CN108351162A - Gas liquefaction system and method - Google Patents
Gas liquefaction system and method Download PDFInfo
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- CN108351162A CN108351162A CN201680049773.6A CN201680049773A CN108351162A CN 108351162 A CN108351162 A CN 108351162A CN 201680049773 A CN201680049773 A CN 201680049773A CN 108351162 A CN108351162 A CN 108351162A
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- heat exchanger
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- liquefaction
- liquefaction system
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- 238000000034 method Methods 0.000 title claims abstract description 65
- 239000012530 fluid Substances 0.000 claims abstract description 74
- 230000008569 process Effects 0.000 claims abstract description 60
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 31
- 238000001816 cooling Methods 0.000 claims abstract description 22
- 239000003345 natural gas Substances 0.000 claims abstract description 7
- 230000006835 compression Effects 0.000 claims description 41
- 238000007906 compression Methods 0.000 claims description 41
- 239000007788 liquid Substances 0.000 claims description 26
- 239000007789 gas Substances 0.000 claims description 25
- 238000011144 upstream manufacturing Methods 0.000 claims description 8
- 230000009467 reduction Effects 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000003208 petroleum Substances 0.000 claims 1
- 239000003507 refrigerant Substances 0.000 abstract description 3
- 238000003860 storage Methods 0.000 description 12
- 229930195733 hydrocarbon Natural products 0.000 description 11
- 150000002430 hydrocarbons Chemical class 0.000 description 11
- 239000004215 Carbon black (E152) Substances 0.000 description 10
- 238000001704 evaporation Methods 0.000 description 9
- 230000008020 evaporation Effects 0.000 description 8
- 230000006870 function Effects 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 238000005057 refrigeration Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 239000004615 ingredient Substances 0.000 description 6
- 230000002093 peripheral effect Effects 0.000 description 6
- 239000003381 stabilizer Substances 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000010276 construction Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 241001672694 Citrus reticulata Species 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000000518 rheometry Methods 0.000 description 1
- 238000005476 soldering Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000004804 winding 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
- 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
- F25J1/003—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"
- F25J1/0045—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 vaporising a liquid 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
- F25J1/02—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
- 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
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied 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
- 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
Abstract
Liquefaction system is configured with single methane expander to provide main refrigerant function.The fluid circuit that liquefaction system may include heat exchanger and couple with heat exchanger, fluid circuit are configured to make the process streams cycle for entering feed from natural gas.Fluid circuit may include：The methane expander coupled with heat exchanger；The sub-cooling unit coupled with methane expander, sub-cooling unit are configured to form liquid natural gas (LNG) product from process streams；And it is placed in the first throttling device between heat exchanger and sub-cooling unit.Methane expander and first throttling device may be configured to that process streams is made to be expanded into pressure process, and pressure process is between the first pressure and the second pressure of process for leaving sub-cooling unit for entering feed.
Description
Cross reference to related applications
The Serial No. 62/210,827 submitted for 27th this application claims August in 2015 and entitled " SYSTEM AND
The priority of the U.S. Provisional Application of PROCESS FOR PRODUCTION OF LIQUID NATURAL GAS ", this application
Content is incorporated herein by quoting with it.
Background
Liquefied natural gas can be conducive to transport and store hydrocarbon and related material.Generally, process can greatly reduce the volume of gas.
The liquid of generation is particularly suitable for for example carrying out long-distance transportation by track and highway transportation tank car.This for abroad transport and/
Or it is especially economical to transport for the region that this piping infrastructure can not reach.
Summary
The theme of the disclosure relates generally to make to enter the liquefied system of hydrocarbon stream.These systems may be configured to typically in heat exchange
Cooling is provided at device, nearly to match the cooling curve of natural gas.In this way, system can form liquefied natural gas (LNG) stream.One
A little systems can provide refrigerating function by circulating a refrigerant through heat exchanger.This " refrigeration " process generally is suitable for small rule
Mould LNG facility.On the other hand, the embodiments herein may be configured to " expander " process, it makes to be originated from into natural gas
Fluid circulation is cooled down with being realized at heat exchanger.In an implementation, embodiment may be configured to make fluid in intermediate pressure
It is recycled under power, pressure of the intermediate pressure between the pressure for entering hydrocarbon stream and the stream (for example, boil-off gas) entered from storage facility
Between.This feature can reduce expansion ratio, to form LNG stream using the abundant refrigerating function of single methane expander offer.
Compared with executing needed for liquefaction process, these improvement can reduce the fund cost and operation complexity of embodiment.
Embodiment can be applied in many different types for the treatment of facilities.On the coast and/or marine it can find these
Facility.In one application, embodiment, which can be coupled to, resides in the processing of land ((or on bank) typically on the coast) and sets
Shi Zhong, or it is combined into part of it.These treatment facilities can be handled from the day of the production facility found on the coast with sea
Right gas feed.Offshore production is conducive to transport from the feed of gas field and/or the rich oil Tanaka extraction for being loaded with gas using piping
It is defeated to arrive treatment facility.For LNG processing, the refrigeration equipment properly constructed or " refrigeration chain " that can be used will be fed for treatment facility
It is transformed into liquid.In other applications, embodiment can be coupled in the production facility on ship (or similar floating ship), it also by
Referred to as floating liquefied natural gas (LNG) facility.
The brief description of attached drawing
Reference briefly is carried out to attached drawing now, wherein：
Fig. 1 depicts the schematic diagram of the exemplary embodiment of liquefaction system；
Fig. 2 depicts to realize the exemplary schematic diagram of the component of the liquefaction system of Fig. 1；
Fig. 3 depicts to realize the exemplary schematic diagram of the component of the liquefaction system of Fig. 1；
Fig. 4 depicts to realize the exemplary schematic diagram of the component of the liquefaction system of Fig. 1；
Fig. 5 depicts the schematic diagram of the compression circuit for being used in the liquefaction system of Fig. 1,2,3 and 4；And
Fig. 6 depicts the flow chart for making to enter the exemplary embodiment for being fed liquefied process.
Under applicable circumstances, same reference numeral indicates identical or corresponding component and unit through several views, it
Be it is out-of-proportion, unless otherwise prescribed.Embodiment disclosed herein may include in one or more of several views
Or the element occurred in the combination of several views.In addition, method is only exemplary and can be for example, by individual grade
Resequence, add grade, remove grade and/or make independent grade to change to change.
Detailed description
Following discussion describes the various embodiments that can be used to handle the hydrocarbon for being stored as liquid natural gas (LNG).These
Embodiment includes fluid circuit, and fluid circuit makes cycle hydrocarbon stream flash, and the then cooling cycle hydrocarbon stream under intermediate pressure, in
Between pressure between entering the "high" pressure of feed hydrocarbon boil-off gas from storage facility between " low " pressure.Other embodiments exist
In the range of disclosed theme.
Fig. 1 shows the exemplary embodiment for making the liquefied liquefaction system 100 (also referred to as " system 100 ") of hydrocarbon stream
Schematic diagram.Under higher level, system 100 can have the fluid circuit 102 for receiving the feed 104 from source 106.Into to
Material 104 can be vaporous form (also referred to as " gas " or " natural gas "), the ingredient with mainly methane.The implementation of system 100
Example can be compatible with about 93% (930000 ppmV) or the higher ingredient of methane of first concentration.In use, system
100 can form one or more products (for example, first product 108), typically meet the liquid natural gas of storage specification
(LNG).These specifications could dictate that the second concentration of the methane of LNG product 108, it is less than the first concentration for entering feed 104.
In one example, the second concentration of the methane in the first product 108 may be about 99% or higher (990000 ppmV).Fluid returns
LNG product 108 can be assigned to storage facility 110 and/or other attached procedures equipment by road 102.
Fluid circuit 102 may be configured to form circulation of fluid (for example, gas and liquid) and make its cycle.For clarity,
These fluids are identified as process streams 112 in Fig. 1.In an implementation, fluid circuit 102 may include first heat exchanger
114 (also referred to as " principal heat exchange 114 ").The example of principal heat exchange 114 can have multiple passages, and each passage is in logical
The form in road, it may include that (" coil winding formula exchanges for aluminium soldering fin (" plate-fin exchanger ") and/or tubular coil
Device ").Such construction can be conducive to exchange the thermal energy among the fluid for transporting through principal heat exchange 114 indirectly.Channel
It can couple with multiple processing units, with exchange process stream 112 at various temperatures.The example of process streams 112 can be steam, liquid
With the form of mixed phase.But in an implementation, fluid circuit 102 is configured to that process streams 112 is made to remain individually
Phase, vapor phase or liquid phase.Processing unit may be disposed to sub-cooling unit 116, compression unit 118 and methane expander 120.
Broadly, use sub-cooling unit 116 that can improve the operation of fluid circuit 102 within system 100.Sub-cooling unit
116 may be configured to by process streams 112 be flashed between enter the pressure of feed 104 with as secondary into becoming a mandarin boil-off gas
And/or the pressure between the pressure of the similar stream from storage facility 110.The liquid flashed under this " centre " pressure can be located
In the temperature being suitable for store at such as storage facility 110.In addition, forming liquid under this intermediate pressure is effectively reduced stream
The expansion ratio in body circuit 102, to allow system 100 the case where only there are one methane expander (for example, methane expanders 120)
Under efficiently run.This improves the structure for simplifying fluid circuit 102, to reduce the fund and running cost of system 100, and
And thus, it is lowered into the totle drilling cost that feed 104 arrives the liquefaction process of LNG product 108.
Fig. 2 shows the examples of the component to realize the liquefaction system 100 for obtaining the first product 108 from entrance feed 104.
At sub-cooling unit 116, fluid circuit 102 can have the first container 122 coupled with second heat exchanger 124.Second heat is handed over
The example of parallel operation 124 can have there are two passage, but additional passage can be used in certain realizations of system 100.Fluid circuit
102 can form fluid path 126, and the passage of its second heat exchanger 124 is linked together.In compression unit 118, fluid returns
Road 102 is in combination with one or more compression circuits (for example, the first compression circuit 128 and second compression circuit 130).First compression
Circuit 128 can couple via principal heat exchange 114 with sub-cooling unit 116.In methane expander 120, fluid circuit 102 can
Open loop is formed with turbine 132, preferably there is turbine 132 turbo-compressor 134, turbo-compressor 134 to be configured to
Response comes from the work(of turbine expander 136 and runs.Turbine 132 can have pairs of entrance (for example, first entrance 138
With second entrance 140) and pairs of outlet (for example, first outlet 142 and second outlet 144).Entrance 138,140 and outlet
142,144 connection turbines 132 and principal heat exchange 114 and the second compression circuit 140.
Fluid circuit 102 can benefit from can be conducive to generate LNG product 108 process one or more auxiliary parts or
Peripheral member.For example, fluid circuit 102 may include one or more throttling sets 146.The example of throttling set 146 may include
Valve (for example, throttle valve (Joule-Thompson valves)) and/or the similarly device (Fig. 1) of the stream of suitable process of inhibition stream 112.
In use, throttling set 146 can be as making fluid parameter (for example, temperature, pressure etc.) realize necessary to certain variations
It is placed between the component in fluid circuit 102.
The left side of flow chart in fig. 2 starts, and 102 bootable process streams 112 (Fig. 1) of fluid circuit pass through various components
To generate LNG product 108.In an implementation, it can enter at a temperature of first pressure and first into feed 104 main
First passage of heat exchanger 114, typically under ambient temperature prevailing in system 100 and/or peripheral facilities.First pressure
It may depend on the operation of facility and/or equipment.Exemplary pressure may be about 720 psig, but be likely to fall about 500
In the range of psig to about 900 psig.Into ranging from about -150 °F to about -220 °F of the second temperature of feed 104
Lower separating device (at 148).
The cooling feed 104 that enters can be directed to first throttling device (for example, throttling set 146) by fluid circuit 102.
This first throttling device " flash distillation " enters feed 104 122 upstream of the first container, to effectively make pressure from the first pressure
Power is reduced to above-mentioned intermediate pressure.Flash distillation is beneficial for the structure for simplifying system 100 under this intermediate pressure.
In an implementation, first throttling device can be left (150 under the pressure less than first pressure into feed 104
Place), pressure is in the range of such as about 90 psig to about 150 psig.Temperature can about -200 °F to about -
Change in 240 °F of range.
Fluid circuit 102 can will enter feed 104 at a temperature of the pressure of reduction and/or reduction and be directed to the first container
122.The feed 104 that enters that process in the first container 122 can will be in intermediate pressure (and being in mixed phase form) is separated into
Top product and bottom product are in respectively vaporous form and liquid form.In an implementation, fluid circuit 102
Liquid bottoms product can be directed to the first passage of second heat exchanger 124.This first passage further decreases liquid bottom
The temperature of portion's product so that the temperature of LNG product 108 is in about -230 °F to about -265 °F of range.
Liquid bottoms product can be divided into one or more parts by fluid circuit 102 in the downstream of second heat exchanger 124.
Fluid circuit 102 can be guided first part as LNG product 108.Fluid circuit 102 can be via fluid path 126 by second
The second passage of second heat exchanger 124 is led back in part.This second part can be used to make to flow through second heat exchanger 124
The liquid bottoms product of first passage is subcooled.In an implementation, fluid circuit 102 may include being placed in second heat exchanger
Second throttling device (for example, throttling set 146) between 124 the first passage and second is secondary.This second throttling device
It is configured so to second part to leave under the pressure of second part (at 154), reaches about 2 psig to about 30
The range of psig.During operation, second part conduct at a temperature of this pressure and about -205 °F to about -255 °F
Steam leaves the second passage of second heat exchanger 124 (at 156).
Fluid circuit 102 can be such that the steam from second heat exchanger 124 is combined with stream 158.This feature can be main
The upstream of heat exchanger 114 forms " evaporation " vapor stream.The example of stream 158 may include evaporation steam from storage tank and/or
The steam that process from storage facility 110 generates.Typically, 158 pressure is flowed to be in relative into 104 pressure of becoming a mandarin
" low " pressure.This pressure may depend on the specification at storage facility 110, it can be required from about 1 psig (or " not pressurizeing ") extremely
The pressure of about 30 psig (" pressurization ").As discussed above, the second throttling device in fluid circuit 102 can construct
The pressure match of Cheng Yuliu 158.
Fluid circuit 102 can will come from the first container 122 and the second heat via the individual passage of principal heat exchange 114
The vapor stream of exchanger 124 is directed to compression unit 118.Vapor stream from the first container 122 can enter principal heat exchange
114 the second passage.The third passage of principal heat exchange 114 can be entered by evaporating vapor stream.In second passage and third passage
Each keep corresponding rheology warm so that stream leaves at a temperature of about 90 °F to about 110 °F (at 160,162).
In one implementation, within about 3 °F of the attemperator that this temperature can also be found in compression circuit 128,130.
Evaporation vapor stream from third passage can be directed to the first compression circuit 128 by fluid circuit 102.First compression
The construction in circuit 128 can have one or more compression stages, so that the pressure of evaporation vapor stream is increased from " low " pressure of stream 158.
But for many applications, two grades and/or three grades can be suitable.In an implementation, vapor stream is evaporated
It can be from about 90 psig to leaving last compression stage under the pressure of about 150 psig (at 164).
Evaporation vapor stream can be directed to the second compression circuit 130 by fluid circuit 102 under this pressure.Second compression and back
Road 130 may include one or more compression stages.But for many applications, two grades and/or three grades can be suitable
's.The compression stage of second compression circuit 130 can be independent or be to separate with the compression stage of the first compression circuit 128.This
A application for discussing the system 100 entirely or partly combined for being also contemplated by the grade that can benefit from compression circuit 128,130.
In one implementation, fluid circuit 102 is flowed in combination with evaporation vapor stream and " recycling " from methane expander 120.Knot
Conjunction can occur in the upstream of the second compression circuit 130, to generate the combination vapor stream into the second compression circuit 130.At one
In implementation, vapor stream can be last (at 168) from about 550 psig to leaving under the pressure of about 600 psig
Compression stage.
Compressed vapour stream can be directed to turbo-compressor 134 by fluid circuit 102 under this pressure.This equipment can structure
Cause to further increase the pressure of compressed vapour stream.In an implementation, compressed vapour stream can in about 1200 psig or
The turbo-compressor 134 (at 170) is left under lower pressure.This upper limit of pressure or " pole top " can be used to flange rank
Remain 600 pounds or lower.
Compressed vapour stream from turbo-compressor 134 can be directed to the of principal heat exchange 114 by fluid circuit 102
Four-pass.This four-pass provides refrigerating function to principal heat exchange 114.In an implementation, fluid circuit 102
It may be configured with the cooler (or similar device) being placed between principal heat exchange 114 and turbo-compressor 134.This cooler
Compressed vapour stream can be made to cool down so that compressed vapour stream enters four-pass at a temperature of about 110 °F (at 172).But
It is that this temperature can change in the range of about 90 °F to about 110 °F.Compressed vapour stream can be in optimization principal heat exchange
Four-pass is left at a temperature of refrigeration in 114.This temperature can be in about -20 °F to about 40 °F of range.
Cooled vapor stream from four-pass can be directed to turbine expander 136 by fluid circuit 102.This equipment is transported
Behavior make vapor stream from about 90 psig to the pressure of about 150 psig and than leave principal heat exchange 114 (
At 148 and 176) cold about 3 °F of vapor stream at a temperature of leave (at 174).It is worth noting that, the pressure of vapor stream
(at 174) and the pressure in the exit for the first throttle valve being discussed above are equal or essentially identical (at 150).Fluid circuit
102 can be directed to expanding vapor stream the 5th passage of principal heat exchange 114.This 5th passage is in principal heat exchange
Additional refrigeration is provided at 114.As mentioned above, fluid circuit 102 holds in combination with expanding vapor stream with from first
The vapor products overhead of device 122 is flowed with formation " recycling " for being used in the second compression circuit 130.
Fluid circuit 102 may be configured to flow from the compression for leaving the second compression circuit 130 to form " releasing " stream.In the runtime
Between, this " releasing " stream can be directed to first throttling device by fluid circuit 102 via the 6th passage of principal heat exchange 114
(for example, throttling set 146).In an implementation, fluid circuit 102 may include in the second compression circuit 130 and turbine
Flow control valve (or similar device) between compressor 134.Flow control valve may be in response to the flow rate of the steam in fluid circuit 102
Variation operation." releasing " stream can leave the 6th passage (at 176) at a temperature of from about 90 °F to about 110 °F, and
And (for example, under from about 90 psig to the range of about 150 psig) leave first under the pressure less than first pressure
Throttling set (at 178).
Fig. 3 depicts the example for the additional member that can help to realize liquefaction system 100.Fluid circuit 102 may include detaching
Unit 180, to be fed 104 removal of impurities (for example, heavy hydrocarbon) from entrance.The example of separative element 180 may include pairs of container
(for example, second container 182 and third container 184).Third container 184 may also benefit from using one or more peripheral members
(for example, peripheral member 186).The example of peripheral member 186 may include pump, boiler, heater and can be conducive to container 182,184
One or more of operation similar device.In an implementation, peripheral member 186 can be presented as boiler, it joins
Connect third container 184 and piping 188 and/or similar ancillary equipment (for example, pipeline, tank etc.).
Fluid circuit 102 may be configured to connection principal heat exchange 114 and separative element 180.This construction can will come from
The feed 104 that enters of first passage is directed to the 4th throttling set (for example, throttling set 146).This 4th throttling set can
It is lowered into the pressure of feed 104 so that enter feed 104 and left under the pressure less than 720 psig (at 190).It is based on
Into the ingredient of feed 104, this expansion stages can be necessary.For example, expansion stages may be configured to make from container 182,184
The pressure of product remains under the critical pressure of impurity (for example, heavy hydrocarbon) found in the ingredient for entering feed 104 or is less than
The critical pressure.This construction allows container 182,184 to run under low pressure, and the ingredient to ensure bottom product is miscellaneous rich in these
Matter.
Fluid circuit 102 can processing enters feed 104 under a reduced pressure in container 182.These processes can be formed
It is respectively at the top product and bottom product of vaporous form and liquid form.In an implementation, fluid circuit 102 can
Liquid bottoms product from second container 182 is directed to third container 184.5th throttling set is (for example, throttling set
146) it can be used to further decrease the pressure and/or temperature of the liquid bottoms product of 184 upstream of third container.Liquid bottoms product
Can be left at a temperature of from about 200 psig to the pressure of about 250 psig and from about -80 °F to about -120 °F
Five throttling sets (at 192).The example of third container 184 is operable to stabilizer to remove lighter hydrocarbons, to be formed for storage
For " stabilization " liquid bottoms product.This liquid bottoms product can be liquid petroleum product (LPG).In use, stablize
Tower 184 can be processed from standard pipe size and be used for large-scale output speed.In one example, stabilizer can be used ten
Two pallets so that vapor products overhead meets the specification of LNG product 108.Fluid circuit 102 may include condenser, but this
Construction may not be necessary, because stabilizer, Er Qiezheng can be entered at a temperature of less than about -100 °F by entering feed 110
Gas top product can leave stabilizer at -50 °F or at hotter temperature.
Vapor overhead product from container 182,184 can be directed to the only of principal heat exchange 114 by fluid circuit 102
Vertical passage.These vapor overhead products can have the ingredient for the specification for meeting LNG product 108.In an implementation, come
The 7th is left from the temperature of the vapor overhead product of second container 182 in the range from about -80 °F to about -120 °F
Passage (at 194).Vapor overhead product from stabilizer 184 can be in the upstream of the 6th passage of principal heat exchange 114
It is combined with " releasing " vapor stream from methane expander 120.In this respect, fluid circuit 102 may include the 6th throttling set
(for example, throttling set 146), with reduce let off steam stream in pressure and with the vapor overhead product from stabilizer 184
Pressure match.On the other hand, if the pressure for stream of letting off steam is higher than the pressure for entering feed 104, stream of letting off steam can be with
It is combined into feed 104.
Fig. 4 depicts the example of liquefaction system 100.Storage facility 110 may include the 4th container 196 and tank 198.Section five,
Stream device (for example, throttling set 146) can be used to reduce the pressure and/or temperature of the LNG product 108 of 196 upstream of the 4th container.
In one example, LNG product 108 can be from about 2 psig to leaving the 5th throttling set under the pressure of about 30 psig
(at 199).Temperature can change in the range from about -250 °F to about -265 °F.Process in 4th container 196 can
Top product and bottom product are formed, each is in vaporous form and liquid form.Liquid bottoms product can transport tank
198.In an implementation, the vapor overhead product from the 4th container 196 and the boil-off gas from tank 198 can be formed
Stream 158, fluid circuit 102 makes stream 158 be combined with from the stream of sub-cooling unit 116.
Fig. 5 depicts the example of compression circuit 200.This example can be used to realize compression circuit 138, one of 140
Or both (Fig. 2,3 and 4).Compression circuit 200 has first end 202 and the second end 204.End 202 can be handed over main heat
Parallel operation 114 couples.When as the second compression circuit 130, the second end 204 can couple with turbo-compressor 134.
Compression circuit 200 may be configured to improve pressure, without making the process streams from first end 202 to the second end 204
116 temperature increases.This function may be embodied in various components (for example, cooler, compressor etc.).In an implementation
In, compression circuit 200 may include the container 206 at first end 202 (or " entrance ").The example of container 206 can be presented as
Attemperator or similar device make it less overheat to be lowered into the temperature of gas.This device can with tool there are one or it is more
The compressed path 208 of a compression stage (for example, the first order 210, the second level 212 and third level 214) couples.Nominally Ge Geji
It may include cooler 216 and compressor 218.The example of cooler 216 can be air-cooled type, but the disclosure is not limited to select
It selects any specific type or does not limit the variation of these devices.Compressor 218 can be by gas, motor and turbo-driven dress
It sets, is arranged between the cooler 216 of adjacent compression stage 210,212,214, keep and/or carry as noted herein
The pressure of high process streams 116.The quantity of compression stage may depend on application, and wherein system 100 a implementation is configured to make
The first compression circuit 138 tool there are two grade or three grades and the second compression circuit 140 tool, there are three grades.
Fig. 6 depicts the flow chart for making to enter the exemplary embodiment for being fed liquefied process 300.Process 300 can
Including at the stage 302 mixed phase flow will be flashed to from the vapor stream for entering feed.Process 300 may also include, in the stage
At 304, mixed phase flow is separated into first-class and second.Process 300 may include, at the stage 306, the second streaming is led to
Over-heat-exchanger, and at the stage 308, the first part of second is guided to form liquid natural gas (LNG) product, and
At the stage 310, second part and boil-off gas are mixed.Mixed phase flow can be between the first pressure and evaporation for entering feed
Intermediate pressure between the second pressure of gas.In an implementation, process 300 may include, at the stage 312, by
The first-class and second part with boil-off gas is compressed into the third pressure more than first pressure.Process 300 may also include, in rank
At section 314, make first-class and second part with boil-off gas from third pressure expansion to intermediate pressure.Then process 300
It may be configured to return to the stage 314, to be effectively formed the circulation loop that can be used to provide refrigerating function at heat exchanger.
In an implementation, process 300 may also include, at the stage 316, released under third pressure it is first-class and with evaporation
A part for the second part of gas, and at the stage 318, the part is made to be flashed to intermediate pressure.Process 300 can be further
Including at the stage 320, the part and mixed phase flow are mixed under intermediate pressure.Then process 300 can return to the stage 304.
Also as shown in Figure 6, process 300 may include, at the stage 322, will enter feed and be separated into vapor stream and liquid stone
Oily (LPG) product.
More than considering, the process efficiency of some embodiments is more advantageous than nitrogen expander process, but more mixed than an equal amount of
It closes refrigeration system and needs more horsepower.Some embodiments include only single expander, it is than can be used two of concurrent working
Certain system smallers of expander.In addition, unlike realizing the system of hybrid refrigeration process, some embodiments need not freeze
Agent, to eliminate the needs to the use of refrigerant, processing and scene storage.
It should understand that as used herein with odd number narration and with the element of word "one" or " one " beginning or with function
To be not excluded for the element or function of plural number, except non-clearly describing this exclusion.In addition, " one of invention to statement
The reference of embodiment " is not construed as excluding in the presence of the additional embodiment also in relation with the feature described.
The written description uses examples to disclose embodiment, including optimal mode, and also makes any technology people in this field
Member can put into practice embodiment, including manufacture and use any device or system, and the method for carrying out any combination.Embodiment
Patentable range is defined by the claims, and may include the other examples that those skilled in the art expect.If this
The other examples of sample have not different from the structural detail of the literal language of claim, or if they include and claim
Equivalent structural elements of the literal language without substantial differences, then they be intended to be within the scope of the claims.
Claims (20)
1. a kind of liquefaction system, including：
First heat exchanger；And
The fluid circuit coupled with the first heat exchanger, the fluid circuit are configured to make to enter feed from natural gas
Process streams cycle through the first heat exchanger, the fluid circuit includes：
The methane expander coupled with the first heat exchanger；
The sub-cooling unit coupled with the methane expander, the sub-cooling unit are configured to natural from process streams formation liquid
Gas (LNG) product；And
The first throttling device being placed between the first heat exchanger and the sub-cooling unit,
Wherein, the first throttling device is configured to that the process streams is made to be expanded into intermediate pressure, and the intermediate pressure is between institute
It states between the first pressure and the second pressure of the process streams for leaving the sub-cooling unit of feed.
2. liquefaction system according to claim 1, which is characterized in that the second pressure is from 1 psig to 30 psig
Range in.
3. liquefaction system according to claim 1, which is characterized in that the methane expander makes the process streams be expanded into
The intermediate pressure.
4. liquefaction system according to claim 1, which is characterized in that the fluid circuit is configured in the sub-cooling unit
Downstream and the first heat exchanger upstream receiving stream and it is mixed with the process streams.
5. liquefaction system according to claim 5, which is characterized in that the fluid circuit includes compression circuit, the pressure
Retraction road is configured to receive the process streams from the sub-cooling unit via the first heat exchanger.
6. liquefaction system according to claim 1, which is characterized in that the fluid circuit includes being placed in the first throttle
The first container between device and the sub-cooling unit, wherein the first container is configured to form first from the process streams
Stream and second, and wherein, the second forms the LNG product.
7. liquefaction system according to claim 1, which is characterized in that the sub-cooling unit includes second heat exchanger, institute
Second heat exchanger is stated to be configured to the process streams being cooled to the second temperature less than first temperature from the first temperature.
8. liquefaction system according to claim 7, which is characterized in that the second heat exchanger has the first passage and the
Two passages, and wherein, first passage is connected to second passage by the fluid circuit.
9. liquefaction system according to claim 8, which is characterized in that the fluid circuit includes being placed in first passage
Second throttling device between the second time, and wherein, the second throttling device is configured to make the process streams
Pressure reduction to the second pressure.
10. liquefaction system according to claim 1, which is characterized in that the liquefaction system further comprises and described
The second container of one heat exchanger connection is so that described be separated into steam and liquid into feed, wherein the fluid circuit warp
The steam is directed to the first throttling device from the second container by the first heat exchanger.
11. liquefaction system according to claim 10, which is characterized in that the liquefaction system further comprises and described
Two containers and the first heat exchanger connection third container so that the liquid from the second container be separated into steam and
Liquid, wherein the steam is directed to described by the fluid circuit via the first heat exchanger from the third container
First throttling device.
12. a kind of equipment, including：
First heat exchanger；And
The second heat exchanger coupled with the first heat exchanger,
Wherein, the equipment is configured to make to be originated from the fluid circulation into natural gas so that enters the second heat exchanger
Fluid is in intermediate pressure, and the intermediate pressure, which is less than the first pressure into natural gas and is more than, leaves described second
The second pressure of the fluid of heat exchanger.
13. equipment according to claim 12, which is characterized in that the equipment further comprises：
In the first throttling device that the downstream of the first heat exchanger and the upstream of the second heat exchanger couple, wherein
The first throttling device is configured to make fluid expansion to the intermediate pressure.
14. equipment according to claim 12, which is characterized in that the equipment further comprises：
In the second throttling device that the downstream of the second heat exchanger couples, wherein the second throttling device is configured to make
Fluid expansion is to the second pressure.
15. equipment according to claim 14, which is characterized in that the second heat exchanger includes the first passage and second
Passage, and wherein, the second throttling device setting is between first passage and the second time.
16. a kind of liquefaction process, including：
Make to be originated from into the vapor stream of feed and flashes to mixed phase flow；
The mixed phase flow is set to be separated into first-class and second；
The second is set to transport through heat exchanger；
The first part of the second is guided to form liquid natural gas (LNG) product；And
Second part and boil-off gas are mixed,
Wherein, the mixed phase flow is in intermediate pressure, and the intermediate pressure is between the first pressure for entering feed and institute
Between the second pressure for stating boil-off gas.
17. liquefaction process according to claim 16, which is characterized in that the liquefaction process further comprises：
Described first-class and with the boil-off gas the second part is compressed to the third more than the first pressure
Pressure.
18. liquefaction process according to claim 17, which is characterized in that the liquefaction process further comprises：
Make the described first-class and second part with the boil-off gas from the third pressure expansion to the centre
Pressure.
19. liquefaction process according to claim 17, which is characterized in that the liquefaction process further comprises：
A part for the second part described first-class and with the boil-off gas is set to be released under the third pressure；
The part is set to be flashed to the intermediate pressure；And
The part and the mixed phase flow are mixed under the intermediate pressure.
20. liquefaction process according to claim 19, which is characterized in that the liquefaction process further comprises：
By described the vapor stream and liquid petroleum (LPG) product are separated into feed.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201562210827P | 2015-08-27 | 2015-08-27 | |
| US62/210827 | 2015-08-27 | ||
| US14/985490 | 2015-12-31 | ||
| US14/985,490 US20170059241A1 (en) | 2015-08-27 | 2015-12-31 | Gas liquefaction system and methods |
| PCT/US2016/048780 WO2017035402A2 (en) | 2015-08-27 | 2016-08-25 | Gas liquefaction system and methods |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108351162A true CN108351162A (en) | 2018-07-31 |
Family
ID=58097831
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680049773.6A Pending CN108351162A (en) | 2015-08-27 | 2016-08-25 | Gas liquefaction system and method |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20170059241A1 (en) |
| EP (1) | EP3341667A2 (en) |
| CN (1) | CN108351162A (en) |
| AU (3) | AU2016310502B2 (en) |
| CA (1) | CA2995844A1 (en) |
| WO (1) | WO2017035402A2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112556311A (en) * | 2019-09-26 | 2021-03-26 | 乔治洛德方法研究和开发液化空气有限公司 | Gas liquefaction device |
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| JPH05203342A (en) * | 1991-01-25 | 1993-08-10 | Nippon Sanso Kk | Method and device for liquefying supercritical gas |
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| WO2007142668A1 (en) * | 2006-06-08 | 2007-12-13 | Conocophillips Company | Lng system with optimized heat exchanger configuration |
| US20130199238A1 (en) * | 2011-08-10 | 2013-08-08 | Conocophillips Company | Liquefied natural gas plant with ethylene independent heavies recovery system |
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| US4435198A (en) * | 1982-02-24 | 1984-03-06 | Phillips Petroleum Company | Separation of nitrogen from natural gas |
| US5036671A (en) * | 1990-02-06 | 1991-08-06 | Liquid Air Engineering Company | Method of liquefying natural gas |
| US6658890B1 (en) * | 2002-11-13 | 2003-12-09 | Conocophillips Company | Enhanced methane flash system for natural gas liquefaction |
| KR20130056294A (en) * | 2010-07-28 | 2013-05-29 | 에어 프로덕츠 앤드 케미칼스, 인코오포레이티드 | Integrated liquid storage |
| US9863697B2 (en) * | 2015-04-24 | 2018-01-09 | Air Products And Chemicals, Inc. | Integrated methane refrigeration system for liquefying natural gas |
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2015
- 2015-12-31 US US14/985,490 patent/US20170059241A1/en active Pending
-
2016
- 2016-08-25 AU AU2016310502A patent/AU2016310502B2/en active Active
- 2016-08-25 EP EP16764017.6A patent/EP3341667A2/en active Pending
- 2016-08-25 CN CN201680049773.6A patent/CN108351162A/en active Pending
- 2016-08-25 WO PCT/US2016/048780 patent/WO2017035402A2/en unknown
- 2016-08-25 CA CA2995844A patent/CA2995844A1/en active Pending
-
2021
- 2021-09-16 AU AU2021232758A patent/AU2021232758B2/en active Active
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2023
- 2023-02-13 AU AU2023200787A patent/AU2023200787A1/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3677019A (en) * | 1969-08-01 | 1972-07-18 | Union Carbide Corp | Gas liquefaction process and apparatus |
| JPH05203342A (en) * | 1991-01-25 | 1993-08-10 | Nippon Sanso Kk | Method and device for liquefying supercritical gas |
| CN1138960C (en) * | 2000-01-10 | 2004-02-18 | 普莱克斯技术有限公司 | Cryogenic industrial gases liquefaction system |
| WO2007142668A1 (en) * | 2006-06-08 | 2007-12-13 | Conocophillips Company | Lng system with optimized heat exchanger configuration |
| US20130199238A1 (en) * | 2011-08-10 | 2013-08-08 | Conocophillips Company | Liquefied natural gas plant with ethylene independent heavies recovery system |
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| CN112556311A (en) * | 2019-09-26 | 2021-03-26 | 乔治洛德方法研究和开发液化空气有限公司 | Gas liquefaction device |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2016310502A1 (en) | 2018-03-15 |
| EP3341667A2 (en) | 2018-07-04 |
| AU2016310502B2 (en) | 2021-06-24 |
| WO2017035402A3 (en) | 2017-05-18 |
| AU2021232758B2 (en) | 2023-04-06 |
| US20170059241A1 (en) | 2017-03-02 |
| AU2023200787A1 (en) | 2023-03-09 |
| CA2995844A1 (en) | 2017-03-02 |
| AU2021232758A1 (en) | 2021-10-14 |
| WO2017035402A2 (en) | 2017-03-02 |
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Application publication date: 20180731 |