CN107560316A - natural gas liquefaction system and method - Google Patents
natural gas liquefaction system and method Download PDFInfo
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- CN107560316A CN107560316A CN201610502505.7A CN201610502505A CN107560316A CN 107560316 A CN107560316 A CN 107560316A CN 201610502505 A CN201610502505 A CN 201610502505A CN 107560316 A CN107560316 A CN 107560316A
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- natural gas
- liquefaction system
- gaseous
- cooling
- gas liquefaction
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 670
- 239000003345 natural gas Substances 0.000 title claims abstract description 332
- 238000000034 method Methods 0.000 title description 12
- 238000001816 cooling Methods 0.000 claims abstract description 48
- 238000007710 freezing Methods 0.000 claims abstract description 45
- 230000008014 freezing Effects 0.000 claims abstract description 45
- 230000006835 compression Effects 0.000 claims abstract description 44
- 238000007906 compression Methods 0.000 claims abstract description 44
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 37
- 238000010438 heat treatment Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims description 43
- 239000012530 fluid Substances 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 35
- 238000001035 drying Methods 0.000 claims description 23
- 239000000203 mixture Substances 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 230000006837 decompression Effects 0.000 claims description 2
- 238000010586 diagram Methods 0.000 description 20
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 17
- 229930195733 hydrocarbon Natural products 0.000 description 13
- 150000002430 hydrocarbons Chemical class 0.000 description 13
- 239000004215 Carbon black (E152) Substances 0.000 description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 9
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 239000012535 impurity Substances 0.000 description 6
- 229960004424 carbon dioxide Drugs 0.000 description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 230000004931 aggregating effect Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- CNKHSLKYRMDDNQ-UHFFFAOYSA-N halofenozide Chemical compound C=1C=CC=CC=1C(=O)N(C(C)(C)C)NC(=O)C1=CC=C(Cl)C=C1 CNKHSLKYRMDDNQ-UHFFFAOYSA-N 0.000 description 3
- 239000001307 helium Substances 0.000 description 3
- 229910052734 helium Inorganic materials 0.000 description 3
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 229910001868 water Inorganic materials 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000000112 cooling gas Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 description 1
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 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
- 239000001273 butane Substances 0.000 description 1
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000003129 oil well Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
-
- 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
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
- F25J1/0037—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—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
- F25J1/0032—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—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 the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- 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
- F25J1/0201—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 only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—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 only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"
Landscapes
- 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
The invention discloses a kind of natural gas liquefaction system.The natural gas liquefaction system includes：Heat exchanger, for cooling down the natural gas of supply to obtain the natural gas of cooling；First supersonic speed condenser, for condensing the natural gas of the cooling to produce liquefied natural gas, and export at least a portion freezing gaseous natural gas and be heated to the heat exchanger to obtain the natural gas of heating；And compression unit, for compressing the natural gas of the heating, and natural gas to the heat exchanger for providing compression to be cooled with the common and described at least a portion freezing gaseous natural gas progress heat exchange of the natural gas of the supply.The invention also discloses a kind of natural gas liquefaction.
Description
Technical field
The present invention relates to a kind of natural gas liquefaction system and method.
Background technology
Natural gas is a kind of fossil fuel, can be taken as a kind of energy and be used to heat, cook and generate electricity.It can also be by
It is used as motor vehicle fuel and the industrial chemicals of the preparation as plastic manufacturing and other important organic chemistry materials.The volume of natural gas
Can significantly it reduce after being liquefied.The volume of liquefied natural gas is the 1/625 of gaseous natural gas volume, so liquefied natural gas holds
Easily it is stored and transports.A kind of traditional natural gas liquefaction system carrys out liquefied natural gas using ice chest.Ice chest utilizes nitrogen, first
Alkane or including but not limited to nitrogen, methane, the mix refrigerant of ethane and/propane circulate flow through ice chest to cool down wherein
Natural gas.The cost of ice chest is higher and volume is larger.
Therefore, it is necessary to a kind of natural gas liquefaction system and method are provided for solving at least part above mentioned problem.
The content of the invention
One aspect of the present invention is to provide a kind of natural gas liquefaction system.The natural gas liquefaction system includes：Heat is handed over
Parallel operation, for cooling down the natural gas of supply to obtain the natural gas of cooling；First supersonic speed condenser, for condensing the cooling
Natural gas produce liquefied natural gas, and export at least a portion freezing gaseous natural gas and be heated to come to the heat exchanger
Obtain the natural gas of heating；And compression unit, for compressing the natural gas of the heating, and the natural gas of compression is provided to described
Heat exchanger comes with the natural gas of the supply jointly and described at least a portion freezes gaseous natural gas progress heat exchange and by
Cooling.
Another aspect of the present invention is to provide a kind of natural gas liquefaction.The natural gas liquefaction includes：It is cold
But the natural gas supplied obtains the natural gas of cooling；Produced by the natural gas of the first supersonic speed condenser condensation cooling
Raw liquefied natural gas, and the liquefied natural gas and freezing gaseous natural gas are exported from the first supersonic speed condenser；It is heated to
A few part freezes gaseous natural gas to obtain the natural gas of heating；The natural gas of the heating is compressed to obtain the natural of compression
Gas；And the natural gas of the compression and the common and described at least a portion freezing gaseous natural gas of natural gas of the supply are carried out
Heat exchange and be cooled.
Brief description of the drawings
It is described in conjunction with the accompanying drawings for embodiments of the present invention, the present invention may be better understood, in accompanying drawing
In：
Fig. 1 show the schematic diagram of the natural gas liquefaction system of one embodiment of the invention；
Fig. 2 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 3 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 4 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 5 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 6 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 7 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 8 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Fig. 9 show the schematic diagram of the natural gas liquefaction system of another embodiment of the present invention；
Figure 10 show the flow chart of the natural gas liquefaction of one embodiment of the invention.
Embodiment
To help those skilled in the art definitely to understand present invention theme claimed, with reference to attached
The embodiment of the present invention is described in detail in figure.Below in the detailed description of these embodiments, this specification
Some known functions or construction are not described in detail to avoid unnecessary details and have influence on the disclosure of the present invention.
Unless otherwise defined, the claims and technical term used in the description or scientific terminology are should be
The ordinary meaning that the personage with general technical ability is understood in the technical field of the invention.This specification and claims
Used in " first ", " second " and similar word be not offered as any order, quantity or importance, and simply use
To distinguish different part and element.The similar word such as "one" or " one " is not offered as quantity limitation, but represents
Exist at least one.Either the similar word such as " with " means to appear in the element before " comprising " or " with " " comprising "
Either object covers the element or object and its equivalent element for appearing in " comprising " or " having " presented hereinafter, it is not excluded that
Other elements or object.
" gas " and can represent to be different from the gaseous material or mixture of liquid or solid-state with " steam " used interchangeably.
Similarly, " liquid " represents to be different from gaseous state or the liquid or mixture of solid-state.
" natural gas " refers to the multielement gas obtained from natural oil well or underground gassiness formation.The component of natural gas
It can significantly modify with pressure.A kind of typical natural gas is main component comprising methane.Raw natural gas can also include ethane, again
Hydrocarbon, one or more sour gas (such as carbon dioxide, hydrogen sulfide, carbonyl sulfide, carbon disulfide, mercaptan) and a small amount of impurity
(such as water, helium, nitrogen, iron sulfide, wax, crude oil).The component of raw natural gas can change.
" sour gas " is the impurity being entrained in natural gas.Typically, sour gas includes carbon dioxide and hydrogen sulfide,
But any number of other impurities may also form sour gas.Sour gas typically contains energy and sour gas by contact
The absorbent of reaction, such as amine, gas remove.When absorbent is rich in sour gas, adsorption step can be used to from suction
Receive agent separating acid gas.Then, absorbent reusable edible, then for absorbing sour gas.
" liquefied natural gas " (Liquefied Natural Gas) is the liquid condensed of natural gas, generally comprises high percentage
The methane of ratio, but micro other elements and/or composition can be also included, it is including but not limited to ethane, propane, butane, two
Carbonoxide, nitrogen, helium, hydrogen sulfide or impurity.Natural gas can be processed to remove one or more components (such as sour gas
Body) or impurity (such as water or heavy hydrocarbon), liquid is cooled to by cooling at approximately atmospheric pressure afterwards.
" heavy hydrocarbon " is more than or equal to three hydro carbons for the number of carbon, is alternatively referred to as " hydrocarbon of high carbon number " or is referred to as " C3+ ".Weight
Hydrocarbon can include the hydrocarbon of propane, normal butane, iso-butane, pentane or higher molecular weight.
" gas reducing liquid (Natural Gas Liquid) " is condensed fluid, generally comprises the heavy hydrocarbon of high percentage, but
Also micro other elements and/or composition can be included, its including but not limited to methane, ethane, carbon dioxide, nitrogen, helium,
Hydrogen sulfide, and/or pollutant.
" compressor " refers to the device of compressed gas, including pump, compressor turbine, reciprocating compressor, piston compressor,
Rotary Compressor, screw compressor or the device or component of being capable of compressed gas.
" heat exchanger " refer to allow two or more fluids by and two or more fluids is carried out heat exchange
Tank, tower, unit or other devices.Such as shell and tube heat exchanger, freezing Wound-rotor type heat exchanger or welding aluminum sheets fin-shaped type.
" supersonic condensing device " (or making " supersonic cyclone separator ") refers to the main dress for using reducing and expansion Laval nozzle
Put, the energy (pressure and temperature) of gas is converted into the kinetic energy (speed) of gas wherein.The speed of gas reaches supersonic speed.By
In the acceleration of gas, temperature and pressure substantially reduces, therefore the subject component in gas is liquefied.Liquefied subject component leads to
High-speed rotational is crossed to be separated from gas.Then the speed of gas is lowered and the pressure of gas returns to almost original pressure
Power.Reducing and expansion Laval nozzle can be designed with the subject component that liquefies according to specific subject component.
" decompressor " refers to the device of the pressure for reducing fluid, and fluid is reduced typically by way of expanding fluid
Pressure and temperature." Joule-Thomson (Joule-Thomson) valve " is a kind of decompressor, and it is caused using gas expansion
Gas-cooled Joule-Thomson principle.In certain embodiments, Joule-Thomson valve can by other expansion gears, such as
Turbo-expander, instead of.
" knockout drum " refers to is separated into single gaseous parts and liquid part by the gaseous state of input and fluid liquid wherein
Tank body.Typically, knockout drum has significantly interface, and such gas and liquid are due to Gravity Separation.
Fig. 1 show the schematic diagram of the natural gas liquefaction system 100 of one embodiment.Natural gas liquefaction system 100 includes
Heat exchanger 26, the first supersonic condensing device 30 and compression unit 21.The natural gas that heat exchanger 26 is used for cooling down supply obtains
The natural gas 28 of cooling.First supersonic speed condenser 30 is used for condensing the natural gas 28 of cooling to produce liquefied natural gas, and defeated
Go out at least a portion freezing gaseous natural gas to be heated to heat exchanger 26 to obtain the natural gas 60 of heating.Compression unit 21 is used
To compress the natural gas 60 of heating, and the natural gas of compression is provided to the natural gas of heat exchanger 26 and supply is common and freezing
Gaseous natural gas carries out heat exchange and is cooled.
In the present embodiment, natural gas liquefaction system 100 includes purifier units 13 for receiving raw natural gas 11, and it can profit
Made a return journey with any number of processing procedure and remove sour gas and other impurities 15.Purifier units 13 can be freezing distillation unit,
Such as rely amp- Holmes (Ryan-Holmes) processing system.Other freezing distillation techniques and system can also be used, such as control
Fine frozen area technology.Non-frozen technology and system also can be used to purify, such as heating processing system, amine desulfurization process system.Come
It can be used in other systems or processing from the sour gas 15 of purifier units 13.Returned for example, carbon dioxide can be used for oil
Receive, hydrogen sulfide can prepare sulphur using Crouse (Claus) technique.In one embodiment, when removing sour gas 15, carry
Pure unit 13 can also remove heavy hydrocarbon, and it can also be used in other systems or processing.
The natural gas 17 of purification from purifier units 13 is supplied to drying unit 19, and drying unit 19 is done using ethylene glycol
Dry method, drier, pressure swing adsorption method or other techniques remove water vapour.It is single can be located at purification for drying unit 19 in one embodiment
Before member 13.
Dry natural gas 20 from drying unit 19 is supplied to compression unit 21.Compression unit 21 is used for compression drying
Natural gas 20.Compression unit 21 carrys out compressed natural gas to expected pressure including one or more compressors.In diagram embodiment
Middle compression unit 21 includes the first compressor 22 and the second compressor 23, and dry natural gas 20 flows through the first compressor 22 and pressed
Contracting.In one embodiment, the pressure of dry natural gas 20 is increased to about 200-250 by the first compressor 22 from about 54 bars
Bar.The pressure of dry natural gas 20 can change according to practical application.In one embodiment, the second compressor 23 is used for compressing
The natural gas 60 of heat obtains natural gas 61, and natural gas 61 and the natural gas 20 dried are mixed and compressed by the first compressor 22.
It is only unrestricted example to illustrate embodiment, and different compression units and compressor can be used in some other embodiment.
Such as the natural gas 60 and dry natural gas 20 of heating can be respectively by different compressor compresses, afterwards in heat exchanger 26
Mixing.
The natural gas 62 of compression from compression unit 21 is supplied to heat exchanger 26, the day of the cooling compression of heat exchanger 26
Right gas 62.Heat exchanger 26 includes first passage 25 and second channel 27.In one embodiment, heat exchanger 26 promotes to pass through
The heat exchange of the fluid of first passage 25 and fluid by second channel 27.First passage 25 is received and cooled down single from compression
The natural gas 24 of the compression of member 21.In one embodiment, heat exchanger 26 cools down the natural gas 62 of compression from about 45 DEG C
To 6 DEG C, but not limited to this.Temperature can change in other embodiments.
In some other embodiments, raw natural gas 11 can be purified unit before heat exchanger 26 is supplied to
13rd, one or more of drying unit 19 and compression unit 21 are handled, or other devices in Fig. 1 are not shown in by other
Processing.The natural gas of supply can be raw natural gas 11, the natural gas 17 of purification, the natural gas 20 dried or the natural gas compressed
62。
The natural gas 28 for carrying out the cooling of automatic heat-exchanger 26 is supplied to the first supersonic condensing device 30.First supersonic condensing
The natural gas 28 that device 30 is used for condensing cooling produces liquefied natural gas, and exports liquefied natural gas and freezing gaseous natural gas.Greatly
The natural gas 28 of partial cooling is liquefied as liquefied natural gas, and the natural gas 28 of sub-fraction cooling is not liquefied and from first
Exported in supersonic condensing device 30 with gaseous state.At least a portion of freezing gaseous natural gas from the first supersonic condensing device 30
Recycling produces liquefied natural gas in the natural gas liquefaction system 100.The second channel 27 of heat exchanger 26 receives simultaneously
The recycle sections of heating frozen gaseous natural gas.
First supersonic condensing device 30 includes being used for exporting the first outlet 34 of the Part I 38 of freezing gaseous natural gas
With for export including liquefied natural gas and freezing gaseous natural gas another part fluid-mixing 32 second outlet 36.It is cold
The major part for freezing gaseous natural gas exports from first outlet 34, and the remainder for freezing gaseous natural gas is blended in liquefaction naturally
Exported in gas from second outlet 36.Natural gas liquefaction system 100 using the first supersonic condensing device 30 replace traditional ice chest come
Liquefied natural gas is prepared, the size of the first supersonic condensing device 30 is much smaller than the size of ice chest, therefore natural gas liquefaction system 100
It is more compact.
In one embodiment, natural gas liquefaction system 100 includes at least one knockout drum connected with second outlet 36,
For isolating at least a portion freezing gaseous natural gas from fluid-mixing 32.In the illustrated embodiment, the first knockout drum 40
For isolating the Part II 42 of freezing gaseous natural gas from fluid-mixing 32.The day of separation from the first knockout drum 40
Right gas 44 is liquefied natural gas.
In one embodiment, the natural gas 44 of separation is supplied to the first decompressor connected with the first knockout drum 40
46, to reduce the pressure of the liquefied natural gas 44 from the first knockout drum 40 and export liquefied natural gas and low-pressure gaseous natural gas
Gas-liquid mixture 48.In one embodiment, the first decompressor 46 by the pressure of the liquefied natural gas 44 of separation from about
60-80 bars drops to about 1-3 bars, but not limited to this.At elevated pressures, such as about 60-80 bars, be liquid, so to natural gas 44
And portion of natural gas is changed into gaseous state after being depressured, therefore the fluid 48 exported from decompressor 46 is the gas-liquid mixed stream of natural gas
Body.Decompressor 46 drops to the pressure of liquefied natural gas 44 pressure of general liquefied natural gas storage and transport, such as about
1-3 bars.Typically, the first decompressor 46 is Joule-Thomson valve.
Gas-liquid mixture 48 from the first decompressor 46 is supplied to the second knockout drum 50.Second knockout drum 50 from from
Low-pressure gaseous natural gas 54 is isolated in the gas-liquid mixture 48 of first decompressor 46.The fluid 52 of second knockout drum 50 output
It is completely or generally liquefied natural gas and its pressure is pressure that liquefied natural gas is easy to store and transported.From the second knockout drum
The liquefied natural gas fluid 52 of 50 outputs can be the product of natural gas liquefaction system 100, and it can store or be supplied to downstream
System (not shown).Part I 38 and Part II of the pressure of low-pressure gaseous natural gas 54 less than freezing gaseous natural gas
42.In one embodiment, the pressure of the Part I 38 and Part II 42 that freeze gaseous natural gas is about 60-80 bars,
And the pressure of low-pressure gaseous natural gas 54 is about 1-3 bars.
Natural gas liquefaction system 100 includes aggregating apparatus 56, for receiving the Part I 38 of freezing gaseous natural gas, the
Two parts 42 and low-pressure gaseous natural gas 54, and the freezing gaseous state for exporting uniform pressure (about 40 bars to about 60 bars) is natural
The Part I 38 of gas, Part II 42 and low-pressure gaseous natural gas 54 converge fluid 58 (or making recirculated fluid) to heat
Exchanger 26.In one embodiment, aggregating apparatus 56 is ejector, its using laval nozzle Venturi effect.
Heat exchanger 26 flows through second channel 27 by the gas progress heat exchange with flowing through first passage 25 to heat
Recirculated fluid 58.Heat exchanger 26 with flowing through the recirculated fluid 58 of second channel 27 by carrying out heat exchange to cool down compression
Natural gas 62.The natural gas 62 of compression with the circulation of fluid 58 in second channel 27 completely by carrying out heat exchange to be cooled to
Expected temperature, without other cooling sources or cooling agent.The cold energy that the natural gas 62 of compression obtains is substantially equal to recirculation flow
The cold energy that body 58 provides.In one embodiment, the natural gas 62 of compression is cooled to about 6 DEG C from about 45 DEG C, and is being followed
Circulation body 58 is heated approximately at 36 DEG C, but not limited to this from about -15 DEG C.
Fig. 2 show the schematic diagram of the natural gas liquefaction system 200 of another embodiment.Natural gas liquefaction shown in Fig. 2
System 200 is similar to the natural gas liquefaction system 100 shown in Fig. 1.Natural gas liquefaction system 200 shown in Fig. 2 is different from Fig. 1 institutes
The main distinction of the natural gas liquefaction system 100 shown is by following paragraph description.The drying unit of natural gas liquefaction system 200
The dry natural gas 220 of 219 outputs is uncompressed to be supplied to heat exchanger 226, and its pressure can be, for example, about 54 bars.One
In individual embodiment, Fig. 1 the first compressor 22 can omit.The cool drying natural gas 220 of heat exchanger 226 to low temperature, such as
About -35 DEG C, the temperature is less than corresponding temperature in Fig. 1, such as 6 DEG C.
Natural gas liquefaction system 200 includes the 3rd knockout drum 264 connected with heat exchanger 226, carrys out self-heating for receiving
The natural gas 228 of the cooling of the first passage 225 of exchanger 226 and the separating natural airsetting liquid from the natural gas 228 of cooling
266.Natural gas 268 after separation from the 3rd knockout drum 264 is supplied to the first supersonic condensing device 230 to produce liquefaction day
Right gas.When raw natural gas 211 are not comprising heavy hydrocarbon or comprising Minor Heavy Hydrocarbon, the 3rd knockout drum 264 can omit.
Natural gas liquefaction system 200 includes cooling device 270, for cooling down from the first supersonic condensing device 230 extremely
Few part freezing gaseous natural gas is supplied to heat exchanger 226.A part for the condensed natural gas that cooled device 270 cools down
Including Part I 238 and Part II 242 with freezing gaseous natural gas roughly the same or close to pressure.In a reality
Apply in example, low-pressure gaseous natural gas 254 can be released, and the pressure of the part is different from Part I 238 and Part II 242
Pressure.In another embodiment, Part I 238, Part II 242 and low-pressure gaseous natural gas 254 can pass through Fig. 1
In aggregating apparatus 56 collect after be cooled device 270 cool down.In the illustrated embodiment, cooling device 270 is that the second decompression fills
Put, typically Joule-Thomson valve.Second decompressor can be with cooling gas and while expanding gas.In one embodiment
In, the pressure of recirculated fluid 258 is about 4 bars.
The recirculated fluid 258 for carrying out self-cooling set 270 is supplied to the second channel 227 of heat exchanger 226, is heated to
Close to the temperature of the temperature of dry natural gas 220.Carry out the recirculated fluid 260 of the heating of automatic heat-exchanger 226 by compression unit
221 compressions, and the recirculated fluid 262 compressed is recycled to dry natural gas 220.The compression heating of compression unit 221 follows again
Circulation body 260 to the pressure close to dry natural gas 220 pressure.In one embodiment, the second compressor 223 is by heating
Recirculated fluid 260 is compressed to about 54 bars from about 4 bars, and the design of second compressor 223 is compressed different from the second of Fig. 1
Machine 23.
Heat exchanger 226 is to flowing through the dry natural gas 220 of first passage 225 and the recirculated fluid 262 of compression and stream
The recirculated fluid 258 for crossing second channel 227 carries out the recirculated fluid that heat exchange comes cool drying natural gas 220 and compression
262.Therefore, the Part I 238 for freezing gaseous natural gas and Part II 242 are cooled to a temperature, example by cooling device 270
Such as, about -62 DEG C, the temperature is less than the temperature of the natural gas 228 for the cooling that heat exchanger 226 exports, so as to ensure to dry day
Right gas 220 and the recirculated fluid 262 of compression can pass through the Part I 238 and Part II with freezing gaseous natural gas
242 carry out heat exchanges and are cooled to expected temperature.
Fig. 3 show the schematic diagram of the natural gas liquefaction system 300 of another embodiment.Natural gas liquefaction shown in Fig. 3
System 300 is similar to the natural gas liquefaction system 200 shown in Fig. 2.Natural gas liquefaction system 300 shown in Fig. 3 is different from Fig. 2 institutes
The main distinction of the natural gas liquefaction system 200 shown is that the cooling device 372 of natural gas liquefaction system 300 includes expander, is used
To expand and cool down the Part I 338 and Part II 334 of freezing gaseous natural gas.Expander has to be subtracted with the second of Fig. 2
The similar function of pressure device 270.
Fig. 2 and Fig. 3 illustrate only two examples of cooling device, but cooling device can be that other being capable of cooling gas
Device.
Fig. 4 show the schematic diagram of the natural gas liquefaction system 400 of another embodiment.Natural gas liquefaction shown in Fig. 4
System 400 is similar to the natural gas liquefaction system 100 shown in Fig. 1.Natural gas liquefaction system 400 shown in Fig. 4 is different from Fig. 1 institutes
The main distinction of the natural gas liquefaction system 100 shown is that Fig. 4 natural gas liquefaction system 400 includes the second supersonic condensing device
474th, the 4th knockout drum 475 and the 3rd compressor 476.Second supersonic condensing device 474 is used for removing from the natural gas of supply
Gas reducing liquid 478.In the illustrated embodiment, drying unit 419 is located at the upstream of the second supersonic condensing device 474.Include weight
The dry natural gas 420 of hydrocarbon is supplied to the second supersonic condensing device 474.Heavy hydrocarbon is liquefied to form gas reducing liquid 478, and naturally
Airsetting liquid 478 separates in the second supersonic condensing device 474 with dry natural gas 420.In one embodiment, some natural gases
It is blended in gas reducing liquid 478, the 4th knockout drum 475 isolates at least a portion natural gas from gas reducing liquid.Separation
The natural gas 479 gone out mixes into the natural gas fluid 480 of the second supersonic condensing device 474 output and flows into the 3rd compressor
476。
The design of second supersonic condensing device 474 may differ from the first supersonic condensing device 430.Second supersonic condensing device
474 Mach 2 ship 1.1-1.6, and the Mach 2 ship 2-3 of the first supersonic condensing device 430.Natural gas fluid 480 and isolate
The temperature of natural gas 479 be about 2-35 DEG C, pressure is about 30-40 bars, and the output of the first supersonic condensing device 430 is cold
The temperature for freezing gaseous natural gas 438 is about -5 to 0 DEG C, and pressure is about 60-80 bars.
The pressure of natural gas fluid 480 from the second supersonic condensing device 474 is less than the pressure of dry natural gas 420.
3rd compressor 476 is used for compressed natural gas fluid 480 to provide under expecting pressure the 3rd of (such as about 100 bars) the compression stream
Body 482 is to compression unit 421.In one embodiment, the 3rd compressor 476 can be omitted, and natural gas fluid 480 can be pressed
Contracting unit 421 is compressed to expecting pressure, such as about 210 bars, to the first supersonic condensing device 430.In such the present embodiment
Unit 421 can be designed to different from the compression unit 21 in Fig. 1.
Fig. 5 show the schematic diagram of the natural gas liquefaction system 500 of another embodiment.Natural gas liquefaction shown in Fig. 5
System 500 is similar to the natural gas liquefaction system 200 shown in Fig. 2.Natural gas liquefaction system 500 shown in Fig. 5 is different from Fig. 2 institutes
The main distinction of the natural gas liquefaction system 200 shown be natural gas liquefaction gas system 500 include the second supersonic condensing device 574,
4th knockout drum 575 and the 3rd compressor 576, those devices are similar to corresponding device in Fig. 4.Fig. 5 the second Supersonic quickly cooling
Condenser 574 also can be used to remove the gas reducing liquid in dry natural gas 520.4th knockout drum 575 can be used to from natural airsetting
Gaseous natural gas is isolated in liquid.3rd compressor 576 is used for compressed natural gas fluid 580 and the natural gas 579 isolated.
Fig. 6 show the schematic diagram of the natural gas liquefaction system 600 of another embodiment.Natural gas liquefaction shown in Fig. 6
System 600 is similar to the natural gas liquefaction system 300 shown in Fig. 3.Natural gas liquefaction system 600 shown in Fig. 6 is different from Fig. 3 institutes
The main distinction of the natural gas liquefaction system 300 shown be natural gas liquefaction gas system 600 include the second supersonic condensing device 674,
4th knockout drum 675 and the 3rd compressor 676, those devices are similar to corresponding device in Fig. 4 and Fig. 5.
In Fig. 4 to Fig. 6 embodiment, the 3rd compressor 476,576,676 be located at the second supersonic condensing device 474,
574th, 674 downstream.In another embodiment, the 3rd compressor 476,576,676 be located at the second supersonic condensing device 474,
574th, compression drying natural gas 420,520,620 is carried out in 674 upstream, to ensure from the second supersonic condensing device 474,574,674
The pressure of the natural gas fluid 480,580,680 of output can reach expecting pressure.
Fig. 7 show the schematic diagram of the natural gas liquefaction system 700 of another embodiment.Natural gas liquefaction shown in Fig. 7
System 700 is similar to the natural gas liquefaction system 400 shown in Fig. 4.Natural gas liquefaction system 700 shown in Fig. 7 is different from Fig. 4 institutes
The main distinction of the natural gas liquefaction system 400 shown is that the drying unit 719 of Fig. 7 natural gas liquefaction system 700 is located at second
The downstream of supersonic condensing device 774.Second supersonic condensing device 774 is used for removing natural airsetting from the natural gas 717 of purification
Liquid and at least a portion vapor 778, and export the fluid 786 comprising natural gas and part vapor.Drying unit 719 is used for
Vapor is removed from the fluid 786 from the second supersonic condensing device 774, to export dry natural gas 720.In the present embodiment
Because water vapor portion is removed by the second supersonic condensing device 774, thus the size of drying unit 719 can be designed to it is smaller come
Remove remaining vapor.Fluid 778 can include some natural gases being blended in gas reducing liquid and the vapor removed, the
Four knockout drums 775 isolate at least a portion natural gas from fluid 778.
Fig. 7 the second supersonic condensing device 774 can be designed to different or big with Fig. 4 the second supersonic condensing device 474
Cause identical, but be different from the first supersonic condensing device 730, so that natural gas liquid and some vapor can be removed.In an implementation
In example, the Mach 2 ship 1.1-1.6 of the second supersonic condensing device 774.In one embodiment, from the second supersonic condensing device 774
The temperature of the fluid 786 of output is about 25-35 DEG C, and pressure is about 35-45 bars.In one embodiment, compressor can quilt
There is provided in the upstream of the second supersonic condensing device 774 or downstream to improve the pressure of natural gas, because the second supersonic condensing device
774 can reduce the pressure for flowing through natural gas therein.
Fig. 8 show the schematic diagram of the natural gas liquefaction system 800 of another embodiment.Natural gas liquefaction shown in Fig. 8
System 800 is similar to the natural gas liquefaction system 500 shown in Fig. 5.Natural gas liquefaction system 800 shown in Fig. 8 is different from Fig. 5 institutes
The main distinction of the natural gas liquefaction system 500 shown is that the drying unit 819 of Fig. 8 natural gas liquefaction system 800 is located at second
The downstream of supersonic condensing device 874.Fig. 8 the second supersonic condensing device 874, the 4th knockout drum 875 is similar with drying unit 819
Corresponding device in Fig. 7.
Fig. 9 show the schematic diagram of the natural gas liquefaction system 900 of another embodiment.Natural gas liquefaction shown in Fig. 9
System 900 is similar to the natural gas liquefaction system 600 shown in Fig. 6.Natural gas liquefaction system 900 shown in Fig. 9 is different from Fig. 6 institutes
The main distinction of the natural gas liquefaction system 600 shown is that the drying unit 919 of Fig. 9 natural gas liquefaction system 900 is located at second
The downstream of supersonic condensing device 974.Fig. 9 the second supersonic condensing device 974, the 4th knockout drum 975 is similar with drying unit 919
Corresponding device in Fig. 7 and Fig. 8.
Figure 10 show the flow chart of the natural gas liquefaction 110 of one embodiment.Natural gas liquefaction 110 includes
Step 111-115.In step 111, the natural gas of supply is cooled down to obtain the natural gas of cooling.In step 112, by the first surpassing
The natural gas of velocity of sound condenser condensation cooling produces liquefied natural gas, and output liquefaction is natural from the first supersonic speed condenser
Gas and freezing gaseous natural gas.In step 113, heating at least a portion freezes gaseous natural gas to obtain the natural gas of heating.
In step 114, the natural gas of heating is compressed to obtain the natural gas of compression.In step 115, the natural gas and the day of supply of compression
Right gas carries out heat exchange and is cooled with least a portion freezing gaseous natural gas jointly.It is reusable after the natural air cooling of compression
To produce liquefied natural gas.
The division of action in the sequencing and step of step in Figure 10 is not limited to the embodiment of diagram.For example,
Step can perform in a different order, and the action in a step can be with the action knot in another or other multiple steps
Close, or split into several sub-steps.In addition in certain embodiments, before method 110, during and/or can also have afterwards
Other one or more actions.
Although the present invention is described in detail with reference to specific embodiment, those skilled in the art can
, can be so that many modifications may be made and modification to the present invention to understand.It is therefore contemplated that claims are intended to cover
All such modifications and modification in true spirit of the present invention and scope.
Claims (20)
1. a kind of natural gas liquefaction system, it is characterised in that it includes：
Heat exchanger, for cooling down the natural gas of supply to obtain the natural gas of cooling；
First supersonic speed condenser, for condensing the natural gas of the cooling to produce liquefied natural gas, and export at least one
Freezing gaseous natural gas is divided to be heated to the heat exchanger to obtain the natural gas of heating；And
Compression unit, for compressing the natural gas of the heating, and natural gas to the heat exchanger for providing compression comes and institute
The natural gas of supply is stated to carry out heat exchange with described at least a portion freezing gaseous natural gas jointly and be cooled.
2. natural gas liquefaction system as claimed in claim 1, it is characterised in that：The first supersonic condensing device includes being used for
Export the first outlet of the Part I of the freezing gaseous natural gas and for exporting including the liquefied natural gas and described
The second outlet of the fluid-mixing of another part of gaseous natural gas is freezed, and the natural gas liquefaction system is including at least one
The knockout drum connected with the second outlet, it is natural for isolating at least a portion freezing gaseous state from the fluid-mixing
Gas.
3. natural gas liquefaction system as claimed in claim 2, it is characterised in that：At least one knockout drum includes first point
From tank, for isolating the Part II of the freezing gaseous natural gas from the fluid-mixing and exporting the liquefaction naturally
Gas, the natural gas liquefaction system include the first decompressor connected with first knockout drum, for reducing from described
The pressure of the liquefied natural gas of first knockout drum and the gas-liquid mixture for exporting liquefied natural gas and low-pressure gaseous natural gas, and institute
Stating natural gas liquefaction system also includes the second knockout drum, for being separated from the gas-liquid mixture from first decompressor
Go out low-pressure gaseous natural gas.
4. natural gas liquefaction system as claimed in claim 3, it is characterised in that：The natural gas liquefaction system includes collecting dress
Put, for receiving Part I, Part II and the low-pressure gaseous natural gas of the freezing gaseous natural gas and exporting identical
The Part I of the condensed natural gas of pressure, Part II and low-pressure gaseous natural gas converge fluid to the heat exchange
Device.
5. natural gas liquefaction system as claimed in claim 1, it is characterised in that：The natural gas liquefaction system include and it is described
3rd knockout drum of heat exchanger connection, for removing natural airsetting from the natural gas of the cooling from the heat exchanger
Liquid.
6. natural gas liquefaction system as claimed in claim 1, it is characterised in that：The natural gas liquefaction system includes cooling and filled
Put, for cooling down at least a portion freezing gaseous natural gas from the first supersonic condensing device and by the natural gas of cooling
It is supplied to the heat exchanger.
7. natural gas liquefaction system as claimed in claim 6, it is characterised in that：The cooling device includes the second decompression and filled
Put.
8. natural gas liquefaction system as claimed in claim 6, it is characterised in that：The cooling device includes expander.
9. natural gas liquefaction system as claimed in claim 1, it is characterised in that：The natural gas liquefaction system includes being located at institute
The second supersonic condensing device before heat exchanger is stated, for removing gas reducing liquid from the natural gas of the supply.
10. natural gas liquefaction system as claimed in claim 9, it is characterised in that：The natural gas liquefaction system includes being located at
The drying unit in the second supersonic condensing device downstream, the second supersonic condensing device are used for the natural gas from the supply
Middle removal at least a portion vapor, and the drying unit is used for removing the natural gas from the second supersonic condensing device
In vapor.
11. natural gas liquefaction system as claimed in claim 9, it is characterised in that：The natural gas liquefaction system includes being located at
The drying unit of the second supersonic condensing device upstream, for removing the vapor in the natural gas of supply.
12. a kind of natural gas liquefaction, it is characterised in that it includes：
The natural gas for cooling down supply obtains the natural gas of cooling；
The natural gas of the cooling is condensed by the first supersonic speed condenser to produce liquefied natural gas, and from the first ultrasonic quickly cooling
The liquefied natural gas and freezing gaseous natural gas are exported in condenser；
Heating at least a portion freezes gaseous natural gas to obtain the natural gas of heating；
The natural gas of the heating is compressed to obtain the natural gas of compression；And
The natural gas of the compression and the common and described at least a portion freezing gaseous natural gas of natural gas of the supply are carried out
Heat exchange and be cooled.
13. natural gas liquefaction as claimed in claim 12, it is characterised in that：The output liquefied natural gas and freezing gas
The step of state natural gas including export it is described freezing gaseous natural gas Part I and output include the liquefied natural gas with
The fluid-mixing of another part of the freezing gaseous natural gas, the natural gas liquefaction are included from the fluid-mixing
Isolate at least a portion freezing gaseous natural gas.
14. natural gas liquefaction as claimed in claim 13, it is characterised in that：The step of separation, includes：
The Part II of the freezing gaseous natural gas is isolated from the fluid-mixing,
The pressure of the liquefied natural gas is reduced to obtain the gas-liquid mixture of liquefied natural gas and low-pressure gaseous natural gas, and
Low-pressure gaseous natural gas is isolated from the gas-liquid mixture.
15. natural gas liquefaction as claimed in claim 14, it is characterised in that：The natural gas liquefaction includes collecting
It is described freezing gaseous natural gas Part I, Part II and low-pressure gaseous natural gas and export the described cold of uniform pressure
The Part I of solidifying natural gas, Part II and low-pressure gaseous natural gas converge fluid.
16. natural gas liquefaction as claimed in claim 12, it is characterised in that：The natural gas liquefaction is included from institute
State in the natural gas of cooling and remove gas reducing liquid.
17. natural gas liquefaction as claimed in claim 12, it is characterised in that：The natural gas liquefaction, which is included in, to be added
At least a portion freezing gaseous natural gas from the first supersonic condensing device is cooled down before hot step.
18. natural gas liquefaction as claimed in claim 12, it is characterised in that：The natural gas liquefaction is included in cold
But gas reducing liquid is removed from the natural gas of the supply by the second supersonic condensing device before the natural gas supplied.
19. natural gas liquefaction as claimed in claim 18, it is characterised in that：The natural gas liquefaction includes passing through
The second supersonic condensing device removes at least a portion vapor from the natural gas of the supply, and is gone by drying unit
Except the vapor in the natural gas from the second supersonic condensing device.
20. natural gas liquefaction as claimed in claim 18, it is characterised in that：The natural gas liquefaction is included in
Vapor is removed from the natural gas of supply by drying unit before except gas reducing liquid.
Priority Applications (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610502505.7A CN107560316A (en) | 2016-06-30 | 2016-06-30 | natural gas liquefaction system and method |
| CA3028738A CA3028738A1 (en) | 2016-06-30 | 2017-06-28 | System and method for producing liquefied natural gas |
| EP17740171.8A EP3479037B1 (en) | 2016-06-30 | 2017-06-28 | System and method for producing liquefied natural gas |
| PCT/US2017/039711 WO2018005626A1 (en) | 2016-06-30 | 2017-06-28 | System and method for producing liquefied natural gas |
| US16/306,886 US20210033337A1 (en) | 2016-06-30 | 2017-06-28 | System and method for producing liquefied natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610502505.7A CN107560316A (en) | 2016-06-30 | 2016-06-30 | natural gas liquefaction system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107560316A true CN107560316A (en) | 2018-01-09 |
Family
ID=59351077
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610502505.7A Pending CN107560316A (en) | 2016-06-30 | 2016-06-30 | natural gas liquefaction system and method |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20210033337A1 (en) |
| EP (1) | EP3479037B1 (en) |
| CN (1) | CN107560316A (en) |
| CA (1) | CA3028738A1 (en) |
| WO (1) | WO2018005626A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113701448A (en) * | 2021-07-05 | 2021-11-26 | 中国科学院理化技术研究所 | Hydrogen liquefaction system and hydrogen liquefaction device based on multistage supersonic two-phase expander |
| CN113701447A (en) * | 2021-07-05 | 2021-11-26 | 中国科学院理化技术研究所 | Hydrogen liquefaction circulation system and hydrogen liquefaction device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113701450A (en) * | 2021-07-05 | 2021-11-26 | 中国科学院理化技术研究所 | Hydrogen supersonic speed two-phase direct expansion liquefaction system and hydrogen liquefaction device |
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- 2017-06-28 EP EP17740171.8A patent/EP3479037B1/en active Active
- 2017-06-28 US US16/306,886 patent/US20210033337A1/en not_active Abandoned
- 2017-06-28 WO PCT/US2017/039711 patent/WO2018005626A1/en unknown
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113701448A (en) * | 2021-07-05 | 2021-11-26 | 中国科学院理化技术研究所 | Hydrogen liquefaction system and hydrogen liquefaction device based on multistage supersonic two-phase expander |
| CN113701447A (en) * | 2021-07-05 | 2021-11-26 | 中国科学院理化技术研究所 | Hydrogen liquefaction circulation system and hydrogen liquefaction device |
Also Published As
| Publication number | Publication date |
|---|---|
| EP3479037B1 (en) | 2024-02-14 |
| WO2018005626A1 (en) | 2018-01-04 |
| US20210033337A1 (en) | 2021-02-04 |
| EP3479037A1 (en) | 2019-05-08 |
| CA3028738A1 (en) | 2018-01-04 |
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