EP0470532B1 - Verfahren zum Verdampfen von flüssigem Erdgas - Google Patents

Verfahren zum Verdampfen von flüssigem Erdgas Download PDF

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Publication number
EP0470532B1
EP0470532B1 EP91113073A EP91113073A EP0470532B1 EP 0470532 B1 EP0470532 B1 EP 0470532B1 EP 91113073 A EP91113073 A EP 91113073A EP 91113073 A EP91113073 A EP 91113073A EP 0470532 B1 EP0470532 B1 EP 0470532B1
Authority
EP
European Patent Office
Prior art keywords
natural gas
fluid
cycle
stage
heated
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
EP91113073A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0470532A1 (de
Inventor
Hans Dr.-Ing. Schmidt
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP0470532A1 publication Critical patent/EP0470532A1/de
Application granted granted Critical
Publication of EP0470532B1 publication Critical patent/EP0470532B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F17C9/04—Recovery of thermal energy
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification

Definitions

  • the invention relates to a method for vaporizing liquid, pressurized natural gas with energy generation by heating and vaporizing the liquid natural gas in a multi-stage heat exchange with fluids conducted in separate circuits, with part of the natural gas warmed to ambient temperature being used as the fluid for a first circuit branched off, relieved of work, condensed in the heat exchange with liquid natural gas, pumped to the pressure level of the liquid natural gas and admixed with the natural gas to be heated before the first heat exchange stage.
  • the present invention was therefore based on the object of developing the method of the type mentioned at the outset in such a way that a lower investment cost, combined with an equally good or even better energy recovery, is ensured.
  • the fluid of the first circuit is divided into two partial flows after the work-related relaxation and condensation, one of which is compressed to the pressure of the natural gas to be evaporated and mixed with it and the second parallel to the natural gas to be evaporated, but separately from this through all heat exchange stages, evaporated, warmed and then released as a natural gas low-pressure product.
  • the fluid of the first circuit that is to say natural gas warmed to ambient temperature
  • the fluid of the first circuit is expanded to the desired delivery pressure in the process according to the invention and then condensed against liquid natural gas to be heated.
  • a partial stream of the fluid is compressed to the pressure of the liquid natural gas stream and mixed again.
  • the other partial flow is evaporated and warmed up again parallel to the path of the natural gas flow and drawn off as a separate product gas flow.
  • the partial flow is expediently drawn off after the condensation of the fluid, since the composition of the product stream is only equal to the composition of the liquid natural gas fed into the system in the event of strongly fluctuating operating conditions.
  • the amount of fluid diverted from the vaporized natural gas flow depends on the desired amount of product gas that is to be delivered at a lower pressure level than the liquid natural gas feed stream.
  • the process according to the invention can also be used to process liquid natural gas flows of different inlet pressures by bringing them to a common high pressure and evaporating the total flow in the heat exchange with fluids from several circuits.
  • product streams of different pressures can advantageously be generated in a system without increasing the number of system components involved in the method compared to the prior art.
  • a plurality of product streams can also be generated at different pressure levels, for which the fluid of the first circuit is expanded in a multi-stage, work-performing manner.
  • the multi-stage work-relieving relaxation can be carried out by expansion machines connected in series as well as with units operated in parallel. If the expansion machines are connected in series, at least part of the already reduced pressure fluid is further expanded. If the expansion machines are connected in parallel, the fluid is distributed to branch flows, each of which is expanded to different pressure levels.
  • parallel and serial modes of operation of the expansion machines can also be combined with one another.
  • the multi-stage relaxation work is carried out by distributing the fluid of the first circuit to branch streams before it releases the work is, each of which is relieved of work and condensed in different condensation stages, whereupon a partial flow is branched off and heated and drawn off parallel to the path of the natural gas to be heated.
  • the fluid of the first circuit is expanded in a one-stage work-performing manner.
  • this procedure contains an advantageous aspect.
  • the further treatment of the work-relieved relaxed fluid of the first circuit can be chosen such that branch streams branched on partial streams are omitted, while only the branch stream to be completely mixed again with the natural gas to be evaporated is retained after its condensation.
  • the described procedure represents only a particularly preferred special case of the possibilities of multi-stage relaxation.
  • the branch streams generated in serial mode of operation can be used, since the invention can be applied to all multi-stage fluid streams relaxed .
  • a fluid is conducted in a second circuit, which is relaxed in a one-stage work-performing manner after heating to ambient temperature in order to obtain energy.
  • This embodiment of the method according to the invention can also be modified in that a fluid is conducted in a second circuit which, after heating to ambient temperature, is broken down into partial streams which are expanded in a work-producing manner in order to obtain energy.
  • mixture circuits are particularly favorable. It is proposed to use a C1 / C2 / C3 hydrocarbon mixture or a C1 / C2 hydrocarbon mixture or a C2 / C3 hydrocarbon mixture as the fluid of the second circuit.
  • C1 to C6 hydrocarbons are also particularly favorable to use a mixture of C1 to C6 hydrocarbons as the fluid of the second circuit, the C2 content being less than 90 mol%.
  • the designations C1 to C6 denote hydrocarbons with one to six carbon atoms.
  • the selection of the heat-exchanging fluid of the second circuit depends on the composition of the natural gas stream to be evaporated in order to make the thermal contact of the streams with one another particularly efficient and to provide the greatest possible energy for work-related relaxation.
  • Pure substances can also be used as fluids of the second circuit.
  • ammonia, propane or chlorofluorocarbons can be used favorably. In the latter case, there is also the possibility of mixing different chlorofluorocarbons for the fluid.
  • the fluid of the further circuit is advantageously expanded in a single stage or, with particular preference, also in a multi-stage work-performing manner.
  • Every process for the vaporization of liquid natural gas with simultaneous energy generation is based on the principle, a heating medium that is at the highest temperature level participates in the heat exchange to withdraw the required energy in the form of heat. It is particularly favorable for the invention if the circulation fluids are heated to ambient temperature in the last heat exchange stage by heat exchange with a glycol-water solution.
  • the number of separate circuits is limited to the first fluid circuit and the circuit of the heating medium.
  • a further embodiment of the method according to the invention provides that the fluids of the second and / or third circular run after their condensation against natural gas to be heated and pumps at elevated pressure in whole or in part in order to conduct the condensation level corresponding to the pressure level and to participate in the heat transfer only at the next higher heat exchange level.
  • the device used to carry out the method consists of heat exchange / condensation stages, at different temperature levels for the heat exchange of the circulating fluids with the natural gas to be evaporated, at least one heating stage in which the natural gas and the circulating fluids are heated to the highest process temperature against a heating medium, expansion machines for work relaxation and pumps for the recompression of the fluids condensed during heat exchange.
  • the heat exchange / condensation stages it is particularly favorable to design the heat exchange / condensation stages as straight tube heat exchangers with multiple tube paths or bundles, or as wound tube heat exchangers with multiple tube paths.
  • Another option is to use straight tube heat exchangers with only one tube path. In this case, several of these heat exchangers are connected in parallel for each heat exchange / condensation stage.
  • FIG. 1 shows the execution of the method according to the invention, in which a second fluid circuit is used in addition to the heating circuit and the first circuit.
  • a liquid, pressurized natural gas stream 1 is heated in a heat exchanger E1 against condensing natural gas from line 2b.
  • this liquid natural gas stream can be composed of individual streams which are brought to a common high pressure.
  • heat exchanger E2 the natural gas stream to be evaporated is further heated against the fluid of a second circuit which is conducted in the circuit of lines 3a, 3b and 3c.
  • the final heating of the natural gas is carried out in heat exchanger H3A in countercurrent to the heating medium to be cooled from line 4.
  • part of the gaseous natural gas stream 1 warmed to ambient temperature is drawn off via a branch line 2a, expanded in a work-performing manner in expansion machine X1, and condensed in heat exchanger / condensation stage E1.
  • a partial stream 2c intended for delivery is separated off and heated and evaporated in the heat exchangers E1, E2 and H3B parallel to the natural gas path.
  • This partial flow forms the natural gas low-pressure product.
  • the Residual condensed natural gas of line 2b is, as in the known method, compressed by pump P1 and mixed with the liquid natural gas stream 1 to be evaporated.
  • the fluid of the second circuit draws its energy for work performance and natural gas heating from the heating medium provided in line 4.
  • the fluid of the second circuit After passing through heat exchanger H3C, the fluid of the second circuit has evaporated and is fed through line 3a to the expansion turbine X2 and expanded in a work-performing manner.
  • the resulting pressure-reduced stream 3b is then condensed in heat exchanger E2 against condensed pressure-increased fluid of the second circuit, the natural gas stream to be heated in line 1 and the natural gas low-pressure product stream to be heated in parallel and brought to increased pressure again by means of pump P2.
  • the medium used to heat the fluids to the highest process temperature is fed via line 4, and through the parallel heat exchangers H3A (in thermal contact with the natural gas to be evaporated under high pressure), H3B (in thermal contact with the low-pressure product to be heated) and heat exchanger H3C (in thermal contact with fluid to be evaporated from the second circuit) and drawn off after the heat removal via line 5.
  • H3A in thermal contact with the natural gas to be evaporated under high pressure
  • H3B in thermal contact with the low-pressure product to be heated
  • heat exchanger H3C in thermal contact with fluid to be evaporated from the second circuit
  • the method according to the invention provides significant advantages compared to the simplest method variant of DE-A 38 36 061. While the method according to the invention manages with only one evaporation system, in a method according to the state of the art Technology two separate systems can be used. The mechanical effort is halved accordingly by using the invention.
  • FIG. 2 shows an embodiment of the method according to the invention, in which two circulating fluids are expanded in a multi-stage, work-performing manner.
  • natural gas streams which have different admission pressure, are brought to a common increased pressure and fed to the natural gas evaporation plant in the common line 1.
  • This common stream is heated and evaporated in gradual thermal contact with the heat exchange fluids of the individual circuits.
  • Part of the high-pressure product formed is drawn off in line 2c, while the remaining part is relaxed in the expansion machine X4 while performing work.
  • the pressure-reduced product formed in line 2b is then heated in heat exchanger H3E against heating fluid to ambient temperature. Part of this product is drawn off via line 2b ', while the part which is discharged via line 2a forms the fluid of the first circuit.
  • the fluid stream 2a is divided into the branch streams 3a and 3b for energy generation, and these streams are expanded in the expansion machines X1B and X1A to different pressure levels while performing work.
  • the relaxed branch flow 3a is condensed in heat exchanger E1A against liquid natural gas to be heated in line 1. After the condensation, a partial stream at reduced pressure is drawn off and heated and evaporated parallel to the remaining natural gas path and drawn off as product in line 4. The rest of the condensed portion is compressed to the natural gas pressure by means of pump P1A and mixed with the liquid natural gas before it passes through the first heat exchanger.
  • the relaxed branch flow 3b is carried out in an analogous manner, with the heat exchange or condensation in heat exchanger E1B of the flows taking place at a higher temperature / heat exchange level.
  • each pressure level corresponds to a heat exchange / condensation level of the fluid assigned to it.
  • the heat exchange stage at the lowest temperature level must be used, while the condensation / heat exchange stages at the higher temperature level can be charged with increasing pressure.
  • the fluid of the second circuit is also expanded in a two-stage work-performing manner by distributing the evaporated fluid stream 6 leaving the heating stage H3D to branch streams 6a and 6b. These are brought to different pressures by means of expansion machines X2A and X2B, condensed against natural gas and fluid to be heated in condensation stages E2A and E2B according to their pressure level and mixed again after compression to a common pressure in pumps P2A and P2B.
  • the fluid of the third circuit 7 is expanded in a one-stage work-performing manner by means of expansion machine X3 and is condensed in condensation stage E3 against natural gas of different pressures. After compression in P3 to the outlet pressure and passage through heat exchange stages E3 and H3F, the cycle closes. Analogous to the first two circuit fluids, the fluid of the third circuit can be expanded in several stages.
  • the heat required for energy production and vaporization of natural gas comes from a heating circuit, which is indicated by lines 8 and 9.
  • the warm heating medium 8 is distributed to the heating stages H3A to H3F and releases its heat there to the vaporized natural gas product streams of different pressures and the fluids of the first to third circuits.
  • the cooled heating medium is drawn off via line 9.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Exhaust Gas After Treatment (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP91113073A 1990-08-07 1991-08-03 Verfahren zum Verdampfen von flüssigem Erdgas Expired - Lifetime EP0470532B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4025023 1990-08-07
DE4025023A DE4025023A1 (de) 1990-08-07 1990-08-07 Verfahren zum verdampfen von fluessigem erdgas

Publications (2)

Publication Number Publication Date
EP0470532A1 EP0470532A1 (de) 1992-02-12
EP0470532B1 true EP0470532B1 (de) 1994-01-19

Family

ID=6411793

Family Applications (1)

Application Number Title Priority Date Filing Date
EP91113073A Expired - Lifetime EP0470532B1 (de) 1990-08-07 1991-08-03 Verfahren zum Verdampfen von flüssigem Erdgas

Country Status (7)

Country Link
EP (1) EP0470532B1 (ko)
JP (1) JPH0747748B2 (ko)
KR (1) KR960004253B1 (ko)
DE (2) DE4025023A1 (ko)
ES (1) ES2051058T3 (ko)
PT (1) PT98585B (ko)
TW (1) TW204365B (ko)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4317187B2 (ja) * 2003-06-05 2009-08-19 フルオー・テクノロジーズ・コーポレイシヨン 液化天然ガスの再ガス化の構成および方法
DE10358311A1 (de) * 2003-12-11 2005-07-14 Bayerische Motoren Werke Ag System und Verfahren zur Verdampfung eines kryogen gespeicherten Kraftstoffs
FR2879720B1 (fr) * 2004-12-17 2007-04-06 Snecma Moteurs Sa Systeme de compression-evaporation pour gaz liquefie
CA2686850A1 (en) * 2007-05-30 2008-12-11 Fluor Technologies Corporation Lng regasification and power generation
JP5970349B2 (ja) 2012-11-16 2016-08-17 日本発條株式会社 ストラット形懸架装置と、懸架装置用圧縮コイルばね
EP3527869A1 (de) 2018-02-16 2019-08-21 Siemens Aktiengesellschaft Lng wiedervergasung
JP2023149895A (ja) * 2022-03-31 2023-10-16 住友精密工業株式会社 熱交換システム

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4479350A (en) * 1981-03-06 1984-10-30 Air Products And Chemicals, Inc. Recovery of power from vaporization of liquefied natural gas
DE3836061A1 (de) * 1987-12-21 1989-06-29 Linde Ag Verfahren zum verdampfen von fluessigem erdgas

Also Published As

Publication number Publication date
PT98585B (pt) 1999-01-29
JPH06279773A (ja) 1994-10-04
DE59100889D1 (de) 1994-03-03
DE4025023A1 (de) 1992-02-13
EP0470532A1 (de) 1992-02-12
TW204365B (ko) 1993-04-21
KR960004253B1 (ko) 1996-03-28
PT98585A (pt) 1994-01-31
JPH0747748B2 (ja) 1995-05-24
ES2051058T3 (es) 1994-06-01
KR920004764A (ko) 1992-03-28

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