US20220307765A1 - Process and plant for producing liquefied natural gas - Google Patents

Process and plant for producing liquefied natural gas Download PDF

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Publication number
US20220307765A1
US20220307765A1 US17/597,181 US202017597181A US2022307765A1 US 20220307765 A1 US20220307765 A1 US 20220307765A1 US 202017597181 A US202017597181 A US 202017597181A US 2022307765 A1 US2022307765 A1 US 2022307765A1
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Prior art keywords
natural gas
countercurrent
mixed refrigerant
absorption
propane
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US17/597,181
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Heinz Bauer
Michael Warter
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Linde GmbH
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Linde GmbH
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Assigned to LINDE GMBH reassignment LINDE GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: Warter, Michael, BAUER, HEINZ
Publication of US20220307765A1 publication Critical patent/US20220307765A1/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—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
    • F25J1/0214—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 dual level refrigeration cascade with at least one 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
    • F25J1/0002—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"
    • F25J1/0042—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 liquid expansion with extraction of work
    • 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
    • F25J1/003—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
    • F25J1/0057—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 after expansion of the liquid refrigerant stream with extraction of work
    • 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
    • F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts 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
    • 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
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
    • F25J1/0241—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling wherein the overhead cooling comprises providing reflux for a fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0258—Construction and layout of liquefaction equipments, e.g. valves, machines vertical layout of the equipments within in the cold box
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0263—Details of the cold heat exchange system using different types of heat exchangers
    • 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.
    • F25J1/0295—Shifting of the compression load between different cooling stages within a refrigerant cycle or within a cascade refrigeration system
    • 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
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/60—Natural gas or synthetic natural gas [SNG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the invention relates to a process and to a plant for producing benzene according to the preambles of the independent claims.
  • natural gas For liquefaction and non-pressurized storage, natural gas must be cooled down to low temperatures of approximately ⁇ 160° C. In this state, the liquefied natural gas can be economically transported by cargo ship or truck, since it has only 1/600th of the volume of the gaseous substance at atmospheric pressure.
  • Natural gas generally contains a mixture of methane and higher hydrocarbons, along with nitrogen, carbon dioxide, and further undesirable constituents. Prior to liquefaction, these components must be partially removed in order to avoid solidification during liquefaction or in order to satisfy customer requirements.
  • the methods used for this purpose such as adsorption, absorption and cryogenic rectification, are generally known.
  • mixed refrigerants consisting of various hydrocarbon components and nitrogen are used in natural gas condensing processes.
  • methods in which two mixed refrigerant circuits are used are known.
  • natural gas for example, which, in addition to methane, contains higher hydrocarbons, such as ethane, propane, butane, etc., but has already been freed of acid gases and dried beforehand, can be subjected to separation of the higher hydrocarbons and subsequent liquefaction.
  • the separation of the higher hydrocarbons is accompanied by a separation of benzene, which is undesirable in the remaining liquefied natural gas.
  • Benzene is used as a key or marker component in corresponding methods and can also be used as an indicator component for the separation.
  • the object of the present invention is, therefore, to improve natural gas liquefaction using two mixed refrigerant circuits.
  • the present invention proposes a process for producing liquefied natural gas and a corresponding plant according to the preambles of the respective independent claims.
  • pressure level and “temperature level” to characterize pressures and temperatures, which is supposed to mean that corresponding pressures and temperatures in a corresponding plant do not have to be used in the form of exact pressure or temperature values. However, such pressures and temperatures typically fall within certain ranges that are, for example, ⁇ 10% about an average. In this case, corresponding pressure levels and temperature levels can be in disjointed ranges or in ranges which overlap one another. In particular, pressure levels, for example, include unavoidable or expected pressure losses. The same applies to temperature levels.
  • the pressure levels indicated here in bar are absolute pressures.
  • expansion machines are referred to here, they are typically understood to mean known turboexpanders, which have radial impellers arranged on a shaft.
  • a corresponding expansion machine can, for example, be mechanically braked or coupled to a device, such as a compressor or a generator.
  • Expansion of a mixed refrigerant within the scope of the present invention is typically carried out using an expansion valve and not using an expansion machine.
  • a “heat exchanger” for use in the context of the present invention can be designed in any manner constituting usual practice in the field. It serves for the indirect transfer of heat between at least two fluid flows guided, for example, in countercurrent, here in particular a comparatively warm natural gas feed flow or a gaseous fraction formed therefrom and one or more cold mixed refrigerant flows.
  • a corresponding heat exchanger can be formed from one or more heat exchanger sections connected in parallel and/or in series, e.g., from one or more wound heat exchangers or corresponding sections. In addition to wound heat exchangers of the type already mentioned, other types of heat exchangers may also be used within the scope of the present invention.
  • the relative spatial terms “upper,” “lower,” “over,” “under,” “above,” “below,” “adjacent to,” “next to,” “vertical,” “horizontal,” etc. here refer to the reciprocal arrangement of components during normal operation.
  • An arrangement of two components “one above the other” is understood here to mean that the upper end of the lower of the two components is located at a lower geodetic height than the lower end of the upper of the two components or at the same geodetic height thereas, and the vertical projections of the two components overlap.
  • the two components are arranged exactly one above the other, that is to say the central axes of the two components run on the same vertical straight line.
  • the axes of the two components need not lie exactly vertically one above the other, they may also be offset from one another.
  • a countercurrent absorber is used.
  • a liquid fraction (“sump liquid”) and a gaseous fraction (“head gas”) can typically be removed from a lower region (“sump”) or from an upper region (“head”).
  • Countercurrent absorbers are also generally known from the field of separation technology. They are used for absorption in the phase countercurrent and are therefore also referred to as countercurrent columns. During absorption in the countercurrent, the releasing gas phase flows upwards through an absorption column.
  • the receiving solution phase flows towards the gas phase.
  • the gas phase is “washed” with the solution phase.
  • Built-in components that ensure a gradual (trays, spray zones, rotating plates, etc.) or continuous (random filling of filling material, packings, etc.) phase contact are typically provided in a corresponding absorption column.
  • a liquid stream, also referred to as “absorption liquid,” is fed into an upper region of a countercurrent absorber, whereby components are washed out of a gaseous stream that is fed in more deeply.
  • feed of natural gas is referred to below, this is to be understood to mean natural gas that has been subjected, in particular, to acid gas removal and optional further conditioning.
  • heavy hydrocarbons such as butanes and/or pentanes, along with hydrocarbons having six or more carbon atoms, may already have been separated from corresponding feed of natural gas.
  • the feed of natural gas is, in particular, anhydrous and has a content of, for example, more than 85% methane and contains, in particular, ethane and propane in the remainder. Nitrogen, helium and other light components may also still be contained.
  • liquefied natural gas is referred to below, it is understood to mean a cryogenic liquid at the atmospheric boiling point of methane or below, especially at ⁇ 160 to ⁇ 164° C., which comprises more than 85% methane, especially more than 90% methane, and the methane content of which is in any case higher than that of the natural gas used.
  • the liquefied natural gas is, in particular, significantly lower in benzene than the feed of natural gas and comprises benzene only at a maximum content given below.
  • a method for producing liquefied natural gas using two mixed refrigerants is disclosed, for example, in U.S. Pat. No. 6,119,479.
  • the higher hydrocarbons contained in the natural gas feed can be separated from it this in a countercurrent absorber as needed.
  • the natural gas feed can be cooled down in a first colling step, depending on the composition, to a temperature in the range of ⁇ 20° C. to ⁇ 70° C. and then fed into the countercurrent absorber.
  • the countercurrent absorber can have a sump heater. Sump liquid separated in the countercurrent absorber contains at least a portion of the higher hydrocarbons from the natural gas feed. The sump liquid can be returned to the countercurrent absorber in part as absorption liquid and, if necessary, also partially supplied to a head gas of the countercurrent absorber after its removal from the countercurrent absorber.
  • the head gas of the countercurrent absorber is depleted of at least a portion of the higher hydrocarbons and is subsequently subjected to a second cooling step, which initiates the liquefaction.
  • Benzene is also used as the key component here, which benzene may be contained in the head gas of the countercurrent absorber, and thus in the natural gas to be liquefied, in particular at less than 1 ppm on a molar basis.
  • the contents of other higher hydrocarbons result therefrom; however, these are typically less critical.
  • Benzene is, in particular, to be regarded as critical in natural gas liquefaction because it can solidify at the low temperatures used.
  • a first mixed refrigerant (warm mixed refrigerant, WMR) is subjected to compression in gaseous form in the order indicated below, condensed by cooling, subcooled, expanded, heated in the first heat exchanger, in particular completely evaporated thereby, and subsequently subjected to compression again.
  • WMR warm mixed refrigerant
  • the first mixed refrigerant can be subcooled in particular in the first heat exchanger, the previous cooling takes place in a further heat exchanger.
  • a second mixed refrigerant (cold mixed refrigerant, CMR) can be subjected to compression in gaseous form, condensed subcooled by cooling, relaxed, heated in the second heat exchanger, in particular completely evaporated thereby, and subsequently subjected to compression again.
  • the subcooling of the second mixed refrigerant can take place in particular in the second heat exchanger, the previous cooling in the first and the second heat exchangers.
  • the first and second heat exchangers are in particular used in a known manner per se as coiled heat exchangers (coil wound heat exchanger, CWHE), wherein the heating of the mixed refrigerant takes place, after its expansion, in particular on the shell side, i.e., in a jacket space surrounding the heat exchanger tubes or, into which the mixed refrigerant is expanded.
  • the media to be cooled down are guided tube-side, i.e., through the correspondingly provided heat exchanger tubes.
  • the heat exchanger tubes are provided in bundles in corresponding heat exchangers, so that the term “tube-side” or “bundle-side” is used here for a corresponding flow guide.
  • Processes for natural gas liquefaction must be able to be flexibly adapted to different plant capacities and operating conditions.
  • the processes as explained, which use two mixed refrigerant circuits, are preferably used, where large ambient temperature fluctuations result in significantly different refrigerant condensation conditions. These can be taken into account more efficiently if a mixture comprising refrigerant components is used instead of a single pure component, such as propane.
  • a compact plant layout (e.g., mandatory for offshore installations) can be achieved by minimizing the number of plant components and by reducing the space between the plants, which can be determined based on safety aspects.
  • the plant components known to be hazardous include pumps for liquid hydrocarbons (risk of leakage and liquid discharge) and all types of devices that contain significant amounts of liquid propane.
  • the present invention solves the problems explained by dispensing with hydrocarbon pumps and largely dispensing with propane as a refrigerant component in corresponding mixed refrigerants.
  • a natural gas feed of the type explained above which contains methane and higher hydrocarbons, including benzene, is cooled down as a whole in a first cooling step using a first (“warm”) mixed refrigerant cooled down to a first temperature level, in particular from ⁇ 20° C. to ⁇ 70° C., and then subjected to countercurrent absorption using an absorption liquid to form a benzene-depleted gas fraction.
  • a natural gas feed of the type explained above which contains methane and higher hydrocarbons, including benzene
  • a first (“warm”) mixed refrigerant cooled down to a first temperature level, in particular from ⁇ 20° C. to ⁇ 70° C.
  • the benzene-depleted gas fraction has, in particular, a content of less than 1 ppm on a molar basis of benzene, wherein the content of benzene in the natural gas feed is significantly higher, for example 5 to 500 ppm.
  • the gas fraction formed is enriched in methane and depleted of the higher hydrocarbons.
  • the gas fraction can also be (essentially) free of hydrocarbons having five and optionally more carbon atoms, so that depletion (essentially) to zero can take place.
  • higher hydrocarbons may also still be contained, and a sump liquid formed during countercurrent absorption can also have certain proportions of methane.
  • the degree of separation or accumulation and depletion achieved in countercurrent absorption depends upon the subsequent use of corresponding fractions and the respective tolerable contents of the specified components.
  • a portion of the gas fraction from countercurrent absorption which is correspondingly depleted (or essentially free) of benzene (and other higher hydrocarbons) is cooled down in a second cooling step using a second (“cold”) mixed refrigerant cooled down to a second temperature level of, in particular, ⁇ 145° C. to ⁇ 165° C. and liquefied to give liquefied natural gas.
  • Liquefied natural gas formed in this way can be subjected to any further processing or conditioning (expansion, subcooling, etc.).
  • the first and second mixed refrigerants are low in propane (having a content of less than 5 mole percent propane) or (essentially) propane-free, and the absorption liquid for the countercurrent absorption is formed from a further portion of the gas fraction from the countercurrent absorption, which (geodetically) is condensed above the countercurrent absorption and returned to the countercurrent absorption without pumping.
  • propane having a content of less than 5 mole percent propane
  • propane-free propane-free
  • the absorption liquid for the countercurrent absorption is formed from a further portion of the gas fraction from the countercurrent absorption, which (geodetically) is condensed above the countercurrent absorption and returned to the countercurrent absorption without pumping.
  • the present invention reduces or eliminates the use of appreciable amounts of propane-containing media.
  • propane is considered a dangerous refrigerant due to the combination of high volatility and high molecular weight.
  • a corresponding refrigerant must necessarily be conveyed by means of machines, with which there is an increased probability of propane leakage. This is no longer the case within the scope of the present invention, which means that it is also suitable and advantageous, in particular, for plant layouts having limited installation space, for example modularized plants and/or floating plants with which the base area is limited and additional installation space requiring safety equipment can only be installed with difficulty.
  • the absorption liquid for countercurrent absorption is formed from the further portion of the gas fraction from the countercurrent absorption, condensed above the countercurrent absorption and returned to the countercurrent absorption without pumping, this (possibly propane-containing) medium does not require the detrimental use of pumps having the problems explained.
  • the invention thus provides a solution in which the use of significant amounts of propane-containing media is essentially dispensed with, either by using refrigerant mixtures that previously contained propane in a low-propane or propane-free manner or by conveying a propane-containing head gas from the countercurrent absorption without pumping.
  • the process proposed in the context of the present invention has the same or a higher thermodynamic efficiency in comparison to known methods.
  • the investment costs can be reduced without increasing the operating costs.
  • a countercurrent absorber is advantageously used in countercurrent absorption, which countercurrent absorber is operated with a head condenser arranged above an absorption region of the countercurrent absorber, wherein the head condenser is used to condense the further portion of the gas fraction.
  • An “absorption region” is to be understood here as meaning the region having built-in components as explained above.
  • the head condenser can be integrated into the countercurrent absorber or at least partially arranged within the countercurrent absorber.
  • An integrated head condenser comprises a heat exchange structure in a common column jacket, in which material exchange structures of the type explained above are also arranged, wherein the heat exchange structure, for example, a cooling coil or the like is separated from a region containing the material exchange structures, in particular by a liquid accumulation bottom or a liquid-tight bottom.
  • the first refrigerant mixture advantageously comprises in total more than 90 mole percent ethane, isobutane and n-butane and in total less than 10, preferably less than 5 mole percent nitrogen, methane, propane and hydrocarbons having five or more carbon atoms.
  • the small amount of propane proves unproblematic.
  • the second mixed refrigerant advantageously has more than 98 mole percent nitrogen, methane and ethane in total and less than 2 mole percent propane and higher hydrocarbons in total.
  • a first heat exchanger is advantageously used in the first cooling step, wherein the first mixed refrigerant in gaseous form is subjected to, in particular, single-stage compression in a first mixed refrigerant circuit, condensed by cooling, subcooled, relaxed, heated in the first heat exchanger, in particular completely evaporated thereby, and subsequently subjected to compression again.
  • the subcooling of the first mixed refrigerant can take place, in particular, in the first heat exchanger, the previous cooling in a further heat exchanger.
  • the compression of the first mixed refrigerant thus takes place, in particular, in a single stage and without intermediate cooling, which would constitute a risk of partial condensation and a need to convey the condensate to the high-pressure side of the compressor. This disadvantage is remedied here.
  • a second heat exchanger is advantageously used in the second cooling step, wherein the second mixed refrigerant in a second mixed refrigerant circuit is subjected to, in particular multi-stage, compression, condensed by cooling, subcooled, relaxed, heated in the second heat exchanger, in particular completely evaporated thereby, and subsequently subjected to compression again.
  • the subcooling of the second mixed refrigerant can take place, in particular, in the second heat exchanger, the previous cooling in the first and the second heat exchangers.
  • first and second heat exchangers may be designed as wound heat exchangers and, in particular, with one or two (serial) bundles in a common jacket in each case.
  • a header for the second mixed refrigerant which receives said refrigerant after it has condensed, can be designed in particular for a pressure that is 2 to 10 bar above a suction pressure of a compressor or of a first of several compressors used in compressing the second mixed refrigerant.
  • a series of three compressors can be used for compressing the first and the second mixed refrigerant, a first of which compresses the first mixed refrigerant and the further two compress the second mixed refrigerant.
  • Such compressors can be designed for (almost) identical shaft powers, i.e., 331 ⁇ 3 ⁇ 3% of the total power consumption.
  • the second mixed refrigerant is advantageously used after heating and evaporation in the second heat exchanger and before compression during the condensation of the further portion of the gas fraction from the countercurrent absorption and is further heated thereby. In this way, a particularly advantageous utilization of this second mixed refrigerant results.
  • the first (but not the second) heat exchanger is advantageously used for cooling the first mixed refrigerant and/or the second (and additionally the first) heat exchanger is used for cooling the second mixed refrigerant. Further cooling after compression or after compression steps can take place in a known manner, for example using air or water coolers.
  • a rising gas phase is formed in countercurrent absorption at least in part by feeding in further natural gas feed, which was subjected to the first cooling step.
  • the rising gas phase can also be provided at least in part by evaporation of a portion of a sump liquid formed in the countercurrent absorption.
  • working liquid expanders can be used instead of expansion valves. This reduces energy consumption.
  • the present invention is suitable for typical natural gases so that the natural gas feed can contain, in particular, at least 80% methane and, in the methane-free remainder, at least 50% ethane and propane.
  • the liquefied natural gas advantageously contains at least 90% methane, wherein a methane content in the liquefied natural gas is higher than in the natural gas feed.
  • the present invention further extends to a plant for producing benzene, reference being made to the corresponding independent claim with regard to its specific features.
  • a plant for producing benzene reference being made to the corresponding independent claim with regard to its specific features.
  • such an arrangement is designed for carrying out a process as previously explained in different embodiments.
  • FIG. 1 illustrates a plant according to an embodiment of the present invention in the form of a simplified process flow diagram.
  • FIG. 2 illustrates a plant according to a further embodiment of the invention in the form of a simplified process flow diagram.
  • FIG. 1 a plant according to a particularly preferred embodiment of the present invention is shown in the form of a greatly simplified schematic process flow diagram and is designated as a whole by 100.
  • the plant 100 illustrated in FIG. 1 is supplied with natural gas feed NG, which is first divided into two partial streams.
  • a first partial stream is cooled down in a first heat exchanger E 1 , which can in particular be designed as a wound heat exchanger, in a first cooling step to a first temperature level of, for example, ⁇ 20° C. to ⁇ 70° C. and then fed approximately centrally into a countercurrent absorber T 1 .
  • the second partial flow of the natural gas feed NG which is expanded via a valve V 6 , is fed into a lower region of the countercurrent absorber T 1 , where it rises essentially in gaseous form.
  • Gas is withdrawn from an upper region of the countercurrent absorber T 1 and is cooled down in a head condenser E 2 , which can be designed, for example, as a plate heat exchanger, and fed into a head space of the countercurrent absorber T 1 .
  • Liquid precipitating here is returned as a return flow to the countercurrent absorber T 1 and washes out heavier components from the natural gas feed, which pass into a sump liquid of the countercurrent absorber T 1 .
  • the sump liquid of the countercurrent absorber T 1 can be expanded via a valve V 5 and discharged from the plant 100 as a heavy fraction HHC (heavy hydrocarbon).
  • Head gas of the countercurrent absorber T 1 i.e., a methane-rich gas fraction
  • a second heat exchanger E 3 which can also be designed as a wound heat exchanger, and, after expansion, discharged via a valve V 4 as liquefied natural gas LNG from the plant 100 .
  • the plant 100 comprises two mixed refrigerant circuits.
  • a first (“warm”) mixed refrigerant WMR is subjected to single-stage compression in gaseous form in a compressor C 1 and subsequently cooled down in an air cooler and/or water cooler E 4 and thereby condensed.
  • Condensate can be obtained in a separation vessel D 1 .
  • This is first further cooled down in the first heat exchanger E 1 on the bundle side, then expanded via a valve V 1 and fed into the jacket space of the first heat exchanger E 1 , where it is heated, completely evaporated and subsequently subjected to compression again.
  • the compression of the first mixed refrigerant takes place here, in particular, in the single-stage compressor C 1 without intermediate cooling, which would constitute a risk of partial condensation and a need to convey the condensate to the high-pressure side of the compressor. This disadvantage is remedied here.
  • a second mixed refrigerant CMR is subjected to a gradual compression in compressors LP C 2 and HP C 2 in gaseous form and subsequently cooled down in each case, for example in air coolers and/or water coolers E 5 and E 6 . Further cooling takes place on the bundle side in the first heat exchanger E 1 and then in the second heat exchanger E 3 .
  • feeding into a buffer vessel D 2 takes place. Condensate withdrawn therefrom is expanded via a valve V 3 and fed jacket-side into the second heat exchanger E 2 , where it is heated and completely evaporated.
  • the gaseous second mixed refrigerant CMR is used as refrigerant in the aforementioned head condenser E 2 before it is again subjected to compression.
  • a return pump can be dispensed with by installing the head condenser E 2 , which is operated using tactile heat of the second mixed refrigerant, which leaves the second heat exchanger E 3 as a vapor above the countercurrent absorber T 1 .
  • the return flow formed from the gas from the countercurrent absorber T 1 is returned to the countercurrent absorber T 1 purely by the effect of gravity.
  • FIG. 2 a plant according to a further embodiment of the present invention is shown in the form of a greatly simplified schematic process flow diagram and is designated as a whole by 200.
  • a first difference from the embodiment of the plant 100 according to FIG. 1 here is that the countercurrent absorber T 1 is not supplied with a partial flow of the natural gas feed, but instead a reboiler E 7 is provided which evaporates a portion of the sump liquid of the countercurrent absorber T 1 and thus forms a portion of the rising gas phase in the countercurrent absorber T 1 .
  • a further difference from the embodiment of the plant 100 according to FIG. 1 is, furthermore, that the head condenser E 3 in the form of corresponding heat exchanger structures is displaced into the head space of the countercurrent absorber T 1 , whereby corresponding installation space is potentially saved.
  • valve V 1 can also be replaced by a expansion machine X 3 (not shown).

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