CN102239377B - The method and system of the liquefied natural gas (LNG) production for optimizing - Google Patents
The method and system of the liquefied natural gas (LNG) production for optimizing Download PDFInfo
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- CN102239377B CN102239377B CN200980133223.2A CN200980133223A CN102239377B CN 102239377 B CN102239377 B CN 102239377B CN 200980133223 A CN200980133223 A CN 200980133223A CN 102239377 B CN102239377 B CN 102239377B
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 239000003949 liquefied natural gas Substances 0.000 title description 32
- 238000001816 cooling Methods 0.000 claims abstract description 35
- 239000003345 natural gas Substances 0.000 claims abstract description 33
- 239000003507 refrigerant Substances 0.000 claims abstract description 11
- 238000007906 compression Methods 0.000 claims abstract description 7
- 239000012530 fluid Substances 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 32
- 238000005057 refrigeration Methods 0.000 claims description 29
- 238000003860 storage Methods 0.000 claims description 18
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 230000001276 controlling effect Effects 0.000 claims description 2
- 230000000930 thermomechanical Effects 0.000 claims 2
- 230000004087 circulation Effects 0.000 description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 210000000038 chest Anatomy 0.000 description 11
- 238000000034 method Methods 0.000 description 11
- 239000000203 mixture Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 230000004301 light adaptation Effects 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 230000002349 favourable Effects 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000004781 supercooling Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000012536 storage buffer Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M buffer Substances [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000000969 carrier Substances 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 230000004899 motility Effects 0.000 description 2
- 229910052756 noble gas Inorganic materials 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000003466 anti-cipated Effects 0.000 description 1
- 239000007853 buffer solution Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000000295 complement Effects 0.000 description 1
- 230000000875 corresponding Effects 0.000 description 1
- 230000001808 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000001419 dependent Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000001131 transforming Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
A kind of method and system for the cooling assembly production fluid in next life by means of the single-phase gaseous refrigerant of use and overcooled natural gas, this cooling assembly includes: at least two decompressor (1 3)；Compressor assembly (5 7)；For from the heat exchanger assembly (8) of absorbing natural gas heat；And radiating subassembly (10 12).Novel feature according to the present invention is: arrange decompressor (1 3) in decompressor loop；A kind of and identical cold-producing medium is only used in all loops；Being delivered in heat exchanger assembly (8) by the cold-producing medium stream of the expansion from each decompressor, each decompressor is all in being suitable for close phase being de-superheated, condense or being cooled down and/or natural gas carries out overcooled quality stream and temperature levels；And by means of compressor assembly, in the stream of compression, providing cold-producing medium to each decompressor, this compressor assembly has compressor or compressor stage, it is achieved that for the inlet pressure being suitable for and the outlet pressure of each decompressor.
Description
Background technology
Energy requirement in the world increases, and is predicted as continuing to increase.As energy carrier natural gas in recent years
Receive more and more attention, and anticipated natural gas will become more important.For long-distance transmissions natural gas, liquefy sky
So gas LNG is often thought of as optimal selection, especially in foreign country.
Be difficult to dispose (stranded) natural gas or associated gas as the gas from Petroleum Production " garbage "
Source.Seldom these sources of the gas are utilized at present.Generally they are burnt.Along with the rise of Gas Prices with to environment
These sources are utilized and become more feasible economically and the most also become more important by more concerns.These
Source is the most all marine, and, the liquefaction on floating production storage offloading's FPSO unit is optimal under many circumstances
Select.FPSO provides motility, this is because FPSO can relatively easily move to other source.The challenge of FPSO is can
Space.Additionally, the weight of equipment also should be made to minimize, and cold-producing medium should be preferably non-flammable.
Major issue during LNG produces is energy requirement.Produce the high energy requirement of every kilogram of LNG, i.e. specific consumption, make
Its most lucrative and less environmental protection.The quantity of economically feasible source of the gas can diminish.Relatively low energy requirement rate is removed
Outside reduction running cost, cost of also reducing investment outlay, this is because equipment will be less.
Land LNG produces does not has same restriction for weight and space, but the LNG of energy efficient produces as being but
Important.Along with place capacity becomes increasing, energy efficiency also becomes more and more important.
Generally in cascade arrangement, relate to the technology of multi-component refrigrant MCR be considered as LNG produce the most efficient
Technology.This technology is generally used in bigger equipment, base load equipment, and is used in medium-scale setting to a certain extent
In Bei.Due to its complexity, therefore MCR technology costly and also control the slowest.In addition, it is necessary to gas supplements (make-up) group
Part guarantees being correctly composed of MCR cold-producing medium.It is a further drawback that cold-producing medium is flammable, this is probably a problem, especially
At sea in facility.
If the Refrigeration Technique of one pack system using noble gas (such as nitrogen) can be to compare energy efficient, it will be
Cost, compactedness, weight, robustness, control and safety aspect show and are markedly improved.So, in large-scale equipment
It also can be interesting for realizing this technology.
United States Patent (USP) 5.768.912 and 5.916.260 propose the work that LNG based on nitrogen list refrigerant technology produces
Skill.This cold-producing medium is divided into the separate stream of at least two, and the separate stream of the two is carried out in the separate decompressor of at least two
Cooling and expansion.Each stream is inflated until the suction pressure of compressor bank, the namely minimum refrigerant pressure in device, because of
This, can use energy more more than necessary energy.
United States Patent (USP) 6.412.302 describes a kind of LNG liquefaction package, and this assembly uses two independent expander refrigeration
Circulation, wherein, a circulation has methane or hydrocarbon mixture, and another circulation has nitrogen.Each circulation has one
Decompressor at different temperatures horizontal operation.Each in circulation can be individually controlled.Two separate cold-producing mediums are used to incite somebody to action
Need two cold-producing medium buffer systems.Inflammable cold-producing medium is used to also imply that restriction or extra equipment.
Industrial waste gas (process gas) is used to be authorized to as the MCR technique of cold-producing medium and several patents of device, example
Such as United States Patent (USP) 7.225.636 and European patent 1455152.Having in common that of these patents, heat absorption includes cold-producing medium
Phase transformation, this gives more complicated system inherently.Thus need more equipment, and control to become complicated and sensitive.
Need efficient technique based on inert one-component refrigerant.The present invention describes use noble gas conduct
Cold-producing medium, there is flexibly control, energy efficient compact LNG produce assembly.
Summary of the invention
The present invention relates to the method and system that a kind of LNG for optimizing produces.In order to make specific consumption minimize, need to make
Heat exchanger minimization of loss.This is by arranging at least two decompressor in one or more one pack systems and single-phase kind of refrigeration cycle
Realize, in order to can control respectively to enter the quality stream of decompressor, temperature and pressure level.By such layout, system
Cold process can be suitable under different pressure and temperatures the gas composition of change, and can make efficiency optimization simultaneously.Should
Control be inherently robust and flexibly.LNG according to the present invention produces equipment can be suitable for different sources of the gas, and simultaneously
Low specific consumption can be kept.
In an aspect, the present invention relates to a kind of for by means of use single-phase gaseous refrigerant cooling assembly next life
Production fluid and overcooled natural gas method, this cooling assembly includes: two or three decompressors；Compressor assembly；With
In the heat exchanger assembly from absorbing natural gas heat；And radiating subassembly, and additionally, the method includes: at two or three
Arranging decompressor in decompressor loop, each decompressor is independently controlled；A kind of and identical system is only used in all loops
Cryogen；The cold-producing medium stream of the expansion from each decompressor is delivered in heat exchanger assembly, wherein in the feelings of two decompressors
Under condition: the cold-producing medium stream from the first decompressor is in the quality stream being de-superheated, condense and cooling down of the close phase of applicable natural gas
And temperature levels, and it is in overcooled quality stream and the temperature water of applicable natural gas from the cold-producing medium of the second decompressor
Flat；In the case of three decompressors: the cold-producing medium stream from the first decompressor is in the quality being de-superheated of applicable natural gas
Stream and temperature levels, the cold-producing medium stream from the second decompressor is in the condensation of the close phase of applicable natural gas and the quality stream of cooling
And temperature levels, and it is in overcooled quality stream and the temperature water of applicable natural gas from the cold-producing medium of the 3rd decompressor
Flat；And by means of compressor assembly, in the stream of compression, providing cold-producing medium to each decompressor, this compressor assembly has pressure
Contracting machine or compressor stage, it achieves the inlet pressure being suitable for for each decompressor and outlet pressure.
In another aspect, the present invention relates to a kind of for by means of use single-phase gaseous refrigerant cooling assembly next life
Production fluid and overcooled natural gas system, this cooling assembly includes: two or three decompressors；Compressor assembly；With
In the heat exchanger assembly from absorbing natural gas heat；And radiating subassembly, wherein, decompressor is arranged in two or three decompressors
In loop, each decompressor is independently controlled；All decompressor loops include identical cold-producing medium；Swollen from each decompressor
Swollen cold-producing medium stream is passed in heat exchanger assembly, and wherein, heat exchanger assembly includes for being de-superheated of close phase, condenses and cold
But and overcooled independent path, each path all in applicable natural gas being de-superheated, condense or cool down of close phase,
And overcooled quality stream and temperature levels；And by means of compressor assembly, carry to each decompressor in the stream of compression
For cold-producing medium, this compressor assembly has compressor or compressor stage, and it achieves applicable the entering for each decompressor
Mouth pressure and outlet pressure.
Dependent claims is described in detail preferred embodiment.
The outlet pressure of decompressor is controlled so as to the highest, and simultaneously to the heat exchanger produced for overcooled LNG
Device is presented with required cryogenic temperature.Then, the suction pressure keeping each compressor stage is the highest.This is with prior art not
With, see for example United States Patent (USP) 5.916.260, wherein, all streams all be inflated until minimum refrigerant pressure.The present invention's is main
It is improved by making than merit amount (specific work volume) and minimizing than suction volume of compressor, thus improves overall system
System efficiency.Line size is reduced, thus valve and actuating device (actuator) are less.All of these factors taken together contributes to significantly
Ground reduces cost and space requirement.Installment work also can become more uncomplicated thus more efficient.
Reduce heat exchanger be lost in K cryogenic treatment it is critical that.The important embodiment of the present invention is that it passes through
Make process of refrigerastion be suitable for main three different stages that LNG produces, the temperature difference be reduced to minimum: be de-superheated, condense (super
The cooling of the close phase under critical pressure) and supercooling.This is different from prior art, such as United States Patent (USP) 6.412.302, its
Close phase is de-superheated and condenses/cool down not there is adaptation respectively.
The single cold-producing medium using gas phase is operated by the present invention.Nitrogen is obvious alternative.Non-flammable is in such as sea
Upper facility is considered as advantage.A kind of one-component refrigerant is only used to also reduce complexity.
Accompanying drawing explanation
Accompanying drawing shows the preferred embodiments of the present invention.
Fig. 1 shows the principle stage of liquefied natural gas (LNG) production, and wherein, it is with three straight lines that corresponding cooling capacity needs
Represent.
Fig. 2 shows warm build-up curve and the example of cold build-up curve of the present invention.
Fig. 3 depicts the embodiment including three decompressors of the present invention.
Fig. 4 shows the further embodiment including being arranged in three decompressors in three separate kind of refrigeration cycle.
Fig. 5 shows the embodiment only including two decompressors.
Fig. 6 depicts similar to Fig. 5 but decompressor is arranged in the embodiment in separate kind of refrigeration cycle.
Fig. 7 shows the embodiment allowing to shunt cold-producing medium stream and merge.
Fig. 8 shows a part of Fig. 7, and wherein, at least one in Fig. 3 to decompressor illustrated in fig. 6 is provided with string
The decompressor of connection coupling.
Detailed description of the invention
The present invention relates to the production of liquefied natural gas LNG.Depending on source of the gas, composition can difference.Such as, gas composition is permissible
Including: the methane of 88%, the heavy hydrocarbon of 9%, the carbon dioxide of 2% and the water of 1%, nitrogen and other minimum gas.In liquefaction
Before, need carbon dioxide, water (will freeze) and harmful minimum gas (such as H2S) concentration is reduced to acceptable
Level, or it is removed from air-flow.Gas well gas, will be through pre-treatment step before entering liquefaction step.At Fig. 3 to Fig. 6
In, represent this pretreated natural gas flow by reference 9.
The process that LNG produces can be largely classified into three different stages: A) it is de-superheated；B) condensation；And C) supercooling,
See the schematic outline in Fig. 1.The critical pressure of methane is about 46 bars.Critical pressure depends on that the composition of gas source will
Upwards change from 46 bars.More than the critical pressure of natural gas composition, condensation is impossible.But, replace condensation, natural
The stage that gas will increase through specific heat capacity.
Each stage is required for different ratio cooling capacities (specific cooling capacity).Change to reduce
The loss of hot device, it is necessary to make the temperature difference between warm current and cold flow in whole LNG production process minimize.Multiple swollen by utilizing
Swollen machine, wherein, each decompressor can control by quality stream, stress level and temperature respectively, can be at refrigeration capacity and cold
But close temperature adaptation is realized between needing.Fig. 1 represents the cooling capacity of three phases with three straight lines.Independent control
Decompressor the cooling capacity in each stage is made main contributions.The optimal number of decompressor will depend upon which source of the gas composition,
Gas pressure, required temperature and the capacity of LNG plant.
Fig. 3 shows the configuration according to the present invention.Three decompressors 1,2,3 (such as turbo-expander) provide to ice chest 8
The air-flow of the expansion of different temperatures, the air-flow of this expansion is suitable for the liquefaction process of natural gas flow 9.Compressor bank 5,6,7 is served
All these three decompressor.Decompressor 3 provides stream 60 to ice chest 8, and this stream 60 is adapted for carrying out the most supercool of natural gas flow 9
But, such as temperature range is down to-160 DEG C from-85 DEG C, sees Fig. 1.More than-85 DEG C, stream 60 is contributed limited in ice chest 8
Clean refrigeration capacity, this is because provided by decompressor 3 respectively and the quality stream 59 that returned and quality stream 61 equal.Expand
Machine 2 provides stream 56 to ice chest 8, and this stream 56 is suitably executed condensation or the cooling of the gas of high heat capacity, sees Fig. 1.The temperature of this process
Degree is interval between-85 DEG C and-25 DEG C.Decompressor 3, the quality stream 55 being provided by decompressor 2 respectively and being returned are provided
With quality stream 57, the cooling capacity of p-more than 25 DEG C had limited contribution.Decompressor 1 provides stream 52 to ice chest 8, this stream 52
It is adapted for carrying out being de-superheated so that be down to the higher operating temperature of decompressor 2 from the inlet temperature of natural gas flow 9, i.e.-25
℃.The quality stream reference 51,53 provided and returned represents.
Compressor 5,6,7 is installed in series to form compressor bank.Compressor bank can include the level of varying number, and often
Level has the compressor of one or more parallel connection.Pressure ratio on every grade is optimized to the temperature requirements in ice chest 8.These pressures
Force rate and quality stream can be by what the speed controlling of compressor was varied and controlled during operation.Hold such that it is able to adjust
Amount and temperature range.
By changing the total inventory in device, thus it is possible to vary overall stress level also controls total capacity.Storage Buffer Unit is even
It is connected to the suction side of low pressure compressor level and the waste side of high pressure compressor.Valve 32 and 34 passes to buffer container 25 for control
Send cold-producing medium.
Heat exchanger 10,11,12 discharges heat to surrounding.
Fig. 3 also show how different decompressors 1,2,3 is connected to the example of compressor bank 5,6,7.Decompressor 3 is presented
With the exit gas stream 58 from heat dissipation heat exchanger 11, and two other decompressor 1,2 is presented with from heat dissipation heat exchanger
The exit gas stream 50,54 of 10.Generally, by the application present invention, expander inlet pressure and outlet pressure can be made to fit
Close each decompressor.
Embodiment according to Fig. 3 shows that ice chest 8 is provided service by three separate decompressor loops.Due to example
Such as the mechanical requirements of ice chest assembly 8, so the cold-producing medium stream relevant with ice chest assembly 8 is shunted and merged is favourable.
Fig. 7 shows the example for shunting cold-producing medium stream and merge.In the upstream of decompressor, warm current 50 is split into stream 51
With stream 55.In the downstream of decompressor, cold flow 52 and 56 is merged into stream 54.By the upstream at decompressor, warm current is shunted,
And in the downstream of decompressor, cold flow is merged, it is possible to achieve process efficiently.But, this configuration has intrinsic lacking
Point, the single inlet pressure and the outlet pressure that are i.e. suitable for each decompressor are impossible.Reduce optimized energy effect
The potential of rate.
By application the present embodiment, all of compressor and decompressor are all integrated in same refrigerating plant.Thus give
Go out the potential realizing the solution closely for rotating equipment, thus reduce cost.Additionally, compressor stage 5,
6, each in 7 is drawn from three the different suction pressures formed by decompressor 1,2,3.By from maximum possible
Pressure, i.e. quality stream 61,57,53, draws so that compressor work minimizes, thus improves aggregate efficiency.
The suction volume of compressor is also minimized.The size of pipeline is reduced, thus valve and actuating device are less.Will be aobvious
Write ground reduction space requirement and cost will be lower.Installment work also will become less complicated and more efficient.
Mainly being improved by of energy efficiency employs three of three different phases being suitable for natural gas liquefaction separately
Decompressor circuit.This is different from prior art, such as, in United States Patent (USP) 6.412.302, do not have for close phase
The adaptation of the difference being de-superheated and condensing/cool down.The thermodynamic results of described system may refer to Fig. 3.Each by amendment
Quality stream, pressure ratio and the temperature of decompressor 1,2 and 3, can be by by the distance institute between cold build-up curve and warm build-up curve
The heat exchanger loss of instruction is reduced to minimum.
The cold-producing medium using gas phase is operated by this refrigerating plant.Nitrogen is gas to be applied, this is because
It has favourable attribute and is the cold-producing medium being proved to.The molal weight of nitrogen is more than the molal weight of methane.With
When turbocompressor, high molecular weight is favourable.United States Patent (USP) 6.412.302 proposes use methane or hydrocarbon mixing
Thing.Hydrocarbon is also inflammable, this in some applications, the most at sea it is considered to be shortcoming in facility.
Fig. 4 shows the second embodiment, and wherein, each in decompressor 1,2,3 operates in separate circulation, should
Circulation has the compressor configuration of their own.Decompressor 1,2,3 be respectively by compressor 13, compressor 14,15 and compressor 16,
17,18 supply.Compressor or the quantity of compressor stage in each circulation can change.As it is shown on figure 3, decompressor 1,
2, each in 3 will provide the refrigeration capacity in applicable different temperatures region to ice chest 8.
Separate circulation gives the motility of the improvement about pressure, temperature and quality flow control, i.e. different natural gass
The refrigeration capacity processing stage of liquefaction.Can control by storage respectively and compressor speed controls each circulation.Fig. 4
Show that storage controls the example of assembly.The separate circulation of these three is connected to storage buffer container 25, this storage buffer container
The 25 minimum high pressure being maintained below in circulation and the pressure higher than the high-low pressure in circulation.Valve 26 to 31 will be used for
Quality is transmitted between circulation and container 25.Although circulation works respectively, but they are mutual when being controlled device
Connect and complementary.Separate storage controls to give the probability of the overall stress level changed in each circulation.
Control thought makes the system with separate circulation be robust and can adapt to source of the gas stream and composition flexibly
Change and emergent situation.Possible shortcoming is probably the more compressor of needs.But, with the system shown in Fig. 3
Compare, mainly will not increase total suction volume.
As it is shown in figure 1, it is substantially favourable for using three decompressors during LNG produces.But, by using
Four or more decompressor can realize the most higher efficiency, and this is not shown.Reason is warm build-up curve and cold
Even preferably adaptation between build-up curve.In energy efficiency is conclusive large-scale equipment, it may be possible to accept
The complexity increased.
Fig. 5 with Fig. 6 shows the embodiment that LNG based on the principle identical with shown in Fig. 3 and Fig. 4 produces, but only has
Two rather than three decompressors.Fig. 5 depicts the example with public compressor bank, and Fig. 6 shows and includes separate following
The example of ring.In the case of shown two kinds, decompressor 3 is suitable for carrying out liquefied natural gas supercooling, and decompressor 2 be suitable for right
Dense gas carries out being de-superheated and condensing/cool down.Thus, decompressor 2 is used for producing liquefied natural gas, and decompressor 3 was used for
Cooling.Compared with the solution with three decompressors, warm adaptation between build-up curve and cold build-up curve will be poor,
But configure more uncomplicated.Compared with the embodiment with three decompressors, total compressor suction volume will not reduce, and this is
Because compressor 6,5 or 14, the inlet capacity of 15 must be increased, to process being de-superheated and condensing/cool down two of dense gas
Person.
As for having the described system of three decompressors, can be controlled by storage and compressor speed controls perform appearance
Amount controls.For separate circulation, see Fig. 6, can be with the stress level of independently controlled two circulations.It is by wrapping that storage controls
Include what the refrigerant quality buffer system of container 25 and valve 28,29,30 and 31 performed.Pressure in container 25 is kept
Less than the minimum high pressure in system and higher than the high-low pressure in system.Valve is for container transport quality with from container biography
Transmission quality.For the system of the connection in Fig. 5, container 25 and valve 32 and 34 arrange storage control.By change system
Product storage, thus it is possible to vary total stress level, and can be with control capability.Compressor speed change may be used for changing total appearance
Amount, but it is also used for the control respectively of each compressor stage, thus have an opportunity to change capacity on different stress levels.
Decompressor 2 in Fig. 5 and Fig. 6 provides cooling capacity in high temperature circulation.This cooling capacity can such as be passed through
Two decompressors of series connection provide, and see Fig. 8.Low pressure the most swollen of high temperature circulation it is being down to through the second decompressor 2b
Before swollen, first quality stream 55 will expand and be down to intermediate pressure in decompressor 2a, and carry out supercooling in ice chest 8.Multiple
Polygamy will somewhat increase, but this will improve energy efficiency.In principle, can be with the decompressor of two or more series connection
Replace any one in decompressor 1,2 and 3.
All solutions presented above are not limited to liquefied natural gas (LNG) production.Bog (is also considered as natural
Gas) re-liquefied be Another Application, wherein, the present invention can be used on such as marine LNG carrier and in land terminal.
Although being not shown, it will be understood that: more than three decompressor is applicable, such as four or
The most multiple.
Example:
The present invention the most as shown in Figure 3 is applied to typical gas source, depends on external condition, it is possible to achieve be big
The energy efficiency calculated of about 0.32kWh/kg LNG.Compared with prior art solution, this is to be markedly improved, such as root
According to United States Patent (USP) 6.412.302, under equal environmental condition and based on this description in proposed by operation data, it is had
The energy efficiency calculated having is 0.44kWh/kg LNG.
Claims (18)
1. one kind is used for by means of the cooling assembly production fluid in next life using single-phase gaseous refrigerant and overcooled natural gas
Method, described cooling assembly includes:
Two or three kind of refrigeration cycle, each kind of refrigeration cycle includes a decompressor in its decompressor loop；
Compressor assembly；
Heat exchanger assembly, for from absorbing natural gas heat；
Radiating subassembly；And
Storage container,
Described method feature is:
In two or three decompressor loops, arrange that described decompressor, each decompressor are independently controlled；
A kind of and identical cold-producing medium is only used in all decompressor loops；
The cold-producing medium stream of the expansion from each decompressor is delivered in described heat exchanger assembly, wherein,
-in the case of two decompressors:
Cold-producing medium stream from the first decompressor be in the close phase of applicable natural gas the quality stream being de-superheated, condense and cooling down and
Temperature levels, and overcooled quality stream and the temperature levels of applicable natural gas it is in from the cold-producing medium of the second decompressor；
-in the case of three decompressors:
Cold-producing medium stream from the first decompressor is in the quality stream being de-superheated and the temperature levels of applicable natural gas, from second
The cold-producing medium stream of decompressor is in the condensation of the close phase of applicable natural gas and the quality stream of cooling and temperature levels, and from
The cold-producing medium of three decompressors is in overcooled quality stream and the temperature levels of applicable natural gas；
And by means of described compressor assembly, in the stream of compression, provide described cold-producing medium, described compression to each decompressor
Thermomechanical components has compressor or compressor stage, it is achieved that for the inlet pressure being suitable for and the outlet pressure of each decompressor,
Wherein, each kind of refrigeration cycle in kind of refrigeration cycle is connected to described storage container, and
By using described storage container and valve to change cold-producing medium storage, the refrigeration controlling kind of refrigeration cycle independently of one another is held
Amount.
Method the most according to claim 1, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly form the integrated cooling assembly with separate decompressor loop.
Method the most according to claim 1, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly form integrated cooling assembly, wherein to the cold flow in the described decompressor loop relevant with described heat exchanger assembly
Merge.
Method the most according to claim 1, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly form integrated cooling assembly, wherein relevant with described heat exchanger assembly in the upstream pair of described decompressor described in
Warm current in decompressor loop shunts.
Method the most according to claim 1, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly forming integrated cooling assembly, wherein warm current is shunted by the upstream at described decompressor, and to described
The relevant cold flow of heat exchanger assembly merges.
Method the most according to claim 1, it is characterised in that each decompressor is connected to described compressor assembly, with
The most fluidly form separate kind of refrigeration cycle.
Method the most according to claim 1, it is characterised in that control each system is changed independently by separate storage
Described refrigeration capacity in SAPMAC method.
Method the most according to claim 7, it is characterised in that control described refrigeration by compressor speed and hold
Amount.
Method the most according to claim 1, it is characterised in that with intercooled, the series connection that have between decompressor level
Two or more decompressor connected replaces any one in described decompressor.
10. one kind is used for by means of the cooling assembly production fluid in next life using single-phase gaseous refrigerant and overcooled natural gas
System, described cooling assembly includes:
Two or three kind of refrigeration cycle, each kind of refrigeration cycle includes a decompressor in its decompressor loop；
Compressor assembly；
Heat exchanger assembly, for from absorbing natural gas heat；
Radiating subassembly；And
Storage container,
Described system features is:
In two or three decompressor loops, arrange that described decompressor, each decompressor are independently controlled；
All decompressor loops include identical cold-producing medium；
Cold-producing medium stream from the expansion of each decompressor is passed in described heat exchanger assembly, wherein, and described heat exchanger package
Part includes being de-superheated, condense and cooling down and overcooled independent path for close phase, and each path is natural all in being suitable for
It is de-superheated, condenses or cools down described in the close phase of gas and overcooled quality stream and temperature levels；
It is by mean of described compressor assembly to the cold-producing medium of each decompressor, provides in the stream of compression, described compression
Thermomechanical components has compressor or compressor stage, it is achieved that for the inlet pressure being suitable for and the outlet pressure of each decompressor；
Each kind of refrigeration cycle in kind of refrigeration cycle is connected to described storage container；And
By using described storage container and valve to change the cold-producing medium storage of kind of refrigeration cycle, control refrigeration independently of one another and follow
The refrigeration capacity of ring.
11. systems according to claim 10, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly form the integrated cooling assembly with separate decompressor loop.
12. systems according to claim 10, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly form integrated cooling assembly, wherein to the cold flow in the described decompressor loop relevant with described heat exchanger assembly
Merge.
13. systems according to claim 10, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly form integrated cooling assembly, wherein relevant with described heat exchanger assembly in the upstream pair of described decompressor described in
Warm current in decompressor loop shunts.
14. systems according to claim 10, it is characterised in that described decompressor is connected to described compressor assembly, with
The most fluidly forming integrated cooling assembly, wherein warm current is shunted by the upstream at described decompressor, and to described
The relevant cold flow of heat exchanger assembly merges.
15. systems according to claim 10, it is characterised in that each decompressor is connected to described compressor assembly, with
The most fluidly form separate kind of refrigeration cycle.
16. systems according to claim 10, it is characterised in that described refrigeration capacity passes through to divide in each kind of refrigeration cycle
The storage opened controls and is varied independently.
17. systems according to claim 16, it is characterised in that described refrigeration capacity is controlled by compressor speed
System.
18. systems according to claim 10, it is characterised in that any one in described decompressor is had decompressor
Two or more decompressor intercooled, that be connected in series between Ji is replaced.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NO20083740 | 2008-08-29 | ||
| NO20083740A NO331740B1 (en) | 2008-08-29 | 2008-08-29 | Method and system for optimized LNG production |
| PCT/NO2009/000302 WO2010024691A2 (en) | 2008-08-29 | 2009-08-27 | Method and system for optimized lng production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102239377A CN102239377A (en) | 2011-11-09 |
| CN102239377B true CN102239377B (en) | 2016-12-14 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5768912A (en) * | 1994-04-05 | 1998-06-23 | Dubar; Christopher Alfred | Liquefaction process |
| CN2766203Y (en) * | 2005-04-15 | 2006-03-22 | 林福粦 | Air separator for recovering cold energy of liquefied natural gas |
| EP1939564A1 (en) * | 2006-12-26 | 2008-07-02 | Repsol Ypf S.A. | Process to obtain liquefied natural gas |
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5768912A (en) * | 1994-04-05 | 1998-06-23 | Dubar; Christopher Alfred | Liquefaction process |
| CN2766203Y (en) * | 2005-04-15 | 2006-03-22 | 林福粦 | Air separator for recovering cold energy of liquefied natural gas |
| EP1939564A1 (en) * | 2006-12-26 | 2008-07-02 | Repsol Ypf S.A. | Process to obtain liquefied natural gas |
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