EP0975923B1 - Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes - Google Patents

Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes Download PDF

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Publication number
EP0975923B1
EP0975923B1 EP98924120A EP98924120A EP0975923B1 EP 0975923 B1 EP0975923 B1 EP 0975923B1 EP 98924120 A EP98924120 A EP 98924120A EP 98924120 A EP98924120 A EP 98924120A EP 0975923 B1 EP0975923 B1 EP 0975923B1
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EP
European Patent Office
Prior art keywords
refrigerant
mixed
hydrocarbon
refrigerant mixture
liquefying
Prior art date
Legal status (The legal status 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 status listed.)
Expired - Lifetime
Application number
EP98924120A
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German (de)
English (en)
French (fr)
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EP0975923A1 (de
Inventor
Rudolf Stockmann
Wolfgang FÖRG
Manfred BÖLT
Manfred Steinbauer
Christian Pfeiffer
Pentti Paurola
Arne Olav Fredheim
Oystein Sorensen
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Linde GmbH
Equinor ASA
Original Assignee
Linde GmbH
Den Norske Stats Oljeselskap AS
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Publication of EP0975923A1 publication Critical patent/EP0975923A1/de
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of 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
    • 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
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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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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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
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    • 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
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    • 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
    • F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
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    • 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
    • F25J1/0248—Stopping of the process, e.g. defrosting or deriming, maintenance; Back-up mode or systems
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    • 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
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    • 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
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    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
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    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/912—External refrigeration system
    • Y10S62/913—Liquified gas

Definitions

  • the invention relates to a process for liquefying a hydrocarbon-rich Electricity, especially a natural gas flow, through indirect heat exchange with the refrigerants of a refrigerant mixture circuit cascade, the Refrigerant mixture circuit cascade from at least 3 different ones Refrigerant mixture circuits having refrigerant compositions, the first of the 3 pre-cooling refrigerant mixture circuits, the second Refrigerant mixture circuit of the liquefaction and the third Refrigerant mixture circuit of the subcooling of the liquefied Hydrocarbon-rich electricity is used.
  • liquefaction processes are known in which the for Liquefaction does not require refrigeration energy using a refrigerant circuit cascade however, a mixed refrigerant cycle cascade is provided; see e.g. B. LINDE reports from technology and science, issue 75/1997, pages 3 - 8.
  • the ones in it The refrigerant circuit cascade described consists of a propane or propylene, an ethane or ethylene and a methane refrigeration cycle.
  • This Refrigerant circuit cascade can be viewed as energetically optimized, is however comparatively complicated due to the 9 compressor stages.
  • DE-A 35 21 060 A generic method is known from DE-A 35 21 060. This However, according to this knowledge, the procedure has never been implemented Service. The reason for this is likely to be that in DE-A 35 21 060 described method is comparatively complex in terms of plant technology and moreover has a comparatively high need for investment.
  • the object of the present invention is to provide a generic method for Liquefying a hydrocarbon-rich stream, in particular a natural gas stream, to specify a one compared to the named liquefaction processes has reduced specific energy consumption and the realization of a smaller antagen size and associated lower investment costs allows.
  • Such cold suction compressors have the advantage that the suction The medium should not be warmed up to ambient temperature before being drawn in must, which saves heating surface and thus the heat exchanger is dimensioned smaller and can be made cheaper.
  • the cold suction compression thus also enables the realization of a liquefaction process that a reduced specific compared to the known liquefaction processes Has energy consumption.
  • the first of the three coolant mixture circuits the refrigerant mixture circuit cascade - the so-called P recooling R efrigerant C ycle (PRC) -. Serves for cooling and partial or complete condensation of the required for the liquefaction and subcooling refrigerant mixtures as well as the pre-cooling of the hydrocarbon-rich stream.
  • the second refrigerant mixture circuit - the so-called L iquefaction R efrigerant C ycle (LRC) -. Is the partial or total condensation of the need for sub-cooling the refrigerant mixture and the condensation of the hydrocarbon-rich stream.
  • the third refrigerant mixture circuit - the so-called S ubcooling R efrigerant C ycle (SRC) -. Serves the necessary subcooling of the liquefied hydrocarbon-rich stream and the sub-cooling of the SRC-refrigerant mixture circuit itself.
  • SRC S ubcooling R efrigerant C ycle
  • the first of the three refrigerant mixture circuits as a refrigerant Ethylene or ethane
  • propane and butane are used.
  • This PRC mixed refrigerant circuit serves the provision of refrigerant in one Temperature range from ambient temperature to between approx. -35 and approx. -55 ° C.
  • the second of the three refrigerant mixture circuits as a refrigerant Methane
  • ethylene or ethane and propane are used.
  • the third of the three Refrigerant mixture circuits are preferably a mixture of refrigerants Nitrogen, methane and ethylene or ethane are used.
  • the third or SRC refrigerant mixture circuit is used for Provision of cold to between approx. -85 and approx. -160 ° C.
  • the procedure according to the invention leads to a reduction in the specific Energy consumption and investment costs because the three refrigerant mixture circuits optimally to the enthalpy-temperature curves of the hydrocarbon to be liquefied Current and the refrigerant mixtures are adapted or are adapted can. This compares to a dual flow refrigeration process
  • the more efficient procedure can either be the required liquefaction plant reduce and thus reduce the cost of the system or the capacity of the liquefying hydrocarbon-rich electricity can with constant Plant size can be enlarged.
  • the refrigerant required for the liquefaction of the hydrocarbon-rich stream is provided by at least three refrigerant mixture circuits.
  • a "P", "L” or “S” for P RC, L RC or S RC refrigerant mixture circuit is placed in front of the reference numerals of the individual refrigerant mixture circuits in FIGS. 1 to 5.
  • an optionally pretreated natural gas stream which has a temperature between 10 and 40 ° C. and a pressure between 30 and 70 bar, is fed via line 1 to a first heat exchanger E1.
  • the natural gas flow is pre-cooled to a temperature between -35 and -55 ° C. against the refrigerant mixture of the first or PRC-refrigerant mixture circuit in line P14, which has been expanded in an expansion valve P13.
  • the refrigerant mixture of the third or SRC refrigerant mixture circuit is the Heat exchanger E1 via line S5 with a temperature between 10 and 40 ° C and a pressure between 30 and 60 bar and counter in the heat exchanger E1 the previously mentioned refrigerant mixture in line P14 cooled and partially condensed, the refrigerant mixture in line P 14 at a pressure between 2 and 6 bar evaporated.
  • the refrigerant mixture of the SRC refrigerant mixture circuit leaves the heat exchanger E1 via line S6 a temperature between -35 and -55 ° C.
  • the refrigerant mixture of the second or LRC refrigerant mixture circuit is the Heat exchanger E1 via line L5 with a temperature between 10 and 40 ° C and fed a pressure between 15 and 25 bar and in the heat exchanger E1 the refrigerant mixture of the PRC refrigerant mixing circuit in line P14 condensed.
  • the refrigerant mixture in the LRC-refrigerant mixture circuit is switched off the heat exchanger E1 with a temperature between -35 and -55 ° C.
  • the evaporated and overheated refrigerant mixture of the PRC refrigerant mixture circuit in line P14 contains, according to an advantageous Embodiment of the method according to the invention, essentially 0 to 40 mol% Ethylene or ethane, 30 to 40 mol% propane and 20 to 30 mol% butane.
  • This Refrigerant mixture is the separator P1 with a pressure of 2 to 6 bar fed.
  • the gaseous gas drawn off at the top of the separator P1 via line P2 Refrigerant mixture is in the compressor P3 to a pressure between 6 and 10 bar compacted. This is followed, preferably against sea water, air or against an appropriate cooling medium, cooling the compressed Mixture in the cooler P4 to a temperature between 10 and 40 ° C.
  • the refrigerant mixture is then passed to another via line P5 Separator P6 fed.
  • the gaseous product at the top of the separator P6 Fraction of the refrigerant mixture is fed to the second compressor stage P8 and compressed to a pressure between 10 and 20 bar.
  • the liquid fraction from the separator P6 is by means of the pump P7, preferably a centrifugal pump, pumped to a pressure between 10 and 20 bar and then with the in the Compressor P8 merged compressed refrigerant mixture flow.
  • the compression of the refrigerant mixture of the first or PRC refrigerant mixture circuit preferably takes place in a two-stage, housed centrifugal compression device that both the cooler P4 and contains the separator P6.
  • Centrifugal compression device instead of Centrifugal compression device also an axial compression device be provided.
  • the compressed refrigerant mixture of the PRC-refrigerant mixture circuit is in the cooler P9, preferably against sea water or an equivalent Cooling medium, condensed and slightly up to a temperature range of 10 to 40 ° C supercooled.
  • the mixture of refrigerants is then added to line P10 Heat exchanger E1 supplied and in this to a temperature between -35 and -50 ° C against itself supercooled.
  • the evaporation temperature which after the Joule-Thomson expansion in Pressure relief valve P13 - or alternatively in a pressure relief turbine - achieved depends essentially on the degree of hypothermia before Expansion as well as the evaporation pressure in the temperature range between -38 and from -53 ° C.
  • the second or LRC refrigerant mixture circuit serves the liquefaction of the pre-cooled natural gas stream in line 2.
  • the refrigerant mixture of this LRC-refrigerant mixture circuit essentially consists from a mixture of 5 to 15 mol% methane, 0 to 80 mol% ethylene or ethane and 10 to 20 mole percent propane.
  • the pre-cooled natural gas flow is the heat exchanger E2 supplied via line 2, in this up to a temperature between -80 and -100 ° C cooled and then via line 3 from the heat exchanger E2 deducted.
  • the refrigerant mixture of the third or SRC refrigerant mixture circuit is the Heat exchanger E2 via line S6 with a temperature between -35 and -50 ° C supplied and against the refrigerant of the LRC-refrigerant mixture circuit in the Line L10 condensed.
  • the refrigerant mixture in line L10 evaporates a pressure level between 1.5 and 6 bar.
  • the cooled refrigerant mixture of the SRC refrigerant mixture circuit is at a temperature between -80 and -100 ° C withdrawn from the heat exchanger E2 via line S7.
  • the evaporated and overheated refrigerant mixture of the LRC-refrigerant mixture circuit in line L10 the separator L1 is connected with a Pressure supplied between 1.5 and 6 bar.
  • the one at the head of the separator L1 gaseous refrigerant mixture is fed to the compressor L3 via line L2 and compressed to a pressure between 10 and 20 bar.
  • the compressor is E3 preferably designed as a single-case axial or centrifugal compressor.
  • Such cold suction compressors have the advantage that the suction Medium does not have to be warmed up to ambient temperature before being drawn in, which saves heating area and thus reduces the size of the heat exchanger and can be made cheaper.
  • the compressed refrigerant mixture of the LRC-refrigerant mixture circuit is in the cooler L4, preferably against sea water or an equivalent Cooling medium, cooled down to a temperature between 10 and 40 ° C. That from the Cooler L4, drawn off via line L5, as previously mentioned, liquefied in the heat exchanger E1, via line L6 to the heat exchanger E2 fed and in this up to a temperature between -80 and -100 ° C against itself even hypothermic.
  • the evaporation temperature of the refrigerant mixture after the Joule-Thomson relaxation in the relaxation valve L9 - or alternatively in one Expansion turbine - is between -82 and -112 ° C.
  • the third or SRC refrigerant mixture circuit serves to subcool the liquefied hydrocarbon-rich electricity or natural gas electricity. This Hypothermia is sensible or necessary so that it does not exceed the required amount of the flash gas after the expansion of the liquefied hydrocarbon-rich Electricity occurs in a downstream nitrogen removal unit.
  • the refrigerant mixture of the third or SRC refrigerant mixture circuit consists of according to a further advantageous embodiment of the method according to the invention, essentially from a mixture of 0 to 10 mol% nitrogen, 40 to 65 mol% Methane and 0 to 40 mole% ethylene or 0 to 30 mole% ethane.
  • the liquefied hydrocarbon rich supplied via line 3 to the heat exchanger E3 Current is in the heat exchanger E3 up to a temperature of -150 to -160 ° C supercooled. After this supercooling, the hydrocarbon-rich or Natural gas electricity withdrawn via line 4 from the heat exchanger E3 and in essentially to atmospheric pressure using a Joule-Thomson relaxation in the relief valve 5 - or alternatively in a relaxation turbine - relaxed.
  • the refrigerant mixture supplied to the heat exchanger E3 via line S9 third or SRC refrigerant mixture circuit is in the heat exchanger E3 undercooled and then in the expansion valve S10 also a Joule-Thomson expansion subjected.
  • the expansion valve S10 can again an expansion turbine can be provided.
  • the relaxation in Relief valve S10 takes place at a pressure level between 2 and 6 bar.
  • the Evaporation of the refrigerant mixture in the heat exchanger E3 serves both Hypothermia of the already liquefied hydrocarbon-rich stream as well the self-subcooling of the refrigerant mixture of the SRC-refrigerant mixture circuit that has not yet relaxed.
  • the evaporated and overheated refrigerant mixture of the SRC refrigerant mixture circuit is fed to a separator S1 via line S11.
  • the gaseous refrigerant mixture obtained at the top of the separator S1 is over Line S2 fed to a compressor S3.
  • the refrigerant mixture emerging from the compressor S3 is then in the Cooler S4, preferably against sea water or an appropriate cooling medium, cooled.
  • each of the three refrigerant mixing circuits has Design of the method according to the invention, downstream of the respective Expansion valves P13, L9 and S10 a separator / storage tanks P11, L7 or S8.
  • these separators / storage tanks can also be used on everyone other suitable location of the refrigerant mixture circuits can be provided.
  • Control valves P15, L11 and S12 are provided in lines P16, L12 and S13. These control valves are used to control the fluid level within the Regulate separator / storage tank P 11, L7 or S8.
  • the control valves P15, L11 and S12 closed so that the separator / storage tank P11, L7 and S8 with the Refrigerant mixture of the respective refrigerant mixture circuit are filled; to it makes sense that the separators / storage tanks P11, L7 and S8 control valves - which are not shown in Figures 1 to 5 - are provided.
  • This will store the refrigerant mixture at the coldest point of the enables the respective refrigerant mixture circuit, whereby the start-up procedure at the restart is accelerated.
  • the separators / storage tanks P11, L7 and S8 should preferably be dimensioned so that they cover the entire Can store the mixed refrigerant quantity of a mixed refrigerant circuit.
  • the method according to the invention is further developed that the Compressors P8, P3, L3 and S3 driven by only one gas turbine drive G. become; represented by the dash-dotted line (Note: Even if the Figures 3 to 5 the names of the compressors or compressor stages compared Figures 1 and 2 have been changed, it should be clarified by the dash-dotted line, that even in these embodiments of the method according to the invention only one Compressor drive is required.).
  • FIG. 2 shows a liquefaction process for natural gas, which is essentially identical to that of FIG. 1. However, the first, second and third or PRC, LRC and SRC refrigerant mixture circuits are only partially shown for the sake of clarity.
  • the hydrocarbon-rich stream or natural gas stream to be liquefied becomes the Heat exchanger E1 supplied via line 1. On an appropriately chosen one Temperature level, it is withdrawn from the heat exchanger E1 via line 1 'and a separation column T1, which has a reboiler R1. This separation column T1 is used to separate heavy hydrocarbons at the bottom of the Separation column T1 are withdrawn via line 8.
  • the heavy hydrocarbons obtained at the top of the separation column T1 depleted natural gas is in turn the heat exchanger E1 via line 2 ' fed. In this it is cooled further and over as a partially condensed stream Line 2 "to a separator D. The accumulating in the bottom of the separator D. Liquid fraction is returned to the head by means of pump P1 via line 2 "' given the separation column T1. The one at the head of the separator Hydrocarbon-rich fraction is the heat exchanger E2 via line 2 fed and liquefied in this. The liquefied passes through line 3 Hydrocarbon-rich electricity then in the heat exchanger E3, in which he is hypothermic.
  • the supercooled liquefied hydrocarbon-rich stream is then over Line 4 of the separation column T2, wherein it is used for the purpose of heating the Reboilers R2 before relaxing in the relaxation valve 5 through the column sump to be led.
  • the separation column T2 is used to separate nitrogen and methane, one of which is these two components rich current at the top of the separation column T2 via line 6 is subtracted.
  • This nitrogen and methane-rich withdrawn via line 6 Electricity - the so-called tail gas - is in the heat exchanger E4 against a partial flow of the am Head of the separator D withdrawn hydrocarbon-rich stream that the Heat exchanger E4 is fed via line 9, heated.
  • the liquefied it Hydrocarbon-rich partial flow is then via line 10 and Expansion valve 11 also on the separation column T2 - either on the same Soil or any soil below the hydrocarbon-rich feed point Current in line 4 - given.
  • Figure 3 shows a further advantageous embodiment of the method according to the invention.
  • the first or PRC refrigerant mixture circuit is modified.
  • the LRC and SRC refrigerant mixture circuits are identical to those as shown in Figure 1.
  • the compressed (P3) refrigerant mixture is brought to a temperature in the cooler P4 cooled between 10 and 40 ° C and liquefied. Then it becomes the Heat exchanger E1 supplied via line P10 and supercooled in it. A partial flow of the supercooled refrigerant mixture is in the expansion valve P13 - or alternatively in a relaxation turbine - relaxed and in the heat exchanger E1 evaporated again. This partial refrigerant mixture stream is then piped P14 fed to the separator P1 at a pressure of 2 to 6 bar. That on the head of the Separator P1 drawn off via line P2 gaseous refrigerant mixture is in compresses the compressor P3 to a pressure between 6 and 10 bar.
  • a second partial flow of the liquefied and supercooled refrigerant mixture is opened withdrawn from a higher temperature level from the heat exchanger E1 and in Pressure relief valve P17 - or alternatively in a pressure relief turbine - relaxed.
  • Pressure relief valve P17 or alternatively in a pressure relief turbine - relaxed.
  • this partial flow of The refrigerant mixture also evaporates in the heat exchanger E1 and via line P18 fed to the separator P6. That at the head of the separator P6 via line P19 withdrawn gaseous refrigerant mixture is also the compressor P3 on one Intermediate pressure stage supplied.
  • Partial refrigerant mixture After mixing and compressing the two described Partial refrigerant mixture flows to approx. 15 to 20 bar in the compressor P3, preferably against sea water, against air or against a corresponding one Cooling medium, cooling and liquefying the compressed refrigerant mixture in the Cooler P4 at a temperature between 10 and 40 ° C.
  • the enthalpy-temperature diagram of the one to be evaporated and heated The mixed refrigerant flow of the PRC mixed refrigerant circuit can better match the Enthalpy-temperature diagrams of all flows to be cooled (natural gas flow, PRC, LRC and SRC refrigerant mixture circuit) can be adapted.
  • the very big one Gas flow on the suction side of the compressor P3 is divided into two flows. This requires additional piping and control equipment. The However, the dimensions of the pipelines are smaller. Overall, the Energy consumption of this embodiment of the method according to the invention lower.
  • FIGS. 4 and 5 show further advantageous configurations of the method according to the invention.
  • the first or PRC and / or the second or LRC refrigerant mixture circuit are modified.
  • the SRC refrigerant mixture circuit is identical to that as shown in Figures 1 and 3.
  • the SRC refrigerant mixture cycle is therefore not shown in full.
  • the first or PRC refrigerant mixture circuit is also identical to that as shown in FIG. 3.
  • the compressed and then in the cooler L4 to a temperature between 10 and Refrigerant mixture cooled to 40 ° C of the second or LRC refrigerant mixture circuit is first the heat exchanger E1 via line L5 fed and liquefied in this. Then the refrigerant mixture is over Line L6 supplied to the heat exchanger E2 and supercooled in it. A partial flow of the supercooled refrigerant mixture is in the expansion valve L9 - or alternatively in addition in a relaxation turbine - relaxed and evaporated in the heat exchanger E2. Then this refrigerant mixture partial flow is via line L10 Separator L1 supplied. That at the head of the separator L1 via line L2 withdrawn gaseous refrigerant mixture is in the compressor L3 to a pressure compressed between 10 and 20 bar.
  • a second partial flow of the supercooled refrigerant mixture of the LRC-refrigerant mixture circuit is at a higher temperature level from the Heat exchanger E2 removed and in expansion valve L13 - or alternatively in a relaxation turbine - relaxed.
  • this partial flow of the refrigerant mixture is also in the Heat exchanger E2 evaporates and is fed to separator L15 via line L14.
  • the gaseous gas drawn off at the top of the separator L15 via line L16 Refrigerant mixture is also the compressor L3 at an intermediate pressure level fed.
  • Cooler L4 After mixing the two partial refrigerant mixture flows described in the Compressor L3 takes place, preferably against sea water, against air or against an appropriate cooling medium, a cooling of the compressed refrigerant mixture in the Cooler L4 to a temperature between 10 and 40 ° C.
  • the compressed and then in the cooler L21 to a temperature between 10 and 40 ° C cooled and partially liquefied refrigerant mixture is first about Line L5 fed to a separator L13.
  • the gaseous fraction of the Refrigerant mixture is drawn off at the top of the separator L13 via line L6, liquefied in the heat exchanger E1 and supercooled in the heat exchanger E2.
  • the liquid part of the refrigerant mixture is obtained from the bottom of the separator L13 withdrawn via line L14, subcooled in the heat exchanger E1 and in the Heat exchanger E2 brought to a less low temperature level.
  • This liquefied and supercooled partial refrigerant mixture stream is then in the Pressure relief valve L15 - or alternatively in a pressure relief turbine - relaxed, also evaporated in the heat exchanger E2 and the evaporated Refrigerant mixture partial flow mixed in line L 10.
  • the relief valve L15 Separator / storage tank and the corresponding control valves in FIG. 5 not shown.
  • the gaseous gas drawn off at the top of the separator L1 via line L2 Refrigerant mixture is in the compressor L3 to a pressure between 6 and 10 bar compacted. This is followed, preferably against sea water, air or against an appropriate cooling medium, cooling the compressed Refrigerant mixture in the cooler L4 to a temperature between 10 and 40 ° C.
  • the refrigerant mixture is passed to another via line L16 Separator L17 supplied.
  • the gaseous product at the top of the L17 separator Fraction of the refrigerant mixture is via line L18 of the second compressor stage L19 fed and compressed to a pressure between 12 and 25 bar.
  • the Liquid fraction from the separator L17 is preferably by means of the pump L20 a centrifugal pump, pumped to a pressure between 12 and 25 bar and then with the mixed refrigerant flow compressed in the compressor L19 merged.
  • the compression of the refrigerant mixture of the second or LRC refrigerant mixture circuit preferably takes place in a two-stage, housed centrifugal compression device that both the cooler L4 and contains the separator L17.
  • Centrifugal compression device instead of Centrifugal compression device also an axial compression device be provided.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP98924120A 1997-04-18 1998-04-15 Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes Expired - Lifetime EP0975923B1 (de)

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DE19716415A DE19716415C1 (de) 1997-04-18 1997-04-18 Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
DE19716415 1997-04-18
PCT/EP1998/002198 WO1998048227A1 (de) 1997-04-18 1998-04-15 Verfahren zum verflüssigen eines kohlenwasserstoff-reichen stromes

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