CN107208962A

CN107208962A - Dual mixed refrigerant systems

Info

Publication number: CN107208962A
Application number: CN201580059218.7A
Authority: CN
Inventors: J·L·赛特尔; T·D·米勒; D·D·米勒
Original assignee: Black and Veatch Holding Co
Current assignee: Black and Veatch Holding Co
Priority date: 2014-08-29
Filing date: 2015-08-04
Publication date: 2017-09-26
Also published as: SK242017A3; CA2959119A1; RU2017110052A3; MX2017002486A; BR112017003554A2; RU2696662C2; RU2017110052A; US20160061517A1; AU2015307117B2; WO2016032700A1; AR101557A1; CO2017002301A2; AP2017009786A0; AU2015307117A1

Abstract

There is provided for reclaiming the method and system that liquefied natural gas (LNG) flows from hydrocarbonaceous feed air-flow using dual closed loop mixed-refrigerant cycle.Specifically, method and system described herein can be used for by using the first refrigeration system and the second refrigeration system the efficiently and effectively liquefied methane from hydrocarbonaceous feed air-flow, and first refrigeration system and the second refrigeration system are in fluid communication with turbine expander and separator.

Description

Dual mixed refrigerant systems

Technical field

The present invention relates generally to the method and system for reclaiming liquefied natural gas (" LNG ") from gas containing hydrocarbon.More Exactly, the present invention, which is related generally to, includes the method and system of dual mixed refrigerant systems.

Background technology

In recent years, the demand of natural gas constantly increases.In many instances, it is found that natural gas is located remotely from the city of natural gas In the region of field.Except non-natural gas are located close enough to the position in market, then construction pipeline come transport natural gas be only it is feasible , otherwise natural gas must be transported by tank car etc..The transport of natural gas in vapour form needs sizable tank car Volume；Therefore, liquefaction is traditionally carried out to natural gas is used to store and transport.The method of use and its storage of liquefied natural gas It is well-known.When can obtain surplus natural gas when, natural gas can also be liquefied at point of use, but may with The point of use that future can be transported to is larger compared to required volume.Such storage can be used, for example, to be needed in winter peak value Seek the winter peak demand for meeting and exceeding by the available natural gas of existing pipe-line system during the cycle.Various other industry Using need by natural gas liquefaction for storage.

Before this, the material such as natural gas is for example, by those utilizations shown in the 4th, 033, No. 735 United States Patent (USP) The method of single mixed refrigerant is liquefied.Such method has many advantages better than other methods (for example, cascade system), Because they need less expensive equipment and control difficulty relatively low.Unfortunately, single mixed refrigerant method is contacted with level System, which is compared, needs more power to a certain extent.

Cascade system, for example, the system shown in the 3rd, 855, No. 810 United States Patent (USP), substantially utilizes multiple refrigeration Region, the refrigerant of its mid-boiling point reduction obtains gasifying providing cooling.However, cascade system is still under the behaviour of poor efficiency Make.

Although having been achieved with progress in liquefaction Technology of Natural Gas, still needed for operating efficiency and power consumption Improve.

The content of the invention

One or more embodiments described herein is related to the method for the gas containing hydrocarbon that liquefies.Methods described includes： (a) stream of entering by the first mix refrigerant and including gas containing hydrocarbon is incorporated into the first refrigeration system；(b) by with described Enter at least a portion of stream described in indirect heat exchange cooling first refrigeration system of one mix refrigerant so as to shape Enter stream into the first cooling；(c) it is by cooling down second refrigeration with the indirect heat exchange of second mix refrigerant First cooling in system enter at least a portion of stream to form the second cooling enter stream；(d) turbine expansion is made At least a portion for the entering stream expansion for entering stream or second cooling of first cooling described in device is so as to form expansion Enter stream；(e) at least a portion for entering stream of the expansion in separation separator is so as to form top layer vapor fraction and liquid State bottom fraction；(f) the top layer vapor fraction in first refrigeration system or second refrigeration system is cooled down extremely A few part；And (g) drives compressor with the turbine expander.

One or more embodiments described herein is related to the method for the gas containing hydrocarbon that liquefies.Methods described includes： (a) stream of entering by the first mix refrigerant and including gas containing hydrocarbon is incorporated into the first refrigeration system；(b) by with described Enter at least a portion of stream described in indirect heat exchange cooling first refrigeration system of one mix refrigerant so as to shape Enter stream into the first cooling；(c) it is by cooling down second refrigeration with the indirect heat exchange of second mix refrigerant First cooling in system enter at least a portion of stream to form the second cooling enter stream；(d) separator is separated In second cooling enter at least a portion of stream to form top layer vapor fraction and liquid bottom cut；And (e) at least a portion of first refrigeration system or the top layer vapor fraction in second refrigeration system is cooled down.

One or more embodiments described herein is related to the system for the gas containing hydrocarbon that liquefies.The system includes： (a) the first refrigeration system, it includes the first cooled region being disposed therein, wherein first cooled region is configured to lead to Cross and the cooling of the indirect heat exchange of the first mix refrigerant includes gas containing hydrocarbon enters stream so as to form the charging of the first cooling Stream；(b) the first closed loop hybrid refrigeration cycle, it is at least partially disposed in first refrigeration system, wherein described first Closed loop hybrid refrigeration cycle includes the first mix refrigerant；(c) the second refrigeration system, it connects with the first refrigeration system fluid It is logical, wherein second refrigeration system includes the second cooled region being disposed therein, wherein second cooled region is through matching somebody with somebody Put with by with the indirect heat exchange of the second mix refrigerant cools down first cooling enters stream so as to forming the second cooling Enter stream；(d) the second closed loop hybrid refrigeration cycle, it is at least partially disposed in second refrigeration system, wherein institute Stating the second closed loop hybrid refrigeration cycle includes second mix refrigerant；(e) turbine expander, it is with the described first refrigeration System or second refrigeration system be in fluid communication, wherein the turbine expander be configured so that it is described first cooling enter stream Or the stream of entering of second cooling is expanded into expansion stream；(f) separator, it is in fluid communication with the turbine expander, wherein The separator is configured to the flow separation that expands into top layer vapor fraction and liquid bottom cut；(g) conduit, it is used for At least a portion of the top layer vapor fraction is set to return to first refrigeration system or second refrigeration system；And (h) compressor, it is driven by the work(from the turbine expander at least in part, wherein the compressor is configured at least Partly compress first mix refrigerant, second mix refrigerant or the top layer vapor fraction.

Brief description of the drawings

Embodiments of the invention are described herein with reference to the following drawings, in the accompanying drawings：

Fig. 1 describes to be closed for reclaiming the dual of liquefied natural gas stream from feed stream according to one embodiment of present invention Ring mixed refrigerant systems；

Fig. 2 describes dual closed loop mixed refrigerant systems according to an embodiment of the invention, and the system includes：Connection Turbine expander, heavy substance separator and compressor to the first refrigeration system；

Fig. 3 describes dual closed loop mixed refrigerant systems according to an embodiment of the invention, and the system includes：Connection To the first refrigeration system turbine expander and heavy substance separator and be connected to the compression of the first closed loop hybrid refrigeration cycle Machine；

Fig. 4 describes dual closed loop mixed refrigerant systems according to an embodiment of the invention, and the system includes：Connection To the first refrigeration system turbine expander and heavy substance separator and be connected to the compression of the second closed loop hybrid refrigeration cycle Machine；

Fig. 5 describes dual closed loop mixed refrigerant systems according to an embodiment of the invention, and the system includes：Connection Turbine expander, heavy substance separator and compressor to the second refrigeration system；

Fig. 6 describes dual closed loop mixed refrigerant systems according to an embodiment of the invention, and the system includes：Connection To the second refrigeration system turbine expander and heavy substance separator and be connected to the compression of the first closed loop hybrid refrigeration cycle Machine；And

Fig. 7 describes dual closed loop mixed refrigerant systems according to an embodiment of the invention, and the system includes：Connection To the second refrigeration system turbine expander and heavy substance separator and be connected to the compression of the second closed loop hybrid refrigeration cycle Machine.

Embodiment

The described in detail below of embodiments of the invention with reference to accompanying drawing.The embodiment is intended to sufficient detailed description sheet The various aspects of invention are to enable those skilled in the art to put into practice the present invention.Can be using other embodiments and can To be changed on the premise of the scope of claims is not departed from.Therefore, it should not be considered as described in detail below with limit Meaning processed.The complete model for the equivalent that the scope of the present invention is only authorized by appended claims and this claims Enclose to define.

The present invention relates generally to the method and system for the gas containing hydrocarbon that liquefies to be consequently formed the liquefaction including methane Natural gas (LNG) flows.As described below, these method and systems can be aided in come self-contained using dual mixed refrigerant systems The liquefaction of the methane of appropriate hydrocarbon gas.The various implementations of dual mixed refrigerant systems are hereinafter further described according to Fig. 1 to Fig. 7 Example.

Now then referring to Fig. 1, there is provided the liquefied natural gas configured according to one or more embodiments of the invention (LNG) The schematic representation of recvery facility 10.Liquefied natural gas (LNG) recvery facility 10 can be exercisable so that what is entered is hydrocarbonaceous The significant portion condensation and supercooling of methane in gas feed stream, method is with the first refrigeration system 12 and the second refrigeration system 14 Cooling gas.According to various embodiments of the present invention, it be describe hereinafter referring to figs. 1 to Fig. 7 on liquefied natural gas (LNG) The additional detail of configuration and the operation of recvery facility 10.

As shown in figure 1, gas containing hydrocarbon, which enters stream, initially to introduce liquefied natural gas (LNG) recovery by conduit 110 In facility 10.Gas containing hydrocarbon can be any suitable hydrocarbonaceous fluid stream, for example, for example, natural gas flow, synthesis gas Stream, cracking air-flow, the associated gas from Petroleum Production, or its combination.In conduit 110 a variety of gas can be derived from containing hydrocarbon stream Body source (not shown), including (but not limited to)：Natural gas line distribution network；Hydrocarbon producing well；Unconventional gas production unit；Stone Oily chemical treatment；Coal bed processing unit；Refinery's processing unit, for example, fluidized catalytic cracker (FCC) or petroleum coke Change equipment；Or heavy oil processing unit, for example, oil sands upgrader.

Depending on its source, gas containing hydrocarbon can include different amounts of methane, nitrogen, hydrogen, carbon monoxide, titanium dioxide Carbon, sulfur-bearing species, and other hydro carbons.For example, gas containing hydrocarbon can include at least 1,5,10,15 or 25 and/or be no more than 99th, the methane of 95,90,80,70 or 60 molar percentages.More precisely, gas containing hydrocarbon can be arrived including scope 1 to 99,5 95th, 10 to 90,15 to 80, or 25 to 70 molar percentages methane.It should be noted that all molar percentages be all based on it is hydrocarbonaceous The total moles of gas.

In various embodiments, gas containing hydrocarbon from including few hydrogen to not include hydrogen.For example, gas containing hydrocarbon can With the hydrogen including less than 10,5,1 or 0.5 molar percentage.

In various embodiments, gas containing hydrocarbon can from including few carbon monoxide to not include carbon monoxide.Citing comes Say, gas containing hydrocarbon can include the carbon monoxide no more than 20,10,5 or 1 molar percentage.

In various embodiments, gas containing hydrocarbon can from including few nitrogen to not include nitrogen.For example, containing the hydrocarbon gas Body can include the nitrogen no more than 20,10,5 or 1 molar percentage.

In various embodiments, gas containing hydrocarbon can from including few carbon dioxide to not include carbon dioxide.Citing comes Say, gas containing hydrocarbon can include be no more than 20,10,5, or 1 molar percentage carbon dioxide.

In various embodiments, gas containing hydrocarbon, to sulfur-containing compound is not included, can contain from including few sulfur-containing compound Sulphur compound includes any compound containing sulphur.For example, gas containing hydrocarbon can include no more than 20,10,5 or 1 moles The sulfur-containing compound of percentage.

In addition, gas containing hydrocarbon can include same amount of C₂-C₅Component, it includes paraffin and its alkene isomer.Lift For example, gas containing hydrocarbon can include the C less than 30,25,15,10,5 or 2 molar percentages₂-C₅Component.

In addition, gas containing hydrocarbon can include same amount of C₆₊Component, it includes the carbon chain length with least six carbon atom Compound and paraffin and its alkene isomer based on hydro carbons.For example, gas containing hydrocarbon can include less than 30,25, 15th, 10,5, or 2 molar percentages C₆₊Compound.

In addition, gas containing hydrocarbon can include same amount of impurity, for example, for example, benzene, toluene and dimethylbenzene (“BTX”).For example, gas containing hydrocarbon can include the BTX components less than 30,25,15,10,5,2 or 1 molar percentage.

As shown in figure 1, the gas containing hydrocarbon in conduit 110 can initially be guided to pretreatment zone 16, wherein can be One or more undesirable components are removed before cooling from gas.In one or more embodiments, pretreatment zone 16 can include one or more vapor liquid separation vessels (not shown), for removing aqueous water or hydrocarbon from feed gas Class component.Optionally, pretreatment zone 16 can remove region (not shown) comprising one or more gases, for example, example Such as, amine unit (amine unit) or molecular sieve, for removing carbon dioxide and/or Containing Sulfur from the air-flow in conduit 110 Compound.

The treated air-flow for leaving pretreatment zone 16 by conduit 112 can then be guided to dewatering unit 18, Essentially all of residual water can be wherein removed from feed stream.Dewatering unit 18 can be removed using any of water System, for example, for example, the bed of molecular sieve.Once through drying, the air-flow in conduit 114 can have at least 5,10 or 15 DEG C and/or no more than 50,45 or 40 DEG C of temperature.More precisely, air-flow in conduit 114 can have 5 to 50 DEG C, 10 Temperature in the range of 45 DEG C or 15 to 40 DEG C.Additionally or alternatively, the air-flow in conduit 114 can have at least 1.5, 2.5th, 3.5 or 4.0 and/or no more than 9.0,8.0,7.5 or 7MPa pressure.More precisely, air-flow in conduit 114 can be with With the pressure in the range of 1.5 to 9.0,2.5 to 8.0,3.5 to 7.5 or 4.0 to 7.0MPa.

As shown in figure 1, the hydrocarbon containing feed stream in conduit 114 be directed into the first cooling zone of the first refrigeration system 12 The first cooling duct 22 in domain 20.As described further below, the first refrigeration system 12 can be exercisable to pass through Indirect heat exchange cooling and any heat friendship of the feed stream in condensation pipe 114 at least in part with the first mix refrigerant The series connection of parallel operation or heat exchanger.In one or more embodiments, the first refrigeration system 12 can be brazing aluminium heat exchanger, It includes the multiple coolings being disposed therein and heating passage (for example, core), for promoting one or more processing streams and one Indirect heat exchange between individual or multiple cold-producing medium streams.

By the hydrocarbonaceous feed air-flow of the cooling duct 22 of the first cooled region 20 can by with refrigerant heat passage The indirect heat exchange of the first mix refrigerant in 24 is cooled down, and this is hereinafter described in further detail.Such as institute herein Use, term " mix refrigerant " refers to the refrigerant composition for including two or more composition.

Air-flow in conduit 116 can be subsequently introduced into second in the second cooled region 26 of the first refrigeration system 12 In cooling duct 28.In various embodiments, can be with by the hydrocarbonaceous feed air-flow of the cooling duct 28 of the second cooled region 26 Cooled down by the indirect heat exchange with the first mix refrigerant in refrigerant heat passage 30, this is hereinafter further It is described in detail.In certain embodiments, at least a portion of methane component can be cold from gas phase during cooling in feed stream It is solidifying to come out thus to provide the two-phase fluid stream of the cooling in conduit 118.Alternatively, in certain embodiments, the second cooling zone Fluid stream obtained by domain 26 will not be condensed in the methane component in feed stream and conduit 118 will be single-phase vapor stream.

Air-flow in conduit 118 can be subsequently introduced into the 3rd in the 3rd cooled region 32 of the first refrigeration system 12 In cooling duct 34.In certain embodiments, can be with by the hydrocarbonaceous feed air-flow of the cooling duct 34 of the 3rd cooled region 32 Cooled down by the indirect heat exchange with the first mix refrigerant in refrigerant heat passage 36, this is hereinafter further It is described in detail.In various embodiments, at least a portion of the methane component in feed stream can from vapor condensation out with Thus the two-phase fluid stream of cooling in conduit 120 is provided.In one or more embodiments, it is incorporated into the first refrigeration system 12 In the percentage of at least 5,10,25,50,60,70,80 or 90 of total amount of methane can work as cold when leaving three cooled regions 32 It is solidifying.Alternatively, in certain embodiments, the 3rd cooled region 32 will not condense the methane component and conduit in feed stream Fluid stream obtained by 120 will be single-phase vapor stream.

As shown in figure 1, the hydrocarbon containing feed stream in conduit 120 can be subsequently introduced into the single cold of the second refrigeration system 14 But in the cooling duct 40 in region 38.As described further below, the second refrigeration system 14 can be it is exercisable so that The heat exchanger that feed stream in conduit 120 is condensed and is subcooled by the indirect heat exchange with the second mix refrigerant. In one or more embodiments, the second refrigeration system 14 can be brazing aluminium heat exchanger, and it is many that it includes being disposed therein Individual cooling and heating passage (for example, core), for promoting between one or more processing streams and one or more cold-producing medium streams Indirect heat exchange.

Although describing not in Fig. 1 to Fig. 7, in various embodiments, the first refrigeration system 12 and the second refrigeration system Uniting 14 each that may be embodied in identical heat exchanger and in above-mentioned cooled region (20,26,32 and 38) can be herein It is connected in series in single core in heat exchanger.In addition, although Fig. 1 to Fig. 7 depict cooled region (20,26,32 and 38) it Between physical conduit, but those skilled in the art will readily appreciate that and there may be wherein in cooled region (20,26,32 And 38) between the embodiment of physical conduit is not present, especially cooled region (20,26,32 and 38) is connected in series wherein In embodiment.

By the hydrocarbonaceous feed air-flow of the cooling duct 40 of cooled region 38 can by with refrigerant heat passage 42 The indirect heat exchange of the second mix refrigerant condensed and be subcooled, this is hereinafter described in further detail.

When leaving the second refrigeration system 14, the stream of entering of the supercooling in conduit 122 can be then by filling through expansion Put 44 channel expansion, the wherein pressure of the stream can reduce.Expansion gear 44 can include any suitable expansion gear, lift For example, for example, Joule-Thomson valve or the hydraulic turbine.Although explanation is to include single assembly 44 in Fig. 1, it should be understood that can To use any suitable number of expansion gear.In certain embodiments, the expansion can be the substantially expansion of constant enthalpy or wait The expansion of entropy.As used herein, term " substantially constant enthalpy " refer to generate during expanding through performing less than total work 1% work(expansion or the flash steps of surrounding environment are transferred to from fluid.As used herein, " constant entropy " expansion refers to wherein The most of or substantially all work(generated during expanding is transferred to expansion or the flash steps of surrounding environment.

Expansion stream in conduit 124 can be adjusted by valve 46.The stream that the cooling of valve 46 is left by conduit 126 can To be the product rich in liquefied natural gas (LNG).As used herein, " being rich in liquefied natural gas (LNG) " means specific group Into including the methane of at least 50 molar percentages.In conduit 126 rich in liquefied natural gas (LNG) product can have than- 120th, -130, -140 or -145 DEG C low and/or -195, -190, -180 or -165 DEG C of high temperature of ratio.More precisely, conduit The product rich in liquefied natural gas (LNG) in 126 can have arrived-120 to-195 DEG C ,-130 to-190 DEG C ,-140- Temperature in the range of 180 DEG C or -145 to -165 DEG C.

Fig. 1 is returned to, the first refrigeration system 12 is hereinafter described in further detail now and the first closed loop hybrid refrigeration is followed Ring.As shown in figure 1, the first refrigeration system 12 is containing three cooled regions (20,26 and 32), wherein the first closed loop hybrid refrigeration is followed Ring is disposed at least partially therein.

First closed loop hybrid refrigeration cycle includes the first mix refrigerant and following article is described in Fig. 1.When leaving During refrigerant heat passage 24 in the first cooled region 20, the mix refrigerant of gaseous state first in conduit 128 is sent to compression Machine system 48, the compressor assembly includes the first compressor stage 54, the second compressor stage 52 and the 3rd compressor stage 50.

In various embodiments, the mix refrigerant of gaseous state first in conduit 128 can be at least 1.5,2.0 or 2.7MPa And/or no more than 5.0,4.0 or under 3.5MPa pressure.More precisely, the mix refrigerant of gaseous state first in conduit 128 can With under the pressure in the range of 1.5 to 5.0MPa, 2.0 to 4.0MPa or 2.7 to 3.5MPa.Additionally or alternatively, conduit The mix refrigerant of gaseous state first in 128 can less than 50,35 or 25 DEG C and/or temperature higher than -40, -30 or -20 DEG C Under.More precisely, the mix refrigerant of gaseous state first in conduit 128 can be at -40 to 50 DEG C, -30 to 35 DEG C or -20 to 25 Within the temperature range of DEG C.

Although being depicted as in Fig. 1 only containing three levels, those skilled in the art will readily appreciate that compressor 48 can be corrected optionally including more or less levels.In various embodiments, compressor assembly 48 can include axle To compressor, centrifugal compressor, reciprocating compressor, screw compressor or its combination.In addition, compressor assembly 48 can be with By steam turbine, combustion gas turbine, motor or its combination driving.

In various embodiments, refrigerant can pass through the seal leakage of compressor 48.In such embodiment, not Be the refrigerant of emission loss, and be available with sealing gas recovery method, its reclaim refrigerant at least a portion and Return it to refrigerant circuit.Sealing gas recovery method is described in the 8th, 066, No. 023 United States Patent (USP), the patent is with complete The mode that text is quoted is incorporated herein.For example, compressor 48 can have Venturi tube (not shown), for retain from Any sealing gas of compressor leakage.

The mix refrigerant of gaseous state first in conduit 128 be directed into the 3rd compressor stage 50.In various embodiments In, the mix refrigerant of gaseous state first can be compressed at least 2.5,4.0 or 4.8MPa and/or be no more than by the 3rd compressor stage 50 8.0th, 7.0 or 6.3MPa pressure.More precisely, the mix refrigerant of gaseous state first can be compressed to by the 3rd compressor stage 50 2.5 to 8.0MPa, 4.0 pressure arrived in the range of 7.0MPa or 4.8 to 6.3MPa.

The first compressed mix refrigerant is sent to drain cooler 56 by conduit 130, and wherein the stream can be cooled down To close to environment temperature and passing through the indirect heat exchange total condensation with outside cooling media (for example, cooling water or air). As used herein, " total condensation " means that assert stream includes the steam less than 1.0 molar percentages.At one or many In individual embodiment, total condensation stream can include the steam less than 0.5,0.1,0.05 or 0.001 molar percentage.In various realities Apply in example, the first mix refrigerant must be liquid under cooler discharge pressure.

When leaving drain cooler 56 by conduit 132, the first mix refrigerant of total condensation is introduced in first In cooling duct 58 in cooled region 20.In various embodiments, the first mix refrigerant of the total condensation in conduit 132 Can be at least 2.5,4.0 or 4.8MPa and/or no more than 8.0,7.0 or under 6.3MPa pressure.More precisely, conduit First mix refrigerant of the total condensation in 132 can arrive 6.3MPa scopes 2.5 to 8.0MPa, 4.0 to 7.0MPa or 4.8 Under interior pressure.Additionally or alternatively, the first mix refrigerant of the total condensation in conduit 132 can be close to environment temperature At a temperature of degree.

In cooling duct 58, the first mix refrigerant of total condensation can by with refrigerant heat passage 24 The indirect heat exchange supercooling of first mix refrigerant, this is discussed further below.

When leaving cooling duct 58 by conduit 134, at least a portion of the stream can be directed into swollen by conduit 136 Swollen device 60, the wherein pressure of the stream can reduce, thus cooling and the in certain embodiments at least partly vaporization system Cryogen stream.Expansion gear 60 can include any suitable expansion gear, for example, for example, Joule-Thomson valve or water wheels Machine.Although it is to include single assembly 60 to be illustrated in Figure 1, it should be appreciated that any suitable number of expansion gear. In certain embodiments, the expansion can be the substantially expansion of constant enthalpy or the expansion of constant entropy.

Before inflation, first mix refrigerant of total condensation can be at least 2.5,4.0 or 4.8MPa in conduit 136 And/or no more than 8.0,7.0 or under 6.3MPa pressure.More precisely, the first mixing system of the total condensation in conduit 136 Cryogen can be under the pressure in the range of 2.5 to 8.0,4.0 to 7.0 or 4.8 to 6.3MPa.Additionally or alternatively, conduit First mix refrigerant of the total condensation in 136 can less than 30,25 or 15 DEG C and/or higher than -40, -30 or -5 DEG C At a temperature of.More precisely, first mix refrigerant of total condensation can be at -40 to 30 DEG C, -30 to 25 DEG C in conduit 136 Or in the range of -5 to 15 DEG C at a temperature of.

In various embodiments, the first mix refrigerant of total condensation is not subject to phase before the expansion step or afterwards Separation.As used herein, " phase separation " is related to is separated into the corresponding of them by the two phase flow for usually containing liquid and gas Phase.

First mix refrigerant of expansion is introduced in refrigerant heat passage 24 by conduit 138, wherein expand First mix refrigerant can be gasified to provide refrigeration to the first cooled region 20.

In various embodiments, the first mix refrigerant of the expansion in conduit 138 can include less than 5,3,1,0.5 or The gas phase of 0.1 molar percentage.In addition, in certain embodiments, the first mix refrigerant of the expansion in conduit 138 can be At least 1.5,2.0 or 2.7MPa and/or no more than 5.0,4.0 or under 3.5MPa pressure.More precisely, in conduit 138 First mix refrigerant of expansion can be in the pressure in the range of 1.5 to 5.0MPa, 2.0 to 4.0MPa or 2.7 to 3.5MPa Under.Additionally or alternatively, the first mix refrigerant of the expansion in conduit 138 can less than 30,25 or 15 DEG C and/or high At a temperature of -40, -30 or -5 DEG C.More precisely, the first mix refrigerant of the expansion in conduit 138 can be arrived -40 At a temperature of in the range of 30 DEG C, -30 to 25 DEG C or -5 to 15 DEG C.

As described above, the mix refrigerant of gaseous state first of gasification leaves refrigerant heat passage 24 by conduit 128.

At least a portion for returning again to the first mix refrigerant of total condensation in Fig. 1, conduit 134 is directed into second Cooling duct 62 in cooled region 26.In cooling duct 62, the first mix refrigerant of total condensation can by with system The indirect heat exchange of the first mix refrigerant in cryogen heating passage 30 is further subcooled, and this is discussed further below.

When leaving cooling duct 62 by conduit 140, at least a portion of the stream can be directed into swollen by conduit 142 Swollen device 64, the wherein pressure of the stream can reduce, thus cooling and the in certain embodiments at least partly vaporization system Cryogen stream.Expansion gear 64 can include any suitable expansion gear, for example, for example, Joule-Thomson valve or water wheels Machine.Although it is to include single assembly 64 to be illustrated in Figure 1, it should be appreciated that any suitable number of expansion gear. In certain embodiments, the expansion can be the substantially expansion of constant enthalpy or the expansion of constant entropy.In various embodiments, it is completely cold The first solidifying mix refrigerant is not subject to be separated before the expansion step or afterwards.

Before inflation, first mix refrigerant of total condensation can be at least 2.5,4.0 or 4.8MPa in conduit 142 And/or no more than 8.0,7.0 or under 6.3MPa pressure.More precisely, the first mixing system of the total condensation in conduit 142 Cryogen can be under the pressure in the range of 2.5 to 8.0,4.0 to 7.0 or 4.8 to 6.3MPa.Additionally or alternatively, conduit First mix refrigerant of the total condensation in 142 can be less than 0, -10 or -25 DEG C and/or higher than -100, -75 or -50 DEG C At a temperature of.More precisely, the first mix refrigerant of total condensation in conduit 142 can -100 to 0 DEG C, -75 to - At a temperature of in the range of 10 DEG C or -50 to -25 DEG C.

First mix refrigerant of expansion is introduced in refrigerant heat passage 30 by conduit 144, wherein expand First mix refrigerant provides refrigeration through gasifying to the second cooled region 26.In various embodiments, it is swollen in conduit 144 The first swollen mix refrigerant can include the gas phase less than 5,4,3,2,1 or 0.1 molar percentage.In addition, implementing some In example, the first mix refrigerant of the expansion in conduit 144 can at least 0.3,0.5 or 0.65MPa and/or no more than 2.0, Under 1.7 or 1.4MPa pressure.More precisely, the first mix refrigerant of the expansion in conduit 144 can be arrived 0.3 Under pressure in the range of 2.0MPa, 0.5 to 1.7MPa or 0.65 to 1.4MPa.Additionally or alternatively, it is swollen in conduit 144 The first swollen mix refrigerant can be at a temperature of less than 0, -10 or -25 DEG C and/or higher than -100, -75 or -50 DEG C.It is more true Say with cutting, the first mix refrigerant of the expansion in conduit 144 can be in -100 to 0 DEG C, -75 to -10 DEG C, or -50 to -25 DEG C In the range of at a temperature of.

The mix refrigerant of gaseous state first of gasification leaves refrigerant heat passage 30 by conduit 146 and can be introduced into Into the second compressor stage 52.In various embodiments, the mix refrigerant of gaseous state first in conduit 146 can at least 0.3, 0.5 or 0.65MPa and/or no more than 2.0,1.7 or under 1.4MPa pressure.More precisely, the gaseous state first in conduit 146 Mix refrigerant can be under the pressure in the range of 0.3 to 2.0MPa, 0.5 to 1.7MPa or 0.65 to 1.4MPa.Extraly Or alternatively, the mix refrigerant of gaseous state first in conduit 146 can less than 30,25 or 15 DEG C and/or higher than -40, -30 Or at a temperature of -5 DEG C.More precisely, the mix refrigerant of gaseous state first in conduit 146 can be arrived -40 to 30 DEG C, -30 At a temperature of in the range of 25 DEG C or -5 to 15 DEG C.

In various embodiments, the second compressor stage 52 mix refrigerant of gaseous state first can be compressed to at least 1.5, 2.0 or 2.7MPa and/or no more than 5.0,4.0 or 3.5MPa pressure.More precisely, the second compressor stage 52 can be by gas The mix refrigerant of state first is compressed to 1.5 to 5.0MPa, 2.0 pressure arrived in the range of 4.0MPa or 2.7 to 3.5MPa.

The first compressed mix refrigerant from the second compressor stage 52 is sent to intergrade by conduit 148 and cooled down Device 66, the wherein stream can be cooled down by the indirect heat exchange with outside cooling media (for example, cooling water or air).When When leaving intergrade cooler 66 by conduit 150, the compression stream in conduit 150 be directed into conduit 128, wherein such as It is described above it can be directed in the 3rd compressor stage 50 and further compress.

At least a portion for returning again to the first mix refrigerant of total condensation in Fig. 1, conduit 140 is directed into the 3rd Cooling duct 68 in cooled region 32.In cooling duct 68, the first mix refrigerant of total condensation can by with system The indirect heat exchange of the first mix refrigerant in cryogen heating passage 36 is further subcooled, and this is discussed further below.

When leaving cooling duct 68 by conduit 152, the stream of cooling can be guided to expansion gear 70, wherein the stream Pressure can reduce, thus cooling and vaporised refrigerant stream at least in part.Expansion gear 70 can include any suitable Expansion gear, for example, for example, Joule-Thomson valve or the hydraulic turbine.Although it is to include single assembly 70 to be illustrated in Figure 1, It should be appreciated that any suitable number of expansion gear.In certain embodiments, the expansion can be substantially first-class The expansion of enthalpy or the expansion of constant entropy.In various embodiments, the first mix refrigerant of total condensation before the expansion step or It is not subject to be separated afterwards.

Before inflation, first mix refrigerant of total condensation can be at least 2.5,4.0 or 4.8MPa in conduit 152 And/or no more than 8.0,7.0 or under 6.3MPa pressure.More precisely, the first mixing system of the total condensation in conduit 152 Cryogen can be under the pressure in the range of 2.5 to 8.0MPa, 4.0 to 7.0MPa or 4.8 to 6.3MPa.Extraly or substitute First mix refrigerant of the total condensation in ground, conduit 152 can less than -20, -40 or -60 DEG C and/or higher than -120, - 90 or -75 DEG C at a temperature of.More precisely, first mix refrigerant of total condensation can be -120 to -20 in conduit 152 DEG C, in the range of -90 to -40 DEG C or -75 to -60 DEG C at a temperature of.

First mix refrigerant of expansion is introduced in refrigerant heat passage 36 by conduit 154, wherein expand First mix refrigerant provides refrigeration through gasifying to the 3rd cooled region 32.In various embodiments, it is swollen in conduit 154 The first swollen mix refrigerant can include the gas phase less than 10,7,6,4,2,1 or 0.5 molar percentage.In addition, in some realities Apply in example, the first mix refrigerant expanded in conduit 154 can at least 0.1,0.15 or 0.2MPa and/or no more than 2.0, Under 1.5 or 0.5MPa pressure.More precisely, the first mix refrigerant of the expansion in conduit 154 can be arrived 0.1 Under pressure in the range of 2.0MPa, 0.15 to 1.5MPa or 0.2 to 0.5MPa.Additionally or alternatively, it is swollen in conduit 154 The first swollen mix refrigerant can be at a temperature of less than -20, -40 or -60 DEG C and/or higher than -120, -90 or -75 DEG C.More Exactly, the first mix refrigerant expanded in conduit 154 can be at -120 to -20 DEG C, -90 to -40 DEG C or -75 to -60 At a temperature of in the range of DEG C.

The mix refrigerant of gaseous state first of gasification leaves refrigerant heat passage 36 by conduit 156 and can be introduced into Into the first compressor stage 54.In various embodiments, the mix refrigerant of gaseous state first in conduit 156 can at least 0.1, 0.15 or 0.2MPa and/or no more than 2.0,1.5 or under 0.5MPa pressure.More precisely, the gaseous state first in conduit 156 Mix refrigerant can be under the pressure in the range of 0.1 to 2.0MPa, 0.15 to 1.5MPa or 0.2 to 0.5MPa.Extraly Or alternatively, the mix refrigerant of gaseous state first in conduit 156 can be less than 0, -10 or -25 DEG C and/or higher than -100, -75 Or at a temperature of -50 DEG C.More precisely, the mix refrigerant of gaseous state first in conduit 156 can -100 to 0 DEG C, -75 At a temperature of in the range of to -10 DEG C or -50 to -25 DEG C.

When leaving the first compressor stage 54 by conduit 158, the compression stream in conduit 158 be directed into conduit In 146, wherein it can be directed in the second compressor stage 52 and the 3rd compressor stage 50 and further compresses as described above. In various embodiments, the first compressor stage 54 mix refrigerant of gaseous state first can be compressed at least 0.3,0.5 or 0.65MPa and/or no more than 2.0,1.7 or 1.4MPa pressure.More precisely, the first compressor stage 54 can be by gaseous state One mix refrigerant is compressed to the pressure in the range of arriving 1.7MPa or 0.65 to 1.4MPa 0.3 to 2.0MPa, 0.5.

In various embodiments, and as depicted in FIG. 1, the first refrigeration system 12 and the first closed loop hybrid refrigeration cycle Without phase separator.As used herein, " phase separator ", which is understood to cover, to be specially designed for the flow point of partial condensation From any device into liquid and vapor fraction.Therefore, this will not include, for example, suction drum and surge drum.

In certain embodiments, the conduit 136,138,142,144,152 and 154 in Fig. 1 ought visibly in the presence of can be with It is outside positioned at their corresponding cooled region (20,26 and 32).In such embodiment, conduit 136,138,142,144, 152 and 154 can be located at outside heat exchanger or heat exchanger containing corresponding cooled region (20,26 and 32).

First mix refrigerant can include two or more composition in the group being made up of following item：Nitrogen Gas, methane, ethene, ethane, propylene, propane, iso-butane, normal butane, isopentane, pentane, and combinations thereof.In some embodiments In, the first mix refrigerant can include at least two chemical combination in the group being made up of the hydro carbons containing 2 to 4 carbon atoms Thing.In certain embodiments, the first mix refrigerant can have about at ambient temperature 2.5 between 5.65MPa Bubble point pressure.

In some embodiments of the invention, it may be necessary to which it is cold thus to change its to adjust the composition of the first mix refrigerant But curve and its refrigeration potential is therefore changed.Such modification can be used for adapting to, for example, being incorporated into liquefied natural gas (LNG) The change of the composition and/or flow velocity of feed stream in recvery facility 10.In one embodiment, the group of the first mix refrigerant Into the heating curves that can be adjusted such that vaporised refrigerant closely match feed stream and heating refrigerant it is cold But curve.A method for such Curve Matching is described in detail in the 4th, 033, No. 735 United States Patent (USP), the patent Content is incorporated herein in entirety by reference.

Fig. 1 is returned again to, the second refrigeration system 14 and the second closed loop hybrid refrigeration cycle are described in further detail now.Such as Shown in Fig. 1, the second refrigeration system 14 contains single cooled region 38, wherein the second closed loop hybrid refrigeration cycle is set at least in part Put wherein.As used herein, " single cooled region " means that system only includes a region, and stream is entered in this region Cooled down by the indirect heat exchange with single cooling agent.In such embodiment, the system assert will not contain any Other cooled regions.In certain embodiments, single cooling agent can include expansion the first mix refrigerant or expansion the Two mix refrigerants.In various embodiments, the second refrigeration system 14 includes single cooled region, substantially by single cooling zone Domain is constituted, or is made up of single cooled region.

Second closed loop hybrid refrigeration cycle includes in Fig. 1 being described in the second mix refrigerant and following article.When from When opening the refrigerant heat passage 42 in cooled region 38, the mix refrigerant of gaseous state second in conduit 160 is sent to compression Machine system 72, the compressor assembly includes the first compressor stage 74 and the second compressor stage 76.In various embodiments, compressor 72 can be configured to reclaim sealing gas as previously discussed with respect to compressor 48 is described.Therefore, in certain embodiments, compressor 72 Venturi tube (not shown) can be contained, the Venturi tube is designed as retaining the sealing gas leaked into outside compressor.

In various embodiments, the mix refrigerant of gaseous state second in conduit 160 at least 0.1,0.15 or 0.2MPa and/ Or no more than under the pressure in the range of 2.0,1.5 or 0.5MPa.More precisely, the mixing system of gaseous state second in conduit 160 Cryogen can be under the pressure in the range of 0.1 to 2.0MPa, 0.15 to 1.5MPa or 0.2 to 0.5MPa.Extraly or substitute The mix refrigerant of gaseous state second in ground, conduit 160 is less than -20, -40 or -60 DEG C and/or higher than -120, -90 or -75 DEG C At a temperature of.More precisely, the mix refrigerant of gaseous state second in conduit 160 can be at -120 to -20 DEG C, -90 to -40 DEG C Or in the range of -75 to -60 DEG C at a temperature of.

Although being depicted as in Fig. 1 only containing two levels, those skilled in the art will readily appreciate that compressor 72 can be corrected optionally including more or less levels.In various embodiments, compressor assembly 72 can include axle To compressor, centrifugal compressor, reciprocating compressor, screw compressor or its combination.In addition, compressor assembly 72 can be with By steam turbine, combustion gas turbine, motor or its combination driving.

The mix refrigerant of gaseous state second in conduit 160 is introduced in the first compressor stage 74 and then by conduit 162 are sent to intergrade cooler 78, and wherein the stream can be by between outside cooling media (for example, cooling water or air) Heat exchange is connect to be cooled to close to environment temperature.In various embodiments, gaseous state second can be mixed system by the first compressor stage 74 Cryogen is compressed at least 0.3,0.5 or 0.65MPa and/or no more than 3.0,2.5 or 2.0MPa pressure.More precisely, the The mix refrigerant of gaseous state second can be compressed to and be arrived 0.3 to 3.0MPa, 0.5 to 2.5MPa or 0.65 by one compressor stage 74 Pressure in the range of 2.0MPa.

Second mix refrigerant of cooling then can be introduced in the second compressor stage 76 by conduit 164, wherein Second mix refrigerant is further compressed.In various embodiments, the second compressor stage 76 can mix gaseous state second Refrigerant compression is at least 2.5,4.0 or 4.8 and/or no more than 8.0,7.0 or 6.0MPa pressure.More precisely, second The mix refrigerant of gaseous state second can be compressed to 2.5 to 8.0MPa, 4.0 to 7.0MPa or 4.8 and arrive 6.0MPa by compressor stage 76 In the range of pressure.

The second compressed mix refrigerant is then introduced in drain cooler 80 by conduit 166, wherein the stream It can be further cooled to by the indirect heat exchange with outside cooling media (for example, cooling water or air) close to environment temperature Degree.

The second compressed mix refrigerant in conduit 168 is subsequently introduced into the first cooling of the first refrigeration system 12 In cooling duct 82 in region 20.In various embodiments, the second mix refrigerant compressed in conduit 168 can be extremely Lack 2.5,4.0 or 4.8MPa and/or no more than 8.0,7.0 or under 6.0MPa pressure.More precisely, the pressure in conduit 168 The second mix refrigerant contracted can be in the pressure in the range of 2.5 to 8.0MPa, 4.0 to 7.0MPa or 4.8 to 6.0MPa Under.Additionally or alternatively, the second compressed mix refrigerant in conduit 168 can at ambient temperature or environment temperature Near.

In cooling duct 82, the second mix refrigerant can be by mixing system with first in refrigerant heat passage 24 The indirect heat exchange of cryogen is further cooled down.And in cooling duct 82, the second mix refrigerant can be cool below The temperature of the dew point of refrigerant mixture.

Second mix refrigerant of the cooling in conduit 170 is subsequently introduced into the second cooling zone of the first refrigeration system 12 In cooling duct 84 in domain 26.In cooling duct 84, the second mix refrigerant can by with refrigerant heat passage 30 In the indirect heat exchange of the first mix refrigerant further cooled down.And in cooling duct 84, the second mix refrigerant The temperature of the dew point of refrigerant mixture can be cool below.

Second mix refrigerant of the cooling in conduit 172 is subsequently introduced into the 3rd cooling zone of the first refrigeration system 12 In cooling duct 86 in domain 32.In cooling duct 86, the second mix refrigerant can by with refrigerant heat passage 36 In the indirect heat exchange of the first mix refrigerant further cooled down.And in cooling duct 86, the second mix refrigerant The temperature of the bubbling point of refrigerant mixture can be cool below.

When leaving the first refrigeration system 12 by conduit 174, the second mix refrigerant total condensation in conduit 174. Second mix refrigerant of the total condensation in conduit 174 can be subsequently introduced into the cooled region 38 of the second refrigeration system 14 In cooling duct 88 in.

When leaving cooling duct 88 by conduit 176, the second mixed refrigerant stream of supercooling can be guided to expansion The pressure of device 90, the wherein stream can reduce, thus cooling and vaporised refrigerant stream.Before inflation, in conduit 176 completely Second mix refrigerant of condensation can be at least 2.5,4.0 or 4.8MPa and/or no more than 8.0,7.0 or 6.0MPa pressure Under.More precisely, the second mix refrigerant of the total condensation in conduit 176 can be 2.5 to 8.0,4.0 to 7.0 or 4.8 Under pressure in the range of to 6.0MPa.Additionally or alternatively, second mix refrigerant of total condensation can be with conduit 176 At a temperature of less than -120, -130, -140 or -145 DEG C and/or higher than -195, -190, -180 or -165 DEG C.More properly Say, the second mix refrigerant of the total condensation in conduit 176 can -120 to -195 DEG C, -130 to -190 DEG C, -140 to - At a temperature of in the range of 180 DEG C or -145 to -165 DEG C.

Expansion gear 90 can include any suitable expansion gear, for example, for example, Joule-Thomson valve or water Turbine.Although it is to include single assembly 90 to be illustrated in Figure 1, it should be appreciated that any suitable number of expansion dress Put.In certain embodiments, the expansion can be the substantially expansion of constant enthalpy or the expansion of constant entropy.

Expansion stream in conduit 178 can be adjusted by valve 92.In various embodiments, the expansion stream in conduit 178 The gas phase less than 15,10,8,6,2 or 1 molar percentage can be included.In addition, in certain embodiments, it is swollen in conduit 178 Dilatant can be at least 0.3,0.5 or 0.65MPa and/or no more than 3.0,2.0 or under 1.4MPa pressure.More precisely, Expansion stream in conduit 178 can be under the pressure in the range of 0.3 to 3.0MPa, 0.5 to 2.0MPa or 0.65 to 1.4MPa. Additionally or alternatively, the expansion stream in conduit 178 can less than -120, -130 or -140 or -145 DEG C and/or higher than - 195th, at a temperature of -190, -180 or -165 DEG C.More precisely, the expansion stream in conduit 178 can be -120 to -195 DEG C, -130 to -190 DEG C, in the range of -140 to -180 DEG C or -145 to -165 DEG C at a temperature of.

Second mix refrigerant of the expansion in conduit 180 is subsequently introduced into refrigerant heat passage 42, wherein swollen The second swollen mix refrigerant provides refrigeration through gasifying to cooled region 38.In various embodiments, it is swollen in conduit 180 Dilatant can include the gas phase less than 15,10,8,6 or 2 molar percentages.In one or more embodiments, in conduit 180 Second mix refrigerant of expansion can be at least 0.1,0.15 or 0.2MPa and/or no more than 2.0,1.5 or 0.5MPa model Enclose and introduced under interior pressure.More precisely, the second mix refrigerant of expansion in conduit 180 can 0.1 to 2.0MPa, Introduced under pressure in the range of 0.15 to 1.5MPa or 0.2 to 0.5MPa.

In certain embodiments, conduit 174,176,178 and 180 can be located at outside cooled region 38.Implement such In example, conduit 174,176,178 and 180 can be located at outside the heat exchanger containing cooled region 38.

The mix refrigerant of gaseous state second in conduit 160 is then compressed and reclaimed in the above-mentioned methods.In various realities Apply in example, the second mix refrigerant of total condensation is not subjected to being separated before the expansion step or afterwards.

In various embodiments, and as depicted in FIG. 1, the second refrigeration system 14 and the second closed loop hybrid refrigeration cycle Without phase separator.

Second mix refrigerant can include two or more composition in the group being made up of following item：Nitrogen Gas, methane, ethene, ethane, propylene, propane, iso-butane, normal butane, isopentane, pentane, and combinations thereof.In some embodiments In, the second mix refrigerant can include at least two in the group that is constituted selected from the hydro carbons by nitrogen and containing 1 to 3 carbon atoms Plant compound.In various embodiments, at a given pressure the second mix refrigerant by with less than the first mix refrigerant The bubble point temperature of bubble point temperature.In certain embodiments, the second mix refrigerant can have between -60 to -75 DEG C At a temperature of 2.5 to the bubble point pressure between 6.1MPa.

In some embodiments of the invention, it may be necessary to which it is cold thus to change its to adjust the composition of the second mix refrigerant But curve and its refrigeration potential is therefore changed.Such modification can be used for adapting to, for example, being incorporated into liquefied natural gas (LNG) The change of the composition and/or flow velocity of feed stream in recvery facility 10.In one embodiment, the second mixing system can be adjusted The composition of cryogen causes the heating curves of vaporised refrigerant closely to match the cooling of feed stream and the refrigerant of heating Curve.

It should be noted that the conduit being depicted in Fig. 1 between cooled region (20,26,32 and 38) is merely for illustrative purpose Show, and in certain embodiments, figure 1 illustrates tangible conduit may be not present at each conduit.

Although Fig. 1 depicts one embodiment of the inventive method and system, however it is envisaged that having gone out other embodiments, example Such as, Fig. 2 to it is depicted in figure 7 those, it can be incorporated to turbine expander 94, be operably connected to turbine expander 94 Compressor 96 and heavy substance separator 98.It should be noted that all common system components found in Fig. 1 to Fig. 7 all use identical mark Number correspondingly mark.For example, the first refrigeration system 12 and the second refrigeration system 14 Fig. 1 to Fig. 7 in the whole text in all as one man Mark.Worked in addition, the system component in Fig. 1 to Fig. 7 is contemplated to identical or substantially similar manner, unless referred in addition Go out.Only marked difference between Fig. 1 to Fig. 7 is that conduit therein is marked according to their corresponding figure and embodiment 's.For example, in Fig. 2 corresponding conduit be labeled as 2XX, and in Fig. 3 corresponding conduit labeled as 3XX (wherein " X " expression number Word).Conduit in Fig. 1 to Fig. 7 in the whole text in work in the same manner (that is, the corresponding stream for transmitting them), unless in addition Point out.

In fig. 2, liquefied natural gas (LNG) recvery facility 10 is depicted as containing turbine expander 94, the turbine expansion Device is operably connected to the 3rd cooled region 32 of the first refrigeration system 12 by conduit 220.In No. 6,367,286 U.S. Turbine expander is further described in patent, the patent is incorporated herein in entirety by reference.

As shown in Fig. 2, pass through at least a portion of the hydrocarbonaceous feed air-flow of the cooling duct 34 of the 3rd cooled region 32 Turbine expander 94 can be directed into by conduit 220, wherein it can be expanded into two phase flow.Due to expanding, in conduit 222 The temperature at least 2 of the stream that can be less than in conduit 220 of temperature of the fluid stream of flash distillation or expansion, 5 or 10 DEG C and/or it is no more than 50th, 40 or 30 DEG C.In addition, the pressure for the fluid stream for flashing or expanding in conduit 222 can be less than the pressure of the stream in conduit 220 At least 0.1,0.2 or 0.3 and/or no more than 5.0,4.0 or 3.0MPa.In certain embodiments, expansion can be waited substantially Entropy.Although not describing in fig. 2, suction drum can be in the cooling zone of turbine expander 94 and the 3rd in certain embodiments It is in fluid communication between domain 32.

In addition, turbine expander 94 is connected to compressor 96 by axostylus axostyle 95.Compressor 96 can origin at least in part Driven from the work(of turbine expander 94.As described below, compressor 96 is configured to compress at least in part from separator 98 Top layer cut.In various embodiments, compressor 96 can include axial compressor, centrifugal compressor, reciprocating compression Machine, screw compressor, or its combination.In addition, compressor 96 can by steam turbine, combustion gas turbine, motor or its Combination driving.

In various embodiments, compressor 96 can be configured to reclaim blanket gas as previously discussed with respect to compressor 48 is described Body.Therefore, in certain embodiments, compressor 96 can contain Venturi tube (not shown), and the Venturi tube is designed as retaining The sealing gas leaked into outside compressor.

As shown in Fig. 2, the two phase flow expanded in conduit 222 is directed into separator 98, and the separator is by the stream of expansion It is separated into the liquid heavy distillat (conduit 224) of less methane and the top layer vapor fraction (conduit 226) rich in methane.Such as this paper institutes Use, " less methane " and " being rich in methane " refers to that the methane content of the component of separation contains relative to the methane of initial component Amount, the component of separation is from the initial component.Therefore, the component rich in methane with it from component compared with containing more Molar percentage methane, and the component of less methane with it from component compared with containing less molar percentage Methane.In the current situation, the bottom stream of less methane contains relatively low molar percentage compared with the stream from conduit 222 Methane, and the top layer stream rich in methane contains the methane of higher molar percentage compared with the stream from conduit 222.Depend on The content of gas containing hydrocarbon and the operating condition of separation container 98 can change less methane bottom stream and rich in methane top layer stream Amount.

Less methane bottom stream in conduit 224 can be in a liquid state form and can containing initially in conduit 222 What is found in stream has the major part of the compound of six or more carbon atoms.For example, the less methane in conduit 224 Bottom stream, which can include initially appearing in the stream from conduit 222, has the compound of six or more carbon atoms extremely Few 70%, 80%, 90%, 95% or 99%.

The top layer vapor stream rich in methane can include most methane in conduit 226.For example, in conduit 226 Top layer vapor stream rich in methane can include at least about 10,25,40 or 50 and/or no more than about 99.9,99,95 or 85 The methane of molar percentage.More precisely, the top layer vapor stream that methane is rich in conduit 226 can be included in about 10 and arrive 99.9th, the methane of the molar percentage in the range of 25 to 99,40 to 95 or 50 to 85.In addition, being rich in the top of methane in conduit 226 Layer vapor stream can include initially appearing at least 50% of methane in the stream from conduit 222,60%, 70%, 80%, 90%th, 95%, 99% or 99.9%.

Separation container 98 can be any suitable vapor liquid separation vessel and can have any number of reality Or theoretical separation level.In one or more embodiments, separation container 98 can include single separation level, and in other embodiments In, separation container 98 can include 2 to 10,4 to 20, or 6 to 30 reality or theoretical separation level.When separation container 98 is multistage During separation container, the column internals of any suitable type can be used, for example, demister, mesh liner, vapor liquid connect Pallet, dumped packing and/or structured packing is touched to contribute to the heat transfer between steam and liquid flow and/or mass transfer. In some embodiments, when separation container 98 is single-stage separation container, using less column internals or it can not use vertical Post internals.

In various embodiments, separation container 98 can at least 1.5,2.5,3.5 or 4.5 and/or 9.0,8.0,7.0 or Operated under 6.0MPa pressure.More precisely, separation container 98 can be 1.5 to 9.0,2.5 to 8.0,3.5 to 7.0 or 4.5 Operated under pressure in the range of to 6.0MPa.

As those skilled in the art will readily appreciate that, the temperature in separation container 98 can depend on being incorporated into system Neutralize the content for the gas containing hydrocarbon for needing to export and change.In various embodiments, separation container 98 can less than 5,10 or 15 DEG C and/or higher than -195, -185, -175 or -160 DEG C at a temperature of operate.More precisely, separation container 98 can be 15 Operated at a temperature of in the range of to -195 DEG C, 10 to -185 DEG C, 5 to -175 DEG C or 5 to -160 DEG C.

As shown in Fig. 2, the top layer vapor stream rich in methane can be directed to compressor 96 in conduit 226, the compression Machine compresses the stream.Compression stream in conduit 228 is then reintroduced in the cooling duct 34 of the 3rd cooled region 32 with such as Above for further being cooled down and condensed described in Fig. 1.

It should be noted that the first refrigeration system 12, the second refrigeration system 14, the first closed loop hybrid refrigeration cycle (conduit 238,240, 242nd, 244,246,248,250,252,254,256,258,260,262,264,266 and 268), and as depicted in Figure 2 Second closed loop hybrid refrigeration cycle (conduit 270,272,274,276,278,280,282,284,286,288 and 290), not on Fig. 2 is hereinbefore described, with being worked previously with respect to Fig. 1 same ways described.It only difference is and examine Consider labeled different of corresponding conduit in particular system embodiment depicted in figure 2, Fig. 2.In addition, not upper In text on Fig. 2 illustrate be related to liquefaction gas containing hydrocarbon remaining step (conduit 210,212,214,216,218,230, 232nd, 234 and 236) with being worked previously with respect to Fig. 1 same or like modes described.

In figure 3, liquefied natural gas (LNG) recvery facility 10 is depicted as containing turbine expander 94, the turbine expansion Device is operably connected to the 3rd cooled region 32 of the first refrigeration system 12 by conduit 320.As shown in Fig. 3, by the At least a portion of the hydrocarbonaceous feed air-flow of the cooling duct 34 of three cooled regions 32 can be directed into turbine by conduit 320 Expander 94, wherein it can be expanded into two phase flow.Turbine expander 94 can be in the identical or class described as previously discussed with respect to Fig. 2 Operated like under the conditions of.Although not describing in figure 3, suction drum can be in turbine expander 94 and in certain embodiments It is in fluid communication between three cooled regions 32.

The two phase flow expanded in conduit 322 is then routed to separator 98, and the separator is by the flow separation of expansion into first The less liquid heavy distillat (conduit 324) of alkane and the top layer vapor fraction (conduit 326) rich in methane.Separator 98 can be with As previously discussed with respect to Fig. 2 describe identical separation container and can be worked under the conditions of similar operations.After releasing, lead Top layer vapor fraction in pipe 326 be then reintroduced in the cooling duct 34 of the 3rd cooled region 32 with such as above for Further cooled down and condensed described in Fig. 1.

Less methane bottom stream in conduit 324 can be in a liquid state form and can containing initially in conduit 322 What is found in stream has the major part of the compound of six or more carbon atoms.For example, the less methane in conduit 324 Bottom stream, which can include initially appearing in the stream from conduit 322, has the compound of six or more carbon atoms extremely Few 70%, 80%, 90%, 95% or 99%.

The top layer vapor stream rich in methane can include most methane in conduit 326.For example, in conduit 326 Top layer vapor stream rich in methane can include at least about 10,25,40 or 50 and/or no more than about 99.9,99,95 or 85 The methane of molar percentage.More precisely, the top layer vapor stream that methane is rich in conduit 326 can be included in about 10 and arrive 99.9th, the methane in the range of 25 to 99,40 to 95 or 50 to 85 molar percentages.In addition, being rich in the top of methane in conduit 326 Layer vapor stream can include initially appear in the stream from conduit 322 methane at least 50%, 60%, 70%, 80%, 90%th, 95%, 99% or 99.9%.

Fig. 3 is returned again to, turbine expander 94 is connected to compressor 96 by axostylus axostyle 95.Compressor 96 can be at least partly Ground is driven by the work(from turbine expander 94.As shown in Fig. 3, the mix refrigerant of gaseous state first of gasification passes through conduit 364 Leave the refrigerant heat passage 36 in the 3rd cooled region 32 and be subsequently introduced into compressor 96, be introduced in pressure Before contracting machine 48, it is compressed in compressor 96.After being compressed, the compression stream in conduit 366 is introduced in the first pressure Contracting machine level 54 and it is further processed as discussed above for Fig. 1.Although not describing in figure 3, suction drum can To be in fluid communication between compressor 96 and heating passage 36.

It should be noted that the first refrigeration system 12, the second refrigeration system 14, and the second closed loop hybrid refrigeration depicted in figure 3 Circulate (conduit 370,372,374,376,378,380,382,384,386,388 and 390), not on Fig. 3 hereinbefore to it It is described, with being worked previously with respect to Fig. 1 same or like modes described.It only difference is in view of in Fig. 3 What corresponding conduit had been labeled in the particular system embodiment described, Fig. 3 is different.In addition, not above for What Fig. 3 was illustrated is related to the remaining step (and of conduit 310,312,314,316,318,328,330,332 of liquefaction gas containing hydrocarbon 334) and the first closed loop hybrid refrigeration cycle (conduit 336,338,340,342,344,346,348,350,352,354, 356th, 358,360,362 and 368) in the step of do not consider with being worked previously with respect to Fig. 1 same or like modes described.

In Fig. 4, liquefied natural gas (LNG) recvery facility 10 is depicted as containing turbine expander 94, the turbine expansion Device is operably connected to the 3rd cooled region 32 of the first refrigeration system 12 by conduit 420.As shown in Fig. 4, by the At least a portion of the hydrocarbonaceous feed air-flow of the cooling duct 34 of three cooled regions 32 can be directed into turbine by conduit 420 Expander 94, wherein it can be expanded into two phase flow.Turbine expander 94 can be in the identical or class described as previously discussed with respect to Fig. 2 Operated like under the conditions of.Although not describing in Fig. 4, suction drum can be in turbine expander 94 and in certain embodiments It is in fluid communication between three cooled regions 32.

The two phase flow expanded in conduit 422 is then routed to separator 98, and the separator is by the flow separation of expansion into first The less liquid heavy distillat (conduit 424) of alkane and the top layer vapor fraction (conduit 426) rich in methane.Separator 98 can be with As previously discussed with respect to Fig. 2 describe identical separation container and can be worked under the conditions of similar operations.After releasing, lead Top layer vapor fraction in pipe 426 be then reintroduced in the cooling duct 34 of the 3rd cooled region 32 with such as above for Further cooled down and condensed described in Fig. 1.

Less methane bottom stream in conduit 424 can be in a liquid state form and can containing initially in conduit 422 What is found in stream has the major part of the compound of six or more carbon atoms.For example, the less methane in conduit 324 Bottom stream, which can include initially appearing in the stream from conduit 422, has the compound of six or more carbon atoms extremely Few 70%, 80%, 90%, 95% or 99%.

The top layer vapor stream rich in methane can include most methane in conduit 426.For example, in conduit 426 Top layer vapor stream rich in methane can include at least about 10,25,40 or 50 and/or no more than about 99.9,99,95 or 85 The methane of molar percentage.More precisely, the top layer vapor stream that methane is rich in conduit 426 can be included in about 10 and arrive 99.9th, the methane of the molar percentage in the range of 25 to 99,40 to 95 or 50 to 85.In addition, being rich in the top of methane in conduit 426 Layer vapor stream can include initially appearing at least 50% of methane in the stream from conduit 422,60%, 70%, 80%, 90%th, 95%, 99% or 99.9%.

Fig. 4 is returned again to, turbine expander 94 is connected to compressor 96 by axostylus axostyle 95.Compressor 96 can be at least partly Ground is driven by the work(from turbine expander 94.As shown in Fig. 4, the mix refrigerant of gaseous state second of gasification passes through conduit 468 Leave the refrigerant heat passage 42 in cooled region 38 and be subsequently introduced into compressor 96, be introduced in compressor Before 72, it is compressed in compressor 96.After being compressed, the compression stream in conduit 470 is introduced in the first compressor Level 74 and is further processed as discussed above for Fig. 1.Although not describing in Fig. 4, suction drum can be It is in fluid communication between compressor 96 and heating passage 42.

It should be noted that the first refrigeration system 12, the second refrigeration system 14, and the first closed loop mixing system as depicted in figure 4 SAPMAC method (conduit 436,438,440,442,444,446,448,450,452,454,456,458,460,462,464 and 466), It is not described hereinbefore on Fig. 4, with being worked previously with respect to Fig. 1 same or like modes described.Only Difference be to consider particular system embodiment depicted in figure 4, in Fig. 4 corresponding conduit it is labeled not Together.In addition, not above for Fig. 4 illustrate be related to liquefaction gas containing hydrocarbon remaining step (conduit 410,412,414, 416th, 418,428,430,432 and 434) and the second closed loop hybrid refrigeration cycle (conduit 472,474,476,478, 480th, 482,484,486,488 and 490) in the step of do not consider to be risen with the same or like mode described previously with respect to Fig. 1 Effect.

In Figure 5, liquefied natural gas (LNG) recvery facility 10 is depicted as containing turbine expander 94, the turbine expansion Device is operably connected to the cooled region 38 of the second refrigeration system 14 by conduit 522.As shown in Fig. 5, pass through cooling zone At least a portion of the hydrocarbonaceous feed air-flow of the cooling duct 40 in domain 38 can be directed into turbine expander by conduit 522 94, wherein it can be expanded into two phase flow.Turbine expander 94 can be in the same or like condition described as previously discussed with respect to Fig. 2 Lower operation.Although not describing in Figure 5, suction drum can be in turbine expander 94 and cooled region in certain embodiments It is in fluid communication between 38.

The two phase flow expanded in conduit 524 is then routed to separator 98, and the separator is by the flow separation of expansion into first The less liquid heavy distillat (conduit 526) of alkane and the top layer vapor fraction (conduit 528) rich in methane.Separator 98 can be with As previously discussed with respect to Fig. 2 describe identical separation container and can be worked under the conditions of similar operations.

Less methane bottom stream in conduit 526 can be in a liquid state form and can containing initially in conduit 524 What is found in stream has the major part of the compound of six or more carbon atoms.For example, the less methane in conduit 526 Bottom stream, which can include initially appearing in the stream from conduit 524, has the compound of six or more carbon atoms extremely Few 70%, 80%, 90%, 95% or 99%.

The top layer vapor stream rich in methane can include most methane in conduit 528.For example, in conduit 528 Top layer vapor stream rich in methane can include at least about 10,25,40 or 50 and/or no more than about 99.9,99,95 or 85 The methane of molar percentage.More precisely, the top layer vapor stream that methane is rich in conduit 528 can be included in about 10 and arrive 99.9th, the methane of the molar percentage in the range of 25 to 99,40 to 95 or 50 to 85.In addition, being rich in the top of methane in conduit 528 Layer vapor stream can include initially appear in the stream from conduit 524 methane at least 50%, 60%, 70%, 80%, 90%th, 95%, 99% or 99.9%.

Fig. 5 is returned again to, turbine expander 94 is connected to compressor 96 by axostylus axostyle 95.Compressor 96 can be at least partly Ground is driven by the work(from turbine expander 94.As shown in Fig. 5, the top layer vapor stream rich in methane can be by conduit 528 Guide to compressor 96, the compressor compresses stream.Compression stream in conduit 530 is then reintroduced to cooled region 38 Further to be condensed and be subcooled as described in above for Fig. 1 in cooling duct 40.

It should be noted that the first refrigeration system 12, the second refrigeration system 14, the first closed loop hybrid refrigeration cycle (conduit 538,540, 542nd, 544,546,548,550,552,554,556,558,560,562,564,566 and 568), and as depicted in figure 5 Second closed loop hybrid refrigeration cycle (conduit 570,572,574,576,578,580,582,584,586,588 and 590), not on Fig. 5 is hereinbefore described, with being worked previously with respect to Fig. 1 same or like modes described.Only difference It is to consider particular system embodiment depicted in figure 5, labeled different of corresponding conduit in Fig. 5.In addition, Not above for Fig. 5 illustrate be related to liquefaction gas containing hydrocarbon remaining step (conduit 510,512,514,516,518, 520th, 532,534 and 536) with being worked previously with respect to Fig. 1 same or like modes described.

In figure 6, liquefied natural gas (LNG) recvery facility 10 is depicted as containing turbine expander 94, the turbine expansion Device is operably connected to the cooled region 38 of the second refrigeration system 14 by conduit 622.As shown in Fig. 6, pass through cooling zone At least a portion of the hydrocarbonaceous feed air-flow of the cooling duct 40 in domain 38 can be directed into turbine expander by conduit 622 94, wherein it can be expanded into two phase flow.Turbine expander 94 can be in the same or like condition described as previously discussed with respect to Fig. 2 Lower operation.Although not describing in figure 6, suction drum can be in turbine expander 94 and cooled region in certain embodiments It is in fluid communication between 38.

The two phase flow expanded in conduit 624 is then routed to separator 98, and the separator is by the flow separation of expansion into first The less liquid heavy distillat (conduit 626) of alkane and the top layer vapor fraction (conduit 628) rich in methane.Separator 98 can be with As previously discussed with respect to Fig. 2 describe identical separation container and can be worked under the conditions of similar operations.After releasing, lead At least a portion of top layer vapor fraction in pipe 628 is then reintroduced in the cooling duct 40 of cooled region 38 with such as Above for further being condensed and be subcooled described in Fig. 1.

Less methane bottom stream in conduit 626 can be in a liquid state form and can containing initially in conduit 624 What is found in stream has the major part of the compound of six or more carbon atoms.For example, the less methane in conduit 626 Bottom stream, which can include initially appearing in the stream from conduit 624, has the compound of six or more carbon atoms extremely Few 70%, 80%, 90%, 95% or 99%.

The top layer vapor stream rich in methane can include most methane in conduit 628.For example, in conduit 628 Top layer vapor stream rich in methane can include at least about 10,25,40 or 50 and/or no more than about 99.9,99,95 or 85 The methane of molar percentage.More precisely, the top layer vapor stream that methane is rich in conduit 628 can be included in about 10 and arrive 99.9th, the methane of the molar percentage in the range of 25 to 99,40 to 95 or 50 to 85.In addition, being rich in the top of methane in conduit 628 Layer vapor stream can include initially appearing at least 50% of methane in the stream from conduit 624,60%, 70%, 80%, 90%th, 95%, 99% or 99.9%.

Fig. 6 is returned again to, turbine expander 94 is connected to compressor 96 by axostylus axostyle 95.Compressor 96 can be at least partly Ground is driven by the work(from turbine expander 94.As shown in Fig. 6, the mix refrigerant of gaseous state first of gasification passes through conduit 664 Leave the refrigerant heat passage 36 in the 3rd cooled region 32 and be subsequently introduced into compressor 96, be introduced in compression Before machine 48, it is compressed in compressor 96.After being compressed, the compression stream in conduit 666 is introduced in the first compression Machine level 54 and is further processed as discussed above for Fig. 1.Although not describing in figure 6, suction drum can be with It is in fluid communication between compressor 96 and heating passage 36.

It should be noted that the first refrigeration system 12, the second refrigeration system 14, and the second closed loop hybrid refrigeration depicted in figure 6 Circulate (conduit 670,672,674,676,678,680,682,684,686,688 and 690), not on Fig. 6 hereinbefore to it It is described, with being worked previously with respect to Fig. 1 same or like modes described.It only difference is in view of in Fig. 6 What corresponding conduit had been labeled in the particular system embodiment described, Fig. 6 is different.In addition, not above for What Fig. 6 was illustrated is related to the remaining step (and of conduit 610,612,614,616,618,620,630,632 of liquefaction gas containing hydrocarbon 634) and the first closed loop hybrid refrigeration cycle (conduit 636,638,640,642,644,646,648,650,652,654, 656th, 658,660,662 and 668) in the step of do not consider with being worked previously with respect to Fig. 1 same or like modes described.

In the figure 7, liquefied natural gas (LNG) recvery facility 10 is depicted as containing turbine expander 94, the turbine expansion Device is operably connected to the cooled region 38 of the second refrigeration system 14 by conduit 722.As shown in Fig. 7, pass through cooling zone At least a portion of the hydrocarbonaceous feed air-flow of the cooling duct 40 in domain 38 can be directed into turbine expander by conduit 722 94, wherein it can be expanded into two phase flow.Turbine expander 94 can be in the same or like condition described as previously discussed with respect to Fig. 2 Lower operation.Although not describing in the figure 7, suction drum can be in turbine expander 94 and cooled region in certain embodiments It is in fluid communication between 38.

The two phase flow expanded in conduit 724 is then routed to separator 98, and the separator is by the flow separation of expansion into first The less liquid heavy distillat (conduit 726) of alkane and the top layer vapor fraction (conduit 728) rich in methane.Separator 98 can be with As previously discussed with respect to Fig. 2 describe identical separation container and can be worked under the conditions of similar operations.After releasing, lead At least a portion of top layer vapor fraction in pipe 728 is then reintroduced in the cooling duct 40 of cooled region 38 with such as Above for further being condensed and be subcooled described in Fig. 1.

Less methane bottom stream in conduit 726 can be in a liquid state form and can containing initially in conduit 724 What is found in stream has the major part of the compound of six or more carbon atoms.For example, the less methane in conduit 626 Bottom stream, which can include initially appearing in the stream from conduit 724, has the compound of six or more carbon atoms extremely Few 70%, 80%, 90%, 95% or 99%.

The top layer vapor stream rich in methane can include most methane in conduit 728.For example, in conduit 728 Top layer vapor stream rich in methane can include at least about 10,25,40 or 50 and/or no more than about 99.9,99,95 or 85 The methane of molar percentage.More precisely, the top layer vapor stream that methane is rich in conduit 728 can be included in about 10 and arrive 99.9th, the methane of the molar percentage in the range of 25 to 99,40 to 95 or 50 to 85.In addition, being rich in the top of methane in conduit 728 Layer vapor stream can include initially appearing at least 50% of methane in the stream from conduit 724,60%, 70%, 80%, 90%th, 95%, 99% or 99.9%.

Fig. 7 is returned again to, turbine expander 94 is connected to compressor 96 by axostylus axostyle 95.Compressor 96 can be at least partly Ground is driven by the work(from turbine expander 94.As shown in Fig. 7, the mix refrigerant of gaseous state second of gasification passes through conduit 768 Leave the refrigerant heat passage 42 in cooled region 38 and be subsequently introduced into compressor 96, be introduced in compressor Before 72, it is compressed in compressor 96.After being compressed, the compression stream in conduit 770 is introduced in the first compressor Level 74 and is further processed as discussed above for Fig. 1.Although not describing in the figure 7, suction drum can be It is in fluid communication between compressor 96 and heating passage 42.

It should be noted that the first refrigeration system 12, the second refrigeration system 14, and the first closed loop as depicted in Figure 7 mixing system SAPMAC method (conduit 736,738,740,742,744,746,748,750,752,754,756,758,760,762,764 and 766), It is not described hereinbefore on Fig. 7, with being worked previously with respect to Fig. 1 same or like modes described.Only Difference be to consider particular system embodiment depicted in figure 7, in Fig. 7 corresponding conduit it is labeled not Together.In addition, not above for Fig. 7 illustrate be related to liquefaction gas containing hydrocarbon remaining step (conduit 710,712,714, 716th, 718,720,730,732 and 734) and the second closed loop hybrid refrigeration cycle (conduit 772,774,776,778, 780th, 782,784,786,788 and 790) in the step of do not consider to be risen with the same or like mode described previously with respect to Fig. 1 Effect.

Definition

It should be understood that herein below is not meant as the exclusiveness list of defined term.For example, for example, when with upper Hereinafter using when defining term, other definition can be provided in the foregoing description.

As used herein, term " one " and "the" mean one or more.

As used herein, when in the list for two or more project, term "and/or" means to adopt With any one in Listed Items in itself, or can use Listed Items in two or more any combinations.Citing comes Say, if composition be described as containing component A, B and/or C, composition can only contain A；Only contain B；Only contain C；Contain A and B Combination；Combination containing A and C；Combination containing B and C；Or the combination containing A, B and C.

As used herein, term " comprising " is open transitional term, and it is used for the subject described before term The one or more elements described after term are transitioned into, the one or more elements wherein enumerated after transitional term simultaneously differ Surely it is the unique elements for constituting subject.

As used herein, term " having " has and the open implication of " comprising " identical proposed above.

As used herein, term "comprising" has and the open implication of " comprising " identical proposed above.

As used herein, term " first ", " second ", " the 3rd " etc. are used to describe various key elements, and it is such will Element should not be limited by these terms.These terms are only used for distinguishing a key element and another key element and necessarily not implied that specific Order or even specific key element.For example, without departing from the scope of the invention, can in embodiments by One key element is regarded as " first " key element and is regarded as " second " key element in detail in the claims.In embodiment and each rights to independence Being consistent property during profit is required, but such term is not necessarily referring to being consistent therebetween.

Digital scope

Embodiment of the present invention quantifies some parameters related to the present invention using digital scope.It should be understood that when offer number During word scope, such scope should be interpreted to provide word support with the limitation of the lower limit of advocating only to describe the scope and Opinion only describes the limitation of the higher limit of the scope.For example, the digital scope disclosed in 10 to 100 is provided for chatting State and " " be less than the word branch of the opinion of 100 " (not having lower range) more than the opinion of 10 " (not having upper range) and narration Hold.

Claims are not limited to the disclosed embodiments

Invention described above preferred form is used only as diagram, and should not use to explain with restrictive, sense The scope of invention.Without departing from the spirit of the invention, those skilled in the art will be readily available and be described above Exemplary embodiment modification.

Their intention is set fourth as dependent on equivalent principle determining and assessing the suitable of the present invention by the present inventor hereby Local fair scope, because it is related to substantially without departing from the text of the invention still illustrated in such as appended claims Any equipment outside word scope.

Claims

1. a kind of method for the gas containing hydrocarbon that liquefies, methods described includes：

(a) stream of entering by the first mix refrigerant and including gas containing hydrocarbon is incorporated into the first refrigeration system；

(b) by entering stream described in being cooled down with the indirect heat exchange of first mix refrigerant in first refrigeration system At least a portion enter stream so as to form the first cooling；

(c) by cooling down the described first charging cooled down in the second refrigeration system with the indirect heat exchange of the second mix refrigerant At least a portion of stream enters stream so as to form the second cooling；

(d) make described in turbine expander the first cooling enter stream or at least a portion for entering stream of second cooling is swollen It is swollen to enter stream so as to form expansion；

(e) at least a portion for entering stream of the expansion in separation separator is so as to form top layer vapor fraction and liquid bottom Portion's cut；

(f) at least one of the top layer vapor fraction being cooled in first refrigeration system or second refrigeration system Point；And

(g) compressor is driven with the turbine expander.

2. according to the method described in claim 1, it further comprises making at least a portion of first mix refrigerant swollen Swollen the first mix refrigerant so as to form expansion, wherein the first mix refrigerant of the expansion is used as the step (b) Cooling period first mix refrigerant.

3. method according to claim 2, it further comprises making first mix refrigerant in step (b) extremely Few part supercooling so as to form the first mix refrigerant of supercooling, wherein the first mix refrigerant of the supercooling be subjected to it is swollen Swollen first mix refrigerant.

4. according to the method described in claim 1, further comprise making at least a portion of second mix refrigerant to expand So as to form the second mix refrigerant of expansion, wherein the second mix refrigerant of the expansion is used as the step (c) Second mix refrigerant of cooling period.

5. method according to claim 4, further comprises making second mix refrigerant in step (c) at least Part supercooling is so as to form the second mix refrigerant of supercooling, wherein the second mix refrigerant of the supercooling is to be subjected to expansion Second mix refrigerant.

6. according to the method described in claim 1, wherein it is described first cooling enter stream during the expansion of the step (d) Expansion, wherein the top layer vapor fraction is cooled down in first refrigeration system.

7. according to the method described in claim 1, wherein it is described second cooling enter stream during the expansion of the step (d) Expansion, wherein the top layer vapor fraction is cooled down in second refrigeration system.

8. according to the method described in claim 1, wherein at least one of the first mix refrigerant described in the compressor compresses Point.

9. according to the method described in claim 1, wherein at least one of the second mix refrigerant described in the compressor compresses Point.

10. according to the method described in claim 1, wherein the compressor compresses described before the cooling of the step (f) At least a portion of top layer vapor fraction.

11. a kind of method for the gas containing hydrocarbon that liquefies, methods described includes：

(d) at least a portion for entering stream of second cooling in separation separator is so as to form top layer vapor fraction and liquid State bottom fraction；And

(e) at least one of the top layer vapor fraction being cooled in first refrigeration system or second refrigeration system Point.

12. method according to claim 11, it further comprises making at least a portion of first mix refrigerant Expansion is so as to form the first mix refrigerant of expansion, wherein the first mix refrigerant of the expansion is used as the step (b) first mix refrigerant of cooling period.

13. method according to claim 12, it further comprises making first mix refrigerant in step (b) At least a portion supercooling is so as to form the first mix refrigerant of supercooling, wherein the first mix refrigerant of the supercooling is to be subjected to First mix refrigerant of expansion.

14. method according to claim 11, further comprises making at least a portion of second mix refrigerant swollen Swollen the second mix refrigerant so as to form expansion, wherein the second mix refrigerant of the expansion is used as the step (c) Cooling period second mix refrigerant.

15. method according to claim 14, further comprises making second mix refrigerant in step (c) extremely Few part supercooling so as to form the second mix refrigerant of supercooling, wherein the second mix refrigerant of the supercooling be subjected to it is swollen Swollen second mix refrigerant.

16. method according to claim 11, it further comprises making entering for second cooling in turbine expander At least a portion expansion of stream enters stream so as to form expansion, wherein the stream of entering of the expansion is in the separation of (d) It is described second cooling enter stream.

17. method according to claim 16, it further comprises what is driven at least in part by the turbine expander Compressor, wherein the compressor compresses first mix refrigerant, second mix refrigerant or institute at least in part State top layer vapor fraction.

18. method according to claim 17, wherein the compressor compresses first hybrid refrigeration at least in part Agent.

19. method according to claim 17, wherein the compressor compresses second hybrid refrigeration at least in part Agent.

20. method according to claim 17, wherein the compressor compresses the top layer vapor fraction at least in part.

21. method according to claim 11, the top layer vapor fraction being cooled in second refrigeration system At least partially.

22. a kind of system for the gas containing hydrocarbon that liquefies, the system includes：

(a) the first refrigeration system, it includes the first cooled region being disposed therein, wherein first cooled region is configured With by with the cooling of the indirect heat exchange of the first mix refrigerant includes gas containing hydrocarbon enters stream so as to form the first cooling Enter stream；

(b) the first closed loop hybrid refrigeration cycle, it is at least partially disposed in first refrigeration system, wherein described first Closed loop hybrid refrigeration cycle includes first mix refrigerant；

(c) the second refrigeration system, it is in fluid communication with first refrigeration system, wherein second refrigeration system includes setting The second cooled region wherein, wherein second cooled region is configured to the indirect thermal with the second mix refrigerant Exchange cooling first cooling enter stream to form the second cooling enter stream；

(d) the second closed loop hybrid refrigeration cycle, it is at least partially disposed in second refrigeration system, wherein described second Closed loop hybrid refrigeration cycle includes second mix refrigerant；

(e) turbine expander, it is in fluid communication with first refrigeration system or second refrigeration system, wherein the turbine Expander be configured so that it is described first cooling enter stream or it is described second cooling enter stream be expanded into expansion stream；

(f) separator, it is in fluid communication with the turbine expander, wherein the separator is configured to the expansion flow point From into top layer vapor fraction and liquid bottom cut；

(g) conduit, it is used to make at least a portion of the top layer vapor fraction to return to first refrigeration system or described Second refrigeration system；And

(h) compressor, it is driven by the work(from the turbine expander at least in part, wherein the compressor is configured to First mix refrigerant, second mix refrigerant or the top layer vapor fraction are compressed at least in part.

23. system according to claim 22, wherein the turbine expander is in fluid communication with first refrigeration system And at least a portion of the top layer vapor fraction is returned to first refrigeration system by the conduit.

24. system according to claim 22, wherein the turbine expander is in fluid communication with second refrigeration system And at least a portion of the top layer vapor fraction is returned to second refrigeration system by the conduit.