CN101622054A - 减少发电装置中二氧化碳排放的方法 - Google Patents
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Abstract
一种用于减少发电装置中CO2排放的方法，其中所述发电装置包括至少一个与热回收蒸汽发生器设备偶联的燃气轮机，和CO2捕集设备包括吸收器和再生器，所述方法包括如下步骤：(a)将离开具有一定高压的燃气轮机的热废气加入热回收蒸汽发生器设备中，以产生蒸汽和含二氧化碳的烟气物流；(b)通过在具有高操作压力的吸收器中使含二氧化碳的烟气物流与吸收液体接触而从所述烟气物流中脱除二氧化碳，以获得富含二氧化碳的吸收液体和纯化的烟气物流，其中调节燃气轮机的设置和/或构造使得离开燃气轮机的热废气的压力为吸收器的高操作压力的至少40％。
Description
技术领域
本发明涉及减少发电装置中二氧化碳(CO2)排放的方法。
背景技术
世界上大部分能量供应通过在发电装置中燃烧燃料、特别是天然气或合成气而提供。通常在一个或多个燃气轮机中燃烧燃料，和将所得气体用于产生蒸汽。随后将蒸汽用于发电。燃料燃烧导致产生CO2。在最近的几十年中，排放至大气的CO2量在全球范围内已经明显增大。按Kyoto协议，必须减少CO2排放，以防止或抵消不希望的气候变化。
燃气轮机烟气的CO2浓度取决于所应用的燃料和燃烧以及热回收过程，和一般相对低，通常为3-15％。因此，减少CO2排放使得希望从废气中分离出CO2，因为压缩和存放全部烟气物流过于昂贵。因为这个原因，所以使用专用的CO2捕集设备以从烟气物流中脱除CO2和从而产生浓缩的CO2物流是有利的。
例如在EP 1,688,173中描述了这样的方法，其中描述了使用具有吸收器和再生器的CO2捕集设备的用于在海上平台上回收二氧化碳和发电的方法。在进入吸收器之前，使用鼓风机对含CO2的废气加压。对该鼓风机的需求增大了方法的总成本和操作复杂性。
目前已经发现当产生加压的含CO2的废气时，可以实现更简化的方法。
发明内容
为此，本发明提供用于减少发电装置中CO2排放的方法，其中所述发电装置包括至少一个与热回收蒸汽发生器设备偶联的燃气轮机，和CO2捕集设备包括吸收器和再生器，所述方法包括如下步骤：
(a)将离开具有一定高压的燃气轮机的热废气加入热回收蒸汽发生器设备中，以产生蒸汽和含二氧化碳的烟气物流；
(b)通过在具有高操作压力的吸收器中使含二氧化碳的烟气物流与吸收液体接触而从所述烟气物流中脱除二氧化碳，以获得富含二氧化碳的吸收液体和纯化的烟气物流，其中调节燃气轮机的设置使得离开燃气轮机的热废气的压力为吸收器的高操作压力的至少40％。
具体实施方式
在所述方法中，使用包括至少一个燃气轮机的发电装置。通常，将燃料和含氧气体加入燃气轮机的燃烧区中。在燃气轮机的燃烧区中，燃料燃烧从而产生热燃烧气。热燃烧气在燃气轮机中膨胀(通常经由排列成行的膨胀器叶片序列)，和用于通过发电机发电。在燃气轮机中燃烧的适合燃料包括天然气和合成气。
在步骤(a)中，将离开燃气轮机的热废气引入热回收蒸汽发生器设备中。离开燃气轮机的热废气具有一定的高压。热废气的压力由燃气轮机的设置和/或构造决定。例如，通常燃气轮机包括排列成行的膨胀器叶片序列：通过改变膨胀器叶片行数，可以增大燃气轮机的背压，导致热废气具有高压。在所述方法中，调节燃气轮机的设置和/或构造，使得离开燃气轮机的热废气的压力为CO2捕集设备中的吸收器的操作压力的至少40％。优选地，离开燃气轮机的热废气的压力为吸收器的高操作压力的至少50％，更优选为至少60％，仍然更优选为至少70％。
决定燃气轮机电功输出的因素之一是燃气轮机的入口和出口之间的压力差。不希望被具体的理论所束缚，假定更大的压力差将导致更高的电功输出。更大的压力差通常意味着燃气轮机的入口压力将高和出口压力将尽可能接近环境。在所述方法中，调节燃气轮机的设置和/或构造，使得出口压力有目的地升高，这意味着出口压力高于环境压力。结果是，燃气轮机的电功输出将略微低于出口压力接近环境压力的燃气轮机。已经发现，尽管燃气轮机电功输出略低，但是整个过程仍然是更有利的，因为CO2捕集设备的能量需求明显较低。现在，在进入CO2捕集设备的吸收器之前，烟气需要少量加压或不需要加压。因此，现在可以省却在进入CO2吸收器之前通常用于使烟气物流加压的昂贵的和耗能的设备。
优选地，热废气的温度为350-700℃，更优选400-650℃。热废气的组成可以变化，取决于燃气轮机中燃烧的燃料气体和燃气轮机中的条件。通常，热废气含有10-15％的O2。通常，热废气含有3-6％的CO2。
热回收蒸汽发生器设备是提供从热废气中回收热量和将该热量转化成蒸汽的工具的任意设备。例如，热回收蒸汽发生器设备可以包括多根堆叠方式安装的管。将水泵送和循环通过所述管，并可以保持在高温高压下。热废气加热所述管，和用于产生蒸汽。可以设计热回收蒸汽发生器设备，以产生一种、两种或三种类型的蒸汽：高压蒸汽、中压蒸汽和低压蒸汽。
优选地，设计蒸汽发生器以产生至少一定量的高压蒸汽，因为高压蒸汽可用于发电。适合地，高压蒸汽的压力为90-150bara，优选为90-125bara，更优选为100-115bara。适合地，也产生低压蒸汽，低压蒸汽压力优选为2-10bara，更优选至8bara，仍然更优选4-6bara。该低压蒸汽用于使含CO2的吸收液体再生。
在优选实施方案中，在热回收蒸汽发生设备中燃烧一定量的燃料，以产生附加蒸汽。该实施方案提供通过调节加入热回收蒸汽发生器设备的燃料量而控制热回收蒸汽发生器设备中产生的蒸汽的量和类型的可能性。优选地，使用低压蒸汽管路以将加热蒸汽从热回收蒸汽发生器输送至CO2捕集设备。适合地，以闭合回路排列低压蒸汽管路，以使产生的用于发电的蒸汽与过程换热器中使用的蒸汽隔离。
热回收蒸汽发生器设备排出含CO2的烟气。烟气的组成除了其它的以外取决于燃气轮机中使用的燃料类型。适合地，烟气包含0.25-30％(v/v)的CO2，优选1-20％(v/v)。烟气通常还含有氧，优选为0.25-20％(v/v)，更优选5-15％(v/v)，仍然更优选1-10％(v/v)。
在步骤(b)中，通过在高压下使烟气与吸收液体接触而脱除CO2，适合地在吸收器中进行。适合地，吸收在相对低温下和在高操作压力下发生。高压表示CO2吸收器的操作压力高于环境压力。优选地，吸收器的操作压力为50-200mbarg，更优选70-150mbarg。因为烟气已经具有高压，所以烟气压力和吸收器操作压力之间的压力差相对小。因此，在进入吸收器之前，烟气不需要被加压或需要被加压至较低的程度。考虑到大量烟气待加压，使用更小的鼓风机或完全取消鼓风机将导致对整个过程的相当可观的成本节省。因为烟气的温度通常相对高，所以优选在进入吸收器之前使烟气冷却。
吸收液体可以是能够从烟气物流中脱除CO2的任意吸收液体，所述烟气物流包含氧和具有相对低浓度的CO2。该吸收液体可包括化学和物理溶剂或这些的组合。
适合的物理溶剂包括聚乙二醇的二甲基醚化合物。
适合的化学溶剂包括氨和胺化合物。
在一个实施方案中，吸收液体包含选自单乙醇胺(MEA)、二乙醇胺(DEA)、二甘醇胺(DGA)、甲基二乙醇胺(MDEA)和三乙醇胺(TEA)的一种或多种胺。MEA是特别优选的胺，因为它能够吸收相对高百分数的CO2(体积CO2/体积MEA)。因此，包含MEA的吸收液体适合于从具有低浓度CO2、通常是3-10体积％CO2的烟气中脱除CO2。
在另一个实施方案中，吸收液体包含选自甲基二乙醇胺(MDEA)、三乙醇胺(TEA)、N，N′-二(羟基烷基)哌嗪、N，N，N′，N′-四(羟基烷基)-1，6-己二胺和叔烷基胺磺酸化合物的一种或多种胺。
优选地，N，N′-二(羟基烷基)哌嗪是N，N′-二-(2-羟基乙基)哌嗪和/或N，N′-二-(3-羟基丙基)哌嗪。
优选地，四(羟基烷基)-1，6-己二胺是N，N，N′，N′-四(2-羟基乙基)-1，6-己二胺和/或N，N，N′，N′-四(2-羟基丙基)-1，6-己二胺。
优选地，叔烷基胺磺酸化合物选自4-(2-羟基乙基)-1-哌嗪乙烷磺酸、4-(2-羟基乙基)-1-哌嗪丙烷磺酸、4-(2-羟基乙基)哌嗪-1-(2-羟基丙烷磺酸)和1，4-哌嗪二(磺酸)。
在又一个实施方案中，吸收液体包含N-乙基二乙醇胺(EDEA)。
在特别优选的实施方案中，吸收液体包含氨。
在烟气物流包含可测量量的氧、适合地为1-20％(v/v)的氧的情况下，优选将缓蚀剂加入吸收液体。适合的缓蚀剂为例如US 6,036,888中描述的。
在大多数情况下，希望拥有连续的过程，包括吸收液体的再生。因此，优选所述方法还包括步骤(c)：通过在再生器中在高温下使富含二氧化碳的吸收液体与汽提气体接触而使富含二氧化碳的吸收液体再生，以获得再生的吸收液体和富含二氧化碳的气体物流。应理解，用于再生的条件尤其取决于吸收液体的类型和吸收步骤中使用的条件。适合地，再生在与吸收不同的温度和/或不同的压力下发生。
在吸收液体包含胺的情况下，优选再生温度为100-200℃。在吸收液体包含含水胺的情况下，再生优选在1-5bara的压力下发生。
在吸收液体包含氨的情况下，适合地，吸收步骤在低于环境温度的温度下进行，优选为0-10℃，更优选为2-8℃。再生步骤适合地在比吸收步骤中使用的更高的温度下进行。当使用含氨的吸收液体时，离开再生器的富含CO2的气体物流具有高压。适合地，富含CO2的气体物流的压力为5-8bara，优选6-8bara。在其中富含CO2的气体物流需要在高压下的应用中，例如当将它用于注入地下地层中时，有利之处是富含CO2的气体物流已经在高压下。通常，需要一系列的压缩机，以将富含CO2的气体物流加压至所需高压。已经在高压下的富含CO2的气体物流更容易进行进一步加压。
任选地，所述方法还包括步骤(d)：在热回收蒸汽发生设备中燃烧一定量的燃料，以产生附加蒸汽。优选地，通过使用附加量的蒸汽，至少部分满足了再生步骤的热量需求。燃烧的燃料量优选使得附加量的蒸汽足以提供用于使吸收液体再生所需热量的至少80％，更优选至少90％，仍然更优选至少95％和最优选100％。
进行步骤(d)的优选方式是监控由热回收蒸汽发生器设备产生的电，和根据电量调节加入热回收蒸汽发生器设备中的燃料量。如前面所解释的，在热回收蒸汽发生器设备中，优选在蒸汽涡轮中产生高压蒸汽，将所述高压蒸汽例如经由与蒸汽涡轮偶联的发电机转化成电。当CO2捕集设备运转时，由于用于加热CO2捕集设备的再生器所需的从热回收蒸汽发生器设备中抽出的蒸汽量，使得与蒸汽涡轮偶联的发电机的电功输出将下降。通过监控热回收发生器设备的与蒸汽涡轮偶联的发电机的输出，可以调节热回收蒸汽发生器设备中燃烧的燃料量。在输出下降的情况下，可以增大燃烧的燃料量。优选地，在不明显降低与蒸汽涡轮偶联的发电机的电功输出的条件下，预先确定为了能够满足CO2捕集设备的再生器的热量需求而燃烧的燃料量。将CO2捕集设备未运转时与蒸汽涡轮偶联的发电机的电功输出作为基准，和随后确定为了实现相同输出而燃烧的燃料量。
在热回收蒸汽发生器设备中燃烧的适合燃料包括天然气和合成气。
步骤(d)中一定量燃料的燃烧需要存在氧。可以将该氧供应至热回收蒸汽发生器设备，但优选热废气含有氧，和该氧的至少一部分用于步骤(d)的燃料燃烧中。作为使用来自热废气的氧的结果，离开热回收蒸汽发生器设备的烟气中氧量将更低。这有利于CO2吸收过程，特别是当使用胺吸收液体时。氧可以导致胺降解，和可以导致吸收液体中降解产物的形成。因此，烟气的氧含量更低将导致更少的胺降解和更少的降解产物的形成。
优选地，使用二氧化碳压缩机使富含二氧化碳的气体物流加压，以产生加压的二氧化碳物流。需要驱动二氧化碳压缩机。当热回收蒸汽发生器设备中产生的部分蒸汽用于驱动二氧化碳压缩机时，实现了良好的热联合。
优选地，加压CO2物流的压力为40-300bara，更优选50-300bara。可以将具有这些优选范围内压力的CO2物流用于多种目的，特别是用于强化油、煤层甲烷的采收、或用于地下地层中的隔离。特别是对于其中将加压CO2物流注入地下地层中的目的，需要高压。在优选实施方案中，将加压CO2物流用于强化油采收。通过将CO2注入油储层中，可以增大油采收率。通常，将加压CO2物流注入油储层中，其中它与存在的一些油混合。CO2和油的混合物将置换出通过传统注入不能置换出的油。
下面将参考附图1仅以举例方式描述本发明。
在图1中，显示了包括燃气轮机(1)、热回收蒸汽发生器设备(2)和CO2捕集设备(3)的发电装置。在燃气轮机中，将含氧气体经管线4供应至压缩机5。将燃料经管线6供应至燃烧器7，和在压缩的含氧气体存在下燃烧。将所得燃烧气在膨胀器8中膨胀，和用于在发电机9中发电。将含CO2和氧的剩余废气经管线10导向热回收蒸汽发生器设备2。在热回收蒸汽发生器设备中，在加热区11中用热废气加热水以产生蒸汽。将蒸汽经管线12导入蒸汽涡轮13中，以在发电机14中产生附加电功。任选地，将一定量的燃料经管线15导入热回收蒸汽发生器设备和利用来自废气的氧燃烧，以产生附加蒸汽。将含CO2和氧并具有增大的压力的热烟气经管线16导入胺吸收器17。优选地，将热烟气首先在冷却器(未显示)中冷却。在胺吸收器17中，CO2从烟气中转移至胺吸收器内含有的胺液体中。将贫含二氧化碳的纯化的烟气经管线18从胺吸收器中导出。将富含CO2的胺液体经管线19从胺吸收器导入再生器20。在再生器中，使富含CO2的胺液体减压，和在高温下与汽提气体接触，从而将CO2从胺液体中转移至汽提气体中，以获得再生的胺液体和富含CO2的气体物流。将富含CO2的气体物流经管线21从再生器中导出。优选地，使用CO2压缩机(未显示)使富含CO2的气体物流加压，和在其它位置使用加压CO2物流。将再生的胺液体经管线22从再生器导入胺吸收器。利用经管线23从蒸汽涡轮13导入再生器的低压蒸汽供应为提供再生器高温所需的热量。
Claims (10)
1.一种用于减少发电装置中CO2排放的方法，其中所述发电装置包括至少一个与热回收蒸汽发生器设备偶联的燃气轮机，和CO2捕集设备包括吸收器和再生器，所述方法包括如下步骤：
(a)将离开具有一定高压的燃气轮机的热废气加入热回收蒸汽发生器设备中，以产生蒸汽和含二氧化碳的烟气物流；
(b)通过在具有高操作压力的吸收器中使含二氧化碳的烟气物流与吸收液体接触而从所述烟气物流中脱除二氧化碳，以获得富含二氧化碳的吸收液体和纯化的烟气物流，其中调节燃气轮机的设置和/或构造使得离开燃气轮机的热废气的压力为吸收器的高操作压力的至少40％。
2.权利要求1的方法，其中离开燃气轮机的热废气的压力为吸收器的高操作压力的至少50％，优选至少60％，更优选至少70％。
3.权利要求1或2的方法，其中吸收器的高操作压力为50-200mbarg，优选70-150mbarg。
4.权利要求1-3任一项的方法，还包括如下步骤：
(c)通过在再生器中在高温下使富含二氧化碳的吸收液体与汽提气体接触而使富含二氧化碳的吸收液体再生，以获得再生的吸收液体和富含二氧化碳的气体物流。
5.权利要求1-4任一项的方法，所述方法还包括如下步骤：
(d)利用二氧化碳压缩机使富含二氧化碳的气体物流加压，其中优选将热回收蒸汽发生器设备中产生的蒸汽的第一部分用于驱动二氧化碳压缩机。
6.前述权利要求任一项的方法，其中在热回收蒸汽发生器设备中燃烧一定量的燃料，以产生附加量的蒸汽，其中优选热回收蒸汽发生器设备中燃烧的燃料量使得附加量的蒸汽足以提供使吸收液体再生所需热量的至少80％。
7.前述权利要求任一项的方法，其中热回收蒸汽发生器设备中产生的至少部分蒸汽是高压蒸汽，优选压力为90-125bara，更优选为100-115bara。
8.权利要求5-7任一项的方法，其中将加压的富含二氧化碳的气体物流用于强化油采收。
9.前述权利要求任一项的方法，其中吸收液体包含胺，优选为选自单乙醇胺(MEA)、二乙醇胺(DEA)、二甘醇胺(DGA)、甲基二乙醇胺(MDEA)、三乙醇胺(TEA)、N-乙基二乙醇胺(EDEA)、N，N′-二(羟基烷基)哌嗪、N，N，N′，N′-四(羟基烷基)-1，6-己二胺和叔烷基胺磺酸化合物的一种或多种胺。
10.权利要求1-8任一项的方法，其中吸收液体包含物理溶剂或氨。
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- 2008-01-23 WO PCT/EP2008/050735 patent/WO2008090168A1/en active Application Filing
- 2008-01-23 JP JP2009546747A patent/JP5574710B2/ja active Active
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Cited By (6)
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| CN101766948A (zh) * | 2010-03-11 | 2010-07-07 | 南京信息工程大学 | 用于膜接触器捕集co2气体的复合溶液 |
| CN101766948B (zh) * | 2010-03-11 | 2011-12-14 | 南京信息工程大学 | 用于膜接触器捕集co2气体的复合溶液 |
| CN102454481A (zh) * | 2010-10-22 | 2012-05-16 | 通用电气公司 | 包括二氧化碳收集***的联合循环动力装置 |
| CN102454481B (zh) * | 2010-10-22 | 2015-11-25 | 通用电气公司 | 包括二氧化碳收集***的联合循环动力装置 |
| CN103534444A (zh) * | 2011-03-31 | 2014-01-22 | 阿尔斯通技术有限公司 | 用于控制co2捕获用废热的***和方法 |
| CN104641079A (zh) * | 2012-03-29 | 2015-05-20 | 阿尔斯通技术有限公司 | 用于操作联合循环发电设备的方法和使用该方法的联合循环发电设备 |
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|---|---|
| AU2008208882B2 (en) | 2011-04-14 |
| JP2010516941A (ja) | 2010-05-20 |
| WO2008090168A1 (en) | 2008-07-31 |
| ATE553832T1 (de) | 2012-05-15 |
| CA2676088A1 (en) | 2008-07-31 |
| AU2008208882A1 (en) | 2008-07-31 |
| EP2107930B1 (en) | 2012-04-18 |
| CN101622054B (zh) | 2012-12-05 |
| JP5574710B2 (ja) | 2014-08-20 |
| US20100162703A1 (en) | 2010-07-01 |
| CA2676088C (en) | 2015-05-26 |
| EP2107930A1 (en) | 2009-10-14 |
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