CN103189473A - 用于在间接加热的气化过程中制备焦炭的方法和装置 - Google Patents
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Abstract
本发明涉及一种用于在间接加热的气化工艺中制备焦炭(PC)的方法,其中向气化反应器(1)供应煤颗粒,将气化工艺中供应的工艺气体(P)在气化反应器(1)中还原为合成气(S),借此将合成气(S)从气化反应器(1)移除。本发明还涉及用于实施所述方法的装置。根据本发明的方法的区别之处在于,在气化进行的同时,煤的焦化也在气化反应器(1)内部布置的内反应器(4)中进行,内反应器(4)被间接加热,在焦化过程中焦炭(PC)和可燃气体在内反应器(4)中产出,而可燃气体则被用于气化反应器(1)的气化过程中的间接加热。
Description
技术领域
本发明涉及一种用于在间接加热的气化过程中制备焦炭的方法,其中向气化反应器供应煤颗粒,并将气化过程中供应的工艺气体(process gas)在气化反应器中还原为合成气,由此将合成气移出气化反应器。本发明还涉及实施所述方法的装置。
背景技术
煤是一种基础物质,其不仅是我们最重要的能源,还是许多类型工艺中的重要化学物质。煤的强还原电位被用于例如用煤还原铁矿石的冶金工艺中。此外,从钢铁工业回收氧化性残余物料是煤利用的一个例子。这些工艺目前主要基于经预处理以获得对于例如焦炭炉中的工艺过程的强度和性质合适的化石煤。如果可引入再生煤(基于生物质),应能够减少来自这些类型的工艺的二氧化碳排放。本专利描述一种用于在生物质的间接加热气化过程中通过对煤进行碳化来制备用作例如还原剂的煤/焦炭的方法。
气化是一种从固体燃料产生气态燃料的方法。该技术被用于煤、残余煤产物、石油残余物、废物和生物质。该反应是基于以下事实,即氧化性气体(例如CO2和H2O)被加热,并与煤([C]还原剂)反应,其间形成一氧化碳(CO)和氢气(H2),其中热量被用来驱动吸热的反应。一氧化碳(CO)和氢气(H2)的气体混合物通常被称为合成气。
常规的气化方法是在供应过热蒸汽下以远远低于化学计量的方式燃烧煤。燃烧向装置供应热量和燃烧废气(CO2和H2O)。没有燃烧但过热的煤与废气和供应的蒸汽反应。煤(C)将二氧化碳(CO2)还原为一氧化碳(CO),并将水蒸气(H2O)还原为氢气(H2)。所用的热量降低温度,并且反应性下降。煤的反应性很大程度依赖于温度,同时反应的平衡性也依赖于温度。虽然存在基于空气的燃烧,但是基于氧气的燃烧仍是目前与气化相关的用于燃烧的主要方法。
煤、残余煤产物、石油残余物、废物和生物质气化的问题在于它们不是均质材料,而是在反应过程中释放出的不同重量的组分(焦油)和复杂的组分(芳族物)。这些组分不能可靠地反应,而必须在可使用合成气,或进一步将合成气精炼为液体烃或其它燃料之前进行后续分离。
在气化反应之前,可通过将煤、残余煤产物、石油残余物、废物和生物质热解而分离这些具有不同重量的组分(焦油)和复杂组分(芳族物)。此时获得的且由可冷凝产物和气体组成的热解产物可以用作气化工艺中的燃料。在上述的气化中,热解反应是工艺的一部分。但是,具有不同重量的组分(焦油)和复杂的组分(芳族物)与工艺中想要得到的合成气在同一反应器中。因此,在没有例如冷凝、包壳(cladding)等反应器本身存在的物理问题下,具有不同重量的组分(焦油)和复杂的组分(芳族物)的处理成为气化工艺有效性的限制因素。
以前从US4007014已知一种用于使活性炭再活化的装置和方法。该装置包括干馏反应器和向其供应活性炭的内反应器,其中将提供的活性炭再活化,这是因为蒸汽形式的反应器气体与向下传入内反应器的活性炭接触。为了使反应器气体能够进入内反应器中,反应器在其夹套表面中设置有开口,即在干馏反应器和内反应器之间发生气体交换。这与本发明的基本原理之一恰恰相反。
以前从SE532711已知一种用于制备合成气的方法和装置,其中反应器的间接加热通过反应器中存在的燃烧器进行。
发明内容
本发明的主要目的涉及一种方法和装置,其通过使用间接加热的气化反应器,能够管控上述的合成气净化和物理性限制现象的问题。
在间接加热的气化过程中的煤的同步碳化(carburization)是指用于碳化的热量可从用于气化工艺的反应器获得。为此目的而设计、并具有单独料流的加热反应器布置在气化反应器中。用于煤的加热反应器被气化反应器内部的辐射间接加热。在已经焦化的煤在底部出料前,为了在气化反应器中被加热处理至高温,煤被进料入该内加热反应器的顶部。气体向上通过反应器而煤向下通过。此逆流运动使反应器的温度和组成变化达到均衡。较重的组分(如芳族物)可依靠反应器中的高温而裂解成较小的分子。焦化而来的可燃气体被返回并与生物质热解放出的燃料气体混合。全部燃料气体体积可用于干燥、热解、焦化和气化的加热要求。如果产生任何余量,它可以有利地用于进一步的能量要求等。
本发明的目的和特征通过以下的独立权利要求的特征所给出的方法和装置来实现。本发明的优选实施方案限定于从属权利要求中。
附图说明
下面参照所附附图来描述根据本发明的一个优选实施方案,其中:
图1示出了根据本发明的一个优选方法的流程图,该流程图也示意性地示出了形成用于实施该方法的装置的单元。
具体实施方式
图1示意性地示出了形成用于实施该方法的装置的多个单元。将装置单元连接在一起的线路、管道等未详细说明或示出。合适地形成线路、管道等以实现它们的功能,即在装置的单元之间传输气体和固体物质。
图1示出了间接加热的气化反应器1,其通常是一个陶瓷衬里的反应器。该反应器以这样的方式构成,即它可以在两个独立的料流C1和C2中气化和焦化煤颗粒C。因此,用于焦化煤的内反应器4并入气化反应器1中。固体煤颗粒的一部分通过料流C2被供应至内反应器4中,并且部分通过料流C1和工艺气体P一起通过喷射喷嘴5被供应至气化反应器1中。煤颗粒C来自气化前的热解。料流C1的煤颗粒C的尺寸优选足以能与工艺气体P的进气流一起被载入气化反应器1。通向内反应器4的煤颗粒通常大于外部气化反应器1的煤颗粒。工艺气体P可以是蒸汽或从燃烧阶段回收或净化的废气A。内反应器4中的焦化减少了该料流中的煤的量,因为形成了类似于热解气的可燃气,但是其组成由反应器温度控制,而此时的反应器温度显著更高。高于之前热解中的温度的内反应器4中的煤从300℃至700℃的升温预计会使固体煤组分减少10%至35%。
如果工艺气体P是经回收的废气A,其可以含有水蒸气(H2O)和二氧化碳(CO2)。工艺气体P被从换热器2中排出的合成气S提取的热量预热。气化反应器1中发生的反应是通过喷射喷嘴5喷入的料流C1将工艺气体P中的组分(H2O和CO2)还原为合成气S(H2和CO),其消耗由燃烧器Br 1供应至Br n的热量。通过来自燃烧器Br 1至Br n的供热,经由所进行的气化过程,使得焦化反应在内反应器4中并行地发生。
气化反应器1被燃烧器Br 1至Br n间接加热(其中n指气化反应器1所需的燃烧器数量)。内反应器4以相同的间接方式被燃烧器Br 1至Br n间接加热。通过Br 1至Br n的辐射,向气化反应供应热量,其中燃烧发生在辐射管内,即与气化料流是隔离的。在气化反应器1中,Br 1至Br n与工艺气体P或其反应产物之间没有发生直接的气体交换。内反应器4与气化反应器1中进行的气化工艺也没有发生气体交换。
用燃料F供应燃烧器Br 1至Br n,燃料F优选地来自于之前的含煤材料的热解步骤。供应以空气、富氧气的空气或纯氧气的形式存在的氧化剂O用于燃烧。换热器3从排出的废气A中提取热量,并预热进入的氧化剂O。废气A进入烟气净化器,其中如进入的含煤材料所要求的,使用旋风分离器、催化净化器、过滤器(电气的或织物的)和洗涤器,以满足对于工艺排放所涉及的要求。
煤C来自之前的热解步骤且含有灰分残余物。通过将气化反应器1中的温度控制至低于(或高于)灰分的熔化温度,优选地可通过后续的高温旋风分离器(或以流动形式例如熔渣)将其除去。
排出的合成气S可用作用于燃烧目的的能量气体,或用作用于进一步精制为液体燃料的基料(用于典型的运输工具燃料的费托合成、乙醇生产等)。
气化反应器1中的压力可控制为从大气压至高得多的压力(>100巴(g))。
可控制气化反应器1和内反应器4的温度,以获得合成气S和焦炭PC的最大收率。典型的数值在750-1300℃之间。
另一种可选的工艺气体P和煤C的间接加热的实施方案是可布置在反应器内部的管道***,其中燃烧发生在该反应器中,并且在这种情况下所述管道***成为气化反应器1和内反应器4。该设计可认为特别是具有显著更高温度的炉。
气化反应器1的几何结构由气化工艺所需的反应时间控制,而反应时间则由所选的温度控制。内反应器4的几何结构由煤焦化的质量流量以及在为反应器1选择的温度下将煤变为焦炭的加热升温和保持时间的要求来控制。该几何结构可以是以管形式而旋转对称的,这可以实现非常紧凑的气化过程,至与炉子类似的、进而不需要旋转对称的更大容积的设计。所述反应器的尺寸可以设计成从小规模到非常大的工业规模。
来自气化反应器1的合成气S(H2和CO)含有高达60%的氢气,其余为一氧化碳、二氧化碳或甲烷,其基于进料的工艺气体P的组成。
具有用于煤焦化的内反应器的间接加热的气化反应器的热效率程度变得非常高,并且,包括之前的热解步骤以及所需的干燥在内,该集成装置可达到高达80%的热效率。
Claims (10)
1.在间接加热的气化过程中制备焦炭(PC)的方法,其中向气化反应器(1)供应煤颗粒,并且将气化过程中供应的工艺气体(P)在气化反应器(1)中还原为合成气(S),借此将合成气(S)从气化反应器(1)移除,其特征在于,在气化进行的同时,煤的焦化也在气化反应器(1)内部布置的内反应器(4)中进行,内反应器(4)被间接加热,焦炭(PC)和可燃气体在焦化过程中在内反应器(4)中产出,并且所述可燃气体被用于在气化反应器(1)中的气化中的间接加热。
2.权利要求1的方法,其特征在于,工艺气体(P)通过合成气(S)的换热而被预热。
3.权利要求1或2的方法,其特征在于,内反应器(4)被间接加热。
4.前述权利要求中任一项的方法,其特征在于,在焦化过程中煤释放出被利用的可燃气体。
5.前述权利要求中任一项的方法,其特征在于,气化反应器(1)和内反应器(4)中的温度在750°-1300°之间。
6.前述权利要求中任一项的方法,其特征在于,在气化反应器(1)的压力可以控制为从大气压至高于100巴(g)的压力。
7.用于在间接加热的气化过程中制备焦炭(PC)的装置,其中所述装置包括气化反应器(1)、布置在气化反应器(1)中产生辐射热的燃烧器(Br 1-Brn),并包括用于向气化反应器(1)内部供应煤颗粒和工艺气体的喷射喷嘴(5)、布置在气化反应器(1)中的内反应器(4),并且以这样的方式形成内反应器(4):在焦化过程中煤颗粒通过内反应器(4),其特征在于,提供从内反应器(4)向燃烧器(Br 1-Br n)传导在焦化过程中产生的可燃气体的手段。
8.权利要求7的装置,其特征在于,内反应器(4)具有位于气化反应器(1)外部的用于煤颗粒的供应端部,并且内反应器(4)具有位于气化反应器(1)外部的用于焦化煤的出料端部。
9.权利要求7或8的装置,其特征在于,其包括用于加热工艺气体(P)和冷却合成气(S)的第一换热器(2)。
10.权利要求9的装置,其特征在于,其包括从源自燃烧器(Br 1-Br n)中燃烧的废气中提取热量的第二换热器(3)。
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CN104140848A (zh) * | 2014-07-01 | 2014-11-12 | 江苏金江生物能源科技有限公司 | 一种子母垃圾秸秆气化炉 |
CN104232170A (zh) * | 2014-09-05 | 2014-12-24 | 黄熙瑜 | 一种生物质能源综合利用方法 |
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