EP4230937A1 - Procédé et installation de production d'un produit liquide à base d'hydrocarbures - Google Patents

Procédé et installation de production d'un produit liquide à base d'hydrocarbures Download PDF

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Publication number
EP4230937A1
EP4230937A1 EP22020072.9A EP22020072A EP4230937A1 EP 4230937 A1 EP4230937 A1 EP 4230937A1 EP 22020072 A EP22020072 A EP 22020072A EP 4230937 A1 EP4230937 A1 EP 4230937A1
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EP
European Patent Office
Prior art keywords
refrigerant
heat exchanger
pure substance
exchanger arrangement
pure
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.)
Pending
Application number
EP22020072.9A
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German (de)
English (en)
Inventor
Daniel Garthe
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Linde GmbH
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Linde GmbH
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Publication date
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Priority to EP22020072.9A priority Critical patent/EP4230937A1/fr
Publication of EP4230937A1 publication Critical patent/EP4230937A1/fr
Pending legal-status Critical Current

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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
    • F25J1/0243—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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0085—Ethane; Ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0087—Propane; Propylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—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
    • F25J1/0215—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 with one SCR 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
    • F25J1/0211—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
    • F25J1/0215—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 with one SCR cycle
    • F25J1/0216—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 with one SCR cycle using a C3 pre-cooling cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • 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
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers

Definitions

  • the present invention relates to a process and a plant for producing a liquefied hydrocarbon product according to the respective preambles of the independent patent claims.
  • the invention proposes a method and a plant for producing a liquefied hydrocarbon product with the respective features of the independent patent claims. Refinements of the invention are the subject matter of the dependent claims and the following description.
  • the present invention can be used in particular in connection with the liquefaction of natural gas after suitable processing, but is also suitable for the liquefaction of other hydrocarbon mixtures, in particular methane-rich hydrocarbon mixtures with a methane content of more than 80%, or possibly corresponding pure substances.
  • hydrocarbon feeds are referred to generically herein as "hydrocarbon feeds".
  • a hydrocarbon feed is therefore in particular processed natural gas, which does not have to consist exclusively of hydrocarbons, but can also contain nitrogen and other gas components such as noble gases (especially helium).
  • mixed refrigerants made of different hydrocarbon components and nitrogen can be used in natural gas liquefaction.
  • one, two or three mixed refrigerant circuits can be used (single mixed refrigerant, SMR; dual mixed refrigerant, DMR; mixed fluid cascade, MFC).
  • Mixed refrigerant circuits with propane pre-cooling (C3MR) are also known.
  • the present application can relate in particular to the latter case, in which case propane is used as the pure refrigerant.
  • pressure level and “temperature level” to characterize pressures and temperatures, which is intended to express that corresponding pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values.
  • pressures and temperatures typically range within certain ranges, for example ⁇ 10% around an average value.
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another. In particular, for example, pressure levels include unavoidable or expected pressure losses. The same applies to temperature levels.
  • a "heat exchanger” for use in the context of the present invention can be of any type which is conventional in the art. It is used for the indirect transfer of heat between at least two fluid flows, e.g. in counterflow to one another. In the latter case, it is a "counterflow heat exchanger".
  • a corresponding heat exchanger can be formed from a single or several heat exchanger sections connected in parallel and/or in series, e.g. from one or more coiled heat exchangers or corresponding sections.
  • a counterflow heat exchanger which can be designed in particular as a (brazed) fin-plate heat exchanger made of aluminum (Brazed Aluminum Plate-Fin Heat Exchanger, PFHE; designations according to the German and English edition of ISO 15547-2:3005),
  • heat exchangers are also used, in which a fluid to be cooled is guided in corresponding lines (for example a tube bundle) through a jacket space into which a fluid used for cooling is expanded.
  • a “pure substance refrigerant” is mentioned below, this is to be understood in particular as meaning a refrigerant that has more than 90 mole percent, in particular more than 95 mole percent or more than 99 mole percent, of a single component.
  • the component can in particular be ethylene, ethane, propylene or propane.
  • a “mixed refrigerant” is characterized in particular by the fact that it has a number of components, none of which is contained in a content of more than 80 mole percent, in particular more than 70 mole percent or more than 60 mole percent.
  • the components can be, in particular, nitrogen, methane, ethane, propane, butane and pentane and unsaturated equivalents of these compounds.
  • such a mixed refrigerant can be propane-free or have propane in a content of at most 10 mole percent, in particular at most 5 mole percent or at most 1 mole percent.
  • the present invention proposes a method for producing a liquid hydrocarbon product using a gaseous hydrocarbon feed, in which a pure substance refrigerant circuit operated with a pure substance refrigerant, which has a first heat exchanger arrangement, and a mixed refrigerant cycle operated with a mixed refrigerant, which has a second heat exchanger arrangement, are provided and wherein at least a portion of the hydrocarbon feed is first pre-cooled using the pure refrigerant cycle and then liquefied to the liquid hydrocarbon product using the mixed refrigerant cycle.
  • the pure substance refrigerant partial flows of the pure substance refrigerant at different feed pressure levels and at different Feed-in temperature levels are fed in, with the pure substance partial refrigerant flows being brought to the feed-in pressure levels and feed-in temperature levels by expansion starting from a common pre-expansion pressure level and different pre-expansion temperature levels (these terms are used in particular to refer to the pressure or temperature levels immediately upstream of the expansion, which can take place in particular by means of suitable valves).
  • the pre-expansion temperature levels are selected in such a way that the pure substance partial refrigerant flows are still in the supercooled state at the feed temperature levels.
  • At least part of the mixed refrigerant of the mixed refrigerant circuit is also cooled by means of the pure substance refrigerant circuit.
  • the pre-cooling of the hydrocarbon charge and the refrigerant mixture is carried out in particular by means of two series-connected heat exchangers of the first heat exchanger arrangement in the pure refrigerant circuit. As already expressed in other words, these are cooled by feeding in supercooled pure refrigerant fractions or partial flows at different evaporation pressure levels, the different feed temperature levels. Up to the lowest pressure level, all pure refrigerant fractions or partial flows are supercooled, in particular by the evaporation of the next lower pure refrigerant pressure level or the corresponding pure refrigerant partial flow, to such an extent that the pure refrigerant fractions are still supercooled after their expansion in corresponding valves, with an extent of supercooling being advantageous configurations given below.
  • a partial flow taken from the cold side of the first heat exchanger arrangement can also be further cooled, as explained below, using the mixed refrigerant circuit, so that it is also supercooled after corresponding expansion.
  • the pre-cooling of the hydrocarbon charge and the mixed refrigerant using the first heat exchanger arrangement or the pure substance refrigerant can be carried out within the scope of the present invention, in particular in the supercritical state, in order to avoid the need for a separator between the two heat exchanger arrangements.
  • the cooling (in heat exchanger E7) and the liquefaction (in heat exchanger E8) take place in indirect heat exchange against the refrigerant mixture of a mixed refrigerant circuit. More precisely, the cooling (in heat exchanger E7) takes place in the heat exchange against the fully evaporated mixed refrigerant of the mixed refrigerant circuit.
  • condensed Mixed refrigerant of the mixed refrigerant circuit is pre-cooled by means of a pure substance refrigerant circuit (comprising heat exchangers E1 to E4) and the composition of the mixed refrigerant and/or the compressor discharge pressure of the mixed refrigerant circuit are selected such that the refrigerant mixture is completely liquefied by the pure substance refrigerant circuit.
  • a cooling of the mixture refrigerant in the heat exchangers E1 to E4 above its critical pressure also leads to a single-phase state downstream of the heat exchanger E4.
  • the pure refrigerant circuit includes, among other things, the containers D1 to D5 and the jacket spaces of the heat exchangers E1 to E4.
  • the inventory of pure liquid refrigerant contained therein may represent a safety risk for the entire system.
  • the large devices D1 to D4 and E1 to E4 are usually brought individually to the construction site and cause high installation costs due to the time-consuming assembly.
  • the pure substance refrigerant circuit can be redesigned in such a way that a high degree of prefabrication can be achieved and the liquid inventory of refrigerant is significantly reduced.
  • compact heat exchangers such as plate heat exchangers without phase separators can be used to feed the individual pure refrigerant flows in the pure refrigerant circuit according to one embodiment of the present invention.
  • the footprint of a plate heat exchanger solution for the pure refrigerant circuit decreases significantly compared to traditional solutions using kettle-type heat exchangers.
  • the hydrocarbon inventory in the pure substance refrigerant circuit decreases in the process described. Due to the lower hydrocarbon inventory and due to the fact that plate heat exchangers are usually built in cold boxes with welded flange connections, which significantly reduces the potential for leakage, the entire process can be implemented with less safety-related effort.
  • the pure refrigerant is cooled in the first heat exchanger arrangement, with part of the pure refrigerant substreams being removed from the first heat exchanger arrangement at their pre-expansion temperature levels.
  • the pure component refrigerant flows can be branched off in particular from a common flow of the pure component refrigerant, which is fed to the first heat exchanger arrangement on the warm side, in particular via intermediate removals from the plate heat exchangers used here and between them.
  • part of the pure substance refrigerant cooled in the first heat exchanger arrangement is further cooled in the second heat exchanger arrangement, with the at least one of the pure substance refrigerant partial flows being formed at its pre-expansion temperature level using the pure substance refrigerant further cooled in the second heat exchanger arrangement.
  • a bypass can be used for better controllability of the temperature, as in figure 1 explained.
  • part of the pure refrigerant cooled in the first heat exchanger arrangement can be expanded to obtain a two-phase flow, the two-phase flow being subjected to phase separation to obtain a gas phase and a liquid phase, and the gas phase and the liquid phase then being fed to the first heat exchanger arrangement become.
  • the decoupling of the pure substance refrigerant circuit from the mixed refrigerant circuit and the simpler design of the heat exchanger arrangement used in the latter is also advantageous here.
  • the pure component refrigerant flows are each heated in the first heat exchanger arrangement from the feed temperature level to an extraction temperature level and to the extraction temperature level of the first Removed heat exchanger assembly. In particular, they are vaporized during this heating.
  • the feed-in temperature levels and the removal temperature levels of the pure component refrigerant flows each enclose temperature intervals, with the temperature intervals for the pure component refrigerant flows not overlapping one another. This corresponds in particular to the subcooling already mentioned above due to the evaporation of the respectively next lower pure substance refrigerant pressure level or the corresponding pure substance refrigerant partial flow.
  • the pure component refrigerant streams are jointly fed to compression and condensation after removal from the first heat exchanger arrangement before they are supercooled in the first heat exchanger arrangement, as is known per se in a corresponding pure substance refrigerant circuit.
  • the pure substance refrigerant partial streams are present at the infeed temperature levels in a state that is at least 3 K supercooled, in particular in a state that is at least 5 K, 7 K or 10 K supercooled.
  • plate (fin) heat exchangers can be used in the first heat exchanger arrangement.
  • a pure substance refrigerant circuit denoted overall by 10
  • a heat exchanger arrangement (“first" heat exchanger arrangement) having a first heat exchanger E1 and a second heat exchanger E2
  • a mixed refrigerant circuit denoted overall by 20
  • a third heat exchanger E3 and a fourth heat exchanger E4 (or corresponding Sections of a tube bundle heat exchanger) having a heat exchanger arrangement (“second" heat exchanger arrangement) shown.
  • a hydrocarbon charge in the example shown natural gas NG, is fed via a line 1, if necessary, to a compressor C3 and, in particular, compressed to a supercritical state (see flow point 2).
  • the hydrocarbon charge (see stream point 3) is pre-cooled in the heat exchangers E1 and E2 of the first heat exchanger arrangement (see stream point 4 and 5) and, following this pre-cooling, it is heavily supercooled in the heat exchangers E3 and E4 of the second heat exchanger arrangement (see stream point 6).
  • the pure substance refrigerant of the pure substance refrigerant circuit 10 is liquefied in a condenser E5 and fed to a buffer tank D1 (see current point 11).
  • the liquid pure refrigerant (see current point 12) is then supercooled in a heat exchanger E6 and fed to a heat exchanger E1 (see current point 13).
  • the complete pure substance refrigerant of the pure substance refrigerant circuit 10 is supercooled in the heat exchanger E1 at the highest pressure level (pressure level 1) in the pure substance refrigerant circuit (see current point 14).
  • the first part of stream 14 is expanded via a line 15 and a valve V1 to the second highest pressure in the pure substance refrigerant circuit 10 (pressure level 2, see stream point 16) and then completely evaporated in heat exchanger E1 (see stream point 17).
  • the supercooling of the pure refrigerant flow 16 takes place through the evaporation of the pure refrigerant flow 22 at the next lower pressure level, pressure level 3.
  • the second part of stream 14 (see stream point 20) is further supercooled in heat exchanger E2.
  • a partial flow thereof is withdrawn from the heat exchanger E2 via a line 21 (see flow point 21) and expanded to the third-highest pressure level in a valve V2.
  • the supercooled pure refrigerant 22 is then completely evaporated in the heat exchanger E1, see flow point 23.
  • the pure refrigerant 22 is supercooled by evaporating the pure refrigerant flow 32 at the next lower pressure level, pressure level 4.
  • the remaining portion of the pure refrigerant stream 20 is in turn further supercooled in the heat exchanger E2, see stream point 30.
  • a first partial stream thereof (see stream point 31) is expanded to the fourth pressure level in a valve V3 and fed supercooled into the heat exchanger E2, see stream point 32.
  • This pure refrigerant flow is completely evaporated in the heat exchanger E2, see flow point 33.
  • the pure refrigerant 32 is in turn supercooled by the evaporation of the pure refrigerant flow 44 at the next lower pressure level, pressure level 5.
  • the pure refrigerant flow 40 is further supercooled in the heat exchanger E3, which is located in the mixed refrigerant circuit, see flow point 41, 42 and 43.
  • a bypass around the heat exchanger E3 can be provided for better controllability of the temperature, see flow points 46 and 47 and valves V5A and V5B .
  • the pure refrigerant flow 44 is fed subcooled into the heat exchanger E2 and then completely evaporated in the example shown at the lowest pressure level (pressure level 5), see flow point 45.
  • phase separators allows a targeted and controllable distribution of the liquid and gas phase to the heat exchanger and thus prevents maldistribution and the associated thermal and mechanical stress.
  • these phase separators require a lot of space and usually store a large proportion of the liquid hydrocarbon inventory of the entire refrigerant circuit.
  • the use of phase separators can be used with the one presented here procedures are dispensed with.
  • the space required for a plate exchanger solution designed in this way as a pure substance refrigerant circuit is correspondingly significantly reduced in comparison to conventional kettle-type solutions.
  • the hydrocarbon inventory in the pure substance refrigerant circuit decreases considerably in the process described. Due to the lower hydrocarbon inventory and the fact that plate heat exchangers are typically built in cold boxes with welded flange connections, thus significantly reducing the potential for leakage, the entire process can be built with less safety engineering effort, as discussed above.
  • the entire mixed refrigerant flow 50 is compressed and after-cooled to a supercritical state in the two compressors C2A and C2B and the corresponding aftercoolers E7 and E8, see flow point 51, 52, 53 and 54.
  • the mixed refrigerant flow in the heat exchangers is similar to the hydrocarbon-rich fraction E1 and E2 pre-cooled and then fed into the heat exchanger E3.
  • a separator before the mixed refrigerant flow 56 is fed into the heat exchanger E3 is not required, since the mixed refrigerant flow 56 is supercritical.
  • the pure substance refrigerant stream 40 is not supercooled in the heat exchanger E3 in the mixed refrigerant circuit, but instead is fed into the heat exchanger E2 as a two-phase stream after direct expansion in the valve V4.
  • the pure refrigerant stream 44 must first be separated into a gas phase and a liquid phase in the phase separator D2. It can thus be ensured that the two-phase stream 44 is fed into the heat exchanger E2 in a controlled manner by being divided into the streams 44A and 44B. Incorrect distributions and thermal stresses on the heat exchanger E2 can thus be minimized.

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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)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP22020072.9A 2022-02-21 2022-02-21 Procédé et installation de production d'un produit liquide à base d'hydrocarbures Pending EP4230937A1 (fr)

Priority Applications (1)

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EP22020072.9A EP4230937A1 (fr) 2022-02-21 2022-02-21 Procédé et installation de production d'un produit liquide à base d'hydrocarbures

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3763658A (en) 1970-01-12 1973-10-09 Air Prod & Chem Combined cascade and multicomponent refrigeration system and method
WO2008019999A2 (fr) * 2006-08-14 2008-02-21 Shell Internationale Research Maatschappij B.V. Procédé et appareil de traitement d'un flux d'hydrocarbure
EP2199716A2 (fr) * 2008-12-12 2010-06-23 Air Products And Chemicals, Inc. Agencement de pré-refroidissement alternatif
DE102009018248A1 (de) 2009-04-21 2010-10-28 Linde Aktiengesellschaft Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3763658A (en) 1970-01-12 1973-10-09 Air Prod & Chem Combined cascade and multicomponent refrigeration system and method
WO2008019999A2 (fr) * 2006-08-14 2008-02-21 Shell Internationale Research Maatschappij B.V. Procédé et appareil de traitement d'un flux d'hydrocarbure
EP2199716A2 (fr) * 2008-12-12 2010-06-23 Air Products And Chemicals, Inc. Agencement de pré-refroidissement alternatif
DE102009018248A1 (de) 2009-04-21 2010-10-28 Linde Aktiengesellschaft Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
"Advanced Natural Gas Engineering", 2010, GULF PUBLISHING COMPANY, article "Liquefied Natural Gas (LNG"
"Ullmann's Encyclopedia of Industrial Chemistry", 15 July 2006, article "Natural Gas"
JOSTEIN PETTERSEN ET AL: "C02 as Precooling Refrigerant in Floating LNG Production Plants", AICHE SPRING MEETING. NATURAL GAS UTILIZATION,, 25 April 2004 (2004-04-25), pages 490 - 497, XP009103332 *

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