CN101544901B - 生物质热裂解制取生物油的方法及装置 - Google Patents
生物质热裂解制取生物油的方法及装置 Download PDFInfo
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- CN101544901B CN101544901B CN200910026737XA CN200910026737A CN101544901B CN 101544901 B CN101544901 B CN 101544901B CN 200910026737X A CN200910026737X A CN 200910026737XA CN 200910026737 A CN200910026737 A CN 200910026737A CN 101544901 B CN101544901 B CN 101544901B
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- gas
- perolene
- heating unit
- biomass
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- 239000002028 Biomass Substances 0.000 title claims abstract description 65
- 238000005336 cracking Methods 0.000 title abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 82
- 238000000034 method Methods 0.000 claims abstract description 27
- 239000007787 solid Substances 0.000 claims abstract description 17
- 238000004227 thermal cracking Methods 0.000 claims abstract description 17
- 239000000919 ceramic Substances 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 105
- 239000000843 powder Substances 0.000 claims description 36
- 239000012075 bio-oil Substances 0.000 claims description 31
- 239000003610 charcoal Substances 0.000 claims description 26
- 238000000197 pyrolysis Methods 0.000 claims description 24
- 238000002485 combustion reaction Methods 0.000 claims description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 claims description 2
- 238000003860 storage Methods 0.000 claims description 2
- 239000000969 carrier Substances 0.000 abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 2
- 239000000779 smoke Substances 0.000 abstract description 2
- 229910052799 carbon Inorganic materials 0.000 abstract 1
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- 238000005243 fluidization Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicium dioxide Chemical compound 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- 229940035295 Ting Drugs 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
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Abstract
本发明提供一种生物质热裂解制取生物油的方法及装置,生物质物料经粉碎、干燥、热裂解、二级冷凝、分离工序制备得到生物油,该装置主要由进料系统、流化床反应器、载热体分离器、气固分离器、载热体加热装置、冷凝器等组成,其中载热体加热装置分两层,用隔热板隔开,均匀分布若干陶瓷热管,陶瓷热管作为传热元件加热载热体。本发明不仅利用热裂解副产物炭和不可冷凝气体作为热裂解液化的能源,而且有效利用载热体加热装置排放的烟气作为流化气,具有工艺过程合理、无二次污染、节能、成本低等多种优点,与现有技术相比,更易于推广应用。
Description
生物质热裂解制取生物油的方法及装置
技术领域
[0001] 本发明涉及生物质再生利用及其能源化技术领域,特别是涉及生物质热裂解液化制取生物油的方法及装置。
背景技术
[0002] 生物质热裂解是指生物质在完全没有氧或缺氧的条件下在极短的时间内加热、冷却,最终生成生物油、炭和不可冷凝气体的过程。国外采用了多种不同的试验装置和技术路线,以达到增加生物油产率和提高能源利用水平的目的。现有技术中也公开了一些关于制备生物油的方法,但多以消耗高品位能源电能为代价或是反应器内有运动部件,结构复杂, 工作可靠性和运行寿命难以保证等限制。中国专利200510057215. 8公开的《生物质热裂解液化的工艺方法及其双塔式装置系统》就是一种生物质热裂解液化制取生物油的工艺系统。由该申请案提出的热裂解工艺流程而确定的装置包括由调频电动机、加料装置、螺旋输送装置组成的给料系统、热解反应塔、载热体分离器、载热体加热塔、鼓风机、热交换器、 初级分离器、气固分离器、冷凝器、气体过滤器、集油器、气体泵、储气罐、氮气罐、载热体调温器、流化气调温器、进料管、冷却水套、载气调节阀、布风孔板、流化气调节阀、载热体回送管、载热体调节器、载热体残碳循环管。其中的关键设备是热解反应塔和载热体加热塔,从该申请案的内容来看,其发明目的是达到了。但是,该申请案提出的热裂解工艺流程及其装置在工业化应用中将受到限制。因为,该申请案提出的生物质粉料在热解反应塔内进行热裂解反应以及燃烧产物炭以预加热载热体的过程中,需要氮气作为载气对设备内的载热体及生物质进行流化,氮气需要预热,且用量很大,不但提高了运行成本,而且使不可冷凝气体的热值降低。另外,该申请案提出的利用载热体调温器对分离出来的载热体进行调温,消耗优质能源来加热中间热载体,使得液化成本较高,不利于产业化;综上所述,整套装置能耗高,在工业化应用中将受到限制。研究表明,生物质热裂解所需热量比较少。生物质快速热裂解一般得到50 % -70 %的生物油,如果反应条件合适,可获得原生物质80 % -85 %的能量,生物油产率可达70%以上,其余产物为焦炭和燃气。Dynamotive的流化床小试装置上的能量衡算表明,每kg生物油热裂解得到的焦炭和燃气的总能量大于其热裂解所需的热量。由此表明,完全可以利用热裂解副产物来为生物质热裂解提供能量,从而实现自热式的热裂解液化。针对上述问题,本发明提出一种自热式无污染的生物质热裂解制取生物油的方法。
发明内容
[0003] 本发明的主要目的是针对现有的生物质热裂解液化工艺中能源利用率不高以及实际生产连续性差等缺点,提出一种自热式无污染的生物质热裂解制取生物油的方法。该方法利用热裂解副产物炭和不可冷凝气体作为热裂解液化的能源,有效利用载热体加热装置排放的烟气作为流化气,并采用载热体循环技术,减少了载热体加热所需热量,从而大幅降低生物质热裂解液化的总成本。所要解决的技术问题是保证生物质在无氧状态下以及最佳热裂解温度范围进行热裂解反应,保证生物质热裂解液化连续性生产,从而更加适于工业化应用。
[0004] 本发明的方法包括以下步骤:
[0005] (a)将生物质物料粉碎至粒径l_2mm,干燥至含水率小于8%,将处理后的生物质粉料倒入预备料斗中存储,待预备料斗充满生物质粉料后,关闭预备料斗的顶盖,使粉料处于无氧状态;并打开原先关闭预备料斗和给料料斗之间的阀门,将预备料斗的粉料缓缓加入给料料斗,通过送料机构将生物质粉料送入流化床反应器。
[0006] (b)生物质粉料在流化床反应器内进行热裂解反应结束后,其载热体与产物热裂解气、炭和灰分一道从反应器内被送出;首先进入载热体分离器进行一级分离,其中载热体被分离出来,剩余的炭、灰分和热裂解气再进入气固分离器,将其中的炭和灰分分离出来。
[0007] (c)分离出来的载热体进入载热体加热装置上层,产物炭和灰分进入载热体加热装置下层,燃烧产物炭和不可冷凝气体以加热载热体;载热体在载热体加热装置上层被加热到设定温度后依靠重力作用沿着载热体回送管顺利进入流化床反应器内以供循环使用。
[0008] (d)同时,载热体加热装置下层排放的高温烟气经过气体过滤器B滤除灰分后一部分通入原料干燥室利用其热量对生物质粉料进行干燥,干燥后的生物质粉料收集于料仓;另一部分通入空气预热器,来预加热助燃空气,被预加热后的助燃空气送入载热体加热装置下层,进行步骤c所述的燃烧产物炭和不可冷凝气体以加热载热体的过程中进行助燃;其热量被充分利用后的烟气从空气预热器的出口排出,通过气体泵B收集在气体缓冲罐中存储,被分为两路继续输送,流量较大的主路进入流化床反应器,在反应器底部预热, 经气体分布板进入上部的流化床反应器;流量较小的一路通往载气输入管,辅助输送生物质粉料。
[0009] (e)在步骤b中所述的气固分离完成后,分离出来的热裂解气分别进入第一级冷凝器和第二级冷凝器,并收集冷凝产物于集油器中;不可冷凝气体与冷凝的生物油分离后, 作为回收气收集;不可冷凝气体经脱二氧化碳工艺后通过气体泵A收集在储气罐中,用作可燃气通入载热体加热装置下层。
[0010] 本发明先向气体缓冲罐内通入一定量的烟气后,打开排气阀将气体缓冲罐内所有气体排空,然后储存烟气;工作过程中,根据反应情况,通过调节阀调节进气流量。
[0011] 实现该生物质热裂解制取生物油的装置系统包括:预备料斗下接给料料斗和送料机构,送料机构一端和气体缓冲罐连接,另一端与流化床反应器连接,流化床反应器的上端面出口与载热体分离器连接,下端面的布风板经风室与气体缓冲罐连接,载热体分离器和气固分离器的一端连接,载热体分离器的另一端和载热体加热装置上层连接;气固分离器的底端和载热体加热装置下层连接,气固分离器经第一级冷凝器、第二级冷凝器、气体过滤器A、气体泵A接储气罐,储气罐和载热体加热装置下层连接,第二级冷凝器底端接集油器,载热体加热装置下层的顶部接气体过滤器B,气体过滤器B分别接空气预热器和原料干燥室,空气预热器一端经气体泵B接气体缓冲罐,另一端分别接鼓风机、载热体加热装置下层,原料干燥室分别接料仓、引风机。
[0012] 所述载热体加热装置分为载热体加热装置上层和载热体加热装置下层,两层之间用隔热板绝对隔开,其中隔热板是倾斜的,隔热板的倾斜方向与水平面的夹角均大于45° ; 载热体加热装置均勻分布有若干陶瓷热管,陶瓷热管作为传热元件加热载热体,陶瓷热管的工质是钠,陶瓷材料是碳化硅。在载热体加热装置下层底部连接有两条输入管,一条输入管向该层输入不可冷凝气体,另一条输入管向该层输入经过空气预热器被预热后的助燃空气,该助燃空气由鼓风机提供。
[0013] 与现有技术相比,本发明有如下进步:
[0014] 1.本发明采用生物质热裂解液化过程中产生的可燃气体和产物炭作为热裂解液化的能源,并且用载热体循环技术,减少了载热体加热所需热量,大幅降低了生物质热裂解液化的总成本。
[0015] 2.本发明采用烟气再循环方式,烟气二次回收利用不仅降低了生产成本,而且合理解决了烟气排放问题。
[0016] 3.本发明载热体加热装置分为两层,均勻分布有若干陶瓷热管,具有很高的导热能力。对其温度、加热速率的调节也比现有技术方便。并且,载热体循环回送至流化床反应器不会带入空气,保证了反应器缺氧的条件,有利于在工业化应用中实现连续性生产。
[0017] 4.本发明的装置系统结构简单,设备投资费用低,适合工业化应用。
[0018] 综上所述,本发明的生物质热裂解制取生物油的方法及装置,其具有上述诸多优点及实用价值,在技术上有较大的进步,较现有的制取生物油的方法更具有产业的广泛利用价值。
附图说明
[0019] 图1-应用本发明工艺方法的装置系统示意图
[0020] 图2-载热体加热装置三视图
[0021] 图3-载热体加热装置立体图
[0022] 图4-陶瓷热管结构示意图
[0023] 图中,1-变频电动机;2-预备料斗;3-给料料斗;4-送料机构;5-流化床反应器; 6-载热体分离器;7-载热体加热装置上层;8-载热体加热装置下层;9-气固分离器;10-第一级冷凝器;11-第二级冷凝器;12-集油器;13-气体过滤器A ; 14-气体泵A ; 15-储气罐; 16-气体过滤器B ;17-空气预热器;18-气体泵B ;19_气体缓冲罐;20-鼓风机;21-原料干燥室;22-料仓;23-引风机;24-载热体加热装置外壳;25-陶瓷热管;26-隔热板;27-冷凝段;28-绝热段;29-蒸发段;FI-流量指示器;PI-压力指示器;TI-温度指示器;TC-温度控制器。
具体实施方式
[0024] 为更进一步阐述本发明为达成预定发明目的所采取的技术手段及功效,以下结合附图及较佳实施例,对依据本发明提出的生物质热裂解制取生物油的工艺方法与实现该方法的装置系统结合起来进行详细说明。
[0025] 生物质热裂解制取生物油的工艺过程如下:生物质物料经粉碎、烘干后放入料仓 22中备用。加热载热体产生的高温烟气经气体过滤器B16滤除灰分后,一部分经引风机23 通入原料干燥室21,另一部分通入空气预热器17预热助燃空气,其热量被充分利用后的烟气,通过气体泵B18收集在气体缓冲罐19,从气体缓冲罐19出来的烟气经转子流量计分成两路:流量较大的主路进入流化床反应器5,在反应器底部预热,经气体分布板进入上部的流化床反应器5 ;流量较小的由载气输入管通入,顺着生物质粉料一同进入流化床反应器 5。两路气体在流化床反应器5内一起流化载热体和生物质粉料的混合物,粉料被闪速加热至IJ 500°C-65(TC的最佳热裂解温度,迅速受热分解释放出挥发分,并在1-2秒的时间内被流化气体快速带离流化床反应器5,载热体、产物炭和灰分同时也被气力夹带出流化床反应器 5。从流化床反应器5出来的载热体和热裂解产物进入二级分离系统,首先进入载热体分离器6进行一级分离,其中载热体被分离出来,进入载热体加热装置上层7,剩余的炭、灰分和挥发分再进入气固分离器9,将其中的炭和灰分分离出来进入载热体加热装置下层8。在载热体加热装置下层8燃烧产物炭和不可冷凝气体加热载热体,以供载热体循环使用。干净的挥发分进入后续的第一级冷凝器10和第二级冷凝器11,冷凝得到的生物油收集在集油器12,不可冷凝气体经过脱二氧化碳工艺后用作可燃气通过气体泵A14通入载热体加热装置下层8。
[0026] 实施例
[0027] 本实施例的实施方案如下:
[0028] (1)原料预处理:本实施例以玉米秆为生物质物料,为提高生物油的产率,必须有很高的加热速率,故要求物料有足够小的粒度,将生物质粉料粉碎至粒径l_2mm。为避免原料中过多的水分带到生物油中,要对原料进行干燥。根据实际生产情况,利用装置系统中载热体加热装置下层8排放的高温烟气来为原料干燥室21提供热能,将生物质粉料干燥至含水率小于8%。
[0029] (2)加热载热体:加热载热体(初次使用时燃料是煤气,循环后是热裂解产物炭和不可冷凝气体),使载热体温度达到设定值(500-650°C)。同时,排放的烟气从载热体加热装置的下层8的顶部排烟口排出经过气体过滤器B16滤除灰分后回收利用,一部分经引风机23接入原料干燥室21,利用其热量来干燥生物质粉料,另一部分通入空气预热器17预热助燃空气,其热量被充分利用后的烟气从空气预热器17的出口排出,通过气体泵B18收集在气体缓冲罐19用作流化气体。
[0030] (3)用收集在气体缓冲罐19中的烟气清洗装置系统,造成流化床反应器5内惰性气氛,避免生物质粉料在热裂解时和空气中的氧气接触发生燃烧反应。
[0031] (4)送料:将处理后的生物质粉料倒入预备料斗2中存储,预备料斗2与给料料斗 3连接,在给料料斗3的出口下装有送料机构4,送料机构4中插有输送循环载气以辅助输送生物质粉料的载气输入管。待预备料斗2充满生物质粉料后,关闭预备料斗2的顶盖,使物料处于无氧状态。并打开原先关闭预备料斗2和给料料斗3之间的阀门,将预备料斗2的粉料缓缓加入给料料斗3,在送料机构4和流化气的共同作用下,使生物质粉料能靠重力和流化气的输送作用及铰龙的旋转顺利从流化床反应器5的进料口输入进流化床反应器5。
[0032] (5)热裂解反应:流化床反应器5是生物质快速热裂解的主要装置,其由给料口、 风室、布风板和反应器出口组成。在流化床反应器5下部和载热体加热装置上层7之间连接有一支载热体回送管(所述载热体回送管是倾斜的,倾斜方向与水平面的夹角大于45° ), 在载热体加热装置上层7被加热的载热体(石英砂)靠重力作用顺着载热体回送管进入流化床反应器5。在流化床反应器5底部连接有流化气输入管,通过该输入管,流化气(收集在气体缓冲罐19内的烟气)被输入进流化床反应器5。生物质粉料和载热体在流化气体的作用下充分混合,生物质粉料被闪速加热到温度范围为500-650°C的最佳热裂解温度。生物质粉料迅速受热分解释放出挥发分,并在1-2秒的时间内被流化气体快速带离流化床反应
5 ο
[0033] (6)气固分离:生物质粉料在流化床反应器5内热裂解反应结束后,载热体、炭和灰分同时也被气力夹带出流化床反应器5。从反应器出来的载热体和热裂解产物进入二级分离系统,首先进入载热体分离器6进行一级分离,其中载热体首先被分离出来,进入载热体加热装置上层7。剩余的产物炭、灰分和挥发分再进入气固体分离器9,将其中的炭和灰分分离出来,通过产物炭回送管(所述产物炭回送管是倾斜的,倾斜方向与水平面的夹角大于45° )进入载热体加热装置下层8,燃烧产物炭和不可冷凝气体,以加热载热体。
[0034] (7)载热体回送:载热体加热装置是生物质热裂解制取生物油的主要装置,载热体加热装置分为载热体加热装置上层7和载热体加热装置下层8,两层之间用隔热板沈绝对隔开,其中隔热板26是倾斜的,隔热板沈的倾斜方向与水平面的夹角均大于45° ;载热体加热装置均勻分布有若干陶瓷热管25,陶瓷热管25作为传热元件加热载热体,陶瓷热管 25的工质是钠,陶瓷材料是碳化硅。载热体加热装置上层7连接有载热体回送管,在载热体加热装置的下层底部连接有两条输入管,一条输入管向该层输入回收气(热裂解产物不可冷凝气体经脱二氧化碳工艺后存储在储气罐15);—条输入管向该层输入经过空气预热器17被预热后的助燃空气,该助燃空气由鼓风机20提供(该助燃空气的输入量以保证欠氧燃烧为度)。由于载热体是在上层单独加热,对其温度、加热速率的调节也比现有技术方便。并且加热后的载热体利用重力作用沿着载热体回送管顺利进入流化床反应器5的过程中不会带入空气,保证了反应器缺氧的条件,避免生物质粉料在热裂解时和空气中的氧气接触发生燃烧反应。
[0035] (8)冷凝:冷凝方式和冷却速度对提高生物油的产率和品质有至关重要的影响。 本实施例采用二级快速冷凝。热裂解气从气固分离器9的顶部输出、进入第一级冷凝器10, 冷凝形式采用浮头式热交换器,冷凝介质采用60°C左右的热水。第一级主要冷凝出水分及重油。然后进入第二级冷凝器11,冷凝形式采用喷淋式冷凝器,冷凝介质采用冰水混合物。 第二级主要冷凝出轻质燃料油。二级冷凝器垂直布置,冷凝器的顶部设有清洁塞口,底部设有集油器12 ( —般为钢瓶)。凝结的生物油从该冷凝器的底部输出,进入集油器12中收集起来。不可冷凝气体作为回收气从冷凝器的顶部输出,经脱二氧化碳工艺后用作可燃气输进载热体加热装置的下层8参与加热载热体的过程而进入下一个工作循环。
[0036] 在本具体实施方式中,需要包裹保温材料的设备、装置或管道上,一定要包裹保温材料。本系统还包括观察运行状态的各种仪器、仪表,控制运行状态的各种阀门等。
[0037] 实施结果如下:
[0038] 以玉米秆为试验原料,生物油质量产率为57%。生物油呈棕褐色,几乎包括了醇、 醚、酯、醛、酚、酮和有机酸等所有种类的含氧有机化合物。玉米秆生物油的典型特性和组成数据如表1所示。
[0039] 表 1
[0040]
Claims (4)
1. 一种生物质热裂解制取生物油的方法,其特征在于包括以下步骤:(a)将生物质物料粉碎至粒径l_2mm,干燥至含水率小于8%,将处理后的生物质粉料倒入预备料斗中存储,待预备料斗(¾充满生物质粉料后,关闭预备料斗O)的顶盖,使粉料处于无氧状态;并打开原先关闭预备料斗(2)和给料料斗(3)之间的阀门,将预备料斗O)的粉料缓缓加入给料料斗(3),通过送料机构(4)将生物质粉料送入流化床反应器(5);(b)生物质粉料在流化床反应器(5)内进行热裂解反应结束后,其载热体与产物热裂解气、炭和灰分一道从反应器内被送出;首先进入载热体分离器(6)进行一级分离,其中载热体被分离出来,剩余的炭、灰分和热裂解气再进入气固分离器(9),将其中的炭和灰分分离出来;(c)分离出来的载热体进入载热体加热装置上层(7),产物炭和灰分进入载热体加热装置下层(8),燃烧产物炭和不可冷凝气体以加热载热体;载热体在载热体加热装置上层 (7)被加热到设定温度后依靠重力作用沿着载热体回送管顺利进入流化床反应器(5)内以供循环使用;(d)同时,载热体加热装置下层⑶排放的高温烟气经过气体过滤器B(16)滤除灰分后一部分通入原料干燥室利用其热量对生物质粉料进行干燥,干燥后的生物质粉料收集于料仓02);另一部分通入空气预热器(17),来预加热助燃空气,被预加热后的助燃空气送入载热体加热装置下层(8),进行步骤c所述的燃烧产物炭和不可冷凝气体以加热载热体的过程中进行助燃;其热量被充分利用后的烟气从空气预热器(17)的出口排出,通过气体泵B(18)收集在气体缓冲罐(19)中存储,被分为两路继续输送,流量较大的主路进入流化床反应器(5),在反应器底部预热,经气体分布板进入上部的流化床反应器(5);流量较小的一路通往载气输入管,辅助输送生物质粉料;(e)在步骤b中所述的气固分离完成后,分离出来的热裂解气分别进入第一级冷凝器 (10)和第二级冷凝器(11),并收集冷凝产物于集油器(1¾中;不可冷凝气体与冷凝的生物油分离后,作为回收气收集;不可冷凝气体经脱二氧化碳工艺后通过气体泵A(14)收集在储气罐(1¾中,用作可燃气通入载热体加热装置下层(8)。
2.根据权利要求1所述的生物质热裂解制取生物油的方法,其特征在于,先向气体缓冲罐(19)内通入一定量的烟气后,打开排气阀将气体缓冲罐(19)内所有气体排空,然后储存烟气;工作过程中,根据反应情况,通过调节阀调节进气流量。
3. 一种利用权利要求1所述的生物质热裂解制取生物油方法的装置,其特征在于,包括预备料斗(¾下接给料料斗C3)和送料机构G),送料机构(4) 一端和气体缓冲罐(19) 连接,另一端与流化床反应器(¾连接,流化床反应器(5)的上端面出口与载热体分离器(6)连接,下端面的布风板经风室与气体缓冲罐(19)连接,载热体分离器(6)和气固分离器 (9)的一端连接,载热体分离器(6)的另一端和载热体加热装置上层(7)连接;气固分离器 (9)的底端和载热体加热装置下层(8)连接,气固分离器(9)经第一级冷凝器(10)、第二级冷凝器(11)、气体过滤器A(13)、气体泵A(14)接储气罐(15),储气罐(15)和载热体加热装置下层(8)连接,第二级冷凝器(11)底端接集油器(12),载热体加热装置下层(8)的顶部接气体过滤器B (16),气体过滤器B (16)分别接空气预热器(17)和原料干燥室(21),空气预热器(17) —端经气体泵B (18)接气体缓冲罐(19),另一端分别接鼓风机(20)、载热体加热装置下层(8),原料干燥室(21)分别接料仓(22)、引风机(23) 0
4.根据权利要求3所述的生物质热裂解制取生物油的装置,其特征在于,所述载热体加热装置分为载热体加热装置上层(7)和载热体加热装置下层(8),两层之间用隔热板 (26)绝对隔开,其中隔热板06)是倾斜的,隔热板06)的倾斜方向与水平面的夹角均大于 45° ;载热体加热装置均勻分布有若干陶瓷热管(25),陶瓷热管0¾作为传热元件加热载热体,陶瓷热管0¾的工质是钠,陶瓷材料是碳化硅;在载热体加热装置下层(8)底部连接有两条输入管,一条输入管向该层输入不可冷凝气体,另一条输入管向该层输入经过空气预热器(17)被预热后的助燃空气,该助燃空气由鼓风机00)提供。
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