KR101637334B1 - Method and apparatus for liquefying natural gas - Google Patents
Method and apparatus for liquefying natural gas Download PDFInfo
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- KR101637334B1 KR101637334B1 KR1020100040584A KR20100040584A KR101637334B1 KR 101637334 B1 KR101637334 B1 KR 101637334B1 KR 1020100040584 A KR1020100040584 A KR 1020100040584A KR 20100040584 A KR20100040584 A KR 20100040584A KR 101637334 B1 KR101637334 B1 KR 101637334B1
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- refrigerant
- heat exchanger
- natural gas
- low temperature
- temperature heat
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 330
- 239000003345 natural gas Substances 0.000 title claims abstract description 160
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000003507 refrigerant Substances 0.000 claims abstract description 243
- 238000007667 floating Methods 0.000 claims abstract description 35
- 239000007789 gas Substances 0.000 claims abstract description 34
- 238000001816 cooling Methods 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims description 42
- 239000003949 liquefied natural gas Substances 0.000 claims description 32
- 230000006835 compression Effects 0.000 claims description 23
- 238000007906 compression Methods 0.000 claims description 23
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- 239000002826 coolant Substances 0.000 claims description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 10
- 239000007791 liquid phase Substances 0.000 description 10
- 239000012071 phase Substances 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000001273 butane Substances 0.000 description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 5
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 5
- 239000001294 propane Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000005856 abnormality Effects 0.000 description 1
- 239000002253 acid 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
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- -1 that is Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Images
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
- F25J1/02—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
- F25J1/0258—Construction and layout of liquefaction equipments, e.g. valves, machines vertical layout of the equipments within in the cold box
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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
- F25J1/0052—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
- F25J1/003—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
- F25J1/0055—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 originating from an incorporated cascade
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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
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR 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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
- F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
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- 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
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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
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
- F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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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.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
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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.
- F25J1/0294—Multiple compressor casings/strings in parallel, e.g. split arrangement
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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
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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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
Abstract
The present invention separates a large heat exchanger installed for liquefying natural gas into a low-temperature heat exchanger and a cryogenic heat exchanger so as to be suitable for a marine environment, so that it is suitable for being mounted on a floating structure used floating in the sea, ≪ / RTI >
According to the present invention, there is provided a natural gas liquefying apparatus for liquefying natural gas by heat exchange with a refrigerant in a heat exchanging means, wherein the heat exchanging means comprises a low temperature heat exchanger for cooling the natural gas extracted from the gas chill to low temperature, And a cryogenic heat exchanger for further cooling and liquefying the cooled natural gas, wherein the low-temperature heat exchanger and the cryogenic heat exchanger are arranged in a horizontal direction to reduce the height of the heat exchanging means. Method is provided.
Description
The present invention relates to a method and an apparatus for liquefying natural gas, and more particularly, to a method and apparatus for liquefying natural gas by separating a large-sized heat exchanger installed for natural gas liquefaction into a low-temperature heat exchanger and an ultra- To a method and apparatus for natural gas liquefaction adapted to be mounted on and used on a floating structure.
Natural gas is transported in a gaseous state through land or sea gas pipelines, or is transported to a remote location where it is stored in an LNG carrier in the form of liquefied natural gas (LNG). Liquefied natural gas is obtained by cooling the natural gas at a cryogenic temperature, and its volume is reduced to approximately 1/600 of that of the natural gas, making it very suitable for long distance transportation through the sea.
A conventionally used method of liquefying natural gas is by passing natural gas through a heat exchanger and cooling it. U.S. Patent Nos. 3,735,600 and 3,433,026 disclose a liquefaction method in which natural gas is supplied to a heat exchanger for liquefaction.
In this specification, natural gas means a mixture containing methane as the main component but containing other hydrocarbon components or nitrogen, and also includes any type (gas phase, liquid phase, or mixed phase of gas phase and liquid phase) .
In order to store and transport natural gas in a liquid state, the natural gas must be cooled to about -151 캜 to -163 캜, where the LNG has a pressure of about atmospheric pressure. In the prior art, methods such as a cascade process, a mixed refrigerant process, a refrigerant gas expander process and the like have been used for the cooling of natural gas in a liquefaction facility on the land.
Floating structures such as LNG FPSO (Floating, Production, Storage and Offloading), which can directly produce and store natural gas directly from raw natural gas extracted from gas fired offshore, have been proposed recently, There has been a demand for a liquefaction apparatus for natural gas.
The method of liquefaction of natural gas on land can not be applied to floating structures in the sea as it is, and needs to be improved to suit the marine environment. In the case of LNG FPSO, small- and medium-scale liquefaction facilities are highly feasible, and gas refrigerant expansion processes and mixed refrigerant processes are attracting attention as a liquefaction process suitable for this.
However, heat exchangers such as BAHX (Brazed Aluminum Heat Exchanger) or SWHE (Spiral Wound Heat Exchanger) are used for such a liquefaction facility. In particular, SWHE is expensive and high in height (for example, approximately 50 m) There is a possibility that a safety problem may occur.
In order to solve these problems, the present invention is characterized in that, instead of installing a single large heat exchanger in a floating structure for liquefying natural gas, a relatively low-temperature low-temperature heat exchanger and a cryogenic heat exchanger are installed, It is an object of the present invention to provide a method and apparatus for liquefying natural gas which can minimize the influence due to fluctuations in the sea and efficiently perform a liquefaction process by constituting a refrigerant circuit for circulating refrigerant in a single circuit .
According to an aspect of the present invention, there is provided a natural gas liquefying apparatus for liquefying natural gas by heat exchange with a coolant in a heat exchange unit, wherein the heat exchange unit comprises a low temperature heat exchanger for cooling the natural gas extracted from the gas chill to a low temperature And a cryogenic heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger, wherein the low temperature heat exchanger and the ultra low temperature heat exchanger are arranged in a horizontal direction to reduce the height of the heat exchanging means A natural gas liquefaction apparatus is provided.
Preferably, the natural gas liquefier includes a refrigerant circuit composed of a single circuit for sequentially liquefying natural gas by circulating the refrigerant through the low-temperature heat exchanger and the cryogenic heat exchanger.
Wherein the natural gas liquefier comprises a cold separator for separating natural gas cooled at a low temperature in the low temperature heat exchanger into natural gas in a gaseous state and natural gas in a liquid state and supplying natural gas in a gaseous state to the cryogenic heat exchanger .
It is preferable that the natural gas liquefier includes means for separating the liquid natural gas separated by the cold separator by the component.
The refrigerant heated by the natural gas in the cryogenic heat exchanger is preferably supplied to the low temperature heat exchanger and precool the natural gas before being supplied to the cryogenic heat exchanger.
The refrigerant heated by the natural gas in the cryogenic heat exchanger is separated into a gaseous refrigerant and a liquid refrigerant through the gas-liquid separator and is supplied to the low-temperature heat exchanger.
Preferably, a plurality of the low-temperature heat exchangers are provided, and the gaseous refrigerant separated through the gas-liquid separator and the liquid-state refrigerant are supplied to a plurality of the low-temperature heat exchangers through separate supply lines.
It is preferable to have at least one compression unit including a refrigerant compressor for compressing the refrigerant that cools the natural gas through heat exchange with the natural gas and a refrigerant condenser for condensing the compressed refrigerant.
The refrigerant supplied to the low temperature heat exchanger in the compression unit is separated and supplied to the gaseous refrigerant and the liquid refrigerant through the discharge separator.
The natural gas liquefaction apparatus may further include a refrigerant compressor for compressing the refrigerant and a refrigerant condenser for condensing the compressed refrigerant, wherein the refrigerant compressor is a multi-stage compressor.
The refrigerant supplied to the low temperature heat exchanger may include a first refrigerant supply line for supplying the liquid refrigerant separated by the intermediate separator in the partially condensed refrigerant cooled by the intermediate cooler included in the refrigerant compressor to the low temperature heat exchanger , A gaseous refrigerant separated by the intermediate separator is compressed again by the refrigerant compressor and is partially condensed by the refrigerant condenser, and a second refrigerant for supplying the liquid refrigerant separated from the discharge separator to the low temperature heat exchanger And a third refrigerant supply line for supplying the gaseous refrigerant separated from the discharge separator to the low temperature heat exchanger.
The refrigerant supplied to the low temperature heat exchanger through the third refrigerant supply line is cooled and partially condensed by the refrigerant returning from the cryogenic temperature heat exchanger and is separated into a gaseous refrigerant and a liquid refrigerant by the first refrigerant separator Respectively, and then the natural gas is cooled in the cryogenic heat exchanger.
Preferably, the refrigerant supplied to the low-temperature heat exchanger through the first and second refrigerant supply lines is expanded and then supplied to the low-temperature heat exchanger to cool the natural gas.
The expanded refrigerant is mixed with the refrigerant supplied to the low temperature heat exchanger in the cryogenic heat exchanger, and returned to the low temperature heat exchanger to cool the natural gas.
According to another aspect of the present invention, there is provided a natural gas liquefaction apparatus for liquefying natural gas by exchanging natural gas with a refrigerant on a floating structure used floating on the sea, wherein the natural gas liquefying apparatus installed on the upper deck of the floating structure, A low temperature heat exchanger for cooling the natural gas to a low temperature; A cryogenic heat exchanger disposed on an upper deck of the floating structure and horizontally disposed in the low temperature heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger; A refrigerant circuit for sequentially liquefying the natural gas by circulating the refrigerant through the low temperature heat exchanger and the cryogenic heat exchanger; A natural gas liquefaction apparatus is provided.
And a NGL facility for separating the heavy hydrocarbon component from the partially condensed natural gas cooled in the low temperature heat exchanger.
Preferably, the refrigerant circuit includes a plurality of compressors including a refrigerant compressor and a refrigerant condenser.
Preferably, the low temperature heat exchanger is a Plate Fin Heat Exchanger (PFHE) type heat exchanger, and the cryogenic heat exchanger is a SWHE (Spiral Wound Heat Exchanger) type heat exchanger.
According to another aspect of the present invention, there is provided a floating structure used floating in a sea, comprising: a low-temperature heat exchanger installed on an upper deck of the floating structure for cooling natural gas extracted from a gas- A cryogenic heat exchanger disposed on an upper deck of the floating structure and horizontally disposed in the low temperature heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger; A refrigerant circuit for sequentially liquefying the natural gas by circulating the refrigerant through the low temperature heat exchanger and the cryogenic heat exchanger; And a natural gas liquefaction apparatus including the natural gas liquefaction apparatus.
The floating structure is preferably LNG FPSO.
According to another aspect of the present invention, there is provided a natural gas liquefaction method for liquefying natural gas by heat exchange with a refrigerant in a heat exchange unit, comprising: a low temperature heat exchanger for cooling natural gas extracted from a gas chill to a low temperature; Temperature heat exchanger, the refrigerant passing through the low-temperature heat exchanger and the refrigerant passing through the ultra-low temperature heat exchanger is circulated through a single refrigerant circuit A natural gas liquefaction method is provided.
In accordance with the present invention as described above, it is possible to provide a low-temperature heat exchanger and a cryogenic heat exchanger, which are relatively small in size, instead of installing a single large heat exchanger in a floating structure for liquefying natural gas, and provide a low-temperature heat exchanger and a cryogenic heat exchanger A natural gas liquefaction method and apparatus in which a refrigerant circuit for circulating refrigerant for delivery is constituted by a single circuit can be provided.
Accordingly, the present invention can provide a natural gas liquefaction method and apparatus which can minimize the influence due to fluctuations in the sea, efficiently perform the liquefaction process, and is suitable for use in a floating structure.
1 is a conceptual view of a floating structure in which a natural gas liquefaction apparatus according to the present invention is installed, and
2 is a conceptual diagram for explaining a natural gas liquefaction apparatus according to the present invention.
Hereinafter, a method and apparatus for liquefying natural gas according to a preferred embodiment of the present invention will be described in detail with reference to the drawings.
The natural gas liquefaction apparatus according to the present invention can be installed in a marine structure such as LNG plant, LNG carrier, and LNG FPSO (Floating, Production, Storage and Offloading) installed on land or in the sea. LNG FPSO is a floating marine structure that is used to liquefy natural gas produced directly from the sea and store it in the LNG storage tank and to transfer the LNG stored in the LNG storage tank to the LNG transport if necessary.
As shown in FIG. 1, the natural gas liquefaction apparatus 1 according to the present invention for liquefying natural gas extracted from a gas chest provided in a floating structure 2, is extracted from a gas chest, A low-temperature heat exchanger 3 for cooling natural gas from which impurities such as carbon dioxide and acid gas have been removed, a cryogenic heat exchanger 4 for liquefying natural gas cooled at a low temperature in the low-temperature heat exchanger 3, , And a refrigerant circuit (5) for supplying compressed and condensed refrigerant to the low temperature heat exchanger (3) and the cryogenic heat exchanger (4) to exchange heat with the natural gas to liquefy the natural gas.
According to the present invention, as the refrigerant circulated in the refrigerant circuit (5), a mixed refrigerant in which components such as methane, ethanol, propane, butane, and nitrogen are mixed at a certain ratio may be used. The mixing ratio of each component can be determined according to the process conditions.
As described above, according to the natural gas liquefier 1 of the present invention, by using a plurality of heat exchangers, that is, the low temperature heat exchanger 3 and the cryogenic heat exchanger 4 in series, The size, especially the height, of the heat exchanger can be reduced as compared to heat exchangers such as the widely used Spiral Wound Heat Exchanger (SWHE). Accordingly, it is possible to minimize the influence of the movement of the floating structure and improve the liquefaction efficiency in the marine environment in which the shaking motion occurs, and to minimize the use of the supporting member required for installing the heat exchanger.
2, a method and apparatus for liquefying natural gas according to an embodiment of the present invention will be described in more detail.
As described above with reference to Fig. 1, the natural gas liquefaction apparatus of the present invention comprises: a low-temperature heat exchanger 3 for primarily pre-cooling natural gas; and a natural low-temperature heat exchanger And a refrigerant circuit (5) for liquefying natural gas by supplying refrigerant to the low temperature heat exchanger (3) and the cryogenic temperature exchanger (4) and exchanging heat with the natural gas, .
The liquefaction process of natural gas can be carried out as follows.
The natural gas that has been subjected to a pretreatment process such as the removal of impurities after being extracted from the gas well is supplied to the low temperature heat exchanger 3 through the natural gas supply line L11 and heat exchanged with the refrigerant in the low temperature heat exchanger 3 And is subsequently cooled. The natural gas cooled in the low temperature heat exchanger 3 can be cooled to about -50 to 60 캜 and can be partially condensed.
The primarily cooled natural gas is supplied to the cryogenic heat exchanger 4 through the natural gas supply line L11 and is secondarily cooled through heat exchange with the refrigerant in the cryogenic heat exchanger 4. [ The natural gas cooled in the cryogenic heat exchanger 4 can be mostly condensed and the liquid natural gas, that is, liquefied natural gas (LNG), is supplied through the
According to a modified embodiment of the present invention, the natural gas delivered from the low-temperature heat exchanger 3 to the cryogenic heat exchanger 4 is separated from the
Natural gas contains hydrocarbon components such as methane, ethane, propane, and butane. Methane, ethane, etc., which have relatively high liquefaction point and relatively low carbon number, are relatively low in liquid hydrocarbon such as butane and propane. Accordingly, the natural gas of the gas phase classified by the
The liquid natural gas classified from the
The circulation process of the refrigerant can be performed as follows.
The refrigerant compressed in the
According to the present invention, one or more compression units provided with a
Since the configuration of the
When the refrigerant compressor (21) is driven, the refrigerant contained in the suction drum (23) provided on the upstream side of the refrigerant compressor (21) is supplied to the refrigerant compressor (21) and compressed. Since the refrigerant compressor is composed of multiple stages, the refrigerant compressed at the intermediate pressure in the primary compression stage is cooled in the intermediate refrigerator (24) and then compressed to the high pressure in the secondary compression stage.
In the
On the other hand, the refrigerant of the gaseous component compressed at the high pressure in the secondary compression step is lowered in the refrigerant condenser 26 (hereinafter also referred to as an aftercooler) so that the hydrocarbon component can be partially condensed and a partially condensed refrigerant The liquid component is separated into the gas phase and the liquid phase again in the
Here, in each compression zone, the respective refrigerant distributions separated in the same step are joined together before being supplied to the low temperature heat exchanger 3.
The refrigerant supplied to the low-temperature heat exchanger 3 through the first refrigerant supply line L21 and the second refrigerant supply line L22 flows through the low-temperature heat exchanger 3 and then flows through the
On the other hand, the refrigerant fraction supplied to the low-temperature heat exchanger 3 through the third refrigerant supply line L23 is separated into the gas phase and the liquid phase in the first
The liquid-phase refrigerant supplied to the cryogenic temperature heat exchanger 4 through the fourth refrigerant supply line L24 is discharged from the middle of the cryogenic temperature heat exchanger 4 to the outside, expanded through the
The gaseous refrigerant supplied to the cryogenic temperature heat exchanger 4 through the fifth refrigerant supply line L25 is discharged from the upper end of the cryogenic temperature heat exchanger 4 to the outside, expanded through the
In this cryogenic heat exchanger (4), heat is taken from the natural gas and the heated refrigerant is partially vaporized, and the gas phase and the liquid phase coexist. The liquid refrigerant is discharged from the lower end of the cryogenic heat exchanger 4 and supplied to the low temperature heat exchanger 3 through the first refrigerant return line L31 and the gaseous refrigerant flows from the lower portion of the cryogenic heat exchanger 4 And is supplied to the low temperature heat exchanger 3 through the second refrigerant return line L32.
As described above, the refrigerant returning from the cryogenic heat exchanger (4) to the refrigerant compressor (21) is mixed with the refrigerant expanded after passing through the low temperature heat exchanger (3) and then supplied to the low temperature heat exchanger (3).
Here, when a plurality of low-temperature heat exchangers 3 are used, the refrigerant can be returned to the low-temperature heat exchanger 3 through the second
Since the refrigerant supplied from the cryogenic heat exchanger 4 to the low temperature heat exchanger 3 is conveyed through the second
When the refrigerant in a vapor-liquid mixed state is directly supplied to a plurality of low-temperature heat exchangers, a relatively large amount of gaseous refrigerant is supplied to a specific low-temperature heat exchanger, and a relatively large amount of liquid refrigerant is supplied to another low- There is a possibility that operating conditions may be different for each heat exchanger.
If a plurality of low-temperature heat exchangers 3 are provided so as to separately supply a gas component and a liquid component, the same amount of gas component and liquid component can be supplied to each of the low-temperature heat exchangers 3, which is preferable.
The returning refrigerant can be mixed with the gas component and the liquid component immediately before being supplied to the low temperature heat exchanger (3) and can pass through the low temperature heat exchanger (3). The return refrigerant heated while passing through the low temperature heat exchanger (3) while cooling the natural gas supplied to the cryogenic temperature heat exchanger (4) and the supply refrigerant (that is, the refrigerant moving from the refrigerant compressor to the cryogenic heat exchanger) (L35) to the suction drum (23).
According to one embodiment of the present invention, a PFHE (Plate Fin Heat Exchanger) type heat exchanger may be used as the low temperature heat exchanger for precooling natural gas, and a SWHE (Spiral Wound Heat Exchanger type heat exchanger may be used. However, according to an alternative embodiment of the present invention, a PFHE type heat exchanger may be used as the cryogenic heat exchanger.
In addition, according to one embodiment of the present invention, the refrigerant compressed in the compressor is separated into three (that is, after passing through the liquid refrigerant separation, the compressor and the condenser separated in the
In addition, according to one embodiment of the present invention, a step of extracting NGL having a large amount of heavy hydrocarbon components from the natural gas cooled and partially condensed in the low temperature heat exchanger 3 is carried out together. However, if necessary, The NGL extraction process may be omitted if it is not necessary to separate the LNG component and the LPG component.
According to the method and apparatus for liquefying natural gas of the present invention, a single mixed refrigerant cycle (SMR) constituting a single closed loop is constructed in accordance with characteristics of a marine environment by using a mixed refrigerant composed of nitrogen and hydrocarbon system , And NGL (Natural Gas Liquid) treatment process, it is possible to implement an appropriate liquefaction process for a floating structure such as LNG FPSO having a limited space.
As described above, the natural gas liquefaction method and apparatus according to the present invention have been described with reference to the drawings. However, the present invention is not limited to the above-described embodiments and drawings, It will be understood by those skilled in the art that various changes and modifications may be made.
1: Natural gas liquefier 2: Floating structure 3: Low temperature heat exchanger 4: Cryogenic heat exchanger 5: Refrigerant circuit 11: Cold separator 12: Pressure reducing valve 13: LNG receiver 15: A refrigerant compressor, a compressor, a suction drum, a suction drum, an intermediate cooler, an intermediate separator, a refrigerant condenser, L12 is a first natural gas supply line, L13 is a natural gas supply line, L13 is a liquid natural gas supply line, Gas supply line L14 a second natural gas supply line L21 a first refrigerant supply line L22 a second refrigerant supply line L23 a third refrigerant supply line L24 a fourth refrigerant supply line L25 fifth L31 is the first refrigerant return line, L32 is the second refrigerant returning line, L33 is the third refrigerant returning line, L34 is the fourth refrigerant returning line, and L35 is the fifth refrigerant returning line. sign
Claims (21)
Wherein the heat exchange means comprises a low temperature heat exchanger for cooling the natural gas extracted from the gas well to a low temperature and a cryogenic heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger, The height of the heat exchange means is reduced by arranging the cryogenic heat exchanger in the horizontal direction,
The refrigerant heated by the natural gas in the cryogenic heat exchanger is supplied to the low temperature heat exchanger, precooling the natural gas before being supplied to the cryogenic heat exchanger,
The refrigerant heated by the natural gas in the cryogenic heat exchanger is separated into a gaseous refrigerant and a liquid refrigerant through the gas-liquid separator and is supplied to the low temperature heat exchanger. When the refrigerant passes through the low temperature heat exchanger, Wherein the refrigerant is in a state of being mixed with the refrigerant in a state of being mixed.
And a refrigerant circuit consisting of a single circuit for sequentially liquefying the natural gas by circulating the refrigerant through the low temperature heat exchanger and the cryogenic heat exchanger sequentially.
And a cold separator separating the natural gas cooled at a low temperature in the low temperature heat exchanger into a natural gas in a gaseous state and a natural gas in a liquid state and supplying the gaseous natural gas to the cryogenic heat exchanger, Device.
And means for separating the liquid natural gas separated by the cold separator by the component.
Wherein a plurality of the low temperature heat exchangers are installed and the gaseous refrigerant separated through the gas-liquid separator and the liquid refrigerant are supplied to the plurality of low temperature heat exchangers through separate supply lines.
Wherein the natural gas liquefier comprises at least one compressor including a refrigerant compressor for compressing a refrigerant that cools natural gas through heat exchange with natural gas, and a refrigerant condenser for condensing the compressed refrigerant.
Wherein the refrigerant supplied to the low-temperature heat exchanger in the compression unit is separately supplied to the gaseous refrigerant and the liquid refrigerant through the discharge separator.
A refrigerant compressor for compressing the refrigerant, and a refrigerant condenser for condensing the compressed refrigerant, wherein the refrigerant compressor is a multi-stage compressor.
The refrigerant supplied to the low temperature heat exchanger may include a first refrigerant supply line for supplying the liquid refrigerant separated by the intermediate separator in the partially condensed refrigerant cooled by the intermediate cooler included in the refrigerant compressor to the low temperature heat exchanger , A gaseous refrigerant separated by the intermediate separator is compressed again by the refrigerant compressor and is partially condensed by the refrigerant condenser, and a second refrigerant for supplying the liquid refrigerant separated from the discharge separator to the low temperature heat exchanger And a third refrigerant supply line for supplying gaseous refrigerant separated from the discharge separator to the low temperature heat exchanger.
The refrigerant supplied to the low temperature heat exchanger through the third refrigerant supply line is cooled and partially condensed by the refrigerant returning from the cryogenic temperature heat exchanger and is separated into a gaseous refrigerant and a liquid refrigerant by the first refrigerant separator And the natural gas is cooled in the cryogenic heat exchanger after each expansion.
Wherein the refrigerant supplied to the low temperature heat exchanger through the first and second refrigerant supply lines is expanded and then supplied to the low temperature heat exchanger to cool the natural gas.
Wherein the expanded refrigerant is mixed with the refrigerant supplied to the low temperature heat exchanger in the cryogenic temperature heat exchanger and returned to the low temperature heat exchanger to cool the natural gas.
A low temperature heat exchanger installed on an upper deck of the floating structure for cooling the natural gas extracted from the gas chill to a low temperature;
A cryogenic heat exchanger disposed on an upper deck of the floating structure and horizontally disposed in the low temperature heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger;
A refrigerant circuit for sequentially liquefying the natural gas by circulating the refrigerant through the low temperature heat exchanger and the cryogenic heat exchanger; / RTI >
The refrigerant heated by the natural gas in the cryogenic heat exchanger is supplied to the low temperature heat exchanger, precooling the natural gas before being supplied to the cryogenic heat exchanger,
The refrigerant heated by the natural gas in the cryogenic heat exchanger is separated into a gaseous refrigerant and a liquid refrigerant through the gas-liquid separator and is supplied to the low temperature heat exchanger. When the refrigerant passes through the low temperature heat exchanger, Wherein the refrigerant is in a state of being mixed with the refrigerant in a state of being mixed.
Further comprising an NGL facility for separating heavy hydrocarbons from the partially condensed natural gas cooled in said low temperature heat exchanger.
Wherein the refrigerant circuit includes a plurality of compression units including a refrigerant compressor and a refrigerant condenser.
Wherein the low temperature heat exchanger is a Plate Fin Heat Exchanger (PFHE) type heat exchanger, and the cryogenic heat exchanger is a SWHE (Spiral Wound Heat Exchanger) type heat exchanger.
A low temperature heat exchanger installed on an upper deck of the floating structure for cooling the natural gas extracted from the gas chill to a low temperature;
A cryogenic heat exchanger disposed on an upper deck of the floating structure and horizontally disposed in the low temperature heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger;
A refrigerant circuit for sequentially liquefying the natural gas by circulating the refrigerant through the low temperature heat exchanger and the cryogenic heat exchanger; / RTI >
The refrigerant heated by the natural gas in the cryogenic heat exchanger is supplied to the low temperature heat exchanger, precooling the natural gas before being supplied to the cryogenic heat exchanger,
The refrigerant heated by the natural gas in the cryogenic heat exchanger is separated into a gaseous refrigerant and a liquid refrigerant through the gas-liquid separator and is supplied to the low temperature heat exchanger. When the refrigerant passes through the low temperature heat exchanger, Wherein the natural gas liquefaction device has a natural gas liquefying device in which the refrigerant in a state of being condensed is combined.
Wherein the floating structure is LNG FPSO.
A low temperature heat exchanger for cooling the natural gas extracted from the gas well to a low temperature and a cryogenic heat exchanger for further cooling and liquefying the natural gas cooled in the low temperature heat exchanger, The refrigerant passing through the low temperature heat exchanger and the refrigerant passing through the cryogenic temperature heat exchanger form one refrigerant circuit,
The refrigerant heated by the natural gas in the cryogenic heat exchanger is supplied to the low temperature heat exchanger, precooling the natural gas before being supplied to the cryogenic heat exchanger,
The refrigerant heated by the natural gas in the cryogenic heat exchanger is separated into a gaseous refrigerant and a liquid refrigerant through the gas-liquid separator and is supplied to the low temperature heat exchanger. When the refrigerant passes through the low temperature heat exchanger, Wherein the refrigerant is in a state of being mixed with the refrigerant in a state of being mixed.
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| KR101336679B1 (en) * | 2012-01-17 | 2013-12-04 | 고등기술연구원연구조합 | Natural gas liquefaction system and startup method thereof |
| KR101278587B1 (en) * | 2012-05-22 | 2013-06-25 | 연세대학교 산학협력단 | Liquefaction method of natural gas for energy reduction |
| KR101386543B1 (en) * | 2012-10-24 | 2014-04-18 | 대우조선해양 주식회사 | System for treating boil-off gas for a ship |
| KR101640768B1 (en) | 2013-06-26 | 2016-07-29 | 대우조선해양 주식회사 | Method for building a ship |
| FR3047552A1 (en) * | 2016-02-05 | 2017-08-11 | Air Liquide | OPTIMIZED INTRODUCTION OF A DIPHASIC MIXED REFRIGERANT CURRENT IN A NATURAL GAS LIQUEFACTION PROCESS |
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| JP2001004271A (en) * | 1999-06-22 | 2001-01-12 | Iwatani Internatl Corp | System for producing liquefied gas |
| KR100397527B1 (en) | 1995-04-18 | 2003-11-28 | 쉘 인터내셔널 리써치 마챠피즈 비 브이 | Cooling of the fluid stream |
| WO2008009721A2 (en) | 2006-07-21 | 2008-01-24 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for liquefying a hydrocarbon stream |
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| EP1939564A1 (en) * | 2006-12-26 | 2008-07-02 | Repsol Ypf S.A. | Process to obtain liquefied natural gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| KR100397527B1 (en) | 1995-04-18 | 2003-11-28 | 쉘 인터내셔널 리써치 마챠피즈 비 브이 | Cooling of the fluid stream |
| JP2001004271A (en) * | 1999-06-22 | 2001-01-12 | Iwatani Internatl Corp | System for producing liquefied gas |
| WO2008009721A2 (en) | 2006-07-21 | 2008-01-24 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for liquefying a hydrocarbon stream |
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