WO2019040521A1 - Récupération de fluide frigorigène et d'azote - Google Patents

Récupération de fluide frigorigène et d'azote Download PDF

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Publication number
WO2019040521A1
WO2019040521A1 PCT/US2018/047371 US2018047371W WO2019040521A1 WO 2019040521 A1 WO2019040521 A1 WO 2019040521A1 US 2018047371 W US2018047371 W US 2018047371W WO 2019040521 A1 WO2019040521 A1 WO 2019040521A1
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WO
WIPO (PCT)
Prior art keywords
nitrogen
vapor
compressor
heat exchanger
rich
Prior art date
Application number
PCT/US2018/047371
Other languages
English (en)
Inventor
Jay C. SCHLEICHER
Christopher Scott YOUNT
Karl Erhard BECK
Original Assignee
GE Oil & Gas, LLC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by GE Oil & Gas, LLC filed Critical GE Oil & Gas, LLC
Priority to CN201880054250.XA priority Critical patent/CN111108335B/zh
Priority to AU2018320785A priority patent/AU2018320785B2/en
Priority to EP18849226.8A priority patent/EP3673219A4/fr
Priority to CA3073283A priority patent/CA3073283C/fr
Priority to KR1020207006807A priority patent/KR102391748B1/ko
Priority to MX2020001893A priority patent/MX2020001893A/es
Publication of WO2019040521A1 publication Critical patent/WO2019040521A1/fr

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Classifications

    • 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.
    • 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.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D17/00—Radial-flow pumps, e.g. centrifugal pumps; Helico-centrifugal pumps
    • F04D17/08—Centrifugal pumps
    • F04D17/10—Centrifugal pumps for compressing or evacuating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/08—Sealings
    • F04D29/10—Shaft sealings
    • F04D29/12—Shaft sealings using sealing-rings
    • F04D29/122—Shaft sealings using sealing-rings especially adapted for elastic fluid pumps
    • F04D29/124—Shaft sealings using sealing-rings especially adapted for elastic fluid pumps with special means for adducting cooling or sealing fluid
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
    • F04D—NON-POSITIVE-DISPLACEMENT PUMPS
    • F04D29/00—Details, component parts, or accessories
    • F04D29/70—Suction grids; Strainers; Dust separation; Cleaning
    • F04D29/701—Suction grids; Strainers; Dust separation; Cleaning especially adapted for elastic fluid pumps
    • F04D29/706—Humidity separation
    • 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"
    • F25J1/0045—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
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • 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
    • F25J1/0082—Methane
    • 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
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0236—Heat exchange integration providing refrigeration for different processes treating not the same feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/066—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of nitrogen
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2345/00—Details for charging or discharging refrigerants; Service stations therefor
    • F25B2345/001—Charging refrigerant to a 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2500/00—Problems to be solved
    • F25B2500/22—Preventing, detecting or repairing leaks of refrigeration fluids
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B45/00—Arrangements for charging or discharging refrigerant
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Definitions

  • Systems and methods are provided for reducing loss of refrigerant and/or nitrogen in liquefaction systems that liquefy gases, e.g., natural gas.
  • Liquefied natural gas is natural gas which has been cooled to a temperature of approximately -162 degrees Celsius ( ⁇ -260 degrees Fahrenheit) with a pressure of up to approximately 25 kPa (4 psig) and has thereby taken on a liquid state.
  • Natural gas is primarily composed of methane, and can include ethane, propane, and heavy hydrocarbon components such as butanes, pentanes, hexanes, benzene, toluene, ethylbenzene, and xylenes. Many natural gas sources are located a significant distance away from the end-consumers.
  • One cost-effective method of transporting NG over long distances is to liquefy the natural gas, converting it to liquefied natural gas (LNG), and to transport it in tanker ships, also known as LNG-tankers. The LNG is transformed back into gaseous natural gas at the destination.
  • a compressor compresses a mixed refrigerant MR to an elevated pressure, forming a pressurized MR.
  • the pressurized MR is delivered to a cold box, which in turn is used to cool an NG feedstock to form LNG.
  • MR and nitrogen can leak from the compressor.
  • the nitrogen can employed as part of a dry gas seal employed for containment of MR within the compressor and mixes with the MR.
  • the leaked MR and nitrogen are captured and delivered to a flare to be burned. Over time this lost, flared MR and nitrogen must be replaced for the liquefaction process to continue, which is costly.
  • a liquefaction system includes a first compressor and a recovery system in fluid communication with the first compressor.
  • the recovery system can include a first heat exchanger configured to receive a first vapor from the first compressor.
  • the first vapor can be, for example, a mixed refrigerant and nitrogen.
  • the first heat exchanger can be configured to convert the first vapor to a mixture of nitrogen rich vapor and a hydrocarbon rich liquid.
  • the first heat exchanger can have at least one cooling element configured to receive a cold fluid that provides refrigeration to the first vapor, and a separator configured to receive the mixture of hydrocarbon rich liquid and nitrogen rich vapor from the first heat exchanger, and to separate the hydrocarbon rich liquid and the nitrogen rich vapor.
  • a method of operating a liquefaction system can include receiving a seal gas including hydrocarbons at a seal assembly of a first compressor.
  • the method can also include receiving a nitrogen vapor a the seal assembly of the first compressor.
  • the method can additionally include receiving, at a first heat exchanger, a first vapor including at least a portion of the seal gas and at least a portion of the nitrogen vapor.
  • the method can also include transferring a cold fluid to a cooling element of the first heat exchanger.
  • the method can further include transferring heat from the first vapor to the cold fluid, thereby creating a mixture of nitrogen rich vapor and a hydrocarbon rich liquid.
  • the method can also include separating the hydrocarbon rich liquid from the nitrogen rich vapor at a separator positioned downstream of the first heat exchanger.
  • FIG. 1 is a diagram of one exemplary embodiment of a liquefaction system
  • FIG. 2 shows a cross-sectional view of a sealing assembly of a compressor
  • FIG. 3 is a schematic of one exemplary embodiment of a mixed refrigerant (MR) recovery system
  • FIG. 4 is a schematic of one exemplary embodiment of a nitrogen recovery system; and [0011] FIG. 5 is a flow diagram illustrating one exemplary embodiment of operating a liquefaction system.
  • compression system involves utilizing a recovery system that allows the refrigerant to be captured and injected directly back into the compressor or into circulation elsewhere within the refrigeration process, thereby eliminating, or mitigating, loss of refrigerant from the refrigeration system.
  • MR mixed refrigerant
  • direct recovery and reintroduction of MR into the compressor, or into circulation within the refrigeration process may not be feasible.
  • the MR that leaks from the compressor does so through the seals of the compressor.
  • Such compressor seal can include dry seals that employ nitrogen gas as a buffer gas and this nitrogen can contaminate the MR.
  • a mixture of MR and nitrogen can leak from the compressor.
  • direct reintroduction of the MR and nitrogen mixture into the compressor can result in performance degradation, since the composition of the MR within the liquefaction system will be altered, becoming enriched with nitrogen.
  • MR and nitrogen recovery systems can be employed to capture leaked mixtures of MR and nitrogen from a compressor of a liquefaction system.
  • the MR and nitrogen recovery systems are each configured to separate the MR from the nitrogen (e.g., by condensing the MR hydrocarbons), allowing recovery of the MR and nitrogen.
  • Recovered MR can safely be reintroduction back into the compressor, and/or into circulation within the refrigeration process.
  • Recovered nitrogen can be used as a component of the buffer gas of the compressor seals, and/or for use elsewhere.
  • FIG. 1 illustrates one embodiment of a new LNG liquefaction system 100.
  • the liquefaction system 100 includes a refrigerant supply system 102 containing a mixed refrigerant MR 102v in a vapor state, a compression system 106, one or more condensers 108, a heat exchanger 112, and a natural gas (NG) supply system 114 containing natural gas (NG) feedstock 114v in a vapor state.
  • the refrigerant supply system 102 is in fluid communication with the compression system 106, and a valve 104 is interposed therebetween for regulating a flow rate of the supply MR 102v to the compression system 106.
  • the condensers 108 are in fluid communication with, and downstream from, the compression system 106.
  • the heat exchanger 112 is in fluid communication with, and downstream from, the condensers 108.
  • An expansion valve 110 is interposed between the condensers 108 and the heat exchanger 112.
  • the heat exchanger 112 is in further configured to receive the NG feedstock 114v from the NG supply system 114.
  • the heat exchanger 112 is also in fluid communication with the valve 104.
  • the valve 104 regulates a flow of mixed refrigerant, supply MR 102v in a vapor state at a first temperature Tl and a first pressure PI from the refrigerant supply system 102 to the compression system 106.
  • the compression system 106 can be, e.g., a multistage
  • compression system including a compressor 105.
  • Embodiments of the compressors 105 can adopt a variety of forms.
  • Examples of the compressor 105 can include a single-casing compressors, multi-stage compressors, and trains of multiple compressors, each with one or more compression stages.
  • the compressors 105 are driven by a mover, which can be, e.g., a gas turbine, a steam turbine, an expander, or an electric motor that receives electric power 107 from an external power source (not shown).
  • the compression system 106 increases the temperature and pressure of the supply MR 102v from the first temperature Tl and the first pressure PI, yielding a high- temperature, high-pressure mixed refrigerant MR 102v' in the vapor state that possesses a second temperature T2 greater than the first temperature Tl and second pressure P2 greater than the first pressure P 1.
  • the high-pressure, high-temperature MR 102v' can subsequently flow to one or more condensers 108 that are downstream of the compression system 106.
  • the condensers 108 can be any device (e.g., condensers, intercoolers, air coolers, etc.) configured to facilitate a phase change of the high-temperature, high-pressure MR 102v' from vapor, or mostly vapor, to a predominantly liquid state, liquid MR 1021, by removing excess heat generated during the compression process.
  • the liquid MR 1021 can possess a third temperature T3 that is less than the first and second temperatures Tl, T2. For clarity of discussion, it is assumed that the pressure of the liquid MR 1021 remains constant at the second pressure P2.
  • FIG. 1 illustrates the condensers 108 as being downstream from the compression system 106.
  • the condensers can be located between stages of the compressors of the compression system 106. Condensers integrated with the compressors of the compression system can be provided in lieu of, or in addition to, condensers downstream from the compression system.
  • the liquid MR 1021 output by the condensers 108 travels through the expansion valve 110.
  • the expansion valve 110 creates a pressure drop that puts at least a portion of the liquid MR 1021 in a low-pressure, low-temperature, liquid state, MR 102 .
  • the low-pressure, low-temperature liquid MR 1021' can possess a third pressure P3 that is lower than the first and second pressures PI, P2. It is assumed for clarity of discussion that the temperature of the low-temperature, low-pressure liquid MR 102 remains constant at T3. However, in alternative embodiments, the temperature of this liquid MR can be less than the second temperature P2.
  • NG natural gas
  • the heat exchanger 112 can be any type of heat exchanger.
  • Examples of the heat exchanger 1 12 can include core plate and fin, etched plate, diffusion bonded, wound coil, shell and tube, plate-and-frame, and the like.
  • the NG feedstock 114v can contain both NG vapor 120 and heavy hydrocarbon components (HHCs) such as butanes, pentanes, hexanes, benzene, toluene, ethylbenzene, and xylenes. It can be desirable to remove HHCs during production of the LNG 124 to prevent them from freezing.
  • the heat exchanger 112 can include a HHC separation system 116 configured to remove HHCs from the NG feedstock 114v. As the NG feedstock 114v is cooled within the heat exchanger 112, HHCs condense at higher temperatures than lighter molecules, e.g., methane.
  • a liquid 118 containing primarily HHCs can be separated from NG feedstock 114v, yielding a purified NG vapor 120 by the HHC separation system 116.
  • the purified NG vapor 120 flows through the heat exchanger 112 and condenses to form the LNG 124.
  • the LNG 124 can be subsequently let down in pressure and stored in a storage vessel (not shown).
  • the liquid 118 can be handled in a variety of ways. In one embodiment, as shown, the liquid 118 exits the heat exchanger 112 and is stored in a HHC storage vessel 122. In alternative embodiments, not shown, the HHC liquid can be put through a multistage distillation process to separate it into its constituent components. The separated constituents can be stored in respective storage vessels.
  • the low-temperature, low-pressure liquid MR 102 ⁇ absorbs heat from the NG feedstock 114v, the purified NG vapor 120, and/or the LNG 124 within the heat exchanger 112. The absorbed heat is sufficient to result in vaporization of the low-temperature, low- pressure liquid MR 102 ⁇ .
  • the MR that leaves the heat exchanger 112 undergoes a phase change to a vapor.
  • This vapor can be recovered in the form of recycled MR 102v" that flows to the valve 104 to the compression system 106.
  • the recycled MR 102v" can be conditioned to the first temperature Tl and the first pressure PI prior to delivery at the valve 104 by one or more conditioning systems (not shown).
  • one or more conditioning systems not shown.
  • the compressors 105 can leak MR (e.g., supply MR 102v and/or high-temperature, high-pressure MR 102v') and nitrogen due to imperfect sealing at various locations.
  • the liquefaction system 100 can also include at least one of an MR recovery system 300 and a nitrogen recovery system 400 in fluid communication with the compressor 105 of the compression system 106.
  • the MR recovery system 300 and the nitrogen recovery system 400 are each configured to separate the leaked MR from the nitrogen (e.g., by condensing the MR hydrocarbons), allowing recovery of the MR and nitrogen.
  • the MR recovery system 300 is further configured to reintroduce recovered MR back into the compressor 105 of compression system 106, and/or into circulation within other portions of the liquefaction system 100 (e.g., between the condensers 108 and the expansion valve 110.
  • the nitrogen recovery system 400 is further configured to reintroduce recovered MR as a component of the buffer gas of the compressor seals, and/or for use elsewhere.
  • FIG. 2 illustrates a cross-sectional view of a compressor 200 including a seal assembly 201 that can be used within a compression system, such as the compression system 106 shown in FIG. 1, to contain MR (e.g., supply MR 102v and or high-temperature, high-pressure MR 102v').
  • the seal assembly 201 is positioned adjacent to an intake port and/or a discharge port of the compressor 200 to prevent leakage of fluids from the compressor.
  • the seal assembly 201 includes a primary seal 202, a secondary seal 204, and a tertiary seal 206 positioned along a length of a shaft 203 of the compressor 200, between a compressor side 209 and a bearing side 211 of the compressor 200, to separate fluids that are within the compressor 200.
  • the primary and secondary seals 202, 204 can be, e.g., dry gas seals, and the tertiary seal 206 can be, e.g., a type of carbon ring seal.
  • the compression side 209 can include a compression chamber (not shown) used to compress MR (e.g., supply MR 102v), and the bearing side 211 can include one or more bearings (not shown) positioned about the shaft 203 of the compressor to allow the shaft 203 to rotate.
  • MR magnetic resonance
  • bearing side 211 can include one or more bearings (not shown) positioned about the shaft 203 of the compressor to allow the shaft 203 to rotate.
  • seal assembly 201 of FIG. 2 is illustrated in the form of a tandem type dry gas sealing system, other sealing systems can be used. Examples can include single dry gas seals, double dry gas seals, multi-arranged dry gas seals, labyrinth type seals, carbon ring type seals, any combination of the aforementioned seals, or any other type of seal known in the art.
  • supply MR 102v, high-temperature, high-pressure MR 102v', and combinations thereof in the form of unfiltered MR 209 is present at a compressor side pressure.
  • the supply MR 102v possesses the first temperature Tl and first pressure PI and the high-temperature, high-pressure MR 102v' possess the second temperature T2 and the second pressure P2.
  • the unfiltered MR 209 can possess a temperature ranging from approximately the first temperature Tl to the second temperature T2 and a pressure ranging from approximately the first pressure PI and the second pressure P2. Solely for clarity, it is assumed in the discussion below that the unfiltered MR 209 possesses the second pressure P2.
  • the unfiltered MR 209 can leak through a sealing element 230 which can be, e.g., a labyrinth seal, and into the seal assembly 201, which can damage the primary, secondary, and tertiary seals 202, 204, 206.
  • a sealing element 230 which can be, e.g., a labyrinth seal
  • filtered, high-pressure MR 208, or another seal gas can be delivered to a region 205 of the seal assembly 201 positioned adjacent the compressor side 209.
  • the filtered, high-pressure MR 208 can pressurize a cavity 207 located adjacent the sealing element 230 to a fourth pressure P4 that is higher than that of the second pressure P2 on the compressor side 209, thereby preventing the unfiltered MR 209 from leaking into the seal assembly 201.
  • a portion of the filtered MR 208 can leak through the primary seal 202 and travel to a primary vent 212.
  • a buffer gas such as, e.g., nitrogen 214 (e.g., nitrogen vapor), can be delivered to a primary buffer region 216 adj acent to the primary vent 212.
  • the nitrogen 214 can be at a fifth pressure P5 that is high pressure than the fourth pressure P4 observed at the primary vent 212.
  • a portion of the nitrogen 214 can leak through a sealing element 232 which can be, e.g., a labyrinth seal that prevents MR leakage, into the primary buffer region 216.
  • the nitrogen 214 that leaks through the sealing element 232 can combine with the MR that leaks through the primary seal 202 (e.g., unfiltered MR 209, filtered MR 208) to create a mixture 218 of MR leakage and the nitrogen 214 at the primary vent 212.
  • Another portion of the nitrogen 214 can leak through the secondary seal 204 and travel to a secondary vent 220.
  • the mixture 218 of MR leakage and nitrogen 214 can be delivered from the primary vent 212 to a flare to be burned.
  • nitrogen 222 can also be injected into a secondary buffer region 224 between the secondary vent 220 and the bearing side 211 of the seal assembly 201. A portion of the nitrogen 222 that is delivered to the secondary buffer region 224 can leak beyond the tertiary seal 206 and travel to the secondary vent 220. Nitrogen 226 from the secondary vent 220 can be captured and reintroduced to the seal assembly 201 as buffer gas.
  • embodiments of the present disclosure illustrate systems and corresponding methods that facilitate recovery of the MR (e.g., unfiltered MR 209, filtered MR 208) that leaks from a compressor of a liquefaction system (e.g., compressor 105 of liquefaction system 100) can be recovered and returned to circulation. This significantly reduces the need to stock, purchase and reintroduce "lost" MR into the liquefaction system 100.
  • MR e.g., unfiltered MR 209, filtered MR 208
  • a compressor of a liquefaction system e.g., compressor 105 of liquefaction system 100
  • FIG. 3 is a schematic diagram illustrating one exemplary embodiment of a new MR recovery system n for recovering all or a portion of either (or both) MR leakage (e.g., unfiltered MR 209, filtered MR 208) and/or nitrogen 214 that leaks from a compressor (e.g., compressor 105 of compression system 106).
  • MR leakage e.g., unfiltered MR 209, filtered MR 208
  • nitrogen 214 e.g., nitrogen 214 that leaks from a compressor
  • the MR recovery system 300 includes a heat exchanger 302 and a two-phase separator 308.
  • the heat exchanger 302 is configured to receive a cold fluid 304 and a nitrogen rich vapor 305 having MR components and nitrogen (e.g., mixture 218) from a compressor of a compression system, such as compressor 105 of the compression system 106 shown in FIG. 1.
  • the heat exchanger 302 can include at least one cooling element configured to receive the cold fluid 304 and provide refrigeration to the nitrogen rich vapor 305.
  • the two-phase separator 308 is configured to separate an input fluid into two or more different phases.
  • the cold fluid 304 can be a liquefied product created by the liquefaction system 100.
  • the cold fluid 304 can be LNG, such as the LNG 124 that exits the heat exchanger 1 12 shown in FIG. 1.
  • the cold fluid 304' that leaves the heat exchanger 302 is delivered to a storage vessel 320, via valve 311, to be stored and/or distributed as desired.
  • the cold fluid 304 can be a refrigerant from another refrigeration system configured for the described purpose. Therefore, the cold fluid 404' that leaves the heat exchanger 302 can continue within a refrigeration cycle to provide refrigeration to the nitrogen rich vapor 305
  • the heat exchanger 302 can take a variety of forms.
  • the heat exchanger 302 can be, e.g., a shell and tube heat exchanger, or it can be a condensing coil heat exchanger.
  • other heat exchangers such as core, core plate-and-fin, etched plate, diffusion bonded, wound coil, shell and tube, plate-and-frame, etc. can be used.
  • valves 309, 311 are positioned on either side of the heat exchanger 302 control a flow rate of the cold fluid 304 through the heat exchanger 302.
  • the nitrogen rich vapor 305 prior to being delivered to the heat exchanger 302, the nitrogen rich vapor 305 is delivered to a nitrogen removal assembly 303 positioned upstream of the heat exchanger 302.
  • the nitrogen rich vapor 305 can be the mixture 218 of leaked MR and nitrogen.
  • the nitrogen removal assembly 303 is configured to removes a portion of the nitrogen from the nitrogen rich vapor 305 and outputs a nitrogen poor vapor 307 that contains less nitrogen than the nitrogen rich vapor 305.
  • the nitrogen removal assembly 303 can be an absorption bed.
  • the nitrogen poor vapor 307 exiting the nitrogen removal assembly 303 is delivered to the heat exchanger 302.
  • the nitrogen poor vapor 307 and the cold fluid 304 travel through the heat exchanger 302, heat is transferred from the nitrogen poor vapor 307 to the cold fluid 304 such that the nitrogen poor vapor 307 begins to cool and condense. While the nitrogen poor vapor 307 is cooled within the heat exchanger 302, hydrocarbon components that make up MR condense at higher temperatures than lighter components such as nitrogen. Therefore, a mixture 306 of a nitrogen rich vapor 310, and a hydrocarbon rich liquid 312 can be formed. The mixture 306 can be cooled sufficiently to achieve the nitrogen rich vapor 310 with high purity due to preferential condensation of hydrocarbon components. In some cases, the mixture 306 is cooled sufficiently to produce the nitrogen rich vapor 310 with approximately 95% purity. As an example temperature of the mixture 306 that exits the heat exchanger 302 can be at a temperature in the range of approximately -51 to -160 degrees Celsius (-60 to -257 degrees Fahrenheit).
  • the mixture 306 exiting the heat exchanger 302 flows to the two-phase separator 308.
  • the two-phase separator 308 is configured to receive the mixture 306 of the nitrogen rich vapor 310 and hydrocarbon rich liquid 312 from the heat exchanger 302 and to separate the nitrogen rich vapor 310 and the hydrocarbon rich liquid 312.
  • the hydrocarbon rich liquid 312 is delivered to a pump 316 that pumps the hydrocarbon rich liquid 312 to a refrigerant supply system, such as refrigerant supply system 102 shown in FIG. 1, and the nitrogen rich vapor 310 is delivered to a flare 322.
  • the hydrocarbon rich liquid 312 and/or the nitrogen rich vapor 330 output from the two-phase separator 308 can be handled differently than discussed above.
  • the hydrocarbon rich liquid can be directly reintroduced to circulation within the liquefaction system (e.g., between the condenser and the expansion valve), or it can be vaporized and reintroduced within the compressor as the filtered MR 208 described above with regard to FIG. 2.
  • the hydrocarbon rich liquid is heated before reintroduction into circulation within the liquefaction system, and/or prior to reintroduction within the compressor of the compression system, to prevent low-temperature embrittlement of components of the liquefaction system and/or the compressor.
  • the hydrocarbon rich liquid can be distilled to separate various hydrocarbon components such as, e.g., methane, ethylene, and propane, and pentanes such that they can be stored separately within the refrigerant supply system.
  • various hydrocarbon components such as, e.g., methane, ethylene, and propane, and pentanes such that they can be stored separately within the refrigerant supply system.
  • the nitrogen rich vapor output from the two-phase separator can be handled differently than flaring.
  • the nitrogen rich vapor can be distilled to further purify the nitrogen.
  • the purified nitrogen vapor can be delivered back to the compressor as a buffer gas of a dry seal of the compressor, it can be stored in a storage vessel, or it can be delivered to other components within a liquefaction system.
  • a distillation system can be used to separate components of the nitrogen poor vapor into nitrogen rich vapor and hydrocarbon rich liquid, rather than the heat exchanger and two-phase separator. In either case, each of the components of the nitrogen poor vapor 307 can be separated, reintroduced to the liquefaction system 100, stored, and/or distributed as desired.
  • FIG. 4 shows one example of a nitrogen recovery system 400 for recovering nitrogen and MR that leaks from a compressor 429 of a compressor system 430.
  • the compressor system 430 can be compression system 106 of liquefaction system 100.
  • Nitrogen buffer gas that leaks from the compressor e.g., compressor 105, compressor 200
  • a buffer gas e.g., nitrogen 214 of seal assembly 201.
  • the nitrogen recovery system 400 includes a heat exchanger 402 and a two-phase separator 408,
  • the heat exchanger 402 is configured to receive a cold fluid 404 and a vapor 405 having MR components and nitrogen from a compressor (e.g., compressor 105, compressor 200) of a compression system, such as the compression system 106 shown in FIG. 1.
  • the heat exchanger 402 can generally be similar to heat exchanger 302. Valves 409, 411 are positioned on either side of the heat exchanger 402 for control a flow rate of the cold fluid 404 through the heat exchanger 402.
  • the two-phase separator 408 can be generally similar to the two-phase separator 308 and is configured to separate an input fluid into two or more different phases.
  • the cold fluid 404 is a liquefied product created by the liquefaction system 100.
  • the cold fluid 404 can be LNG, such as the LNG 124 that exits the heat exchanger 112 shown in FIG. 1.
  • the cold fluid 404 can be, e.g. propane, R-134A, propylene, etc.
  • the cold fluid 404 can be liquid nitrogen or ethylene stored at the liquefaction system 100.
  • the cold fluid 404' that leaves the heat exchanger 402, via valve 411 is delivered to a storage vessel 420 to be stored, and/or distributed as desired.
  • the cold fluid 404 can be a refrigerant from another refrigeration system configured for the described purpose. Therefore, the cold fluid 404' that leaves the heat exchanger 402 can continue within a refrigeration cycle to provide refrigeration to the vapor 405.
  • the heat exchanger 402 As the vapor 405 and the cold fluid 404 travel through the heat exchanger 402, heat is transferred from the vapor 405 to the cold fluid 404 such that the vapor 405 begins to cool and condense. As the vapor 405 is cooled within the heat exchanger 402, hydrocarbon components that make up MR condense at higher temperatures than lighter components such as nitrogen. Therefore, a mixture 406 of a nitrogen rich vapor 410 and a hydrocarbon rich liquid 412 can exit the heat exchanger 402. The mixture 406 can be cooled sufficiently such that the nitrogen rich vapor 410 is of high purity due to preferential condensation of hydrocarbon components. In some cases, the mixture 406 is cooled sufficiently to produce the nitrogen rich vapor 410 with approximately 95% purity. For example, the mixture 406 can exit the heat exchanger 402 at a temperature in a range of approximately -118 to -160 degrees Celsius (-180 to -257 degrees Fahrenheit).
  • the mixture 406 exiting the heat exchanger 402 is flow to the two-phase separator 408 and is separated into the nitrogen rich vapor 410 and the hydrocarbon rich liquid 412.
  • the nitrogen rich vapor 410 is combined with nitrogen vapor 431 from the compressor 429 of the compressor system 430 (e.g., a first compressor), and is delivered to a second compressor 425.
  • the nitrogen vapor 431 can be nitrogen that leaks from a compressor, such as nitrogen 226 described above with regard to FIG. 2.
  • Nitrogen vapor 424 exiting the second compressor 425 is urged into combination with nitrogen vapor 426 from a nitrogen source 428 such that it is delivered back to the compressor 429 of the compressor system 430 to be used as a buffer gas (e.g., nitrogen 214 of seal assembly 201), as described above with regard to FIG. 2.
  • the nitrogen vapor 424 can be heated prior to being combined with the nitrogen vapor 426 from the nitrogen source 428, and/or prior to reintroduction into the compressor system 430, to prevent low temperature embrittlement of components of the compressor system 430.
  • the nitrogen rich vapor 410 is delivered to a nitrogen removal system 417 prior to combination with the nitrogen vapor 431 from the compressor of the compressor system 430 and input to the second compressor 425.
  • the nitrogen removal system 417 is positioned downstream from the two-phase separator 408 and configured to remove at least a portion of nitrogen within the nitrogen rich vapor 410.
  • the nitrogen removal system 417 can be an adsorption bed that removes a portion of adsorbed nitrogen. The adsorbed nitrogen is released as a result of a desorption process, and the released nitrogen is delivered to the second compressor 425, and combined with the nitrogen vapor 426, as described above.
  • the nitrogen vapor 424 output by the second compressor 425 can be handled differently than being combined with the nitrogen vapor 426.
  • the nitrogen vapor can be compressed, condensed, and stored in a storage vessel (not shown).
  • the nitrogen vapor can be stored as a vapor, or delivered to another component of a liquefaction system for use elsewhere.
  • the hydrocarbon rich liquid 412 that exits the two-phase separator 408 is delivered to a pump 416 that pumps the hydrocarbon rich liquid 412 to a flare 422.
  • the hydrocarbon rich liquid 412 can be handled differently.
  • a portion of the hydrocarbon rich liquid 412 can be distilled to remove excess nitrogen. The distillation process separates the hydrocarbon rich liquid 412 into various hydrocarbon components such as methane, ethylene, and propane, and pentanes such that they can be stored separately within a refrigerant supply system.
  • a distillation system can be used to separate components of the vapor 405. Accordingly, each of the components of the vapor can be separated, reintroduced to a liquefaction system, stored, and/or distributed as desired.
  • FIG. 5 is a flow diagram illustrating one exemplary embodiment of a method 500 for operating a liquefaction system.
  • Embodiments of the method include operations 502-512. It can be understood that, in alternative embodiments, the method can include greater or fewer operations and the operations can be performed in an order different than illustrated in FIG. 5.
  • a seal gas is received at a seal assembly of a first compressor (e.g., compressor 105).
  • the seal gas is a mixed refrigerant (MR), such as supply MR 102v, high-temperature, high-pressure MR 102v', and combinations thereof.
  • MR mixed refrigerant
  • a nitrogen vapor is received at the seal assembly of the first compressor.
  • the nitrogen vapor is the nitrogen 214 employed as a buffer gas in the seal assembly 201.
  • a first vapor is received at the first heat exchanger.
  • the first vapor includes at least a portion of the sea gas and at least a portion of the nitrogen vapor.
  • a cold fluid is transmitted to a cooling element of the first heat exchanger.
  • the cold fluid can be cold fluid 304.
  • the cold fluid 304 include a liquefied product created by the liquefaction system 100 (e.g., LNG 124 that exits the heat exchanger 112), a refrigerant from another refrigeration system, different from the liquefaction system 100, and combinations thereof.
  • heat is transferred from the first vapor to the cold fluid, thereby creating a mixture of nitrogen rich vapor and a hydrocarbon rich liquid.
  • the nitrogen rich vapor is possesses approximately 95% purity or greater.
  • the heat transfer can be performed by a heat exchanger (e.g., 302, 402).
  • the hydrocarbon rich liquid is separated from the nitrogen rich vapor at a separator (e.g., 308, 408) positioned downstream of the first heat exchanger.
  • a separator e.g., 308, 408
  • Embodiments of the method 900 can optionally include one or more of the following operations.
  • the method 500 can include receiving the nitrogen rich vapor (e.g., 410) at a second compressor.
  • the second compressor can be second compressor 425 and the nitrogen rich vapor 410 can be received from the heat exchanger 402.
  • the nitrogen rich vapor 410 is compressed by the second compressor 425.
  • At least a portion of the nitrogen rich vapor 410 output by the second compressor 425 is delivered to the seal assembly of the first compressor (e.g., 201).
  • the nitrogen rich vapor 410 is combined with the nitrogen 214 prior to delivery to the seal assembly 201.
  • the method 500 can include receiving a methane-containing vapor at a second heat exchanger and removing heat from the methane-containing vapor within the second heat exchanger to thereby create the cold fluid.
  • the methane-containing vapor can be a natural gas (NG).
  • the second heat exchanger can be heat exchanger 302.
  • the method 500 can include receiving a second vapor at a nitrogen removal assembly positioned upstream of the first heat exchanger.
  • the second vapor includes at least a portion of the seal gas and at least a portion of the nitrogen vapor.
  • the second vapor is nitrogen rich vapor 305 and the nitrogen removal assembly is nitrogen removal assembly 303.
  • the nitrogen removal assembly removes a portion of the nitrogen vapor from the second vapor, thereby generating the first vapor (e.g., nitrogen poor vapor 307).
  • the method 500 can include receiving the nitrogen rich vapor at a nitrogen removal assembly positioned downstream of the separator; and removing a portion of the nitrogen from the nitrogen rich vapor.
  • the separator is two- phase separator 408, the nitrogen removal assembly positioned downstream of the two-phase separator 408 is nitrogen removal system 417, and the nitrogen rich vapor is nitrogen rich vapor 410.
  • the method 500 can include receiving the hydrocarbon rich liquid at a pump (e.g., 316, 416) and pumping the hydrocarbon rich liquid (e.g., 312, 412) to a storage vessel (e.g., 322, 422).
  • MR recovery system 300 and/or the nitrogen recovery system 400, can be implemented in liquefaction system that produces liquefied petroleum gas (LPG), ethane, propane, helium, ethylene etc.
  • LPG liquefied petroleum gas
  • Exemplary technical effects of the methods, systems, and devices described herein include, by way of non-limiting example, the ability to recover, and separate, and store MR components and/or nitrogen that leak from a compressor.
  • Other technical effects of the methods, systems, and devices described herein include the ability to reintroduce the MR components into circulation within a liquefaction system, and/or to reuse recovered nitrogen as a buffer gas within a compressor. Recovering and reusing MR and nitrogen can minimize loss of MR and nitrogen which can lower the total operating cost of a liquefaction system. Additionally, recovering the MR, rather than burning it, can reduce environmental emissions by reducing the amount of MR that is burned.
  • phrases such as "at least one of or "one or more of may occur followed by a conjunctive list of elements or features.
  • the term “and/or” may also occur in a list of two or more elements or features. Unless otherwise implicitly or explicitly contradicted by the context in which it is used, such a phrase is intended to mean any of the listed elements or features individually or any of the recited elements or features in combination with any of the other recited elements or features.
  • Approximating language may be applied to modify any quantitative representation that could permissibly vary without resulting in a change in the basic function to which it is related. Accordingly, a value modified by a term or terms, such as “about” and “substantially,” are not to be limited to the precise value specified. In at least some instances, the approximating language may correspond to the precision of an instrument for measuring the value.
  • range limitations may be combined and/or interchanged, such ranges are identified and include all the sub-ranges contained therein unless context or language indicates otherwise.

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  • Separation By Low-Temperature Treatments (AREA)

Abstract

La présente invention concerne des systèmes, des dispositifs et des procédés de récupération de fluide frigorigène mixte et/ou d'azote dans des systèmes de liquéfaction. Les systèmes, dispositifs et procédés facilitent la récupération de fluide frigorigène mixte (MR) et/ou de vapeur d'azote qui peuvent fuir d'un compresseur, la séparation entre le MR et l'azote, et la réutilisation du MR et/ou de l'azote dans le système de liquéfaction. La récupération et la réutilisation du MR et/ou de l'azote peuvent réduire au minimum la perte de MR et d'azote, ce qui peut abaisser le coût de fonctionnement total d'un système de liquéfaction. De plus, la récupération du MR, plutôt que sa combustion, peut réduire les émissions dans l'environnement par réduction de la quantité de MR qui est brûlée.
PCT/US2018/047371 2017-08-21 2018-08-21 Récupération de fluide frigorigène et d'azote WO2019040521A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
CN201880054250.XA CN111108335B (zh) 2017-08-21 2018-08-21 制冷剂和氮气回收
AU2018320785A AU2018320785B2 (en) 2017-08-21 2018-08-21 Refrigerant and nitrogen recovery
EP18849226.8A EP3673219A4 (fr) 2017-08-21 2018-08-21 Récupération de fluide frigorigène et d'azote
CA3073283A CA3073283C (fr) 2017-08-21 2018-08-21 Recuperation de fluide frigorigene et d'azote
KR1020207006807A KR102391748B1 (ko) 2017-08-21 2018-08-21 냉매 및 질소 회수
MX2020001893A MX2020001893A (es) 2017-08-21 2018-08-21 Recuperacion de refrigerante y nitrogeno.

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US201762548163P 2017-08-21 2017-08-21
US62/548,163 2017-08-21
US16/023,885 2018-06-29
US16/023,885 US20190056175A1 (en) 2017-08-21 2018-06-29 Refrigerant and nitrogen recovery

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EP (1) EP3673219A4 (fr)
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CN (1) CN111108335B (fr)
AU (1) AU2018320785B2 (fr)
CA (1) CA3073283C (fr)
MX (1) MX2020001893A (fr)
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3140938A1 (fr) 2022-10-17 2024-04-19 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de récupération de gaz pour compresseur

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3108167B1 (fr) * 2020-03-11 2022-02-11 Gaztransport Et Technigaz Système de traitement d’un gaz naturel issu d’une cuve d’un ouvrage flottant configuré pour alimenter en gaz naturel en tant que carburant un appareil consommateur de gaz naturel
FR3127555A1 (fr) * 2021-09-30 2023-03-31 Gaztransport Et Technigaz Système de traitement d’un gaz naturel issu d’une cuve d’un ouvrage flottant configuré pour alimenter en gaz naturel en tant que carburant un appareil consommateur de gaz naturel

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6295833B1 (en) * 2000-06-09 2001-10-02 Shawn D. Hoffart Closed loop single mixed refrigerant process
US20080251129A1 (en) * 2007-04-10 2008-10-16 Hoffart Shawn D System and method for collecting and increasing the pressure of seal leak gas
US20160102908A1 (en) * 2014-10-10 2016-04-14 Air Products And Chemicals, Inc. Refrigerant Recovery in Natural Gas Liquefaction Processes
CN205561416U (zh) * 2016-03-23 2016-09-07 山西国新和盛新能源有限公司 一种压缩机凝液回收系统
WO2016174706A1 (fr) * 2015-04-27 2016-11-03 三菱重工コンプレッサ株式会社 Système de récupération de gaz, système de compression et système de cycle frigorifique

Family Cites Families (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2598785A (en) * 1950-01-04 1952-06-03 Phillips Petroleum Co Treatment of gaseous hydrocarbon material streams
CN1032384C (zh) * 1991-10-07 1996-07-24 三电有限公司 带可变容量控制装置的斜盘式压缩机
US5533437A (en) * 1995-01-20 1996-07-09 Air Products And Chemicals, Inc. Recovery of hydrocarbons from polyalkene product purge gas
US6497750B2 (en) * 2001-02-26 2002-12-24 Engelhard Corporation Pressure swing adsorption process
US6425267B1 (en) * 2001-07-27 2002-07-30 Membrane Technology And Research, Inc. Two-step process for nitrogen removal from natural gas
US20030073788A1 (en) * 2001-10-12 2003-04-17 Golden Timothy Christopher Recovery of olefin monomers
US7442231B2 (en) * 2004-08-23 2008-10-28 Syntroleum Corporation Electricity generation system
JP4857766B2 (ja) * 2005-12-28 2012-01-18 株式会社日立プラントテクノロジー 遠心圧縮機およびそれに用いるドライガスシールシステム
KR20080057461A (ko) * 2006-12-20 2008-06-25 신영중공업주식회사 Ｌｎｇ ｂｏｇ 재액화 장치 및 방법
AU2010248092A1 (en) * 2009-05-14 2011-12-01 Exxonmobil Upstream Research Company Nitrogen rejection methods and systems
EP2597406A1 (fr) * 2011-11-25 2013-05-29 Shell Internationale Research Maatschappij B.V. Procédé et appareil pour éliminer l'azote d'une composition d'hydrocarbures cryogénique
US9488187B2 (en) * 2013-02-11 2016-11-08 Dresser-Rand Company Seal assembly for centrifugal compressors
KR101634848B1 (ko) * 2013-10-31 2016-06-29 현대중공업 주식회사 액화가스 처리 시스템
JP6498785B2 (ja) * 2015-02-04 2019-04-10 サムスン ヘビー インダストリーズ カンパニー リミテッド 船舶の蒸発ガス処理装置および処理方法
CN204630249U (zh) * 2015-04-22 2015-09-09 邯郸派瑞节能控制技术有限公司 氮气回收装置
US20170131027A1 (en) * 2015-11-06 2017-05-11 Fluor Technologies Corporation Systems and Methods for LNG Refrigeration and Liquefaction
CN106761958B (zh) * 2017-01-19 2018-03-30 联优机械(常熟)有限公司 透平膨胀机组密封气回收系统

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6295833B1 (en) * 2000-06-09 2001-10-02 Shawn D. Hoffart Closed loop single mixed refrigerant process
US20080251129A1 (en) * 2007-04-10 2008-10-16 Hoffart Shawn D System and method for collecting and increasing the pressure of seal leak gas
US20160102908A1 (en) * 2014-10-10 2016-04-14 Air Products And Chemicals, Inc. Refrigerant Recovery in Natural Gas Liquefaction Processes
WO2016174706A1 (fr) * 2015-04-27 2016-11-03 三菱重工コンプレッサ株式会社 Système de récupération de gaz, système de compression et système de cycle frigorifique
CN205561416U (zh) * 2016-03-23 2016-09-07 山西国新和盛新能源有限公司 一种压缩机凝液回收系统

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3673219A4 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3140938A1 (fr) 2022-10-17 2024-04-19 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de récupération de gaz pour compresseur
WO2024083386A1 (fr) 2022-10-17 2024-04-25 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de récupération de gaz pour compresseur

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AU2018320785A1 (en) 2020-03-19
EP3673219A1 (fr) 2020-07-01
CA3073283A1 (fr) 2019-02-28
CN111108335B (zh) 2022-07-05
AU2018320785B2 (en) 2021-07-15
MX2020001893A (es) 2020-09-07
EP3673219A4 (fr) 2021-10-06
US20190056175A1 (en) 2019-02-21
KR20200033968A (ko) 2020-03-30
CN111108335A (zh) 2020-05-05
US20230168029A1 (en) 2023-06-01
CA3073283C (fr) 2023-01-10

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