CN1116501C - 利用烃类原料生产电能、蒸汽和二氧化碳的工艺 - Google Patents

利用烃类原料生产电能、蒸汽和二氧化碳的工艺 Download PDF

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CN1116501C
CN1116501C CN98814162A CN98814162A CN1116501C CN 1116501 C CN1116501 C CN 1116501C CN 98814162 A CN98814162 A CN 98814162A CN 98814162 A CN98814162 A CN 98814162A CN 1116501 C CN1116501 C CN 1116501C
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gas
unit
turbine
steam
atr
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CN1301327A (zh
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H·O·弗杰尔霍格
H·R·尼尔森
W·索伊兹
M·赛格尼
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

本发明涉及一种利用烃类原料来生产电能、蒸汽和二氧化碳的工艺，所述的二氧化碳为浓缩的形式，该工艺包括：在一个空气驱动的自热反应器(ATR)单元中形成合成气体、对形成的合成气体进行热量交换以产生蒸汽、在一个一氧化碳转移反应器单元和二氧化碳分离单元中处理至少一部分合成气体以形成浓缩的二氧化碳和贫的含氢气体，所述气体的至少一部分在一个联成循环气轮机中燃烧而产生电能，其中，来自于所述气轮机单元的空气被供应至ATR单元，来自于气轮机的废气进行热交换而形成蒸汽，所述的蒸汽与上游产生的蒸汽一起用来在蒸汽气轮机中产生基本无CO2的电能。所述蒸汽可被输送到气轮机来稀释含氢气体混合物。该工艺可与生产合成气体产品如甲醇和/或氨气的工艺联合使用。可在燃料电池中利用来自于二氧化碳去除单元的一部分气体。

Description

利用烃类原料生产电能、蒸汽和二氧化碳的工艺
本发明涉及一种利用烃类原料生产电能、蒸汽和浓缩形式的二氧化碳产品的工艺。本发明还包括与所述的工艺相结合选择生产基于合成气体的产品。
电能是在一个与转化厂结合为一体的联合循环电厂中生产出来的，其中气轮机是以含氢气体为燃料。(整体式转化联合循环(IRCC))。这个工艺中的一个主要问题是在氮氧化物排放量最小同时得到最优化的电能和蒸汽的条件下操纵气轮机。
在互联网上的网址为http：/www.hydro.com/konsern/news/eng/1998/980423e.html处公开了一种用来生产电能、蒸汽和浓缩的二氧化碳的工艺。在这个公开文件中描述了这样一种生产工艺，包括：天然气与蒸汽反应而产生含氢气体，所述气体在一个联合循环式气轮机中燃烧而产生电能。
从日本专利申请JP608041中还可进一步了解到利用一种燃烧氢气的涡轮机来生产电能。根据这个申请文件，通过部分氧化所述燃料而使1∶0.5至1∶0.7的摩尔比的天然气和氧气反应来产生氢和一氧化碳。将空气供应到一个压力变动氧气吸附分离器(PSA)中，然后所述氧气被输送到一个自热反应器(ATR)中，在所述的自供热反应器(ATR)中，天然气就被转化为氢和一氧化碳。被转化的气体进入一个转移反应器中，在所述的转移反应器中，一氧化碳转化为二氧化碳。然后气体混合物被引导入一个隔膜分离器中，在所述的隔膜分离器中，氢气从二氧化碳中分离出来。分离出的CO2被冲洗掉，然后排出。基本不含含碳化合物的氢被用于气轮机中来产生电能。这个工艺需要氧气并需要一个动力消耗PSA单元。根据该申请的流程图，天然气必须被减压至接近周围压力才允许添加氧气。在PSA中分离后，必须对氧气进行二次压缩。所有这些额外的压缩均降低了该工艺的效率。
本发明的一个主要目的是提供一种利用烃类原料蒸汽转化的改进的发电的工艺，其中产生的相当一部分CO2以高度浓缩的CO2气流的形式而分离出来且氮氧化物的排放量在常规气轮机接受的水平之内。
本发明的另一个目的是利用在所述电能产生过程中形成的合成气体的至少一部分来生产合成气体产品，特别是氨、甲醇和/或二甲醚。
对于产生电能来说，本发明可与以燃烧烃类原料如天然气为基础的传统电厂相竞争。但是，仅燃烧烃类的一个主要的缺点是二氧化碳的排放，因为燃烧废气只有少量的二氧化碳，目前不能经济地回收。氮氧化物(NOX)的排放根据运行状况的变化而变化，这也构成了一个排放的问题。
在减少二氧化碳和氮氧化物(NOX)的排放时的一个主要的问题在于：获得所需要的排放减少量，而不使发电过程的效率的降低至不可接受的程度。根据上面的要求，在评价基本工艺中的第一步为合成气体的生产步骤。发明人通过考虑不同的工艺发现自热反应器(ATR)可具有多种优点并决定进一步寻找最好的工艺来运行自供热反应器(ATR)。与上面所述的日本专利申请中的教导相反，本申请发明人发现自热反应器(ATR)应该是一个空气驱动反应器，也就是说，该反应器不是一个氧气驱动反应器。ATR的应用从灵活性的角度来讲存在多种优势。这样，运行的压力可根据整体的经济性原则来选择。甲烷减少率(slip)可根据下游单元的操作而变化，最后在ATR中产生的合成气体为适于气体驱动气轮机的较贫气体，并与现存在的大规模联合循环电厂(IRCC)中应用的燃料混合物相当。
适用于该工艺的烃类原料为天然气、石脑油、各种汽油馏分等。通过在ATR之前应用一个预先转化器，原料就会具有较大的灵活性。本发明中优选的原料为天然气。
现在已发现：氮氧化物(NOX)的问题与气轮机的运行条件密切相关。氮氧化物(NOX)的形成与该气轮机中的燃烧温度有关。因此，应当采取适当的措施来控制所述的燃烧温度。为将燃烧温度保持在所需的水平并仍能保持可接受的发电能力，在所述气轮机中燃烧的气体混合物的范围可通过对该工艺的设计来选择。气轮机中的燃烧温度在很大程度上是由燃烧气体的组成决定的。现在已发现空气驱动的ATR可提供一种贫的氢基燃料气体混合物，所述的燃料混合气体与在IGCC厂中应用的气体相当。现在已认识到有利的是在气轮机的空气压缩机排气处为ATR抽取工艺空气及添加至所需的ATR喷射压力。另外，空气的流量也可被调节至满足甲烷减少率的需要及满足在燃气轮机燃烧系统中形成可接受的NOX水平的燃料气体混合物的组成的需要。从气轮机中与空气一起被抽取的氮气作为燃料气体混合物的一种组分而返回至气轮机的部分中去，这样就可极大地保持气轮机中质量流量。
如果需要的话，可向气轮机中喷射适量的蒸汽来减少NOX的形成。对燃烧器的优化设计也可减少NOX的排量。
在本发明的内容范围内，一种可选择的方式为将ATR与一个转化交换器联合使用。现在已发现这种选择可增加对浓缩形式的CO2的回收。
为得到最大的灵活性，基本的发电原理可与以现存的工艺气流为基础的各种产品的生产相结合。这样，一个甲醇单元就可利用来自于ATR的一些合成气体而一个氨设备也可利用在合成气体的移动反应之后而从二氧化碳中分离出来的氢气/氮气的一部分。氨设备需要的唯一的附加单元是一个常规隔膜分离单元和一个处于合成氨反应器上游的甲烷转化装置。
本发明的范围包括：在一个空气驱动ATR单元中形成合成气体、对形成的合成气体进行热量交换，从而产生蒸汽。然后，在一个一氧化碳转移反应器中处理至少一部分冷却的合成气体，所述的一氧化碳转移反应器可以是一个单个的单元或两个一氧化碳转移反应器，其中一个是低温反应器而另一个是高温反应器。所述的气流还进一步在一个二氧化碳单元中进行处理以形成浓缩的二氧化碳流及贫的含氢气体的气流，所述气体的至少一部分在一个联合循环气轮机中燃烧而生成电能。来自于所述气轮机中的空气被供应到ATR单元。对来自于气轮机的废气进行热量交换形成蒸汽而与在上游产生的蒸汽一起在一个蒸汽涡轮机中被用来生产电能。
ATR单元可与一个转化交换器相结合而所述的原料也可在这两个单元中进行分配，输送至ATR中的原料最好占原料总量的50-80％。
在ATR单元的上游可布置一个预先转化器。
在该工艺中产生的一小部分蒸汽可被输送至气轮机来稀释含氢气体，这样就可降低气轮机中的燃烧温度。
来自于气轮机的废气的至少一部分可作为氧气源而被循环输送至ATR或与输送至气轮机的空气相结合。
合成气体的一部分可被用来生产甲烷，这种生产工艺可结合图1而按着上述的各种方式来进行。
来自于二氧化碳分离单元的气体的一部分可被用来生产氨。在这种情况下，将一种流体输送至隔膜分离单元用于分离出氢气，所述的氢气与另一含氢气流相混合，从而使混合的气流中的氮与氢的比例为1∶3。来自于隔膜分离单元的氮气返回至主要的含氢气流中，然后被输送至气轮机。
结合下面的实施例及对附图的描述，下面将对本发明进行进一步的解释和阐述。
图1所示为基本发电原理的一个简化流程图；
图2所示为与一个甲醇设备和/或一个氨设备联合使用的基本原理的简化流程图。
图1显示了实现本发明的一个例子。气态的烃类原料如天然气作为气流1供应，在气流1穿过管道2之前被加热和压缩，然后被传送至一个饱和器3中，在饱和器3中，所述气流1与工艺水4和通过管线4b供应的经脱盐工艺的补充水相混合。然后至少部分用水饱和的烃类原料，作为流体5而输送入ATR单元6中。压缩空气通过管道7而供应到ATR单元6中。一个预先转化器可选择性地布置在ATR的上游。这样将增加烃类原料的灵活性。然后就可允许使用含量更多较重的烃类原料。空气供给29的至少一部分可从燃气气轮机的空气压缩器处来供应并被增压至必要的喷射压力。所述的单元6也可以是包括有一个ATR和一个转化交换器的组合单元。应供应到各个单元中的烃类原料的量可在一个较宽的范围内变化。进入ATR的实际分配量为原料的50-80％而其余部分则分配至转化交换器中。来自于ATR单元6的合成气体8在作为流体11而被供应到一个转移转化器单元12之前在一个锅炉(蒸汽发生器)9中冷却。所述的转移转化器单元可包含两个常规一氧化碳转移反应器即一个低温(LT)反应器和一个高温(HT)反应器或仅包含一个单个的一氧化碳转移反应器。将产生的气体混合物13冷却，在单元14中将冷凝水除去，然后将产生的气体混合物作为流体15供应到一个CO2吸收器16中，CO2和吸收物质就从吸收器16中通过管道18而供应到一个解吸器19中。作为流体20b的补偿吸收物质被供应到单元19中。再生吸附物质如一种胺溶液可通过管道20而循环至吸收器16。在单元22中将CO2流21中的水除去。来自于单元22和14的工艺水可循环供应至饱和器3。高度浓缩的CO2流可被压缩并通过管道23的输送而作进一步的应用，例如可作为油田或气田的喷射气体。来自于CO2吸收器16的气流17主要包含氢和氮及少量的CO、CO2、CH4。流体17然后就被用作联合循环燃气轮机24的燃料，空气25也供应到所述的燃气轮机24中。蒸汽10也可选择性地被供应到气轮机24中来减少NOX。可在一个燃料电池中利用至少一部分流体17来产生直流电。如果电能是用于电解作用，则采用这种选择性电能就不需要整流器。气轮机24产生的废气26与蒸汽发生器27中的水进行热交换，来自于蒸汽发生器的蒸汽在气流31被供应至发电机32之前在热交换器30中被过热，蒸汽10也被供应到发电机32中。废气28可被循环至转化器单元6或与空气供给25混合输送至气轮机24。
图2中，一个合成氨设备和一个甲醇合成设备在图1中所示的基本工艺中结合为一体。这种联合工艺可包括所述的两个设备或包括其中之一。合成气体34可来自于流体11并被供应到一个甲醇合成装置35。未转化的合成气体37可被循环至合成气体流11处而生成的甲醇产品则通过管道36排出。所述的合成气体34作为另一选择可在一个气体分离隔膜单元中进行处理而除去氢和二氧化碳而作为原料以供应至甲醇合成装置。该原料也从流体23中得到额外的二氧化碳的供应。来自于所述隔膜分离单元的其他部分则重新循环至流体11。
用于氨合成的原料可来自于管道17。一股侧流体38首先被输送至气体隔膜分离单元40而将氢42供应到管道39中，从而将H2和N2的比例调整为3∶1，然后在甲烷化单元43中处理气体混合物，再后在氨合成装置44产生氨45。来自于隔膜分离单元40的氮通过管道41而被循环输送至进料17而进入氢燃气轮机24。
实施例1
该实施例显示了在图1中所示的生产工艺中，本发明在发电量、效率及作为浓缩气流的二氧化碳的回收方面的效果。该实施例还显示了与同样利用一个初级-次级转化器生产合成气体的工艺相比，所述工艺生产的效率、浓缩二氧化碳的回收及生产的全部能量的情况。该示范性的例子显示了废气循环至ATR的效果，另外该例子还显示出将ATR与一个转化交换器结合的效果。在下面的表格中所述的结合为ATR-RE结合。在下表中将根据本发明的工艺与利用次级和初级转化器SR/PR的组合而生产合成气体的工艺进行了比较。在表中，进入到转化器单元中的蒸汽和碳的摩尔比称为：蒸汽∶碳。
                                                  表1
 以ATR为基础两个一氧化碳转移反应器  以ATR为基础一个一氧化碳转移反应器  使用ATR废气循环不进行冷却  使用ATR废气循环冷却温度30℃  使用ATR废气循环，不进行冷却，减少工艺蒸汽  使用ATR-RE  即ATR和转化器的结合  SR/PR，两个一氧化碳转移反应器
  天然气LVH(MW)  823.2  823.2  823.2  823.2  823.2  823.2  882.71
  蒸汽∶碳  2.0∶1  2.0∶1  2.6∶1  2.6∶1  2.0∶1  3.2∶1  2.8∶1
  作为气轮机燃料的燃气组成CH4COO2H2N2Ar 0.01750.00520.00060.56110.41060.0049 0.01730.01180.00060.54760.40550.0048 0.00950.00240.00050.42160.55920.0067 0.0170.00280.00050.40150.57130.0069 0.01090.00390.00050.42820.57570.0069 0.00230.00340.00070.62720.36210.0043 0.03280.00380.0010.76970.18460.0021
  气体流量kmol/hr  17.176  17.390  23.648  23.148  22.971  17.641  15.520
  功率.MW气轮机功率.MW蒸汽功率.MWExp.comp功率.MW空气压缩机 287.42139.544.3433.82 287.87137.94.3433.82 298.82143.644.3480.66 295.25135.284.3461.12 298.39154.384.3480.64 302.03113.104.3430.61 289.77149.114.4612.55
  总功率.MW  397.48  396.29  366.14  373.75  376.47  388.86  430.79
  效率％  48.3  48.1  44.5  45.4  45.7  46.9  48.8
  CO2回收率％ 88.8 85.7 91.7 87.3 90.3 95.8 84.5
从上面的结果可以看出，根据本发明的生产工艺可回收产生的CO2的95.8％。该结果还显示出在发明的内容范围内，生产的效率、电力功率及CO2的量根据运行条件的变化而变化，该工艺具有很大的灵活性。形成的NOX通常为输送至气轮机的气体中的氢所占的百分比的函数。
本发明提供了一种生产清洁的二氧化碳的工艺，所生产的二氧化碳适合作为在油田中进行注射的驱动气。这样，IRCC工厂就可以以最少的二氧化碳排量而运行。另外，该工艺还提供了一种以氢为基础的贫的燃料混合气体，该混合气体适宜于在目前的燃气轮机工艺中进行燃烧。当仅需要减少NOX的量时，可向燃气轮机输送气体混合物用蒸汽进行适度稀释。

Claims (11)

1.一种利用烃类原料(1)来生产电能、蒸汽和浓缩形式的二氧化碳的方法，该方法包括：在一个空气驱动的自热反应器(ATR)单元(6)中形成合成气体，对形成的合成气体(8)进行热量交换而产生蒸汽(10)，其特征在于：在一个转移转化器单元(12)和二氧化碳吸收器(16)和解吸器(19)中处理至少一部分合成气体用来形成浓缩的二氧化碳(21)和贫的含氢气体(17)，所述含氢气体的至少一部分在一个联合循环燃气轮机(24)中燃烧而产生电能，其中，来自于所述气轮机(24)的空气被供应至ATR单元(6)，对来自于气轮机(24)的废气(26)进行热量交换而形成蒸汽，所述的蒸汽与在所述单元(12)的上游产生的蒸汽(10)一起被用来在发电机(32)中产生基本无CO2的电能。
2.根据权利要求1所述的方法，其特征在于：该工艺利用一个转化器单元，所述转化器单元包括一个与转化交换器结合的ATR(6)。
3.据权利要求1所述的方法，其特征在于：烃类原料(1)的50-80％被供应到ATR(6)而剩余的原料被供应到转化交换器。
4.据权利要求1所述的方法，其特征在于：该工艺利用一个布置在ATR单元(6)之前的预先转化器。
5.根据权利要求1所述的方法，其特征在于：该工艺利用一个单个的一氧化碳转移反应器单元(12)。
6.根据权利要求1所述的方法，其特征在于：该工艺包括将蒸汽输送至气轮机(24)来稀释包含有氢气的气体混合物(17)。
7.根据权利要求1所述的方法，其特征在于：来自于气轮机(24)的废气(28)被循环至ATR单元(6)。
8.根据权利要求1所述的方法，其特征在于：在该工艺中来自于气轮机(24)的废气(28)的至少一部分与供应到所述气轮机中的空气(25)相结合。
9.根据权利要求1所述的方法，其特征在于：合成气体(11)的一部分被利用来生产甲醇而其余部分的合成气体在用来生成电能之前在下游单元中作进一步的处理。
10.据权利要求1所述的方法，其特征在于：来自于二氧化碳去除单元(16)的含氢气体(17)的一部分被用来生产氨(45)，包括在一个隔膜单元(40)中分离所述气体以将氮和氢的比例调节至生成氨的条件，并将分离出的氮气返回至主含氢气体流(17)，其中，对所述包含的氮和氢的比例为1∶3的气流在合成氨之前在一个甲烷转化单元(43)中进行处理。
11.根据权利要求1所述的方法，其特征在于：将来自于二氧化碳去除单元(16)的包含有氢气的气体(17)的一部分进行输送而作为燃料供给燃料电池以生产电能。
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