US3886758A - Processes for the production of nitrogen and oxygen - Google Patents

Processes for the production of nitrogen and oxygen Download PDF

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Publication number
US3886758A
US3886758A US390943A US39094373A US3886758A US 3886758 A US3886758 A US 3886758A US 390943 A US390943 A US 390943A US 39094373 A US39094373 A US 39094373A US 3886758 A US3886758 A US 3886758A
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Prior art keywords
nitrogen
stream
compressed
oxygen
pressure
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US390943A
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English (en)
Inventor
Guy Perrotin
Jean-Pierre Anselmini
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Air Liquide SA
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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
    • 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
    • F25J3/04—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 for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons
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    • 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
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    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Definitions

  • the present invention relates to a process and an installation for obtaining oxygen and a high proportion of nitrogen, on th e one'hand in liquid phase, and on the other hand in gaseous phase at one or more pressure levels, starting with air and a source of available refrigeration, for example. a liquefied natural gas being revaporised.
  • the present invention permits these disadvantages to be overcome and in addition loads to certain supplementary advantages, such as simplicity in operation and flexibility, provided that an external source of refrigeration is available.
  • This invention does in effect make it possible to limit to the minimum the compression of gases, or carrying out these compression operations at low temperature as often as possible, to reduce the number and the total installed power and to limit the machines, of considerably the height of the exchangers (because of the treatment of the gases under pressure or by liquefactionvaporisation in the main exchange line).
  • This invention also makes it possible to simplify the operation of an installation for the production of oxygen and a high proportion of nitrogen in gaseous form and under pressure and/or in liquid form, because such aninstallation requires only a small number of compressors and a single turbine, these machines generally being of the centrifugal type.
  • the versatility of such an installation is such that the various products can be obtained with very variable quantities of external refrigeration, which can if necessary be reduced to zero. Moreover, the proportions between the various products can vary' within very wide limits.
  • the present invention has for its object a process for obtaining oxygen and nitrogen. possibly on the one hand in liquid phase and, on the other hand, in gaseous phase. wherein a part of the reheated pure gaseous nitrogen originating from the separation stage is compressed, cooled and condensed by exchange with a liquid natural gas being revaporised, expanded, a part of the expanded liquid fraction being at least utilised for ensuring the reflux of the said separation stage and the vaporised fraction being reunited with the nitrogen compressed before the said compression wherein liquid nitrogen and gaseous nitrogen and oxygen, are ob tained at different pressure levels, the said part of the reheated pure gaseous nitrogen reunited with part of this gaseous nitrogen extracted before the end of reheating, after condensation and before its expansion, is subcooled by counter-current flow of the fraction vaporised during the said expansion, possibly after being recondensed by exchange with the pure oxygen liquid fraction obtained at the bottom of the separation and reunited after subcooling with nitrogen at intermediate pressure.
  • At least a part of the liquefied fraction thus expanded is at least partly used for obtaining a fraction of expanded liquid pure nitrogen, this liquid fraction being subcooled beforehand in counter-current with a fraction vaporised during the said subsequent expansion.
  • a part of the pure liquid oxygen originating from the said separation is compressed, heated and vaporised, the other part being subcooled in countercurrent with a vaporised fraction during the subsequent expansion and partially obtained expanded to the liquid state.
  • the compression of the heated gaseous nitrogen is effected in a single step or in several separate steps, and preferably in two steps by passing over at an intermediate pressure.
  • the gaseous nitrogen, compressed, cooled and condensed by exchange with a liquid natural gas being revaporised is subcooled in at least two steps before two successive expansion; the fraction vaporised during the first expansion and having effected the first subcooling is reunited with a part of the nitrogen compressed at intermediate pressure, then liquefied, preferably by exchange with the oxygen-enriched liquid fraction obtained in the said separation, then subcooled, preferably by exchange, at least with the pure gaseous nitrogen originating from the separation, and finally reunited with the liquid fraction, obtained after the first expansion, before the latter fraction is subjected to the said second expansion.
  • the said separation is effected by distillation at a single pressure or by distillation at two different pressures.
  • the air prior to the separation by distillation, is compressed to a first level, purified, then cooled by exchange with a fraction of natural gas and finally compressed to a higher pressure level.
  • liquid nitrogen and oxygen in pure form at relatively low pressure for example atmospheric pressure
  • gaseous nitrogen and oxygen in pure form at medium pressure for example, of the order of 5 bars
  • gaseousnitrogen and oxygen in pure form at possibly different high pres sures (such as at pressures of respectively 15 and 40 bars), by expansion of a part of the liquid pure oxygen originating from the separation, after subcooling by the gaseous fractions due to the expansion: by expansion of a part of the pure liquid nitrogen originating, in gaseous form, from the separation, and having been compressed in one or more steps to the said high pressure, then cooled and liquefied by exchange with a liquid natural gas by reyaporisation and expanded in one or more steps after one or more subcooling operations with the gaseous fractions obtained during the said expansion operations; by vaporisation and heating of a part of the liquid pure oxygen originating from the separation; by heating of a part of the pure gaseous nitrogen originating from the separation; by compression of a part of the liquid pure oxygen originating from the separation, followed by vaporisatiion and reheating; by compression of a part of the gaseous pure nitrogen originating from the separation, previously at least in part completely reheated.
  • FIG. 1 shows one embodiment of an installation ac cording to the present invention, comprising a double distillation column and a single compression stage of the gaseous pure nitrogen.
  • FIG. 2 represents another embodiment of an installation according to the present invention, comprising a distillation column under a single pressure and two stages for compressing gaseous pure nitrogen.
  • FIG. 1 illustrates one application of the process, in the case where it is desired to produce simultaneously gaseous oxygen at 5 and 40 bars, gaseous nitrogen at 5 and 15 bars, liquid oxygen and liquid nitrogen, making use of the refrigeration of a liquefied natural gas undergoing revaporisation.
  • the air to be treated enters the unit at 1, after being filtered. It is compressed at 6 bars in the first stages of the isothermal compressor 2, then cleansed from water and carbon dioxide by absorption of these impurities in the purification stage 3.
  • a second fraction is directed towards the subcooler 19, in which it is cooled in counter-current with the vaporised fraction in the expansion which follows this exchanger.
  • the vaporised fraction is returned to the impure" nitrogen flow (line 20).
  • the impure nitrogen is extracted at the intermediate position in the column 14 and this nitrogen is reheated in the exchangers l3 and some of the exchangers 7 before being expanded in the turbine 21 and then reheated in the line 20.
  • the pure nitrogen fraction is extracted by way of the line 22; it is reheated in the exchangers 13 and then leaves under a pressure of 5 bars (line 23). A part of this fraction is drawn off at line 24 from the exchangers 7 before complete reheating, and the mixed with a part of the nitrogen obtained at the hot end of the exchangers 7.
  • the remainder of the nitrogen is compressed at 40 bars, then cooled and condensed in the exchanger 28 in counter-current with the natural gas at bars which is being vaporised.
  • the liquid nitrogen at 5 bars, obtained in the separator 30, has two destinations:
  • one part is directed via the line 31 towards the subcooler 32 and then expanded; the liquid fraction thus collected in the separator 33 is supplied for use.
  • the other part is sent via the line 34 to return to the column 14.
  • FIG. 2 illustrates a modification of the installation shown in FIG. 1, which only differs from the latter as regards the following main points;
  • the air is only compressed to about 5 bars in a single compressor, then purified;
  • the part of the cold production which was assured by the compression of the treated air at 5 to 15 bars is replaced by a nitrogen cycle between 5 and l5 bars.
  • the nitrogen at 15 bars is drawn off on the one hand at the delivery end of the first stage of the compressor 26 and on the other hand in the separator 30 at 15 bars.
  • the nitrogen cycle according to FIG. 2 can be used in the case of FIG. 1.
  • the nitrogen at bars is introduced into the column 9 and liquefied at the top in contact with liquid oxygen. After being subcooled in 13, it can also be introduced after expansion at 5 bars into the column 14 and hence participate in the rectification.
  • the energy necessary for the compression of the pure gaseous nitrogen can be at least partly produced by expansion of a fluid flowing through an auxiliary cycle, firstly undergoing cooling and condensation by heat exchange with the said source of available refrigeration, compression by a pump and vaporisation.
  • This fluid flowing through the auxiliary cycle can be a single constituent, such as ethylene ethane, propane; it can also be composed of at least two constituents, such as an ethane-propane-butane mixture.
  • the expansion in the turbine can be accompanied by a partial liquefaction.
  • the said vaporisation, following the compression of the fluid flowing through the auxiliary cycle, is obtained by heat exchange with a flow at a higher temperature and particularly by means of residual vapours drawn off from the vapour cycle generation energy for the compression of the air prior to the treatment for separation of the air.
  • a process for separating air into oxygen and nitrogen, while vaporizing liquefied natural gas comprising:
  • a process for separating air into oxygen and nitro- 6 gen, while vaporizing liquefied natural gas comprising:
  • a process for separating air into oxygen and nitrogen, while vaporizing liquefied natural gas comprising:
  • a process for separating air into oxygen and nitrogen, while vaporizing liquefied natural gas comprising:

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US390943A 1969-09-10 1973-08-23 Processes for the production of nitrogen and oxygen Expired - Lifetime US3886758A (en)

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FR6930785A FR2060184B1 (enrdf_load_stackoverflow) 1969-09-10 1969-09-10
US6959170A 1970-09-04 1970-09-04
US390943A US3886758A (en) 1969-09-10 1973-08-23 Processes for the production of nitrogen and oxygen

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JP (1) JPS501359B1 (enrdf_load_stackoverflow)
CA (1) CA947636A (enrdf_load_stackoverflow)
DE (1) DE2044363C2 (enrdf_load_stackoverflow)
ES (1) ES383502A1 (enrdf_load_stackoverflow)
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JPS5382687A (en) * 1976-12-28 1978-07-21 Nippon Oxygen Co Ltd Air liquefaction rectifying method
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
US5037462A (en) * 1986-04-02 1991-08-06 Linde Aktiengesellschaft Process and device for production of nitrogen
US5036672A (en) * 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
US5139547A (en) * 1991-04-26 1992-08-18 Air Products And Chemicals, Inc. Production of liquid nitrogen using liquefied natural gas as sole refrigerant
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
US5205127A (en) * 1990-08-06 1993-04-27 Air Products And Chemicals, Inc. Cryogenic process for producing ultra high purity nitrogen
US5220798A (en) * 1990-09-18 1993-06-22 Teisan Kabushiki Kaisha Air separating method using external cold source
EP1314941A3 (de) * 2001-11-23 2003-08-27 Messer AGS GmbH Verfahren und Vorrichtung zur Erzeugung von Stickstoff aus Luft
US20040083756A1 (en) * 2002-11-01 2004-05-06 Jean-Pierre Tranier Combined air separation natural gas liquefaction plant
US20040227040A1 (en) * 2002-04-19 2004-11-18 Crain Enterprise, Inc. Geomatic pole support and foot therefor
EP1544560A1 (en) * 2003-12-19 2005-06-22 Linde BOC Process Plants LLC Process and apparatus for producing liquid nitrogen
US20080000266A1 (en) * 2006-06-30 2008-01-03 Dee Douglas P System to increase capacity of LNG-based liquefier in air separation process
US20080190118A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and unloading of lng from the tank
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
EP2050999A1 (en) 2007-10-19 2009-04-22 Air Products and Chemicals, Inc. System to cold compress an air stream using natural gas refrigeration
US7552599B2 (en) 2006-04-05 2009-06-30 Air Products And Chemicals, Inc. Air separation process utilizing refrigeration extracted from LNG for production of liquid oxygen
US20090199591A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Liquefied natural gas with butane and method of storing and processing the same
US20090259081A1 (en) * 2008-04-10 2009-10-15 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US20090266086A1 (en) * 2007-04-30 2009-10-29 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Floating marine structure having lng circulating device
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
EP2551619A1 (de) 2011-07-26 2013-01-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff und Drucksauerstoff durch Tieftemperaturzerlegung von Luft
US20150188172A1 (en) * 2013-12-31 2015-07-02 Doosan Heavy Industries & Construction Co., Ltd. Fuel cell system using natural gas
WO2018213507A1 (en) * 2017-05-16 2018-11-22 Ebert Terrence J Apparatus and process for liquefying gases

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JPS5527274B2 (enrdf_load_stackoverflow) * 1974-06-07 1980-07-19
US4400188A (en) * 1981-10-27 1983-08-23 Air Products And Chemicals, Inc. Nitrogen generator cycle
JP4707865B2 (ja) * 2001-04-18 2011-06-22 エア・ウォーター株式会社 深冷空気分離装置
JP4908740B2 (ja) * 2004-03-23 2012-04-04 株式会社神戸製鋼所 深冷空気分離装置の運転方法
RU2460952C2 (ru) * 2010-07-20 2012-09-10 Общество с ограниченной ответственностью "ЗИФ" (ООО"ЗИФ) Способ разделения воздуха
RU2522132C2 (ru) * 2012-07-10 2014-07-10 Ооо "Зиф" Способ разделения воздуха
DE102013012657A1 (de) 2013-07-30 2013-10-31 Linde Aktiengesellschaft Verfahren zur Erzeugung zumindest eines Luftprodukts und Luftbehandlungsanlage
FR3074274B1 (fr) * 2017-11-29 2020-01-31 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de separation d'air par distillation cryogenique
EP3696486A1 (de) * 2019-02-13 2020-08-19 Linde GmbH Verfahren und anlage zur bereitstellung eines oder mehrerer sauerstoffreicher, gasförmiger luftprodukte

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JPS5382687A (en) * 1976-12-28 1978-07-21 Nippon Oxygen Co Ltd Air liquefaction rectifying method
US5037462A (en) * 1986-04-02 1991-08-06 Linde Aktiengesellschaft Process and device for production of nitrogen
US4834785A (en) * 1988-06-20 1989-05-30 Air Products And Chemicals, Inc. Cryogenic nitrogen generator with nitrogen expander
US5036672A (en) * 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
US5205127A (en) * 1990-08-06 1993-04-27 Air Products And Chemicals, Inc. Cryogenic process for producing ultra high purity nitrogen
US5220798A (en) * 1990-09-18 1993-06-22 Teisan Kabushiki Kaisha Air separating method using external cold source
US5139547A (en) * 1991-04-26 1992-08-18 Air Products And Chemicals, Inc. Production of liquid nitrogen using liquefied natural gas as sole refrigerant
US5141543A (en) * 1991-04-26 1992-08-25 Air Products And Chemicals, Inc. Use of liquefied natural gas (LNG) coupled with a cold expander to produce liquid nitrogen
EP1314941A3 (de) * 2001-11-23 2003-08-27 Messer AGS GmbH Verfahren und Vorrichtung zur Erzeugung von Stickstoff aus Luft
US20040227040A1 (en) * 2002-04-19 2004-11-18 Crain Enterprise, Inc. Geomatic pole support and foot therefor
US20040083756A1 (en) * 2002-11-01 2004-05-06 Jean-Pierre Tranier Combined air separation natural gas liquefaction plant
US7143606B2 (en) * 2002-11-01 2006-12-05 L'air Liquide-Societe Anonyme A'directoire Et Conseil De Surveillance Pour L'etide Et L'exploitation Des Procedes Georges Claude Combined air separation natural gas liquefaction plant
EP1544560A1 (en) * 2003-12-19 2005-06-22 Linde BOC Process Plants LLC Process and apparatus for producing liquid nitrogen
US7552599B2 (en) 2006-04-05 2009-06-30 Air Products And Chemicals, Inc. Air separation process utilizing refrigeration extracted from LNG for production of liquid oxygen
US20080000266A1 (en) * 2006-06-30 2008-01-03 Dee Douglas P System to increase capacity of LNG-based liquefier in air separation process
US7712331B2 (en) 2006-06-30 2010-05-11 Air Products And Chemicals, Inc. System to increase capacity of LNG-based liquefier in air separation process
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US20080190118A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and unloading of lng from the tank
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US20080190117A1 (en) * 2007-02-12 2008-08-14 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank and operation of the same
US20090211262A1 (en) * 2007-02-12 2009-08-27 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship having lng circulating device
US10508769B2 (en) 2007-02-12 2019-12-17 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
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US20090266086A1 (en) * 2007-04-30 2009-10-29 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Floating marine structure having lng circulating device
US20080295527A1 (en) * 2007-05-31 2008-12-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Lng tank ship with nitrogen generator and method of operating the same
CN101413750B (zh) * 2007-10-19 2013-06-19 气体产品与化学公司 利用天然气制冷对空气流进行冷压缩的系统
US20090100863A1 (en) * 2007-10-19 2009-04-23 Air Products And Chemicals, Inc. System to Cold Compress an Air Stream Using Natural Gas Refrigeration
US8601833B2 (en) * 2007-10-19 2013-12-10 Air Products And Chemicals, Inc. System to cold compress an air stream using natural gas refrigeration
EP2050999A1 (en) 2007-10-19 2009-04-22 Air Products and Chemicals, Inc. System to cold compress an air stream using natural gas refrigeration
US20090199759A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20100012015A1 (en) * 2008-02-11 2010-01-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US20090199591A1 (en) * 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Liquefied natural gas with butane and method of storing and processing the same
US7841288B2 (en) 2008-02-11 2010-11-30 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US7644676B2 (en) 2008-02-11 2010-01-12 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
US9086188B2 (en) 2008-04-10 2015-07-21 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US20090259081A1 (en) * 2008-04-10 2009-10-15 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and system for reducing heating value of natural gas
US20100122542A1 (en) * 2008-11-17 2010-05-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Method and apparatus for adjusting heating value of natural gas
CN102901322A (zh) * 2011-07-26 2013-01-30 林德股份公司 通过低温空气分离获得压力氮和压力氧的方法和装置
CN102901322B (zh) * 2011-07-26 2016-08-10 林德股份公司 通过低温空气分离获得压力氮和压力氧的方法和装置
EP2551619A1 (de) 2011-07-26 2013-01-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff und Drucksauerstoff durch Tieftemperaturzerlegung von Luft
US20150188172A1 (en) * 2013-12-31 2015-07-02 Doosan Heavy Industries & Construction Co., Ltd. Fuel cell system using natural gas
US11139497B2 (en) * 2013-12-31 2021-10-05 Doosan Heavy Industries & Construction Co., Ltd. Fuel cell system using natural gas
WO2018213507A1 (en) * 2017-05-16 2018-11-22 Ebert Terrence J Apparatus and process for liquefying gases
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

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DE2044363C2 (de) 1982-07-29
GB1329861A (en) 1973-09-12
FR2060184A1 (enrdf_load_stackoverflow) 1971-06-18
CA947636A (en) 1974-05-21
JPS501359B1 (enrdf_load_stackoverflow) 1975-01-17
FR2060184B1 (enrdf_load_stackoverflow) 1973-11-16
DE2044363A1 (de) 1971-04-15
ES383502A1 (es) 1972-12-16

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