CN1965204A - Mixed refrigerant liquefaction process - Google Patents

Mixed refrigerant liquefaction process Download PDF

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Publication number
CN1965204A
CN1965204A CNA2005800174924A CN200580017492A CN1965204A CN 1965204 A CN1965204 A CN 1965204A CN A2005800174924 A CNA2005800174924 A CN A2005800174924A CN 200580017492 A CN200580017492 A CN 200580017492A CN 1965204 A CN1965204 A CN 1965204A
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China
Prior art keywords
cooling agent
blending constituent
constituent cooling
heat exchange
stream
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Granted
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CNA2005800174924A
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Chinese (zh)
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CN100504262C (en
Inventor
J·B·斯通
D·J·霍里兹
E·L·金布尔
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ExxonMobil Upstream Research Co
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Exxon Production Research Co
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Publication of CN1965204A publication Critical patent/CN1965204A/en
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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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic 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
    • 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"
    • F25J1/0042—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 liquid expansion with extraction of work
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—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
    • 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
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/12—Inflammable refrigerants
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/13—Economisers
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

A method for liquefying a natural gas stream is provided. In one embodiment, the method includes placing a mixed component refrigerant in a heat exchange area with a process stream; separating the mixed component refrigerant at one or more pressure levels to produce a refrigerant vapor and a refrigerant liquid; bypassing the refrigerant vapor around the heat exchange area to a compression unit; and passing the refrigerant liquid to the heat exchange area. In another embodiment, the method further includes partially evaporating the refrigerant liquid stream within the heat exchange area to retain a liquid fraction of at least 1% by weight.

Description

Mixed refrigerant liquefaction process
The cross reference of related application
[0001] the application requires the rights and interests of U.S. Provisional Application 60/565,589, and its applying date is on June 23rd, 2004.
Background
Technical field
[0002] embodiment of the present invention relate generally to for example method of natural gas of blending constituent coolant cools air-flow of using.
Association area is described
[0003] natural gas is liquefied usually and transports, and consumes country with the supply main energy sources.Be liquefied natural gas, (feed gas) is at first processed for unstripped gas, removes pollutant and the ratio heavy hydrocarbon of pentane at least.Then, usually under high pressure, cool off this purified gas by the indirect heat exchange of one or more cool cycles.Because the complexity of equipment needed thereby and the efficient performance of cooling agent, such cool cycles is at capital consumption and operating aspect cost height.Therefore, to improve cooling effectiveness, reduce equipment volume and reduce running cost method have demand.
General introduction
[0004] provides the method for liquefied natural gas air-flow.In one embodiment, this method is included in and places the blending constituent cooling agent in the heat exchange zone that contains process stream (process stream); Under one or more stress level, separate the blending constituent cooling agent, to produce coolant vapours and coolant liquid; Coolant vapours is passed through around the heat exchange zone bypass, enter compression unit; And make coolant liquid pass through heat exchange zone.
[0005] in another embodiment, this method is included in and places the blending constituent cooling agent in the heat exchange zone that contains process stream; Withdraw from two strands or the effluent of multiply blending constituent cooling agent more from heat exchange zone; The effluent that separates the blending constituent cooling agent under one or more stress level is to produce coolant vapours and coolant liquid; Coolant vapours is passed through around the heat exchange zone bypass, enter compression unit; And make coolant liquid pass through heat exchange zone.
[0006] in another embodiment, this method is included in and places the blending constituent cooling agent in the heat exchange zone that contains process stream; Under one or more stress level, separate the blending constituent cooling agent, to produce coolant vapours stream and coolant liquid stream; Coolant vapours stream is passed through around the heat exchanging region bypass, enter compression unit; Make coolant liquid stream pass through heat exchange zone; And the coolant liquid stream of in heat exchange zone, partly vaporizing, to keep at least 1% liquid component by weight.
[0007] in another embodiment, this method is included in and places the first blending constituent cooling agent in first heat exchange zone that contains process stream; Under one or more stress level, separate the first blending constituent cooling agent, to produce coolant vapours stream and coolant liquid stream; Coolant vapours stream is passed through around the first heat exchanging region bypass, enter compression unit; Make coolant liquid stream by first heat exchange zone, with the process for cooling material flow; And in second heat exchange zone that contains process stream, place the second blending constituent cooling agent through cooling off, with this process stream that liquefies.
[0008] in another embodiment, this method is included in and places the first blending constituent cooling agent in first heat exchange zone that contains process stream; Under one or more stress level, separate the blending constituent cooling agent, to produce coolant vapours stream and coolant liquid stream; Coolant vapours stream is passed through around the first heat exchanging region bypass, enter compression unit; Make coolant liquid stream turn back to first heat exchange zone, with cooling blast; In second heat exchange zone that contains process stream, place the second blending constituent cooling agent through cooling off; And the second blending constituent cooling agent of under single stress level, vaporizing, with this air-flow that liquefies.
[0009] still in another embodiment, this method comprises makes blending constituent cooling agent stream and process stream carry out heat exchange, and this cooling agent stream comprises liquid coolant; And before vaporizing fully, this liquid coolant flow quilt ended heat exchange.
[0010] still in other embodiments, this method comprises liquefied natural gas, and it is by placing the blending constituent cooling agent in containing the heat exchange zone of process stream; Under one or more stress level, separate the blending constituent cooling agent, to produce coolant vapours and coolant liquid; At least make coolant liquid pass through heat exchange zone; And the coolant liquid of in heat exchange zone, partly vaporizing, to keep liquid phase.In optional embodiment, this method is included in and places the blending constituent cooling agent in the heat exchange zone that contains process stream; Withdraw from two strands or the effluent of multiply blending constituent cooling agent more from heat exchange zone; The effluent that separates the blending constituent cooling agent under one or more stress level is to produce coolant vapours and coolant liquid; At least make coolant liquid pass through heat exchange zone; And the coolant liquid of in heat exchange zone, partly vaporizing, to keep liquid phase.
Describe in detail
Introduce and definition
[0011] will provide detailed description now.Each of appended claim limits an independent invention, and it is believed to comprise the equivalent of a plurality of elements of claim and specified limit for the purpose of encroaching right.Based on context, can only be meant some specific embodiments to quoting in some cases of " invention " below.In other cases, can think, quoting of " invention " is meant one or more described main body in the claim, but need not to be whole claims.Below each invention will be described in more detail, comprise specific embodiment, description and example, but the present invention is not limited to these embodiments, description and example, and it is included to make those of ordinary skill in the art can realize and use the present invention when should patent information combining with obtainable information and technology.Defined a plurality of term used herein below.With regard to employed term in the claim was not defined below, it should be given the wideest definition, and promptly the personnel of association area have given the scope of this definition, as reflecting in the patent of published publication and publication.
[0012] term " blending constituent cooling agent (mixed component refrigerant) " and " MCR " are exchanged use, refer to contain the mixture of two or more coolant compositions.The example of the MCR of Miao Shuing is " MCR " and " the 2nd MCR " herein.
[0013] term " coolant composition (refrigerant component) " refers to be used for the material that heat is transmitted, and it absorbs heat and emit heat under higher temperature under lower temperature.For example, " coolant composition " in the compression cooling system will absorb heat by vaporization under lower temperature and pressure, and emit heat by condensation under higher temperature and pressure.Alkane, alkene and alkynes, nitrogen, chlorinated hydrocabon, fluorinated hydrocarbons, other halogenated hydrocarbon that illustrative coolant composition can include, but not limited to have 1 to 5 carbon atom with and composition thereof or combination.
[0014] term " natural gas (natural gas) " is meant the mixture of light hydrocarbon gas or two or more light hydrocarbon gas.Illustrative light hydrocarbon gas can include, but not limited to methane, ethane, propane, butane, pentane, hexane, its isomers, its unsaturates and their mixture.Term " natural gas " may further include the impurity of certain level, for example nitrogen, hydrogen sulfide, carbon dioxide, nitric sulfid, sulphur alcohol and water.According to storing source and any pre-treatment step for example amine extraction or the drying by carrying out as molecular sieve, the accurate percentage composition of natural gas changes.At least one example of " natural gas " composition is to contain about 55 mole percent methane or more gas.
[0015] term " gas (gas) " and " steam (vapor) " are used interchangeably, and refer to have the material or the mixture of substances that are different from liquid or solid-state gaseous form.
[0016] material that can comprise the mixture of substances that is not 100% steam described in term " part vaporization (partially evaporated) "." part vaporization " stream can have vapor phase and liquid phase.At least one example of " part vaporization " stream comprises such stream: have at least 1% or by weight at least 2% or by weight at least 3% or by weight at least 4% or by weight at least 5% liquid phase by weight, and surplus is a vapor phase.In one or more specific embodiments, " part vaporization " stream has such liquid range: from 1% or by weight 3% or by weight 10% low scope by weight to 90% or by weight 97% or by weight 99% high scope by weight.
[0017] term " heat exchange zone (heat exchange area) " is meant a kind of or combination in the dissimilar equipment as known in the art that helps to conduct heat of phase Sihe.For example, " heat exchange zone " can be included in or to small part be included in one or more plant spiral wound form interchangers, heat radiation type interchanger, shell-and-tube interchanger, maybe can tolerate herein below known in the art any other type heat exchanger of process conditions in greater detail.
[0018] term " compression unit (compression unit) " refers to any type or the combination of similar or different compression devices, and can comprise the auxiliary equipment that is used for pressurized contents or mixture of substances as known in the art." compression unit " can adopt one or more compression stage.Illustrative compressor can include, but not limited to for example reciprocating type and Rotary Compressor of positive displacement type, and power type such as centrifugal and Axial Flow Compressor.Illustrative auxiliary equipment can include, but not limited to suck separation container (suction knock-out vessel), discharging cooler (discharge coolers or chillers), recirculation cooler and combination arbitrarily thereof.
Specific embodiments
[0019] a plurality of specific embodiments are described below, at least some embodiments also are described in the claims.For example, at least one embodiment relates to the method for liquefied natural gas stream, and it is by placing the blending constituent cooling agent and separating the blending constituent cooling agent to produce coolant vapours and coolant liquid under one or more stress level in containing the heat exchange zone of process stream.Coolant vapours passes through around the heat exchange zone bypass, enters compression unit, and coolant liquid passes through heat exchange zone.
[0020] at least one other specific embodiments relates to liquefied natural gas stream, and it is by placing the blending constituent cooling agent and withdrawing from two strands or the effluent of multiply blending constituent cooling agent more from heat exchange zone in containing the heat exchange zone of process stream.Then, under one or more stress level, separate the effluent of blending constituent cooling agent, to produce coolant vapours and coolant liquid.Coolant vapours passes through around the heat exchange zone bypass, enters compression unit, and makes coolant liquid pass through heat exchange zone.
[0021] there is another specific embodiments to relate to liquefied natural gas stream again, it is by placing the blending constituent cooling agent and separate the blending constituent cooling agent under one or more stress level, to produce coolant vapours stream and coolant liquid stream in containing the heat exchange zone of process stream.Coolant vapours stream passes through around the heat exchanging region bypass, enters compression unit.Make coolant liquid stream by heat exchange zone, and the coolant liquid stream of in heat exchange zone, partly vaporizing, to keep at least 1% liquid fraction by weight.
[0022] there is another specific embodiments to relate to the method for liquefied natural gas stream again, it is by placing the first blending constituent cooling agent and separate the first blending constituent cooling agent under one or more stress level, to produce coolant vapours stream and coolant liquid stream in containing first heat exchange zone of process stream.Coolant vapours stream is passed through around the first heat exchanging region bypass, enter compression unit, and make coolant liquid stream by first heat exchange zone, with the process for cooling material flow.Then, in second heat exchange zone that contains process stream, place the second blending constituent cooling agent, with this process stream that liquefies through cooling off.
[0023] there is another specific embodiments to relate to liquefied natural gas stream again, it is by placing the first blending constituent cooling agent in containing first heat exchange zone of process stream, with under one or more stress level, separate the blending constituent cooling agent, flow to produce coolant vapours stream and coolant liquid.Coolant vapours stream is passed through around the first heat exchanging region bypass, enter compression unit, and make coolant liquid stream by first heat exchange zone, with cooling blast.In second heat exchange zone that contains process stream, place the second blending constituent cooling agent through cooling off, and the second blending constituent cooling agent of under single stress level, vaporizing, with this air-flow that liquefies.
[0024] have another specific embodiments to relate to the cooled natural gas process stream again, it carries out heat exchange by making blending constituent cooling agent stream with process stream.This cooling agent stream comprises liquid coolant, and is ended heat exchange before the vaporization fully in this liquid coolant flow.
[0025] still in other embodiments, coolant vapours stream or multiply coolant vapours stream does not need bypass by heat exchanger or a plurality of heat exchanger and/or do not need directly to be sent into compression unit.In such embodiments, vapor stream or multiply vapor stream can for example be returned to heat exchanger or a plurality of heat exchanger, and perhaps they can bypass pass through heat exchanger or a plurality of heat exchanger, and are sent in the equipment of non-compression unit.Therefore, the embodiment of this method comprises herein the modification of any embodiment of describing, and wherein coolant vapours stream or multiply coolant vapours stream do not need bypass by heat exchanger or a plurality of heat exchanger and/or do not need directly to be sent into compression unit.Such embodiment comprises, for example, liquefied natural gas, it passes through: place the blending constituent cooling agent in containing the heat exchange zone of process stream; Under one or more stress level, separate the blending constituent cooling agent, to produce coolant vapours and coolant liquid; At least make coolant liquid pass through heat exchange zone; And the coolant liquid of in heat exchange zone, partly vaporizing, to keep liquid phase.Such embodiment also is included in and places the blending constituent cooling agent in the heat exchange zone that contains process stream; Withdraw from two strands or the effluent of multiply blending constituent cooling agent more from heat exchange zone; The effluent that separates the blending constituent cooling agent under one or more stress level is to produce coolant vapours and coolant liquid; At least make coolant liquid pass through heat exchange zone; And the coolant liquid of in heat exchange zone, partly vaporizing, to keep liquid phase.
Specific embodiments in the accompanying drawing
[0026] now the specific embodiments shown in the accompanying drawing will be described.What emphasize is that claim should not be understood as that the aspect that is subject in the accompanying drawing.Fig. 1 diagram has been described to use to the blending constituent coolant cools of small part vaporization or the process for cooling of liquefaction process material flow or unstripped gas.Fig. 2 diagram has been described to use and has wherein been contained the cools down of two or more heat exchange zones or the process for cooling of liquefaction process material flow or unstripped gas.Fig. 3 diagram has described to use the process for cooling of two kinds of blending constituent coolant cools or liquefaction process material flow and unstripped gas.Fig. 4 illustrates the another kind of method of using liquid coolant gathering system process for cooling material flow or unstripped gas.Simple and clear and convenient on describing, when these process for cooling relate to by cross cold with the natural gas that produces liquefied natural gas (" LNG ") process stream or during unstripped gas, they will be further described in this article.
Fig. 1
[0027] Fig. 1 diagram described to use to the blending constituent cooling agent of small part vaporization with the process for cooling 5 of process for cooling material flow or unstripped gas at least.In heat exchanger 10, make flow of feed gas 12 and blending constituent cooling agent (" MCR ") stream 30 carry out heat exchange.Be explained in more detail as following, MCR stream 30 expanded and cooling, with heat exchanger 10 in from flow of feed gas 12 except that reducing phlegm and internal heat.Although not shown, other process stream that need cool off can enter heat exchanger 10.The non-limitative example of other stream like this comprise other cooling agent stream, will in the operation stage of back with other hydrocarbon streams of air-flow 12 blending, and the stream of integrating with one or more classification treatment step.
[0028] as shown in Figure 1, heat exchanger 10 is the single unit that contain at least one heat exchange zone.Although it is not shown, but as described below, heat exchanger 10 can comprise two or more heat exchange zones, for example two, three, four or five, described heat exchange zone can be contained in the single unit, and perhaps each district can be contained in the independent unit.
[0029] unstripped gas 12 natural gas preferably, and can contain methane in mole at least 55% or at least 65% or at least 75%.MCR stream 30 can comprise one or more in alkane, alkene and alkynes, nitrogen, chlorinated hydrocabon, fluorinated hydrocarbons, other halogenated hydrocarbon and their mixture or the composition with 1 to 5 carbon atom.In one or more specific embodiments, MCR stream 30 is mixtures of ethane and propane.In one or more specific embodiments, MCR stream 30 is mixtures of ethane, propane and iso-butane.In one or more specific embodiments, MCR stream 30 is mixtures of methane, ethane and nitrogen.
[0030] MCR stream 30 is cooled in heat exchange zone 10, and withdraws from heat exchange zone 10 as stream 40.Use expansion gear that stream 40 is expanded, produce two phase flow 50 (stream that promptly has vapor phase and liquid phase).Illustrative expansion gear includes, but are not limited to valve, control valve, joule Thomsons valve (Joule Thompson valve), Venturi (Venturi device), fluid expansion reservoir, the hydraulic turbine and similar device.Preferably, expansion gear 45 is self-driven expansion valve or joule Thomsons valve.Then, two phase flow 50 is separated in separator 55, produces vapor stream 60 and liquid stream 65.Preferably, two phase flow 50 is carried out flash separation (flashsepearation).Heat exchange zone 10 is passed through in vapor stream 60 bypasses, and is directly sent into compression unit 75.
Therefore [0031] after being depressurized and being cooled, liquid stream 65 returns heat exchange zone 10, in this heat exchange zone 10 since with the heat exchange of process gas flow 12 and MCR stream 30, liquid stream 65 is evaporated wholly or in part.This evaporates fully or the part evaporation current withdraws from heat exchange zone 10 as stream 70.In one or more specific embodiments, stream 70 has at least 85% or by weight at least 90% or by weight at least 99% steam component by weight, and surplus is a liquid phase component.In one or more specific embodiments, stream 70 is the vapor streams that do not contain liquid phase.Stream 70 flows to compression unit 75 subsequently.
[0032] according to process conditions and requirement, compression unit 75 can adopt one or more compression stage.Preferably, compression unit 75 adopts two or more compression stages, and wherein each compression stage utilizes intercooler to remove the heat of compression.Then, compressed stream is admitted to heat exchange zone 10 as stream 30.More go through exemplary compression unit below.
[0033] by vapor stream 60 is directly sent into compression unit 75 (promptly making the coolant vapours bypass pass through compression unit around heat exchange zone) around heat exchange zone 10, can avoid some distribution problem relevant with the two-phase cooling agent.Term " two-phase cooling agent (two-phase refrigerant) " is meant the vapor phase cooling agent with at least some liquid phase coolant and by volume at least 10%.Because the two-phase cooling agent distributes in heat exchange zone and is not suitable for, two-phase distributes and can cause liquefied gas yield to reduce and revenue losses.Being not suitable for distributing and can causing the heat transfer of poor efficiency of two-phase cooling agent in heat exchange zone, because compare with liquid phase, the vapor phase of two-phase cooling agent occupies more volume in heat exchange zone.Because compare with the liquid phase of evaporation usefulness, vapor phase is very little for the contribution of heat exchange, thereby the cooling capacity of infringement cooling agent.
[0034] and, can be effectively on maintenance time (engineering time) and the equipment bought, be expensive to the waterpower design of the system of heat exchanger or a plurality of heat exchangers with the two-phase coolant distribution.Under departing from regard to the too many situation of the design condition aspect temperature, pressure and/or the flow velocity, the behavior of this design more is difficult to prediction.Be particularly suited for arrangement with the heat exchanger that be arranged in parallel according to the benefit of describing that one or more embodiment obtained herein, described heat exchanger is from common source charging cooling agent, this is because vapor phase is removed, thereby eliminates this distribution factor.
Fig. 2
[0035] Fig. 2 diagram has described to use the heat exchanger that wherein contains the above heat exchange zone process for cooling 100 with cooling or liquefaction process material flow or unstripped gas.Process for cooling 100 adopts heat exchanger 200 and MCR compression unit 300, and this heat exchanger 200 contains two or more heat exchange zones, three districts as shown in Figure 2.Flow of feed gas 102 is cooled by blending constituent cooling agent (mixed component refrigerant (" MCR ")) in heat exchanger 200.Although not shown, other process stream that need cool off can enter heat exchanger 200.The non-limitative example of other stream like this comprise other cooling agent stream, will in the operation stage of back with other hydrocarbon streams of air-flow 102 blending, and the stream of integrating with one or more classification treatment step.
[0036] composition of flow of feed gas 102 depends on that it stores the source, but for example can comprise in mole and can reach 99% methane, can reach 15% ethane, can reach 10% propane and can reach 30% nitrogen in mole in mole in mole.In a specific embodiments, flow of feed gas 102 can comprise the methane of at least 55 moles of % of by volume or at least 65 moles of % or at least 75 moles of %.In another embodiment, flow of feed gas 102 can also comprise in mole and can reach 1%, maybe can reach 2% and maybe can reach 5% non-hydrocarbons compound, for example water, carbon dioxide, sulfur-containing compound, mercury with and combination.In one or more specific embodiments, can carry out the purifying step (not shown) to feed stream 102, with before entering heat exchanger 200 from flow of feed gas 102 stripping (strip) or otherwise remove most these non-hydrocarbons compounds, if not whole words of these non-hydrocarbons compounds.
[0037] in certain embodiments, flow of feed gas 102 from low 15 ℃ or 25 ℃ or 35 ℃ in the temperature range of high 40 ℃ or 45 ℃ or 55 ℃ and from low by 4,000kPa or 6,000kPa or 7,000kPa is to from high by 8,500kPa or 10,000kPa or 12 enters heat exchanger 200 in the pressure limit of 000kPa.Flow of feed gas 102 withdraws from heat exchanger 200 as the stream 104 that has cooled off.The stream 104 that has cooled off is withdrawing from heat exchanger 200 from low-70 ℃ or-80 ℃ or-100 ℃ to high-60 ℃ or-50 ℃ or under-35 ℃ the temperature range.
MCR
[0038] blending constituent cooling agent (mixed component regrigerant (" MCR ")) mixture of ethane, propane and iso-butane preferably.MCR can contain in the ethane between the mole about 20% to about 80%, in the propane between the mole about 10% to about 90% with in the iso-butane between the mole about 5% to about 30%.In one or more specific embodiments, in a MCR concentration range of ethane for from mole low 20% or 30% or 40% to high by 60% or 70% or 80%.In one or more specific embodiments, in MCR the concentration range of propane for from mole low 10% or 20% or 30% to high by 70% or 80% or 90%.In one or more specific embodiments, in MCR the concentration range of iso-butane for from mole low 3% or 5% or 10% to high by 20% or 25% or 30%.
[0039] in one or more specific embodiments, MCR has about 32 to about 45 molecular weight.More preferably, the molecular weight ranges of MCR is to high by 42 or 43 or 45 from low 32 or 34 or 35.Further, the molar ratio range of MCR and flow of feed gas 102 is to high by 1.8 or 2.0 or 2.2 from low 1.0 or 1.2 or 1.5.In one or more specific embodiments, the mol ratio of MCR and flow of feed gas 102 is at least 1.0 or at least 1.2 or at least 1.5.
Heat exchanger
[0040] consider heat exchanger 200 in more detail, MCR enters heat exchanger 200 as stream 202.At least a portion stream 202 is withdrawn from from first heat exchange zone of heat exchanger 200 as effluent 203.Use expansion gear 205 to make effluent 203 expand into first pressure, produce two phase flow 207 (stream that promptly contains vapor phase and liquid phase).In one or more specific embodiments, this first pressure limit is low 800kpa or 1, and 200kpa or 1,500kpa be to high by 1,900kpa or 2,200kpa or 2,600kpa.Therefore, the temperature range of the stream 207 through expanding is low 0 ℃ or 3 ℃ or 4 ℃ to high 6 ℃ or 10 ℃ or 15 ℃.Preferably, make effluent 203 expand into 1,600kpa to 1, the temperature of the pressure of 800kpa and 4 ℃ to 6 ℃.
[0041] then, two phase flow 207 is separated in separator 210, produces vapor stream 214 and liquid stream 212.Preferably, two phase flow 207 is carried out flash separation.Heat exchanger 200 is passed through in vapor stream 214 bypasses, and is directly sent into compression unit 300.By making vapor stream 214 directly be sent into compression unit 300 (that is, making coolant vapours pass through compression unit), can avoid top pointed some distribution problem relevant with the two-phase cooling agent around the heat exchange zone bypass around heat exchanger 200.
[0042] after being depressurized and therefore being cooled, liquid stream 212 returns heat exchange zone 200, and in this heat exchange zone 200, because the heat exchange in heat exchanger 200, liquid stream 212 is evaporated wholly or in part.This evaporates fully or the stream of part evaporation withdraws from heat exchanger 200 as stream 216.In one or more specific embodiments, stream 216 has at least 85% or by weight at least 90% or by weight at least 99% steam component by weight, and surplus is a liquid phase component.In one or more specific embodiments, stream 216 is the vapor streams (i.e. vaporization fully) that do not contain liquid phase.Stream 216 can be as shown in Figure 1 and vapor stream 214 combinations from separator 210, forms the circular flow 218 that flow to compression unit 300.
[0043] will be at least another part stream 202 withdraw from from second heat exchange zone of heat exchanger 200 as effluent 213.Use expansion gear 215 to make effluent 213 expand into second pressure, produce stream 217.Stream 217 contains vapor phase and liquid phase.In one or more specific embodiments, this second pressure limit is that low 250kpa or 400kpa or 500kpa are to high 600kpa or 700kpa or 850kpa.Therefore, the temperature range of the stream 217 through expanding is that low-60 ℃ or-50 ℃ or-40 ℃ are to high-30 ℃ or-20 ℃ or-10 ℃.Preferably, make effluent 213 expand into 550kpa to the pressure of 570kpa and-35 ℃ to-45 ℃ temperature.
[0044] then, two phase flow 217 is separated in separator 220, produces vapor stream 224 and liquid stream 222.Preferably, two phase flow 217 is carried out flash separation.Heat exchanger 200 is passed through in vapor stream 224 bypasses, and is directly sent into compression unit 300.The liquid stream 222 that is depressurized and therefore is cooled returns heat exchange zone 200, and in this heat exchange zone 200, because the heat exchange in heat exchanger 200, liquid stream 222 is evaporated wholly or in part.This evaporates fully or the stream of part evaporation withdraws from heat exchanger 200 as stream 226.In one or more specific embodiments, stream 226 has at least 85% or by weight at least 90% or by weight at least 99% steam component by weight, and surplus is a liquid phase component.Stream 226 can be as shown in Figure 1 and vapor stream 224 combinations from separator 220, forms the circular flow 228 that flow to compression unit 300.
[0045] still another part stream 202 is withdrawn from from the 3rd heat exchange zone of heat exchanger 200 as effluent 223.Use expansion gear 225 to make effluent 223 expand into the 3rd pressure, produce the stream 227 that contains vapor phase and liquid phase.In one or more specific embodiments, the 3rd pressure limit is that low 80kpa or 120kpa or 150kpa are to high 180kpa or 200kpa or 250kpa.Therefore, the temperature range of the stream 227 through expanding is that low-110 ℃ or-90 ℃ or-80 ℃ are to high-60 ℃ or-50 ℃ or-30 ℃.Preferably, make effluent 223 expand into 160kpa to the pressure of 180kpa and-65 ℃ to-75 ℃ temperature.
[0046] then, two phase flow 227 is separated in separator 230, produces flash streams 234 and saturated liquid stream 232.Preferably, two phase flow 227 is carried out flash separation.Heat exchanger 200 is passed through in vapor stream 234 bypasses, and is directly sent into compression unit 300.The saturated liquid stream 232 that is depressurized and therefore is cooled returns heat exchange zone 200, and in this heat exchange zone 200, because the heat exchange in heat exchanger 200, liquid stream 232 is evaporated wholly or in part.This evaporates fully or the stream of part evaporation withdraws from heat exchanger 200 as stream 236.In one or more specific embodiments, stream 236 has at least 85% or by weight at least 90% or by weight at least 99% steam component by weight, and surplus is a liquid phase component.Stream 236 can be as shown in Figure 2 and vapor stream 234 combinations from separator 230, forms the circular flow 238 that flow to compression unit 300.
[0047] in one or more above-mentioned specific embodiments, expansion gear can be any decompressor.Illustrative expansion gear includes, but are not limited to valve, control valve, joule Thomsons valve, Venturi, fluid expansion reservoir, the hydraulic turbine and similar device.Preferably, expansion gear the 205,215, the 225th, self-driven expansion valve or joule Thomsons valve.
[0048] as mentioned above, heat exchanger 200 is passed through in vapor stream 214,224,234 bypasses, and is directly sent into compression unit 300.This bypass structure has been avoided relevant with the two-phase cooling agent as explained above distribution problem.And the part vaporization cooling agent that contains two-phase that withdraws from heat exchange zone is set (configurate) for reducing the mechanical stress in the heat exchange zone.Mechanical stress may be the product along the fast temperature transformation of shared volume of liquid phase and the shared volume of vapor phase.Temperature transition from the volume of liquid or two-phase fluid part to the volume of vapor phase part can cause stress fracture when startup, shut-down or mal-operation, maybe can cause the fatigue failure of interchanger.Therefore, set the ANALYSIS OF COOLANT FLOW condition, make incomplete vaporization coolant liquid stream 212,222 and 232 and the intrinsic effect of the mechanical stress that rapid temperature gradient causes do not occur.System for the system transition that cooling agent is vaporized fully becomes cooling agent partly to be vaporized can improve flow velocity, changes steam pressure, changes the cooling agent composition and more has more high boiling component to comprise, the perhaps combination of any of these design parameter.
MCR compression unit 300
[0049] MCR compression unit 300 comprises the stress level that one or more are different.Preferably, the suction of each compression stage is corresponding to the stress level of circular flow 218,228,238.In at least one specific embodiments, first compression stage comprises suction separation container 310 (suction knock-out vessel) and compressor 320.In at least one specific embodiments, second compression stage comprises suction separation container 330, compressor 340 and discharging cooler 350.In at least one specific embodiments, the 3rd compression stage comprises suction separation container 360, compressor 370 and discharging cooler 380.In at least one specific embodiments, compression unit 300 further comprises final cooler or condenser 390.
[0050] cooler 350,380 and 390 can be to be fit to the heat exchanger of any kind of described process conditions herein.Illustrative heat exchanger includes, but are not limited to shell-and-tube interchanger, core still formula interchanger (core-in-kettle exchanger) and brazed aluminum radiating fin heat exchanger.In one or more specific embodiments, factory's cooling water is used as heat transfer medium, with process for cooling fluid in cooler 350,380 and 390.In one or more specific embodiments, air is used as heat transfer medium, with process for cooling fluid in cooler 350,380 and 390.And in one or more above-mentioned embodiment, the flash streams 214,224,234 that bypass is passed through makes cooling agent stream 216,226,236 coolings to the small part vaporization of withdrawing from heat exchanger 200.Similarly, the stream 218,228,238 of combination of suction inlet that is recycled to compression unit 300 is lower on temperature, and has therefore reduced the load request of discharging cooler 350,380 and 390.
[0051] more specifically with reference to first compression stage, stream 322 withdraws from the phase I 320.In one or more specific embodiments, stream 322 pressure limit is to high 600kpa or 700kpa or 800kpa from low 200kpa or 300kpa or 400kpa.Stream 322 temperature range is to high 20 ℃ or 25 ℃ or 30 ℃ from low 5 ℃ or 10 ℃ or 15 ℃.
[0052] with reference to second compression stage, stream 342 withdraws from second stage 340 and is cooled in discharging cooler 350, with output stream 352.In one or more specific embodiments, stream 342 pressure limit be from low 800kpa or 1, and 200kpa or 1,400kpa arrive high by 1,800kpa or 2,000kpa or 2,500kpa.In one or more specific embodiments, stream 352 temperature range is to high 40 ℃ or 45 ℃ or 55 ℃ from low 15 ℃ or 25 ℃ or 35 ℃.
[0053] with reference to the 3rd compression stage, stream 372 withdraws from the phase III 370 and is cooled in discharging cooler 380, with output stream 382.In one or more specific embodiments, stream 372 pressure limit be from low by 1, and 600kpa or 2,400kpa or 2,900kpa arrive high by 3,500kpa or 4,000kpa or 5,000kpa.Stream 372 temperature range is to high 100 ℃ or 120 ℃ or 150 ℃ from low 40 ℃ or 50 ℃ or 60 ℃.In one or more specific embodiments, stream 382 temperature range is to high 40 ℃ or 50 ℃ or 60 ℃ from low 0 ℃ or 10 ℃ or 20 ℃.
[0054] in one or more some embodiment, stream 382 flows to condenser 390, produces stream 392.Stream 392 temperature range is to high 40 ℃ or 45 ℃ or 55 ℃ from low 0 ℃ or 10 ℃ or 20 ℃.In one or more some embodiment, when high pressure liquid refrigerant entered heat exchanger 200 as stream 202, stream 392 flow to buffer container 295, to consider to provide the time of staying from operability.
Fig. 3
[0055] cooling or liquefaction process 100 can further adopt second heat exchanger 400 and the 2nd MCR compression unit 500, as shown in Figure 3.Process for cooling has been described in Fig. 3 diagram, and described process for cooling uses two kinds of blending constituent cooling agents in independent heat exchanger, so that cooling or liquefaction process material flow and unstripped gas.Yet first heat exchanger 200 and second heat exchanger 400 can be contained in the common unit.Which kind of situation no matter, first heat exchanger 200 and second heat exchanger 400 all preferably are arranged in series, as shown.
[0056] stream 104 through cooling that leaves first heat exchanger 200 passes through the second blending constituent cooling agent (" the 2nd MCR ") by cold excessively in second heat exchanger 400.Stream 104 through cooling withdraws from second heat exchanger 400 as fluidized flow 106.In certain embodiments, fluidized flow 106 in scope for withdrawing from heat exchanger 400 from low-220 ℃ or-180 ℃ or-160 ℃ to high-130 ℃ or-110 ℃ or under-70 ℃ the temperature.In a specific embodiments, fluidized flow 106 is withdrawing from heat exchanger 400 under about-145 ℃ to about-155 ℃ temperature.In certain embodiments, fluidized flow 106 is from low by 3 in scope, and 900kpa or 5,800kpa or 6,900kpa be to high by 9,000kpa or 10, and 000kpa or 12 withdraws from heat exchanger 400 under the pressure of 000kpa.
The 2nd MCR
[0057] in one or more specific embodiments, the second blending constituent cooling agent (" the 2nd MCR ") can be identical with the first blending constituent cooling agent (" MCR ").In one or more specific embodiments, the 2nd MCR can be different.For example, the 2nd MCR can be the mixture of nitrogen, methane and ethane.In one or more specific embodiments, the 2nd MCR can comprise in the nitrogen between mole about 5% and 20%, in the methane between mole about 20% and 80% with in the ethane between mole about 10% and 60%.In one or more specific embodiments, the concentration range of the nitrogen among the 2nd MCR in mole from low 5% or 6% or 7% to high by 15% or 18% or 20%.In one or more specific embodiments, the concentration range of the methane among the 2nd MCR in mole from low 20% or 30% or 40% to high by 60% or 70% or 80%.In one or more specific embodiments, the concentration range of the ethane among the 2nd MCR in mole from low 10% or 15% or 20% to high by 45% or 55% or 60%.
The molecular weight ranges of [0058] the 2nd MCR is to high by 25 or 26 or 27 from low 18 or 19 or 20.In one or more specific embodiments, the molecular weight of the 2nd MCR is about 18 to about 27.Further, the 2nd MCR and the molar ratio range of stream 104 through cooling are to high by 0.8 or 0.9 or 1.0 from low 0.5 or 0.6 or 0.7.In one or more specific embodiments, the mol ratio of the 2nd MCR and the stream 104 through cooling off is at least 0.5 or at least 0.6 or at least 0.7.
[0059] the 2nd MCR can be fed to first heat exchanger 200 by flowing 402, with pre-cooled before entering second heat exchanger 400 or condensation the 2nd MCR.Stream 402 in first heat exchanger 200 by being cooled with a MCR indirect heat transfer.Stream 402 has the pressure of scope from low 2900kpa or 4300kpa or 5500kpa to high 6400kpa or 7500kpa or 9000kpa.Stream 402 has scope from low 0 ℃ or 10 ℃ or 20 ℃ to high 40 ℃ or 50 ℃ or 70 ℃ temperature.
[0060] the 2nd MCR withdraws from first heat exchanger 200 as stream 404.In one or more specific embodiments, stream 402 is become not contain the liquid stream 404 of steam component by total condensation in first heat exchanger 200.In one or more specific embodiments, stream 402 by with a MCR indirect heat transfer by partial condensation, make stream 404 have at least 85% or by weight at least 90% or by weight at least 95% or by weight at least 99% liquid component by weight.In one or more specific embodiments, stream 404 has scope from low by 2, and 500kpa or 4,000kpa or 5,000kpa be to high by 6,000kpa or 7,000kpa or 9, the pressure of 000kpa.In one or more specific embodiments, stream 404 has scope from low-110 ℃ or-90 ℃ or-80 ℃ to high-60 ℃ or-50 ℃ or-30 ℃ temperature.
[0061] in one or more specific embodiments, the process stream of other that need cool off can enter heat exchanger 400.The non-limitative example of other stream like this comprise other cooling agent stream, other will in post-processing stages with the hydrocarbon stream of stream 102 blending and the stream of integrating with one or more classification treatment step.
Second heat exchanger
[0062] considers second heat exchanger 400 in more detail, in buffer container 406, collect the 2nd MCR, and it is fed in second heat exchanger 400 as stream 410, wherein said the 2nd MCR has been cooled in first heat exchanger 200 and at least by partial condensation, if not by whole words of condensations.The 2nd MCR withdraws from second heat exchanger 400 as stream 415.In one or more specific embodiments, stream 415 has scope from low by 2, and 800kpa or 4,200kpa or 5,500kpa be to high by 6,200kpa or 7,000kpa or 8, the pressure of 500kpa.In one or more specific embodiments, stream 415 has scope from low-230 ℃ or-190 ℃ or-170 ℃ to high-140 ℃ or-120 ℃ or-70 ℃ temperature.
[0063] in one or more specific embodiments, use expansion gear 450 makes stream 415 decompressions (promptly expanding) of withdrawing from second heat exchanger 400.Then, use expansion gear 420 to make further decompression of stream 415, to produce stream 425.Reach as mentioned above, expansion gear 420,450 can be any decompressor, includes but not limited to valve, control valve, joule Thomsons valve, Venturi, fluid expansion reservoir, the hydraulic turbine and similar device.Preferably, expansion gear 420 is self-driven expansion valve or joule Thomsons valve.Preferably, expansion gear 450 is the fluid expansion reservoir or the hydraulic turbine.In one or more specific embodiments, stream 425 has the pressure of scope from low 200kpa or 300kpa or 400kpa to high 500kpa or 600kpa or 700kpa; Has scope from low-250 ℃ or-200 ℃ or-170 ℃ to high-140 ℃ or-110 ℃ or-70 ℃ temperature.Preferably, make stream 425 expand into the temperature of pressure from 435kpa to 445kpa and-150 ℃ to-160 ℃.
[0064] after the isenthalpic expansion in expansion gear 420, stream 425 is vaporized in second heat exchanger 400 fully or part is vaporized and withdraw from second heat exchanger 400 as stream 430.In one or more specific embodiments, stream 425 is vaporized under single stress level in second heat exchanger 400 or the part vaporization fully.In one or more specific embodiments, stream 425 is quilt vaporization (promptly all being vapor phase) fully under first stress level in second heat exchanger 400.In one or more specific embodiments, the single stress levels in second heat exchanger 400 are maintained at from low 150kpa or 250kpa or 350kpa in the scope of high 400kpa or 500kpa or 600kpa.Preferably, the single stress level in second heat exchanger 400 is between about 350kpa and the about 450kpa.
The 2nd MCR compression unit
[0065] then, stream 430 is admitted to second compression unit 500.According to technological requirement, compression unit 500 can comprise one or more compression step.In one or more specific embodiments, compression unit 500 comprises two compression stages, as shown in Figure 3.For example, compression unit 500 has first compression stage 510 and second compression stage 520.
[0066] in the operation, stream 430 is flowed through and is sucked separation container 510A, and wherein vapor stream lasts till first compression stage 510 and is cooled in aftercooler 515, obtains flowing 512.In one or more specific embodiments, stream 512 has scope from low by 1, and 900kpa or 2,800kpa or 3,500kpa be to high by 4,000kpa or 4,800kpa or 5, the pressure of 800kpa; And has scope from low 15 ℃ or 25 ℃ or 30 ℃ to high 40 ℃ or 50 ℃ or 60 ℃ temperature.
[0067] stream 512 is flowed through and is sucked separation container 520A, and wherein vapor stream lasts till second compression stage 520 and is cooled.In more a plurality of embodiments, the vapor stream 522 that leaves second compression stage 520 has scope from low by 2, and 900kpa or 4,300kpa or 5,200kpa be to high by 6,400kpa or 7,500kpa or 9, the pressure of 000kpa; And has scope from low 15 ℃ or 25 ℃ or 35 ℃ to high 40 ℃ or 45 ℃ or 60 ℃ temperature.Subsequently, vapor stream 522 is cooled in aftercooler 525, and is recycled to first heat exchanger 200 as stream 402.
Fig. 4
[0068] Fig. 4 diagram has described to use the another kind of method of liquid coolant gathering system process for cooling material flow or unstripped gas.As shown in Figure 4, the liquid coolant from separator 510A and 520B collection can have fluid to transmit with pump 530.Pump 530 turns back in the technology this liquid coolant by flowing 532.This makes a kind of processing effective (effective) and efficient (efficient) mode of the blending constituent cooling agent of part vaporization in heat exchange zone become possibility.Alternatively, the liquid coolant from separator 510A and 510B collection can be discharged from and remove.Similarly, although not shown, the knock-out drum of compression unit 300 (for example drum 310,330 and 360) can be equipped with similar liquid coolant gathering system.

Claims (66)

1. the method for liquefied natural gas stream comprises:
In containing the heat exchange zone of process stream, place the blending constituent cooling agent;
Under one or more stress level, separate described blending constituent cooling agent, to produce coolant vapours and coolant liquid;
Described coolant vapours is passed through around described heat exchange zone bypass, enter compression unit;
Make described coolant liquid by described heat exchange zone;
The part described coolant liquid of vaporizing in described heat exchange zone is to keep liquid phase.
2. the described method of claim 1, wherein said heat exchange zone is comprised in the single heat exchanger.
3. the described method of claim 1, wherein said heat exchange zone is comprised in two or more heat exchangers.
4. the described method of claim 1, wherein said heat exchange zone comprise two or more and are included in district in the single heat exchanger.
5. the described method of claim 1, wherein said heat exchange zone comprises two or more districts, and wherein each district is comprised in the single heat exchanger.
6. the described method of claim 1, wherein said heat exchange zone comprise two or more and are included in district in two or more heat exchangers.
7. the described method of claim 1, wherein said material process flow is made up of natural gas basically.
8. the described method of claim 1, the wherein said first blending constituent cooling agent comprises ethane, propane and iso-butane.
9. the described method of claim 1, the wherein said first blending constituent cooling agent comprises ethane and propane.
10. the described method of claim 1, the wherein said first blending constituent cooling agent comprises methane, ethane and nitrogen.
11. the described method of claim 1 is wherein separated described blending constituent cooling agent and is comprised and make described blending constituent cooling agent expand into about 80kpa to about 2, the pressure between the 600kpa.
12. the described method of claim 1 is wherein separated described blending constituent cooling agent and is comprised and make described blending constituent cooling agent expand into about 250kpa to about 2, the pressure between the 200kpa.
13. the described method of claim 1 is wherein separated described blending constituent cooling agent and is comprised and make described blending constituent cooling agent expand into about 500 kpa to about 1, the pressure between the 900kpa.
14. the described method of claim 1, wherein separate described blending constituent cooling agent and comprise that the first that makes described blending constituent cooling agent expand into about 1,500kpa is to about 1, first pressure between the 900kpa, and make the second portion of described blending constituent cooling agent expand into about 500kpa to second pressure between about 700kpa.
15. the described method of claim 1 is wherein separated described blending constituent cooling agent and is comprised that the first that makes described blending constituent cooling agent expand into about 800kpa to about 2, first pressure between the 600kpa; Make the second portion of described blending constituent cooling agent expand into about 250kpa to second pressure between about 850kpa; And the third part that makes described blending constituent cooling agent expand into about 80kpa to the 3rd pressure between about 250kpa.
16. the method for liquefied natural gas stream comprises:
In containing the heat exchange zone of process stream, place the blending constituent cooling agent;
Withdraw from two strands or the effluent of the described blending constituent cooling agent of multiply more from described heat exchange zone;
The effluent that separates described blending constituent cooling agent under one or more stress level is to produce coolant vapours and coolant liquid;
Described coolant vapours is passed through around described heat exchange zone bypass, enter compression unit;
Make described coolant liquid by described heat exchange zone; With
The part described coolant liquid of vaporizing in described heat exchange zone is to keep liquid phase.
17. the described method of claim 16 is wherein separated described blending constituent cooling agent and is comprised that the effluent that makes described blending constituent cooling agent expand into about 80kpa to about 2, the pressure between the 600kpa.
18. the described method of claim 16, wherein separate described blending constituent cooling agent comprise the swollen effluent of described blending constituent cooling agent is expanded arrive to about 250kpa about 2, the pressure between the 200kpa.
19. the described method of claim 16, wherein separating described blending constituent cooling agent comprises and makes first effluent of described blending constituent cooling agent expand into about 1,500kpa is to about 1, first pressure between the 900kpa, and make second effluent of described blending constituent cooling agent expand into about 500kpa to second pressure between about 700kpa.
20. the described method of claim 16 is wherein separated described blending constituent cooling agent and is comprised that first effluent that makes described blending constituent cooling agent expand into about 800kpa to about 2, first pressure between the 600kpa; Make second effluent of described blending constituent cooling agent expand into about 250kpa to second pressure between about 850kpa; And the 3rd effluent that makes described blending constituent cooling agent expand into about 80kpa to the 3rd pressure between about 250kpa.
21. the described method of claim 16, the wherein said first blending constituent cooling agent comprises ethane, propane and iso-butane.
22. the described method of claim 16, the wherein said first blending constituent cooling agent comprises ethane and propane.
23. the described method of claim 16, the wherein said first blending constituent cooling agent comprises methane, ethane and nitrogen.
24. the described method of claim 1, the described coolant liquid of wherein partly vaporizing in described heat exchange zone has kept at least 1% liquid component by weight.
25. the described method of claim 24 is wherein separated described blending constituent cooling agent and is comprised and make described blending constituent cooling agent expand into the pressure of about 80kpa between about 180kpa.
26. the described method of claim 24 is wherein separated described blending constituent cooling agent and is comprised and make described blending constituent cooling agent expand into the pressure of about 250kpa between about 600kpa.
27. the described method of claim 24 is wherein separated described blending constituent cooling agent and is comprised and make described blending constituent cooling agent expand into the pressure of about 800kpa between about 1900kpa.
28. the described method of claim 24, wherein separate described blending constituent cooling agent and comprise that the first that makes described blending constituent cooling agent expand into about 1,200kpa is to about 2, first pressure between the 200kpa, and make the second portion of described blending constituent cooling agent expand into about 400kpa to second pressure between about 700kpa.
29. the described method of claim 24, wherein separating described blending constituent cooling agent, to comprise that the first that makes described blending constituent cooling agent expand into about 1, and 500kpa is to about 1, first pressure between the 900kpa; Make the second portion of described blending constituent cooling agent expand into about 500kpa to second pressure between about 600kpa; And the third part that makes described blending constituent cooling agent expand into about 150kpa to the 3rd pressure between about 180kpa.
30. the described method of claim 24, wherein vaporize described coolant liquid of part produces the two-phase cooling agent that contains by weight at least 1% liquid component.
31. the described method of claim 24 wherein produces the two-phase cooling agent that contains by weight at least 3% liquid component to vaporize described coolant liquid of small part.
32. the described method of claim 24, wherein said material process flow is made up of natural gas basically.
33. the described method of claim 24, the wherein said first blending constituent cooling agent comprises ethane, propane and iso-butane.
34. the described method of claim 24, the wherein said first blending constituent cooling agent comprises ethane and propane.
35. the described method of claim 24, the wherein said first blending constituent cooling agent comprises methane, ethane and nitrogen.
36. the method for liquefied natural gas stream comprises:
In containing first heat exchange zone of process stream, place the first blending constituent cooling agent;
Under one or more stress level, separate the described first blending constituent cooling agent, to produce coolant vapours stream and coolant liquid stream;
Described coolant vapours stream is passed through around the described first heat exchanging region bypass, enter compression unit;
Make described coolant liquid stream by described first heat exchange zone, to cool off described process stream; With
In second heat exchange zone that contains process stream, place the second blending constituent cooling agent, with the described process stream that liquefies through cooling off.
37. the described method of claim 36 further is included in the described coolant liquid stream of partly vaporizing in described first heat exchange zone, to keep at least 1% liquid component by weight.
38. the described method of claim 36 further is included in the described second blending constituent cooling agent of partly vaporizing in described second heat exchange zone, to keep at least 1% liquid component by weight.
39. the described method of claim 36 is wherein separated the described first blending constituent cooling agent and comprised that the described first blending constituent cooling agent is expand into is about 1,200kpa is to about 2, the pressure between the 200kpa.
40. the described method of claim 36 is wherein separated the described first blending constituent cooling agent and is comprised and make the described first blending constituent cooling agent expand into the pressure of about 400kpa between about 700kpa.
41. the described method of claim 36 is wherein separated the described first blending constituent cooling agent and is comprised and make the described first blending constituent cooling agent expand into the pressure of about 120kpa between about 200kpa.
42. the described method of claim 36, wherein separate the described first blending constituent cooling agent and comprise that the first that makes the described first blending constituent cooling agent expand into about 1,500kpa is to about 1, first pressure between the 900kpa, and make the second portion of the described first blending constituent cooling agent expand into about 500kpa to second pressure between about 600kpa.
43. the described method of claim 36, wherein separating the described first blending constituent cooling agent, to comprise that the first that makes the described first blending constituent cooling agent expand into about 1, and 500kpa is to first pressure between about 1,900 kpa; Make the second portion of the described first blending constituent cooling agent expand into about 500kpa to second pressure between about 600kpa; And the third part that makes the described first blending constituent cooling agent expand into about 150kpa to the 3rd pressure between about 180kpa.
44. the described method of claim 36, wherein said material process flow is made up of natural gas basically.
45. the described method of claim 36, the wherein said first blending constituent cooling agent comprises ethane, propane and iso-butane.
46. the described method of claim 36, the wherein said first blending constituent cooling agent comprises ethane and propane.
47. the described method of claim 36, the wherein said second blending constituent cooling agent comprises methane, ethane and nitrogen.
48. the method for liquefied natural gas stream comprises:
In containing first heat exchange zone of process stream, place the first blending constituent cooling agent;
Under one or more stress level, separate described blending constituent cooling agent, to produce coolant vapours stream and coolant liquid stream;
Described coolant vapours stream is passed through around the described first heat exchanging region bypass, enter compression unit;
Make described coolant liquid stream turn back to described first heat exchange zone, to cool off described air-flow;
In second heat exchange zone that contains process stream, place the second blending constituent cooling agent through cooling off; With
The described second blending constituent cooling agent of vaporization under single stress level is with the described air-flow that liquefies.
49. the described method of claim 48 further is included in the described coolant liquid stream of partly vaporizing in described first heat exchange zone, to keep at least 1% liquid component by weight.
50. the described method of claim 48 further is included in the described second blending constituent cooling agent of partly vaporizing in described second heat exchange zone, to keep at least 1% liquid component by weight.
51. the described method of claim 48 is wherein separated the described first blending constituent cooling agent and comprised that the described first blending constituent cooling agent is expand into is about 1,200kpa is to about 2, the pressure between the 200kpa.
52. the described method of claim 48 is wherein separated the described first blending constituent cooling agent and is comprised and make the described first blending constituent cooling agent expand into the pressure of about 400kpa between about 700kpa.
53. the described method of claim 48 is wherein separated the described first blending constituent cooling agent and is comprised and make the described first blending constituent cooling agent expand into the pressure of about 120kpa between about 200kpa.
54. the described method of claim 48, wherein separate the described first blending constituent cooling agent and comprise that the first that makes the described first blending constituent cooling agent expand into about 1,500kpa is to about 1, first pressure between the 900kpa, and make the second portion of the described first blending constituent cooling agent expand into about 500kpa to second pressure between about 600kpa.
55. the described method of claim 48, wherein separating the described first blending constituent cooling agent, to comprise that the first that makes the described first blending constituent cooling agent expand into about 1, and 500kpa is to about 1, first pressure between the 900kpa; Make the second portion of the described first blending constituent cooling agent expand into about 500kpa to second pressure between about 600kpa; And the third part that makes the described first blending constituent cooling agent expand into about 150kpa to the 3rd pressure between about 180kpa.
56. the described method of claim 48, wherein the described second blending constituent cooling agent of vaporization comprises by the described second blending constituent cooling agent of decompressor flash distillation under single stress level, the pressure in reaching from 200kpa to the 700kpa scope.
57. the described method of claim 48, wherein the described second blending constituent cooling agent of vaporization comprises by the described second blending constituent cooling agent of valve flash distillation under single stress level, the pressure in reaching from 400kpa to the 500kpa scope.
58. the described method of claim 48, the wherein said second blending constituent cooling agent in described first heat exchange zone by being cooled with the described first blending constituent cooling agent heat exchange.
59. the described method of claim 48, the wherein said second blending constituent cooling agent in described first heat exchange zone by being condensed with the described first blending constituent cooling agent heat exchange.
60. the described method of claim 48, wherein said material process flow is made up of natural gas basically.
61. the described method of claim 48, the wherein said first blending constituent cooling agent comprises ethane, propane and iso-butane.
62. the described method of claim 48, the wherein said first blending constituent cooling agent comprises ethane and propane.
63. the described method of claim 48, the wherein said second blending constituent cooling agent comprises methane, ethane and nitrogen.
64. the method for cooled natural gas process flow comprises:
Make blending constituent cooling agent stream and process stream carry out heat exchange, described cooling agent stream comprises liquid coolant; With
Ended heat exchange before the vaporization fully in described liquid coolant flow.
65. the method for liquefied natural gas stream comprises:
In containing the heat exchange zone of process stream, place the blending constituent cooling agent;
Under one or more stress level, separate described blending constituent cooling agent, to produce coolant vapours and coolant liquid;
At least make described coolant liquid by described heat exchange zone; With
The part described coolant liquid of vaporizing in described heat exchange zone is to keep liquid phase.
66. the method for liquefied natural gas stream comprises:
In containing the heat exchange zone of process stream, place the blending constituent cooling agent;
Withdraw from two strands or the effluent of the described blending constituent cooling agent of multiply more from described heat exchange zone;
The effluent that separates described blending constituent cooling agent under one or more stress level is to produce coolant vapours and coolant liquid;
At least make described coolant liquid pass through heat exchange zone; With
The part coolant liquid of vaporizing in described heat exchange zone is to keep liquid phase.
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