CN1768241B - 用于提供加压气体的方法和设备 - Google Patents
用于提供加压气体的方法和设备 Download PDFInfo
- Publication number
- CN1768241B CN1768241B CN2004800084980A CN200480008498A CN1768241B CN 1768241 B CN1768241 B CN 1768241B CN 2004800084980 A CN2004800084980 A CN 2004800084980A CN 200480008498 A CN200480008498 A CN 200480008498A CN 1768241 B CN1768241 B CN 1768241B
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- CN
- China
- Prior art keywords
- storage facility
- cryogenic
- heat exchanger
- separation unit
- cryogenic liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000009434 installation Methods 0.000 title description 2
- 239000007788 liquid Substances 0.000 claims abstract description 127
- 238000000926 separation method Methods 0.000 claims abstract description 66
- 238000002309 gasification Methods 0.000 claims description 17
- 238000011144 upstream manufacturing Methods 0.000 claims description 16
- 239000000284 extract Substances 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 9
- 238000000746 purification Methods 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims 1
- 238000009834 vaporization Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 27
- 239000001301 oxygen Substances 0.000 description 24
- 229910052760 oxygen Inorganic materials 0.000 description 24
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 23
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 9
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000005086 pumping Methods 0.000 description 6
- 238000002955 isolation Methods 0.000 description 4
- 229910052786 argon Inorganic materials 0.000 description 3
- 210000000038 chest Anatomy 0.000 description 3
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 230000010355 oscillation Effects 0.000 description 1
- 150000002926 oxygen Chemical class 0.000 description 1
- 229940063746 oxygen 20 % Drugs 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
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- F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
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Abstract
本发明涉及一种用于通过使来自至少两个低温分离单元(A,B,C,D)的低温液体气化而提供加压气体的方法。每个单元都包括热交换器(1)和塔系统(2,3)。在第一工作模式下,从每个低温分离单元中的塔抽取低温液体,对该低温液体的至少一部分加压(7,8)以提供加压的低温液体(9),并在热交换器(1)中使该加压低温液体的至少一部分气化,以提供部分加压气体(10)。将低温液体从该低温分离单元输送(6)到共用贮存装置(12),并且在所述低温分离单元的至少一个的热交换管路(1)中使至少一种来自该贮存装置的液体(28A、28B、28C、28D)气化。
Description
技术领域
本发明涉及一种用于提供至少一种加压气体的方法和设备,尤其是用于从由低温贮存装置支持的低温分离单元(例如用ASU表示的空气分离单元)向用户提供气态产品(氮、氧、氩)的方法和设备。本发明还涉及提供其它低温液体例如氢、氦和一氧化碳的设备。
本发明尤其涉及由多个工业设备提供气体的方法。
背景技术
EP-A-0452177中示出一种应急/急救气化器,其中来自贮存装置的液态氮在热交换器中通过与周围空气热交换而气化。
EP-A-0628778公开了一种低温液体贮存装置,液体从该贮存装置泵送出,然后在输送给用户之前在气化器中气化。
文章“Large Oxygen Plant Economics and Reliability”,W.J.Scharle,Bulletin Y-143,National Fertilizer Division Centre,Tennessee ValleyAuthority,Muscle Shoals,Ala.以及“Oxygen Facilities for Synthetic FuelProjects”,W.J.Scharle and K.Wilson,Journal of Engineering forIndustry,November 1981,Vol.103,pp.409-417,说明了用于应急氧生产的系统,该系统主要包括:
·包含一定量液态产品的贮存装置,
·多个泵(为了可靠,有两个),其抽取该贮存装置中容纳的液体,以将其压缩到通常输送给用户的压力(管路中的压力),
·用于使该受压液体气化的热交换器。
在这些辅助单元的出口,气体(的温度)通常接近环境温度,并且气体被输送给用户。根据现场可用的能源及其成本,热交换器可将例如空气、蒸汽、热水和燃烧废气用作热源以使受压液体气化。
这些应急设备的一个主要特征是它们的启动时间。该启动时间尤其重要,因为其决定对用户的气体供给的品质和连续性。在启动该生产单元之后的过长的启动时间会在管路中产生非常大的压降,并且在用户的处理过程中发生故障以及导致设备停工。
在上面的文章所述的氧生产系统的情况下,提供气态氧缓冲容器,以在启动泵所必需的时间(根据上文提到的W.J.Scharle的文章,大约15-20分钟)内提供加压产品。
通常,如果将气化泵持久地保持在低温下,则该应急系统达到其稳定状态下的全容量/负荷(full capacity)所必需的时间是大约5分钟,该时间分成用于泵启动的1-2分钟以及用于热交换器气化的起始(ramp-up)的2-3分钟。合理地选择各种元件(在泵和贮存装置之间以及泵和热交换器之间的短管道)的结构和设置,能够使此时间缩短为大约3分钟。在某些情况下,对于管路中允许的压力波动限制,3分钟的时间间隔仍过长:此时,如上所述,一种技术方案是在热交换器(例如在200巴下)的下游安装气体缓冲容器,其尺寸设计成可提供1-3分钟的产品供给,此时间是泵-气化器系统达到其正常工作状态所需的时间。这种技术方案的缺陷是其价格高(安装体积大、压力高、用于填充该缓冲容器的泵)。本发明的一个目的是避免使用这种昂贵的即时启用(immediate-resumption)系统。当必须由多个低温分离单元提供加压气体时,会发生特别的问题。对于大的项目,例如,需要四个或五个空气分离单元,每个分离单元都使用例如两个液态氧泵或单个液态氧泵,该泵可能发生故障。为了获得可接受的适用性(availability),必须在每个单元上安装一个备用泵,这意味着泵的数量很多。本发明的另一个目的是避免(使用)过多的泵,而获得的适用性与通过在每个单元上设置备用泵获得的适用性相当。可进行这样的安排,即在来自每个单元的液体被泵送和重新分配给该单元以便在每个单元的热交换管路中气化之前,可将来自每个单元的所有液体输送到一共用贮存装置。但是,在这种情况下,如果一个单元的纯度降低,则该单元不能与其它单元隔离开,并且其生产不能与其它单元的生产分开。如果一个单元的低温液体生产受到污染,则防止污染该贮存装置(该贮存装置还用于提供散货市场中的LOX(液氧),其纯度可能不仅仅由气体使用者确定)以及整个生产是很重要的。本发明的另一个目的是,在一个单元的纯度降低的情况下,能够使该单元与贮存装置隔离开,从而防止污染该贮存装置,并且根据用户的需求,继续或停止由该单元进行的生产,而其它单元进行的生产不受影响。
发明内容
根据本发明的一个方面,提出了一种用于通过使来自至少两个低温分离单元的低温液体气化而提供加压气体的方法,每个单元都包括热交换器和塔系统,其中,在每个单元中:
a)在热交换器中冷却加压并净化的气体混合物以产生加压、净化及冷却的气体混合物;
b)在塔系统中分离该加压、净化及冷却的气体混合物;
c)从该塔系统中抽取低温液体,并且在第一工作模式下,在该热交换器中使第一部分加压低温液体气化以提供部分加压气体,以及
d)由每个单元提供加压气体,或者混合来自该低温分离单元的加压气体,
其中,
e)根据第一工作模式,将来自各低温分离单元的第二部分低温液体输送到一贮存装置,以及
f)根据第一工作模式,将来自该贮存装置的低温液体输送到各热交换器以使得该液体在该热交换器中气化。
优选地,根据第一工作模式,等量的液体进入和离开所述贮存装置,从而该贮存装置中的液面基本恒定。
根据本发明的其它特定方面:
-对于每个低温分离单元,在贮存装置的上游没有对第二部分低温液体加压,和/或在热交换器的上游对第一部分低温液体加压;
-在第一工作模式下,将来自贮存装置的低温液体输送到至少一个低温分离单元的热交换器,优选地输送到至少两个低温分离单元的热交换器,并且在该热交换器或这些热交换器中使该低温液体气化以提供部分加压气体;
-在共用贮存装置的下游和热交换器的上游对低温液体加压;
-在一低温分离单元停止工作的情况下,则根据第二工作模式,共用贮存装置优选地在加压步骤之后供给一共用气化器,在该共用气化器中,来自共用贮存装置的低温液体通过与加热流体进行热交换而气化,以提供全部或部分加压气体;
-在共用气化器中气化的低温液体仅来自共用贮存装置;
-在每个低温分离单元中,用于分离的全部气体混合物在热交换器中通过与来自塔系统的至少一种气体和至少一种低温液体进行热交换而冷却;
-通过至少一个泵对第一部分低温液体加压,并且根据第三工作模式,在一低温分离单元的至少一个泵停止运转的情况下,为了补偿由于该泵停止运转而导致的加压液体的损失,相对于在该停止运转的泵运转时的流量增加输送到贮存装置的第二部分低温液体,并且在该单元的一个泵保持正常运转状态的情况下,相对于该停止运转的泵运转时的流量增加来自塔系统并输送到该低温分离单元的热交换器的低温液体的流量:
-在一低温分离单元的至少一个泵停止运转的情况下,对于其泵正在运转的至少一个其它空气分离单元,相对于该停止运转的泵运转时的流量增加第一部分低温液体,并且对于其泵正在运转的至少一个其它空气分离单元,相对于该停止运转的泵运转时的流量减少输送到贮存装置的第二部分低温液体;
-在一低温分离单元停止工作的情况下,对于至少一个保持工作状态的低温分离单元,相对于该停止工作的单元工作时的流量减少从至少一个低温分离单元输送到共用贮存装置的第二部分低温液体,优选地减少至为零,并相对于该(停止工作的)单元工作时的流量增加输送到热交换器的第一部分低温液体;
-只有在至少一个低温分离单元停止工作的情况下,才将低温液体从贮存装置输送到共用气化器。
如果相同的加压装置用于对来自贮存装置且将在至少一个低温分离单元的热交换器内气化的液体以及来自贮存装置且将在气化器中气化的液体加压,则这些加压装置可持久地工作,因为它们在分离单元正常工作(第一工作模式,使直接或间接输送到热交换器的液体气化)和停止工作(第二工作模式,使液体在气化器中气化以代替由至少一个分离单元生成的气体)时都起作用。
根据本发明的另一目的,提出了一种用于通过使来自至少两个低温分离单元的低温液体气化而提供加压气体的设备,每个单元都包括热交换器和塔系统,每个单元中包括:
a)用于将加压并净化/提纯的气体混合物输送到热交换器以产生加压、净化及冷却的气体混合物的装置;
b)用于将该加压、净化及冷却的气体混合物输送到塔系统的装置;
c)用于从塔系统抽取低温液体的装置,和将该至少第一部分加压低温液体输送到热交换器以提供部分加压气体的装置;
d)用于提供加压气体的装置;
并且,还包括一共用贮存装置和用于将来自低温分离单元的第二部分低温液体输送到该共用贮存装置的装置,和用于将来自该贮存装置的低温液体输送到各低温分离单元的热交换器的装置。
优选地,该设备在塔系统的下游和共用贮存装置的上游不包含任何加压装置。
根据本发明的其它特定方面,该设备可包括:
-在塔系统的下游和热交换器的上游的加压装置,该加压装置优选地具有连接到热交换器和共用贮存装置上的出口和/或连接到塔系统和贮存装置上的入口;
-用于将来自共用贮存装置的低温液体输送到至少一个低温分离单元的热交换器的装置;
-用于在共用贮存装置的下游和热交换器的上游对低温液体加压的装置;
-一共用气化器、用于从共用贮存装置供给该共用气化器的装置、优选地位于共用贮存装置的下游和该共用气化器的上游的加压装置和用于允许加热流体和低温液体在气化器中进行热交换的装置;
-相同的加压装置在共用贮存装置的下游和共用气化器的上游连接并连接到低温分离单元的至少一个热交换器上(通常是每个低温分离单元的热交换器)。
优选地,在共用气化器中气化的低温液体仅从共用贮存装置获得。
对于每个低温分离单元,一低温液体管路可使塔系统与热交换器相连接而不经过共用贮存装置,一低温液体管路可经由共用贮存装置连接塔系统和热交换器。
该设备可包括用于调节从至少一个低温分离单元输送到共用贮存装置的液体的流量的装置,和/或用于调节从该共用贮存装置输送到所述低温分离单元的热交换器的液体的流量的装置。
该设备还可包括用于混合来自至少两个低温分离单元的加压气体以提供加压气体的装置。
该气化器适于允许在低温液体和不进行低温分离的加热流体例如蒸汽或大气之间进行热交换。
根据第一工作模式,对于单个单元,该分离单元产生在热交换器中气化的液体,该液体的一部分被直接输送到该热交换器,而其余部分经由贮存装置输送到该热交换器。
根据第二工作模式,对于单个单元,在该单元不工作的情况下,不再有液体输送到热交换器,并且来自贮存装置的液体供给一气化器,液体在该气化器内气化。
优选地,根据第一工作模式,液体通过至少一个用于直接输送到热交换器的液体的泵以及至少另一个用于来自贮存装置的液体的泵加压。在第二工作模式中,相同的泵或至少另一个泵还用于对输送到气化器的液体加压,从而根据第一和第二工作模式该至少另一个泵持久地工作。
根据第三工作模式,对于单个单元,如果对直接输送到热交换器的液体加压的泵之一不工作,则通过使用保持工作状态的泵对部分液体加压而将该部分液体继续直接输送到热交换器,并将液体的其余部分经由贮存装置输送到热交换器。
共用贮存装置可位于一分离单元的冷箱内。
附图说明
下面将参照附图较详细地说明本发明。
图1和2是根据本发明的装置的实施例的示意图。
具体实施方式
在图1的实施例中,四个空气分离单元A、B、C和D向至少一个共同的用户提供加压氧气。这四个单元基本相同,每个单元都包含主热交换器1A、1B、1C、1D和双塔,该双塔包括中压塔2A、2B、2C、2D和低压塔3A、3B、3C、3D。从每个ASU抽取的液态氧4A、4B、4C、4D的流量基本相同。
由于各单元的操作和配置基本相同,所以此处仅详细说明单个单元A。
加压并净化的空气在热交换器1A中通过与来自低压塔3A的至少一种气体和液态氧4A进行热交换而被冷却。冷却的空气以气态的形式被输送到中压塔2A。部分空气通过与液态氧气化发生热交换而液化,然后被输送给中压塔和/或低压塔。可使用任何已知的装置例如Claude涡轮机和/或鼓风涡轮机(blowing turbine)和/或氮涡轮机(nitrogen turbine)和/或通过液体辅助来使该单元保持冷却。附图中没有示出中压塔和低压塔之间常用的回流升高管路(reflux rise line),也没有示出富氮流体的排出装置。
在所述实施例中,在正常工作模式下,将液态氧4A从低压塔3A中抽入一容器内并分成两部分。第一部分液态氧4A,例如所抽取的流量的80%,由例如两个并行的泵7A、8A压缩,这两个泵的尺寸均有利地为一(泵)列的容量的50%,该列中的每一个(泵)均接纳第一部分液态氧的一半,并且每个泵均在例如其容量的80%下运转,即,在此示例中为分离单元的液态氧容量的40%。显然,这两个泵7A、8A可由这样的单个泵代替,即该单个泵的容量相应地为例如一(泵)列的100%,并对全部第一部分液态氧加压。被泵送的液态氧流经由管路9A输送到热交换器1A,并在该热交换器内气化以形成可输送给用户的加压气体10A。该气体通常与来自其它单元B、C、D的排出气体10B、10C、10D汇合。
构成所抽取的氧的其余部分或在此示例中占20%的第二部分液态氧流经管路5A以汇入通向共用贮存装置12的共用管路6,来自分离单元的氧被贮存在该贮存装置中,该共用管路6同样还由其它ASU供给。该共用管路可由各(泵)列专用的管路代替。
因此,在正常模式下,贮存装置一直由所有(或至少一部分,给出的仅是一个示例)ASU供给,因而,其泵20和22恒定地进行“处理”操作,接近它们的正常状态(regime)。这些泵按照与来自每个ASU的液体相同的比例(在此示例中,从每个ASU抽取液态氧的20%)将液体重新分配给每个ASU。这样,在热交换器1中气化的液体构成所抽取的氧流的100%,其中该氧流的80%直接来自泵7、8,20%经过贮存装置12和泵20、22。从而这些泵20、22在一个ASU停止工作时处于即时启用状态,此时,这些泵马上转到“应急气化”功能(而对于上述操作,它们处于第一工作模式)。
当具有两个并行的氧泵的ASU的一个泵例如泵7A停止运转时,则8A(中氧流)增加至由该ASU抽取的氧流的50%,从该ASU到共用贮存装置12的液态氧输送管路5A(中氧流)上升到从ASU A抽取的氧流的50%,并且其它ASU B、C、D的其它泵(中氧流)都例如(可考虑其它工作点)上升至从各ASU B、C、D抽取的氧流的45%(以泵送所抽取的氧流的90%),并且流经共用贮存装置的来自其它ASU的液体减少为从各ASU抽取的氧流的10%。泵20和22仍处于相同的80%状态,并且由这些泵20和22泵送的液体仍以与从各ASU被抽取的方式相同的方式重新分配,或者在此示例中,从ASU A抽取的氧流的50%分配给具有泵7A的ASU A,向其它ASU中的每一个分配所抽取的氧流的10%。
如果同一单元的所有泵都停止运转,则来自该单元的液体的100%被输送到贮存装置,而其它单元在与贮存装置隔离的“隔离模式”下工作。在另一个单元的一个泵停止运转的情况下,来自每个仅有一个泵在工作的单元的液体的50%被输送,其它单元在隔离模式下工作。然后,用于来自贮存装置的液体的泵在其容量的100%下工作,并且将液体的50%输送给每个仅有一个泵在工作的单元。
位于来自贮存装置12的低温液体的泵20和22的下游的管路24经由管路32连接到气化器34上。该气化器用于通过使该低温液体与加热流体例如空气、蒸汽、热水或燃烧废气进行热交换而使该低温液体气化。
当一ASU停止工作时,其它ASU的泵7和8(中氧流)上升到50%,从而使各ASU与贮存装置“隔离”,不再需要使液体经由管路6流经贮存装置12。然后贮存装置12的泵20和22泵送取自该贮存装置12的储备物的液体14。被泵送的液体在共用气化器34内气化。从而,泵20、22消耗贮存装置中的液体;但是在前述工作模式中,它们仅泵送与来自ASU的液体相同量的液体,因此贮存装置中的液面基本不会降低。泵20、22已经处于(即时启用)状态(并且接近其完全状态)可确保通过共用气化器实际进行即时启用,而不需要另外投资于高压缓冲贮存容器等。
每个空气分离单元优选地具有冷箱,贮存装置位于这些冷箱中的一个内或者自身具有绝热层。
对于未示出的其中空气分离单元具有单个低温液体泵的情况,当该泵停止运转时,所有液体都被输送到共用贮存装置,由泵20、22或一单个泵泵送,并被输送到其泵停止运转的分离单元的热交换器的冷端,以供给该ASU的生产。
图2中的装置包括图1的所有元件,但是不同之处在于:
经由共用管路6输送到共用贮存装置12的液体不是来自将液体输送到专用泵7A、8A的管路4A-4D,而是来自专用管路30A-30D,该管路30A-30D使来自低压塔3A-3D的容器与共用管路6相连接。明显地,管路4A和30A的低温液体基本具有相同的组成。使每个ASU与贮存装置相连接的专用管路可代替共用管路6。
该方法基本上以与图1中所示的方式相同的方式操作。
对于图1和图2中的两个实施例,应理解的是,如果低压塔3在足够高的压力下工作,则泵7、8不是必须的。
被气化和混合以形成加压气体的加压液体可以是氮或氩。
所述塔系统可包括传统的双塔、在低压塔中具有双气化器的双塔或三塔。在至少一个分离单元上还可设置氩塔。
氧气可在分离单元的主热交换管路中气化,或者可在专用热交换器中通过与空气进行热交换而气化。
对于本领域技术人员而言明显的是,在下面的权利要求的框架内可具有其它修改和变型。
Claims (25)
1.用于通过使来自至少两个低温分离单元(A,B,C,D)的低温液体气化而提供加压气体的方法,每个单元都包括热交换器(1)和塔系统(2,3),其中,在每个分离单元中:
a)在所述热交换器中冷却加压并净化的气体混合物以产生加压、净化及冷却的气体混合物;
b)在所述塔系统中分离所述加压、净化及冷却的气体混合物;
c)从所述塔系统抽取低温液体,并且在为正常工作模式的第一工作模式下,在所述热交换器中使第一部分加压低温液体(4,9)气化以提供部分加压气体,以及
d)由每个单元提供加压气体,
其中,根据该第一工作模式:
e)将来自各低温分离单元的第二部分低温液体输送到一共用贮存装置(12),以及
f)将来自所述贮存装置的低温液体输送到各热交换器以使得该液体在该热交换器中气化。
2.根据权利要求1所述的方法,其特征在于,对于每个低温分离单元,在所述贮存装置的上游没有对所述第二部分低温液体加压,和/或在所述热交换器(1)的上游对所述第一部分低温液体加压。
3.根据权利要求1或2所述的方法,其特征在于,在所述第一工作模式下,将来自所述贮存装置(12)的低温液体输送到至少一个低温分离单元(A,B,C,D)的热交换器(1),并且在该热交换器或这些热交换器内使所述低温液体气化以提供一部分加压气体(10)。
4.根据权利要求3所述的方法,其特征在于,在所述共用贮存装置(12)的下游和所述热交换器(1)的上游对所述低温液体加压。
5.根据权利要求1或2所述的方法,其特征在于,根据其中一低温分离单元停止工作的第二工作模式,所述共用贮存装置(12)供给一共用气化器(34),在该共用气化器中,来自所述共用贮存装置的低温液体通过与加热流体进行热交换而气化,以提供全部或部分加压气体。
6.根据权利要求5所述的方法,其特征在于,在所述共用气化器(34)中气化的低温液体仅来自所述共用贮存装置(12)。
7.根据权利要求1或2所述的方法,其特征在于,在每个低温分离单元中,用于分离的全部气体混合物在所述热交换器中通过与来自所述塔系统的至少一种气体和至少一种低温液体进行热交换而冷却。
8.根据权利要求1或2所述的方法,其特征在于,通过至少一个泵(7,8)对所述第一部分低温液体(4,9)加压,并且根据其中一低温分离单元的至少一个泵停止运转的第三工作模式,为了补偿由于该泵停止运转而导致的加压液体的损失,相对于该停止运转的泵运转时的流量增加输送到所述贮存装置(12)的第二部分低温液体,并且在该单元的一个泵保持正常运转状态的情况下,相对于该停止运转的泵运转时的流量增加来自所述塔系统并输送到所述低温分离单元的热交换器(1)的低温液体的流量。
9.根据权利要求8所述的方法,其特征在于,在一低温分离单元(A)的至少一个泵(7,8)停止运转的情况下,对于其泵正在运转的至少一个其它空气分离单元(B,C,D),相对于该停止运转的泵运转时的流量增加第一部分低温液体,并且对于其泵正在工作的至少一个其它空气分离单元(B,C,D),相对于该停止运转的泵运转时的流量减少输送到所述贮存装置的第二部分低温液体。
10.根据权利要求1或2所述的方法,其特征在于,在一低温分离单元(A)停止工作的情况下,对于至少一个保持工作状态的低温分离单元,相对于该停止工作的单元(A)工作时的流量减少从至少一个低温分离单元(B,C,D)输送到所述贮存装置(12)的第二部分低温液体,并且相对于该停止工作的单元(A)工作时的流量增加输送到所述热交换器的第一部分低温液体。
11.根据权利要求5所述的方法,其特征在于,只有在至少一个低温分离单元停止工作的情况下,才将低温液体从所述贮存装置(12)输送到共用气化器(34)。
12.根据权利要求3所述的方法,其特征在于,在所述第一工作模式下,将来自所述贮存装置(12)的低温液体输送到至少两个低温分离单元的热交换器。
13.根据权利要求5所述的方法,其特征在于,所述共用贮存装置(12)在加压步骤之后供给所述共用气化器(34)。
14.根据权利要求10所述的方法,其特征在于,将所述第二部分低温液体减少至零。
15.用于通过使来自至少一个低温分离单元(A,B,C,D)的低温液体气化而提供加压气体的设备,每个单元都包括热交换器(1)和塔系统(2,3),每个低温分离单元中包括:
a)用于将加压并净化的气体混合物输送到所述热交换器以产生加压、净化及冷却的气体混合物的装置;
b)用于将所述加压、净化及冷却的气体混合物输送到所述塔系统的装置;
c)用于从所述塔系统抽取低温液体的装置,和将至少第一部分加压低温液体(4,9)输送到所述热交换器以提供部分加压气体的装置;
d)用于提供加压气体的装置;
所述设备还包括一共用贮存装置(12)和用于将来自低温分离单元的第二部分低温液体(5,30)输送到所述共用贮存装置的装置,以及用于将来自所述贮存装置的低温液体输送到每个低温分离单元的所述热交换器的装置。
16.根据权利要求15所述的设备,其特征在于,该设备在所述塔系统(2,3)的下游和所述共用贮存装置(12)的上游不包含任何加压装置。
17.根据权利要求15或16所述的设备,其特征在于,该设备在所述塔系统的下游和所述热交换器的上游包括加压装置(7,8)。
18.根据权利要求15或16所述的设备,其特征在于,该设备包括用于在所述共用贮存装置的下游和所述热交换器的上游对低温液体加压的装置(20,22)。
19.根据权利要求15或16所述的设备,其特征在于,该设备包括一共用气化器(34)、用于从所述共用贮存装置(12)供给所述共用气化器的装置和用于允许加热流体和低温液体在气化器中进行热交换的装置。
20.根据权利要求19所述的设备,其特征在于,该设备还包括位于所述共用贮存装置的下游和所述共用气化器的上游的加压装置(20,22)。
21.根据权利要求20所述的设备,其特征在于,相同的加压装置(20,22)在所述共用贮存装置(12)的下游和所述共用气化器(34)的上游连接并连接到低温分离单元的至少一个热交换器(1)上。
22.根据权利要求19所述的设备,其特征在于,在所述共用气化器(34)中气化的低温液体仅从所述共用贮存装置(12)获得。
23.根据权利要求15或16所述的设备,其特征在于,对于每个低温分离单元,一低温液体管路(9)使所述塔系统(2,3)与所述热交换器相连接而不经过所述共用贮存装置(12),另一低温液体管路经由所述共用贮存装置连接所述塔系统和所述热交换器。
24.根据权利要求15或16所述的设备,其特征在于,该设备包括用于调节从至少一个或每个低温分离单元输送到所述共用贮存装置的液体的流量的装置,和/或用于调节从所述共用贮存装置输送到所述低温分离单元中的至少一个的热交换器的液体的流量的装置。
25.根据权利要求15所述的设备,其特征在于,该设备包括用于混合来自至少两个低温分离单元的加压气体(10)以提供加压气体的装置。
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FR2814178B1 (fr) * | 2000-09-18 | 2002-10-18 | Air Liquide | Alimentation en air enrichi en oxygene d'une unite de production de metal non-ferreux |
US6357259B1 (en) * | 2000-09-29 | 2002-03-19 | The Boc Group, Inc. | Air separation method to produce gaseous product |
DE10111428A1 (de) * | 2001-03-09 | 2002-09-12 | Linde Ag | Verfahren und Vorrichtung zur Zerlegung eines Gasgemischs mit Notbetrieb |
FR2828729B1 (fr) * | 2001-08-14 | 2003-10-31 | Air Liquide | Installation de production d'oxygene sous haute pression par distillation d'air |
FR2831953B1 (fr) * | 2001-11-05 | 2004-09-24 | Air Liquide | Procede de distillation d'air avec production d'argon et installation de distillation d'air correspondante |
FR2844344B1 (fr) * | 2002-09-11 | 2005-04-08 | Air Liquide | Installation de production de grandes quantites d'oxygene et/ou d'azote |
-
2003
- 2003-04-02 FR FR0304105A patent/FR2853407B1/fr not_active Expired - Fee Related
-
2004
- 2004-03-12 EP EP04720050A patent/EP1613911A1/fr not_active Withdrawn
- 2004-03-12 US US10/551,602 patent/US7444834B2/en not_active Expired - Fee Related
- 2004-03-12 WO PCT/FR2004/050105 patent/WO2004090445A1/fr active Application Filing
- 2004-03-12 KR KR1020057018543A patent/KR101042097B1/ko not_active IP Right Cessation
- 2004-03-12 CN CN2004800084980A patent/CN1768241B/zh not_active Expired - Lifetime
- 2004-03-12 JP JP2006505850A patent/JP2006522307A/ja active Pending
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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CN1108698A (zh) * | 1993-06-07 | 1995-09-20 | 乔治·克劳德方法的研究开发空气股份有限公司 | 为使用空气组分的设备提供加压气体的方法和装置 |
CN1290325A (zh) * | 1998-02-04 | 2001-04-04 | 德士古发展公司 | 带有内设气化器的综合的低温空气分离装置 |
US6128921A (en) * | 1998-02-06 | 2000-10-10 | L'air Liquide | Air distillation plant comprising a plurality of cryogenic distillation units of the same type |
Also Published As
Publication number | Publication date |
---|---|
KR20050119173A (ko) | 2005-12-20 |
US7444834B2 (en) | 2008-11-04 |
CN1768241A (zh) | 2006-05-03 |
JP2006522307A (ja) | 2006-09-28 |
WO2004090445A1 (fr) | 2004-10-21 |
FR2853407A1 (fr) | 2004-10-08 |
FR2853407B1 (fr) | 2012-12-14 |
KR101042097B1 (ko) | 2011-06-16 |
US20070101763A1 (en) | 2007-05-10 |
EP1613911A1 (fr) | 2006-01-11 |
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