CN100338344C - 用低甲烷浓度和高惰性气体浓度的储气向燃气轮机供给燃料的方法 - Google Patents

用低甲烷浓度和高惰性气体浓度的储气向燃气轮机供给燃料的方法 Download PDF

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CN100338344C
CN100338344C CNB2004100978646A CN200410097864A CN100338344C CN 100338344 C CN100338344 C CN 100338344C CN B2004100978646 A CNB2004100978646 A CN B2004100978646A CN 200410097864 A CN200410097864 A CN 200410097864A CN 100338344 C CN100338344 C CN 100338344C
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F·F·密特利克
D·J·维克多利
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ExxonMobil Chemical Patents Inc
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Abstract

本发明涉及一种用甲烷体积浓度为百分之40至约百分之80的天然气储气中的甲烷气体向燃气轮机供给燃料的方法，该方法包括：将第一天然气气流中的惰性气体与甲烷气体分离，提供分离的甲烷气体和分离的惰性气体；将分离的惰性气体、加入的氢气或催化转化成的氢气和甲烷体积浓度为百分之40至百分之80的第二天然气气流混合，提供氢气增强的惰性气体/甲烷气体/氢气气体混合物；以及用该氢气增强的惰性气体/甲烷气体/氢气气体混合物向燃气轮机供给燃料。本发明能够使发电燃气轮机的输出增加约5至约20%。

Description

用低甲烷浓度和高惰性气体浓度的储气向燃气轮机供给燃料的方法
技术领域
本发明涉及低甲烷浓度和高惰性气体浓度天然气的燃烧过程。更具体地说，本发明涉及通过提高惰性气体的相对浓度来利用所含甲烷的体积浓度为约从百分之40到百分之80的天然气储气并将所生产的甲烷用于生产管道质量天然气的方法。
背景技术
目前，大部分甲烷储气具有相对较低的甲烷气体浓度。多数这些储气中甲烷气体的体积浓度约从百分之40到百分之80。目前，是通过从天然气中除去杂质，从而形成甲烷体积浓度通常从约百分比大于或等于95至约百分比大于或等于99的管道质量天然气。从经济上考虑，将甲烷体积浓度约从百分之40到百分之80的天然气转变成管道质量的天然气，向燃气轮机供给燃料来发电是不实际的，因为该转变过程的成本非常高。而且，甲烷体积浓度约从百分之40到百分之80的天然气不能作为燃气轮机的可靠燃料源来产生高输出功率的电力，尤其是在该范围的低端值处，因为在没有特殊设备、催化剂和没有特殊的氧与其他可燃物补偿的情况下，这么低的甲烷浓度不能提供用于燃料燃烧的稳定火焰。并且，甲烷体积浓度为百分之40至80的气流还有由于燃气轮机中的较高火焰温度而产生高NOx排出的问题。
与通过制成管道质量天然气向燃气轮机供给燃料的方法相比，用甲烷体积浓度为百分之40至80且含有大量惰性气体的天然气储气并将该气流或该气流的一部分进行提纯，来向燃气轮机供给燃料的方法使成本大大降低，在经济上更为有利。
发明内容
本发明涉及一种用甲烷体积浓度约为百分之40至80的低甲烷浓度和高惰性气体浓度的天然气储气向燃气轮机供给燃料的方法。本发明能够利用这些比通过制成管道质量天然气向燃气轮机供给燃料的方法所需成本显著降低的储气来向燃气轮机供给燃料用以发电。如上所述，目前，这些储气只能用于在除去杂质之后生成合适的燃气轮机燃料。还如前所述，现在的方法成本非常高，根据当前的天然气价格，这在经济上没有吸引力。本发明的方法能够根据环保需要除去来自天然气储气的气体中的杂质，并按能使燃气轮机产生的电力输出增加约5至20％的量将惰性气体留在燃料中。本发明方法的一个方式是试图将惰性气体留在燃料中，使流过燃气轮机的质量流量最大并提高电力输出，不需要花费生产管道质量甲烷气体和向燃料中掺混额外的惰性气体以增加流过燃气轮机的质量流量及降低火焰温度来减小NOx的排出的成本。
在本发明的一个方式中，采用天然气气流和用于生产管道质量天然气的方法。在此方式中，提纯处理过程中将所含甲烷体积浓度从约百分之40至百分之80的天然气储气中的惰性气体与甲烷气体分离。可以仅对一定量的甲烷进行分离，以便提供惰性气体增强的甲烷气体混合物，与以管道质量的天然气向燃气轮机供给燃料的方法相比，能够有效使燃气轮机的能量输出增加约5至约20％。然后，将经分离过程产生的提纯甲烷气流送去进一步提纯，生产管道质量天然气。或者，可以使惰性气体与甲烷气体整体分离，然后将与甲烷分离的该惰性气体与没有除去惰性气体的天然气气流混合(或其它含百分之40至百分之80体积浓度甲烷的气流)，混合量为应使燃气轮机的输出比利用管道质量的天然气向燃气轮机供给燃料的方法增加约5至约20％。
在本发明的一个方式中，氮气是主要的惰性气体，可用膜将惰性氮气与天然气和其中的甲烷进行初级分离。市场上可购得的、适于该分离过程的膜有Air Liquide公司(Houston Texas)的Medal。此分离过程可以只按如上所述能使燃气轮机输出增加的量进行，或者将与天然气分离的氮气与天然气储气混合，以便提供惰性气体增强的天然气，使燃气轮机的输出比利用管道质量的天然气向燃气轮机供给燃料的方法增加约5至约20％。
当二氧化碳的体积浓度在约百分之45以内时，可以用膜来分离二氧化碳。在另一方式中，当二氧化碳是主要的惰性气体，其体积浓度超过约百分之45时，二氧化碳在低温下与甲烷体积浓度为约百分之40至约百分之80的天然气储气分离。在本发明的一个方式中，当天然气的压力较高，例如大于约2500psig时，该高压进料气体闪蒸到低压，例如约500psig。膨胀时的Joule Thomson效应有效提供了一定量的冷却，以便进行低温分离。当天然气储气的压力较低，如低于约1100psig时，可以通过天然气储气的外部制冷为二氧化碳与天然气储气及其中的甲烷进行分离提供有效冷却而达到分离的目的。
在一个非常重要的方式中，将惰性气体与天然气储气及其中的甲烷分离，从而提供甲烷体积浓度为约百分之40的甲烷气体。从天然气储气中分离的甲烷可以送去进行进一步处理，以便制成管道质量的天然气。从天然气气流中分离出来的惰性气体再送回到从油井中出来的天然气气流中，按能有效提供甲烷体积浓度为小于约百分之40的甲烷/惰性气体混合物的量进行混合，以便提供惰性气体增强的甲烷气体混合物。将惰性气体增强的甲烷气体混合物与氢气混合，或者在一个重要方式中，将恰好足够的甲烷转变成氢气，以便生成氢气和惰性气体和甲烷气体的燃料气混合物，该气体燃料混合物不仅可作为一种可接受的燃气轮机的燃料，而且该混合物能有效提供火焰稳定性(例如提供至少为110BTU/标准立方英尺气体热量的气体)，且产生的能量比甲烷含量在约百分比大于或等于95至约百分比大于或等于99体积的的标准天然气更高。若需要的话，将氢气和惰性气体和甲烷气体混合气进行脱水，以便除去足够量的水，从而提供具有火焰稳定性的氢气和惰性气体和甲烷气体混合气。在一个重要方式中，该混合气含有至少约百分之6体积的氢气。然后再将具有火焰稳定性的氢气增强型脱水氢气和惰性气体和甲烷气体混合气用于向燃气轮发电机供给燃料。按此方式，本发明的方法比使用甲烷含量在约百分之95至约百分比大于或等于99体积的标准天然气的燃气轮机的方法能使燃气轮机电力输出有效增加至少约百分之10。在大多数情况下，输出能够增加至少约百分之20并能达到百分之30，而后一界限值是由于受燃气轮机的机械设计限制。
在本发明的一个方式中，天然气中的一部分甲烷通过催化转变或重构成氢气，然后再形成氢气增强型氢气和惰性气体和甲烷混合气。实现该转变的反应式包括：
CH4+CO2→2CO+2H2
CH4+2H2O→CO2+4H2
在另一重要方式中，尤其是其中甲烷转变成氢气时，在转变反应之前，利用物理溶剂从天然气中除去硫化氢和其它酸性成分例如COS、RSH和RSSR，从而生成脱硫天然气，物理溶剂有选择地除去硫化氢和其他酸性气体，但是很少除去二氧化碳和其他惰性气体例如氦气、氩气和氮气。在此方式中，物理溶剂从以下组中选择，该组包括甲醇、聚乙二醇二甲醚混合物(分子量为约280)、碳酸丙二酯(沸点240℃)、N-甲基-2-吡咯烷酮(沸点202℃)、低聚乙二醇甲基异丙基醚的混合物(沸点320℃)、膦酸三正丁酯(在30mm Hg时沸点180℃)和氰基乙酸甲酯(沸点202℃)。该脱硫天然气与足量水混合，以便能从甲烷足量产生氢气，从而获得火焰稳定性或是BTU/Scf值至少为约110。在该方式中，重要的是在将一部分甲烷变换成氢气步骤之前要除去硫化氢和其他酸性气体，因为该重构过程是一个催化反应，硫化氢气体和其他酸性气体可能会使催化剂中毒。对酸性条件敏感且可在本发明该方式中使用的催化剂包括United Catalyst有限公司的C11系列催化剂、Haldor Topsoe公司的R67和BASF公司的G1-25。用于脱硫天然气的高温“重构催化剂”通常为铁、铬和铜，用于脱硫天然气的低温“重构催化剂”通常由铜、锌和铝制成。
在另一重要方式中，重构反应在酸性条件下利用催化剂进行，该催化剂例如United Catalyst有限公司的C25系列催化剂、BASF公司的K8-11催化剂和Haldor Topsoe公司的SSK催化剂。通常，这些催化剂是铬钼催化剂。在本发明的这一方式中，将酸性天然气与水混合，水的量应足以形成能够形成或重构成氢气含量足以使富含氢气的氢气和惰性气体和甲烷混合气具有火焰稳定性的甲烷气体/水混合物，该氢气和惰性气体和甲烷混合气含有不超过百分之40体积的甲烷。
在惰性气体与天然气储气混合之后，该惰性气体增强的甲烷气体混合物可以含有低至百分之35、百分之25或者甚至低于百分之20体积的甲烷，且仍然比以用氢气提供火焰稳定性的管道质量甲烷作为燃气轮机燃料提供更多的能量。在本发明的实际操作中，应将足量的甲烷转变成氢气，以生成氢气体积含量为至少百分之6，优选是从约百分之6至约百分之10的氢气增强型氢气和惰性气体和甲烷混合气。这将生成具有火焰稳定性的氢气增强型氢气和惰性气体和甲烷混合气，该氢气增强型氢气和惰性气体和甲烷混合气能非常有效地向燃气轮机供给燃料，以便发电。
附图的简要说明
图1是例示说明本发明方法的一个流程图，在该方法中，一些甲烷转变成氢气，从而形成氢气和惰性气体和甲烷气体混合物，以便向燃气轮机供给燃料。
图2是例示说明本发明方法的一个流程图，在该方法中，高压进料天然气闪蒸成低压，将同在该高压进料天然气中的甲烷气体与二氧化碳气体分离。
图3是例示说明本发明方法的一个流程图，在该方法中，低压进料天然气利用外部制冷设备冷冻，将同在该低压进料天然气中的甲烷气体与二氧化碳气体分离。
具体实施方式
将甲烷体积浓度从约百分之40至约百分之80和较高浓度惰性气体如氮气、二氧化碳、氦气和氩气的天然气储气传送给分离单元，以便使天然气储气中的惰性气体与甲烷气体分离。这样形成相对较纯的甲烷气流和惰性气体和甲烷气流。若储气氮气含量较高时，可用膜来使氮气与甲烷气体分离，该膜例如Medal膜。当惰性气体是二氧化碳时，可以利用如图2和3所示的低温分离过程使惰性气体与甲烷气体分离。当甲烷气体与惰性气体分离后，分离出来的相对较纯甲烷气体可以传送给如熟知的生产管道质量天然气所用的进一步提纯装置。若惰性气体与甲烷气体分离后，惰性气体和甲烷气流并没有足够的惰性气体用来增大所述燃气轮机的能量输出，那么还可以在惰性气体和甲烷气流中加入惰性气体，以使能量输出比以管道质量天然气作为燃料的燃气轮机增加从约5至约20％。或者，未将惰性气体成分分离的部分天然气气流再与从储气气流中分离出的惰性气体，按所提供的惰性气体增强天然气能使燃气轮机的输出比以管道质量的天然气作为燃料的燃气轮机的增加约5至约20％的量进一步混合。
在一个重要方式中，可以将足量的惰性气体与惰性气体和甲烷气流混合或与天然气储气混合，从而使气体混合物中甲烷含量降低到小于百分之40的体积浓度。参考图1可以看到，在此方式中，将甲烷体积浓度不多于百分之40的惰性气体增强甲烷气体混合物利用物理溶剂处理，在不除去惰性气体的情况下除去硫化氢气体或其他酸性气体成分，从而提供甲烷体积浓度不超过百分之40的脱硫天然气，该物理溶剂例如为甲醇、聚乙二醇二甲醚混合物、碳酸丙二酯、N-甲基-2-吡咯烷酮、低聚乙二醇甲基异丙基醚的混合物、膦酸三正丁酯和氰基乙酸甲酯。物理溶剂处理步骤可以在天然气进料中的惰性气体与甲烷气体分离步骤之前或之后进行。然后，将脱硫天然气通过管道1传送给氧化锌保护床2，以避免硫化氢气体溢出。脱硫天然气从氧化锌保护床2送出，并在管道3中与水混合，从而提供甲烷气体和水混合物。该气体和水混合物在管道3中在约70和约355psig下传送至进料排出物换热器4，在该进料排出物换热器4处，脱硫天然气和水混合物的温度升高至约800。必须将足量的水与天然气混合，以便能足够转变成氢气，从而使该氢气增强的脱硫氢气和惰性气体和甲烷混合气在传送给燃气轮机发电时具有火焰稳定性。当脱硫天然气与水混合并在进料排出物换热器中加热后，加热的脱硫天然气和水混合物通过管道5在约345psig和约800下传送给余热蒸汽发生器盘管6(HRSG盘管)，以便使脱硫天然气和水混合物的温度进一步升高，并在管道3中提供温度为约950的高热脱硫气体和水混合物。然后，该高热脱硫气体和水混合物在约340psig下通过管道7传送给重构反应室8，以便将该脱硫气体和水中的一部分甲烷转变成氢气增强的甲烷和氢气和水混合物。脱硫气体和水混合物中的甲烷在至少约700，优选从约900至约950和约340psig下进行催化反应，使甲烷和水反应生成氢气。更高温度有利于该转变，但是更高压力对该转变有不利影响。压力不应当超过1500psig。在将足量甲烷转变成氢气，使脱水(下文中将介绍)后的气体中含有至少约百分之6体积的氢气之后，该氢气增强的甲烷和氢气和水混合物通过管道9在约855和335psig条件下传送回进料排出物换热器，以便将热量转移给进入该进料排出物换热器的水和甲烷气体。在该氢气增强的甲烷和氢气和水混合物的温度降低后，它通过管道10传送到脱水分离罐(KO罐)12，以减少氢气增强型氢气和惰性气体和甲烷混合气中的含水量。在KO罐中降温到露点，使水能够冷凝并与气体分离。足量的水被除去，使其具有火焰稳定性，且提供热量至少约110BTU/标准立方英尺气体的气体。通常，约百分之97至约百分之99重量的水从该气体中除去。将氢气增强甲烷和氢气和水混合物脱水而生成的水利用冷凝水泵16并通过管道14从KO罐12中排出，并在约100和500psig下通过管道18送回进料排出物换热器4。现在，脱水的含有至少百分之6体积的氢气或含足以提供火焰稳定性氢气的氢气增强型氢气和惰性气体和甲烷混合气从KO罐通过管道20在约100和约psig下供给燃气轮发电机。这些气体的热量至少为约110BTU/标准立方英尺气体，并能为燃气轮发电机提供稳定的火焰。
同样的方法也可以用于所采用的催化剂对天然气中酸性气体不敏感或不受该酸性气体毒化的酸性天然气的应用过程中。不过，为了使该方法适应环保要求，可以至少部分除去至少某些酸性气体，例如H2S。
本发明可通过下面的实例说明。
                                实施例I
                               燃气轮机性能
  现场条件   Units   No Aug   Power Aug
  环境温度      60   60
  环境压力   Psia   11.57   11.57
  环境相对温度   ％   60   60
  进口压降   In H2O   3.0   3.0
  性能
  总发动机输出   KW   156,100   157,100
  热消耗(LHV)   Btu/h×10-8   1,477.1   1,486.9
  热速率(LHV)   Btu/kWh   9,461   9,462
  Misc.   1.8   1.8
  LHV   Btu/Lb   2,424.0   2,424.0
  Btu/Scf   212.5   212.5
  燃气流速   Ib/s   169.3   170.4
  压力   Psia   325   325
  温度      80   80
  Power Aug Inj Conditions
  组成   ％Vol
  二氧化碳   100.0   100.0
  流速   Ib/s   0.0   4.0
  压力   Psia   285   285
  温度      300   300
  排出气条件   Units   No Aug   Power Aug
  排出气流量   Ib/s   925.3   930.4
  排出气温度      1,093.1   1,095.1
  排出气组成   ％Vol
  二氧化碳   13.79   14.12
  氩气   1.07   1.07
  氮气   65.78   65.53
  氧气   9.83   9.74
  水   9.53   9.55
  排气压降   In H2O   15.0   15.0
  NOx(热)   ppmvd@15％O2   ＜10   ＜10
下面是有关图2方法的数据，例示说明本发明的方法，其中高压进料天然气闪蒸成低压，以便使同在该高压供给的天然气中的甲烷气体与二氧化碳气体分离。
下面是有关图3方法的数据，例示说明本发明的方法，其中低压进料天然气利用外部制冷设备冷冻，以便使同在该低压供给的天然气中的甲烷气体与二氧化碳气体分离。
回流2570FWHP 1378Mscfd
  组分   热含量，BTU/SCF   HHVBTU/SCF   过热回收   产物回收
  进料   出售/燃料   燃料   损耗   进料   出售   燃料   损耗
  瞬时Mscfd平均Mscfd瞬时GBTU/D平均GBTU/DHC损失(％)GBTU/D   25001925.0   1378.01061.1   36.928.4   1122.0863.9 734.1565.2 656.9505.8 17.6113.62.38％ 66.851.59.02％ 11.39％
  N2CO2H2SC1C2C3iC4nC4iC5nC5C6+H2O   0.0041080.7129090.0056590.2683710.0051060.0015990.0003990.0003980.0001980.0004920.0007560.000005   0.0074120.5235220.0034710.4589540.0051900.0009800.0001640.0001310.0000420.0000870.0000000.000047   0.0074120.5235220.0034710.4589540.0051900.0009800.0001640.0001310.0000420.0000870.0000000.000047   0.0000500.9455070.0083460.0343040.0050030.0023590.0006880.0007260.000390.00098900   00027194111240   00046492100000   00046492100000   0003596222400   0.00.00.01010.01769.62516.13251.93262.34000.94008.95502.50.0   99％40％34％94％56％34％23％18％12％10％0％   1％60％66％6％44％66％77％82％88％90％100％
  总计   1.000000   1.000000   1.000000   0.998362   294   477   477   60
利用率＝77％
  功率，MW   总计   GT1   GT2   Elec   LM6000
  制冷R404a/C0   0.00   0.00   44,500HP@90F33,184kW@90F6,644热耗，BTU/hP7,096GBTU/D@总功率
  SG1   58.85   58.85
  SG2   0.00   0.00
  CO2注入泵   23.50   23.50
  Condy新鲜气体   0.00   0.00
  功率MW   82.35   0.00   58.85   23.50
  No.of LM6000s   2   0   1   1
  燃料GBTU/D   17.61   -   12.58   5.03
总马力    110,431    HP
HC出售    624        Mscfd HC
          177        HP/Mscfd
                                             2500psi 1200M，45％C1.HSC
                                                  情况(主体)
                                                    气流
  名称   1001   1002   1003   2001   2002
  蒸汽分数   0.0000   1.0000   1.0000   0.9736   0.0000
  温度(F)   712.9   300.0*   300.0*   257.3   80.00*
  压力(psia)   5746.*   5746.*   5746.*   2570.*   2550.
  摩尔流量(MMSCFD)   142.0*   2168.*   2310.   2310.   2310.
  质量流量(lb/hr)   2.809e+05   8.681e+06   8.982e+06   8.962e+06   8.962e+06
  液体体积流量(桶/天)   1.927e+04   8.751e+05   8.944e+05   8.944e+05   8.944e+05
  热流量(kW)   -4.965e+05   -9.053e+06   -9.550e+06   -9.550e+06   -9.842e+06
  组分摩尔分数(氮)   0.00008   0.0041*   0.0038   0.0038   0.0038
  组分摩尔分数(CO2)   0.00008   0.7121*   0.6683   0.6683   0.6683
  组分摩尔分数(H2S)   0.0000*   0.0053*   0.0050   0.0050   0.0050
  组分摩尔分数(甲烷)   0.00008   0.2678*   0.2513   0.2513   0.2513
  组分摩尔分数(乙烷)   0.0000*   0.0051*   0.0048   0.0048   0.0048
  组分摩尔分数(丙烷)   0.0000*   0.0016*   0.0015   0.0015   0.0015
  组分摩尔分数(H2O)   1.0000*   0.0007*   0.0622   0.0622   0.0622
  名称   3000   4001   4050   4100   4101
  蒸汽分数   1.0000   1.0000   0.3125   1.0000   1.0000
  温度(F)   80.85   80.00   9.808   11.65   30.27
  压力(psia)   900.7   2550.   900.0*   900.0   890.00
  摩尔流量(MMSCFD)   1199.   0.0000   1800.   1199.   1199.
  质量流量(lb/hr)   4.080e+06   0.0000   7.210e+06   4.060e+06   4.080e+06
  液体体积流量(桶/天)   4.822e+05   0.0000   7.271e+05   4.822e+05   4.822e+05
  热流量(kW)   -4.039e+06   0.0000   -7.759e+06   -4.080e+06   -4.066e+06
  组分摩尔分数(氮)   0.0074   0.0041   0.0041   0.0074   0.0074
  组分摩尔分数(CO2)   0.5249   0.7083   0.7123   0.5249   0.5249
  组分摩尔分数(H2S)   0.0035   0.0053   0.0053   0.0035   0.0035
  组分摩尔分数(甲烷)   0.4576   0.2668   0.2683   0.4576   0.4576
  组分摩尔分数(乙烷)   0.0052   0.0051   0.0051   0.0052   0.0052
  组分摩尔分数(丙烷)   0.0010   0.0016   0.0016   0.0010   0.0010
  组分摩尔分数(H2O)   0.0000   0.0056   0.0000   0.0000   0.0000
  名称   4110   4111   4210   4215   5001
  蒸汽分数   1.0000   1.0000   0.0000   0.0000   0.0000
  温度(F)   219.6   120.0*   65.00   127.9   80.00
  压力(psia)   3000.*   2980.   900.0   3800.*   2550.
  摩尔流量(MMSCFD)   1199.   1199.   965.0   965.0   2176.
  质量流量(lb/hr)   4.080e+06   4.080e+06   4.585e+06   4.585e+06   8.689e+06
  液体体积流量(桶/天)   4.822e+05   4.822e+05   3.917e+05   3.917e+05   8.755e+05
  热流量(kW)   -4.015e+06   -4.077e+06   -5.165e+06   -5.145e+06   -9.310e+06
  组分摩尔分数(氮)   0.0074   0.0074   0.0000   0.0000   0.0041
  组分摩尔分数(CO2)   0.5249   0.5249   0.9451   0.9451   0.7083
  组分摩尔分数(H2S)   0.0035   0.0035   0.0075   0.0075   0.0053
  组分摩尔分数(甲烷)   0.4576   0.4576   0.0332   0.0332   0.2668
  组分摩尔分数(乙烷)   0.0052   0.0052   0.0050   0.0050   0.0051
  组分摩尔分数(丙烷)   0.0010   0.0010   0.0024   0.0024   0.0016
  组分摩尔分数(H2O)   0.0000   0.0000   0.0000   0.0000   0.0056
                                         2500psi 1200M，45％C1.HSC
                                              情况(主体)
                                                 气流
  名称   5002   5003   5004   5005   5006
  蒸汽分数   1.0000   0.0000   0.0000   0.0000   0.3721
  温度(F)   97.50   69.00*   53.00   53.00   14.30
  压力(psia)   2500.*   2490.   2480.   2480.   900.0*
  摩尔流量(MMSCFD)   2164.   2164.   1800.   363.5   363.5
  质量流量(lb/hr)   8.665e+06   8.665e+06   7.210e+06   1.456e+06   1.456e+06
  液体体体积流量(桶/天)   8.739e+05   8.739e+05   7.271e+05   1.468e+05   1.468e+05
  热流量(kW)   -9.231e+06   -9.281e+06   -7.745e+06   -1.564e+06   -1.564e+06
  组分摩尔分数(氮气)   0.0041   0.0041   0.0041   0.0041   0.0041
  组分摩尔分数(CO2)   0.7123   0.7123   0.7123   0.7123   0.7123
  组分摩尔分数(H2S)   0.0053   0.0053   0.0053   0.0053   0.0053
  组分摩尔分数(甲烷)   0.2683   0.2683   0.2683   0.2683   0.2683
  组分摩尔分数(乙烷)   0.0051   0.0051   0.0051   0.0051   0.0051
  组分摩尔分数(丙烷)   0.0016   0.0016   0.0016   0.0016   0.0016
  组分摩尔分数(H2O)   0.0000   0.0000   0.0000   0.0000   0.0000
  名称   5090   6001   9901   9902   kW(输出)
  蒸汽分数   -   0.0000   0.0000   0.0000   -
  温度(F)   -   80.00   53.00*   43.00*   -
  压力(psia)   15.00*   2550.   2480.   2470.   -
  摩尔流量(MMSCFD)   12.10   134.1   2164.   1800.   -
  质量流量(lb/hr)   2.394e+04   2.726e+05   8.665e+06   7.210e+06   -
  液体体积流量(桶/天)   1642.   1.888e+04   8.739e+05   7.271e+05   -
  热流量(kW)   -   -5.325e+05   -9.309e+06   -7.759e+06   5.119e+04
  组分摩尔分数(氮气)   0.0000   0.0000   0.0041   0.0041   -
  组分摩尔分数(CO2)   0.0000   0.0190   0.7123   0.7123   -
  组分摩尔分数(H2S)   0.0000   0.0003   0.0053   0.0053   -
  组分摩尔分数(甲烷)   0.0000   0.0000   0.2683   0.2683   -
  组分摩尔分数(乙烷)   0.0000   0.0000   0.0051   0.0051   -
  组分摩尔分数(丙烷)   0.0000   0.0000   0.0016   0.0016   -
  组分摩尔分数(H2O)   1.0000   0.9807   0.0000   0.0000   -
  名称   kW(注入泵)   Q(排料)   Q(dummy 3B)   Q(dummy-01)   Q(再沸器A)
  蒸汽分数   -   -   -   -   -
  温度(F)   -   -   -   -   -
  压力(psia)   -   -   -   -   -
  摩尔流量(MMSCFD)   -   -   -   -   -
  质量流量(lb/hr)   -   -   -   -   -
  液体体体积流量(桶/天)   -   -   -   -   -
  热流量(kW)   2.034e+04   6.221e+04   2.747e+04   -   5.053e+04
  组分摩尔分数(氮气)   -   -   -   -   -
  组分摩尔分数(CO2)   -   -   -   -   -
  组分摩尔分数(H2S)   -   -   -   -   -
  组分摩尔分数(甲烷)   -   -   -   -   -
  组分摩尔分数(乙烷)   -   -   -   -   -
  组分摩尔分数(丙烷)   -   -   -   -   -
  组分摩尔分数(H2O)   -   -   -   -   -
回流850PSIA@ 2070FWHP
  组分   热含量，BTU/SCF   HHVBTU/SCF   过热回收   产物回收
  进料   出售/燃料   燃料   损耗   进料   出售   燃料   损耗
  瞬时Mscfd平均Mscfd瞬时GBTU/D平均GBTU/DHC损失(％)GBTU/D   10811027.0   614.8584.1   17.116.3   468.2442.9 317.4301.5 285.9271.6 7.977.82.48％ 27.025.78.42％ 10.90％
  N2CO2H2SC1C2C3iC4nC4iC5nC5C6+H2O   0.0041080.7129090.0056590.2683710.0051060.0015990.0003990.0003980.0001980.0004920.0007560.000005   0.0072070.5352640.0035580.4472000.0052670.0010100.0001680.0001340.0000430.0000870.0000000.000062   0.0072070.5352640.0035580.4472000.0052670.0010100.0001680.0001340.0000430.0000870.0000000.000062   0.0000210.9471780.0084300.0325410.0048940.0023760.0007040.0007460.0004020.00102600   00027194111240   00045293100000   00045293100000   0003396222400   0.00.00.01010.01769.62516.13251.93262.34000.94008.95502.50.0   100％43％36％95％59％36％24％19％12％10％0％   0％57％64％5％41％64％76％81％88％90％100％
  总计   1.000000   1.000000   1.000000   0.998317   294   465   465   58
利用率＝95％
  功率，MW   总计   GT1   GT2   Elec   LM6000
  制冷R404a/C0   0.00   0.00   44,500HP@90F33,184kW@90F6,644热耗，BTU/hp7,096GBTU/D@总功率
  SG1   27.56   27.56
  SG2   0.00   0.00
  CO2注入泵   9.69   9.69
  Condy新鲜气体   0.00   0.00
  总计MW   37.25   0.00   27.56   9.69
  No.of LM6000s   2   0   1   1
  燃料GBTU/D   7.97   -   5.89   2.07
总马力      49,952       HP
HC出售      271          Mscfd HC
            184          HP/Mscfd
                                        Dehy&Reflux塔2070FWHP.hsc
                                          主体：气流
                                              气流
  名称   1001   1002   1003   2001   2002
  蒸汽分数   0.0000   1.0000   1.0000   0.9681   0.9408
  温度(F)   712.9   300.0*   300.0*   244.0   80.00*
  压力(psia)   5746.*   5746.*   5748.   2070.*   2050.
  摩尔流量(MMSCFD)   71.00*   1084.*   1155.   1155.   1155.
  质量流量(lb/hr)   1.404e+05   4.340e+06   4.481e+06   4.481e+06   4.481e+06
  液体体积流量(桶/天)   9636.   4.376e+05   4.472e+05   4.472e+05   4.472e+05
  热流量(kW)   -2.483e+05   -4.527e+06   -4.775e+06   -4.775e+06   -4.911e+06
  组分摩尔分数(氮气)   0.0000*   0.0041*   0.0038   0.0038   0.0038
  组分摩尔分数(CO2)   0.0000*   0.7121*   0.6683   0.6683   0.6683
  组分摩尔分数(H2S)   0.0000*   0.0053*   0.0050   0.0050   0.0050
  组分摩尔分数(甲烷)   0.0000*   0.2678*   0.2513   0.2513   0.2513
  组分摩尔分数(乙烷)   0.0000*   0.0051*   0.0048   0.0048   0.0048
  组分摩尔分数(丙烷)   0.0000*   0.0016*   0.0015   0.0015   0.0015
  组分摩尔分数(H2O)   1.0000*   0.0007*   0.0622   0.0622   0.0622
  名称   3000   4001   4050   4100   4101
  蒸汽分数   -   1.0000   0.3738   1.0000   1.0000
  温度(F)   -   80.00   9.978   10.99   26.03
  压力(psia)   -   2050.   850.0*   850.0   840.00
  摩尔流量(MMSCFD)   -   1087.   900.0   614.7   614.7
  质量流量(lb/hr)   -   4.342e+06   3.604e+06   2.112e+08   2.112e+06
  液体体积流量(桶/天)   -   4.376e+05   3.635e+05   2.472e+05   2.472e+05
  热流量(kW)   -   -4.639e+06   -3.874e+06   -2.118e+06   -2.113e+06
  组分摩尔分数(氮气)   -   0.0041   0.0041   0.0072   0.0072
  组分摩尔分数(CO2)   -   0.7092   0.7123   0.5352   0.5352
  组分摩尔分数(H2S)   -   0.0053   0.0053   0.0036   0.0036
  组分摩尔分数(甲烷)   -   0.2672   0.2683   0.4473   0.4473
  组分摩尔分数(乙烷)   -   0.0051   0.0051   0.0053   0.0053
  组分摩尔分数(丙烷)   -   0.0016   0.0016   0.0010   0.0010
  组分摩尔分数(H2O)   -   0.0043   0.0000   0.0000   0.0000
  名称   4110   4210   4215   5001   5002
  蒸汽分数   1.0000   0.0000   0.0000   0.0000   1.0000
  温度(F)   225.2   60.01   118.6   60.00   82.33
  压力(psia)   3000.*   850.0   3800.*   2050.   2000.*
  摩尔流量(MMSCFD)   614.7   467.2   467.2   0.0000   1082.
  质量流量(lb/hr)   2.112e+06   2.221e+06   2.221e+06   0.0000   4.333e+06
  液体体积流量(桶/天)   2.472e+05   1.897e+05   1.897e+05   0.0000   4.389e+05
  热流量(kW)   -2.085e+06   -2.504e+06   -2.495e+06   0.0000   -4.617e+06
  组分摩尔分数(氮气)   0.0072   0.0000   0.0000   0.0041*   0.0041
  组分摩尔分数(CO2)   0.5352   0.9453   0.9453   0.7092*   0.7123
  组分摩尔分数(H2S)   0.0036   0.0076   0.0076   0.0053*   0.0053
  组分摩尔分数(甲烷)   0.4473   0.0328   0.0328   0.2672*   0.2683
  组分摩尔分数(乙烷)   0.0053   0.0049   0.0049   0.0051*   0.0051
  组分摩尔分数(丙烷)   0.0010   0.0024   0.0024   0.0016*   0.0016
  组分摩尔分数(H2O)   0.0000   0.0000   0.0000   0.0043*   0.0000
                                          Dehy&Reflux塔2070FWHP.hsc
                                               主体：气流
                                                  气流
  名称   5003   5004   5005   5006   5090
  蒸汽分数   1.0000   0.0000   0.0000   0.4201   -
  温度(F)   62.00*   50.00   50.00   13.33   -
  压力(psia)   1990.   1980.   1980.   850.0*   15.00*
  摩尔流量(MMSCFD)   1082.   900.0*   181.9   181.9   4.671
  质量流量(lb/hr)   4.333e+06   3.604e+06   7.285e+05   7.285e+05   9239.
  液体体积流量(桶/天)   4.369e+05   3.635e+05   7.348e+04   7.346e+04   633.9
  热流量(kW)   -4.639e+06   -3.869e+06   -7.819e+05   -7.819e+05   -2.193e+04
  组分摩尔分数(氮气)   0.0041   0.0041   0.0041   0.0041   0.0000
  组分摩尔分数(CO2)   0.7123   0.7123   0.7123   0.7123   0.0000
  组分摩尔分数(H2S)   0.0053   0.0053   0.0053   0.0053   0.0000
  组分摩尔分数(甲烷)   0.2683   0.2883   0.2683   0.2683   0.0000
  组分摩尔分数(乙烷)   0.0051   0.0051   0.0051   0.0051   0.0000
  组分摩尔分数(丙烷)   0.0016   0.9016   0.0016   0.0016   0.0000
  组分摩尔分数(H2O)   0.0000   0.0000   0.0000   0.0000   1.0000
  名称   6001   9901   9902   Kw(输出)   kW(注入泵)
  蒸汽分数   0.0000   0.0000   0.0000   -   -
  温度(F)   80.00   50.00*   43.00*   -   -
  压力(psia)   2050.   1980.   1970.   -   -
  摩尔流量(MMSCFD)   68.43   1082.   900.0   -   -
  质量流量(lb/hr)   1.390e+05   4.333e+06   3.604e+06   -   -
  液体体积流量(桶/天)   9630   4.369e+05   3.835e+05   -   -
  热流量(kW)   -2.718e+05   -4.651e+06   -3.874e+06   2.756e+04   9694.
  组分摩尔分数(氮气)   0.0000   0.0041   0.0041   -   -
  组分摩尔分数(CO2)   0.0187   0.7123   0.7123   -   -
  组分摩尔分数(H2S)   0.0003   0.0053   0.0053   -   -
  组分摩尔分数(甲烷)   0.0000   0.2683   0.2683   -   -
  组分摩尔分数(乙烷)   0.0000   0.0051   0.0051   -   -
  组分摩尔分数(丙烷)   0.0000   0.0016   0.0016   -   -
  组分摩尔分数(H2O)   0.9810   0.0000   0.0000   -   -
  名称   Q(dummy 3B)   Q(再沸器A)   Q(再沸器-A)   Q(Sea1)   Q(SW冷却器)
  蒸汽分数   -   -   -   -   -
  温度(F)   -   -   -   -   -
  压力(psia)   -   -   -   -   -
  摩尔流量(MMSCFD)   -   -   -   -   -
  质量流量(lb/hr)   -   -   -   -   -
  液体体积流量(桶/天)   -   -   -   -   -
  热流量(kW)   1.206e+04   2.142e+04   2.141e+04   -   1.360e+05
  组分摩尔分数(氮气)   -   -   -   -   -
  组分摩尔分数(CO2)   -   -   -   -   -
  组分摩尔分数(H2S)   -   -   -   -   -
  组分摩尔分数(甲烷)   -   -   -   -   -
  组分摩尔分数(乙烷)   -   -   -   -   -
  组分摩尔分数(丙烷)   -   -   -   -   -
  组分摩尔分数(H2O)   -   -   -   -   -

Claims (5)

1.一种用甲烷体积浓度为百分之40至百分之80的天然气储气中的甲烷气体向燃气轮机供给燃料的方法，该方法包括：
由天然气储气提供第一天然气气流；
将第一天然气气流中的惰性气体与甲烷气体分离，提供分离的甲烷气体和分离的惰性气体；
将分离的惰性气体、氢气和甲烷体积浓度为百分之40至百分之80的第二天然气气流混合，提供氢气增强的惰性气体和甲烷气体和氢气气体混合物，其中，与第二天然气气流混合的惰性气体量将使甲烷气体相对于惰性气体和甲烷气体总体积的甲烷体积百分比降低到约百分之40以下，混合的氢气量应能有效提供该氢气增强的惰性气体和甲烷气体和氢气气体混合物的火焰稳定性；以及
用该氢气增强的惰性气体和甲烷气体和氢气气体混合物向燃气轮机供给燃料。
2.根据权利要求1所述的向燃气轮机供给燃料的方法，其中氢气增强的惰性气体和甲烷气体和氢气气体混合物包括至少百分之6体积的氢气。
3.根据权利要求1所述的向燃气轮机供给燃料的方法，该方法进一步包括使天然气或氢气增强的惰性气体和甲烷气体和氢气气体混合物脱水的步骤，该脱水步骤能够有效使氢气增强的惰性气体和甲烷气体和氢气气体混合物具有至少110BTU/标准立方英尺气体的热量。
4.根据权利要求1或3所述的向燃气轮机供给燃料的方法，其中基于甲烷和惰性气总体积计，分离的惰性气体中含有小于百分之35体积的甲烷，而氢气增强的惰性气体、甲烷气体和氢气气体混合物含有百分之6至百分之10体积的氢气。
5.根据权利要求1或3所述的向燃气轮机供给燃料的方法，其中基于甲烷和惰性气体总体积计，该分离的惰性气体中含有小于百分之20体积的甲烷，而氢气增强的惰性气体和甲烷气体和氢气气体混合物含百分之6至百分之10体积的氢气。
CNB2004100978646A 1999-12-13 2000-12-13 用低甲烷浓度和高惰性气体浓度的储气向燃气轮机供给燃料的方法 Expired - Fee Related CN100338344C (zh)

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US09/460,149 1999-12-13
US09/460,149 US6298652B1 (en) 1999-12-13 1999-12-13 Method for utilizing gas reserves with low methane concentrations and high inert gas concentrations for fueling gas turbines

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HK1053667A1 (en) 2003-10-31
CN1414999A (zh) 2003-04-30
AU779291C (en) 2007-12-13
US20030084668A1 (en) 2003-05-08
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EP1240279B1 (en) 2005-11-16
HK1082785A1 (en) 2006-06-16
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HK1082784A1 (en) 2006-06-16
US20050182283A1 (en) 2005-08-18
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US7350359B2 (en) 2008-04-01
CN1651737A (zh) 2005-08-10
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US6298652B1 (en) 2001-10-09
CN1304741C (zh) 2007-03-14
CN1651739A (zh) 2005-08-10
CN1304742C (zh) 2007-03-14
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US6907737B2 (en) 2005-06-21
EP1240279A1 (en) 2002-09-18
ATE310068T1 (de) 2005-12-15
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