CN102216711A - 液态和气态氮物流、富氦气流,和脱氮的碳氢化合物物流的生产方法和相关的设备 - Google Patents
液态和气态氮物流、富氦气流,和脱氮的碳氢化合物物流的生产方法和相关的设备 Download PDFInfo
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- CN102216711A CN102216711A CN2009801460160A CN200980146016A CN102216711A CN 102216711 A CN102216711 A CN 102216711A CN 2009801460160 A CN2009801460160 A CN 2009801460160A CN 200980146016 A CN200980146016 A CN 200980146016A CN 102216711 A CN102216711 A CN 102216711A
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- nitrogen
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 308
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 155
- 239000007788 liquid Substances 0.000 title claims abstract description 47
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 44
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 44
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 42
- 239000001307 helium Substances 0.000 title claims abstract description 36
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 36
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000004519 manufacturing process Methods 0.000 title claims description 19
- 238000001816 cooling Methods 0.000 claims abstract description 85
- 238000000034 method Methods 0.000 claims abstract description 71
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 38
- 238000010992 reflux Methods 0.000 claims abstract description 23
- 238000007906 compression Methods 0.000 claims description 50
- 230000006835 compression Effects 0.000 claims description 44
- 238000005057 refrigeration Methods 0.000 claims description 28
- 239000000284 extract Substances 0.000 claims description 27
- 230000008961 swelling Effects 0.000 claims description 17
- 238000010438 heat treatment Methods 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 12
- 238000009835 boiling Methods 0.000 claims description 11
- 238000005194 fractionation Methods 0.000 claims description 11
- 238000000605 extraction Methods 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 3
- 230000008020 evaporation Effects 0.000 claims description 3
- 150000002829 nitrogen Chemical class 0.000 claims description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 32
- 239000007789 gas Substances 0.000 description 18
- 239000003949 liquefied natural gas Substances 0.000 description 14
- 239000012530 fluid Substances 0.000 description 11
- 239000003345 natural gas Substances 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000000567 combustion gas Substances 0.000 description 3
- 230000006837 decompression Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- 206010061876 Obstruction Diseases 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000005304 joining Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- QGZKDVFQNNGYKY-NJFSPNSNSA-N nitrogen-16 Chemical compound [16NH3] QGZKDVFQNNGYKY-NJFSPNSNSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
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- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Abstract
该方法包括一引入物流(72)在一上游热交换器(28)中的冷却。其包括将冷却的引入物流(76)引入进一分馏塔(50)中和在分馏塔(50)底部提取脱氮的碳氢化合物物流。所述方法包括将来自分馏塔(50)顶部的一富氮物流(106)引入进一分离球(60)中,和回收来自分离球(60)的顶部气流,用于形成富氦物流(20)。来自第一分离球(60)底部的液流(110)被分为一液态氮物流(18)和回流式地被引入进分馏塔(50)顶部的第一回流物流(114)。
Description
技术领域
本发明涉及从包含碳氢化合物、氦气和氮气的装料流开始生产液态氮物流、气态氮物流、富氦气流和脱氮的碳氢化合物物流的一种生产方法。
背景技术
这类方法尤其应用在对由液化天然气(GNL)或气体形式的天然气(GN)组成的装料流的处理。
该方法适用于新型的天然气液化装置或新型的气体形式的天然气的处理装置。本发明还应用于现有装置的性能改进。
在这些设备中,天然气在被运送到消费者之前或在存储或运输之前需要进行脱氮。实际上,从地层中开采的天然气经常包括数量不容忽视的氮气。此外其经常包含氦气。
已知的脱氮方法允许获得一种脱氮的碳氢化合物物流,其可在液化天然气的情形中以液体的形式被运送至存储装置,或在天然气的情形中被运送至气体分配装置。
这些脱氮方法此外产生富氮物流,这些富氮物流要么被使用于提供设备运行所必需的氮气,要么用于提供富氮的可燃气体,这种燃烧气体用于在实施该方法时所使用的压缩机的燃气透平。作为变型,这些富氮物流在杂质,如甲烷被焚尽后从火炬塔中释放进大气。
前述的方法并不完全地令人满意,尤其是由于应用于碳氢化合物生产的新的环境限制。实际上,为了使得通过该方法生产的氮气能够在生产装置中被使用或释放进大气,氮气需要具有很高的纯度。
通过该方法生产和用于在燃气透平中使用的可燃物流相反地需要包含小于15%到30%的氮气,用于在设计的特别烧嘴中燃烧,以限制排放进大气的氮氧化物的生成。这些排放尤其是在用于实施该方法的设备的启动阶段发生,在该阶段脱氮的方法还不是很有效的。
此外,出于经济的原因,这类脱氮方法的能量效率需要持续地进行改进。前述类型的方法并不允许对从地下开采的天然气中包含的氦气进行再利用,可是氦气是一种具有很大经济价值的稀有气体。
为了至少部分地消除这些问题,文献US 2007/0245771描述前述类型的一种方法,其同时生产液态氮物流、富氦物流,和包含大约30%的氮气和大约70%的碳氢化合物的气体流。该富氮的气体流在该设备中用于形成一种可燃物流。
然而该方法并不是完全令人满意的,这是因为产生的纯氮数量相对地少。此外,可燃物流包含很大数量的氮气,这些氮气是不与现存的各种燃气透平相兼容的,并且会产生大量的污染排放。
发明内容
本发明的目的之一在于获得碳氢化合物装料流的一种经济的脱氮方法,其允许对包含在装料流中的氮气和氦气进行再利用,同时至少限制对环境有害的排放。
为此,本发明的对象在于前述类型的一种方法,其包括以下步骤:
-膨胀所述装料流,用于形成一膨胀的装料流;
-将所述膨胀的装料流分成第一引入物流和第二引入物流;
-所述第一引入物流在一上游热交换器内通过与一制冷气流的热交换进行冷却,该制冷气流通过在一制冷循环中动态膨胀地获得,用于获得被冷却的第一引入物流;
-所述第二引入物流经过第一下游热交换器进行冷却,用于形成被冷却的第二引入物流;
-将所述被冷却的第一引入物流和所述被冷却的第二引入物流引入进一分馏塔中,所述分馏塔包括多个理论分馏级;
-提取至少一个重沸物流和使所述重沸物流在所述第一下游热交换器中流通,用于冷却所述第二引入物流;
-在所述分馏塔底部提取一底部物流,用于形成所述脱氮的碳氢化合物物流;
-在所述分馏塔顶部提取一富氮的顶部物流;
-经过至少一个第二下游热交换器对所述富氮的顶部物流进行加热,用于形成一被加热的富氮物流;
-提取和膨胀所述被加热的富氮物流的第一部分,用于形成气态氮物流;
-压缩所述被加热的富氮物流的第二部分,用于形成一压缩的再循环的氮物流,并且,所述压缩的再循环的氮物流按经过所述第一下游交换器和经过所述的或每个的第二下游交换器流动的方式进行冷却;
-液化和局部膨胀所述再循环的氮物流,用于形成一膨胀的富氮物流;
-在第一分离球中引入来自所述膨胀的富氮物流的至少一部分;
-回收来自所述第一分离球的顶部气流,用于形成富氦物流;
-回收来自所述第一分离球底部的液流,并将该液流分成一液态氮物流和第一回流物流;
-在所述分馏塔顶部中按回流方式引入所述第一回流物流。
根据本发明的方法可包括一个或多个以下的特征,单独地或根据技术上所有可能的组合:
-全部的所述膨胀的富氮物流在膨胀后直接地被引入进所述第一分离球中;
-所述膨胀的富氮物流被引入进布置在所述第一分离球上游的第二分离球中,来自所述第二分离球的顶部物流被引入进所述第一分离球中,所述第二分离球的至少一部分底部物流按回流方式被引入进所述分馏塔的顶部中;
-所述第二分离球的底部物流被分成引入进所述分馏塔中的第二回流物流和一冷却补给物流,冷却补给物流在经过所述第二下游热交换器前与所述富氮的顶部物流相混合;
-所述分馏塔的操作压力小于5巴,有利地小于3巴;
-所述制冷循环是反向的布雷顿制冷循环类型的一封闭循环,所述方法包括以下步骤:
●在一循环热交换器中加热所述制冷气流,直到基本等于周围环境温度的一温度;
●压缩所述被加热的制冷气流,用于形成一压缩的制冷气流,并在所述循环热交换器中按与来自所述第一上游热交换器的被加热的制冷气流热交换的方式进行冷却,用于形成一被冷却的压缩制冷气流;
●动态膨胀所述被冷却的压缩制冷气流,用于形成所述制冷气流,并将所述制冷气流引入进所述第一上游热交换器中;
-所述循环热交换器通过下游交换器之一形成,所述压缩的制冷气流在所述下游交换器中按与来自所述分馏塔顶部的富氮顶部物流热交换的方式至少部分地被冷却;
-所述制冷循环是半开放循环,所述方法包括以下步骤:
●提取至少一馏分的所述压缩的循环的富氮物流,所述压缩的循环的富氮物流被压缩到第一压力,用于形成一富氮的提取物流;
●在一循环热交换器中冷却富氮的提取物流,用于形成一被冷却的提取物流;
●动态膨胀来自所述循环热交换器的所述被冷却的提取物流的,用于形成所述制冷气流,并将所述制冷气流引入进所述上游热交换器中;
●在一压缩机中压缩来自所述上游热交换器的制冷气流,并将该物流再引入进所述压缩的再循环的氮物流中,该氮物流被压缩到小于所述第一压力的第二压力;
-所述装料流是一气流,所述方法包括以下步骤:
●液化所述装料流,以按经过一液化热交换器的方式来形成一液态装料流;
●在所述液化热交换器中按与来自所述装料流的一气流进行热交换的方式,对来自所述分馏塔底部的脱氮的碳氢化合物物流进行蒸发;
-通过脱氮的碳氢化合物物流的蒸发提供的制冷相当于大于90%、有利地大于98%的装料流的液化所需的制冷;
本发明的对象还在于从包含碳氢化合物、氮气和氦气的装料流开始生产液态氮物流、气态氮物流、富氦气流和脱氮的碳氢化合物物流的生产设备,所述设备包括:
-膨胀装料流的膨胀部件,用于形成一膨胀的装料流;
-分开所述膨胀装料流的分开部件,其将所述膨胀装料流分成第一引入物流和第二引入物流;
-冷却第一引入物流的冷却部件,其包括一上游热交换器和一制冷循环,用于通过与在所述制冷循环中的动态膨胀获得的一制冷气流进行热交换的方式来获得冷却的第一引入物流;
-冷却第二引入物流的冷却部件,其包括第一下游热交换器,用于形成冷却的第二引入物流;
-一分馏塔,其包括多个理论分馏级;
-将所述冷却的第一引入物流和所述冷却的第二引入物流引入进所述分馏塔中的引入部件;
-提取至少一个重沸物流的提取部件和所述重沸物流在第一下游热交换器中流通的流通部件,用于冷却所述第二引入物流;
-在所述分馏塔的底部提取用于形成脱氮的碳氢化合物物流的一底部物流的提取部件;
-在分馏塔顶部提取一富氮的顶部物流的提取部件;
-加热富氮的顶部物流的加热部件,其包括至少一个第二下游热交换器,用于形成一被加热的富氮物流;
-提取和膨胀部件,其提取和膨胀所述加热的富氮物流的第一部分,用于形成气态氮物流;
-压缩部件,其压缩所述加热的富氮物流的第二部分,用于形成一再循环的氮物流,和冷却部件,其按经过第一下游交换器和经过所述的或每个的第二下游交换器流动的方式冷却所述压缩的再循环的氮物流;
-局部液化和膨胀部件,其局部液化和膨胀所述再循环的氮物流的,用于形成一膨胀的富氮物流;
-第一分离球;
-在所述第一分离球中引入来自所述膨胀的富氮物流的至少一部分的引入部件;
-回收部件,其回收来自所述第一分离球的顶部气流,用于形成富氦物流;
-回收来自第一分离球的底部的液流的回收部件和将该液流分成一液态氮物流和第一回流物流的分开部件;
-将所述第一回流物流按回流方式引入进所述分馏塔顶部中的引入部件。
根据本发明的设备可包括一个或多个以下的特征,单独地或根据技术上所有可能的组合:
-所述设备包括将全部的所述膨胀的富氮物流引入进所述第一分离球中的引入部件;和
-所述设备包括布置在所述第一分离球上游的第二分离球,和将膨胀的富氮物流引入进第二分离球中的引入部件,所述设备包括将来自第二分离球的顶部物流引入进第一分离球中的引入部件,和将第二分离球的至少一部分底部物流回流进分馏塔顶部中的引入部件。
附图说明
通过阅读接下来的仅作为示例提供且参照附录图示的描述,本发明将更好地得到理解,附图中:
-图1是实施根据本发明的第一生产方法的第一设备的功能概要简图;
-图2是与图1相似的实施根据本发明的第二生产方法的第二设备的视图;
-图3是与图1相似的实施根据本发明的第三生产方法的第三设备的视图;
-图4是与图1相似的实施根据本发明的第四生产方法的第四设备的视图;
-图5是与图1相似的实施根据本发明的第五生产方法的第五设备的视图;和
-图6是与图1相似的实施根据本发明的第六生产方法的第六设备的视图。
具体实施方式
图1示出根据本发明的第一设备10,其用于从通过液化天然气(GNL)原料获得的液态装料流12生产富碳氢化合物的脱氮液化天然气流14、用于使用在设备10中的气态氮物流16、液态氮物流18和富氦物流20。
如通过图1所示,设备10包括冷却装料流的一上游部分22和一下游分馏部分24。
上游部分22包括一液体减压透平26、一上游热交换器28,该交换器用于借助于一冷却循环30对装料流12进行冷却。
在该示例中,冷却循环30是反向的布雷顿制冷循环类型的一封闭循环。其包括一循环热交换器32、一上游分级压缩装置34和一动态膨胀透平36。
在图1的示例中,上游分级压缩装置34包括两层级,每层级包括一压缩机38A、38B和一空气或水冷却制冷器40A、40B。上游装置34的至少一个压缩机38A与动态膨胀透平36相联接,以提高该方法的效率。
下游分馏部分24包括一分馏塔50,其具有多个理论分馏级。下游部分24此外包括塔底的第一下游交换器52、第二下游交换器54和第三下游交换器56。
下游部分24此外包括一下游分级压缩装置58和塔顶的第一分离球60。
下游压缩装置58在该示例中包括串联安装的三个压缩层级,每层级包括连续布置的压缩机62A、62B、62C和水或空气冷却的制冷器64A、64B、64C。
现在将描述根据本发明的第一生产方法。
在接下来的整个描述中,将通过相同的数字标识表示流体物流和载运流体物流的管道。相同地,所考虑的压力是绝对压力,并且除了相反地进行指明,所考虑的百分比是摩尔百分比。
液态装料流12在该示例中是液化天然气流(GNL),其包括(摩尔)氦气0.1009%、氮气8.9818%、甲烷86.7766%、乙烷2.9215%、丙烷0.8317%、i-C4碳氢化合物0.2307%、n-C4碳氢化合物0.1299%、i-C5碳氢化合物0.0128%、n-C5碳氢化合物0.0084%、n-C6碳氢化合物0.0005%、苯0.0001%、二氧化碳0.0050%。
因此,该物流12包括大于70%的碳氢化合物摩尔浓度、在5%到30%之间的氮气摩尔浓度、和在0.01%到0.5%之间的氦气摩尔浓度。
装料流12具有小于-130℃的一温度,例如小于-145℃。该物流具有大于25巴的一压力,和特别是等于34巴。
在第一实施方式中,装料流12是液态的,以使得其组成在所述方法中直接可使用的液态装料流68。
液态装料流68被引入进液体减压透平26中,在其中液态装料流被减压到小于15巴的一压力,特别是等于6巴直到小于-130℃的一温度,和特别是等于-150.7℃。
在液态减压透平26的出口,一膨胀的装料流70形成。该膨胀装料流70被分为第一主引入物流72,用于通过制冷循环30被冷却,和第二引入物流74。
第一引入物流72具有大于10%的膨胀装料流70的一质量流。其被引入进上游热交换器28中,在热交换器中其被冷却到小于-150℃的一温度,和特别是等于-160℃,以提供冷却的第一引入物流76。
在上游交换器28中,第一引入物流72被布置以与在循环30中流动的制冷气流进行热交换,如在下文中将描述的。
冷却的第一引入物流76在第一减压阀78中被膨胀,直到小于3巴的一压力,继而被引入至分馏塔50的一中间层级N1。
第二引入物流74被运送直到塔底的第一下游交换器52,在该交换器中其被冷却直到小于-150℃的一温度,和特别是等于-160℃,以提供冷却的第二引入物流80。
冷却的第二引入物流80在第二减压阀82中被膨胀,直到小于3巴的一压力,继而被引入至分馏塔50的中间层级N1。
在该示例中,冷却的第一引入物流76和冷却的第二引入物流80被引入至分馏塔50的相同层级N1。
一重沸物流84从位于中间层级N1下方的分馏塔50的一下部层级N2被提取。重沸物流84经过塔底的第一下游交换器52,用于被布置以与第二引入物流74进行热交换和冷却该第二物流74。继而其被再引入至分馏塔50底部附近,位于下部层级N2的下方。
分馏塔50在低压下运行,特别是小于5巴,有利地小于3巴。在该示例中,分馏塔50基本在1.3巴运行。
分馏塔50产生一底部物流86,其用于形成富脱氮的液化天然气的物流14。该脱氮的液化天然气流包括数量受控的氮气,例如小于1%摩尔百分比。
底部物流86在一泵88中在5巴下进行泵唧,以形成富碳氢化合物的脱氮物流14,和用于向大气压力下的一存储地点发送,和形成用于被利用的脱氮的液化天然气流。物流14是可以液体形式被运输的一种液化天然气流,例如在一液化天然气运输船中进行运输。
分馏塔50此外产生一富氮顶部物流90,其从该分馏塔50的顶部被提取。该顶部物流90具有有利地小于1%的碳氢化合物摩尔浓度,和甚至更为有利地小于0.1%。其具有大于0.2%的氦气摩尔浓度,和有利地大于0.5%。
在图1上的示例中,顶部物流90的摩尔成分如下:氦气0.54%、氮气99.40%和甲烷0.06%。
富氮顶部物流90继而依次地经过第二下游交换器54、第一下游交换器52,然后经过第三下游交换器56,用于连续地被加热到-20℃。
在第三下游交换器56的出口,获得一加热的富氮物流92。该物流92因而被分成生产的氮气的第一少数部分94,和再循环的氮气的第二部分96。
少数部分94具有在物流92的质量流的10%到50%之间的一质量流。少数部分94经过第三减压阀98被膨胀,用于形成气态氮物流16。
该气态氮物流16具有大于大气压力的一压力,并且特别是大于1.1巴。其具有大于99%的氮气摩尔浓度。
多数部分96被引入进下游压缩装置58中,在该装置中其依次地在每个压缩层级中经过一压缩机62A、62B、62C和一制冷器64A、64B、64C。
多数部分96继而被压缩到大于20巴的一压力,和特别是基本等于21巴,用于形成一压缩的再循环的氮物流100。
压缩的再循环的氮物流100因而具有大于10℃的一温度,和特别是等于38℃。
压缩的再循环的氮物流100依次地经过第三下游交换器56、继而经过塔底的第一下游交换器52和然后经过第一下游交换器54。
在第二下游交换器54中和第三下游交换器56中,再循环的氮物流100对流式地进行流动和在顶部氮物流90进行热交换。因此,顶部氮物流90转让千卡给再循环的氮物流100。
在塔底的第一热交换器52中,再循环的氮物流100此外被布置以与重沸物流84进行热交换,用以通过该物流84被冷却。
在通过第二下游交换器54中,再循环的氮物流100形成一再循环的冷凝氮物流102,基本上是液态的。该液流包括大于90%的液体馏分并且具有小于-160℃的一温度,和有利地等于-170℃。
继而,冷凝物流102在第四减压阀104中被膨胀,以提供一两相流体106,其被引入进第一分离球60中。
第一分离球60在顶部产生一富氦的顶部气流,该气流在经过第五减压阀108后,形成富氦气流20。
富氦气流20具有大于10%的氦气摩尔浓度。其用于被运送到一纯氦生产装置,以在该装置中进行处理。根据本发明的方法允许回收至少60%(摩尔)的在装料流12中存在的氦气。
第一分离球60在底部产生一底部液态氮物流110。该底部物流110被分成生产的液态氮的一少数部分112和回流的氮物流的一多数部分114。
少数部分112具有小于底部物流110的质量流的10%,和特别是在0%到10%之间的一质量流。少数部分112在第六减压阀116中被膨胀,以形成生产的液态氮物流18。生产的氮物流具有大于99%的氮气摩尔浓度。
多数部分114经过第七减压阀118被膨胀到分馏塔的压力,用于形成第一回流物流,继而被引入至分馏塔50的一顶部层级N3,顶部层级位于该分馏塔顶部下方和中间层级N1的上方。氮气在多数部分114中的摩尔馏分大于99%。
在图1上示出的示例中,制冷循环30是反向的布雷顿制冷循环类型的一封闭循环,其使用惟一地气态的一制冷气流。
在该示例中,制冷气流通过基本纯净的氮气形成,其氮气摩尔浓度大于99%。
给送到上游交换器28的制冷气流130具有小于-150℃的一温度,并且特别是等于-165℃,和大于5巴的一压力和特别是基本等于9.7巴。制冷气流130经过循环热交换器32流动,在循环热交换器中制冷气流通过与第一主引入物流72的热交换被加热。
因此,在上游交换器28的出口的加热的制冷气流132的温度小于-150℃和特别是等于-153℃。
在依次地被引入进上游分级压缩装置34的压缩机38A、38B和制冷器40A、40B前,加热的物流132在循环热交换器32中经历新的一次加热。
在上游装置34的出口,其形成压缩的制冷气流134,该气流通过在循环热交换器32中与来自上游交换器28的加热的制冷气流132进行热交换被冷却。
冷却的压缩物流136因而具有大于15巴的一压力,和特别是基本等于20巴以及小于-130℃的一温度和特别是基本等于-141℃。
冷却的压缩物流136继而被引入进动态膨胀透平36中。该物流在膨胀透平36中经历动态膨胀,以提供在上文中描述的温度和压力下的制冷气流130。
在一有利变型中,上游和下游压缩装置34和58被集成在多主体的同一机器中,其具有单一马达,用于驱动压缩机38A、38B和压缩机62A到62C。
在图1的方法中说明的不同物流的温度、压力和质量流示例在下面的表格中进行总结:
物流 | 温度(℃) | 压力(巴) | 流量(千克/小时) |
12 | -149.5 | 34 | 177 365 |
70 | -150.7 | 6 | 177 365 |
76 | -160 | 6 | 135 142 |
80 | -160 | 6 | 42 223 |
84 | -163.6 | 1.4 | 168 931 |
86 | -159.7 | 1.4 | 154 923 |
14 | -159.5 | 5 | 154 923 |
90 | -193.4 | 1.3 | 55 761 |
92 | -20 | 1.3 | 55 761 |
16 | -20.4 | 1.1 | 20 219 |
100 | 38 | 21 | 35 541 |
106 | -173 | 9 | 35 541 |
20 | -180.5 | 4 | 1 663 |
18 | -182 | 4 | 560 |
114 | -173 | 9 | 33 319 |
130 | -165 | 9.7 | 86 840 |
132 | -153 | 9.7 | 86 840 |
136 | -141.5 | 19.5 | 86 840 |
所述方法的能量消耗如下:
压缩机62A:1300千瓦
压缩机62B:1358千瓦
压缩机62C:1365千瓦
压缩机38B:2023千瓦
总计:6046千瓦
根据本发明的第二设备140在图2上示出。该第二设备140用于实施根据本发明的第二生产方法。
该设备140与第一设备10的不同之处在于,其包括第二分离球142,第二分离球插置在第四减压阀104的出口和第一分离球60的入口之间。
根据本发明的第二方法与第一方法的不同之处在于,仅一部分由在第四减压阀104中的冷却的再循环氮物流102的膨胀产生的两相流体106在第一分离球60中被接纳。
因此,在第四减压阀104的出口形成的两相流体106被引入进第二分离球142中,而非直接地进入第一分离球60中。此外,冷却的氮物流102不经过第二下游交换器54。
在第二分离球142中产生的顶部流体144经过第二下游交换器54,以在第二下游交换器中被冷却,继而以冷却的顶部流体146的形式被引入进第一分离球60中。
从第二分离球142底部抽取的底部流体148被分为第二回流氮物流150和一冷却补给物流152。
在第八减压阀154中膨胀后,第二回流氮物流150被引入至分馏塔50的一顶部层级N4,其位于第一回流物流114引入进分馏塔50的引入层级N3的附近和下方。
在图2上以虚线示出的一变型中,回流物流114、150被引入至分馏塔50的相同顶部层级N3。
第二回流物流150的质量流大于底部流体148的质量流流体的90%。
第二冷却补给物流152在第二下游交换器54的上游被再引入进顶部物流90中,以提供用于冷却和部分地冷凝在第二下游交换器54中经过的顶部流体144的千卡。
由顶部物流90和冷却补给物流152的混合产生的混合物流156依次地被引入进第二下游交换器54中,继而被引入进第一下游交换器52中,在其中混合物流与再循环的氮物流100和第二引入物流74进行热交换,以冷却这些物流。
根据本发明的第二方法此外以与根据本发明的第一方法相似的方式进行操作。
在该方法中,装料流12是一液化天然气流(GNL),其包括与前述的装料流成分相同的成分。
在图2上的示例中,顶部物流90的摩尔成分如下:氦气0.54%、氮气99.35%和甲烷0.11%。
在图2的方法中说明的不同物流的温度、压力和质量流示例在下面的表格中进行总结:
物流 | 温度(℃) | 压力(巴) | 流量(千克/小时) |
12 | -149.5 | 34 | 177 365 |
70 | -150.7 | 6 | 177 365 |
76 | -160 | 6 | 134 400 |
80 | -160 | 6 | 43 150 |
84 | -163.6 | 1.4 | 169 069 |
86 | -159.7 | 1.4 | 155 100 |
14 | -159.5 | 5 | 155 100 |
90 | -193.4 | 1.3 | 52 390 |
92 | -32 | 1.3 | 52 678 |
16 | -32.1 | 1.1 | 22 140 |
100 | 38 | 19.7 | 30 550 |
106 | -180 | 5 | 30 550 |
146 | -186 | 4.7 | 3 940 |
150 | -179.8 | 5 | 26 320 |
152 | -179.8 | 5 | 288 |
20 | -186.3 | 4.7 | 271 |
18 | -186.3 | 4.7 | 28 |
114 | -186.3 | 4.7 | 3 640 |
130 | -163 | 9.7 | 112 100 |
132 | -154 | 9.7 | 112 100 |
136 | -140 | 19.2 | 112 100 |
所述方法的能量消耗如下:
压缩机62A:1482千瓦
压缩机62B:912千瓦
压缩机62C:708千瓦
压缩机38B:2584千瓦
总计:5686千瓦
根据本发明的第三设备160,其用于实施根据本发明的第三方法,在图3上示出。
第三设备160与第一设备10的不同之处在于,存在一分馏部分162和一上游液化交换器164,分馏部分162和上游液化交换器164被布置在液体减压透平26的上游。
在该示例中,装料流12是气体形式的天然气(GN)。其首先被引入进液化交换器164中,以被冷却到小于-20℃的一温度和基本等于-30℃。
装料流12继而被运送到分馏部分162中,分馏部分产生C5 +碳氢化合物含量小的一处理气体166,和富C5 +碳氢化合物的液化气的一馏分168。C5 +碳氢化合物在处理气体166中的摩尔浓度小于300ppm。
处理气体166被再引入进液化交换器164中,以被液化和向液化交换器164的出口提供液态装料流68。
处理气体166没有重成分,例如苯,其结晶温度高,会容易地被液化和没有在液化交换器164中堵塞的风险。
为了提供冷却装料流12和处理气体166所需的千卡,根据本发明的第三方法包括:在经过泵88后,富脱氮的碳氢化合物物流14经过交换器164。
为此,分馏塔50的底部液流86被泵唧到大于20巴的一压力,有利地大于28巴,用于在液化交换器164中被再利用,和允许装料流12的冷却和处理气体166的液化。
通过脱氮的碳氢化合物物流14的蒸发提供的制冷相当于超过90%,有利地超过98%的装料流12的液化所需的制冷。
相同地,在通过塔底的下游交换器52之后和在引入进第三下游交换器56之前,在氮物流102中提取一提取物流170。提取物流170继而在以辅助气态氮物流172的形式被给送到交换器164出口之前,被引入进液化交换器164中。
提取馏分170的质量流相对于富氮的顶部物流90的质量流比例如在0%到50%之间。
根据本发明的第三方法此外以与根据本发明的第一方法相似的方式运行。
装料流12在该示例中是气体形式的天然气流,其包括(摩尔):氦气0.1000%、氮气8.9000%、甲烷85.9950%、乙烷3.0000%、丙烷1.0000%、i-C4碳氢化合物0.4000%、n-C4碳氢化合物0.3000%、i-C5碳氢化合物0.1000%、n-C5碳氢化合物0.1000%、n-C6碳氢化合物0.0800%、苯0.0200%、二氧化碳0.0050%。
液态装料流68因而包括与所描述的用于根据本发明的第一和第二方法的液化天然气流12的成分相同的成分。
在图3上的示例中,顶部物流90的摩尔成分如下:氦气1.19%、氮气98.64%和甲烷0.16%。
在图3的示例中示出的不同物流的温度、压力和质量流量的实例在下表中列出。
物流 | 温度(℃) | 压力(巴) | 流量(千克/小时) |
12 | 38 | 40 | 182 700 |
166 | -38 | 35 | 177 470 |
68 | -152 | 34 | 177 470 |
70 | -152.8 | 6 | 177 470 |
76 | -159.5 | 6 | 139 733 |
80 | -160 | 6 | 37 779 |
84 | -161.5 | 2.7 | 174 559 |
86 | -158.3 | 2.7 | 165 811 |
14 | -157.2 | 28 | 165 811 |
90 | -186.7 | 2.6 | 24 896 |
92 | -20 | 2.6 | 24 896 |
16 | -20.7 | 2.5 | 11 083 |
100 | 38 | 39.7 | 13 813 |
106 | -177 | 9 | 13 813 |
20 | -180.41 | 5 | 370 |
18 | -179.8 | 5 | 248 |
114 | -176.9 | 9 | 13 195 |
130 | -165.8 | 9.7 | 61 629 |
132 | -155 | 9.7 | 61 629 |
136 | -143 | 19.2 | 61 629 |
所述方法的能量消耗如下:
压缩机62A:632千瓦
压缩机62B:388千瓦
压缩机62C:325千瓦
压缩机38B:1440千瓦
总计:2785千瓦
根据本发明的第四设备180,其用于实施根据本发明的第四方法,在图4上示出。该第四设备180与第三设备170的不同之处在于,存在如在第二设备中的两分离球60、142。
其运行此外与第三设备160的运行相似。
根据本发明的第五设备190在图5上示出,用于实施根据本发明的第五方法。
第五设备190与第四设备180的不同之处在于,冷却循环30是一半开放循环。为此,制冷循环30的制冷流体通过压缩的再循环的氮物流100的一分支流192形成,该压缩氮物流100被压缩到基本等于40巴的第一压力P1,在上游压缩装置58的出口被提取。
分支流192的质量流小于少数部分96的质量流的99%。
分支流192被引入进循环热交换器32中,用于在交换器32出口形成冷却的压缩物流136,继而在透平36中膨胀后,形成引入进上游交换器28中的制冷气流130。
制冷气流130因而具有大于99%的氮气摩尔浓度和小于0.1%的碳氢化合物摩尔浓度。
在通过交换器32后,在被再引入进压缩的再循环的氮物流100之前,在压缩装置58的倒数第二级和最后一级之间,在小于第一压力P1的第二压力P2,加热的制冷气流132被引入进与透平36相联接的压缩机38A中,继而被引入进制冷器40A中。
根据本发明的第六设备200在图6上示出。
根据本发明的第六设备200与第四设备180的不同之处在于,循环交换器32通过与第三下游交换器56相同的热交换器组成。
来自上游交换器28的加热的制冷气流132被引入进第三下游交换器56中,在第三下游交换器中其被布置以与来自第二下游交换器52的混合物流156和与来自下游压缩装置58的压缩的再循环的氮物流100进行热交换。
相同地,压缩的制冷气流134在被引入进动态膨胀透平36中之前,经过第三下游交换器56,以被冷却。
根据本发明的第六方法的运行此外与根据本发明的第四方法的运行相似。
借助于根据本发明的方法,可灵活地和经济地生产基本纯净的气态氮16、基本纯净的液态氮18、和以后可在氦气生产工厂被再利用的富氦物流20。
所述方法此外生产一种富脱氮的碳氢化合物物流14,其可以气体或液体的形式被使用。
通过本方法产生的所有流体因而是可以此被使用和再利用的。
该方法可不加区别地与由液化天然气或气体形式的天然气组成的装料流12共同使用。
通过调节在制冷循环30的制冷气流130中由第二引入物流72提取的热功率,可容易地对由本方法生产的液态氮18的数量进行控制。
Claims (13)
1.从包含碳氢化合物、氦气和氮气的装料流开始生产液态氮物流(18)、气态氮物流(16)、富氦气流(20)和脱氮的碳氢化合物物流(14)的生产方法,所述方法包括以下步骤:
-膨胀所述装料流(12),用于形成一膨胀的装料流(70);
-将所述膨胀的装料流(70)分成第一引入物流(72)和第二引入物流(74);
-所述第一引入物流(72)在一上游热交换器(28)内通过与一制冷气流(130)的热交换进行冷却,该制冷气流通过在一制冷循环(30)中动态膨胀地获得,用于获得被冷却的第一引入物流(76);
-所述第二引入物流(74)经过第一下游热交换器(52)进行冷却,用于形成被冷却的第二引入物流(80);
-将所述被冷却的第一引入物流(76)和所述被冷却的第二引入物流(80)引入进一分馏塔(50)中,所述分馏塔包括多个理论分馏级;
-提取至少一个重沸物流(84)和使所述重沸物流(84)在所述第一下游热交换器(52)中流通,用于冷却所述第二引入物流(74);
-在所述分馏塔(50)底部提取一底部物流(86),用于形成所述脱氮的碳氢化合物物流(14);
-在所述分馏塔(50)顶部提取一富氮的顶部物流(90);
-经过至少一个第二下游热交换器(54,56)对所述富氮的顶部物流(90)进行加热,用于形成一被加热的富氮物流(92);
-提取和膨胀所述被加热的富氮物流(92)的第一部分(94),用于形成气态氮物流(16);
-压缩所述被加热的富氮物流(92)的第二部分(96),用于形成一压缩的再循环的氮物流(100),并且,所述压缩的再循环的氮物流(100)按经过所述第一下游交换器(52)和经过所述的或每个的第二下游交换器(54,56)流动的方式进行冷却;
-液化和局部膨胀所述再循环的氮物流(100),用于形成一膨胀的富氮物流(106);
-在第一分离球(60)中引入来自所述膨胀的富氮物流(106)的至少一部分(106;146);
-回收来自所述第一分离球(60)的顶部气流,用于形成富氦物流(20);
-回收来自所述第一分离球(60)底部的液流(110),并将该液流(110)分成一液态氮物流(18)和第一回流物流(114);
-在所述分馏塔(50)顶部中按回流方式引入所述第一回流物流(114)。
2.根据权利要求1所述的方法,其特征在于,全部的所述膨胀的富氮物流(106)在膨胀后直接地被引入进所述第一分离球(60)中。
3.根据权利要求1所述的方法,其特征在于,所述膨胀的富氮物流(106)被引入进布置在所述第一分离球(60)上游的第二分离球(142)中,来自所述第二分离球(142)的顶部物流(144)被引入进所述第一分离球(60)中,所述第二分离球(142)的至少一部分底部物流(148)按回流方式被引入进所述分馏塔(50)的顶部中。
4.根据权利要求3所述的方法,其特征在于,所述第二分离球的底部物流(148)被分成引入进所述分馏塔(50)中的第二回流物流(150)和一冷却补给物流(152),冷却补给物流(152)在经过所述第二下游热交换器(54)前与所述富氮的顶部物流(90)相混合。
5.根据权利要求4所述的方法,其特征在于,所述分馏塔(50)的操作压力小于5巴,有利地小于3巴。
6.根据前述权利要求中任一项所述的方法,其特征在于,所述制冷循环(30)是反向的布雷顿制冷循环类型的一封闭循环,所述方法包括以下步骤:
-在一循环热交换器(32)中加热所述制冷气流(130),直到基本等于周围环境温度的一温度;
-压缩所述被加热的制冷气流(132),用于形成一压缩的制冷气流(134),并在所述循环热交换器(32)中按与来自所述第一上游热交换器(28)的被加热的制冷气流(132)热交换的方式进行冷却,用于形成一被冷却的压缩制冷气流(136);
-动态膨胀所述被冷却的压缩制冷气流(136),用于形成所述制冷气流(130),并将所述制冷气流(130)引入进所述第一上游热交换器(28)中。
7.根据权利要求6所述的方法,其特征在于,所述循环热交换器(32)通过下游交换器(52,54,56)之一(56)形成,所述压缩的制冷气流(134)在所述下游交换器(56)中按与来自所述分馏塔(50)顶部的富氮顶部物流(90)热交换的方式至少部分地被冷却。
8.根据权利要求1到5中任一项所述的方法,其特征在于,所述制冷循环(30)是半开放循环,所述方法包括以下步骤:
-提取至少一馏分的所述压缩的循环的富氮物流(100),所述压缩的循环的富氮物流(100)被压缩到第一压力(P1),用于形成一富氮的提取物流(192);
-在一循环热交换器(32)中冷却富氮的提取物流(192),用于形成一被冷却的提取物流;
-动态膨胀来自所述循环热交换器(32)的所述被冷却的提取物流的,用于形成所述制冷气流(130),并将所述制冷气流(130)引入进所述上游热交换器(28)中;
-在一压缩机中压缩来自所述上游热交换器的制冷气流(132),并将该物流再引入进所述压缩的再循环的氮物流(100)中,该氮物流被压缩到小于所述第一压力(P1)的第二压力(P2)。
9.根据前述权利要求中任一项所述的方法,其特征在于,所述装料流(12)是一气流,所述方法包括以下步骤:
-液化所述装料流(12),以按经过一液化热交换器(164)的方式来形成一液态装料流(68);
-在所述液化热交换器(164)中按与来自所述装料流(12)的一气流(166)进行热交换的方式,对来自所述分馏塔(50)底部的脱氮的碳氢化合物物流(14)进行蒸发。
10.根据权利要求9所述的方法,其特征在于,通过脱氮的碳氢化合物物流(14)的蒸发提供的制冷相当于大于90%、有利地大于98%的装料流(121)的液化所需的制冷。
11.从包含碳氢化合物、氮气和氦气的装料流(12)开始生产液态氮物流(18)、气态氮物流(16)、富氦气流(20)和脱氮的碳氢化合物物流(14)的生产设备(10;140;160;180;190;200),所述设备包括:
-膨胀装料流(12)的膨胀部件(26),用于形成一膨胀的装料流70);
-分开所述膨胀装料流(70)的分开部件,其将所述膨胀装料流分成第一引入物流(72)和第二引入物流(74);
-冷却第一引入物流(72)的冷却部件(28;30),其包括一上游热交换器(28)和一制冷循环(30),用于通过与在所述制冷循环(30)中的动态膨胀获得的一制冷气流(130)进行热交换的方式来获得冷却的第一引入物流(76);
-冷却第二引入物流(74)的冷却部件,其包括第一下游热交换器(52),用于形成冷却的第二引入物流(80);
-一分馏塔(50),其包括多个理论分馏级;
-将所述冷却的第一引入物流(76)和所述冷却的第二引入物流(80)引入进所述分馏塔(50)中的引入部件;
-提取至少一个重沸物流(84)的提取部件和所述重沸物流(84)在第一下游热交换器(52)中流通的流通部件,用于冷却所述第二引入物流(74);
-在所述分馏塔(50)的底部提取用于形成脱氮的碳氢化合物物流(14)的一底部物流(86)的提取部件;
-在分馏塔(50)顶部提取一富氮的顶部物流(90)的提取部件;
-加热富氮的顶部物流(90)的加热部件,其包括至少一个第二下游热交换器(54,56),用于形成一被加热的富氮物流(92);
-提取和膨胀部件,其提取和膨胀所述加热的富氮物流(92)的第一部分(94),用于形成气态氮物流(16);
-压缩部件(58),其压缩所述加热的富氮物流(92)的第二部分(96),用于形成一再循环的氮物流(100),和冷却部件,其按经过第一下游交换器(52)和经过所述的或每个的第二下游交换器(54,56)流动的方式冷却所述压缩的再循环的氮物流(100);
-局部液化和膨胀部件(104),其局部液化和膨胀所述再循环的氮物流(100)的,用于形成一膨胀的富氮物流(106);
-第一分离球(60);
-在所述第一分离球(60)中引入来自所述膨胀的富氮物流(106)的至少一部分的引入部件;
-回收部件,其回收来自所述第一分离球(60)的顶部气流,用于形成富氦物流(20);
-回收来自第一分离球(60)的底部的液流(110)的回收部件和将该液流分成一液态氮物流(112)和第一回流物流(114)的分开部件;
-将所述第一回流物流(114)按回流方式引入进所述分馏塔(50)顶部中的引入部件。
12.根据权利要求11所述的设备(10;160),其特征在于,所述设备包括将全部的所述膨胀的富氮物流(106)引入进所述第一分离球(60)中的引入部件。
13.根据权利要求11所述的设备(140;180;190;200),其特征在于,所述设备包括布置在所述第一分离球(60)上游的第二分离球(142),和将膨胀的富氮物流(106)引入进第二分离球(142)中的引入部件,所述设备包括将来自第二分离球(142)的顶部物流(144)引入进第一分离球(60)中的引入部件,和将第二分离球(142)的至少一部分底部物流(148)回流进分馏塔(50)顶部中的引入部件。
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PCT/FR2009/051884 WO2010040935A2 (fr) | 2008-10-07 | 2009-10-02 | Procede de production de courants d'azote liquide et gazeux, d'un courant gazeux riche en helium et d'un courant d'hydrocarbures deazote et installation associee |
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AU2009300946A1 (en) | 2010-04-15 |
BRPI0920814A2 (pt) | 2015-12-22 |
WO2010040935A3 (fr) | 2011-06-03 |
BRPI0920814B1 (pt) | 2020-04-07 |
US9316434B2 (en) | 2016-04-19 |
NZ592143A (en) | 2012-11-30 |
FR2936864B1 (fr) | 2010-11-26 |
EP2344821B1 (fr) | 2018-01-24 |
EA020215B1 (ru) | 2014-09-30 |
CA2739696C (fr) | 2017-01-24 |
WO2010040935A2 (fr) | 2010-04-15 |
MY160839A (en) | 2017-03-31 |
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