CN102047038B - 一种流化床煤气化工艺用余热锅炉 - Google Patents

一种流化床煤气化工艺用余热锅炉 Download PDF

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CN102047038B
CN102047038B CN2009801205788A CN200980120578A CN102047038B CN 102047038 B CN102047038 B CN 102047038B CN 2009801205788 A CN2009801205788 A CN 2009801205788A CN 200980120578 A CN200980120578 A CN 200980120578A CN 102047038 B CN102047038 B CN 102047038B
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waste heat
heat boiler
economizer
fluidized bed
superheater
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CN102047038A (zh
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顾鸣海
孙松良
骆光亮
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COMPREHENSIVE ENERGY Co Ltd
Synthesis Energy Systems Inc
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    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
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    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/02—Header boxes; End plates
    • F28F9/0236—Header boxes; End plates floating elements
    • F28F9/0241—Header boxes; End plates floating elements floating end plates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10J2300/00—Details of gasification processes
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    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
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Abstract

一种流化床煤气化工艺用余热锅炉，包括串联而成的高温蒸发器(200)、过热器(300)、低温蒸发器(400)、省煤器(500)。过热器(300)、低温蒸发器(400)和省煤器(500)采用水管式结构，高温蒸发器(200)采用火管式结构。

Description

一种流化床煤气化工艺用余热锅炉
技术领域
本发明涉及一种余热锅炉，特别涉及一种流化床煤气化工艺用余热锅炉。
背景技术
余热锅炉，是利用生产过程中的余热作为热源来生产蒸汽的换热器，它既是工艺流程中的冷却器，又利用余热提供蒸汽。根据结构形式，余热锅炉根据高温气体通过管内还是管外，可分为管壳式余热锅炉和烟道式余热锅炉。火管锅炉，又称为管壳式余热锅炉，烟气在受热管管内流动，水在管外的管壳中流动。热量通过受热管的管壁传递给受热管管外的水。通常管壳式余热锅炉只是水的蒸发，没有过热段和省煤段。大型管壳式余热锅炉有汽包、上升管、下降管，小型管壳式余热锅炉采用锅壳上部的空间进行汽水分离。实际上，管壳式余热锅炉的结构与管壳式换热器无多大区别，并同样有固定管板式、浮头式及U型管式等。水管锅炉，又称烟道式余热锅炉，水或蒸汽在受热管的管内流动，烟气在受热管管外的烟道中流动。烟气通过冲刷管子的外表面将热量传递给管内的水或蒸汽。通常烟道式余热锅炉由过热段、蒸发段、省煤段以及汽包、上升管、下降管组成。
流化床煤气化工艺中，常用的工艺技术是粗合成气的冷却。煤气化炉生产的粗合成气出气化炉温度为850-1000℃，必须经过除尘和冷却工艺，才能进入下阶段的脱硫和脱碳工艺，生产出合格的净化合成气。已知技术中，煤气化用的余热锅炉为包括高温蒸发器、过热器、低温蒸发器、省煤器，其中高温蒸发器、过热器、低温蒸发器和省煤器均采用火管式锅炉结构形式。如中国实用新型公开说明书CN2426069公开了一种热管式余热锅炉就是一种火管式锅炉结构形式。
但是，由于流化床煤气化工艺生产的粗合成气中含有大量的煤灰和半焦，这些煤灰和半焦对过热器、低温蒸发器、省煤器的火管锅炉进口部分经常快速的冲刷，将使过热器、低温蒸发器、省煤器的火管锅炉进口部分产生磨损，引起管漏停车。
还有就是由于目前高温蒸发器的火管锅炉为直型火管锅炉，其脱盐水产生的气体和部分水蒸气浮起于高温蒸发器的火管顶部而经常引发局部过热，引起高温蒸发器的火管花板和火管局部的高温烧毁。
在已公开技术中，高温蒸发器、过热器、低温蒸发器、省煤器四个部分分开放置，占地大，检修和保养也很复杂、麻烦。
已公开技术中，省煤器的材料采用碳钢，由于省煤器的温度一般不会太高，就容易引起钢管外表面结露腐蚀。
发明内容
本发明所要解决的技术问题首先是为了解决已知技术中流化床煤气化工艺生产的粗合成气中粉尘对过热器、低温蒸发器、省煤器的火管锅炉的金属部分磨损问题而提出一种煤气化用余热锅炉。
本发明所要解决的技术问题其次是为了解决已知技术中脱盐水产生的气体和部分水蒸气浮起于高温蒸发器的火管顶部而经常引发局部过热，引起高温蒸发器的火管花板和火管局部的高温烧毁问题而提出一种流化床煤气化工艺用余热锅炉。
本发明所要解决的技术问题再次是为了解决已知技术中高温蒸发器、过热器、低温蒸发器、省煤器四个部分分开放置，占地大，检修和保养也很复杂、麻烦问题而提出一种流化床煤气化用余热锅炉。
本发明所要解决的技术问题还有是为了解决已知技术中省煤器钢管外表面容易结露腐蚀问题而提出一种流化床煤气化工艺用余热锅炉。
本发明所要解决的技术问题可以通过以下技术方案来实现：
一种流化床煤气化工艺用余热锅炉，包括串联而成的高温蒸发器、过热器、低温蒸发器、省煤器，其过热器、低温蒸发器和省煤器采用水管式结构，而高温蒸发器仍采用火管式结构的方案。采用该技术方案后，流化床煤气化炉工艺生产的粗合成气首先流经高温蒸发器的火管，对火管外的水、汽或汽水混合物加热。然后烟气依次进入过热器、低温蒸发器和省煤器的壳程，对过热器、低温蒸发器和省煤器管程内的水、汽或汽水混合物加热。粗合成气经过冷却和除尘工艺，形成净化合成气，然后进入下阶段的脱硫和脱碳等精制工艺。本发明将过热器、低温蒸发器和省煤器设置成水管式锅炉结构形式，并通过控制粗合成气的气速在一个比较低的速度下，如2m/s-8m/s，这样低速度下粗合成气中的半焦粉尘对过热器、低温蒸发器和省煤器金属部分的磨损很小，因此解决了现有技术中粗合成气中粉尘对过热器、低温蒸发器、省煤器的火管锅炉的金属部分磨损问题。
本发明还可以通过控制高温蒸发器的火管进口部分的粗合成气进口气速，如15m/s-30m/s，就能解决高温蒸发器的火管锅炉经常出现的快速磨损的问题。同时在高温蒸发器中，用于支撑火管管束的支撑件的热强度不够，而且制成支撑件的金属材料在一氧化碳和氢气同时存在的还原性气氛中有渗碳和粉化的可能性，因此本发明高温蒸发器的火管管束通过上下两个花板与高温蒸发器壳体连接，将火管管束支撑在高温蒸发器的壳体中，这样可以不在需要使用高温支撑件将火管管束支撑在高温蒸发器的壳体中。
由于在正常工作时，高温蒸发器中上下压差较大(如＞1.0MPa)，而且高温蒸发器的火管的管壁温度较高(可能在200-400℃之间)，高温蒸发器壳体壁面的温度较低，两者之间存在膨胀量的差异，为了解决高温蒸发器的火管与壳体之间膨胀量不一致的问题。现有技术中应用的平板式花板只能依靠本身变形来解决这个问题，而且这种花板不适合在上下两侧压差较大的环境中工作，容易导致断裂。而本发明的上下花板采用蝶形花板，依靠蝶形花板的挠性来解决高温蒸发器的火管与壳体之间膨胀量不一致的问题，并且蝶形花板完全能够在上下两侧压差较大的情况下工作。
本发明的另一个改进是在高温蒸发器采用斜管结构形式的火管锅炉，本发明的这项改进改变了传统的直型火管结构，有效避免了直型火管锅炉的脱盐水产生的气体和部分水蒸气浮起于火管顶部引发局部过热，引起火管的花板和火管顶局部的高温烧毁的问题。
本发明的另一个改进是将高温蒸发器、过热器、低温蒸发器、省煤器同放于一个钢制容器中，形成一个组合式结构的流化床煤气化工艺用余热锅炉，此种结构紧凑，管理方便。
设置时，过热器、低温蒸发器和省煤器同轴设置且相互之间留有一定的间隔，高温蒸发器为斜置式高温蒸发器，其火管管束的第一轴线与过热器、低温蒸发器和省煤器同轴的第二轴线之间形成一定的夹角，该夹角为5-10度。
或者将高温蒸发器、过热器、低温蒸发器、省煤器做成四段，相互之间通过法兰形式连接，采用这样的改进，如果流化床煤气化工艺用余热锅炉需要维修时，可把高温蒸发器、过热器、低温蒸发器、省煤器独立的抽出，如同抽屉，简单方便实用。
设置时，高温过热器设置在最顶部，过热器位于高温过热器的下方，低温蒸发器位于过热器的下方，省煤器则位于低温蒸发器的下方。
本发明的过热器、低温蒸发器、省煤器包括壳体和采用支架安装在壳体内的水平盘管，水平盘管沿管体轴线的一侧或两侧设置有操作空间，便于工人进去安装，清灰，拆卸等活动。
本发明的省煤器的壳体和水平盘管采用合金钢制造，此种方式可以避免引起钢管外表面结露腐蚀。
本发明将水在管道外受热(烟气在管道内传热)和水在管道内受热(烟气在管道外传热)两种传热、产生蒸汽工艺方法的巧妙结合利用，同时解决了充分回收热量和尽可能减少管道及内部结构磨损两个问题。
附图说明
下面结合附图和具体实施方式对本发明作进一步详细说明。
图1是本发明流化床煤气化工艺用余热锅炉的结构示意图。
图2是本发明高温蒸发器与余热锅炉上口之间的连接关系示意图。
其中：100-余热锅炉上口，200-高温蒸发器，300、过热器，400、蒸发器，500、省煤器，600、余热锅炉下口。
具体实施方式
下面结合附图给出本发明的一个具体实施例。
如图1所示，本发明的流化床煤气化工艺用余热锅炉是由余热锅炉上口100、高温蒸发器200、过热器300、蒸发器400、省煤器500、余热锅炉下口600六段组成，形成组合式结构。具体设置时，余热锅炉上口100位于流化床煤气化用余热锅炉的最顶部，高温过热器200设置在余热锅炉上口100下方，过热器300位于高温过热器200的下方，低温蒸发器400位于过热器300的下方，省煤器500则位于低温蒸发器400的下方，余热锅炉下口600位于流化床煤气化用余热锅炉的最底部。过热器300、低温蒸发器400和省煤器500采用水管式结构，而高温蒸发器200仍采用火管式结构的方案。这样流化床煤气化炉工艺生产的粗合成气首先通过余热锅炉上口100流经高温蒸发器200的火管管束220，对火管管束220外的水、汽或汽水混合物加热。然后依次进入过热器300、低温蒸发器400和省煤器500的壳程，对过热器300、低温蒸发器400和省煤器500管程内的水、汽或汽水混合物加热。粗合成气经过冷却和除尘工艺，形成净化合成气，然后通过余热锅炉下口600进入下阶段的脱硫和脱碳等精制工艺。将过热器300、低温蒸发器400和省煤器500设置成水管式结构形式，并通过控制粗合成气的气速到一个比较低的速度，如2m/s-8m/s，这样低速度下粗合成气中的半焦粉尘对过热器300、低温蒸发器400和省煤器500金属部分的磨损很小，解决了现有技术中粗合成气中粉尘对过热器300、低温蒸发器400、省煤器500的火管锅炉的金属部分磨损问题。
还有就是严格控制高温蒸发器200的火管管束220进口部分的粗合成气进口气速，如为15m/s-30m/s。这样高温蒸发器200的火管管束220经常出现的快速磨损问题也就迎刃而解。本领域普通技术人员可以通过现有技术来控制粗合成气进口气速，比如阀门，气速调节装置等。参见图2，同时在高温蒸发器200中，火管管束220通过上下两个花板230与高温蒸发器200的壳体210连接，这样可以不再需要使用高温支撑件来支撑火管管束220。上下花板230采用蝶形花板，依靠蝶形花板的挠性来解决高温蒸发器200的火管管束220与壳体210之间膨胀量不一致的问题。
过热器300、低温蒸发器400和省煤器500同轴设置且相互之间留有一定的间隔，高温蒸发器200为斜置式高温蒸发器，其火管管束220的第一轴线700与过热器300、低温蒸发器400和省煤器500同轴的第二轴线800之间5-10度的夹角，有效避免了直型火管锅炉的脱盐水产生的气体和部分水蒸气浮起于火管顶部引发局部过热，引起火管的花板和火管顶局部的高温烧毁的问题。
过热器300、低温蒸发器400、省煤器500均包括壳体310、410、510和采用支架330、430、530安装在壳体310、410、510内的水平盘管320、420、520，水平盘管320、420、520沿管体轴线的一侧或两侧设置有操作空间(图中未示出)，便于工人进去安装，清灰，拆卸等活动。
如图1所示，余热锅炉上口100的壳体110、高温蒸发器200的壳体210、过热器300的壳体310、蒸发器400的壳体410、省煤器500的壳体510、余热锅炉下口600的壳体610可以制成一个钢制的容器，高温蒸发器200的火管管束220、过热器300的水平盘管310、蒸发器400的水平盘管420、省煤器500的水平盘管520安装在这样一个钢制的容器中，具有结构紧凑、管理方便的优点。
当然也可以将余热锅炉上口100、高温蒸发器200、过热器300、低温蒸发器400、省煤器500、余热锅炉下口600各自独立成段，相互之间通过法兰形式连接，采用这样的改进，如果流化床煤气化用余热锅炉需要维修时，可把高温蒸发器200、过热器300、低温蒸发器400、省煤器500独立的抽出，如同抽屉，简单方便实用。
对于省煤器500的壳体510和水平盘管520本实施例采用合金钢制造，此种方式可以避免室温净水引起钢管外表面结露腐蚀。
本实施例水管结构的过热器300、低温蒸发器400、省煤器500管内的水与管外的热烟气换热升温，同时依靠其本身的压力(来自于锅炉给水泵)与汽包(图中未示出)的压力差克服重力流入汽包；汽包则通过上升管与下降管和火管结构的高温蒸发器200连通，水的汽液两相混合物在汽包与高温蒸发器200之间形成循环，不断产生饱和蒸汽。
流化床煤气化工艺生产出的1000℃粗合成气首先从余热锅炉上口1进入本发明的余热锅炉，流经顶部高温蒸发器200的火管管束220，对火管管束220外的来自汽包的热水进行加热。经过初步冷却后的粗合成气(约800℃)然后依次进入过热器300(出口约600℃)、低温蒸发器400(出口约400℃)和省煤器500(出口约220℃)的壳程，对管程中的水、汽或汽水混合物加热。粗合成气经过冷却和除尘工艺，形成净化合成气，进入下阶段的脱硫和脱碳工艺。
本发明的余热锅炉适用于加压流化床锅炉及煤气化炉的配套余热锅炉。尤其在制备高湿度(37％)水煤气合成中，可用于高温(1100℃)、浓尘(含煤飞灰、煤半焦灰浓度达几百克/标准立方米)、高压(3.0Mpa)的工况条件。

Claims (10)

1.一种流化床煤气化工艺用余热锅炉，包括串联而成的高温蒸发器、过热器、低温蒸发器、省煤器，其特征在于，所述的过热器、低温蒸发器和省煤器采用水管式结构，而高温蒸发器采用火管式结构且为斜置式蒸发器，流化床煤气化工艺生产的粗合成气依次下行经过高温蒸发器、过热器、低温蒸发器、省煤器。
2.如权利要求1所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的高温蒸发器的火管管束通过上下两个花板与高温蒸发器的壳体连接。
3.如权利要求2所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的上下花板为蝶形花板。
4.如权利要求3所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的高温蒸发器、过热器、低温蒸发器、省煤器同放于一个钢制容器中，形成一个组合式结构的流化床煤气化用余热锅炉。
5.如权利要求4所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的过热器、低温蒸发器、省煤器同轴设置且相互之间留有一定的间隔，高温蒸发器的火管管束的第一轴线与过热器、低温蒸发器、省煤器同轴的第二轴线之间形成5-10度的夹角。
6.如权利要求3所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的高温蒸发器、过热器、低温蒸发器、省煤器做成四段，相互之间通过焊接连接或法兰形式连接。
7.如权利要求3所述的流化床煤气化工艺用余热锅炉，其特征在于，过热器、低温蒸发器、省煤器均包括壳体和采用支架安装在壳体内的水平盘管，水平盘管沿管体轴线的一侧或两侧设置有操作空间。
8.如权利要求1所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的省煤器的壳体和水平盘管采用合金钢制造。
9.如权利要求1所述的流化床煤气化工艺用余热锅炉，其特征在于，流经过热器、低温蒸发器和省煤器粗合成气的气速为2m/s-8m/s。
10.如权利要求1所述的流化床煤气化工艺用余热锅炉，其特征在于，所述的高温蒸发器的火管管束进口部分的粗合成气进口气速为15m/s-30m/s。
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WO2009143700A1 (zh) 2009-12-03
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AU2009253634B2 (en) 2014-09-25
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