CN103154208A - 用于生产合成气的方法 - Google Patents
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Abstract
采用通过将固态或液态的含碳燃料与含氧的氧化剂在反应器中气化产生合成气的方法，其中合成气经顶部从反应器中排出，和在反应期间产生的矿物性灰分微滴/熔渣微滴沿重力方向向下从反应器排出，应当能够利用价格明显较低的烟管锅炉代替辐射式锅炉用于排出热量。这由此实现，将合成气不冷却地通过热气过滤器(2)，然后为了冷却而引导通过烟管锅炉(3)，其中在热气过滤器(2)处分离出来的灰分微粒/熔渣微粒沿着重力方向导回气化反应器(2)。
Description
本发明涉及在权利要求1的前序部分中所限定类型的产生合成气的方法。
本申请人的WO2009/080334A2描述了一种也致力于从合成气中除去液态灰分及碱的方法。
世界上存在许多将煤及生物质气化的设备。大多数的这样的设备用于产生合成气、氨、氢或甲醇。
存在的共识是，对于IGCC发电厂以及对于制备合成的能源载体而言，特别有意义的是气流式气化的方法。然而必须显著地提高气流式气化器的可用性。
在气流式气化过程中，如此升高过程温度，使得将煤的矿物成分熔化成液态熔渣。溶渣经过反应器的圆柱形壁向下流动，并通过位于气化器的圆锥形区域的溶渣孔离开气化器。其流入水浴（熔渣浴），在此处固化及被造粒成小的玻璃状粒料。然而，一小部分的液态灰分微滴被合成气一起带走，并通过排气口进入原料气体冷却器。
但是从气化器的顶部区域流出的合成气具有高于1500℃的温度。在该温度下，飞灰微粒或多或少是液态和黏性的。因此在合成气能够与烟管锅炉的热交换管接触之前，必须将合成气冷却至没有黏性的850至900℃的范围。
烟管锅炉在烟气的热利用方面具有许多应用。对于其使用而言主要受入口温度的限制，因为包含于烟气中的灰分微粒在高于850℃的温度时是黏性的，甚至是熔融的。
也存在许多气化方法，这些气化方法以不同的方式进行余热利用，其中在将原料气体转向以及在对流锅炉中利用之前，必须首先用水部分地或用冷气体将热的原料气体在淬火管内冷却至850℃左右的温度。
本发明的目的在于提供能够利用价格明显较低的烟管锅炉代替辐射式锅炉排出热量的方法。
采用开篇提到的类型方法，由此实现本发明的目的，引导合成气不冷却地通过热气过滤器，然后为了冷却而通过烟管锅炉，其中在热气过滤器处分离出来的灰分微粒/熔渣微粒沿着重力方向导回气化反应器。
通过本发明解决了这样的问题，在过早冷却微粒时，它们粘附在烟管锅炉上并且它们因此而堵塞，这导致经常停机来清理相应的设备部件。这通过本发明得以避免。
本发明的实施方案在从属权利要求中给出。在此可以看出，将热气过滤器成型为陶瓷过滤器，其中，将包含在未冷却的合成气中的蒸气状碱经过吸气陶瓷或在与吸气陶瓷接触之后从合成气中除去。
除了使用陶瓷微粒热气过滤器的设计以外，例如存在另一种可能性，在过滤器中插入被涂覆，例如陶瓷涂覆的冷却的管，所述陶瓷例如通过壁骨材料（Bestiftung）施涂在其中，在此其它过滤器设计也是可能的。
根据本发明的一种实施方案，在热气过滤器内将速度调节为1至10m/s，尤其是3m/s。为了优化传热，在这种情况下也可以将烟管锅炉内的速度调节为15-25m/s。
根据本发明的合适的实施方案是，在反应器中以800至1800℃的温度和0.1至10MPh的工作压力下进行气化，以及为了分离过滤器上的杂质而在过滤器之前混入添加剂。
最后，在根据本发明的方法的情况下还可以设计为，依次流经多个过滤阶段，其中，将在最后一个过滤阶段之后的气体出口温度调节为高于灰分/熔渣的流动温度。因此，根据本发明例如可能的是，首先为了熔渣分离使用热气过滤器，以及接着使用由吸气陶瓷构成的过滤器，所述吸气陶瓷在操作时间期间自身缓慢耗尽，并且有时要更换。
为了达到所提出的目的，本发明还提出一种设备，所述设备具有反应器及烟气冷却器，所述反应器用于在将含氧的氧化剂导入反应器的条件下从含碳燃料制备合成气，所述设备的特征在于，在原料气体的流动方向上，在反应器下游首先是灰分微粒/熔渣微粒过滤器，紧接着是吸气陶瓷过滤器，以及这之后是用于气体冷却的烟管锅炉。
根据本发明，这样的设备的另一种实施方案可以是，陶瓷热气过滤器具有陶瓷支撑网以及由填料填充。
在另一种实施方案中可以设计为，过滤器及烟管锅炉设置有压力监测器，用于探测工作压力和/或压差。
在这种情况下，设备在另一种实施方案中的特征可以在于，在一个或多个过滤器中使用的填料可以成型为球体、腊希格环、挡环、鞍形体、或圆柱体，或是由天然材料破碎形成的不规则体，其中填料可以具有蜂窝结构或薄片结构。
以下例如借助于附图进一步阐释本发明。
图1中显示了气化反应器1的示意图，
图2中显示了具有热气过滤器的气化反应器的放大视图，以及
图3中显示了根据本发明的方法的原理图。
图1中图示了整体上用1标记的汽化反应器，其在顶部区域配有通常用2标记的热气过滤器，在所述热气过滤器上连接有烟管锅炉3。
反应器1和过滤器2由此直接彼此重叠，即过滤器2在一定程度上构成反应器出口。相对于现有技术，借此可以避免额外的容器、额外的熔渣排出装置，以及因此避免相联系的热损失。
在图示的实施例中，热气过滤器具有置于陶瓷网5上的陶瓷填料8。在该处被分离出的熔融态灰分在图2中标记为6，它们回流至具有熔渣出口7的反应器内腔9，如箭头13所示。
将例如燃料及水蒸气导入反应器内9采用两个箭头10和11简化描述。
在图2的示意实施例中，还在热气过滤器2的上方表明了例如在意欲使用时损耗并且可更换的定位在那里的吸气陶瓷过滤器12，这没有更详细地示出。
在图1中参数还表示：
T=温度
Ts=渣的熔融温度
w=各气体的流速
图3显示了使用根据本发明的具有下游的高温过滤器2以及再下游的烟管锅炉3的气化反应器1的示意性工艺原理图。
如还在图2中，来自高温过滤器2的熔渣回流由箭头13符号表示，同样还有导入燃料和水蒸气（箭头10和11）。
如图3中所示，烟管锅炉3下游是洗涤器14、饱和器15、以及CO变换器16。
由于在反应器1的顶部区域中，反应器1配有过滤器2，另外提供了很紧密的可构造性，在这种情况下，可以使热气（T>TS)转向，因为在所述气体中已经没有熔渣微粒存在。相反地，在现有技术中将热气冷却至远低于Ts，以在其能够到达烟管锅炉及/或废热锅炉之前，
避免烟管锅炉堵塞以及因此的停机。在反应器1的顶部区域配备的过滤器2的有利之处因此还在于，可以使用具有非常高温度
的热气产生水蒸气，而不是直到850至900℃的温度才使用。
当然，还在许多方面对上述本发明的实施例进行修改，但不背离本发明的基本构想。因此例如可以使碱与作为添加剂添加到烟气流中吸气微粒化合。
权利要求书(按照条约第19条的修改)
1.通过将固态或液态的含碳燃料与含氧的氧化剂在反应器中气化产生合成气的方法，其中合成气经顶部从反应器中排出，和在反应期间产生的矿物性灰分微滴/熔渣微滴沿重力方向向下从反应器排出，其特征在于，在反应器中以800℃至1800℃的温度下进行气化，以及引导合成气不冷却地通过热气过滤器，然后为了冷却而通过烟管锅炉，其中在热气过滤器处分离出来的灰分微粒/熔渣微粒沿着重力方向导回气化反应器。
2.根据权利要求1的方法，其特征在于，将热气过滤器成型为陶瓷过滤器，其中，将包含在未冷却的合成气中的蒸气状碱经过在陶瓷上涂覆的吸气材料或在与在陶瓷上涂覆的吸气材料接触之后从合成气中除去。
3.根据权利要求1或2的方法，其特征在于，在热气过滤器内将气体速度调节为1至10m/s，尤其是3m/s。
4.根据权利要求1或2的方法，其特征在于，将烟管锅炉中的气体速度调节为15-25m/s。
5.根据权利要求1至4中一项或多项的方法，其特征在于，在反应器中的气化在0.1至10MPa的工作压力下进行，以及为了分离过滤器上的杂质而在过滤器之前混入添加剂。
6.根据权利要求1至5中一项或多项的方法，其特征在于，依次流经多个过滤阶段，其中，将在最后一个过滤阶段之后的气体出口温度调节为高于灰分/熔渣的流动温度。
7.根据权利要求1至6中一项或多项的方法，其特征在于，将来自反应器的合成气引导到配置在反应器的顶部区域的热气过滤器中。
8.用于进行权利要求1至7中一项或多项的方法的设备，所述设备具有反应器及烟气冷却器，所述反应器用于在将含氧的氧化剂导入反应器的条件下从含碳燃料制备合成气，所述设备的特征在于，在原料气体的流动方向上，在反应器(1)下游首先是灰分微粒/熔渣微粒过滤器(2)，紧接着是由涂覆有吸气材料的陶瓷制成的过滤器，以及这之后是用于气体冷却的烟管锅炉(3)。
9.根据权利要求8的设备，其特征在于，陶瓷热气过滤器(2)具有陶瓷支撑网(5)以及由填料(8)填充。
10.根据权利要求8或9的设备，其特征在于，过滤器(2)及烟管锅炉(3)设置有压力监测器，用于探测工作压力和/或压差。
11.根据权利要求8、9或10的设备，其特征在于，在一个或多个过滤器中使用的填料(8)可以成型为球体、腊希格环、挡环、鞍形体、或圆柱体，或是由天然材料破碎形成的不规则体。
12.根据权利要求11的设备，其特征在于，填料(8)具有蜂窝结构或薄片结构。
13.根据权利要求8至12中任一项的设备，其特征在于，在反应器(1)的顶部区域中，反应器(1)配有过滤器(2)。
Claims (13)
1.通过将固态或液态的含碳燃料与含氧的氧化剂在反应器中气化产生合成气的方法，其中合成气经顶部从反应器中排出，和在反应期间产生的矿物性灰分微滴/熔渣微滴沿重力方向向下从反应器排出，其特征在于，引导合成气不冷却地通过热气过滤器，然后为了冷却而通过烟管锅炉，其中在热气过滤器处分离出来的灰分微粒/熔渣微粒沿着重力方向导回气化反应器。
2.根据权利要求1的方法，其特征在于，将热气过滤器成型为陶瓷过滤器，其中，将包含在未冷却的合成气中的蒸气状碱经过吸气陶瓷或在与吸气陶瓷接触之后从合成气中除去。
3.根据权利要求1或2的方法，其特征在于，在热气过滤器内将气体速度调节为1至10m/s，尤其是3m/s。
4.根据权利要求1或2的方法，其特征在于，将烟管锅炉中的气体速度调节为15-25m/s。
5.根据权利要求1至4中一项或多项的方法，其特征在于，在反应器中的气化在800至1800℃的温度和0.1至10MPh的工作压力下进行，以及为了分离过滤器上的杂质而在过滤器之前混入添加剂。
6.根据权利要求1至5中一项或多项的方法，其特征在于，依次流经多个过滤阶段，其中，将在最后一个过滤阶段之后的气体出口温度调节为高于灰分/熔渣的流动温度。
7.根据权利要求1至6中一项或多项的方法，其特征在于，将来自反应器的合成气引导到配置在反应器的顶部区域的热气过滤器中。
8.用于进行权利要求1至7中一项或多项的方法的设备，所述设备具有反应器及烟气冷却器，所述反应器用于在将含氧的氧化剂导入反应器的条件下从含碳燃料制备合成气，所述设备的特征在于，在原料气体的流动方向上，在反应器(1)下游首先是灰分微粒/熔渣微粒过滤器(2)，紧接着是吸气陶瓷过滤器，以及这之后是用于气体冷却的烟管锅炉(3)。
9.根据权利要求8的设备，其特征在于，陶瓷热气过滤器(2)具有陶瓷支撑网(5)以及由填料(8)填充。
10.根据权利要求8或9的设备，其特征在于，过滤器(2)及烟管锅炉(3)设置有压力监测器，用于探测工作压力和/或压差。
11.根据权利要求8、9或10的设备，其特征在于，在一个或多个过滤器中使用的填料(8)可以成型为球体、腊希格环、挡环、鞍形体、或圆柱体，或是由天然材料破碎形成的不规则体。
12.根据权利要求11的设备，其特征在于，填料(8)具有蜂窝结构或薄片结构。
13.根据权利要求8至12中任一项的设备，其特征在于，在反应器(1)的顶部区域中，反应器(1)配有过滤器(2)。
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| CN104673394A (zh) * | 2015-02-04 | 2015-06-03 | 中国五环工程有限公司 | 带废热回收干粉固体燃料气化工艺及其系统 |
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| DE4318385C2 (de) * | 1993-06-03 | 1997-04-10 | Metallgesellschaft Ag | Verfahren zum Abscheiden von Schlacketröpfchen aus einem Rohgas aus der Verbrennung oder Vergasung fester oder flüssiger Brennstoffe |
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| DE10062320A1 (de) * | 2000-12-14 | 2002-06-20 | Borsig Gmbh | Abhitzekessel zum Kühlen von heißem Synthesegas |
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| DE102006050603A1 (de) * | 2006-10-26 | 2008-04-30 | Ständer, Wolfgang, Dr.Ing. | Verfahren zur Vergasung von Biomasse mit kontinuierlichem Eintrag, anschließender Zerkleinerung und Gasreinigung sowie Anlage zur Durchführung dieses Verfahrens |
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| DE4336100C1 (de) * | 1993-10-22 | 1994-11-24 | Metallgesellschaft Ag | Vorrichtung zur Abscheidung flüssiger Asche |
| CN101688135A (zh) * | 2007-05-02 | 2010-03-31 | 帕尔公司 | 用于由可气化原料材料产生合成气的气化装置和方法 |
| WO2009080334A2 (de) * | 2007-12-22 | 2009-07-02 | Uhde Gmbh | Entfernung von flüssigasche und alkalien aus einem synthesegas |
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| CN104673394A (zh) * | 2015-02-04 | 2015-06-03 | 中国五环工程有限公司 | 带废热回收干粉固体燃料气化工艺及其系统 |
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| RU2013116731A (ru) | 2014-10-20 |
| WO2012034654A4 (de) | 2012-06-07 |
| US8877097B2 (en) | 2014-11-04 |
| CL2013000721A1 (es) | 2013-08-02 |
| DE102010045537A1 (de) | 2012-03-15 |
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| KR20130109121A (ko) | 2013-10-07 |
| EP2616528A1 (de) | 2013-07-24 |
| UA109912C2 (uk) | 2015-10-26 |
| WO2012034654A1 (de) | 2012-03-22 |
| AU2011301418B2 (en) | 2015-07-16 |
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