AU2011221424A1 - Natural gas liquefaction - Google Patents
Natural gas liquefaction Download PDFInfo
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- AU2011221424A1 AU2011221424A1 AU2011221424A AU2011221424A AU2011221424A1 AU 2011221424 A1 AU2011221424 A1 AU 2011221424A1 AU 2011221424 A AU2011221424 A AU 2011221424A AU 2011221424 A AU2011221424 A AU 2011221424A AU 2011221424 A1 AU2011221424 A1 AU 2011221424A1
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- Prior art keywords
- feed fraction
- nitrogen
- liquefied
- heat
- exchange process
- Prior art date
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 239000003345 natural gas Substances 0.000 title claims abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 112
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 56
- 238000000034 method Methods 0.000 claims abstract description 47
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 13
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 13
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 238000005057 refrigeration Methods 0.000 claims abstract description 5
- 238000009835 boiling Methods 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 239000007789 gas Substances 0.000 description 9
- 239000003507 refrigerant Substances 0.000 description 5
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 2
- 230000035882 stress Effects 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
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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
- F25J1/0002—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
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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
- F25J1/003—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
- F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
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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
- F25J1/003—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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- 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
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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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
- F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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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
- F25J1/0221—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 the cold stored in an external cryogenic component in an open refrigeration loop
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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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
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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
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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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.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
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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
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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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)
Abstract
Abstract Natural qas liquefaction A method is described for liquefying a hydrocarbon-rich feed fraction, preferably natural gas, against a nitrogen refrigeration cycle, wherein the feed fraction is cooled against 5 gaseous nitrogen that is to be warmed and the feed fraction is liquefied against liquid nitrogen that is to be vaporized. According to the invention - the feed fraction is cooled and liquefied in an at least three-stage heat-exchange 10 process (E1a - E1c), - wherein, in the first section of the heat-exchange process (E1a), the feed fraction (1) is cooled against superheated gaseous nitrogen (9) to the extent that an essentially complete separation (D2) of the relatively heavy components (2') is achievable, 15 - in the second section of the heat-exchange process (E1b), the feed fraction (2) freed from relatively heavy components is partially liquefied against gaseous nitrogen that is to be superheated (9), and - in the third section of the heat-exchange process (Elc), the feed fraction (2) is liquefied against nitrogen that is to be partially vaporized (8). co, w j. c o' 1~ (N w - (N) 0)0 (4D0
Description
- 1 AUSTRALIA PATENTS ACT 1990 COMPLETE SPECIFICATION FOR A STANDARD PATENT ORIGINAL Name of Applicant: Linde Aktiengesellschaft Actual Inventor: Heinz Bauer Address for Service is: SHELSTON IP 60 Margaret Street Telephone No: (02) 9777 1111 SYDNEY NSW 2000 Facsimile No. (02) 9241 4666 CCN: 3710000352 Attorney Code: SW Invention Title: Natural gas liquefaction The following statement is a full description of this invention, including the best method of performing it known to me/us: File: 71446AUP00 2 Description Natural qas liquefaction The invention relates to a method for liquefying a hydrocarbon-rich feed fraction, preferably natural gas, against a nitrogen refrigeration cycle, wherein the feed fraction 5 is cooled against gaseous nitrogen that is to be warmed and the feed fraction is liquefied against liquid nitrogen that is to be vaporized. Hydrocarbon-rich gases, in particular natural gases, are liquefied commercially in a capacity range from 10 to 30 000 tonnes of LNG per day (tato). In plants of medium 10 capacity - this is taken to mean liquefaction processes having a capacity between 300 and 3000 tato of LNG - and large capacity - this is taken to mean liquefaction processes having a capacity between 3000 and 30 000 tato of LNG - those skilled in the art attempt to optimize the operating costs by means of high efficiency. In contrast, in the case of smaller plants - this is taken to mean liquefaction processes having a 15 capacity between 10 and 300 tato of LNG - low capital costs are in the foreground. In such plants, the capital cost proportion of a dedicated refrigeration plant in which the working medium used is, for example, nitrogen or a nitrogen-hydrocarbon mixture, is considerable. Therefore, generation of cold in the liquefaction plant is if possible dispensed with and a suitable refrigerant imported. Customarily, in this case, liquid 20 nitrogen is used and after its use as refrigerant, is given off to the atmosphere in the gaseous state. If in nearby air separation plants unused product amounts of liquid nitrogen can be provided inexpensively, this concept for small liquefaction plants is absolutely commercially expedient. 25 For reasons of costs, in small liquid-nitrogen-cooled plants, brazed aluminium plate heat exchangers are generally used. These appliances, however, are sensitive to high thermal stresses such as can arise, for example, by an oversupply of refrigerant and/or large temperature differences between warm and cold process streams. The resultant mechanical stresses can lead to damage to these appliances. 30 In addition, care must be taken to ensure that, during operation of the liquefaction process, the feed fraction does not fall below the freezing temperature. The solid point of methane at -182*C is markedly above the atmospheric boiling temperature of 3 nitrogen, which is -196*C. Freezing of the plant always causes an unwanted operating fault and can in addition have lasting damage as a consequence. A method of the type in question for liquefying a hydrocarbon-rich feed fraction is 5 known from US patent 5,390,499. This method is suitable, in particular, for plants of small capacity, as explained at the outset. In the liquefaction method described in US patent 5,390,499, the gas that is to be liquefied is cooled and liquefied against nitrogen in two separate heat exchangers. In this case the liquid low-boiling nitrogen is completely vaporized in the second heat exchanger and warmed up to a temperature 10 at which relatively heavy crude gas components can be taken off in the liquid state by means of a separator from the gas that is to be liquefied. In a process procedure as described in US patent 5,390,499, however, the point at which the nitrogen vaporizes completely can vary considerably according to load. This can lead to unwanted process conditions which have the abovementioned disadvantages as a consequence. 15 Any discussion of the prior art throughout the specification should in no way be considered as an admission that such prior art is widely known or forms part of common general knowledge in the field. 20 It is an object of the present invention to overcome or ameliorate at least one of the disadvantages of the prior art, or to provide a useful alternative. In a broad aspect, the present invention provides, a method for liquefying a hydrocarbon-rich feed fraction, wherein 25 - the feed fraction is cooled and liquefied in an at least three-stage heat-exchange process, - wherein, in the first section of the heat-exchange process, the feed fraction is cooled against superheated gaseous nitrogen to the extent that an essentially complete separation of the relatively heavy components is achievable, 30 - in the second section of the heat-exchange process, the feed fraction freed from relatively heavy components is partially liquefied against gaseous nitrogen that is to be superheated, and - in the third section of the heat-exchange process, the feed fraction is liquefied against nitrogen that is to be partially vaporized. 35 4 The expression "heavy components" may be taken to mean hereinafter hydrocarbons from ethane. Further advantageous embodiments of the method according to the invention for 5 liquefying a hydrocarbon-rich feed fraction include - the three-stage heat-exchange process is achieved in one or more heat exchangers, 10 - the condensation pressure of the feed fraction freed from relatively heavy components is adjusted to values between 1 and 15 bara, preferably between 1 and 8 bara, and - the boiling pressure of the gaseous nitrogen that is to be superheated is 15 adjusted to values between 5 and 30 bara, preferably between 10 and 20 bara. The method according to the invention for liquefying a hydrocarbon-rich feed fraction and other advantageous embodiments of the same may be described in more detail hereinafter with reference to the exemplary embodiment shown in the figure. 20 The hydrocarbon-rich feed fraction that is to be liquefied is fed via line 1 to a heat exchanger El. This is subdivided into three sections or stages a to c. The boundaries between these sections or stages are shown by the two dashed lines. In the warmest section a of the heat exchanger El, the hydrocarbon-rich feed fraction is cooled 25 against superheated gaseous nitrogen which is fed via line 9 to the heat exchanger El to the extent that a separation of the heavy components from the feed fraction is possible in a separator D2 downstream of the heat exchanger El. For this purpose, the cooled feed fraction is fed from the heat exchanger El via line 1' to the separator D2. From the bottom phase thereof, via line 2', in which a valve V1 is provided, the 30 unwanted heavy components are taken off in liquid form and released from the process. Instead of the separator D2 shown in the figure, a rectification column can be used to achieve a more precise separation of relatively heavy components or higher 35 hydrocarbons from the feed fraction.
5 At the top of the separator D2, via line 2, the feed fraction that is freed from heavy components is taken off and fed to the second section b of the heat exchanger El. Therein, the feed fraction that is freed from heavy components is partially liquefied 5 against gaseous nitrogen that is to be superheated 9. Then, in the third stage c of the heat exchanger El, the feed fraction is completely liquefied against nitrogen to be partially vaporized which is fed to the heat exchanger El via the line 8. The liquefied feed fraction, after passage through the heat exchanger El via line 3, in 10 which a control valve V3 is arranged, is fed to a storage vessel D4. The liquefied product (LNG) can be discharged therefrom via line 4. The control valve V3 serves for expanding the liquefied feed fraction to the product delivery pressure, which corresponds at least approximately to atmospheric pressure. 15 If the nitrogen is vaporized in the third section c of the heat exchanger El at a pressure of greater than 15 bara, the boiling temperature thereof is no longer low enough in order to subcool the liquefied feed fraction to the extent that outgassing after expansion thereof in the control valve V3 can be prevented. In this case, the boil-off gas formed in the storage vessel D4 is advantageously taken off via line 5, compressed in the 20 compressor C3 and fed back to the feed fraction 2 which is freed from heavy components before liquefaction thereof and re-liquefied in the heat exchanger El. This process procedure should be selected, in particular, in the case of significant temporary storage of the LNG product in an atmospheric flat-bottom tank D4, since the resultant boil-off gas is also processed thereby. 25 The nitrogen required for providing cold is fed to the liquefaction process via line 6. Advantageously, a buffer tank D3 is provided which serves for compensating for quantitative fluctuations of the feed fraction that is to be liquefied and/or of the refrigerant nitrogen. By means of a pump P1, liquid nitrogen is fed in the amount 30 required to a separator D1 via line 7. From the bottom phase of the separator D1, boiling nitrogen is taken off and conducted via line 8 through the coldest section c of the heat exchanger El. The nitrogen that is partially vaporized in this case is then fed via line 8' back to the separator D1.
6 If the reliquefaction process that is still to be described is operated, at least temporarily the generation of cold by the reliquefaction of the nitrogen can exceed the refrigeration requirement of the natural gas liquefaction. An oversupply resulting therefrom of liquid nitrogen can be delivered into the buffer tank D3 via line 8" and valve V6. 5 At the top of the separator D1, gaseous nitrogen is taken off via line 9 and fed to the middle section b of the heat exchanger El. The gaseous nitrogen is conducted through the second and first sections of the heat exchanger El in countercurrent flow to the feed fraction 2 that is to be cooled and partially liquefied, and is warmed and 10 superheated in this process. The superheated nitrogen is then taken off from the process via the line sections 10 and 11. By means of the control valve V4, the boiling pressure of the gaseous nitrogen that is to be superheated 9 can be controlled. Advantageously, this boiling pressure is 15 adjusted to values between 5 and 30 bara, preferably between 10 and 20 bara. Similarly, the condensation pressure of the feed fraction 2 that is freed from relatively heavy components can be controlled by means of the control valve V2. This condensation pressure is preferably adjusted to values between 1 and 15 bara, 20 preferably between 1 and 8 bara. By means of the control valves V2 and/or V4, the temperature profile in the third section c of the heat exchanger El can be controlled thereby. Whereas, by means of the control valve V2, the condensation pressure of the feed fraction is established in 25 the section between the control valves V2 and V3, by means of the control valve V4, the boiling pressure of the nitrogen in the separator D1 and the third section c of the heat exchanger El is controlled. Owing to the above-described subdivision of the heat exchange process into a second and third section and with the phase separation in separator D1 it can then be established exactly in what section of the heat exchanger 30 El a (partial) vaporization or superheating of the nitrogen is taking place. By means of the subdivision of the heat-exchange process El into three sections a to c, it is possible to reliably prevent the phase boundary between liquid and gaseous refrigerant from migrating within the heat exchanger El and thereby causing unwanted 35 thermal and mechanical stresses within the heat exchanger El.
7 If the nitrogen boiling pressure (pN 2 ) and the crude gas condensation pressure (pRG) are selected according to the inequality pRG (bara) 0.3 pN 2 (bara) -1, a thermal overload of the heat exchanger El due to impermissibly high temperature differences can be safely avoided. 5 By restricting the boiling pressure of the liquid nitrogen in the third section c of the heat exchanger El and of the separator D1 to at least 5 bara - the associated boiling temperature is -179*C - it is possible to prevent reliably a temperature below the freezing temperature of methane occurring in the heat exchanger El. Operating 10 problems and possible damage due to solids formation are thereby excluded. The superheated nitrogen taken off from the heat exchanger El via line 10 can, alternatively to a removal via line 11, be at least partially reliquefied. For this purpose the nitrogen is fed via the line sections 12 and 13 to a compression - shown in the 15 figure by a two-stage compressor unit C1/C2, wherein a heat exchanger, E3 or E4 respectively, is connected downstream of each compressor unit - and then is fed via line 14 to a heat exchanger E2. Therein, the nitrogen is reliquefied and then fed to separator D1 via line 15. Pressure regulation of the compressor C2 is performed by the control valve V5. For the purpose of providing cold in the heat exchanger E2, via line 20 16 a substream of the compressed nitrogen stream is taken off, preferably expanded in a multistage manner - shown by the gas expanders X1 and X2 - and then conducted via line 17 through the heat exchanger E2 in countercurrent flow to the nitrogen stream that is to be liquefied. The shafts of the compressors C1 and C2 are preferably coupled to the shafts of the gas expanders X2 and X1. 25 If the above-described reliquefaction process is operated, it is advantageous to feed to the heat exchanger El via line 9 only the amount of gaseous nitrogen that is required for a small positive temperature difference of approximately 3*C between streams 1 and 10 at the warm end of the heat exchanger El. The excess amount of cold gaseous 30 nitrogen is used via line 9' proportionately for reliquefaction in the heat exchanger E2. In principle, the liquefaction process can proceed by means of "imported" nitrogen - in this case, the superheated nitrogen is taken off from the heat exchanger El via the line sections 10 and 11 - by means of reliquefied nitrogen, or by any desired combination 35 of both modes of operation.
Claims (5)
1. Method for liquefying a hydrocarbon-rich feed fraction, preferably natural gas, against a nitrogen refrigeration cycle, wherein the feed fraction is cooled against gaseous nitrogen that is to be warmed and the feed fraction is liquefied against 5 liquid nitrogen that is to be vaporized, wherein - the feed fraction is cooled and liquefied in an at least three-stage heat exchange process - wherein, in the first section of the heat-exchange process, the feed fraction is cooled against superheated gaseous nitrogen to the extent that an essentially 10 complete separation of the relatively heavy components is achievable, - in the second section of the heat-exchange process, the feed fraction freed from relatively heavy components is partially liquefied against gaseous nitrogen that is to be superheated, and - in the third section of the heat-exchange process, the feed fraction is liquefied 15 against nitrogen that is to be partially vaporized.
2. Method according to Claim 1, wherein the three-stage heat-exchange process is achieved in one or more heat exchangers. 20
3. Method according to Claim 1 or 2, wherein the condensation pressure of the feed fraction freed from relatively heavy components is adjusted to values between 1 and 15 bara, preferably between 1 and 8 bara.
4. Method according to any one of the preceding Claims 1 to 3, wherein the boiling 25 pressure of the gaseous nitrogen that is to be superheated is adjusted to values between 5 and 30 bara, preferably between 10 and 20 bara.
5. Method for liquefying a hydrocarbon-rich feed fraction substantially as herein described with reference to any one of the embodiments of the invention illustrated in 30 the accompanying drawing and/or examples.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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DE102010044869A DE102010044869A1 (en) | 2010-09-09 | 2010-09-09 | Liquefied Natural gas |
DE102010044869.9 | 2010-09-09 |
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AU2011221424A1 true AU2011221424A1 (en) | 2012-03-29 |
AU2011221424B2 AU2011221424B2 (en) | 2016-03-31 |
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AU2011221424A Active AU2011221424B2 (en) | 2010-09-09 | 2011-09-09 | Natural gas liquefaction |
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US (1) | US20120060553A1 (en) |
CN (1) | CN102410702B (en) |
AR (1) | AR082919A1 (en) |
AU (1) | AU2011221424B2 (en) |
BR (1) | BRPI1104609A2 (en) |
CH (1) | CH703773B1 (en) |
DE (1) | DE102010044869A1 (en) |
NO (1) | NO20111212A1 (en) |
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DE102011115987B4 (en) | 2011-10-14 | 2019-05-23 | Linde Aktiengesellschaft | Liquefied Natural gas |
US20140157824A1 (en) * | 2012-12-06 | 2014-06-12 | L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Method for improved thermal performing refrigeration cycle |
EP2899116A3 (en) * | 2014-01-22 | 2015-11-25 | Meyer Werft GmbH & Co. KG | Method and tank assembly for the reliquefaction and cooling of liquid natural gas in tank systems |
FR3021091B1 (en) | 2014-05-14 | 2017-09-15 | Ereie - Energy Res Innovation Eng | METHOD AND DEVICE FOR LIQUEFACTING METHANE |
JP6527714B2 (en) * | 2015-02-25 | 2019-06-05 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Liquid fuel gas supply apparatus and supply method |
CN104877724A (en) * | 2015-05-11 | 2015-09-02 | 四川捷贝通能源科技有限公司 | Treatment method for recovering vent natural gas |
FR3045798A1 (en) * | 2015-12-17 | 2017-06-23 | Engie | HYBRID PROCESS FOR THE LIQUEFACTION OF A COMBUSTIBLE GAS AND INSTALLATION FOR ITS IMPLEMENTATION |
US10634425B2 (en) * | 2016-08-05 | 2020-04-28 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Integration of industrial gas site with liquid hydrogen production |
US10393431B2 (en) * | 2016-08-05 | 2019-08-27 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for the integration of liquefied natural gas and syngas production |
US11402151B2 (en) * | 2017-02-24 | 2022-08-02 | Praxair Technology, Inc. | Liquid natural gas liquefier utilizing mechanical and liquid nitrogen refrigeration |
TWI712769B (en) * | 2017-11-21 | 2020-12-11 | 法商液態空氣喬治斯克勞帝方法研究開發股份有限公司 | Bog recondenser and lng supply system provided with same |
JP7026490B2 (en) * | 2017-11-21 | 2022-02-28 | レール・リキード-ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | A BOG recondensing device and an LNG storage system equipped with the BOG recondensing device. |
FR3079923B1 (en) * | 2018-04-05 | 2020-05-29 | Waga Energy | PROCESS FOR LIQUEFACTION OF METHANE GAS BY VAPORIZATION OF NITROGEN, PLANT FOR LIQUEFACTION OF METHANE GAS USING THE PROCESS |
FR3084453B1 (en) * | 2018-07-25 | 2020-11-27 | Air Liquide | METHOD AND APPARATUS FOR THE CRYOGENIC SEPARATION OF A MIXTURE OF CARBON MONOXIDE, HYDROGEN AND METHANE FOR THE PRODUCTION OF CH4 |
US11465093B2 (en) | 2019-08-19 | 2022-10-11 | Exxonmobil Upstream Research Company | Compliant composite heat exchangers |
US20210063083A1 (en) | 2019-08-29 | 2021-03-04 | Exxonmobil Upstream Research Company | Liquefaction of Production Gas |
US11083994B2 (en) | 2019-09-20 | 2021-08-10 | Exxonmobil Upstream Research Company | Removal of acid gases from a gas stream, with O2 enrichment for acid gas capture and sequestration |
US11808411B2 (en) | 2019-09-24 | 2023-11-07 | ExxonMobil Technology and Engineering Company | Cargo stripping features for dual-purpose cryogenic tanks on ships or floating storage units for LNG and liquid nitrogen |
US11703277B2 (en) * | 2020-02-06 | 2023-07-18 | Cosmodyne, LLC | Systems and methods for natural gas cooling |
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US5390499A (en) | 1993-10-27 | 1995-02-21 | Liquid Carbonic Corporation | Process to increase natural gas methane content |
FR2725503B1 (en) * | 1994-10-05 | 1996-12-27 | Inst Francais Du Petrole | NATURAL GAS LIQUEFACTION PROCESS AND INSTALLATION |
DE4440401A1 (en) * | 1994-11-11 | 1996-05-15 | Linde Ag | Process for liquefying natural gas |
EP0723125B1 (en) * | 1994-12-09 | 2001-10-24 | Kabushiki Kaisha Kobe Seiko Sho | Gas liquefying method and plant |
FR2743140B1 (en) * | 1995-12-28 | 1998-01-23 | Inst Francais Du Petrole | METHOD AND DEVICE FOR TWO-STEP LIQUEFACTION OF A GAS MIXTURE SUCH AS A NATURAL GAS |
DE19612173C1 (en) * | 1996-03-27 | 1997-05-28 | Linde Ag | Procedure for liquefaction of hydrocarbon rich process flow, especially natural gas |
NO328493B1 (en) * | 2007-12-06 | 2010-03-01 | Kanfa Aragon As | System and method for regulating the cooling process |
-
2010
- 2010-09-09 DE DE102010044869A patent/DE102010044869A1/en active Pending
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2011
- 2011-09-06 CN CN201110294097.8A patent/CN102410702B/en not_active Expired - Fee Related
- 2011-09-07 CH CH01475/11A patent/CH703773B1/en unknown
- 2011-09-07 NO NO20111212A patent/NO20111212A1/en not_active Application Discontinuation
- 2011-09-07 US US13/226,633 patent/US20120060553A1/en not_active Abandoned
- 2011-09-07 AR ARP110103264A patent/AR082919A1/en active IP Right Grant
- 2011-09-08 BR BRPI1104609-0A patent/BRPI1104609A2/en not_active Application Discontinuation
- 2011-09-09 AU AU2011221424A patent/AU2011221424B2/en active Active
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CN102410702A (en) | 2012-04-11 |
BRPI1104609A2 (en) | 2013-04-24 |
CN102410702B (en) | 2016-01-20 |
CH703773A2 (en) | 2012-03-15 |
US20120060553A1 (en) | 2012-03-15 |
CH703773B1 (en) | 2015-02-27 |
AR082919A1 (en) | 2013-01-16 |
DE102010044869A1 (en) | 2012-03-15 |
AU2011221424B2 (en) | 2016-03-31 |
NO20111212A1 (en) | 2012-03-12 |
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