase passage (the first heat exchange passage) of the heat exchanger group 7 , throttled to 0.25 ⁇ 0.75 MPaA by the second throttling device 52 , reversely entered into the third heat exchange passage for providing cold energy for the heat exchanger group, and then returned to the first stage compressor.
US14/354,964 2011-11-18 2012-09-13 System and method for liquefying natural gas using single mixed refrigerant as refrigeration medium Abandoned US20140283548A1 (en)

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CN201120459032.XU CN202328997U (zh) 2011-11-18 2011-11-18 采用单一混合工质制冷液化天然气的装置
CN201120459032.X 2011-11-18
PCT/CN2012/081334 WO2013071789A1 (zh) 2011-11-18 2012-09-13 采用单一混合工质制冷液化天然气的装置和方法

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US10267559B2 (en) 2015-04-10 2019-04-23 Chart Energy & Chemicals, Inc. Mixed refrigerant liquefaction system and method
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US10677524B2 (en) 2016-04-11 2020-06-09 Geoff ROWE System and method for liquefying production gas from a gas source
US20200370710A1 (en) * 2018-01-12 2020-11-26 Edward Peterson Thermal Cascade for Cryogenic Storage and Transport of Volatile Gases
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KR102312640B1 (ko) * 2013-03-15 2021-10-13 차트 에너지 앤드 케미칼즈 인코포레이티드 혼합 냉매 시스템 및 방법
CN103712413B (zh) * 2013-12-31 2018-08-17 苏州制氧机有限责任公司 一种天然气液化装置
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