CN103380196B - 热解系统中的炭处理方法 - Google Patents

热解系统中的炭处理方法 Download PDF

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CN103380196B
CN103380196B CN201180040309.8A CN201180040309A CN103380196B CN 103380196 B CN103380196 B CN 103380196B CN 201180040309 A CN201180040309 A CN 201180040309A CN 103380196 B CN103380196 B CN 103380196B
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heat transfer
transfer medium
charcoal
separating carbon
burning
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P·帕尔马斯
P·A·瑟克里斯特
D·N·麦尔斯
希德·库尔普拉蒂帕尼加
S·J·弗雷
巴里·弗里尔
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Ensyn Renewables Inc
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Abstract

提供用于控制再热器中的整体热平衡、灰分累积和后燃的碳处理方法。使用传热介质热解含碳的生物质原料，形成热解产物和减效的传热介质。将该减效的传热介质分为分离炭和炭贫化的减效的传热介质。将该炭贫化的减效的传热介质引入传热介质的密相床层，该密相床层由含氧的再生气体流流化。使用该含氧的再生气体流，在该密相床层中燃烧该分离炭的全部或部分。可以将该分离炭的部分排出热解系统，以控制所述整体热平衡和灰分累积。

Description

热解系统中的炭处理方法
优先权陈述
本申请请求2010年7月15日提交的美国申请号12/837,376的优先权。
发明领域
本发明一般地涉及热解系统中的炭处理方法，以及更具体地涉及用于控制热解系统的再热器中的整体热平衡、灰分累积和后燃的碳处理方法。
发明背景
热解是一种热力过程，在此期间，在没有空气的条件下，使用热分解反应器将含碳的固体生物质原料，即“生物质”，如木材、农业废弃物/残余物、藻类、林业副产品、纤维素和木质素、城市垃圾、建筑/拆卸碎片等迅速加热到300℃至900℃的热解温度。可以使用不同的热解方法（包括快速热处理法和催化热解）热解生物质。在这些条件下，形成固态热解产物和气态热解产物。该气态热解产物（“热解气体”）包括不可冷凝的部分和可冷凝的部分（蒸气），该可冷凝的部分可以冷凝成为液态的源自生物质的热解油。该固态热解产物包括含碳的可燃固体，称为“炭”。
正如本领域中已知，通过燃烧热分解反应中产生的该不可冷凝的热解气体和可燃固体在热解反应器的再热器区或单独的再热器（本文统称为“再热器”）中产生用于吸热的热解反应的热量。热量通过“传热介质”从该再热器被传递到该热解反应器。虽然用于吸热的热解反应的热量和环境的热损耗（统称为“热需求”）通常与该再热器中的燃烧所提供的热量平衡，但并不总是能够达到热平衡。某些类型的生物质的热解产生相当多的可燃固体，并因此产生比满足该热解反应器的热需求所需的热能更多的热能。如果产生过多的热量，热解体系可能需要大量的过量稀释空气或需要添置昂贵的冷却系统。
该传热介质通常包括惰性固体，例如沙子。在催化热解中，可以使用催化固体代替惰性固体或附加地，作为传热介质。在热解过程中，可燃固体与惰性固体、催化固体（如果存在）或两者混合，形成减效的传热介质（spentheattransfermedium）。减效的传热介质具有减小的传热能力，以及在催化固体的情况下，也具有降低的催化活性。从该热解气体中分离出来之后，将该减效的传热介质连续地从该热解反应器转移到该再热器，便可恢复传热介质。通过燃烧混合物中的可燃固体在该再热器中再生成该减效的传热介质。然后将再生的传热介质再循环到该热解反应器中。
当该可燃固体在该再热器中燃烧时，其中的金属，通常为碱金属，作为灰分释放出来，与再生的传热介质混合。由于灰分在该热解系统中连续产生，灰分的去除则成为平衡该热解系统的必要。当将再生的传热介质再循环到存在灰分的热解反应器中时，产气的增加可能对生物质的热解产生不利的影响。
将该传热介质作为流化的密相床层保持在该再热器的下部，所述保持借由含氧的再生气体流向上通过该流化的密相床层来实现。该再热器的上部中，再热器烟气为稀相。在该减效的传热介质于该再热器中再生的过程中，该可燃固体的一部分被夹带入该再热器烟气中。该再热器中该密相床层的低高度和该可燃固体的小尺寸和低密度导致相当大量的该可燃固体从该密相床层中逸出并在稀相中燃烧（即所谓的“后燃”）。由于向上通过该密相床层进入稀相的再热器烟气中的该含氧的再生气体的速度（通常为0.76m至0.91m/s（2.5-3ft/s）），该可燃固体也可以被从密相床层“吹”到稀相中。后燃也可能会发生在烟气离开该再热器所通过的压力通风系统和烟气传输管线，而非在该再热器的该密相床层中。
除了该可燃固体的后燃之外，还可能会发生该含氧的再生气体中的一氧化碳后燃为稀相的二氧化碳的情况。再热器通常设计为能够这样操作，以便该含氧的再生气体中的基本上所有的一氧化碳（CO）燃烧形成二氧化碳（CO2），从而向该再热器提供反应热量。然而，也有可能发生稀相烟气CO到CO2的不完全燃烧或者稀相的O2的不完全燃烧。这两个问题也引起了后燃。后燃是放热的，两种情况都必须通过另外注入该含氧的再生气体淬火，否则烟气必然吸收燃烧热量，这会不利地减少传递到该密相床层的热量。
因此，希望提供用于控制热解系统的再热器中的整体热平衡、灰分累积和后燃的方法。此外，从下文详细的本发明说明和所附的权利要求，并结合说明书附图和本发明的背景将显而易见地看出本发明的其他有利的特征和特性。
发明概述
提供用于在热解系统中热解含碳的生物质原料的方法。根据一个示例性的实施方式中，该方法包括使用传热介质热解含碳的生物质原料，形成热解产物和减效的传热介质。将该减效的传热介质分为分离炭（segregatedchar）和炭贫化（char-depleted）的减效的传热介质。将该炭贫化的减效的传热介质引入传热介质的密相床层，该密相床层由含氧的再生气体流流化。
根据本发明的又一示例性实施方式，提供用于控制再热器中的热平衡、后燃和灰分累积的方法。该方法包括将来自热解反应器的减效的传热介质分为炭贫化的减效的传热介质和分离炭。将该炭贫化的减效的传热介质引入传热介质的流化密相床层。该流化密相床层通过含氧的再生气体流和该流化密相床层之上的稀相得以保持。将该分离炭的至少一部分引入到该再热器的该流化密相床层中，其中引入高度要低于该炭贫化的减效的传热介质的引入高度；引入到该再热器以外的含氧的再生气体流中；或两者，以燃烧稀相以下的该分离炭。
根据本发明的又一示例性实施方式，提供用于控制再热器中的热平衡、后燃和灰分累积的方法。该再热器包括传热介质的流化密相床层和稀相。该稀相被置于该流化密相床层的上方。该方法包括将炭基本上从减效的传热介质中分离出来，以形成分离炭和炭贫化的减效的传热介质。该炭贫化的减效的传热介质包括残余炭和惰性固体、催化固体或两者的混合物。将该炭贫化的减效的传热介质引入到该再热器中，使用含氧的再生气体燃烧残余炭以将该炭贫化的减效的传热介质转换成传热介质。通过入口立管将该含氧的再生气体引入到该再热器中。在该再热器外部的该含氧的再生气体中，用来自该流化密相床层的有效量的传热介质燃烧该分离炭。
附图说明
下文将结合如下附图对本发明进行描述，其中相同的附图标记表示相同的元件，以及其中：
图1是根据本发明的示例性实施方式的炭处理方法的流程图；
图2是根据本发明的示例性实施方式，包括气固分离器的双级旋流分离器的示例性整体热解工艺装置的图；
图3A和图3B是根据本发明的各种示例性实施方式，图2的双级旋流分离器中不同操作模式的示意图；
图4是根据本发明的示例性实施方式，包括含于另一气固分离器中耦合至淘析室的旋流分离器的另一示例性整体热解工艺装置的图；
图5是根据本发明的另一示例性实施方式，图4的旋流分离器和淘析室中操作模式的示意图；以及
图6A-图6E是本发明的再热器的各种示例性实施方式的示意图。
发明详述
下面的本发明的详细说明在本质上仅仅是示例性的，其意不在于限制本发明或本申请和本发明的用途。此外，亦没有意图受前述的本发明背景或下文详细的本发明说明中所呈现的任何理论的约束。
本发明的各种示例性实施方式针对用于处理（含碳的生物质原料的热解过程中产生的）可燃固体（下文称为“可燃固体”或“炭”）的方法。将炭从传热介质中分离，以控制该传热介质的再生过程中再热器中的后燃。可以将分离炭的一部分排出，来控制该热解系统中的整体热平衡和灰分累积。
图1是根据本发明的示例性实施方式的炭处理方法10的流程图。图2示出了采用图1的方法10的热解系统5。参照图1和图2，方法10的开始步骤是利用传热介质在热解反应器20中热解含碳的生物质原料15并形成热解产物和减效的传热介质（步骤12）。离开该热解反应器的该减效的传热介质被夹带在气态热解产物（“热解气体”）中，夹带有减效的传热介质的热解气体可参照图2中的参考标号35。正如前面所提到的，该热解产物包括固态热解产物和气态热解产物。气态热解产物45包括可冷凝的部分和不可冷凝的部分47。该可冷凝的部分可以冷凝形成液体的源自生物质的热解油49。该固态热解产物包括含碳的可燃固体（本文也称为“炭”）。
传热介质包括惰性固体（如沙子）、催化固体或两者。离开该热解反应器的传热介质被说成是“减效的”，是因为它包含来自热解过程的含碳的可燃固体。将夹带有减效的传热介质35的气态热解产物从热解反应器20移入气固分离器30a（图2），用于将气态热解产物45与减效的传热介质分离开来以及将减效的传热介质分离为独立的分离炭65的流（stream）和炭贫化的减效的传热介质75的流（步骤70）。本文所用的术语“炭贫化的减效的传热介质”既指已去除了全部炭的减效的传热介质，又指已去除了部分炭但仍保留残余炭的减效的传热介质。
在一个实施方式中，如图2、图3A和图3B所示，该气固分离器30a包括双级旋流分离器。该双级旋流分离器包括一级旋流分离器31和二级旋流分离器33。如图3A和图3B所示，该一级旋流分离器31具有第一出口37，其耦合到该二级旋流分离器33的入口；和第二出口39，其耦合到再热器60的入口。该炭贫化的减效的传热介质75离开该一级旋流分离器31，
并通过管道或浸入管41被导入该再热器60。该管道或浸入管41中的固体水平可以通过第一固体流量控制器43（如L型阀、J型阀、滑阀或诸如此类）来控制，以控制流向该再热器60的该炭贫化的减效的传热介质75（惰性固体、催化固体或两者）的固体流（图3A和3B）。
根据示例性的实施方式，并且如图2、图3A和图3B所示，夹带有减效的传热介质35的气态热解产物流被传入该气固分离器30a的该一级旋流分离器。优选地，该一级旋流分离器收集该炭贫化的减效的传热介质75并将夹带有炭的热解气体的混合物46移入该二级旋流分离器33。如图3A所示，该一级旋流分离器31一般在基本上没有固体的情况下，利用连续相的气态热解气体运行。该炭贫化的减效的传热介质75的固体只有离开该管道或浸入管41中的一级旋流分离器31才能成为连续相，所述离开可另外通过如下方式实现：该一级旋流分离器中的旋流气体涡流24将该炭贫化的减效的传热介质托出该管道或浸入管之外。如图3A所示，该浸入管41中的该炭贫化的减效的传热介质其顶部表面51位于该一级旋流分离器31的底部的下方。必要时，可在该一级旋流分离器的顶部引入氮气吹洗（未示出），以将炭从该一级旋流分离器再次引入（re-entrain）该二级旋流分离器。
为了改善改型的双级旋流分离器中的炭分离，如图3B所示，该第一固体流量控制器43允许该炭贫化的减效的传热介质75的固体颗粒返回该一级旋流分离器的底部（即，接近或进入该旋流分离器的该旋流气体涡流24），从而使该炭贫化的减效的传热介质的该顶部表面51在与图3A中所示的水平相比，较高的水平上。通过将该旋流气体涡流暴露于炭贫化的传热介质，该旋流气体涡流通过托举颗粒并将其带出该一级旋流分离器31，带入处于产物蒸汽和流化气流（该气流由夹带有炭46的热解气体组成）中的该二级旋流分离器33，将较轻和/或较小的可燃固体颗粒（即炭）与传热介质的固体颗粒分离开来。
仍参考图2、图3A和图3B，该二级旋流分离器33收集来自该第一级旋流分离器31的夹带有炭46的热解气体，从而产生了独立的热解气体45的流和分离炭65的流。热解气体45流从该二级旋流分离器33流入冷凝器81（图2）。该可冷凝的热解气体在该冷凝器中冷凝成该液体的源自生物质的热解油49。该不可冷凝的热解气体47可以循环到该再热器60中燃烧和/或循环到该热解反应器20中，作为用于托举该传热介质的介质（如图2中的箭头F所示）。
如下文根据图6A-图6E所述，该分离炭65的至少一部分被转移到该再热器60并进行处理。根据示例性实施方式，以及如图2、图3A和图3B所示，在离开该气固分离器30a之后且进入该再热器60之前，该分离炭的至少一部分可以排出该热解系统（以下称“排出的分离炭”53）（步骤300）。燃烧之前，该分离炭的一部分的排出有助于保持该热解系统中的热平衡，以及有助于通过将可燃固体的一部分在其燃烧之前去除，来管控灰分累积。该排出的分离炭53也可以进一步进行加工；作为最终产品（例如，作为肥料）；发送处理；或其组合。在排出流（exportstream）中，可以在第二固体流控制器57之前或之后去除该排出的分离炭（图3A和图3B）。以下是测定要从该热解系统中去除的排出的分离炭53的量的计算方法，所述量为保持该热解系统中的热平衡所需：
热平衡所要去除的炭（kg/hr）=
FY–{GCp,FG(TFG–T空气)+F(1-XH2O)HRx+F(Cp,F(TRx-TF)+H汽化)+Q损耗+ACp,A(T沙–T空气)}/H燃烧,
其中：
F=潮湿的生物质的进料速率（kg/hr）
G=烟气速率（kg/hr）
Q损耗=通过壁从热解系统到气氛中的热损耗量（J/hr）
A=为炭的完全燃烧所添加的空气（kg/hr）
Y=炭的收率（kg炭/kg潮湿的生物质填料）
XH2O=潮湿的生物质填料中水的质量分数（kg水/kg潮湿的生物质填料）
CP,FG=烟气的热容量（J/kg/℃）
TFG=离开沙燃烧床的烟气的温度（℃）
T空气=空气的入口温度（℃）
TF=潮湿的生物质填料的进口温度（℃）
T沙=炭燃烧区的沙床的温度（℃）
TRX=热解反应温度（℃）
CP,F=潮湿的生物质填料的显热容量（J/kg/℃）
CP,A=空气的热容量（J/kg/℃）
HRX=生物质热解转化为热解产物的反应热（J/kg干的生物质）
H燃烧=沙燃烧床前或其中的炭燃烧热（J/kg炭）
H汽化=潮湿的生物质汽化的潜热（J/kg潮湿的生物质）。
在替代性的实施方式中，如图4和图5所示，含有夹带有减效的传热介质35的气态热解产物的流从该热解反应器20移入气固分离器30b（图4）。该气固分离器30b包括耦合到炭淘析室210的旋流分离器200。该夹带有减效的传热介质35的气态热解产物移入该旋流分离器200，分离为独立的热解气体45的流和减效的传热介质55的流。该热解气体45从气固分离器30b的旋流分离器200移入到该冷凝器81中，以将可冷凝的气态热解产物冷凝为液体的源自生物质的热解油49。该不可冷凝的气态热解气体47离开该冷凝器81，以及可以循环到该再热器60中，作为用于该炭淘析室210的流化淘析气体59的源；和/或循环到该热解反应器20中，作为用于托举该传热介质的介质（如图4中的箭头F所示）。该减效的传热介质55（已去除所述气态热解产物）的第一较大部分可移入该再热器60以及其第二较小部分可移入该炭淘析室210。朝向该再热器的流通过第三固体流量控制器69（如滑动阀）控制（图5）。朝向所述炭淘析室的流通过第四固体流量控制器71控制。减效的传热介质55的所述第二较小部分被引入保持在该炭淘析室210中的传热介质的流化床63中，分离为炭贫化的减效的传热介质75的流以及分离炭和流化淘析气体的流（统一参考图4和图5的参考标号67）。来自该炭淘析室210的该炭贫化的减效的传热介质75的流移入该热解反应器20或者通过第五固体流量控制器61，移入该再热器60。
该炭和流化淘析气体的流67被移入固体-淘析气体分离器68，如堆袋室、静电沉积器、旋流集水分离器（cyclonewaterdeluge）或诸如此类，以分离成分离炭65和流化淘析废气73。由于可燃固体颗粒（即炭）具有比所述传热介质的固体颗粒（即，惰性固体颗粒、催化固体颗粒或两者）低得多的密度和/或更小的粒度，因此，炭容易通过来自该不可冷凝的热解气体47的该流化淘析气体59或通过其它方便的流化气体来淘析。淘析是一种公知的、利用垂直指向的淘析气体流将较轻的颗粒与较重的颗粒分离开来的方法。由于终端速度低于上升流体的速度，可燃颗粒上升到顶部。
如下文根据图6A-图6E所述，该分离炭65的至少一部分被转移到该再热器60并进行处理。根据示例性实施方式，按照与上文关于图2、图3A和图3B所述的相同的方式，以及如图4和图5所示，在离开该气固分离器30b之后且进入该再热器之前，该分离炭的至少一部分可以排出该热解系统（图1，步骤300）。如前所述，燃烧之前，该分离炭的一部分的排出有助于保持该热解系统中的热平衡，以及有助于通过将可燃固体的一部分在其燃烧之前去除，来管控灰分累积。该排出的分离炭也可以进一步进行加工；作为最终产品（例如，作为肥料）；发送处理；或其组合。在排出流程中，可以在固体流控制器之前或之后去除该排出的分离炭。为保持该热解系统中的热平衡，要从该热解系统中排出的分离炭的量按照与上文关于图2、图3A和图3B所述的相同的方式算得。应指出的是，由于进入气固分离器30b的淘析室的固体流与整体固体流相比较小，当仅期望排出一小部分炭的时候，优选使用该气固分离器30b。虽然已经描述了气固分离器30a和30b，其他类型的气固分离器也可以用于将所述热解气体与所述减效的传热介质以及将所述炭的至少一部分与所述减效的传热介质分离开来。
之后，在图2和图4的再热器60中处理来自气固分离器30a以及来自气固分离器30b的所述炭贫化的减效的传热介质75，如图6A-图6E所示。将来自（图2中气固分离器30a的）一级旋流分离器以及来自（图4中气固分离器30b的）炭淘析室的所述炭贫化的减效的传热介质75引入该再热器60的流化密相床层110，以利用含氧再生气体115（优选空气）的流燃烧任何残炭的至少一部分（步骤80）。示例性的再热器60（示于图6A-图6E）包括立式的大致圆筒状的大容器120，其中所述传热介质作为流化密相床层110保持在该再热器中，所述保持通过流化所述传热介质的含氧的再生气体流115（本文中也称为“初级氧化剂流”）（优选是空气）的向上流动实现。所述含氧的再生气体流还搅拌该流化密相床层内的传热介质。所述含氧的再生气体流在入口立管130中上升通过该再热器的底部，进入再热器分配器140a（图6A）、140b（图6B和图6C）、140c（图6D和图6E）并进入该再热器。该入口立管130可在其远端附近包括第一入口导管128和第二入口导管195（图6C和图6E）用于下文所述的目的。由所述传热介质形成的流化密相床层110在容器下部以及稀相150在容器上部。该再热器通常保持在400℃至1000℃的温度。
来自所述含氧的再生气体流的稀相燃烧产物烟气85（图2和图4）包含由可燃固体的燃烧产生的气体，例如二氧化碳；来自所述所述含氧的再生气体流的一氧化碳；来自空气的惰性气体，如氮气；以及未反应的氧气。该燃烧产物烟气85还包含夹带的可燃固体、惰性固体、催化固体或其组合；以及由来自可燃颗粒的碳的燃烧产生的灰分的至少一部分。
没有夹带在所述燃烧产物烟气中的灰分部分保留在传热介质的流化密相床层中。再生的传热介质中灰分的量可能会因灰分的收率和所述燃烧产物烟气中所夹带的灰分的不同而有所不同。根据示例性的实施方式，该再热器中的灰分累积通过如下方式控制：将所述“排出的分离炭”在燃烧之前从所述热解系统中去除（以产生较少的灰分）；或燃烧该再热器的该流化密相床层中的分离炭，以使更多的灰分排出该再热器进入所述燃烧产物烟气中，如下所述。
将来自气固分离器30a或30b的所述炭贫化的减效的传热介质75引入该流化密相床层的下部，以使包含在炭贫化的减效的传热介质的流中的残余炭（如果存在）能够在该流化密相床层中燃烧，如图6A-图6E中表示所述炭贫化的减效的传热介质的流向的箭头A所示。可通过第一阀175控制流量。本文所用的流化密相床层的“下部”意指较之于该流化密相床层的顶面，离该流化密相床层的底面较近的部分。在足以燃烧残余炭，将该“炭贫化的减效的传热介质”转化为“传热介质”的条件下，该炭贫化的减效的传热介质进入所述再热器的含氧的再生气体流中。燃烧产生的热量被传至该流化密相床层中的热传递介质。燃烧使密相床层材料（即该传热介质）的温度升至该热解反应器中所需的操作条件，即300℃至900℃。
之后以相同的方式处理来自气固分离器30a的分离炭65和来自气固分离器30b的分离炭65。仍然参照图1、图2、图4和图6A-图6E，将来自二级旋流分离器（气固分离器30a（图2））的分离炭65的至少一部分引入所述再热器的所述流化密相床层，以使用所述含氧的再生气体燃烧所述分离炭的至少一部分以及提高所述流化密相床层中惰性固体、催化固体或两者的温度（步骤90），如图6A-图6E中表示所述分离炭的流向的箭头B所示。可通过第二阀180控制所述分离炭进入所述流化密相床层的流量。炭流与所述炭贫化的减效的传热介质的分离允许其更深地进入所述流化密相床层，从而减少稀相中后燃的可能。
在如图6A所示的实施方式中，可以将分离炭直接引入流化密相床层以与流化密相床层中的惰性固体、催化固体或两者混合，其中分离炭65然后通过含氧的再生气体流115燃烧，这使传热介质的温度上升到热解温度，如前所述。分离炭的引入高度要低于该炭贫化的减效的传热介质的引入高度，允许更有效的燃烧和额外的燃烧时间。含氧的再生气体流115在入口立管130中上升通过所述再热器的底部并进入所述再热器的底部中的再热器分配器140a中。所述再热器分配器包括开口（图6A中未示出），通过该开口将含氧的再生气体流115排入所述再热器中。
在如图6B-图6E所示的替代性实施方式中，分离炭65可以在所述密相床层中燃烧以及附加地可在所述再热器的外部，在入口立管130中燃烧（步骤100）（图1），含氧的再生气体流115通过入口立管130被向上引入所述密相床层。在附加的燃烧步骤中，分离炭65通过入口立管130的远端附近的第一入口导管128被引入所述含氧的再生气体流以及通过再热器分配器140b或140c被引入再热器60，如下所述。最初在所述入口立管中燃烧所述分离炭，然后在所述密相床层中燃烧未燃的分离炭。如图6C和图6E所示，分离炭65可与来自再热器的密相床层的有效量的（等于A或C的流量）加热的惰性固体、催化固体或两者（即该传热介质）混合，如箭头D所示，这提高了所述分离炭的附加燃烧率。可通过第二入口导管195将加热的惰性固体、加热的催化固体或两者引入所述入口立管以与所述分离炭混合（图6C和图6E）。来自所述再热器的加热的惰性固体、加热的催化固体或者两者的流量可通过第三阀185控制。所述分离炭在所述再热器的外部至少部分地燃烧，同时所述分离炭，在所述含氧的再生气体中，在有或没有加热的传热介质的条件下，在所述入口立管中向上流动，并在所述流化的密相床层中进一步燃烧，从而使稀相或其下游（如压力通风系统160或烟气传输管线170）中分离炭的燃烧（即“后燃”）最小化。再热器分配器140b（图6B和图6C）可包括至少一个开口，通过该开口可以将所述含氧的再生气体和所述分离炭；或所述含氧的再生气体以及分离炭和加热的传热介质的混合物排入所述密相床层的下部。含氧的再生气体流115提供的氧气包括基本上完全的炭（包括残余炭及分离炭）燃烧所需的基本上化学计量的氧气（图6A、图6B和图6C）。可替代地，可以按超过化学计量的10％到15％的量添加超过化学计量的氧气。
在其他实施方式中，如，例如，图6D和图6E中所示，通过含氧的再生气体流（下文称为“初级氧化剂流”）提供少于化学计量的氧气，以及次级氧化剂流125也进入所述再热器。该次级氧化剂流优选包括空气。该次级氧化剂流提供所述再热器中基本上完全的炭（残余炭及分离炭）燃烧所需的全部氧气的25％到75％。通过再热器分配器140c将该初级氧化剂流引入所述再热器。在一个示例性的实施方式中，该再热器分配器140c包括基本上为L型的分配器以及包括开口，通过所述开口将该初级氧化剂流连同至少部分燃烧的分离炭或至少部分燃烧的炭和经加热的传热介质的混合物引入所述再热器。该次级氧化剂流按低于该再热器分配器140c的高度，通过再热器分配器140d进入所述再热器。
来自所述减效的传热介质的可燃固体的燃烧使传热介质再生。再生的传热介质25从所述流化的密相床层的上部撤出，并返回到所述热解反应器20中，如图6A-图6E中的箭头C所示，进一步用作传热介质，如图2和图4所示。来自所述再热器的再生的传热介质25的流量可以通过第四阀190控制。
再次参照图2、图4和图6A-图6E，燃烧产物烟气85经由排气导管（未示出）从再热器60流入位于所述再热器的上部中的压力通风系统160。燃烧产物烟气85通过通风排气或其他方式从所述再热器中去除：从所述压力通风系统，经由烟气传输管线170，进入外部的烟气-固体分离器72，如旋流分离器。在该外部的烟气-固体分离器72中，将燃烧产物烟气85中夹带的固体颗粒的至少一部分，如传热介质和灰分的混合物23，与燃烧产物烟气85分离，形成基本上不含固体的烟气105。该基本上不含固体的烟气可含残余的可燃的固体颗粒和残余的灰分颗粒，因为这些颗粒通常小于（平均）惰性固体颗粒和催化固体颗粒，并因此不能容易地在该外部的烟气-固体分离器72中从烟气中分离。基本上不含固体的烟气可含有残余的灰分颗粒，这使得灰分颗粒能够离开所述再热器范围，从而基本上防止所述再热器中的灰分累积。
如图2和图4，来自烟气-固体分离器的分离的传热介质和灰分的混合物23可再循环至所述再热器，用于分离的传热介质的再生。替代性地，分离的传热介质和灰分的混合物23可从所述热解系统中除去，如图2和图4中的箭头E所示。从经济方面来看，可以将包括催化固体的传热介质再循环至所述再热器，而将成本通常更低的沙从所述热解系统中除去处理。还可通过已知的方法将灰分从所述混合物23中分离并从所述热解系统（未示出）中除去。
从上所述，可以理解的是，已经提供用于炭分离和选择性地从热解系统中去除的炭处理过程的示例性实施方式。这种炭处理过程帮助控制传热介质再生期间再热器中的整体热平衡、灰分累积和后燃。所述炭处理过程有助于，例如流化的密相床层或通入再热器的入口立管中，稀相以下可燃固体和一氧化碳的燃烧，从而使稀相或其下游的燃烧（即“后燃”）最小化，这也导致更多的灰分与燃烧产物烟气一起离开。因此，转移到再热器的密相床层的热量得以提高，用于传热介质的再生，以及灰分累积得以最小化。此外，这种炭处理过程允许将富能量的炭流的一部分选择性地从热解系统除去，以提供再热器中炭燃烧供给的热量与由于显热和潜热，冷原料、周围环境的热损失和热分解反应的热量需求之间的平衡。
虽然前文详细的本发明说明中已经呈现了至少一个示例性的实施方式，但是应该理解的是，存在各种各样的变体。还应当理解的是，一个或多个示例性的实施方式仅仅是例子，并非意在以任何方式限制本发明的范围、适用性或配置。相反，前面的详细说明将为本领域的技术人员提供方便的用于实施本发明的示例性实施方式的路线图，可以理解的是，示例性实施方式中所述的元件其功能和布置可以进行各种改变，而不背离所附的权利要求及其合法等同物中所规定的本发明的范围。

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1.用于在热解系统中热解含碳的生物质原料的方法，该方法包括：
i)使用传热介质热解含碳的生物质原料，形成热解产物和减效的传热介质；
ii)将该减效的传热介质分为分离炭和炭贫化的减效的传热介质；
iii)将该炭贫化的减效的传热介质引入再热器中的传热介质的密相床层，该密相床层由含氧的再生气体流流化；
iv)使用该含氧的再生气体流，在该密相床层中燃烧该分离炭的全部或部分；和
v)在将该分离炭引入该密相床层之前，附加地在该热解系统的再热器外部，于该含氧的再生气体流中燃烧分离炭。
2.根据权利要求1的方法，进一步包括在步骤iv)的燃烧步骤之前，将该分离炭的一部分排出该热解系统。
3.根据权利要求1的方法，其中附加地燃烧该分离炭的步骤包括在入口立管中于含氧的再生气体流中混合来自该密相床层的传热介质和该分离炭。
4.根据权利要求1的方法，其中燃烧和附加地燃烧该分离炭的步骤包括将该分离炭引入到该密相床层中，其中引入高度要低于该炭贫化的减效的传热介质的引入高度。
5.根据权利要求1的方法，其中燃烧和附加地燃烧该分离炭的步骤包括在该含氧的再生气体流中提供大体上至少化学计量的氧以燃烧该分离炭。
6.根据权利要求5的方法，其中燃烧和附加地燃烧该分离炭的步骤还包括在该含氧的再生气体流中提供大体上至少化学计量的氧以燃烧包含在该炭贫化的减效的传热介质的流中的残余炭。
7.根据权利要求1的方法，其中燃烧和附加地燃烧该分离炭的步骤包括在该含氧的再生气体流中提供大体上小于化学计量的氧，并使用次级含氧的再生气体燃烧该分离炭。
8.根据权利要求7的方法，其中燃烧和附加地燃烧该分离炭的步骤还包括在该含氧的再生气体流中提供大体上小于化学计量的氧，并使用次级含氧的再生气体燃烧包含在该炭贫化的减效的传热介质的流中的残余炭。
9.根据权利要求1的方法，其中引入该炭贫化的减效的传热介质的步骤包括燃烧该炭贫化的减效的传热介质中的残余炭。
10.根据权利要求1的方法，其中引入该炭贫化的减效的传热介质的步骤包括将该炭贫化的减效的传热介质引入该密相床层的下部。
11.根据权利要求1的方法，其中分离该减效的传热介质的步骤包括使用双级旋流分离器、耦合至淘析室的旋流分离器或两者进行分离。
12.根据权利要求11的方法，其中该使用双级旋流分离器分离减效的传热介质的步骤包括将该炭贫化的减效的传热介质暴露至一级旋流分离器中的旋流气体涡流，其将夹带有炭的热解气体的混合物托举带出该一级旋流分离器进入二级旋流分离器。
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DK2593530T3 (en) 2017-03-27
CN103380196A (zh) 2013-10-30
AU2011279499B2 (en) 2015-10-01
WO2012009207A3 (en) 2012-04-26
US8499702B2 (en) 2013-08-06
CN106010672A (zh) 2016-10-12
EP2593530B1 (en) 2017-01-25
DK3211060T3 (da) 2019-05-20
NZ605739A (en) 2015-04-24
WO2012009207A2 (en) 2012-01-19
US9422478B2 (en) 2016-08-23
EP2593530A2 (en) 2013-05-22
US20120012039A1 (en) 2012-01-19
CA2805386A1 (en) 2012-01-19
NZ715689A (en) 2017-03-31
AR082214A1 (es) 2012-11-21
EP2593530A4 (en) 2016-01-06
EP3211060B1 (en) 2019-03-13

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