CN107850264B - 处理lng导入终端处的液化天然气流的方法和系统 - Google Patents

处理lng导入终端处的液化天然气流的方法和系统 Download PDF

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Publication number
CN107850264B
CN107850264B CN201680043373.4A CN201680043373A CN107850264B CN 107850264 B CN107850264 B CN 107850264B CN 201680043373 A CN201680043373 A CN 201680043373A CN 107850264 B CN107850264 B CN 107850264B
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natural gas
liquefied natural
stream
gas stream
flow
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CN107850264A (zh
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M·F·达布科夫斯基
L·J·A·M·范坎彭
P·A·维加佩雷斯
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
    • F17C7/02—Discharging liquefied gases
    • F17C7/04—Discharging liquefied gases with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/007—Primary atmospheric gases, mixtures thereof
    • F25J1/0072—Nitrogen
    • 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
    • F25J1/02—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
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    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
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    • F17C2205/00—Vessel construction, in particular mounting arrangements, attachments or identifications means
    • F17C2205/03—Fluid connections, filters, valves, closure means or other attachments
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    • F17C2205/0323—Valves
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C2221/00—Handled fluid, in particular type of fluid
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    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/033—Small pressure, e.g. for liquefied gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/035—High pressure (>10 bar)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
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    • F17C2223/042—Localisation of the removal point
    • F17C2223/043—Localisation of the removal point in the gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
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    • F17C2223/042—Localisation of the removal point
    • F17C2223/046—Localisation of the removal point in the liquid
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Abstract

本发明涉及一种处理LNG导入终端处的液化天然气流的方法。所述方法包括操作气化单元以获得加压的气化天然气流，以及操作灌浆单元以获得液体和固体的浆料以及冷却的气相。所述方法进一步包括从所述灌浆器抽取所述冷却的气相以提供冷却的蒸气流，以及将所述冷却的蒸气流传送到所述气化单元。

Description

处理LNG导入终端处的液化天然气流的方法和系统
技术领域
本发明涉及一种处理液化天然气流的方法和系统。
背景技术
当导入天然气作为液化天然气(LNG)时，在进入市场之前需要对LNG进行再气化。建构LNG导入终端或再气化终端以在供应到气体供应网之前将液化天然气转化回到加压的气相。
同时，对使液体形式的LNG可供终端用户使用的需求日益增加，例如作为运输燃料(例如，汽车、卡车、轮船)。用户购买液体形式的LNG并将其储存于燃油箱中。LNG在使用前(例如)在汽车内部经再气化。
液化天然气的缺点是由于热量进入会产生蒸发气体。在无间歇的压力控制措施的情况下，蒸发气体限制了液体天然气可储存于(例如)燃油箱内部的时间量。
替代液化LNG，可产生包括浆料或浆料LNG的甲烷，浆料为固体和液体天然气的混合物。制备包括浆料或浆料LNG的甲烷的方法为已知的。
浆料LNG的优点是，只要存在固体天然气颗粒，则产生较少蒸发气体或不产生蒸发气体。并且，浆料LNG的密度高于液化天然气的密度，从而允许在给定容量(例如燃油箱)中储存及运输更多分子。
日本专利文献JP2003314954描述其中固体LNG和液体LNG经混合的浆料LNG制造方法。液氮罐安装在液化天然气罐中，且通过固化液化天然气获得的固体物质产生于液氮罐的表面的热交换面上，且通过螺丝钻刮除以与液化天然气混合。JP2003314954的缺点是，其需要大量且复杂的硬件(旋转/移动设备)，这也使得难以按比例增加此程序。此外，需要氮制冷剂的额外的制冷循环，其需要相对较大量的冷却能量。
NBS报告9758，C.f.Sindt等人的Slush and boiling methane characterisation(美国商务部(U.S.Department of Commerce)，国家标准局(National Bureau ofStandards)，基本标准学会(Institute for basic standards)，Boulder、Colorado 80302(1970年7月1日))描述了一种用于制造浆料LNG的实验性分批制造设备。浆料LNG的分批生产不适用于持续的制造方法中。
EP1876404A1描述一种用于制造氮浆料的设备。US 4,009,013描述一种用于制备低沸点气体(例如氮气或氢气)的细粒度浆料的方法。
US2013139544提供一种用于优化液化天然气储存罐中的蒸发气体的再冷凝的系统和方法。
目标为提供一种接收液化天然气流的方法和系统，且使其可以有效方式供市场使用。
发明内容
本发明提供一种处理液化天然气流的方法，所述方法包括
a)通过以下步骤来操作气化单元(A)：
-提供来自一或多个储存罐(1)的第一液化天然气流(10)，
-对所述第一液化天然气流(10)进行加压以提供加压的液化天然气流(12)，
-对所述加压的液化天然气流(12)进行气化以获得加压的气化天然气流(14)，
b)通过以下步骤来操作灌浆单元(B)：
-提供来自所述一或多个储存罐(1)的第二液化天然气流(20)，
-将所述第二液化天然气流(20)传送到其中所述第二液化天然气流(20)被冷却且减压到所述液化天然气流(20)的三相点状态的灌浆器(21)，以获得液体和固体的浆料(22)以及冷却的气相(23)，
-从所述灌浆器(21)抽取所述冷却的气相(23)以提供冷却的蒸气流(24)，以及
-将所述冷却的蒸气流(24)传送到所述气化单元(A)。
根据另一方面，提供一种处理液化天然气流的系统，所述系统包括气化单元(A)，其中所述气化单元(A)包括
-加压器单元(11)，配置成从一或多个储存罐(1)接收第一液化天然气流(10)并产生加压的液化天然气流(12)，
-气化器(13)，配置成接收所述加压的液化天然气流(12)并产生加压的气化天然气流(14)，
其中所述系统进一步包括灌浆单元(B)，其中所述灌浆单元(B)包括
-灌浆器(21)，配置成从一或多个储存罐(1)接收第二液化天然气流(20)并产生液体和固体的浆料(22)以及冷却的蒸气流(24)，
其中所述气化单元(A)与所述灌浆单元(B)流体连通以接收所述冷却的蒸气流(24)的至少一部分。
所述一或多个储存罐可为所述系统的一部分或可与所述系统分离。
气化单元(A)与灌浆单元(B)之间的液体连通可由配置成传送冷却的蒸气流的一或多条管线(例如导管或套管)来提供。
灌浆单元(B)可包括浆料容器和膨胀冷却装置，例如，一或多个平行的节流阀或膨胀阀或一或多个平行的喷射嘴(27)，其中所述膨胀冷却装置定位于所述第二液化天然气流(20)到所述浆料容器的流动路径中。
根据另一方面，提供一种由上述方法或系统获得的液体和固体的浆料，其中所述浆料为固体和液体天然气的混合物。
因此，所述浆料包括固体和液体天然气的混合物，所述固体主要包括甲烷，且所述液体主要包括甲烷。
所述液化天然气流以及液体和固体的浆料主要由甲烷构成，即，至少50mol％的甲烷，典型地至少75mol％的甲烷。
所述液化天然气流以及液体和固体的浆料可进一步包括更重的碳，例如乙烷、丙烷、异丁烷、异戊烷。典型地，较重的烃类组分的摩尔份数小于较轻的烃类组分的摩尔份数。
液化天然气流以及液体和固体的浆料可进一步包括小部分的氮。
视实际的组合物而定，液化天然气流具有独特的三相点压力和三相点温度。本领域技术人员将能够确定给定组合物的精确的三相点压力和三相点温度。针对100％甲烷，三相点状态在0.11688巴下为-182.47℃(90.68K)。
附图说明
将在下文使用实例并且关于附图进一步说明本发明，在附图中；
图1示意性地示出一实施例，
图2示意性地示出一替代实施例，以及
图3示意性地示出另一替代实施例。
在这些图中，相同参考标号将用以指代相同或类似部件。此外，单个参考标号将用以识别导管或管线以及所述管线传送的气流。
具体实施方式
本发明提出提供气化单元以再汽化或再气化液化天然气流，以及灌浆单元以从液化天然气制备固体和液体的浆料或混合物，其中所述气化单元和灌浆单元并行动作，其中在气化单元与灌浆单元之间提供一定的整合。
此方法提供处理液化天然气的有效方式，并且为市场制备液化天然气。第一部分经再气化且制备以传送到气体供应网中，同时第二部分经灌浆且使其可通过卡车或驳船进一步运输或用作燃料(例如用于运输)。通过整合气化和灌浆，可以相对有效的方式实现灌浆，这是由于抽取的冷却的蒸气流可与气化单元合并，例如可与来自储存罐的蒸发气流合并。
图1示出示意性地示出气化单元A和灌浆单元B的实施例。进一步示出储存罐1，其在使用时包括液化天然气。液化天然气在约-160℃的温度下可在大体上大气压力(即，在0到250毫巴的范围内，例如，150毫巴)下储存。液化天然气还可在更高压力(例如大于2巴、大于10巴或甚至大于12巴的压力)和更高温度下储存。根据一实例，第一压力可为15巴。在此压力下，包括流的液体甲烷的温度可为-115℃。
在下文所描述的实施例中，假定液化天然气在大体上大气压力下(即在大气压力的15％内)储存于储存罐中。
第一液化天然气流10和第二液化天然气流20自储存罐1获得。
可使用储存罐或其下游设置的一或多个泵抽装置5完成自储存罐1获得第一液化天然气流10和第二液化天然气流20。通常可在范围为4到14巴(例如12巴)的压力下提供第一液化天然气流10和第二液化天然气流20。
如图1中所示，首先，可使用一或多个泵抽装置5自储存罐1获得主要液化天然气流6，且通过对主要液化天然气流6进行分流(例如通过使用分离器或T接头7等)来获得第一液化天然气流10和第二液化天然气流20。
第一液化天然气流10和第二液化天然气流20的压力可在5到15巴(例如13巴)的范围内。
分离器7可为配置成控制第二液化天然气流20的流速的可控分离器或T接头7。替代地，第一和或第二液化天然气流的流速可由定位于分离器或T接头下游的适当的阀门(图示为阀门70，下文更详细讨论)来控制。
在使用期间可控制、尤其是主动地控制及恒定地或规律地调整第一液化天然气流10与第二液化天然气流20之间的分流比。分流比可定义为第二液化天然气流20的流速除以第一液化天然气流10和第二液化天然气流20的总和。
分流比可在0到0.50或0到0.25的范围内。
根据一实施例，所述分流比可为控制成等于第一值或等于第二值的二进制，所述第一值小于第二值。第一值可与不需要或较少需要浆料的情况相关联。第一值可为零或接近零以防止灌浆单元的管道升温。第二值可与对浆料的高需求相关联，且可在0.01到0.5或0.01到0.25的范围内。
在不需要浆料或在储存装置中存在足量浆料的情况下，分流比可为0。
所述分流比可另外或替代地受流量控制器FC的影响，所述流量控制器响应于在灌浆器中测量的参数来调整阀门70的设置，所述参数例如灌浆器内部的浆料的水平、温度、压力、固相率、灌浆器中产生的浆料的黏度。
气化单元A配置成接收来自一或多个储存罐1的第一液化天然气流10，且对第一液化天然气流10加压以提供加压的液化天然气流12。气化单元A包括加压器单元11，例如泵。加压器单元11包括接收第一液化天然气流10的入口，以及排放加压的液化天然气流12的出口。
具体地说，在参考图1所描述的实施例中，加压器单元11和泵抽装置5可包含于单个装置中。
气化单元A进一步配置成接收加压的液化天然气流12以获得加压的气化天然气流14。气化单元A包括气化器13，所述气化器13包括接收来自加压器单元11的加压的液化天然气流12的入口以及排放加压的气化天然气流14的出口。
气化器13包括热交换器，其中加压的液化天然气流12可与加热介质(例如环境水或空气)交换热量。气化器13的实例可(例如)发现于WO2013186271、WO2013186275、WO2013186277以及WO2008012286中。
加压的气化天然气流14通常具有接近环境温度的温度以及高于50巴(例如高于65巴，例如80巴)的压力。
随后将加压的气化天然气流14传送到气体供应网60。
气化单元可包括控制器，所述控制器控制传送到气体供应网60的加压的气化天然气流14(或下文描述的合并的天然气流14')的压力、流速(能量、质量、体积)中的一或多个。借助于实例，图1示出流量控制器FC1，流量控制器FC1(例如)通过控制可控制阀门111响应于气化天然气流14的所测量参数来控制朝向气化器的流速。
灌浆单元B配置成接收来自一或多个储存罐1的第二液化天然气流20。
可使用不同类型的罐浆单元B。
典型地，灌浆单元B包括灌浆器，所述灌浆器产生固体和液体天然气与冷却的气相23的混合物，尤其是可泵送的混合物。抽取冷却的气相23以提供传送到气化单元A的冷却的气流24。通过此方式整合气化单元A和灌浆单元B。
将在下文描述合适的灌浆单元B。
灌浆单元B包括灌浆器，其包括具有接收第二液化天然气流20的入口的浆料容器21。所述灌浆器配置成将第二液化天然气流20的压力减少至约三相点压力以形成浆料，所述浆料为固体和液体天然气的混合物，尤其是可泵送的混合物。
任选地，如图1中所示，可通过过冷却热交换器80传送第二液化天然气流20，其中第二液化天然气流20在进入浆料容器21之前经过冷却。所述方法可因此包括
-对所述第二液化天然气流20进行过冷却以获得过冷却的第二液化天然气流20'，
-将所述过冷却的第二液化天然气流20'传送到所述浆料容器21，其中所述第二液化天然气流20进一步冷却且减压到三相点状态。
所述灌浆器可包括过冷却热交换器80，且过冷却所述第二液化天然气流20包括：
-通过所述过冷却热交换器80传送第二液化天然气流20。
过冷却热交换器80包括配置成接收第二液化天然气流20的入口81，以及与浆料容器21的入口流体连通以排放过冷却的第二液化天然气流20的出口82。
过冷却热交换器80进一步可包括制冷剂流动路径83、84，合适的过冷却制冷剂可流经所述制冷剂流动路径83、84以向第二液化天然气流20提供冷却功率。
合适的过冷却制冷剂可流经制冷剂流动路径83、84，其中使用过冷却制冷剂循环对所述第二液化天然气流20进行过冷却，其中使过冷却制冷剂(例如氮)循环。过冷却制冷剂循环可通过对加压的液化天然气流12进行气化来获得冷却功率以在气化器13中获得加压的气化天然气流14。
实际上，过冷却的第二液化天然气流可具有低于第二天然气流20的沸点且高于第二天然气流20的三相点温度的温度。
应理解，还可在描述的其它实施例(尤其是参考图2和图3描述的实施例)中采用过冷却。
所述灌浆器可将第二(过冷却)液化天然气流20冷却并减压到第二液化天然气流20的约三相点状态以获得液体和固体的浆料22以及冷却的气相23。这通过将(过冷却的)第二液化天然气流20(20')传送到在天然气流20的三相点压力处或接近三相点压力处保持在低压的浆料容器21来实现，从而冷却且至少部分地固化及蒸发所述第二液化天然气20。所述蒸发将抽取焓，从而冷却气流的非蒸发部分(自热过程)。连同在将气流引入浆料容器中产生的焦耳汤姆逊(Joule Thompson)效应，获得充足冷却以达到三相点温度。
此冷却及减压可通过将第二液化天然气流20膨胀冷却到浆料容器中来实现。膨胀冷却可经由一或多个平行的节流阀或膨胀阀来实现或可经由一或多个平行的喷射嘴27通过喷射冷却来实现。
将获得将呈现在浆料22上方的冷却的气相23。将通过使用适当的蒸气抽取装置经由导管24从灌浆器21抽取冷却的气相23来获得并维持三相点状态。蒸气抽取装置可为压缩器或泵25或喷射器(图3中所示)，从而获得压缩的蒸气流26。
通过抽取冷却的气相23，可主动控制浆料容器21内部的压力。所述
方法可包括通过适时地改变或循环压力来控制浆料容器21内部的压力，从而控制产生的固相率，且从而控制收集的混合物40中的固相率，且从而确保在浆料容器中产生固体和液体的可泵送混合物。
当控制浆料容器中的压力/温度高于三相点时，不产生固体。当控制浆料容器21中的压力/温度低于三相点时，产生相对较高的固相率。由于在包括浆料的甲烷中的所需固相率可能低于在三相点以下操作产生的固相率，因此浆料容器21中的压力可在高于三相点与低于三相点之间适时地循环，从而获得所需固相率。
以此方式可略微改变第二压力以控制浆料容器中的固相率。
浆料容器21为能够耐受相对于其环境的某一负压的容器，且因此还可被称作真空容器。
将由此获得(压缩)的冷却的蒸气流24 26传送到气化单元(A)。
根据一实施例，所述方法包括
-从一或多个储存罐1获得蒸发气流2。
所述蒸发气流是从一或多个储存罐1获得以防止压力上升。蒸发气流2可由蒸发压缩器3压缩，
所述蒸发压缩器3对蒸发气流2进行压缩以提供压缩的蒸发气流4。
根据其实例示出于图1中的实施例，将冷却的蒸气流24传送到气化单元A包括
-对蒸气流24进行压缩以提供压缩的蒸气流26，
将压缩的蒸气流26与压缩的气化天然气流14进行合并以提供合并的天然气流14'。
压缩的蒸气流26的压力通常远低于压缩的气化天然气流14的压力，因此气化单元A可包括额外的压缩器9，压缩器9配置成接收压缩的蒸气流26以获得进一步压缩的蒸气流15，其压力大体上等于压缩的气化天然气流14的压力，且大体上等于气体供应网60的压力，通常为50巴或更大，例如，80巴。可将合并的气流传送到气体供应网60。
可通过将蒸气流传送通过压缩器25来实现对蒸气流24的压缩以获得压缩的蒸气流26。
根据一实施例，所述方法进一步包括
-对蒸发气流2进行压缩以提供压缩的蒸发气流4，
-将所述压缩的蒸发气流4以及压缩的蒸气流26与加压的气化天然气流(14)进行合并以提供合并的天然气流(14')。
可以不同方式及顺序实现这些气流的合并，例如如图2中所示，其中压缩的蒸气流26首先与压缩的蒸发气流4合并，产生气流8，将气流8传送到另外的压缩器9，所述压缩器9配置成接收压缩的蒸气流26以获得进一步压缩的蒸气流15，随后将蒸气流15与加压的气化天然气流14合并。
可通过将蒸发气流传送通过压缩器3来实现对蒸发气流2的压缩以获得压缩的蒸发气流4。
蒸发气流2可通常具有100毫巴的压力，其中压缩的蒸发气流4具有通常6到10巴(例如8巴)的压力。压缩的蒸气流26可具有大体上等于压缩的蒸发气流4的压力。
这提供合并蒸发气流2以及从灌浆器21获得的蒸气流24的有利方式。
现将参考图2描述另一实施例。
根据此实施例，所述方法包括
-对蒸发气流2进行压缩以提供压缩的蒸发气流4，
-将蒸气再冷凝器进料流31供应到再冷凝器30，所述蒸气再冷凝器进料流31包括所述再压缩的蒸发气流4的至少一部分，
-将液体再冷凝器进料流32传送到再冷凝器30，所述液体再冷凝器进料流32包括从所述第一液体天然气流10获取的侧流32，
-从蒸气再冷凝器进料流31和液体再冷凝器进料流32获得再冷凝流33，
-将再冷凝流33与第一液化天然气流10'的剩余物合并以获得再合并的第一液化天然气流10”。
第一液化天然气流的剩余物为第一液化天然气流的一部分而非侧流32。
第一液化天然气流10'的剩余物的流速可借助于可控制阀门322响应于再冷凝器30下方的所测量液位受液位控制器LC控制。
随后使用加压器单元11对再合并的第一液化天然气流10”进行加压以提供加压的液化天然气流12。
侧流32可绕过再冷凝器30，在此情况下与再冷凝流33的合并发生在再冷凝器的下游。替代地，侧流可传送到再冷凝器30的底部，在此情况下与再冷凝流33的合并发生在再冷凝器的底部部分。
将液体再冷凝器进料流32传送到再冷凝器30可由压力控制器PC来控制，所述压力控制器PC借助于可控制阀门321响应于提供再冷凝器30中的压力指示的压力读数来控制再冷凝器进料流32的流速。
根据一实施例，将冷却的蒸气流24传送到气化单元A包括
-对蒸气流24进行压缩以提供压缩的蒸气流26，
且其中所述蒸气再冷凝器进料流31进一步包括压缩的蒸气流26。
参考图2描述的实施例具有可省略额外的压缩器9的优点。
将参考图3描述另一实施例。
根据一实施例，操作灌浆单元B，尤其是从灌浆器21抽取冷却的气相23以提供冷却的蒸气流24包括：
-将作为动力流的第三液化天然气流20'供应到喷射器40的动力流入口41，
-将冷却的蒸气流24的至少一部分供应到喷射器40的吸入流入口42，
-从喷射器出口43获得喷射器出口流28，以及
-将包括所述动力流的喷射器出口流28以及冷却的蒸气流24传送到所述气化单元A。
所述第三液化天然气流20'可从第二液化天然气流20获得作为侧流，但还可从第一液化天然气流10或直接从一或多个储存罐1获得作为侧流。
喷射器出口流28可以与上文参考图1所解释的类似方式传送到气化单元A，即通过压缩气流且将其与加压的气化天然气流14合并以提供合并的天然气流14'。
动力流的流速可由可控制阀门411来控制，其响应于提供灌浆器的操作状态的指示的测量读数由控制可控制阀门411的压力控制器PC2来控制，所述测量读数例如冷却的蒸气流24的压力、浆料容器21内部的冷却的气相23的压力、固相率、黏度或其组合。
替代地，蒸气再冷凝器进料流31可包括喷射器出口流28。
根据图3中所示的实施例，喷射器出口流28与再冷凝流33或与第一液化天然气流10”再合并。
与再冷凝流33合并可发生在再冷凝器的下游或再冷凝器的底部。
根据一实施例，所述方法进一步包括
-从所述灌浆器21获得浆流50以及-将所述浆流50供应到浆料分配器51。
所述浆料分配器可为喷嘴或适合于将一定量的浆料分配到(燃料)罐52(例如运输装置(例如汽车、轮船或飞机)上的罐)的任何其它装置。所述运输装置可使用浆料作为燃料或可将作为货物的浆料运输到目的地，或两者。
所述汽车可为低温道路卡车，其包括低温罐以将浆料LNG运输到储存浆料LNG的零售站点。
所述容器可为船用储存容器，其装配成移动到远处的海上位置以将浆料燃料提供到其它容器。
将浆流供应到浆料分配器51可包括首先将浆流供应到中间浆料储存容器53(如图1中所示)，且在需要时从所述中间浆料储存容器53将浆流供应到浆料分配器51。
根据一实施例，操作灌浆单元B在不需要浆料时中断或以最低限度持续，且在需要浆料时恢复。根据此实施例，操作灌浆单元B包括选择性地在生产水平及中断水平下操作灌浆单元B之间切换，其中与所述生产水平相关联的第二液化天然气流20的第一流速大于与所述中断水平相关联的第二液化天然气流20的第二流速。第二流速可为零或可为非零以维持通过灌浆单元的最小流动以使管道保持低温。
可仅在需要浆料时完全操作灌浆单元B，例如在存在需要补给燃料或再装载的运输装置时，或当中间浆料储存容器53中存在的浆料的量已下降到预定水平以下时。
当操作灌浆单元B在中断水平处中断或继续时，可继续灌浆单元A的操作。
所属领域的技术人员将理解，在不脱离所附权利要求书的范围的情况下，可以多种不同方式实施本发明。

Claims (18)

1.一种处理液化天然气流的方法，所述方法包括
a)通过以下步骤来操作气化单元(A)：
提供来自一或多个储存罐(1)的第一液化天然气流(10)，
对所述第一液化天然气流(10)进行加压以提供加压的液化天然气流(12)，
对所述加压的液化天然气流(12)进行气化以获得加压的气化天然气流(14)，
b)通过以下步骤来操作灌浆单元(B)：
提供来自所述一或多个储存罐(1)的第二液化天然气流(20)，
将所述第二液化天然气流(20)传送到其中所述第二液化天然气流(20)被冷却且减压到所述液化天然气流(20)的三相点状态的灌浆器(21)，以获得液体和固体的浆料(22)以及冷却的气相(23)，
从所述灌浆器(21)抽取所述冷却的气相(23)以提供冷却的蒸气流(24)，以及
将所述冷却的蒸气流(24)传送到所述气化单元(A)。
2.根据权利要求1所述的方法，其中所述方法包括
从所述一或多个储存罐(1)获得蒸发气流(2)。
3.根据权利要求2所述的方法，其中将所述冷却的蒸气流(24)传送到所述气化单元(A)包括
对所述蒸气流(24)进行压缩以提供压缩的蒸气流(26)，
将所述压缩的蒸气流(26)与所述压缩的气化天然气流(14)进行合并以提供合并的天然气流(14')。
4.根据权利要求3所述的方法，其中所述方法进一步包括
对所述蒸发气流(2)进行压缩以提供压缩的蒸发气流(4)，
将所述压缩的蒸发气流(4)以及所述压缩的蒸气流(26)与所述压缩的气化天然气流(14)进行合并以提供合并的天然气流(14')。
5.根据权利要求2所述的方法，其中所述方法包括
对所述蒸发气流(2)进行压缩以提供压缩的蒸发气流(4)，
将蒸气再冷凝器进料流(31)供应到再冷凝器(30)，所述蒸气再冷凝器进料流(31)包括所述压缩的蒸发气流(4)的至少一部分，
将液体再冷凝器进料流(32)传送到所述再冷凝器(30)，所述液体再冷凝器进料流(32)包括从所述第一液化天然气流(10)获取的侧流(32)，
从所述蒸气再冷凝器进料流(31)和所述液体再冷凝器进料流(32)获得再冷凝流(33)，
将所述再冷凝流(33)与所述第一液化天然气流(10')的剩余物合并以获得再合并的第一液化天然气流(10”)。
6.根据权利要求5所述的方法，其中将所述冷却的蒸气流(24)传送到所述气化单元(A)包括
对所述蒸气流(24)进行压缩以提供压缩的蒸气流(26)，
且其中所述蒸气再冷凝器进料流(31)进一步包括所述压缩的蒸气流(26)。
7.根据权利要求6所述的方法，其中操作所述灌浆单元(B)包括：
将作为动力流的第三液化天然气流(20')供应到喷射器(40)的动力流入口(41)，
将所述冷却的蒸气流(24)的至少一部分供应到所述喷射器(40)的吸入流入口(42)，
从喷射器出口(43)获得喷射器出口流(28)，以及
将包括所述动力流的所述喷射器出口流(28)以及所述冷却的蒸气流(24)传送到所述气化单元(A)。
8.根据权利要求7所述的方法，其中所述蒸气再冷凝器进料流(31)包括所述喷射器出口流(28)。
9.根据权利要求7所述的方法，其中所述喷射器出口流(28)与所述再冷凝流(33)或与所述第一液化天然气流(10”)再合并。
10.根据前述权利要求1-9中任一项所述的方法，其中所述方法进一步包括
从所述灌浆器(21)获得浆流(50)以及
将所述浆流(50)供应到浆料分配器(51)。
11.根据前述权利要求1-9中任一项所述的方法，其中所述方法包括对所述第二液化天然气流(20)进行过冷却以获得过冷却的第二液化天然气流(20')，
将所述过冷却的第二液化天然气流(20')传送到所述浆料容器(21)，其中所述第二液化天然气流(20)进一步冷却且减压到三相点状态。
12.根据权利要求11所述的方法，其中所述灌浆器包括过冷器热交换器(80)，且对所述第二液化天然气流(20)进行过冷却包括：
通过所述过冷却热交换器(80)传送所述第二液化天然气流(20)。
13.根据权利要求11所述的方法，其中使用过冷却制冷剂循环对所述第二液化天然气流(20)进行过冷却。
14.根据前述权利要求1-9中任一项所述的方法，其中操作所述灌浆单元(B)包括选择性地在生产水平及中断水平下操作所述灌浆单元(B)之间切换，其中与所述生产水平相关联的所述第二液化天然气流(20)的第一流速大于与所述中断水平相关联的所述第二液化天然气流(20)的第二流速。
15.一种用于处理液化天然气流的系统，所述系统包括气化单元(A)，其中所述气化单元(A)包括
加压器单元(11)，配置成从一或多个储存罐(1)接收第一液化天然气流(10)并产生加压的液化天然气流(12)，
气化器(13)，配置成接收所述加压的液化天然气流(12)并产生加压的气化天然气流(14)，
其中所述系统进一步包括灌浆单元(B)，其中所述灌浆单元(B)包括
灌浆器(21)，配置成从一或多个储存罐(1)接收第二液化天然气流(20)并产生液体和固体的浆料(22)以及冷却的蒸气流(24)，
其中所述气化单元(A)与所述灌浆单元(B)流体连通以接收所述冷却的蒸气流(24)的至少一部分。
16.根据权利要求15所述的系统，其中所述灌浆单元(B)包括浆料容器和膨胀冷却装置，其中所述膨胀冷却装置定位于所述第二液化天然气流(20)到所述浆料容器的流动路径中。
17.根据权利要求16所述的系统，其中所述膨胀冷却装置为一或多个平行的节流阀或膨胀阀或一或多个平行的喷射嘴(27)。
18.一种由权利要求1-14中任一项的方法或由根据权利要求15-16中任一项所述的系统获得的液体和固体的浆料，其中所述浆料是固体和液体天然气的混合物。
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