CN205619689U - System for be used for distillating fractionally and liquefied natural gas feeding stream - Google Patents

System for be used for distillating fractionally and liquefied natural gas feeding stream Download PDF

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Publication number
CN205619689U
CN205619689U CN201620062693.1U CN201620062693U CN205619689U CN 205619689 U CN205619689 U CN 205619689U CN 201620062693 U CN201620062693 U CN 201620062693U CN 205619689 U CN205619689 U CN 205619689U
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stream
overhead
liquefaction
heat exchanger
tower
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T.特隆
G.克里什纳墨菲
M.J.罗伯茨
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F25J3/0214—Liquefied natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F25J3/0615—Liquefied natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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    • 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
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    • 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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    • 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
    • F25J1/0216—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 using a C3 pre-cooling 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
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
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    • F25J1/0237—Heat exchange integration integrating refrigeration provided for liquefaction and purification/treatment of the gas to be liquefied, e.g. heavy hydrocarbon removal from natural gas
    • F25J1/0239—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling
    • F25J1/0241—Purification or treatment step being integrated between two refrigeration cycles of a refrigeration cascade, i.e. first cycle providing feed gas cooling and second cycle providing overhead gas cooling wherein the overhead cooling comprises providing reflux for a fractionation step
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
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    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
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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
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    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/02—Integration in an installation for exchanging heat, e.g. for waste heat recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/18—External refrigeration with incorporated cascade loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons

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  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
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Abstract

This paper has described system for be used for distillating fractionally and liquefied natural gas feeding stream. The natural gas at first distillates fractionally in the scrubbing tower. The top of the tower vapour that comes from the scrubbing tower separately flows and at least one other stream with first -class, the second that forms the first top of the tower thing of liquefied through cooling, condensation. First -class the flowing as the backward flow of the first top of the tower thing of liquefied is returned to the scrubbing tower. The second of the first top of the tower thing of liquefied flows and forms the LNG result. The backward flow that other inter -item transfers of the first top of the tower thing of liquefied provided or produced the domethanizing column, the domethanizing column is used for distillating fractionally the bottom liquid that comes from the scrubbing tower.

Description

System for fractionation and liquefied natural gas feed stream
Technical field
The present invention relates to the method and system for fractionation and liquefied natural gas feed stream.
Heavy hydrocarbon (HHC) is removed from natural gas, such as C6+ hydrocarbon (have 6 or more carbon atoms), then usual, the liquefaction of natural gas is substantially in order to be reduced to certain level by concentration in natural gas for these compositions, and wherein these compositions will not occur condensation in main heat exchanger.C2-C5+ hydrocarbon (having the hydrocarbon of 2-5 or more carbon atoms) is also known as liquefied natural gas (NGL) in the art, generally also separates from natural gas, because they have high market value, and can therefore sell separately.Further, since NGL has more higher calorific value than methane, it may be necessary to reduce level in natural gas for the NGL composition to make LNG product meet the product specification of regulation.When the cold-producing medium for gas deliquescence process comprises one or more hydrocarbon refrigerant, for example, especially when the cascade using ethane and/or propane or mixing cause cool dose of circulation for liquefaction process, also can expect to use the NGL composition (such as ethane or propane) separating to supplement as refrigerant.Traditionally, destilling tower has been used for this purpose.
Background technology
Fig. 1 schematically depict the conventional configuration for fractionation and liquefied natural gas feed stream.Natural gas feed stream 101, pre-process to remove sour gas, water and mercury, and also optionally precool in one or more heat exchangers, it is introduced to scrubbing tower 10, be separated into overhead vapours and the bottom liquid rich in the hydrocarbon heavier than methane of methane rich wherein.Take out vapor stream of top of the tower 202 from the top of scrubbing tower, and take out bottom liquid stream 103 from the bottom of scrubbing tower.
Vapor stream of top of the tower 202 sends to the warm bundle 22 around tubular type main heat exchanger 20, wherein said stream partial condensation.Then take out the stream 203 of partial condensation from warm bundle and phase separator 28, be separated into its liquid and vapor phase to produce liquid stream 120 and steam stream 207.Steam stream 207 sends to the middle bundle 24 of main heat exchanger, the cooling further of wherein said stream and liquefaction, and described fluidized flow 204 then supercooling in the cold bundle 26 of main heat exchanger, produces LNG product stream 205.LNG product stream 205 can flash distillation being sent in LNG storage tank 30, steam gas (BOG) or flash gas 401 to be sent to fuel header (header) by described groove, through burning or recycle (not shown) to vapor stream of top of the tower 202, charging is to main heat exchanger.Liquid stream 120 is back to the top of scrubbing tower 10 as backflow stream from phase separator 28, in order to provide the backflow that scrubbing tower operation is required.If the amount of the backflow producing is more than needed for scrubbing tower, a part of liquid stream 120 can be with the middle bundle 24 flowing 207 hybrid concurrencies and delivering to main heat exchanger.
From the bottom liquid stream 103 of scrubbing tower 10 rich in NGL and HHC, expanded being subsequently sent to the domethanizing column of fractionation unit so that described stream part evaporation, described stream stands to be fractionated further/separate wherein.In the arrangement that Fig. 1 illustrates, fractionation unit comprises domethanizing column (herein also referred to as DeC1 tower), dethanizer (herein also referred to as DeC2 tower), depropanizing tower (herein also referred to as DeC3 tower), and debutanizing tower (herein also referred to as DeC4 tower).Generally, these towers comprise multistage with improve HHC and NGL separate with the lighter component of methane and natural gas.
Bottom liquid 103 from scrubbing tower is separated into overhead vapours and the bottom liquid rich in the hydrocarbon heavier than methane of methane rich by domethanizing column 12.Overhead vapours partly condenses to produce the liquid reflux stream being back to domethanizing column 12 in overhead condenser, and wherein remaining vapor portion takes out as vapor stream of top of the tower 104 from domethanizing column.A part for bottom liquid heats the upflowing vapor (boil-up) to provide domethanizing column 12 in reboiler, and the remainder of bottom liquid takes out as stream 105, expands partly to vaporize described stream, and is sent to dethanizer 14.
The dethanizer 14 and then bottom liquid 105 from domethanizing column is separated into the rich overhead vapours of ethane and the bottom liquid rich in the hydrocarbon heavier than ethane.Overhead vapours condenses in overhead condenser, and a part for the overhead materials of condensation is back to dethanizer 14 as backflow stream, and remainder takes out the liquefaction overhead stream 106 as rich ethane.A part for bottom liquid heats to provide the upflowing vapor of dethanizer 14 in reboiler, and the remainder of bottom liquid takes out as stream 107, expands and is sent to depropanizing tower 16.
Depropanizing tower 16, operates in the way of similar with dethanizer, then separates the bottom liquid 107 from dethanizer to provide the rich overhead stream 108 of liquefaction of propane and the bottom liquid stream 109 rich in the hydrocarbon than propane more weight.Similarly, debutanizing tower 18, operate in the way of similar with dethanizer, then separate the bottom liquid 109 from depropanizing tower to provide the rich overhead stream 108 of liquefaction of butane and the bottom liquid stream 111 rich in the hydrocarbon than butane more weight.
The 106th, overhead stream from the liquefaction of tower DeC2, DeC3 and DeC4 108 and 110 each mainly comprises ethane, propane and butane, and the stream being rich C5+ (pentane and heavier hydrocarbon) from the bottom liquid 111 of tower DeC4, these NGL streams can be sold as mentioned above or to be used as refrigerant in due course supplementary.In some cases, the cut of one or more of these streams also can reinject to LNG product stream with by the adjustment heat value of LNG product stream to optimal value.
As described above, tower DeC1, DeC2, DeC3 and DeC4 are each equipped with overhead condenser, it is by by the condensation of at least a portion of overhead vapours, thus provides the liquid reflux stream being back to top of tower, produces the backflow of tower.There are these overhead condensers and add the capital cost installed and safeguard system.But, remove overhead condenser and unwanted composition will be caused to carry to vapor stream of top of the tower.Condenser improves separative efficiency, and it is especially advantageous to have this condenser in DeC1 and DeC2 tower.The temperature of required cold reflux stream depends on the composition of natural gas flow.NGL content is lower, needs backflow stream colder, effectively to isolate required NGL and HHC composition to liquid condensate stream.Removing overhead condenser from DeC1 and DeC2 tower will cause ethane and propane to carry to the vapor stream of top of the tower from DeC1 and DeC2 respectively.This is present in causing ethane to lose with DeC1 overhead materials and similarly result in extra propane in DeC2 overhead materials, therefore adversely affects (similarly adversely affecting its purposes as supplementary refrigerant and/or the value as commodity) to the purity of the ethane in DeC2 overhead materials.
Generally, propane is used as refrigerant for providing the refrigeration duty of the overhead condenser used by DeC1 tower.Especially, such arrangement considers for using propane pre-cooling mixed cooling medium (C3MR) circulation but, and in fractionation that therefore propane refrigeration is easily applied wherein and liquefaction system.
US 2012/0090350A1 describes thermal value control system and the method for LNG product in middle natural gas liquefaction device.Natural gas feed stream, after initial pretreatment, is incorporated into scrubbing tower so that natural gas feed to be separated into the bottom liquid of the overhead vapours of lean C5+ and rich C3+.The refluxing portion ground of scrubbing tower is provided by using the overhead condenser of low-pressure propane refrigeration.Vapor stream of top of the tower from scrubbing tower sends and is used for liquefying to liquefaction device, and bottom liquid stream is fractionated to provide the liquid stream of the liquid stream of rich C3 and rich C4+ in NGL fractionation unit.
US 6,662,589 and US 2006/0260355A1 describes procedure below, and wherein natural gas feed stream is incorporated into scrubbing tower so that natural gas feed to be separated into overhead vapours and bottom liquid after initial pretreatment.Cool down in the warm district of main heat exchanger from the vapor stream of top of the tower that scrubbing tower takes out and partly condense, then in phase separator, it is separated into liquid phase, it is back to the top of scrubbing tower as liquid reflux stream, and remaining vapor phase cools down further in the cold-zone of main heat exchanger and condenses to provide LNG product.It is fractionated to provide the liquid stream of rich C3, C4 and C5+ NGL fractionation unit (comprising dethanizer, depropanizing tower and debutanizing tower) from the bottom liquid stream that scrubbing tower takes out, and the steam stream of rich C1 and C2.The steam stream of rich C1 and C2 condenses to provide other LNG product in main heat exchanger.
US 2008/0115532A1 described before natural gas liquefaction for removing the operation of the scrubbing tower of heavier hydrocarbon composition from natural gas flow.Backflow for scrubbing tower can be provided by the condensate of overhead condenser and/or LNG stream.
US 2008/0016910A1 and US 2013/0061632A1 describes procedure below, and the natural gas feed stream wherein pre-processing is incorporated in scrubbing tower so that natural gas feed to be separated into overhead vapours and bottom liquid.The vapor stream of top of the tower taking out from scrubbing tower cools down in the warm district of main heat exchanger and condenses.Then, condensate flow is divided into two streams, and a stream is back to the top of scrubbing tower as liquid reflux stream, and another is subcooled to provide LNG product stream in the cold-zone of main heat exchanger.The bottom liquid stream taking out from scrubbing tower is fractionated to provide C2, C3 and C4 product stream NGL fractionating system.
US 4,065,278th, CA1059425 and US 5,659,109 describe the process producing LNG, it is wherein similar to US 6, process described in 662,589 and US 2006/0260355A1, the natural gas feed stream of pretreatment is fractionated in scrubbing tower, with by partial condensation scrubbing tower overhead materials in main heat exchanger and as liquid reflux stream, the liquid phase of separation is back to scrubbing tower provides to the backflow of scrubbing tower, at least a portion of remaining vapor phase cools down further and condenses to provide LNG product.
US 4,445,917 describe the process producing LNG, it is wherein similar to the process described in 2008/0016910A1 and US 2013/0061632A1, the natural gas feed stream of pretreatment is fractionated in scrubbing tower, scrubbing tower overhead materials total condensation, then separately with offer LNG stream and the liquid reflux stream being back to scrubbing tower top.
US 5,956,971 teaches the process producing LNG, and wherein first natural gas feed is processed in the fractionating column with controlled condensing zone.
US 2007012071 describes process and the system producing LNG, and the natural gas feed wherein pre-processing is separated into the overhead materials of methane rich and the bottom liquid of rich C2+ in fractionating column.Overhead stream is condensed, cools down further, and then flash distillation is to produce LNG stream and flash gas.Flash gas is used as refrigerant in main heat exchanger.Then a part for the flash gas of temperature recompresses, cooling, condensation the top being incorporated into fractionating column as backflow stream.
US 5,588,308 describes the process removing NGL from natural gas flow, and wherein natural gas feed partly condenses and be separated into liquid and vapor phase, and vapor phase provides product of natural gas, and liquid phase is incorporated in stripper and is fractionated in stripper to provide NGL to flow.
US 2004/0200353A1 describes the process using scrubbing tower to remove NGL from natural gas feed, providing back up through overhead condenser of described scrubbing tower.
Expect there is improved method and system for fractionation and liquefied natural gas feed stream.
Content of the invention
According to the first aspect of the invention, providing fractionation and liquefied natural gas feed stream method, described method comprises:
A described natural gas feed stream is introduced to scrubbing tower by (), described natural gas feed stream is separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane wherein, described vapor fraction is collected as the first bottom liquid in described wash tower bottoms as the first overhead vapours, described liquid distillate at described scrubbing tower collected overhead；
B () takes out the first vapor stream of top of the tower from the top of described scrubbing tower, and cool down, condense and by described stream separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction；
C the described first-class of the first overhead materials liquefied is back to described scrubbing tower by (), be incorporated into the top of described scrubbing tower as backflow stream, thus provide the backflow of described scrubbing tower；
D () is formed liquefied natural gas (LNG) product stream by the described second of the first overhead materials liquefying；
E () is taken out the first bottom liquid stream by the bottom of described scrubbing tower, and described stream is introduced to domethanizing column, described first bottom liquid stream is separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane wherein, described vapor fraction is collected as the second overhead vapours at described demethanizer overhead, and described liquid distillate is collected as the second bottom liquid at described demethanizer bottom；With
F () is refluxed to the offer of described domethanizing column by following:
(1) one of other streams described in the first overhead materials of liquefaction are introduced to the top of described domethanizing column as backflow stream；And/or
(2) by with one of other streams indirect heat exchange described in the first overhead materials of liquefaction, condense a part for described second overhead vapours to form the second overhead stream of the liquefaction as the top that backflow stream is re-introduced into described domethanizing column.
According to the second aspect of the invention, providing the system for fractionation and liquefied natural gas feed stream, described system comprises:
Scrubbing tower, described scrubbing tower is arranged and operation is used for receiving described natural gas feed stream, and be methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by described flow separation, described vapor fraction is collected as the first bottom liquid in described wash tower bottoms as the first overhead vapours, described liquid distillate at described scrubbing tower collected overhead；
Pipeline group, one or more heat exchangers, optionally one or more separators, it is arranged and operation is flowed at least one the first vapor stream of top of the tower taking out and being cooled down, condense and separate first-class, the second of the first overhead materials that liquefies of the first overhead materials to form liquefaction and the first overhead materials of liquefaction from the top of described scrubbing tower；
Pipeline, it is arranged and operation is for being back to described scrubbing tower by the described first-class of the first overhead materials of liquefaction, is incorporated into the top of described scrubbing tower as backflow stream, thus provides the backflow for described scrubbing tower；
Pipeline, it is arranged and operation is for taking out liquefied natural gas (LNG) product stream being formed by the second of the first overhead materials liquefying from described system；
Domethanizing column, it is arranged and operation is for from bottom reception first bottom liquid stream of described scrubbing tower, and be methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by described flow separation, described methane rich vapor fraction is collected as the second overhead vapours at described demethanizer overhead, and the described liquid distillate rich in the hydrocarbon than methane more weight is collected as the second bottom liquid at described demethanizer bottom；
Pipeline, it is arranged and operation is used for taking out the first bottom liquid stream from the bottom of described scrubbing tower, and described stream is introduced to domethanizing column；With
One below or both:
(1) pipeline, it is arranged and operates the top that one of other streams described in the first overhead materials being used for liquefying are introduced to described domethanizing column as backflow stream, thus provides the backflow of described domethanizing column；
(2) heat exchanger, its arrange and operation for by with one of other streams indirect heat exchange described in the first overhead materials of liquefaction, part condensation by described second overhead vapours forms the second overhead stream of liquefaction, it is re-introduced into the top of described domethanizing column as backflow stream, thus provide the backflow of described domethanizing column, and arrange and operate the pipeline that other streams described in the first overhead materials being used for liquefying are introduced to described heat exchanger.
Brief description
The schematic flow diagram of natural gas fractionation and liquefaction system and method for describing contrast for the Fig. 1, not according to the present invention.
Fig. 2 is for describing the schematic flow diagram of the natural gas fractionation according to embodiment of the present invention and liquefaction system and method.
Fig. 3 is for describing the schematic flow diagram of natural gas fractionation according to another embodiment of the invention and liquefaction system and method.
Fig. 4 is for describing the schematic flow diagram of natural gas fractionation according to another embodiment of the invention and liquefaction system and method.
Fig. 5 is for describing the schematic flow diagram of natural gas fractionation according to another embodiment of the invention and liquefaction system and method.
Fig. 6 is for describing the schematic flow diagram of natural gas fractionation according to another embodiment of the invention and liquefaction system and method.
Fig. 7 is for describing the schematic flow diagram of natural gas fractionation according to another embodiment of the invention and liquefaction system and method.
Detailed description of the invention
The invention provides new option for providing backflow/condensation load to the domethanizing column being integrated with natural gas liquefaction.
More specifically, as mentioned above, according to the first aspect of the invention, provide fractionation and the method for liquefied natural gas feed stream, the wherein overhead vapours cooling from scrubbing tower top, condensation separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction.The first-class of first overhead materials of liquefaction is re-introduced into scrubbing tower to provide the backflow of scrubbing tower, and the second of the first overhead materials of liquefaction provides required LNG product, and other streams of the first overhead materials of liquefaction are for providing or producing the backflow of domethanizing column.
Especially, in preferred embodiments, other streams (other streams of the scrubbing tower overhead materials i.e. liquefying) of the first overhead materials of liquefaction are introduced to the top of domethanizing column as backflow stream, thus provide the backflow of described tower.
Describe with Fig. 1 and compared with above-mentioned conventional configuration, this advantageously allows to remove the overhead condenser for domethanizing column, thus substantially reduces the fund cost of described method and system.
Additionally, first overhead materials (the scrubbing tower tower top i.e. liquefying) of liquefaction is generally colder than condensed overhead materials, the overhead materials of described condensation can be produced by condensing demethanizer column overhead thing in the overhead condenser of propane-cooled.For example, can be by the minimum temperature backflow stream typically about-31 DEG C using the condensation of propane kettle to obtain from the overhead materials of domethanizing column, even and if-40 DEG C or following backflow stream are generally when the scrubbing tower overhead materials being only partially condensate in main heat exchanger or use obtain for the refrigerant of main heat exchanger.Thus, use the first overhead stream of liquefaction as backflow stream in domethanizing column, rather than the overhead condenser of use propane-cooled makes described demethanizer reflux, generally improve methane in domethanizing column to separate with ethane and more heavy constituent, itself and then the rate of recovery improving ethane in the bottom liquid of domethanizing column.
In another embodiment, the backflow of domethanizing column is as provided below: by the first overhead materials with liquefaction (i.e., liquefaction scrubbing tower overhead materials other stream) other stream indirect heat exchanges, make a part for the second overhead vapours (i.e., overhead vapours from domethanizing column) condensation, to form the second overhead stream being re-introduced into the liquefaction to demethanizer overhead as backflow stream.
In the present embodiment, it is still desirable to special overhead condenser is used for domethanizing column, the capital cost saving being obtained by previous embodiment can not therefore be obtained.But, the present embodiment remains and generally uses colder stream to produce the benefit of the backflow of demethaniser, because domethanizing column still uses the scrubbing tower overhead stream of liquefaction providing the cooling load for making demethanizer reflux in the present embodiment, rather than uses propane refrigerant to provide described cooling load.When propane is not precooling refrigerant and possibility is unavailable, the present embodiment is also beneficial.Thus, the present embodiment still separates with ethane and more heavy constituent and to provide benefit to improving methane in domethanizing column.
Article " one " and " a kind of ", as used herein and unless otherwise described, refer to one or more when applying any feature in embodiment of the present invention that specification and claims describe.The use of " one " and " a kind of " is not restricted to refer to single features, unless shown this restriction especially.Article " being somebody's turn to do " before odd number or plural noun or noun phrase represents specially appointed feature and can have the connotation of odd number or plural number, depends on the context using this word.
As used herein, term " natural gas feed stream " also includes the stream comprising synthesis and/or substituting natural gas.Natural gas be mainly composed of methane (it generally comprises at least about 85 moles % of feed stream, more generally at least about 90 moles %, and most commonly about 95 moles of %).Natural gas feed stream is possibly together with other heavier hydrocarbon less amount of, such as ethane, propane, butane, pentane etc..Other typical compositions of raw gas include one or more compositions, such as nitrogen, helium, hydrogen, carbon dioxide and/or other sour gas, and mercury.But, preprocessed according to the natural gas feed stream that the present invention is processed, if as required to reduce the level of any (relatively) high-solidification point composition, such as moisture, sour gas and mercury, reduce level necessary to the solidification to the scrubbing tower making to avoid natural gas feed stream to introduce or other operational issues.
As used herein, term " methane rich " refers to comprise methane as the stream of its main component, cut or part.Described stream, cut or part can have especially and be similar to or more higher methane concentration than natural gas feed stream.Therefore, generally, described stream, cut or part comprise at least about 85 moles %, the methane of more generally at least about 90 moles % and most commonly about 95 moles of % or greater than about 95 moles of %.
As used herein, term " hydrocarbon heavier than methane " refers to the hydrocarbon with (i.e. higher boiling point) lower than methane volatility.Similarly, term " hydrocarbon heavier than ethane " refers to the hydrocarbon with (i.e. higher boiling point) lower than ethane volatility, and term " hydrocarbon heavier than propane " refers to the hydrocarbon with (i.e. higher boiling point) lower than propane volatility, etc..
As used herein, term " rich in the hydrocarbon heavier than methane " refers to relative to natural gas feed stream, rich in the stream of the hydrocarbon heavier than methane, cut or part, the hydrocarbon heavier with the ratio methane therefore compared with natural gas feed stream with higher mole of %.Similarly, term " rich ethane " refers to relative to natural gas feed stream, rich in the stream of ethane, cut or part, etc..
As used herein, term " indirect heat exchange " refers to the heat exchange between two fluids, and wherein said two fluids are kept by some form of physical obstacle separating each other.
In one embodiment, comprise to be taken out the first vapor stream of top of the tower by the top of described scrubbing tower according to the step (b) of first aspect, cool down and partly condense described stream, the liquid of isolated and vapor phase, separately the liquid phase of described separation is to form at least one other stream of the first overhead materials of the first-class and liquefaction of the first overhead materials of liquefaction, cool down and condense at least a portion of the vapor phase of described separation further, to form the second of the first overhead materials of liquefaction.Preferably, then the second of the first overhead materials of liquefaction is subcooled, and then forms LNG product stream.
In another embodiment, the step (b) of the method according to first aspect comprises to be taken out the first vapor stream of top of the tower by the top of described scrubbing tower, stream described in cooling and partial condensation, the liquid of isolated and vapor phase, the at least a portion of the liquid phase separating is formed the first-class of the first overhead materials liquefying, cool down and condense at least a portion of the vapor phase of described separation further, and the stream of the cooling further that is made available separately and condensation is to form at least one other stream of the first overhead materials of the second of the first overhead materials of liquefaction and liquefaction.Preferably, then the second of the first overhead materials of liquefaction is subcooled, and then forms LNG product stream, or cooling and condensation flow through cold, then separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of liquefaction and liquefaction.
In another embodiment, according to first aspect, the step (b) of this method comprises the combination of first the first two embodiment.
In the above-described embodiment, preferably wound tube heat exchanger is for cooling down and condensing the vapor phase of described separation further.Therefore, in one embodiment, the first vapor stream of top of the tower from scrubbing tower top can cool down and partial condensation in the warm bundle around tubular type main heat exchanger, and at least a portion of the vapor phase separating is cooling down and condensation in the middle bundle and/or cold bundle of tubular type main heat exchanger further.In another embodiment, the first vapor stream of top of the tower from described scrubbing tower top can cool down in overhead condenser heat exchanger and partly condense, and at least a portion of the vapor phase of described separation is in cooling and condensation further in tubular type main heat exchanger.
In another embodiment, the step (b) of the described method according to first aspect comprises to take out the first vapor stream of top of the tower from the top of described scrubbing tower, cooling and condense described stream, and by the stream of described cooling and condensation separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction.
In the present embodiment, the stream of cooling and condensation is supercooled, then separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction.Alternatively, the stream of described cooling and condensation can separate first-class and another liquid stream of the first overhead materials to form liquefaction, then described liquid stream be subcooled, then separately to form at least one other stream of the first overhead materials of the second of the first overhead materials liquefying and liquefaction.Alternatively, then the second of the first overhead materials of liquefaction is supercooled forms LNG product stream.
In the present embodiment, preferably wound tube heat exchanger is for cooling down and condensing the first vapor stream of top of the tower from described scrubbing tower top.
According to the method for first aspect, other streams being preferably used as liquefaction the first overhead materials first-class of backflow stream and liquefaction the first overhead materials for step (f) in step (c) have the flow-rate ratio of at least about 9:1.
Therefore, the first flow velocity of liquefaction the first overhead materials being preferably used as backflow in step (c) is about 9 times of the flow velocity of other streams of liquefaction the first overhead materials for step (f) or is more than 9 times, identical benchmark contrasts (such as mass velocity specific mass flow velocity, or molar flow rate ratio mole flow velocity etc.).Described method uses other streams other streams as the first overhead materials of backflow and liquefaction of the first overhead materials of liquefaction in step (f) wherein, condensed by indirect heating in those embodiments a part of of the second overhead vapours, in step (c), be preferably used as 9 times of combination flow velocity of first flow velocity other streams for two for liquefaction first overhead materials of step (f) described in of liquefaction first overhead materials of backflow stream or more than 9 times.
It according in the method for first aspect, in step (c), is preferably used as liquefaction the first overhead materials first-class of backflow stream and other streams of liquefaction the first overhead materials for step (f) each have about-40 DEG C or following temperature.
In preferred embodiments, the methane of the first overhead vapours and each self-contained at least about 95 moles of % of the second overhead vapours.
In preferred embodiments, the second bottom liquid comprises the methane of less than about 5 moles of %.
In one embodiment, described method also comprises: taken out the second vapor stream of top of the tower by the top of domethanizing column；Cooling and condense all or part of of described stream to form other LNG product；And/or all or part of of described stream is used as fuel stream；And/or all or part of of described stream exports as gaseous natural gas product stream.
In one embodiment, described method also comprises to be taken out the second bottom liquid stream by the bottom of described domethanizing column, and is fractionated the second bottom liquid stream to provide one or more natural gas liquids (NGL) to flow.
In one embodiment, the step being fractionated the second bottom liquid stream comprises: described stream is introduced to dethanizer, wherein the second bottom liquid stream is separated into rich ethane fraction and the cut rich in the hydrocarbon heavier than ethane, described rich ethane fraction at the collected overhead of dethanizer as the 3rd overhead vapours, the described cut rich in the hydrocarbon than ethane more weight at the bottom collection of dethanizer as the 3rd bottom liquid.Described method can further include: takes out the 3rd vapor stream of top of the tower from the top of described dethanizer, and cools down and condense described stream to form NGL stream；And/or take out the 3rd bottom liquid stream from the bottom of dethanizer, and it is formed one or more NGL stream.Described method also can comprise the dethanizer that is back to as provided below: by a part for other stream indirect heat exchange condensation the 3rd overhead vapours of the first overhead materials with liquefaction, form the 3rd overhead stream of liquefaction, be re-introduced into the top of described dethanizer as backflow stream.Preferably, the 3rd overhead vapours comprises the ethane of at least about 95%.Preferably, the 3rd bottom liquid comprises the ethane of less than about 5 moles of %.If it is required, the 3rd bottom liquid can for example be fractionated in depropanizing tower and/or in debutanizing tower further, further described 3rd bottom liquid to be separated into rich propane fraction, rich butane cut and/or the cut rich in pentane and heavier hydrocarbon.
As known in the art, term " scrubbing tower ", " domethanizing column " and " dethanizer ", " depropanizing tower " and " debutanizing tower " refers to the type of destilling tower.Term " destilling tower " refers to the tower containing one or more separation levels, is made up of the device of such as filler or column plate, and it strengthens contact and therefore improves the mass transfer rising between steam and the liquid stream flowing downward upwards inside tower.In this way, in top of tower is collected as the rising steam of overhead vapours, the concentration of lighter component (i.e. higher volatility and relatively low boiling point) increases, and the concentration of heavier composition (i.e. relatively low volatility and higher boiling point) increases in tower bottom collection is as the dropping liq of bottom liquid." top " of destilling tower refers to the part of the tower at the separation level pushed up most or on it." bottom " of tower refers to the part of the tower at the separation level at the end or under it." centre position " of tower refers to the position between the top and bottom of tower, separates between level at two.
In the case of scrubbing tower, natural gas feed stream is introduced to (two phase flow as gaseous flow or as partial condensation) scrubbing tower, in the centre position of tower, or more generally, in the bottom of tower.From feed stream upwards rise steam when it separates level by internal one or more of scrubbing tower, then contact with the liquid reflux stream flowing downward, thus " washing " is from the heavier composition of the ratio methane of described steam (that is, removing at least some the described less volatile composition from described steam).As mentioned above, this causes natural gas feed stream to be separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane, described vapor fraction at the collected overhead of scrubbing tower as overhead vapours (herein referring to " the first overhead vapours "), described liquid distillate at the bottom collection of scrubbing tower as bottom liquid (herein referring to " the first bottom liquid ").
In the case of domethanizing column, the first bottom liquid stream from scrubbing tower is further separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane as previously discussed, described vapor fraction at the collected overhead of domethanizing column as overhead vapours (" the second overhead vapours "), described liquid distillate at the bottom collection of domethanizing column as bottom liquid (" the second bottom liquid ").First bottom liquid stream normally partially evaporates (via the expansion of heating and/or stream), is then incorporated into domethanizing column as two phase flow.Generally, described stream is incorporated into domethanizing column in the centre position of tower, the steam that rises upwards from described stream is contacted with the liquid reflux stream flowing downward when it is by one or more separation level, thus " washing " is from the heavier composition of the ratio methane of described steam, when it is by one or more separation level and rising steam upwards is (usual with the liquid flowing downward making from described stream, seethed with excitement by the part making the bottom liquid of the bottom collection at tower and provide) contact, thus " strip " methane and the composition (i.e. from described liquid remove at least some described more volatile composition) lighter than methane from described liquid.
In the case of dethanizer, the second bottom liquid stream from domethanizing column is further separated into rich ethane fraction and the cut rich in the hydrocarbon heavier than ethane as mentioned above, described rich ethane fraction at dethanizer collected overhead as overhead vapours (" the 3rd overhead vapours "), the described cut rich in the hydrocarbon heavier than ethane at the bottom collection of dethanizer as bottom liquid (" the 3rd bottom liquid ").The operation of dethanizer is generally similar to the operation of domethanizing column, except the generally part evaporation of the second bottom liquid stream, then the centre position at tower is incorporated into dethanizer, the withdrawing fluid that rising steam upwards from described stream is flowed downward washes out the composition heavier than ethane, and makes the liquid flowing downward from described stream be stripped off ethane and the composition heavier than ethane by the steam that rises upwards.
As used herein, term " separator " or " phase separator " refer to for example to rouse or the device of container of other forms, and wherein two phase flow can introduce so that described flow separation is its composition steam and liquid phase.
The system of a second aspect of the present invention is adapted for carrying out the method for first aspect, and therefore the above-mentioned benefit of method according to the first aspect of the invention is equally applicable to the system of a second aspect of the present invention.
An embodiment according to second aspect, pipeline group, one or more heat exchanger and one or more separator be arranged and operation is to take out, to cool down, to condense and separately the first vapor stream of top of the tower, and it comprises: arrange and operation to take out the pipeline of the first vapor stream of top of the tower from described scrubbing tower top；The heat exchanger arranged and operate to cool down and flow described in partial condensation or heat exchanger section；Arrange and operate the separator of the liquid with isolated and vapor phase；Arrange and operation with the liquid phase of separately described separation to form pipeline group of other streams of the first overhead materials of the first-class and liquefaction of the first overhead materials of liquefaction；With arrange and operation is to receive, cool down and condense at least a portion of described separation vapor phase to form the heat exchanger of second of the first overhead materials of liquefaction or heat exchanger section further.
Described system can further include arranged and operation to receive and to be subcooled the heat exchanger of the second of the first overhead materials of liquefaction or heat exchanger section.Arranged and operation can comprise the warm bundle around tubular type main heat exchanger with the heat exchanger section cooling down with partial condensation the first vapor stream of top of the tower, and arranged and operation can comprise the middle bundle around tubular type main heat exchanger and/or cold bundle with at least one of heat exchanger section cooling down and condensing described separation vapor phase further.Alternatively, arrange and operation can comprise overhead condenser heat exchanger with the heat exchanger cooling down with partial condensation the first vapor stream of top of the tower, and arrangement and operation can comprise around tubular type main heat exchanger with at least one of heat exchanger cooling down the vapor phase with condensation separation further.
Another embodiment according to second aspect, pipeline group and one or more heat exchanger are arranged and operation is to take out, to cool down, to condense and separately the first vapor stream of top of the tower, and it comprises: arrange and operation to take out the pipeline of the first vapor stream of top of the tower from the top of described scrubbing tower；Arrange and operation is to cool down and to condense the heat exchanger of described stream or heat exchanger section；With arrange and operation with by the stream of cooled and condensation separately to form pipeline group of at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction.
Described system can further include heat exchanger or heat exchanger section, its arranged and operation is to be subcooled described cooled and condensation stream, and then described stream is by separately to form at least one other stream of the first overhead materials of first-class, the second of the first overhead materials of liquefaction of the first overhead materials of liquefaction and liquefaction.Described system can further include heat exchanger or the heat exchanger section arranging and operating the second so that liquefaction first overhead materials is subcooled.
In the embodiment of second aspect, described system also comprises: dethanizer, its arrange and operation with receive from the second bottom liquid stream of described demethanizer bottom and by described flow separation for rich ethane fraction and the cut rich in the hydrocarbon heavier than ethane, described rich ethane fraction at the collected overhead of dethanizer as the 3rd overhead vapours, the described cut rich in the hydrocarbon than ethane more weight at the bottom collection of dethanizer as the 3rd bottom liquid；With arrange and operation to take out the second bottom liquid stream the pipeline that described stream is introduced to dethanizer from the bottom of domethanizing column.Described system can also comprise: arrange and operation is with the pipeline from the top of dethanizer taking-up the 3rd vapor stream of top of the tower, and arrange and operate to receive, cool down and to condense described stream to form one or more heat exchangers of NGL stream；And/or arrange and operate to take out the pipeline of the 3rd bottom liquid stream from the bottom of dethanizer, it is formed one or more NGL stream.Described system can also comprise heat exchanger, described heat exchanger is arranged and operation is with by other stream indirect heat exchanges of the first overhead materials with liquefaction, part condensation by described 3rd overhead vapours forms the 3rd overhead stream of liquefaction, 3rd overhead stream of described liquefaction is re-introduced into the top of described dethanizer as backflow stream, thus provides the backflow of described dethanizer；And arrange and operate so that other streams described in the first overhead materials of liquefaction to be introduced to the pipeline of described heat exchanger.Heat exchanger is operable to flow to form NGL with cooling and condensation the 3rd vapor stream of top of the tower, a part to condense threeth overhead vapours operable with heat exchanger is to form the 3rd overhead stream of liquefaction, 3rd overhead stream of described liquefaction is re-introduced into the top of dethanizer as backflow stream, and described heat exchanger can be a heat exchanger and identical heat exchanger.
Other embodiments of system according to second aspect by the embodiment of the method for first aspect discussed above obviously.
The preferred aspect of the present invention includes following aspect, numbering #1-#27:
#1. fractionation and the method for liquefied natural gas feed stream, described method comprises:
A described natural gas feed stream is introduced to scrubbing tower by (), described natural gas feed stream is separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane wherein, described vapor fraction is collected as the first bottom liquid in described wash tower bottoms as the first overhead vapours, described liquid distillate at described scrubbing tower collected overhead；
B () takes out the first vapor stream of top of the tower from the top of described scrubbing tower, and cool down, condense and by described stream separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction；
C the described first-class of the first overhead materials liquefied is back to described scrubbing tower by (), be incorporated into the top of described scrubbing tower as backflow, thus provide the backflow of described scrubbing tower；
D () is formed liquefied natural gas (LNG) product stream by the described second of the first overhead materials liquefying；
E () is taken out the first bottom liquid stream by the bottom of described scrubbing tower, and described stream is introduced to domethanizing column, described first bottom liquid stream is separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane wherein, described vapor fraction is collected as the second overhead vapours at described demethanizer overhead, and described liquid distillate is collected as the second bottom liquid at described demethanizer bottom；With
F () is refluxed to the offer of described domethanizing column by following:
(1) one of other streams described in the first overhead materials of liquefaction are introduced to the top of described domethanizing column as backflow stream；And/or
(2) by with one of other streams indirect heat exchange described in the first overhead materials of liquefaction, condensing a part for described second overhead vapours to form the second overhead stream of liquefaction, described second overhead stream is re-introduced into the top of described domethanizing column as backflow stream.
The method of #2. aspect #1, wherein step (b) comprises:
The first vapor stream of top of the tower is taken out at the top of described scrubbing tower, cool down and partly condense described stream, the liquid of isolated and vapor phase, by the liquid phase of described separation separately forming at least one other stream of the first overhead materials of the first-class and liquefaction of the first overhead materials of liquefaction, and cool down and condense at least a portion of vapor phase of described separation further to form the second of the first overhead materials of liquefaction；And/or
The first vapor stream of top of the tower is taken out at the top of described scrubbing tower, cool down and partly condense described stream, the liquid of isolated and vapor phase, the at least a portion of the liquid phase of described separation is formed the first-class of the first overhead materials liquefying, cool down and condense at least a portion of the vapor phase of described separation further, and the stream by the cooling further obtaining and condensation separates at least one other stream of the second of the first overhead materials to form liquefaction and the first overhead materials of liquefaction.
The method of #3. aspect #2, wherein:
Make the second supercooling of the first overhead materials of liquefaction, then form described LNG product stream；Or
Make flowing through of cooling and condensation cold, then separately to form at least one other stream of the second of liquefaction the first overhead materials and liquefaction the first overhead materials.
#4. aspect #2 or the method for #3, wherein cooling and the partial condensation in the warm bundle around tubular type main heat exchanger of the first vapor stream of top of the tower from described scrubbing tower top, and at least a portion of the vapor phase of described separation is in cooling and condensation further in the fasciculus intermedius and/or cold bundle of tubular type main heat exchanger.
#5. aspect #2 or the method for #3, wherein the first vapor stream of top of the tower from described scrubbing tower top cools down and partial condensation in overhead condenser heat exchanger, and at least a portion of the vapor phase of described separation is in cooling and condensation further in tubular type main heat exchanger.
The method of #6. aspect #1, wherein step (b) comprises:
Take out the first vapor stream of top of the tower from the top of described scrubbing tower, cooling and condense described stream, and by described cooling and condensate flow separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction.
The method of #7. aspect #6, wherein:
Make described cooling and condensate flow supercooling, then separately to form at least one other stream of the first overhead materials of the second of the first overhead materials of first-class, the liquefaction of the first overhead materials of liquefaction and liquefaction；Or
Described cooling and condensate flow separate first-class and another liquid stream of the first overhead materials to form liquefaction, make described liquid stream be subcooled subsequently, then separately to form at least one other stream of the first overhead materials of the second of the first overhead materials liquefying and liquefaction；Or
Make the second supercooling of the first overhead materials of liquefaction, then form described LNG product stream.
The method of #8. aspect any one of #1 to #7, other streams being wherein used as liquefaction the first overhead materials first-class of backflow stream and liquefaction the first overhead materials for step (f) in step (c) have the flow-rate ratio of at least about 9:1.
The method of #9. aspect any one of #1 to #8, is wherein used as liquefaction the first overhead materials first-class of backflow stream in step (c) and other streams of liquefaction the first overhead materials for step (f) each have about-40 DEG C or following temperature.
The methane of each self-contained at least about 95 moles of % of the method for #10. aspect any one of #1 to #9, wherein said first overhead vapours and the second overhead vapours, and the second bottom liquid comprises the methane of less than about 5 moles of %.
The method of #11. aspect any one of #1 to #10, wherein said method also comprises: taken out the second vapor stream of top of the tower by the top of domethanizing column；Cooling and condense all or part of of described stream to form other LNG product；And/or all or part of of described stream is used as fuel stream；And/or using described stream all or part of as gaseous natural gas product stream export.
The method of #12. aspect any one of #1 to #11, wherein said method also comprises to be taken out the second bottom liquid stream by the bottom of described domethanizing column, and is fractionated the second bottom liquid stream to provide one or more natural gas liquids (NGL) to flow.
The method of #13. aspect #12, wherein the fractionating step of the second bottom liquid stream comprises: be introduced to described stream in dethanizer, second bottom liquid stream is separated into the rich cut of ethane and the cut rich in the hydrocarbon heavier than ethane wherein, the cut of described rich ethane at the collected overhead of dethanizer as the 3rd overhead vapours, the described cut rich in the hydrocarbon than ethane more weight at the bottom collection of dethanizer as the 3rd bottom liquid.
The method of #14. aspect #13, wherein said method also comprises:
The 3rd vapor stream of top of the tower is taken out at the top of described dethanizer, and cools down and condense described stream to form NGL stream；And/or
The 3rd bottom liquid stream is taken out in the bottom of described dethanizer, and it is formed one or more NGL stream.
#15. aspect #13 or the method for #14, wherein said method also comprises as provided below being back in dethanizer: by other stream indirect heat exchanges of the first overhead materials with liquefaction, make the part condensation of the 3rd overhead vapours, forming the 3rd overhead stream of liquefaction, described 3rd overhead stream is re-introduced into the top of described dethanizer as backflow stream.
The method of #16. aspect any one of 13 to #15, wherein said 3rd overhead vapours comprises the ethane of at least about 95%, and described 3rd bottom liquid comprises the ethane of less than about 5 moles of %.
#17. is for the system of fractionation and liquefied natural gas feed stream, and described system comprises:
Scrubbing tower, described scrubbing tower is arranged and operation is used for receiving described natural gas feed stream, and be methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by described flow separation, described vapor fraction is collected as the first bottom liquid in described wash tower bottoms as the first overhead vapours, described liquid distillate at described scrubbing tower collected overhead；
Pipeline group, one or more heat exchangers, optionally one or more separators, it is arranged and operation is flowed at least one the first vapor stream of top of the tower taking out and being cooled down, condense and separate first-class, the second of the first overhead materials that liquefies of the first overhead materials to form liquefaction and the first overhead materials of liquefaction from the top of described scrubbing tower；
Pipeline, it is arranged and operation is for being back to described scrubbing tower by the described first-class of the first overhead materials of liquefaction, is incorporated into the top of described scrubbing tower as backflow stream, thus provides the backflow for described scrubbing tower；
Pipeline, it is arranged and operation is for taking out liquefied natural gas (LNG) product stream being formed by the second of the first overhead materials liquefying from described system；
Domethanizing column, it is arranged and operation is for from bottom reception first bottom liquid stream of described scrubbing tower, and be methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by described flow separation, described methane rich vapor fraction is collected as the second overhead vapours at described demethanizer overhead, and the described liquid distillate rich in the hydrocarbon than methane more weight is collected as the second bottom liquid at described demethanizer bottom；
Pipeline, it is arranged and operation is used for taking out the first bottom liquid stream from the bottom of described scrubbing tower, and described stream is introduced to domethanizing column；With
One below or both:
(1) pipeline, it is arranged and operates the top that one of other streams described in the first overhead materials being used for liquefying are introduced to described domethanizing column as backflow stream, thus provides the backflow of described domethanizing column；
(2) heat exchanger, its arrange and operation for by with one of other streams indirect heat exchange described in the first overhead materials of liquefaction, part condensation by described second overhead vapours forms the second overhead stream of liquefaction, it is re-introduced into the top of described domethanizing column as backflow stream, thus provide the backflow of described domethanizing column, and arrange and operate the pipeline that other streams described in the first overhead materials being used for liquefying are introduced to described heat exchanger.
The system of #18. aspect #17, wherein said pipeline group, one or more heat exchangers, and one or more separator arrange and operation with will described first vapor stream of top of the tower take out, cooling, condensation and separate, it comprises:
Arrange and operation for taking out the pipeline of the first vapor stream of top of the tower from the top of described scrubbing tower；
Arrange and operation is for cooling and the heat exchanger or the heat exchanger section that partly condense described stream；
Arrange and operation is used for the liquid of isolated and the separator of vapor phase；
Pipeline group, arranges and operation is used for the liquid phase of separately described separation to form other streams of the first overhead materials of the first-class and liquefaction of the first overhead materials of liquefaction；With
Heat exchanger or heat exchanger section, arrange and operation is used for receiving, cooling down further and condense at least a portion of the vapor phase of described separation to form the second of the first overhead materials of liquefaction.
The system of #19. aspect #18, wherein said system also comprise arrange and operation for receive and make described liquefaction the first overhead materials second supercooling heat exchanger or heat exchanger section.
#20. aspect #18 or the system of #19, wherein arrangement and operation comprises the warm bundle around tubular type main heat exchanger for the described heat exchanger section of the first vapor stream of top of the tower described in cooling and partial condensation, and arrangement and operation comprise the middle bundle around tubular type main heat exchanger and/or cold bundle with at least one of described heat exchanger section cooling down and condensing described separation vapor phase further.
#21. aspect #18 or the system of #19, the described heat exchanger wherein arranged and operate for the first vapor stream of top of the tower described in cooling and partial condensation comprises overhead condenser heat exchanger, and at least one of described heat exchanger arranging and operating the vapor phase for cooling down further and condensing described separation comprises around tubular type main heat exchanger.
The system of #22. aspect #17, wherein arrange and operation for taking out, cool down, condense and described pipeline group and one or more heat exchanger of separately described first vapor stream of top of the tower comprise:
Arrange and operation for taking out the pipeline of the first vapor stream of top of the tower from the top of described scrubbing tower；
Arrange and operation is for cooling down and condensing heat exchanger or the heat exchanger section of described stream；With
Pipeline group, its arrange and operation for the stream of separately described cooled and condensation to form at least one other stream of the first overhead materials of first-class, the second of the first overhead materials of liquefaction of the first overhead materials of liquefaction and liquefaction.
The system of #23. aspect #22, wherein said system also comprises heat exchanger or heat exchanger section, it is arranged and operation is for making flowing through of described cooled and condensation cold, and then described stream is by separately to form at least one other stream of the first overhead materials of first-class, the second of the first overhead materials of liquefaction of the first overhead materials of liquefaction and liquefaction.
The system of #24. aspect #22, wherein said system also comprises heat exchanger or the heat exchanger section arranging and operating the second supercooling of the first overhead materials for making described liquefaction.
The system of #25. aspect #17 to #24, wherein said system also comprises:
Dethanizer, it is arranged and operation is for from bottom reception second bottom liquid stream of described domethanizing column, and be rich ethane fraction and the cut rich in the hydrocarbon heavier than ethane by described flow separation, described rich ethane fraction is collected as the 3rd bottom liquid at described Deethanizer bottom as the 3rd overhead vapours, the described cut rich in the hydrocarbon than ethane more weight at described dethanizer collected overhead；With
Pipeline, it is arranged and operation is used for taking out the second bottom liquid stream from the bottom of described domethanizing column, and described stream is introduced to dethanizer.
The system of #26. aspect #25, wherein said system also comprises:
Arrange and operation is for the pipeline from the top of described dethanizer taking-up the 3rd vapor stream of top of the tower, and arrangement and operation are for receiving, cooling down and condensing described stream to form one or more heat exchangers that NGL flows；And/or
Arrange and operation for taking out the pipeline of the 3rd bottom liquid stream from the bottom of described dethanizer, it is formed one or more NGL stream.
#27. aspect #25 or the system of #26, wherein said system also comprises heat exchanger, it is arranged and operation is for by other stream indirect heat exchanges of the first overhead materials with liquefaction, make the part condensation of described 3rd overhead vapours, form the 3rd overhead stream of liquefaction, it is re-introduced into the top of described dethanizer as backflow stream, thus provides the backflow of described dethanizer, and arranges and operate the pipeline that other streams described in the first overhead materials being used for liquefying are introduced to described heat exchanger.
It is only used as example, describe the certain preferred embodiments of the present invention with reference now to accompanying drawing 2-7.In above-mentioned Fig. 1 and following Fig. 2-7, when a feature has for multiple figures, for clarity and conciseness for the sake of, this feature specifies identical reference in each figure.
In the embodiment that Fig. 2-7 describes, the main heat exchanger for liquefied natural gas is shown as wound tube heat exchanger.But, although this heat exchanger is preferably used, but main heat exchanger can be equally the heat exchanger of plate-fin heat exchanger or any other species known in the art.Similarly, although in the embodiment described, the coil pipe bundle of main heat exchanger is shown received within single cover or shell, form individual unit, but main heat exchanger can equally comprise two or more unit a series of, each bundle has the cover/shell of oneself, or one or more bundle is contained in a cover/shell, and one or more of the other bundle is contained in one or more different cover/shell.Refrigerant cycle for the refrigerant cold to main heat exchanger supply can be similarly for being applicable to implement any type of natural gas liquefaction.Exemplary cycle that is known in the art and use and that can be used for the present invention includes propane pre-cooling but hybrid refrigeration cycle (C3MR), and single mixing causes cool dose of circulation (SMR), nitrogen expander cycle, methane expander cycle, double mixing and causes cool dose of circulation (DMR) and cascade cycle.
With reference now to Fig. 2, in one embodiment of the invention, natural gas feed stream 101 is generally preprocessed with removal sour gas, water and mercury, and it optionally precools also in one or more heat exchangers, is incorporated into the bottom containing multiple scrubbing towers 10 separating levels.Natural gas feed is separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by scrubbing tower 10, described vapor fraction is collected as overhead vapours (also referred to herein as " the first overhead vapours " or " scrubbing tower overhead vapours ") at top of tower, described liquid distillate at the bottom collection of tower as bottom liquid (also referred to herein as " the first bottom liquid " or " wash tower bottoms liquid ").Take out vapor stream of top of the tower 202 from the top of scrubbing tower, and take out bottom liquid stream 103 from the bottom of scrubbing tower.
First vapor stream of top of the tower 202 sends to main heat exchanger 20 for cooling down and liquefying.In the embodiment described in which, main heat exchanger 20 is the wound tube heat exchanger containing the warm bundle accommodating in single clamshell the 22nd, middle bundle 24 and cold bundle 26.Main heat exchanger can provide any applicable refrigerant (not shown) by any applicable refrigerant cycle being effective to implement natural gas liquefaction.Vapor stream of top of the tower 202 is incorporated into the warm end of main heat exchanger 20, and cooled and be partially condensed to form partial condensation (two-phase) and flow 203 in warm bundle 22.Then described partial condensation stream 203 take out from warm bundle and be separated into liquid phase and vapor phase in phase separator 28 to produce liquid stream 120 and steam stream 207.
Steam stream 207 is back to main heat exchanger 20, and first it cool down in middle bundle 24 further and total condensation is to form the first overhead stream 204 of liquefaction wherein.The then supercooling in cold bundle 26 of first overhead stream of this liquefaction, thus produce LNG product stream 205.LNG product stream 205 can be as shown through flash distillation (such as by by stream by J-T valve) and be sent in LNG storage tank 30 for storing.From groove steam gas (BOG) or flash gas 401 can be sent to fuel header, through burning or be recycled to be fed in the vapor stream of top of the tower of main heat exchanger (not shown).
Liquid stream 120 from phase separator 28 is typically about the temperature of-40 DEG C to about-70 DEG C, is separated thus forms two streams 125 and 121 of the first overhead materials of liquefaction.Stream 125 generally comprises most of flows of stream 120, the flow-rate ratio of stream 125 and stream 121 be typically about 9:1 (therefore stream 125 generally account at least the 90% of stream 120, and stream 121 generally account for stream 120 less than 10%).Stream 125 is back to scrubbing tower 10 (generally by pumping or gravity), is incorporated into the top of scrubbing tower as backflow stream, in order to provide the backflow that scrubbing tower operation is required.Flowing 121 to send to the top of (generally after by J-T valve) domethanizing column 12, as backflow stream to provide domethanizing column to operate required backflow, further describing in will be described in more detail below.
The first bottom liquid stream 103 expanded (for example, as indicated, pass through J-T valve) taking out from scrubbing tower 10, partly to evaporate described stream, is then incorporated into the centre position of the domethanizing column 12 also containing multiple separation level.First bottom liquid 103 is separated into methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by domethanizing column 12, described vapor fraction is collected as overhead vapours (herein also referred to as " the second overhead vapours " or " demethanizer column overhead vapor ") at top of tower, and described liquid distillate is collected as bottom liquid (herein also referred to as " the second bottom liquid " or " demethanizer bottom liquid ") at tower bottom.In the present embodiment, and as previously discussed, by the first overhead stream 121 of liquefaction is introduced to, as backflow stream, the backflow that demethanizer overhead provides domethanizing column.A part for demethanizer bottom liquid heats as shown to provide the upflowing vapor of domethanizing column 12 in reboiler (it can use any applicable thermal source).The remainder of bottom liquid takes out as the second bottom liquid stream 105.
Temperature and pressure in scrubbing tower and domethanizing column generally makes the first overhead vapours and the methane of each self-contained at least about 95 moles of % of the second overhead vapours (i.e. scrubbing tower overhead vapours and demethanizer column overhead vapor) through control, and makes the second bottom liquid (i.e. demethanizer bottom liquid) comprise the methane less than 5 moles of %.This is done so that the rate of recovery of NLG and HHC (i.e. C2+ hydrocarbon) taken out from domethanizing column and the concentration the second bottom liquid stream maximize.Temperature at scrubbing tower and demethanizer overhead is controlled by the temperature of backflow stream 125, and 125 are formed by the first overhead materials liquefying, and this backflow stream is generally of about-40 DEG C or following temperature as above.The temperature of demethanizer bottom is controlled by demethanizer reboiler.Pressure in tower is limited by the pressure of natural gas feed stream 101, and when the first bottom liquid stream 103 (i.e. wash tower bottoms liquid stream) expands, surging declines.
From the demethanizer column overhead vapor of demethanizer overhead taking-up as the second vapor stream of top of the tower 104, can be used for any applicable or needs purpose.For example, it can be used as fuel stream, and/or be sent to pipeline or sell as gaseous natural gas product stream and output.In addition or alternatively, it (not shown) can cool down and condense (separate with the first overhead vapours and/or combine) to be formed and to provide other LNG product in main heat exchanger.
The second bottom liquid stream 105 taking out from the bottom of domethanizing column 12 is fractionated NGL fractionating system further, described NGL fractionating system comprises dethanizer the 14th, depropanizing tower 16 and debutanizing tower 18 in this case, so that provide required NGL stream (for example with as discussed above, it can be used as supplementing refrigerant, as independent merchandise sales, and/or optionally with LNG product in conjunction with to regulate the calorific value of LNG product).
More specifically, second bottom liquid stream (demethanizer bottom liquid) is first cooled (for example, as shown, by using the heat exchanger of empty gas and water or another kind of environment temperature cooling medium), then expanded (for example, as indicated, pass through heat exchanger and J-T valve) with forming part evaporation (two-phase) stream with cooling stream 105, it is incorporated into the centre position of dethanizer 14, and described dethanizer 14 is possibly together with multiple separation levels.Second bottom liquid 105 is separated into rich ethane vapor cut and the liquid distillate rich in the hydrocarbon heavier than ethane by dethanizer 14, described vapor fraction is collected as overhead vapours (being also known as " the 3rd overhead vapours " or " deethanizer overhead vapor " herein) at top of tower, and described liquid distillate is collected as bottom liquid (being also known as " the 3rd bottom liquid " or " Deethanizer bottom liquid " herein) at tower bottom.Backflow for dethanizer is as provided below: condensation deethanizer overhead vapor in overhead condenser heat exchanger (it can be provided with any applicable refrigerant), a part for the overhead materials of condensation is back to dethanizer 14 as backflow stream, and remainder takes out the 3rd overhead stream 106 as liquefaction.A part for Deethanizer bottom liquid, as indicated, heating in reboiler (it can use any applicable thermal source), in order to the upflowing vapor of dethanizer 14 is provided.The remainder of bottom liquid takes out as the 3rd bottom liquid stream 107.
Owing to usual only very small amount of methane is present in the fact that feed to the second bottom liquid stream 105 (demethanizer bottom liquid) of dethanizer (as discussed above), with due to the usual extraordinary fact of the rate of recovery/productivity of ethane (with other NGL) in the second bottom liquid, dethanizer can produce the vapor stream of top of the tower of rich ethane in the present embodiment, its existing high-purity is again with relatively high volume production, so that can be used for the amount maximization supplementing refrigerant and/or the high-purity ethane sold as NGL product stream.Generally, the 3rd overhead vapours (deethanizer overhead vapor) comprises the ethane of at least about 95 moles of %, and the 3rd bottom liquid (Deethanizer bottom liquid) comprises the ethane of less than about 5 moles of %.
3rd bottom liquid stream (Deethanizer bottom liquid) 107 expanded (for example passing through J-T valve), with (two-phase) stream of forming part evaporation, is introduced into the centre position of the depropanizing tower 16 also containing multiple separation level.3rd bottom liquid 107 is separated into rich propane vapor fraction and the liquid distillate rich in the hydrocarbon heavier than propane by depropanizing tower 16, described vapor fraction is collected as overhead vapours (being also known as " the 4th overhead vapours " or " depropanizing tower overhead vapours " herein) at top of tower, and described liquid distillate is collected as bottom liquid (being also known as " the 4th bottom liquid " or " depropanizing tower bottom liquid " herein) at tower bottom.Depropanizing tower back up through in overhead condenser heat exchanger, (be provided with any applicable refrigerant) condensation depropanizing tower overhead vapours provide, the part of overhead materials for condensation is back to depropanizing tower 16 as backflow, and remainder takes out as the 4th overhead stream 108 liquefying.A part for depropanizing tower bottom liquid heats as shown to provide the upflowing vapor of depropanizing tower 16 in reboiler (it can use any applicable thermal source).The remainder of bottom liquid takes out as the 4th bottom liquid stream 109.
4th bottom liquid stream (depropanizing tower bottom liquid) 109 expanded (for example passing through J-T valve), with (two-phase) stream of forming part evaporation, is introduced into the centre position of the debutanizing tower 18 also containing multiple separation level.4th bottom liquid 109 is separated into rich butane vapor fraction and the liquid distillate rich in the hydrocarbon heavier than butane by debutanizing tower 18, described vapor fraction is collected as overhead vapours (being also known as " the 5th overhead vapours " or " debutanizing tower overhead vapours " herein) at top of tower, and described liquid distillate is collected as bottom liquid (being also known as " the 5th bottom liquid " or " debutanizing tower bottom liquid " herein) at tower bottom.Debutanizing tower back up through in overhead condenser, (be provided with any applicable refrigerant) condensation debutanizing tower overhead vapours provide, the part of overhead materials for condensation is back to debutanizing tower 18 as backflow, and remainder takes out as the 5th overhead stream 110 liquefying.A part for debutanizing tower bottom liquid heats as shown to provide the upflowing vapor of debutanizing tower 18 in reboiler (it can use any applicable thermal source).The remainder of bottom liquid takes out as the 5th bottom liquid stream 111.
Compared with the conventional arrangement that Fig. 1 shows, therefore the method and system of the embodiment of the present invention described in Fig. 2 is back in the mode of domethanizing column difference in offer.Especially, although in arrangement in FIG, the overhead stream that the vapor stream of top of the tower taking out from scrubbing tower is cooled, condenses and separately liquefies with offer exactly two, one of them (steam 205) is used as the backflow stream of scrubbing tower as LNG product taking-up and another (stream 120), but in the arrangement of fig. 2, the vapor stream of top of the tower (the i.e. first vapor stream of top of the tower) from scrubbing tower taking-up is cooled, condense and separate at least three stream of the first overhead materials liquefying with offer.First-class (stream 125) of the first overhead materials of liquefaction is back to scrubbing tower as backflow stream, the second (stream 204) of the first overhead materials of liquefaction takes out as LNG product (stream 205), and other streams of at least one of the first overhead materials of liquefaction (stream 121) is introduced to the top of domethanizing column as backflow stream.As described above, this provides the advantage that the needs of special overhead condenser eliminating for domethanizing column, and (generally) provides and colder is back to domethanizing column (thus ethane recovery that enhancing is in demethanizer bottom liquid).
And the liquid that non-usage separates in phase separator 28 from the first overhead materials partial condensation stream 203 makes scrubbing tower and demethanizer reflux, but in alternative arrangement, the backflow of scrubbing tower and/or domethanizing column can be obtained by the one or more colder position of main heat exchanger.
Therefore, at present with reference to Fig. 3, the alternative embodiment of the present invention is described as follows: wherein main heat exchanger has only two bundles, i.e. warms up bundle 22 and cold bundle 26.The first vapor stream of top of the tower 202 taking out from scrubbing tower 10 top is re-introduced into warm bundle 22, but in this case, warm bundle is for cooling down with total condensation vapor stream of top of the tower to form the first overhead stream of liquefaction, then separated with the second 204 of first-class 125th, first overhead materials of liquefaction of the first overhead materials of formation liquefaction, and other streams 121 of the first overhead materials of liquefaction.In embodiment as shown in Fig. 2, first-class the 125 of first overhead materials of liquefaction are then return to the top of scrubbing tower 10 as backflow stream, the second 204 of the first overhead materials of liquefaction is subcooled to provide LNG product stream 205 in cold bundle 26, and other streams 121 of the first overhead materials of liquefaction are introduced to the top of domethanizing column as backflow stream.
Equally, at present with reference to Fig. 4, in still another embodiment, main heat exchanger also only has two bundles, i.e. warm up bundle 22 and cold bundle 26, but in the present embodiment, all restraint cooled 22 and total condensation from the stream 202 of the first overhead materials that scrubbing tower 10 takes out to form the first overhead stream 204 of liquefaction warm, and then this stream be all subcooled the mistake cold flow of the first overhead materials to form liquefaction in cold bundle 26, then separated to form first-class the 125 of the first overhead materials liquefying, other streams 121 of first overhead materials of the second 205 of the first overhead materials of liquefaction and liquefaction.In the present embodiment, the second 205 of the first overhead materials of liquefaction this as LNG product stream take out, it is not necessary to other cooling or process.Embodiment as shown in Fig. 2, first-class the 125 of the first overhead materials of liquefaction are back to the top of scrubbing tower 10 as backflow stream, and other streams 121 of the first overhead materials of liquefaction are introduced to the top of domethanizing column as backflow stream.
In the embodiment that Fig. 3 and 4 describes, first-class the 125 of first overhead materials of liquefaction and other streams 121 generally flow 121 much cooler than first-class the 125 of the first overhead materials of the liquefaction producing in the embodiment that Fig. 2 describes with other, owing to described stream is derived from the colder position of main heat exchanger in Fig. 3 and 4.In the embodiment depicted in fig. 3, the 125 and 121 usual temperature at about-100 DEG C to about-135 DEG C are flowed.In the embodiment showing in the diagram, the usual temperature at about-130 DEG C to about-160 DEG C of stream 125 and 121.Because these streams are in colder temperature, need the flow velocity that these streams are relatively lower, and it can be used for providing scrubbing tower 10 and the necessary backflow of domethanizing column 12, and (flow velocity of stream 125 and 121 required in the diagram is less than those in Fig. 3；Similarly flow velocity needed for 125 and 121 for the stream is less than those in Fig. 2 in figure 3).The arrangement described in Fig. 3 and 4 also eliminates the needs to phase separator 28 quantity reducing bundle required in main heat exchanger, thus reduces these capital costs arranged further.
In further embodiment (not shown), two or more combinations arranged described in Fig. 2,3 and 4 can be used for providing the backflow stream of scrubbing tower and domethanizing column.For example, in arranging at one, for making first-class the 125 of liquefaction the first overhead materials that scrubbing tower refluxes can produce as follows: partly condense the first vapor stream of top of the tower 202 taking out from scrubbing tower, liquid phase is separated in phase separator 28, and the similar fashion showing with Fig. 2 uses liquid phase to form first-class the 125 of the first overhead materials of liquefaction, it is used for making other streams 121 of the first overhead materials of the liquefaction of demethanizer reflux then produce as follows: other streams 121 of first overhead materials of other seconds 204/205 cooling down the first overhead materials separately liquefying with fluidized flow or supercooling stream with formation of the middle bundle of main heat exchanger or cold bundle and liquefaction will be left, with the similar fashion described in Fig. 3 or 4.
Equally, in another arrangement, the backflow of scrubbing tower and/or domethanizing column can be obtained by any other position in main heat exchanger cold end downstream, such as by LNG groove.They also can be obtained by the LNG stream producing in equipment another part, such as end-flash distillation interchanger (not shown), a part 101 for its liquefied natural gas stream, heat BOG or flash gas stream 401 simultaneously.
In still another embodiment, the backflow that can be provided to tower by overhead condenser to the backflow of scrubbing tower and/or domethanizing column is provided to supplement by first and other streams of the first overhead materials of liquefaction, or add to overhead condenser and provide to the backflow of tower, described overhead condenser is supplied with refrigerant and operates with condensation from least a portion of the overhead materials of described tower.
At present with reference to Fig. 5 and 6, yet another embodiment of the present invention shows different from the embodiment of display in Fig. 2, it is that the initial cooling of the first vapor stream of top of the tower 202 and partial condensation do not occur the warm bundle at main heat exchanger, but occur in single overhead condenser heat exchanger, by supplying refrigerant with the identical kind of refrigeration cycle of cooling load to described overhead condenser heat exchanger to main heat exchanger supply refrigerant.In figs. 5 and 6, depict two bundle formula wound tube heat exchangers, cause cool dose of circulation (C3MR) by propane pre-cooling mixing and supply refrigerant to it.As previously noted, main heat exchanger can be another type of heat exchanger, and different types of kind of refrigeration cycle can use equally, but only shows wound tube heat exchanger and C3MR circulation herein for the sake of simplicity.
In the embodiment that Fig. 5 and 6 describes, natural gas and propane refrigerant precool in precooler heat exchanger 34, are then introduced to scrubbing tower as natural gas feed stream 101.The first vapor stream of top of the tower 202 taking out from the top of scrubbing tower 10 (two-phase) that then partly cooling and condensation condense with forming part overhead condenser heat exchanger 32 flows 203.The stream 203 of partial condensation is separated into its liquid and vapor phase to produce liquid stream 120 and steam stream 207 in phase separator 28.Then, it by liquid stream 120 separately to form other streams 121 of the first overhead materials of first-class 125 and liquefaction of the first overhead materials of liquefaction, is then introduced to scrubbing tower 10 and domethanizing column 12 as backflow stream, as previously mentioned with respect to described in the embodiment of display in Fig. 2.Steam stream 207 is incorporated into main heat exchanger 20, and it cools down, condenses and be subcooled the second of the first overhead materials to form liquefaction further wherein, and it takes out as LNG product stream 205.Overhead condenser heat exchanger 32 can be plate-fin heat exchanger, printed circuit heat exchanger or any other applicable heat exchanger.
In the embodiment shown by Fig. 5, the warm mixed cooling medium stream 309 taking out from the bottom of main heat exchanger 20 sends to compressibility and (comprises motor 36, with related compressor and intercooler and aftercooler), this its compressed to form high-pressure refrigerant stream 312.Then, this stream in separator 38 be separated with produce mixed cooling medium steam (MRV) flow 302 and mixed cooling medium liquid (MRL) flow 301.Two streams 301 and 302 send to main heat exchanger with cooling in single loop.The MRV stream of cooled and at least part of condensation takes out from the cold end of the cold bundle of main heat exchanger, expand (for example, by J-T valve, as shown), and be re-introduced into the shell-side of main heat exchanger, as evaporation (vaporized)/vapo(u)rability (vaporizing) the refrigerant stream 308 of cold low-pressure to provide cooling load to the cold bundle of main heat exchanger and warm bundle.Cooled MRL stream takes out from the cold end of the warm bundle of main heat exchanger, then separates to form two streams.One flows through to expand and cold evaporates/low-pressure refrigerant the stream 307 of vapo(u)rability to be formed, and the shell-side being re-introduced into main heat exchanger is to provide other cooling load to the warm bundle of main heat exchanger.Another stream 320 is expanded (for example, by J-T valve, as shown) cold evaporate/low-pressure refrigerant the stream of vapo(u)rability to be formed, generally the temperature of about-60 DEG C to about-120 DEG C, it is by overhead condenser heat exchanger 32 to provide cooling load for partial condensation the first vapor stream of top of the tower 202, and described first vapor stream of top of the tower 202 is from the taking-up of the top of scrubbing tower 10.Then the warm refrigerant stream 350 leaving overhead condenser heat exchanger 32 can warm up the refrigerant combination warmed up of end as stream 309 with leaving main heat exchanger.Alternatively, if stream 350 remains two-phase, it can expand and send the shell-side of the main heat exchanger extremely in centre position further to provide other cooling load to the warm bundle of main heat exchanger.
In single tower top heat exchanger, rather than in the warm bundle of main heat exchanger self, via carrying out partial condensation with the refrigerant heat exchange from main heat exchanger from the benefit of the first vapor stream of top of the tower of scrubbing tower being, it eliminates multiple loop and bundle in main heat exchanger.This also results in the system of the relatively low-complexity being physically easier to perform.Current divider between stream refrigerant vapor 307 and 320 is regulated based on the tower top temperature of tower, and tower top temperature determines based on the required purity of the overhead stream from described tower again.
In the embodiment that Fig. 6 shows, the operation of kind of refrigeration cycle is similar to as Fig. 5 and described above.The only difference is that, in the embodiment that Fig. 6 describes, the refrigerant stream 320 providing to overhead condenser heat exchanger 32 obtains not by coming the MRL flow point of cooling that the cold end warming up bundle from main heat exchanger takes out, but the MRV stream of the cooling by taking out from the cold end of the cold bundle of main heat exchanger and at least part of condensation separately obtains.In this case, flow 320 temperature after inflation and be about-140 DEG C to-160 DEG C, therefore much cooler than refrigerant stream 320 equivalent in the embodiment showing at Fig. 5.
In addition to MRL and the MRV stream of Fig. 5-6 display, exist and can obtain other positions thus sending the refrigerant stream to overhead condenser heat exchanger 32.These change with the kind of refrigeration cycle being used.For example, in the SMR circulation of the mixed cooling medium stream using most four different compositions, the refrigerant for producing backflow can be obtained by these streams any.
At present with reference to Fig. 7, display yet another embodiment of the present invention, it is different from the embodiment that Fig. 2 shows, it is that other streams 121 of the first overhead materials of liquefaction are incorporated into the top of domethanizing column 12 not as backflow stream, but in overhead condenser heat exchanger, it is used as refrigerant stream, wherein part the second overhead vapours (i.e. part demethanizer column overhead vapor) is condensed by other stream indirect heat exchanges of the first overhead materials with liquefaction, to form the second overhead stream of liquefaction, it is re-introduced into the top of domethanizing column as backflow stream.Therefore, although other streams of the first overhead materials of liquefaction are not the backflow stream itself functioning as in domethanizing column, but in the present embodiment, other streams of the first overhead materials of liquefaction supply cooling load really, for producing the backflow in domethanizing column, therefore still produces the backflow of domethanizing column indirectly.
More specifically, with as it is shown in fig. 7, in the present embodiment, the first liquefaction overhead stream 202 taking out from scrubbing tower 10 top restraints again cooled and partial condensation 22 at the warm of main heat exchanger 20, it to form two phase flow 203, in separator 28, is then separated into its liquid phase and vapor phase.Liquid phase 120 is spaced further apart first-class 125 of the first overhead materials to form liquefaction again, and in this case, two of the first overhead materials of liquefaction other streams 121 and 122.The top that first-class the 125 of first overhead materials of liquefaction are re-introduced into as previously mentioned to scrubbing tower 10 is to provide the backflow of this tower.But, two of the first overhead materials of liquefaction other streams 121 and 125 are used as refrigerant stream in this case to supply cooling load to demethanizer column overhead condenser heat exchanger 40 and deethanizer overhead condenser heat exchanger 42 respectively.
In this case, the backflow of domethanizing column 12 is therefore by following generation: taken out demethanizer column overhead vapor stream (" the second overhead vapours ") by the top of domethanizing column；Described stream by one of other streams of the first overhead materials 121 indirect heat exchanges with liquefaction at demethanizer column overhead condenser 40 partial condensation；Separate liquid phase and vapor phase；As the second overhead stream of liquefaction, liquid phase is back to domethanizing column, and it is re-introduced into the top of tower as backflow stream；With take out remaining vapor phase as the second vapor stream of top of the tower 104 (such as with as discussed above, this stream can be used as fuel, and as the output of gaseous natural gas product, and/or liquefaction is to provide other LNG product).
Similarly, in the present embodiment, the backflow of dethanizer 14 is therefore by following generation: take out deethanizer overhead vapor stream (" the 3rd overhead vapours ") from the top of described dethanizer；Described stream is condensed in deethanizer overhead condenser 42 by another other stream 122 indirect heat exchanges of the first overhead materials with liquefaction；As the 3rd overhead stream of liquefaction, a part for liquefaction overhead materials is back to dethanizer, and it is re-introduced into top of tower as backflow stream；With the remainder of the overhead materials taking out liquefaction as the 3rd overhead stream 106 (such as with as discussed above, this stream can be sold as NGL product, is used as to supplement refrigerant, and/or combines to regulate the calorific value of the latter with LNG product) of liquefaction.
The warm current 126 and 127 of the first overhead materials leaves demethanizer column overhead condenser 40 and deethanizer overhead condenser 42, can be used for any applicable or required purposes.For example, they can reinject to natural gas feed, and/or it is supplementary to be used as refrigerant.
Additionally, the many changes arranged shown in Fig. 7 are also possible.For example, not as shown in Figure 7 by phase separator 28 obtain stream the 125th, 121 and 122 some or all, but the colder position of main heat exchanger can be obtained stream the 125th, 121 and/or 122, by similar fashion of the first-class of the first overhead materials of the liquefaction producing in the embodiment that Fig. 3 and 4 describes and other streams.
Embodiment
In order to the operation of the present invention is described, the method removing refrigerant in the natural gas liquefaction system describing such as Fig. 2 and 3 and describing is used the simulation of ASPEN Plus software.
Table 1 below lists the condition of the simulation of the method described for Fig. 2 and the composition of each stream, and table 2 lists the condition of the simulation of the method described for Fig. 3 and the composition of each stream.Data explanation in these forms, utilize a part (by the first overhead vapours cooling taken out from scrubbing tower, liquefaction and separately producing) for other streams of the first overhead materials of liquefaction, to make demethanizer reflux, cause efficiently separating of heavy hydrocarbon and NGL composition and natural gas.Additionally, compared with conventional arrangement for example depicted in figure 1, these arrange the minimizing causing equipment cost, by elimination demethanizer column overhead condenser and reflux drum, thus cause cost savings and simpler operation.
Table 1
Table 2
It should be understood that the present invention is not limited to the details describing above with reference to preferred embodiment, but many improvement and change can be carried out under the spirit of the invention limiting without departing from following claims or scope.

Claims (9)

1. the system for fractionation and liquefied natural gas feed stream, described system comprises:
Scrubbing tower, described scrubbing tower is arranged and operation is used for receiving described natural gas feed stream, and be methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by described flow separation, described vapor fraction is collected as the first bottom liquid in described wash tower bottoms as the first overhead vapours, described liquid distillate at described scrubbing tower collected overhead；
Pipeline group, one or more heat exchangers, optionally one or more separators, it is arranged and operation is flowed at least one the first vapor stream of top of the tower taking out and being cooled down, condense and separate first-class, the second of the first overhead materials that liquefies of the first overhead materials to form liquefaction and the first overhead materials of liquefaction from the top of described scrubbing tower；
Pipeline, it is arranged and operation is for being back to described scrubbing tower by the described first-class of the first overhead materials of liquefaction, is incorporated into the top of described scrubbing tower as backflow stream, thus provides the backflow for described scrubbing tower；
Pipeline, it is arranged and operation is for taking out liquefied natural gas (LNG) product stream being formed by the second of the first overhead materials liquefying from described system；
Domethanizing column, it is arranged and operation is for from bottom reception first bottom liquid stream of described scrubbing tower, and be methane rich vapor fraction and the liquid distillate rich in the hydrocarbon heavier than methane by described flow separation, described methane rich vapor fraction is collected as the second overhead vapours at described demethanizer overhead, and the described liquid distillate rich in the hydrocarbon than methane more weight is collected as the second bottom liquid at described demethanizer bottom；
Pipeline, it is arranged and operation is used for taking out the first bottom liquid stream from the bottom of described scrubbing tower, and described stream is introduced to domethanizing column；With
One below or both:
(1) pipeline, it is arranged and operates the top that one of other streams described in the first overhead materials being used for liquefying are introduced to described domethanizing column as backflow stream, thus provides the backflow of described domethanizing column；
(2) heat exchanger, its arrange and operation for by with one of other streams indirect heat exchange described in the first overhead materials of liquefaction, part condensation by described second overhead vapours forms the second overhead stream of liquefaction, it is re-introduced into the top of described domethanizing column as backflow stream, thus provide the backflow of described domethanizing column, and arrange and operate the pipeline that other streams described in the first overhead materials being used for liquefying are introduced to described heat exchanger.
2. the system for fractionation and liquefied natural gas feed stream according to claim 1, it is characterized in that: described pipeline group, one or more heat exchangers, and one or more separator arranges and operate to take out described first vapor stream of top of the tower, cool down, condense and separately, it comprises:
Arrange and operation for taking out the pipeline of the first vapor stream of top of the tower from the top of described scrubbing tower；
Arrange and operation is for cooling and the heat exchanger or the heat exchanger section that partly condense described stream；
Arrange and operation is used for the liquid of isolated and the separator of vapor phase；
Pipeline group, arranges and operation is used for the liquid phase of separately described separation to form other streams of the first overhead materials of the first-class and liquefaction of the first overhead materials of liquefaction；With
Heat exchanger or heat exchanger section, arrange and operation is used for receiving, cooling down further and condense at least a portion of the vapor phase of described separation to form the second of the first overhead materials of liquefaction.
3. according to claim 2 for fractionation and the system of liquefied natural gas feed stream, it is characterized in that: described system also comprises to arrange and operation is for receiving and making the heat exchanger of second supercooling of the first overhead materials or the heat exchanger section of described liquefaction.
4. the system for fractionation and liquefied natural gas feed stream according to claim 2, it is characterized in that: arrangement and operation comprise the warm bundle around tubular type main heat exchanger for the described heat exchanger section of the first vapor stream of top of the tower described in cooling and partial condensation, and arrangement and operation comprise the middle bundle around tubular type main heat exchanger and/or cold bundle with at least one of described heat exchanger section cooling down and condensing described separation vapor phase further.
5. the system for fractionation and liquefied natural gas feed stream according to claim 2, it is characterized in that: the described heat exchanger arranged and operate for the first vapor stream of top of the tower described in cooling and partial condensation comprises overhead condenser heat exchanger, and at least one of described heat exchanger arranging and operating the vapor phase for cooling down further and condensing described separation comprises around tubular type main heat exchanger.
6. according to claim 1 for fractionation and the system of liquefied natural gas feed stream, it is characterized in that: arrange and operation is for taking out, cooling down, condense and described pipeline group and one or more heat exchanger of separately described first vapor stream of top of the tower comprise:
Arrange and operation for taking out the pipeline of the first vapor stream of top of the tower from the top of described scrubbing tower；
Arrange and operation is for cooling down and condensing heat exchanger or the heat exchanger section of described stream；With
Pipeline group, its arrange and operation for the stream of separately cooled and condensation to form at least one other stream of the first overhead materials of first-class, the second of the first overhead materials of liquefaction of the first overhead materials of liquefaction and liquefaction.
7. the system for fractionation and liquefied natural gas feed stream according to claim 6, it is characterized in that: described system also comprises heat exchanger or heat exchanger section, it is arranged and operation is for making flowing through of described cooled and condensation cold, and then described stream is by separately to form at least one other stream of the first overhead materials of first-class, the second of the first overhead materials of liquefaction of the first overhead materials of liquefaction and liquefaction.
8. the system for fractionation and liquefied natural gas feed stream according to claim 6, is characterized in that: described system also comprises heat exchanger or the heat exchanger section arranging and operating the second supercooling of the first overhead materials for making described liquefaction.
9. the system for fractionation and liquefied natural gas feed stream according to claim 1, is characterized in that: described system also comprises:
Dethanizer, it is arranged and operation is for from bottom reception second bottom liquid stream of described domethanizing column, and be rich ethane fraction and the cut rich in the hydrocarbon heavier than ethane by described flow separation, described rich ethane fraction is collected as the 3rd bottom liquid at described Deethanizer bottom as the 3rd overhead vapours, the described cut rich in the hydrocarbon than ethane more weight at described dethanizer collected overhead；With
Pipeline, it is arranged and operation is used for taking out the second bottom liquid stream from the bottom of described domethanizing column, and described stream is introduced to dethanizer.
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