CN103374424A - Natural gas liquefaction with feed water removal - Google Patents

Natural gas liquefaction with feed water removal Download PDF

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Publication number
CN103374424A
CN103374424A CN2013101243097A CN201310124309A CN103374424A CN 103374424 A CN103374424 A CN 103374424A CN 2013101243097 A CN2013101243097 A CN 2013101243097A CN 201310124309 A CN201310124309 A CN 201310124309A CN 103374424 A CN103374424 A CN 103374424A
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cooling
natural gas
stream
compression
heat exchanger
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A.A.布罗斯托
G.E.基纳
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
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    • F25J1/0057—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream after expansion of the liquid refrigerant stream with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
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    • F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0205—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a dual level SCR refrigeration cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F25J1/0215—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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Abstract

The invention relates to natural gas liquefaction with feed water removal. A method and apparatus for drying and liquefying a natural gas stream is described, in which: (a) the water containing natural gas feed stream is cooled; (b) the cooled natural gas feed stream is dried and further cooled; (c) the dried cooled natural gas stream is heated; (d) the dried rewarmed natural gas stream is cooled and liquefied and at least one compressed refrigerant feed stream is cooled by counter-current indirect heat exchange with an expanded cold refrigerant; and (e) the compressed cold refrigerant stream or streams are expanded, and thereby further cooled, to provide said expanded cold refrigerant; wherein the cooling of the natural gas feed stream in step (a) and heating of the dried cooled natural gas stream in step (c) is by indirect heat exchange between said two streams.

Description

The natural gas liquefaction that dewaters with feed
Technical field
The present invention relates to be used to making the method and apparatus that natural gas flow is dry and liquefy.
Background technology
Comprise at natural gas flow in the situation of water, before the liquefaction of Sweet natural gas can be carried out, be necessary at first to make this fluidized drying to remove all from it or whole water basically.In order to remove water (with other impurity such as mercury) from Sweet natural gas before liquefaction, another common practice is at first feed to be cooled to below the envrionment temperature, especially when envrionment temperature is high.
The example that comprises the liquefaction cycle of this in advance cooling step is in advance cooling mixing cooling agent (" C3MR ") circulation of propane.In these class methods, propane (or the different liqs cooling agent in the steam compression cycle) is used in drying step to carry out before the Sweet natural gas feed being cooled to preferred temperature.Then, be introduced into main cryogenic heat exchanger (" MCHE ") before at now dry feed, can further cool off described feed with the identical liquid cryogen of lower pressure.Be used for the cooling agent of liquefaction, for example mixed cooling medium (" MR ") also is cooled to roughly the same temperature in advance.Therefore, all streams that enter the hot junction of MCHE all are in roughly the same temperature, have reduced thus the thermal stresses among the MCHE.
May there be another problem in the in advance cooling of saturated gas.That is, if strictly do not control the temperature of Sweet natural gas during this cooling step, the risk that then can exist hydrate to form.Single composition liquid cryogen (such as propane) that use is vaporized for cooled natural gas feed in advance allows good temperature control, because under any setting pressure, the temperature of this cooling agent vaporization can not change (yet, for example, for mixed cooling medium stream, vaporization temperature will change with any change of the ratio of the different cooling agent that exist in the stream and with any change of flowing pressure).
At US 4,755, the example that solves the prior art that the hydrate in the C3MR circulation forms has been described in 200, the disclosure of this application is incorporated herein by reference, wherein before dewatering with single composition steam compression cycle freezing Sweet natural gas feed.By with indirect heat exchange from the mixed cooling medium steam of MCHE, with the dry natural gas further cooling before being supplied to MCHE that obtains.
Yet, US 4,755, the C3MR technique of describing in 200 and wherein a shortcoming of other this type of technique of cooled natural gas feed is making Sweet natural gas come in advance with the single composition liquid cryogen in the steam compression cycle before liquefying in the MCHE of mixed cooling medium, they need to use extra refrigerant loop (being propane or other single composition loop).This has increased floor space (footprint) and the capital investment cost of liquefaction device.
Also exist and do not comprise with propane and come the in advance known NG Liquefaction cycle of cooled natural gas feed stream.These comprise such as US 6,347, single mixed cooling medium (" SMR ") circulation of describing in 531, such as US 6,119, two mixed cooling mediums (" DMR ") of describing in 479 circulate and reclaim (" N2 recovery ") circulation such as the nitrogen of describing among the US 2010/0122551, and each disclosure of applying for is incorporated herein by reference.
In these class methods, the part of cooling agent (MR or gaseous nitrogen) can be from main refrigerant loop one extract and be used for before dewatering, cooling off feed.Because MR or provide refrigeration in certain temperature range such as the pure gaseous refrigerant of nitrogen, thereby be difficult to control temperature and form to prevent the water compound.In addition, optimize the MR composition so that the refrigeration under the colder temperature to be provided, and nitrogen reclaim circulation (dense-air refrigeration cycle) inherently under hotter temperature efficient low.From the viewpoint of efficient, need to reduce to cool off in advance responsibility.
US 6,793, and 712 (its disclosure is incorporated herein by reference) disclose cascade process, wherein at first make the saturated gas feed dry and then expand in the isentropic expansion device.Before sour gas is removed, the cold Sweet natural gas that obtains is heated in the second interchanger in First Heat Exchanger and then.Its then before further dewatering by with the second interchanger in cold Sweet natural gas indirect heat exchange cool down, and then equally by with cold Sweet natural gas indirect heat exchange in First Heat Exchanger further the cooling.Then make Sweet natural gas further cooling and liquefaction.The shortcoming of this technique is, its needs at least one rotating machinery (being the isentropic expansion device) and two interchanger an interchanger of side header (or with), and has reduced liquefaction efficiency by the feeding pressure that reduces that the expansion in the isentropic expansion device causes.
Therefore, needs in advance the cooled natural gas feed need alternative and/or improved NG Liquefaction cycle (reclaiming circulation such as but not limited to SMR, DMR and N2) in this area to be used in the situation about dewatering.
A purpose of embodiments of the invention provides a kind of liquefaction cycle, and wherein the temperature mismatch of MCHE bottom reduces, and the overall efficiency of liquefaction cycle improves.
The another purpose of the preferred embodiments of the present invention provides the good temperature control of the in advance cooling period of Sweet natural gas feed, forms in order to prevent or reduce hydrate.
Summary of the invention
According to a first aspect of the invention, provide a kind of be used to making the method that natural gas flow is dry and liquefy, the method comprises:
(a) cooling comprises the Sweet natural gas feed stream of water, to produce the natural gas flow of cooling;
(b) the Sweet natural gas feed diffluence from cooling dewaters and with its further cooling, to produce the natural gas flow of drying, cooling;
(c) natural gas flow of heat drying, cooling is to produce the natural gas flow of drying, improvements;
(d) natural gas flow of drying, improvements is cooled off and liquefaction, and cool off at least one compression refrigerant feed stream by the convection current indirect heat exchange with the cold cooling agent that expands, with the cold cryogen flow that produces liquefied natural gas product stream, at least one compression and the cryogen flow that expands, warms; And
(e) the cold cryogen flow of one or more strands of compressions is expanded and thus further cooling, so that the cold cooling agent of described expansion to be provided;
Wherein, the heating of the Sweet natural gas of the middle drying of the cooling of Sweet natural gas feed stream and step (c), cooling is undertaken by the indirect heat exchange between described two plumes in the step (a).
According to a second aspect of the invention, provide a kind of be used to making the equipment that natural gas flow is dry and liquefy, this equipment comprises:
Joint heat exchanger (economizer heat exchanger), it be used for to receive natural gas flow of saturated gas feed stream and dry, cooling and is used for the natural gas flow that indirect heat exchange by each other cools off saturated gas feed stream and heat drying, cooling, in order to produce saturated gas feed stream and the natural gas flows dry, that get warm again after a cold spell of cooling;
With joint heat exchanger and each other Sweet natural gas feed water scavenging system and the Sweet natural gas feed cooling system of fluid flow communication, it is used for receiving from the joint heat exchanger saturated gas feed stream, dry and further cool off described stream and make the drying that obtains, the natural gas flow of cooling turn back to the joint heat exchanger of cooling;
Main cryogenic heat exchanger, the cooling agent feed stream that it is used for making natural gas flow cooling and the liquefaction of drying, improvements and is used for cooling off by the convection current indirect heat exchange with the cold cooling agent that expands at least one compression is so that the cryogen flow that produces the cold cryogen flow of liquefied natural gas product stream, at least one compression and expansion, warms;
Piping arrangement, it is used for natural gas flow dry, that get warm again after a cold spell is passed to the hot junction of main cryogenic heat exchanger from the joint heat exchanger, and is used for extracting liquefied natural gas product stream from the cold junction of main cryogenic heat exchanger; And
With the cooling agent expansion system of main cryogenic heat exchanger fluid flow communication, its be used for from the cold junction of cryogenic heat exchanger receive at least one compression cold cryogen flow, described cold cooling agent is expanded and thus further cooling and make the cold cooling agent of expansion turn back to the cold junction of cryogenic heat exchanger.
Description of drawings
Fig. 1 is according to an embodiment of the invention be used to making natural gas flow dry and the equipment of liquefaction and the block diagram of method.
Fig. 2 makes the equipment of the dry and liquefaction of natural gas flow and exemplary closed circuit mixed cooling medium system that method is used and the block diagram of technique for being used for of describing at Fig. 1.
Fig. 3 be according to another embodiment of the present invention be used for making natural gas flow dry and the equipment of liquefaction and the block diagram of method.
Embodiment
As mentioned above, in a first aspect of the present invention, provide a kind of be used to making the method that natural gas flow is dry and liquefy, the method comprises above-mentioned steps: (a) cooled natural gas feed stream, (b) the Sweet natural gas feed diffluence from cooling dewaters and makes its further cooling, (c) heat drying, the natural gas flow of cooling, (d) make drying, the natural gas flow cooling that gets warm again after a cold spell and liquefaction are also cooled off the cooling agent feed stream of at least one compression by the convection current indirect heat exchange with the cold cooling agent that expands, and the cold cryogen flow that (e) makes compression expands and thus further cooling, so that the cold cooling agent of described expansion to be provided, wherein, dry in the cooling of Sweet natural gas feed stream and the step (c) in the step (a), the heating of the Sweet natural gas of cooling is undertaken by the indirect heat exchange between described two plumes.
As used herein, term " expansion " refers to reduce by any suitable means the pressure of the fluid of discussing, and in the situation of liquid, unless refer else, can comprise at least part of vaporization or the simply reduction of pressure.
As used herein, term " dry " refers to remove all or whole fluid of water basically from it.More specifically, it means or has removed all water, or the residual amount that keeps is enough low so that can ignore the impact of follow-up fluid handling.Especially, in the situation of " dry natural gas flow ", or removed all water, or the amount of any residual water that keeps in the described stream is enough low consequently can not analyse any operational issue that causes in downstream cooling and the liquefaction process owing to water freezes.
As used herein, term " indirect heat exchange " refers to the heat exchange between two fluid streams, wherein the physical barriers of two fluid streams by certain form keep separated from one another (for example, indirect heat exchange occurs, because the pipe side liquid keeps separating with shell fluid by tube wall) in shell and tube heat exchanger.This is opposite with wherein fluid contact and blendable " direct heat exchange " (for example, as wherein between the convection current of tower of flowing through except in the washing tower that mass transfer also can occur conducting heat).
In a preferred embodiment, in step (c), natural gas flow dry, cooling is heated to the temperature roughly the same with the temperature of the cooling agent feed stream of at least one compression, so that the temperature of the cooling agent feed stream of dry, the natural gas flow that gets warm again after a cold spell and at least one compression is roughly the same when step (d) begins.Preferably, Sweet natural gas feed stream also is in the temperature roughly the same with the temperature of cooling agent feed stream when step (d) begins of drying, the natural gas flow that gets warm again after a cold spell and at least one compression when step (a) begins.
Preferably, in step (c), natural gas flow dry, cooling be heated to temperature with the cooling agent feed stream of at least one compression identical or 20 ℃ of this temperature with interior, more preferably 10 ℃ of this temperature with interior temperature so that the cooling agent feed of dry when step (d) begin, the natural gas flow that gets warm again after a cold spell and at least one compression do not exist between flowing the temperature difference or existence less than 20 ℃, more preferably less than 10 ℃ the temperature difference.Preferably, the Sweet natural gas feed stream temperature when step (a) begin also with the cooling agent feed of dry, the natural gas flow that gets warm again after a cold spell and at least one compression flow temperature when step (d) begins roughly the same or 20 ℃ of this temperature with interior, more preferably in 10 ℃ in this temperature.
In a preferred embodiment, in shell-tube type cryogenic heat exchanger, performing step (d) in the coiled heat exchanger most preferably.
In a preferred embodiment, in the step (b) of the method, the Sweet natural gas feed of cooling stream at first is dried to remove water from it, then is further cooled to produce the natural gas flow of drying, cooling.Alternatively, can carry out described step with reverse order, wherein feed stream at first is further cooled and is then dry to produce the natural gas flow of drying, cooling.Yet a rear selection generally is less preferred.
In one embodiment, step (d) and (e) in cooling agent or mixed cooling medium (mixture that comprises hydrocarbon for example and/or perfluoro-hydrocarbon), the cold cryogen flow of compression is to expand in liquid stream or mixed phase flow and the step (d) in the step (d) in the case, the cryogen flow that warms is mixed phase or vapour stream, or gaseous refrigerant is (such as pure nitrogen gas or argon gas, 99mol.% or higher for example), it runs through step (d) and (e) keeps being basic gaseous form (that is, maximum 12mol.% of cooling agent wherein, more preferably at most 5mol.% and most preferably do not have cooling agent running through step (d) and any point (e) is liquid form).
In a preferred embodiment, the method is further comprising the steps of: (f) compress and preferably cool off the cryogen flow that (for example by one or more interstage coolers and/or aftercooler) expands, warms, to be provided at the cooling agent feed stream of described at least one compression of cooling in the step (d).
In one embodiment, step (f) comprises the cryogen flow that compression and cooling are expanded, warmed, flow and additional compression cryogen flow to be provided at described at least one compression refrigerant feed that cools off in the step (d), the method also comprises to be made described additional compression cryogen flow expansion with the described stream of further cooling and utilizes the described extra cryogen flow of further cooling off in step (b) to come the further Sweet natural gas feed stream that cools off through cooling by indirect heat exchange.Preferably, step (f) comprises the cryogen flow compression that will expand, warm, cools off and is separated, liquid stream with vapour stream that compression refrigerant is provided and compression refrigerant, described vapour stream is formed in the step (d) cooling and at least one compression refrigerant feed stream of liquefaction at least in part, and at least a portion of described liquid stream form expand and then in step (b), be used for by indirect heat exchange and further cooling through the extra cryogen flow of the Sweet natural gas feed stream of cooling.
In another embodiment, in step (d), make the natural gas flow cooling of drying, improvements and liquefy to produce liquefied natural gas product stream and extra liquefied natural gas stream, described extra liquefied natural gas stream is used for further cooling off the Sweet natural gas feed stream through cooling in step (b).Preferably, in step (b), by further cool off the Sweet natural gas feed stream through cooling with the convection current direct heat exchange of described extra liquefied natural gas stream.
Also as indicated above, in a second aspect of the present invention, provide a kind of be used to making the equipment that natural gas flow is dry and liquefy, this equipment comprises above-mentioned joint heat exchanger, Sweet natural gas feed water scavenging system and Sweet natural gas feed cooling system, main cryogenic heat exchanger, piping arrangement and cooling agent expansion system.Described equipment is suitable for the method for executive basis first aspect.Therefore, in the another preferred embodiment of first aspect, the method for executive basis a first aspect of the present invention in according to the equipment of second aspect.
In the preferred embodiment according to the equipment of second aspect, main cryogenic heat exchanger is shell-tube type, and is most preferably coiled heat exchanger.
Sweet natural gas feed water scavenging system is preferably in the upstream of Sweet natural gas feed cooling system, so that at first dry in described water scavenging system from the cooling saturated gas of joint heat exchanger, and then from dry natural gas further cooling in described cooling system of described water scavenging system, turn back to subsequently the drying that saves heat exchanger, the Sweet natural gas of cooling to produce.Alternatively, can reverse the order of described system, so that from first further cooling and then dry in described water scavenging system in described cooling system of the cooling saturated gas that saves heat exchanger.Yet same, a described rear selection generally is less preferred.
Alternatively, at Sweet natural gas feed water scavenging system in the situation of Sweet natural gas feed cooling system upstream, can make the dry natural gas from water scavenging system turn back to joint heat exchanger and further cooling in the joint heat exchanger before being sent to cooling system and therein further cooling, turn back to subsequently the drying that saves heat exchanger, the Sweet natural gas of cooling to produce.
In a preferred embodiment, this equipment comprises that also (it is preferably cooling agent compression and cooling system with the cooling agent compression system of main cryogenic heat exchanger fluid flow communication, described cooling is for example provided by one or more interstage coolers and/or aftercooler), it is used for receiving from the hot junction of cryogenic heat exchanger the hot junction that cryogen flow, the described cooling agent of compression (with preferably cooling) that expands, warms and the cooling agent feed stream that makes at least one compression turn back to cryogenic heat exchanger.Main cryogenic heat exchanger, cooling agent expansion system and cooling agent compression system can form the closed circuit refrigerant system or form its part, are housed inside the cryogen flow that described closed loop system cooling agent interior and circulation within it comprises described compression and expansion.As in according to the method for first aspect, described cooling agent for example can be mixed cooling medium (mixture that comprises hydrocarbon for example and/or perfluoro-hydrocarbon), or such as the pure gaseous refrigerant of pure (for example 99mol.% or higher) nitrogen or argon gas.
In one embodiment, Sweet natural gas feed cooling system is indirect heat exchanger, and this equipment also comprises the additional expansion system with cooling agent compression and cooling system and Sweet natural gas feed cooling system fluid flow communication, it is used for from the cooling agent compression and cooling system receives the cryogen flow of compressed and cooling and described stream is expanded with the described stream of further cooling, and Sweet natural gas feed cooling system comes by indirect heat exchange further cooling through the Sweet natural gas feed stream of cooling with the stream of described further cooling.Cooling agent compression and cooling system also can comprise at least one phase separator, its cooling agent that is used for compressing and cooling off is separated into liquid and gas, described one or more phase separator is communicated with main cryogenic heat exchanger and additional expansion system fluid stream, so that the vapour stream of compression refrigerant is supplied to the hot junction of cryogenic heat exchanger and the liquid stream of compression refrigerant is supplied to the additional expansion system.
In an alternative, this equipment also comprises piping arrangement, it is used for extra liquefied natural gas stream is passed to Sweet natural gas feed cooling system from main cryogenic heat exchanger, and described feed cooling system flows with the Sweet natural gas feed that described extra liquefied natural gas stream further cools off through cooling.For example, Sweet natural gas feed cooling system can be by further cooling off system's (for example washing tower) that the Sweet natural gas feed through cooling off flows with the convection current direct heat exchange of described extra liquefied natural gas stream in the case.
Therefore, the present invention includes the aspect of the following #1 to #20 of being designated as:
#1. method that is used for making natural gas flow drying and liquefaction, the method comprises:
(a) cooling comprises the Sweet natural gas feed stream of water, to produce cooled natural gas stream;
(b) dewater and with its further cooling, to produce the natural gas flow of drying, cooling from the diffluence of cooled natural gas feed;
(c) natural gas flow of heat drying, cooling is to produce the natural gas flow of drying, improvements;
(d) make the natural gas flow cooling of drying, improvements and liquefaction and cool off the cooling agent feed stream of at least one compression by the convection current indirect heat exchange with the cold cooling agent that expands, with the cold cryogen flow that produces liquefied natural gas product stream, at least one compression and expansion, the cryogen flow that warms; And
(e) the cold cryogen flow of one or more strands of compressions is expanded and thus further cooling, so that the cold cooling agent of described expansion to be provided;
Wherein, the heating of the Sweet natural gas of the middle drying of the cooling of Sweet natural gas feed stream and step (c), cooling is undertaken by the indirect heat exchange between described two plumes in the step (a).
#2. is according to the described method of #1, wherein, in step (c), natural gas flow dry, cooling be heated to temperature with the cooling agent feed stream of at least one compression identical or 20 ℃ of this temperature with interior temperature, so that when step (d) begins, between the cooling agent feed stream of dry, the natural gas flow that gets warm again after a cold spell and at least one compression, do not exist the temperature difference or existence less than 20 ℃ the temperature difference.
#3. is according to the described method of #2, wherein, the Sweet natural gas feed stream temperature when step (a) begin is also with in the cooling agent feed of dry, the natural gas flow that gets warm again after a cold spell and at least one compression flows identical or in this temperature 20 ℃ of temperature when step (d) begins.
#4. is according to each described method among the #1 to #3, wherein, and performing step in the wound form cryogenic heat exchanger (d).
#5. is according to each described method among the #1 to #4, and wherein, in step (b), the Sweet natural gas feed of cooling stream at first is dried to dewater from it, and then is further cooled to produce the natural gas flow of drying, cooling.
#6. is according to each described method among the #1 to #5, wherein, step (d) and (e) in cooling agent or mixed cooling medium, the cold cryogen flow of the one or more strands of compressions in the step (d) is that the expansion in liquid phase or mixed phase flow and the step (d), the cryogen flow that warms are mixed phase or vapour stream, or runs through step (d) and (e) keep being the gaseous refrigerant of basic gaseous form.
#7. is according to each described method among the #1 to #6, and wherein, the method also comprises: (f) compression-expansion, the cryogen flow that warms, and to be provided at the cooling agent feed stream of described at least one compression of cooling in the step (d).
#8. is according to the described method of #7, wherein, step (f) comprises the cryogen flow that compression and cooling are expanded, warmed, to be provided at described at least one compression refrigerant feed stream and additional compression cryogen flow of the middle cooling of step (d), the method also comprises to be made described additional compression cryogen flow expansion with the described stream of further cooling and uses the described extra cryogen flow of further cooling off in step (b) to come by indirect heat exchange the Sweet natural gas feed stream of further cooling through cooling off.
#9. is according to the described method of #8, wherein, step (f) comprises the cryogen flow compression that will expand, warm, cools off and is separated, liquid stream with vapour stream that compression refrigerant is provided and compression refrigerant, described vapour stream is formed in the step (d) cooling and at least one compression refrigerant feed stream of liquefaction at least in part, and at least a portion of described liquid stream form expand and then in step (b), be used for by indirect heat exchange and further cooling through the extra cryogen flow of the Sweet natural gas feed stream of cooling.
#10. is according to each described method among the #1 to #7, wherein, in step (d), natural gas flow dry, that get warm again after a cold spell is cooled and liquefies to produce liquefied natural gas product stream and extra liquefied natural gas stream, and described extra liquefied natural gas stream is used for further cooling through the Sweet natural gas feed stream of cooling in step (b).
#11. wherein, in step (b), flows by the Sweet natural gas feed that further cools off through cooling with the convection current direct heat exchange of described extra liquefied natural gas stream according to the described method of #10.
#12. equipment that is used for making natural gas flow drying and liquefaction, this equipment comprises:
The joint heat exchanger, it is used for receiving saturated gas feed stream and natural gas flow dry, cooling, and be used for the natural gas flow that indirect heat exchange by each other cools off saturated gas feed stream and heat drying, cooling, in order to produce saturated gas feed stream and the natural gas flows dry, that get warm again after a cold spell of cooling;
With joint heat exchanger and each other Sweet natural gas feed water scavenging system and the Sweet natural gas feed cooling system of fluid flow communication, it is used for receiving from the joint heat exchanger saturated gas feed stream, dry and further cool off described stream and make the drying that obtains, the natural gas flow of cooling turn back to the joint heat exchanger of cooling;
Main cryogenic heat exchanger, it is used for making natural gas flow cooling and the liquefaction of drying, improvements, and be used for cooling off at least one compression refrigerant feed stream by the convection current indirect heat exchange with the cold cooling agent that expands, so that the cryogen flow that produces the cold cryogen flow of liquefied natural gas product stream, at least one compression and expansion, warms;
Piping arrangement, it is used for natural gas flow dry, that get warm again after a cold spell is passed to the hot junction of main cryogenic heat exchanger from the joint heat exchanger, and is used for extracting liquefied natural gas product stream from the cold junction of main cryogenic heat exchanger; And
With the cooling agent expansion system of main cryogenic heat exchanger fluid flow communication, its be used for from the cold junction of cryogenic heat exchanger receive at least one compression cold cryogen flow, described cold cooling agent is expanded and thus further cooling and make the cold cooling agent of expansion turn back to the cold junction of cryogenic heat exchanger.
#13. is according to the described equipment of #12, and wherein, main cryogenic heat exchanger is coiled heat exchanger.
#14. is according to #12 or the described equipment of #13, wherein, Sweet natural gas feed water scavenging system is in the upstream of Sweet natural gas feed cooling system, so that at first dry in described water scavenging system from the cooling saturated gas of joint heat exchanger, and from the then further cooling in described cooling system of dry natural gas of described water scavenging system, to produce the drying of getting back to subsequently the joint heat exchanger, the Sweet natural gas of cooling.
#15. is according to each described equipment among the #12 to #14, and wherein, this equipment also comprises:
With the cooling agent compression system of main cryogenic heat exchanger fluid flow communication, it is used for receiving from the hot junction of cryogenic heat exchanger the cryogen flow that expands, warm, compress described cooling agent and make the cooling agent feed stream of at least one compression turn back to the hot junction of cryogenic heat exchanger.
#16. is according to the described equipment of #15, wherein, main cryogenic heat exchanger, cooling agent expansion system and cooling agent compression system form the closed circuit refrigerant system or form its part, be contained in the cryogen flow that described closed loop system cooling agent interior and circulation within it comprises described compression and expansion, described cooling agent is mixed cooling medium or pure nitrogen gas or argon gas.
#17. is according to #15 or the described equipment of #16, wherein, the compression of cooling agent compression system and cooling are expanded, the cooling agent that warms, and Sweet natural gas feed cooling system is indirect heat exchanger, and wherein, this equipment also comprises the additional expansion system with cooling agent compression system and Sweet natural gas feed cooling system fluid flow communication, it is used for receiving the cryogen flow of compression and cooling and described stream being expanded with the described stream of further cooling from the cooling agent compression system, and Sweet natural gas feed cooling system comes by indirect heat exchange further cooling through the Sweet natural gas feed stream of cooling with the stream of described further cooling.
#18. is according to the described equipment of #17, wherein, the cooling agent compression system also comprises at least one phase separator, its cooling agent that is used for compressing and cooling off is separated into liquid and gas, described one or more phase separator is communicated with main cryogenic heat exchanger and additional expansion system fluid stream, so that the vapour stream of compression refrigerant is supplied to the hot junction of cryogenic heat exchanger and the liquid stream of compression refrigerant is supplied to the additional expansion system.
#19. is according to each described equipment among the #12 to #16, wherein, this equipment also comprises piping arrangement, it is used for extra liquefied natural gas stream is passed to Sweet natural gas feed cooling system from main cryogenic heat exchanger, and this feed cooling system flows with the Sweet natural gas feed that described extra liquefied natural gas stream further cools off through cooling.
#20. is according to the described equipment of #19, and wherein, Sweet natural gas feed cooling system is washing tower, wherein, and by further cool off the Sweet natural gas feed stream through cooling with the convection current direct heat exchange of described extra liquefied natural gas stream.
Only in the mode of example, some embodiments of the invention are now described with reference to the accompanying drawings.
With reference to Fig. 1, described according to an embodiment of the invention be used to making example devices and the method that natural gas flow is dry and liquefy.Saturated gas feed stream 10 is cooling in joint heat exchanger 11 at first.The saturated gas feed stream 12 of the cooling that obtains is supplied to Sweet natural gas feed water scavenging system 13 with cooling, dry this stream, produces thus dry natural gas stream 14.On stream 12, can be provided with phase separator (for clear and not shown), to remove any water of condensation from described diffluence before being introduced in the water scavenging system 13 at described stream.Dry natural gas flow 14 further cools off the natural gas flow 16 to produce drying, cooling in Sweet natural gas feed cooling system (feed water cooler) 15.The natural gas flow 16 of dry, cooling then by with the convection current indirect heat exchange of saturated gas feed stream 10 in joint heat exchanger 11 temperature recovery, get warm again after a cold spell to produce, dry natural gas flow 17.Therefore, in joint heat exchanger 11, cool off the also natural gas flow 16 of heat drying, cooling of saturated gas stream 10 by the indirect heat exchange between two plumes.Then improvements, dry natural gas flow 17 are sent to main cryogenic heat exchanger (MCHE) 1 to be used for further cooling and to liquefy.
Joint heat exchanger 11 can be the interchanger that is suitable for realizing any type of the convection current indirect heat exchange between saturated gas feed stream 10 and dry, the natural gas flow 16 that cools off, for example shell-tube type, plate-fin or printed circuit type interchanger.
Water scavenging system 13 can be the system that is suitable for making any type of saturated gas fluidized drying/dehydration.Various types of water scavenging systems are well known in the art, and comprise such as the absorption system of glycol dehydration machine or such as the adsorption system of molecular sieve and activated alumina.
The feed water cooler 15 usefulness stream colder than environment comes further cooled natural gas stream.Feed water cooler 15 for example can be indirect heat exchanger, it uses from also being used to MCHE 1 to provide the cryogen flow of the identical cooling agent closed circuit that cools off responsibility as the described stream colder than environment, the example of this layout is drawn in Fig. 2, and the below will describe Fig. 2 in more detail.Alternatively (although suboptimum selection of land), the described stream colder than environment can for example form the part of independent refrigerant cycle, for example in feed water cooler 15 situation for the complete refrigerator of the independent refrigerant cycle of using himself.In either case, feed water cooler 15 can be any flow arrangement, such as convection current or kettle, and types such as shell-tube type, plate-fin or diffusion-combined type, to be used for being implemented in Sweet natural gas and than the indirect heat exchange between the cold stream of environment.
In Fig. 1, water scavenging system 13 is positioned at the upstream of feed water cooler 15, so that dry by water scavenging system before the further cooling in the feed water cooler from the saturated gas feed stream of the cooling that saves heat exchanger 11.If feed water cooler 15 is in the downstream (as shown in fig. 1) of water scavenging system 13, then the feed water cooler 15 employed streams colder than environment cool off dry natural gas flows, and then the drying that obtains and the natural gas flow of cooling 16 cooled off before saturated gas feed stream 10 is being dewatered in joint heat exchanger 11 as required.The feed cooler 15 which uses the cold flow than the ambient mixed refrigerant or a pure gaseous refrigerant (such as nitrogen) is particularly advantageous in the case; for example, wherein the specific environment of the cold stream is also used from the providing cooling in the MCHE 1 closed loop functions in the same refrigerant flow of the refrigerant, because the section in this manner, the cooling heat exchanger 11, the aqueous feed gas stream 10, the mixing result than if used or pure gaseous refrigerant refrigerant (such as nitrogen), to direct cooling gas to said aqueous feed stream 10, the better the cooling gas during the aqueous feed stream 10 to a temperature control.Therefore, cool off in this way saturated gas feed stream 10 and can be reduced in the front cooling period that dewaters forms hydrate in saturated gas feed stream risk.
In the alternative arrangement (not shown), feed water cooler 15 can change the upstream that is placed on water scavenging system 13 into.Yet, use at feed water cooler 15 in the situation of mixed cooling mediums or pure gaseous refrigerant, also have the more risk that forms hydrate during the cooling (in described feed water cooler 15) before in saturated gas feed stream, dewatering.If changing into using, feed water cooler 15 in steam compression cycle, comprises for example complete refrigerator of the independent refrigerant loop of pure liquid cryogen (or azeotrope), then can not there be the risk of any raising of hydrate formation, but will increases capital investment cost and the floor space of equipment to the demand of extra refrigerant loop (being the refrigerant loop of complete refrigerator).
Therefore, generally preferably water scavenging system 13 is positioned at the upstream of feed water cooler 15.
Leave the improvements of joint heat exchanger 11, dry natural gas flow 17 is introduced in the hot junction of main cryogenic heat exchanger (MCHE) 1 as mentioned above, and be cooled and liquefy to produce the liquefied natural gas product stream 18 that extracts from the cold junction of interchanger 1.MCHE 1 forms the part of refrigerating system 2, and closed circuit refrigerant system (using for example mixed cooling medium or pure gaseous refrigerant) for example is to be used for making improvements, dry natural gas flow 17 coolings and to liquefy.In described system, also cooling and produce the cold cryogen flow of one or more strands of compressions in MCHE 1 of the cooling agent feed of one or more strands of compressions stream 3, then it be extracted and expand with further cooling cooling agent from MCHE 1, and then the cold cooling agent of expansion turn back to the cooling responsibility that MCHE 1 cools off with the cold cryogen flow 3 that is provided for making improvements, dry natural gas flow 17 coolings and liquefaction and will compress.Then the expansion that produces owing to the convective heat exchange with the cryogen flow 3 of described improvements, dry natural gas flow 17 and compression, the cooling agent that warms are extracted, compress and turn back to MCHE 1 as the cooling agent feed stream 3 of one or more strands of compressions from MCHE 1.
In the example depicted in fig. 1, the cooling agent feed stream 3 of two bursts of compressions is introduced in the hot junction of MCHE 1, one plume is cooled and is extracted from the cold junction of MCHE 1 as the cold cryogen flow of compression, and another plume is cooled and be extracted as the cold cryogen flow of the compression mid-way from MCHE 1.Then the cold cryogen flow of the compression of extracting from cold junction is striden throttling valve 38 and is expanded, and this thermal insulation (constant enthalpy) further cooling cooling agent that expands provides the cold cooling agent of the expansion of the cold junction that turns back to MCHE 1, thus so that the cooling responsibility to be provided.Similarly, the cold cryogen flow of the compression of extracting from middle position is striden throttling valve 39 and is expanded, and this thermal insulation (constant enthalpy) is expanded and further cooled off cooling agent, provides thus the cold cooling agent of the expansion in the mid-way that turns back to MCHE 1, so that the cooling responsibility to be provided.The cold cooling agent that expands with get warm again after a cold spell, the cooling agent feed of dry natural gas flow 17 and compression flows the 3 opposite directions MCHE that flows through, thereby cools off described stream by the convection current indirect heat exchange.Describe in more detail the other side of exemplary refrigerating system 2 hereinafter with reference to Fig. 2, MCHE 1 forms the part of this system.
Although throttling valve 38 and 39 is used for making the cryogen flow of cooling, compression to expand in Fig. 1, in the present invention, can use be used to making described stream expansion (namely reducing its pressure) in order to reduce device or the system of any type of the temperature of described stream.Therefore, can use be used to any device or the system that make described stream adiabatic expansion, be included in the centrifugal or reciprocating type expander (that is isentropic expansion rather than the isenthalpic expansion of cooling agent, wherein occur) that when producing external work cryogen flow is expanded.For example, be in the situation of liquid stream in the cryogen flow of cooling off, compress, the hydraulic turbine unit (dense fluid expander) that can use cooling agent constant entropy ground to expand.
As describing among Fig. 1, MCHE 1 is the coiled heat exchanger (or other shell and tube heat exchanger) that comprises two tube banks (mid-way of one from the cold cryogen flow of two bursts of compressions of its extraction is between these two tube banks), improvements, dry natural gas flow 17 for example cool off in the first tube bank and alternatively partially or completely liquefaction, and fully liquefaction in second restrains (if not yet fully liquefaction) and/or excessively cold.Yet, can use equally the interchanger of other type and layout.For example, be that it can comprise more or less tube bank in the situation of wound form (or shell-tube type of other type) interchanger at MCHE, and tube bank can be arranged in identical or different shell (in a rear situation, by suitable pipeline interconnection).MCHE also can be the cryogenic heat exchanger for any other type that realizes the convection current indirect heat exchange.For example, MCHE can be plate-fin.But, generally preferably use wound form MCHE.
Improvements, dry natural gas flow 17 and one or more strands of compression refrigerant feed stream 3 preferably enter MCHE 1 under same or analogous temperature, in order to reduce any temperature mismatch between the stream in the hot junction that enters MCHE.The natural gas flow 17 of preferably, improvements, drying and one or more strands of stream 3 are in each other 10 ℃.Typically, the temperature that saturated gas feed stream 10 also is in and stream 17 is similar with 3, and therefore typically equally in 10 ℃ of the temperature of stream 17 and 3.
The use of the joint heat exchanger 11 of arranging as mentioned above and operating provides many benefits.The cooling of saturated gas stream 10 in joint heat exchanger 11 causes than otherwise directly is supplied to the natural gas flow that is supplied to water scavenging system 13 colder in the situation of water scavenging system 13 (stream 12) at saturated gas stream 10 that this allows more preferably dewatering from described natural gas flow then.More specifically, before saturated gas stream is introduced in the water scavenging system 13, its cooling can be reduced the load (going out and removed situation before this stream is introduced in water scavenging system as cause some water condensations in the stream in cooling) in the described system and/or improve as described in the efficient (as being that wherein sorbent material can adsorb the situation of the adsorption system of more water at a lower temperature at water scavenging system for example) of system's removal water.Before introducing in the water scavenging system 13, saturated gas stream also allow control to supply to the temperature of the Sweet natural gas in the water scavenging system 13 its cooling, therefore and avoid as otherwise the operation easier that can be caused by the temperature of the Sweet natural gas more than the design operation temperature that rests on water scavenging system 13 (this can cause in system 13 water from insufficient removal of Sweet natural gas, and therefore unacceptable water level in the Sweet natural gas of described system downstream).
In addition (and as proving in the following example), the contriver finds, by the natural gas flow 16 cooling saturated gas stream 10 in joint heat exchanger 11 to resist drying, cooling, can improve the overall efficiency of dry and liquefaction process.The use of joint heat exchanger 11 has significantly reduced the required cooling responsibility of Sweet natural gas feed cooling system 15, because in the case by after dewatering from the Sweet natural gas of dry, cooling (namely, from flowing 16) reclaim cold and the most of cooling of supply responsibility, it is used for cooling saturated gas stream 10 before the dewatering of water scavenging system 13.Although this also means natural gas flow (natural gas flow 17 that the namely gets warm again after a cold spell) ratio that supplies among the MCHE 1 otherwise changes in the situation about directly supplying among the MCHE 1 hotter at natural gas flow 16 dry, cooling, but the contriver finds, (being to provide in the situation of cryogen flow of identical cooling agent closed circuit of cooling responsibility at MCHE 1 from being used at feed cooling system 15 employed cooling agent particularly) still is provided the overall power consumption of this technique.Be to use in the situation of complete refrigerator of independent refrigerant loop of himself at feed cooling system 15, the reducing of the cooling responsibility that feed cooling system 15 is required also can allow to use less complete refrigerator, allows thus cost of capital to save.
In addition, the natural gas flow 16 of heat drying, cooling allows to reduce to enter any temperature mismatch between the stream in hot junction of MCHE 1 with the Sweet natural gas (namely flowing 17) that the drying that is under the temperature similar to the temperature of the compression refrigerant (namely flowing 3) in the hot junction that also enters MCHE 1, improvements are provided in joint heat exchanger 11.This has then reduced otherwise will the mechanical stress of (particularly in coiled heat exchanger) occur owing to the differential thermal expansion of the member at place, the hot junction of MCHE 1, and has therefore reduced to damage as its result the possibility of MCHE 1.In the MCHE such as some type of brazed aluminum ring type MCHE, be used for avoiding the possible alternative arrangement (not according to the present invention) of any this temperature mismatch under the temperature colder than the temperature of compression cryogen flow and at different positions, dry natural gas stream to be introduced MCHE, more cold junctions towards interchanger do not make natural gas flow get warm again after a cold spell after making the natural gas flow drying with the joint heat exchanger by so-called side heater.Yet the use of side header makes the manufacturing of this MCHE more complicated, and therefore this does not expect yet.
Referring now to Fig. 2, exemplary closed circuit refrigerant system and technique (being shown in Figure 1 for system 2) in the system that Fig. 1 describes have been described to can be used for.Closed loop system in this case and technique comprise and use mixed cooling medium, and also comprise throttling valve 38 and 39, feed water cooler 15 (all as mentioned before), cooling agent compression and cooling system (comprising coolant compressor 21, cooling agent water cooler 22 and phase separator 23) and other throttling valve 28 and 29 except MCHE 1.
In the case, the liquid that to introduce two strands of compression refrigerant feeds streams 3 in the hot junction of MCHE 1 be mixed cooling medium flows 27 and the vapour stream 24 of mixed cooling medium.Vapour stream 24 is cooled and partially or completely liquefaction and be extracted from the cold junction of MCHE 1 as cold (liquid phase or mixed phase) cryogen flow of compression, and liquid stream is cooled and be extracted from the mid-way of MCHE 1 as cold (liquid) cryogen flow of compression.Then these streams are striden respectively throttling valve 38 and 39 and are expanded adiabaticly, with the cold cryogen flow of expansion that the cold junction that turns back to respectively MCHE 1 and mid-way are provided (its can at least in part vaporization owing to described expansion).
The cold mixing cryogen flow that expands through MCHE (namely, the shell-side of in the situation of the shell and tube heat exchanger of wound form or other type, flowing through), and by warm (and, if still then vaporize for liquid phase or mixed phase) with Sweet natural gas and the indirect heat exchange of the compressed mixed cooling agent in the stream 3 of stream in 17.The cooling agent that expand, warms (that is, experienced and flowed the Sweet natural gas in 17 and flow the mixed cooling medium that obtains after the heat exchange of the compressed mixed cooling agent in 3 at cooling agent) is collected and is extracted as flowing 20 hot junctions from interchanger.
Stream 20 is compressed in coolant compressor 21, cooling in cooling agent water cooler 22, and in phase separator 23, be separated into liquid stream 25 (MRL) and vapour stream 24 (MRV).Although in the illustrated embodiment cooling agent water cooler 22 is depicted as the aftercooler that separates with coolant compressor 21, but coolant compressor 21 can be multi-stage compressor, and in the case, cooling agent water cooler 22 can comprise one or the replenishing or substituting as aftercooler of a series of side cooler.Cooling agent water cooler 22 for example also can comprise for the pre-cooler that will flow 20 coolings before coolant compressor 21 compressions.Then vapour stream 24 from phase separator 23 is introduced into the cold junction of MCHE 1 as the vapour stream (it cools off also partially or completely liquefaction and is extracted from its cold junction in MCHE 1) of aforementioned compressed mixed cooling agent.Liquid stream 25 from phase separator 23 is divided into liquid stream 27 (major portions) and liquid stream 26.Liquid stream 27 is introduced into the cold junction of MCHE 1 as the liquid stream (it cools off in MCHE 1 and is extracted from the intermediate position) of aforementioned compressed mixed cooling agent.
The liquid stream 26 of mixed cooling medium is striden throttling valve 28 and is expanded with this stream of further cooling (and in the case at least in part vaporization), and further the stream of cooling is used to provide refrigeration (via indirect heat exchange) in feed water cooler 15, the natural gas flow 16 to be used for further cooling drying natural gas flow 14 to produce drying, cooling.(and now fully vaporization) the mixed cooling medium stream that warms that obtains that leaves feed water cooler 15 can return pressure by valve 29 alternatively, and then at the sucting and the expansion of extracting from the hot junction of MCHE 1, cryogen flow 20 recombine that warm of coolant compressor 21.
Referring now to Fig. 3, described to make alternate exemplary equipment and the method for the dry and liquefaction of natural gas flow, it is described from Fig. 1 aspect two makes amendment (the arbitrary modification to the method for Fig. 1 can be made independently and as shown in Figure 3 in combination).
The first modification is that in equipment and method that Fig. 3 describes, the dry natural gas stream that leaves Sweet natural gas feed water scavenging system 13 at first turned back to joint heat exchanger 11 to be used for therein further cooling before being sent to Sweet natural gas feed cooling system.Therefore, as shown in Figure 3, at first cooling is to produce the saturated gas feed stream 12 of cooling in joint heat exchanger 11 for saturated gas feed stream 10, and it extracts from the mid-way of joint heat exchanger 11 in the case.The saturated gas feed stream 12 of cooling is supplied to water scavenging system 13 with cooling, dry described stream, produce thus dry natural gas stream 14, then it turning back to the mid-way of joint heat exchanger 11 and therein further cooling as stream 30 before the cold junction that saves heat exchanger 11 is extracted and delivers to Sweet natural gas feed cooling system.
The second modification is that in equipment and method that Fig. 3 describes, Sweet natural gas feed cooling system uses the liquefied natural gas stream 34 conducts stream colder than environment that obtains from MCHE 1, to be used for the natural gas flow 14/30 of cooling drying.Sweet natural gas feed cooling system can be the indirect heat exchange system equally, but in this arrangement, preferably, described Sweet natural gas feed cooling system comprises washing tower 31 (or wherein by other system of cooled natural gas stream further with the direct convective heat exchange of natural gas liquids, also allowing thus to occur mass transfer between convection current).This allows the method to be applicable to and need to remove the situation that weighs composition from the Sweet natural gas feed before liquefaction, because washing tower 31 also can be removed these compositions except cooled natural gas.
More specifically, the dry natural gas stream 30 of cooling enters washing tower 31 (it is simple carburettor in this example) and contact with the direct convection current of the backflow of natural gas liquids in joint heat exchanger 11, and the two further cooling flow 30 is also peeled off and weighed composition from flowing 30.Heavy bottoms is removed as stream 32.Formation is dry, then the lighter overhead product of the natural gas flow 33 of cooling gets warm again after a cold spell (as front) in joint heat exchanger 11 and enter the hot junction of MCHE 1 as improvements, dry natural gas flow 17.Improvements, dry natural gas flow 17 partly liquefy (for example intrafascicular at the first winding tube of MCHE), to produce the mixed phase natural gas flow 34 that extracts from the mid-way of MCHE.Then this mixed phase flow 34 is separated into the liquid stream 36 of Sweet natural gas and the vapour stream 37 of Sweet natural gas in return tank 35 or other phase separator.Then liquid stream 36 turn back to washing tower 31, so that aforesaid backflow to be provided.Vapour stream 37 turn back to the mid-way of MCHE and be cooled and liquefy (for example, intrafascicular at the second winding tube of MCHE) to produce natural gas liquids (LNG) product flow 18.
In may the revising of the system/device of in Fig. 3, describing and method, MCHE 1 for example can be and has three tube banks the coiled heat exchanger of (replace describe two), one is used for cooling off in advance feed to produce the backflow for washing tower, one is used for making its liquefaction, and one is used for making it excessively cold.
It is evident that to those skilled in the art the method and apparatus shown in Fig. 1 to Fig. 3 also only represents the possible layout of some of them.Different MR according to the present invention arrange and can comprise a plurality of phase separators, a plurality of compression stage, liquor pump etc.Any MR liquid stream can be utilized and completely or partially vaporized and turn back to the intrasystem different positions of closed circuit MR by feed water cooler 15.Reclaim in the circulation at closed circuit nitrogen, the part of gaseous refrigerant can be used for identical purpose equally.
Example
With reference to Fig. 1, make 10 liquefaction of saturated gas feed stream, it comprises 0.8% nitrogen, 88.2% methane, 6.9% ethane, 2.5% propane and surplus heavy hydrocarbon, uses water saturation, and is under the temperature of the pressure of 1024 psia (7060 kPa) and 118.6 ℉ (48.1 ℃).Natural gas flow 12 leaves joint heat exchanger 11 under 71.6 ℉ (22 ℃).Natural gas flow 14 is in the lower drying of 78.8 ℉ (26 ℃) and leave water scavenging system 13 (slightly hot owing to absorb heat).Then it be cooled to 66.1 ℉ (18.9 ℃) in feed water cooler 15.The cooling effect fluid that is used for feed water cooler 15 is the part from the MR of main MR loop extraction.MR enters feed water cooler 15 as two phase flow under-76.2 ℉ (60.1 ℃), comprise 52.5% steam.It leaves at the lower stream as fully vaporization of 57.0 ℉ (13.9 ℃).It comprises 1.7% nitrogen, 24.5% methane, 43.7% ethane, 13.7% propane and 17.1% iso-pentane.Dry, as to cool off natural gas flow 16 temperature recovery to 115.0 ℉ (46.1 ℃) in joint heat exchanger 11.Natural gas flow 17 dry, that get warm again after a cold spell enters MCHE 1 and leaves as liquified flow 18 under-247.9 ℉ (155.5 ℃).
The MR that comprises nitrogen, methane, ethane, propane and iso-pentane flows (in the case, steam MR stream and liquid MR stream) 3 and enter the hot junction of MCHE under 116.6 ℉ (47 ℃), and this temperature approaches the temperature of the natural gas flow 17 of improvements, drying.
Table 1
Case ? 1 2
Power % 100.00% 97.60%
The water cooler responsibility % 100.00% 26.60%
Table 1 has compared the present invention and conventional prior art is arranged.Case 1 is the conventional SMR circulation of annual about 2,000,000 tons of LNG of production, wherein do not have the feed interchanger, and feed water cooler interchanger (certainty) is in the upstream of water scavenging system.Case 2 is configurations (according to Fig. 1 of the application) of describing in above example.As can be seen, in the present invention, it is about 73% that feed water cooler responsibility (being the required cooling responsibility of feed water cooler 15) reduces, and liquefaction power demand (that is, both required total powers of operation of MCHE 1 and feed water cooler 15) reduces by 2.4%.
If in the method according to the invention feed water cooler 15 is placed on upstream rather than the downstream of water scavenging system 13, then the quantitative result shown in the table 1 is almost completely identical.In the case, natural gas flow 12 was cooled to 71.6 ℉ (22 ℃) in feed water cooler 15 before leaving joint heat exchanger 11 under 83.9 ℉ (28.8 ℃) and being supplied to water scavenging system 13, and natural gas flow 16 dry, cooling reenters joint heat exchanger 11 under 78.8 ℉ (26 ℃).Identical feed water cooler responsibility and the saving of liquefaction power (comparing with the prior art layout of routine) have been realized.Yet, configuration shown in Fig. 1 is suitable for avoiding the hydrate in the feed to form better, and (and therefore also providing the cooling responsibility to MCHE from the mixed cooling medium of refrigerant cycle) was not used in cooled natural gas stream before drying step carries out in the configuration of Fig. 1 because feed water cooler 15.
To understand, and the invention is not restricted to above the details described with reference to preferred embodiment, and under not breaking away from such as the situation in the spirit or scope of the present invention defined in the appended claims, can make many modifications and variations.

Claims (20)

1. one kind is used for making the method that natural gas flow is dry and liquefy, and described method comprises:
(a) cooling comprises the Sweet natural gas feed stream of water, to produce the natural gas flow of cooling;
(b) dewater and further cool off the Sweet natural gas feed stream of described cooling from the Sweet natural gas feed diffluence of described cooling, to produce the natural gas flow of drying, cooling;
(c) heat the natural gas flow of described drying, cooling, to produce the natural gas flow of drying, improvements;
(d) natural gas flow of described drying, improvements is cooled off and liquefaction, and cool off the cooling agent feed stream of at least one compression by the convection current indirect heat exchange with the cold cooling agent that expands, with the cold cryogen flow that produces liquefied natural gas product stream, at least one compression and the cryogen flow that expands, warms; And
(e) the cold cryogen flow of one or more strands of described compressions is expanded and thus further cooling, so that the cold cooling agent of described expansion to be provided;
Wherein, the heating of the natural gas flow of drying, cooling is undertaken by the indirect heat exchange between described two plumes described in the cooling of the stream of Sweet natural gas feed described in the step (a) and the step (c).
2. method according to claim 1, it is characterized in that, in step (c), the natural gas flow of described drying, cooling be heated to temperature with the cooling agent feed of described at least one compression stream identical or 20 ℃ of this temperature with interior temperature, so that when step (d) begins, between the cooling agent feed stream of the natural gas flow of described drying, improvements and described at least one compression, there is not the temperature difference or has the temperature difference less than 20 ℃.
3. method according to claim 2, it is characterized in that the temperature of described Sweet natural gas feed stream when step (a) begin is also with in the cooling agent feed of the natural gas flow of described drying, improvements and described at least one compression flows identical or in this temperature 20 ℃ of temperature when step (d) begins.
4. method according to claim 1 is characterized in that, performing step in the wound form cryogenic heat exchanger (d).
5. method according to claim 1 is characterized in that, in step (b), the Sweet natural gas feed of described cooling stream at first is dried to remove water from it, and then is further cooled to produce the natural gas flow of described drying, cooling.
6. method according to claim 1, it is characterized in that, step (d) and (e) in cooling agent or mixed cooling medium, the cold cryogen flow of the one or more strands of described compressions in the step (d) is that the described expansion in liquid stream or mixed phase flow and the step (d), the cryogen flow that warms are mixed phase or vapour stream, or runs through step (d) and (e) keep being the gaseous refrigerant of basic gaseous form.
7. method according to claim 1 is characterized in that, described method also comprises:
(f) cryogen flow that compress described expansion, warms is to be provided at the cooling agent feed stream of described at least one compression of cooling in the step (d).
8. method according to claim 7, it is characterized in that, step (f) comprises compression and the cryogen flow of cooling off described expansion, warming, to be provided at cooling agent feed stream and the additional compression cryogen flow of described at least one compression of cooling in the step (d), described method also comprises to be made described additional compression cryogen flow expansion with the described stream of further cooling and uses the extra cryogen flow of described further cooling in step (b) to come by indirect heat exchange further to cool off the Sweet natural gas feed stream of described cooling.
9. method according to claim 8, it is characterized in that, step (f) comprises described expansion, the cryogen flow compression of warming, the cooling and be separated, liquid stream with vapour stream that compression refrigerant is provided and compression refrigerant, the cooling agent feed that described vapour stream is formed on middle at least one compression of cooling off and liquefying at least in part of step (d) flows, and at least a portion formation expansion of described liquid stream and the described extra cryogen flow that then flows for the Sweet natural gas feed that further cools off described cooling by indirect heat exchange in step (b).
10. method according to claim 1, it is characterized in that, in step (d), the natural gas flow of described drying, improvements is cooled and liquefies, to produce described liquefied natural gas product stream and extra liquefied natural gas stream, described extra liquefied natural gas stream is used for the Sweet natural gas feed stream of the further described cooling of cooling in step (b).
11. method according to claim 10 is characterized in that, in step (b), by further cooling off the Sweet natural gas feed stream of described cooling with the convection current direct heat exchange of described extra liquefied natural gas stream.
12. one kind is used for making the equipment that natural gas flow is dry and liquefy, described equipment comprises:
The joint heat exchanger, it is used for receiving saturated gas feed stream and natural gas flow dry, cooling, and the indirect heat exchange that is used for by each other cools off described saturated gas feed stream and heats the natural gas flow of described drying, cooling, in order to produce saturated gas feed stream and the natural gas flows dry, that get warm again after a cold spell of cooling;
With described joint heat exchanger and each other Sweet natural gas feed water scavenging system and the Sweet natural gas feed cooling system of fluid flow communication, it is used for receiving the saturated gas feed stream of described cooling, the dry and further described stream of cooling and make the drying that obtains, the natural gas flow of cooling turn back to described joint heat exchanger from described joint heat exchanger;
Main cryogenic heat exchanger, it is used for making natural gas flow cooling and the liquefaction of described drying, improvements, and be used for cooling off by the convection current indirect heat exchange with the cold cooling agent that expands the cooling agent feed stream of at least one compression, in order to produce the cold cryogen flow of liquefied natural gas product stream, at least one compression and the cryogen flow that expands, warms;
Piping arrangement, it is used for the natural gas flow of described drying, improvements is passed to the hot junction of described main cryogenic heat exchanger from described joint heat exchanger, and is used for extracting described liquefied natural gas product stream from the cold junction of described main cryogenic heat exchanger; And
With the cooling agent expansion system of described main cryogenic heat exchanger fluid flow communication, its be used for from the cold junction of described cryogenic heat exchanger receive at least one compression cold cryogen flow, described cold cooling agent is expanded and thus further cooling and make the cold cooling agent of expansion turn back to the cold junction of described cryogenic heat exchanger.
13. equipment according to claim 12 is characterized in that, described main cryogenic heat exchanger is coiled heat exchanger.
14. equipment according to claim 12, it is characterized in that, described Sweet natural gas feed water scavenging system is in the upstream of described Sweet natural gas feed cooling system, so that at first in described water scavenging system, be dried from the saturated gas of the cooling of described joint heat exchanger, and then the Sweet natural gas from the drying of described water scavenging system is further cooled in described cooling system, turns back to subsequently the drying of described joint heat exchanger, the Sweet natural gas of cooling to produce.
15. equipment according to claim 12 is characterized in that, described equipment also comprises:
With the cooling agent compression system of described main cryogenic heat exchanger fluid flow communication, it is used for receiving described expansion, the cryogen flow that warms from the hot junction of described cryogenic heat exchanger, compress described cooling agent and make the cooling agent feed stream of at least one compression turn back to the hot junction of described cryogenic heat exchanger.
16. equipment according to claim 15, it is characterized in that, described main cryogenic heat exchanger, cooling agent expansion system and cooling agent compression system form the closed circuit refrigerant system or form its part, be contained in the cryogen flow that described closed loop system cooling agent interior and circulation within it comprises described compression and expansion, described cooling agent is mixed cooling medium or pure nitrogen gas or argon gas.
17. equipment according to claim 15, it is characterized in that, described cooling agent compression system compresses and cools off described expansion, the cooling agent that warms, and described Sweet natural gas feed cooling system is indirect heat exchanger, and wherein, described equipment also comprises the additional expansion system with described cooling agent compression system and described Sweet natural gas feed cooling system fluid flow communication, it is used for receiving the stream of the cooling agent that compresses and cool off and described stream being expanded with the described stream of further cooling from described cooling agent compression system, and described Sweet natural gas feed cooling system comes by indirect heat exchange further to cool off the Sweet natural gas feed stream of described cooling with the stream of described further cooling.
18. equipment according to claim 17, it is characterized in that, described cooling agent compression system also comprises at least one phase separator, it is used for the cooling agent of described compression and cooling is separated into liquid and gas, described one or more phase separator and described main cryogenic heat exchanger and described additional expansion system fluid stream are communicated with, and are supplied to described additional expansion system so that the vapour stream of compression refrigerant is supplied to the liquid stream of the hot junction of described cryogenic heat exchanger and compression refrigerant.
19. equipment according to claim 12, it is characterized in that, described equipment also comprises piping arrangement, it is used for extra liquefied natural gas stream is passed to described Sweet natural gas feed cooling system from described main cryogenic heat exchanger, and described feed cooling system further cools off the Sweet natural gas feed stream of described cooling with described extra liquefied natural gas stream.
20. equipment according to claim 19 is characterized in that, described Sweet natural gas feed cooling system is washing tower, wherein, and by further cool off the Sweet natural gas feed stream of described cooling with the convection current direct heat exchange of described extra liquefied natural gas stream.
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