CN102676231A - 用于处理灰分的方法以及灰分处理装置 - Google Patents

用于处理灰分的方法以及灰分处理装置 Download PDF

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CN102676231A
CN102676231A CN2012100789136A CN201210078913A CN102676231A CN 102676231 A CN102676231 A CN 102676231A CN 2012100789136 A CN2012100789136 A CN 2012100789136A CN 201210078913 A CN201210078913 A CN 201210078913A CN 102676231 A CN102676231 A CN 102676231A
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J·伊萨克森
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Valmet Power Oy
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Abstract

在处理灰分的方法中，将飞灰从由燃料气化得到的产品气流中分离，将该飞灰在流化床燃烧中燃烧，以降低灰分的碳含量。随后，处理来自燃烧的烟道气。在第一步，在不高于800℃的温度下将灰分在流化床燃烧(流化床反应器1)中燃烧，以降低碳含量，在第二步，将烟道气在独立的燃烧过程(燃烧室7)中燃烧，燃烧条件达到至少850℃的温度。

Description

用于处理灰分的方法以及灰分处理装置
根据权利要求1的前序部分，本发明涉及一种用于处理灰分的方法。根据权利要求6的前序部分，本发明还涉及灰分处理装置。
生产燃料的一种方式为使碳质原料气化，其中碳质原料变为可燃烧的气体。特别流行的原料包括废料，其通常为有机材料，比如不同类型的木材废料和包装废料(例如，纸板和纸)。这些材料也称为回收的燃料。
气化通常在空气不足的条件下，在高温下于流化床工艺中发生。所得到的产品气体适宜在例如常规动力装置的锅炉中燃烧。
在其燃烧之前，在气化中产生的产品气体必须通过除去不同的固体和其他杂质而被纯化。从产品气体分离的所谓的飞灰含有原料的重金属、氯和碱金属中的大多数。灰分的组成取决于气化的原料。
灰分含有使其成为危险废料的可溶性组分。提供用于被分类为危险废料的灰分级分的处理场所。然而，在纯化由气化器产生的气体中得到的灰分具有高含量的烟灰(10-40％)，由于碳含量超过容许的限度，烟灰使得灰分的最终处理变复杂。这种灰分可在危险废料处理装置中经受专门的处理，但是这相对昂贵。
芬兰专利FI 110266公开了一种用于处理已经在气化装置中的来自气化的产品气体的含有烟灰的固体的方法。在该方法中，将具有高烟灰含量并且从产品气流中分离的灰分引入到流化床反应器，流化床反应器用作氧化器，在这里该灰分在800-900℃的温度下燃烧，以将碳氧化为二氧化碳。燃烧烟道气作为二次气化气体被改向至气化器。在这之前，将灰分从烟道气中分离。
然而，再循环烟道气的这样的解决方案存在问题，因为来自氧化的另外的气流富含氧，这使得气化过程的控制更加困难。另外，由于部分容量被烟道气流占据，容量降低，这增加了通过气化器的惰性气流。
本发明的一个目标是呈现一种用于处理富含烟灰的灰分但是同时用于最终处理通过脱烟灰(除去碳残渣)产生的烟道气的方法。为了实现该目标，本发明的方法主要的特征在于呈现在所附权利要求1的特征部分。
在本发明中，从气化的产品气体分离的飞灰在不高于800℃的温度下被流化床燃烧氧化，在第二步，通过流化床燃烧产生的气体在独立的燃烧过程中例如在单独的燃烧室中在至少850℃的温度下燃烧。
通过本发明，气化灰分中的烟灰含量可降低至容许的水平，而无需分解灰分中的氯化合物，并且在分离灰分之后，剩余的气体可在废料指令所需的条件下在高温下燃烧。氯化物在流化床燃烧的相对低的温度下不蒸发，但是与灰分一起被除去。灰分可独立于气化过程例如当不运行气化过程时被处理。此外，可不考虑彼此调节气化过程和灰分处理过程。
以下，结合附图来更详细地描述本发明，该附图为灰分处理装置的工艺流程图。
气化过程同样地已知，不再更详细地描述。原料为通常所谓的回收的燃料，其包括不同类型的城市废料和工业废料，通常为适于能量产生的固体碳质燃料。
将从自燃料气化得到的可燃产品气流中分离的热的飞灰，在图中所示的装置中处理。通常，这样的装置位于与气化器本身和用于燃烧产品气体的动力装置的主锅炉相同的动力装置中，以产生能量。气化过程以及从该过程分离并作为原料供应至装置的灰分用虚线表示。将具有高含量的呈源自气化燃料的烟灰形式的未经反应的碳的该灰分，与另外的燃料一起引入到流化床反应器1，在这里通过供应到反应器中的含氧空气发生燃烧。另外的燃料不是必需的，但是燃烧所需的温度可仅通过包含在灰分中的可燃碳来达到。流化床反应器还含有固体床材料(沙子、石灰石，等)，如果需要，可加入这些固体床材料。流化床反应器1为循环流化床反应器，其具有由旋风器2和返回管3形成的用于床材料的返回循环。在空气不足下操作反应器，以达到600-800℃之间的氧化温度。有利地，氧化温度为约720℃。
反应器1的熔炉为完全耐火材料衬里的(绝热的)；换言之，其不含吸收燃烧热量的传热表面。在床材料的返回循环中，可使用换热器4来调节氧化温度。
在图中的情况下，流化床反应器为循环流化床(CFB)反应器。如果可使得灰分足够粗糙，则还可使用鼓泡流化床(BFB)。
将灰分的较粗糙的级分以底灰形式从反应器1的下部除去，而在旋风器2中不被分离至返回循环的较细级分被烟道气携带沿着烟道气管道5进入灰分分离器6(旋风器)，在这里将其分离，并将烟道气引向燃烧室7。在燃烧室中，气体在于烟道气处测得的短暂地(至少2秒)至少850℃的较高温度下燃烧，以达到根据废料焚烧指令(wasteincineration directive，WID)的条件。如果需要，将维持燃料(其可为天然气或油)沿着管线8引入到燃烧室7。在动力装置中，燃烧室7为与主锅炉分离的独立单元，并且由其产生的烟道气在纯化后被排放到空气中。
在燃烧室7的下游，将烟道气引向烟道气锅炉9，在这里其通过传热介质(例如，在管道中流动的水或水蒸气)被冷却。烟道气锅炉9可在与燃烧室7相同的锅炉中整合。将已冷却的烟道气沿着管道10引向最终的气体过滤器11，该气体过滤器可为袋式过滤器。最后，还可存在其他气体纯化装置，比如催化剂(例如NOX催化剂)。将已纯化的烟道气引向烟囱12或动力装置的主锅炉的烟囱，或引向主锅炉的后部通路的适当的点。灰分处理装置的烟道气和动力装置主锅炉的烟道气还可具体共同的气体纯化器，其中将气体沿着管道10引向主锅炉的后部通路的适当的点。另外，气体过滤器11可用主锅炉的过滤器代替。
该图还显示将助剂供应至灰分分离器6上游的烟道气管道5(箭头A)和冷却器下游、气体过滤器11上游的管道(箭头B)两者中。这些助剂可由具有比待分离的灰分的粒度粗的粒度的固体组成，以促进灰分的分离。

Claims (10)

1.一种处理灰分的方法，其中将飞灰从由燃料气化得到的产品气流中分离，将该飞灰在流化床燃烧中燃烧，以降低灰分中的碳含量，随后处理来自燃烧的烟道气，其特征在于：
在第一步，在不高于800℃的温度下将灰分在流化床燃烧中燃烧，以降低碳含量，和
在第二步，将烟道气在独立的燃烧过程中燃烧，燃烧条件达到至少850℃的温度。
2.权利要求1的方法，其特征在于在燃烧过程之前，将在流化床燃烧的烟道气中夹带的细灰分材料从其中分离。
3.权利要求1或2的方法，其特征在于所述流化床燃烧在循环流化床(CFB)中发生。
4.前述权利要求1-3中任一项的方法，其特征在于在流化床燃烧之后，碳残渣占分离的总灰分量的小于5％重量。
5.前述权利要求中任一项的方法，其特征在于在将烟道气燃烧之后得到的气体与来自动力装置的主锅炉的烟道气一起在一个或多个纯化步骤中纯化。
6.一种灰分处理装置，所述装置具有流化床反应器(1)，所述流化床反应器(1)被配置以燃烧从由燃料气化得到的产品气流分离的飞灰，其特征在于将流化床反应器(1)的烟道气管道(5)引向单独的燃烧室(7)，用于在独立的燃烧过程中燃烧烟道气，并且燃烧室(7)的燃烧温度可调节至比流化床反应器(1)的燃烧温度高的温度。
7.权利要求6的灰分处理装置，其特征在于所述烟道气管道(5)包含灰分分离器(6)，用于分离被烟道气携带的灰分级分。
8.权利要求6或7的灰分处理装置，其特征在于所述流化床反应器(1)为循环流化床(CFB)反应器。
9.权利要求6或8的灰分处理装置，其特征在于所述流化床反应器(1)的熔炉完全绝热。
10.权利要求6-8中任一项的灰分处理装置，其特征在于在燃烧室(7)的下游提供烟道气锅炉(9)，通过该烟道气锅炉引导传热介质的流动，用于冷却烟道气。
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