CN1058839A - 气化燃烧方法及气化发电方法 - Google Patents

气化燃烧方法及气化发电方法 Download PDF

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CN1058839A
CN1058839A CN91104983A CN91104983A CN1058839A CN 1058839 A CN1058839 A CN 1058839A CN 91104983 A CN91104983 A CN 91104983A CN 91104983 A CN91104983 A CN 91104983A CN 1058839 A CN1058839 A CN 1058839A
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藤冈右一
德田君代
一丿濑利光
中岛文也
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Mitsubishi Heavy Industries Ltd
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Abstract

气化燃烧和气化发电方法，其中将燃料和脱硫剂 及空气送入流化床气化炉内，上述燃料一部分气化， 生成的可燃气同时导入燃烧室，上述流化床气化炉内 未气化剩余燃料与脱硫剂一起导入流化床燃烧炉，用 另外供给的空气燃烧，生成的燃烧气导入上述燃烧 室，该燃烧室中上述可燃气用上述燃烧气和另外送入 的空气燃烧。用该燃烧气驱动燃气轮机，并用该燃气 轮机排出的燃烧气产生的蒸汽驱动汽轮机，这两种涡 轮机分别使发电机运转而进行发电。

Description

本发明涉及重质油和煤等低质燃料气化作为用燃气轮机的联合循环工作燃料的气化燃烧方法及气化发电方法。
图4为现有技术中气化燃烧方法所用装置例之一的***图。
煤310和脱硫剂311送入流化床气化炉301，其中煤310气化，煤中硫用脱硫剂311固定成为硫化钙（CaS）。煤310气化生成可燃气313a，在除尘装置303a中除尘。除尘可燃气313b送入燃烧室305。
流化床气化炉301中气化煤生成的炭和脱硫剂的混合物315a及除尘装置303a中回收的炭和脱硫剂的混合物315b送入流化床燃烧炉302中。流化床燃烧炉302中送入空气312b，炭燃烧，硫化钙氧化转化成石膏（CaSO4）。流化床燃烧炉302的流化床内设换热器307，用蒸汽或水318冷却，流化床温度得以调节。
流化床燃烧炉302生成的燃烧气314a在除尘装置303b中除尘。除尘燃烧气314b送入上述燃烧室305中。燃烧室305中流化床气化炉301生成的可燃气313b用从流化床气化炉302导入的燃烧气314b中的剩余氧和另外送入的空气312c燃烧，其燃烧气317送入例如燃气轮机（未示出）。
煤310中灰分和脱硫后脱硫剂311作为流化床燃烧炉302炉底排出灰316a和除尘装置303b排出灰316b原样排除。
燃烧气317量增大时，流化床气化炉301中送入的煤310和空气312a就增加，因此使从流化床气化炉301送入流化床燃烧炉302的炭和脱硫剂315a增加，其中由于送入流化床燃烧炉302的炭量增加，所以空气312b量也增加。燃烧气317量减少时，流化床气化炉301中送入的煤310和空气312a就减少，随后送入流化床燃烧炉302的炭量减少，空气312b也因此减少。
图5为现有重质油发电方法例之一示意图。
重质油601用加压泵502加压后送入气化炉525中。气化炉525中部分燃料601用加压空气607燃烧，使作为热源的碳气化而转换成气体燃料。气化炉625中生成的可燃气608在换热器524中与水610换热而冷到350-450℃。冷却后可燃气608在过滤器505中除尘处理成煤尘浓度1mg/Nm3以下的气体，再送入脱硫装置526中，其中用氧化铁脱硫剂从可燃气608中除去H2S。除尘脱硫后可燃气608a送入燃烧室507，用加压空气607c燃烧成燃烧气609，温度1150-1300℃，再送去驱动燃气轮机509。
根据送入燃气轮机509的燃烧气609的压力和温度可使发电设备送电效率达到最大。燃烧气609能量传给燃气轮机509，用其能量驱动发电机517进行发电。燃气轮机509出口燃烧气609a在排气锅炉510中将热传给水610，温度降至120-130℃后经烟筒514排入大气。
上述排气锅炉510内，设有导入换热器524中冷却可燃气608的水610的换热器521，排气锅炉510中上述燃烧气609a将热能传给换热器524中用以加热可燃气608的水610，水610变为蒸汽611。蒸汽611能量传给汽轮机511，驱动发电机518进行发电。
气化炉525中形成的未燃碳和灰分从气化炉经配管612，料斗515c，516c作为排出灰605a排出。在过滤器505中从可燃气608中回收的尘粒经配管617，料斗515d，516d作为排出灰605b排出。
508为与燃气轮机509直接相连的压缩机，吸入的空气603加压，上述加压空气607送入上述燃烧室507，也送入上述气化炉525。
如图4所示，上述现有气化燃烧方法中，流化床燃烧炉302中设控制燃烧温度的换热器307。但燃料能一部分未作为燃烧气显热送入燃气轮机，直接在汽轮机中回收，所以不用燃气轮机时，发电效率低，这就是问题所在。
该现有方法中，随着流化床气化炉301排出的炭增减，需调节流化床燃烧炉302的空气312b量，所以燃烧气317量变化速度慢。
而且，流化床气化炉301和流化床燃烧炉302间炭移送量变化，为了使燃烧气317温度恒定，需用流化床气化炉301和流化床燃烧炉302间的分配比来调节一定量的空气，所以燃烧气317量变化时，各反应器（炉）的控制就变得非常复杂，这也是缺点所在。
如图5所示，上述发电方法中，脱硫装置所用脱硫剂用了氧化铁，所以脱硫温度最适宜400-450℃。因此必须将气化炉中生成的可燃气冷却至400-450℃。这样一来，必须将可燃气从气化炉出口温度冷至400-450℃，气化炉生成可燃气之热能一部分并不作为驱动燃气轮机的能量，而是用来加热驱动汽轮机的蒸汽，因此并不能使燃气轮机和汽轮机组合使用而达到复合发电设备的理论最大发电效率。
本发明是提出可克服现有技术以上问题的气化燃烧方法和气化发电方法。
为解决上述课题，本发明提出一种燃烧方法，其中将燃料，脱硫剂和空气送入流化床气化炉内，一部分燃料气化，生成的可燃气同时送入燃烧室，上述流化床气化炉内剩余未气化燃料与脱硫剂一起导入流化床燃烧炉，用另外送入的空气燃烧，生成的燃烧气导入上述燃烧室，该燃烧室中上述可燃气用上述燃烧气中的氧和另外送入的空气燃烧。更具体地讲，在上述方法中，上述流化床气化炉，上述流化床燃烧炉和上述燃烧室中送入的总空气量控制为维持上述燃烧室温度所必须的空气量，并且对上述流化床气化炉中直接送入的空气量进行控制以将该流化床气化炉的温度维持在规定值内，对上述流化床燃烧炉中直接送入的空气量进行控制以将该流化床燃烧炉的温度维持在规定值内，而上述燃烧室中直接送入的空气量为上述总空气量减去上述流化床气化炉和上述流化床燃烧炉中直接送入的空气量所得之差。
另外，本发明所涉及的气化发电方法是用上述产生的燃烧室燃烧气驱动燃气轮机，并且该燃气轮机排出的燃烧气产生的蒸汽驱动汽轮机，这两种涡轮机分别使本电机运转而进行发电。
本发明气化燃烧方法中，例如在联合循环负荷变化而要求燃烧室出口燃烧气量增减时，可相互独立地控制空气，将其送入流化床气化炉，流化床燃烧炉和燃烧室，燃烧气量很容易迅速随之变化。
流化床气化炉中形成的可燃气不经冷却直接导入燃烧室，该燃烧室中形成的燃烧气温度高，可简单地使该燃烧室燃烧气量随负荷要求而变化。
如上所述，本发明气化发电方法中，可用燃烧室中形成的高温燃烧气驱动燃气轮机，同时用燃气轮机排出的燃烧气产生的蒸汽驱动汽轮机，所以提高了设备整体热效率。
实施例
图1所示为本发明方法第1实施例所用装置示意图。
煤（10）和脱硫剂（11）送入流化床气化炉（1），其中煤（10）气化，煤中硫用脱硫剂（11）固定成为硫化钙。煤（10）气化生成可燃气（13a），在除尘装置（3a）中除尘。除尘后可燃气（13b）导入燃烧室（5）。
流化床气化炉（1）中未气化煤形成的炭和脱硫剂的混合物（15a）以及除尘装置（3a）中回收的炭和脱硫剂的混合物（15b）送入流化床燃烧炉（2），其中也送入空气，炭燃烧反应，同时硫化钙氧化成石膏。
流化床燃烧炉（2）中形成的燃烧气（14a）在除尘装置（3b）中除尘。除尘后燃烧气（14b）导入上述燃烧室（5），其中可燃气（13b）用燃烧气（14b）中剩余氧和空气（12c）燃烧，形成的燃烧气（17）例如送入燃气轮机（图中未示出）。
煤（10）中灰分和脱硫后脱硫剂分别作为流化床燃烧炉（2）炉底排出灰（16a），而从除尘装置（3b）排出灰（16b）排出。
流化床气化炉（1）中流化床温度为达到高脱硫反应效率且最适于煤气化反应的温度，根据碳种而变化，可达为700-1000℃。而流化床燃烧炉（2）中流化床温度为使硫化钙高效率氧化成石膏且炭高效率燃烧的温度，根据炭种可选为800-1050℃。
本实施例中流化床气化炉（1），流化床燃烧炉（2）和燃烧室（5）的温度分别用检测器（21a），（21b）和（21c）检测，用这些测定值和煤（10）供给量为基础，用控制器（20）计算反应器（1），（2）和（5）中空气（12a），（12b）和（12c）流量，通过控制流量调节阀（19a），（19b）和（19c）而相互独立地调节空气量。
燃烧室（5）出口燃烧气（17）量增大时，流化床气化炉（1）中送入的煤（10）和空气（12a）以及燃烧室（5）中送入的空气（12c）同时增加，燃烧气（17）量就急速壤加。之后从流化床气化炉（1）移送到流化床燃烧炉（2）的炭量也增大，供给流化床燃烧炉（2）的空气（12b）也增加，而供给燃烧室（5）的空气（12c）却减少。燃烧室（5）出口燃烧气（17）量减少时，供给流化床气化炉（1）的煤（10）和空气（12a）以及供给燃烧室（5）的空气（12c）同时减少，之后从流化床气化炉（1）移送到流化床燃烧炉（2）的炭量亦减少，供给流化床燃烧炉（2）的空气（12b）也减少，而供给燃烧室（5）的空气（12c）却增加。因此本实施例中，燃烧室（5）出口燃烧气（17）量很容易迅速发生变化。
本实施例中，流化床燃烧炉（2）内没有现有换热器（图4，307所示），由于不用大量蒸汽或水冷却，所以燃料化学能可全部转换成燃烧气热能。又因这种燃烧气供给燃气轮机，所以联合循环发电效率也比现有水平高。且因流化床燃烧炉（2）内未设换热器，所以流化床燃烧炉建设投资低。
图2所示为本发明方法第2实施例所用装置示意图。本实施例中不经流化床气化炉（1）而直接将煤（106）流化床燃烧炉（2）。
负荷变化时，可按以下顺序使燃烧室（5）出口燃烧气量急速发生变化。例如负荷增大时，供给流化床气化炉（1）的煤（10a）和空气（12a）以及供给流化床燃烧炉（2）的煤（10b）和空气（12b）同时增加，燃烧气（17）量也急速增加。之后随着从流化床气化炉（1）移送到流化床燃烧炉（2）的炭量增加，供给流化床燃烧炉（2）的煤（10b）就减少。
本实施例中，启动时上述流化床气化炉（1）和流化床燃烧炉（2）内同时供给煤（10a）和（10b），同时输送暖气。
图3所示为本发明方法第3实施例所用装置示意图。
重质油201和脱硫剂202以及循环脱硫剂206在混合器101中制成浆料，用加压泵102从常压状态加压后供给加压流化床气化炉103。脱硫剂202可用石灰石或白云石等钙化合物。加压流化床气化炉103的气化压力由后续燃气轮机109的工作压力决定，通常定为15-30ata。加压流化床气化炉103内脱硫剂202粒子用该炉103下方供给的空气207b流化，形成流化床122。流化床122温度定为700-1000℃。流化床122中，重质油热分解，其中的碳和CO2气化反应成CO，同时空气207b和重质油201的热分解产物及空气207b和CO进行燃烧反应，重质油中S与上述脱硫剂202和206反应后作为CaS固定在脱硫剂中。上述脱硫剂还吸附重质油中的V及Na和K等碱金属等，可防止生成气中含有这些成分。可向加压流化床气化炉103供给少量水蒸汽214以更好地控制流化床122的温度并抑制未燃碳量。
加压流化床气化炉103中温度定为700-1000℃，加入的重质油201中40%以上的碳气化成可燃气208，后于旋风分离器104a中除去其中的脱硫剂粒子，再送入过滤器105a。旋风分离器104a中回收的脱硫剂粒子216回收入流化床122中，根据粒子216量，可将其一部分送入后续的流化床燃烧炉119。
过滤器105a中回收的可燃气208中的脱硫剂等粒子217可送入后续的流化床燃烧炉119。
上述流化床气化炉103内流化床122的床高保持一定值，可将脱硫剂粒子及未燃分等粒子212从加压流化床气化炉103送入后续流化床燃烧炉119。
过滤器105a中通过的尘粒量非常低的可燃气208a在氨分解塔106中，用压缩机108加压的空气207d部分燃烧，将可燃气208a的温度升为900-1000℃，然后通过该氨分解塔106内配置的含镍催化剂，可燃气208a中的氨（NH3）及HCN等分解成（N2）。可燃气208a的温度取决于可燃气中含有的H2S以及催化剂的耐久性。可燃气208a从氨分解塔106送入燃烧室107，其中从压缩机108来的空气207c及后续流化床燃烧炉的燃烧气215a完全燃烧，燃烧气209的温度达到1250℃-1500℃，然后送入燃气轮机109。该燃烧气209的温度取决于燃气轮机109的材料构造，温度高，则发电效率升高，反之，则燃气轮机寿命缩短，应选为最适宜的温度。燃烧气209在燃气轮机109中放出能量使其运转，该能量再通过发电机117变成电能。
燃烧气209a通过燃气轮机109减压至近乎常压，然后送入排热锅炉110。排热锅炉110中，燃烧气209a传给换热器121中的水210。水210在换热器中受热蒸发成水蒸汽211。水蒸汽211接受的能量传给汽轮机111使其运转，该汽轮机驱动发电机118，最终变为电能。
汽轮机111排出的水蒸汽211经冷凝器112冷凝，用加压泵113加压后再送入换热器121。
流化床燃烧炉119内导入的空气207a使流化床127流化，从上述加压流化床气化炉103送入的脱硫剂粒子及未燃分等粒子212在该流化床127内将粒子212中的CaS氧化成CaSO4并使未燃分燃烧。
为使CaS转变成CaSO4，流化床燃烧炉内的温度定为600-1000℃。从流化床燃烧炉119炉底排出的脱硫剂粒子213通过联二料斗115a、116a导入分离器120，该分离器120中含CaCO3，CaO的大量粗粒子作为循环脱硫剂206c送入粉碎器123，其中剩余微粉粒子作为排出灰206a排出。上述粉碎器123中粉碎成微粉粒子的循环脱硫剂206送入上述混合器101，作为脱硫剂的一部分回送入加压流化床气化炉103。流化床燃烧炉119中生成的可燃气215送入旋风分离器104b以分离脱硫剂，分离的脱硫剂218回送入流化床燃烧炉119。
另一方面，分离脱硫剂218的燃烧气导入过滤器105b，其中分离出脱硫剂和灰的燃烧气215a导入燃烧室107。过滤器105b中回收的灰和脱硫剂通过联二料斗作为排出灰排出。
上述排气锅炉110中通过的燃烧排气209b经烟筒114扩散到大气中。该燃烧排气209b，如前所述，在加压流化床气化炉103中脱硫并除去Na，K等碱金属和V，而氨分解塔106中氨（NH3），HCN等分解成氮，这样可减少燃烧排气209b中NOX含量，可作为净化气从烟筒排入大气。
上述压缩机108与燃气轮机109直接相连并被驱动，吸入空气203并加压成高压，加压空气207作为前述空气207a，207b分别送入流化床燃烧炉119及加压流化床气化炉103，加压空气107c、107d送入氨吸收塔106和燃烧室107。
如上所述，本实施例中，重质油的化学能转变为电能，重质油中的S、V、Na、K等固定吸收到排出灰206a和206b中，除去NH3、HCN等的重质油201中N可作为N2扩散到大气中。
本实施例中，加压流化床气化炉103及流化床燃烧炉119中未设换热器，因此可缩小这些炉的容量，起动和负荷容易。此外，两炉103，119中形成的气体不进行换热就导入燃烧室及燃气轮机，因此热效率高并提高发电端效率。
本实施例应用重质油，用煤时要用联二料斗，或作为含水浆料用加压泵供给加压流化床气化炉103，同样可作为发电用燃料。
本实施例中，为使上述低质燃料中40%的碳转换成气体，可将流化床温度设为700℃以上。通过调节供给该炉的空气量可控制该流化床气化炉温度。
镍催化剂使NH3，HCN的分解从500℃左右开始，实际上在900℃以上进行反应，这样可防止催化剂形成气中所含硫中毒。因此，流化床气化炉发生气与含镍催化剂接触时温度可定为900-1100℃。
按照本发明气化燃烧方法，煤和重质油等低质燃料气化后用作联合循环等的工作燃料时，对负荷变化的响应性良好并同时可实现高效率的气化燃烧，在燃烧室中可产生高温燃烧气。
按照本发明气化发电方法，用燃烧室产生的高温燃烧气可提高设备热效率，因此可同时提高送电端效率，缩小了流化床气化炉和流化床燃烧炉的容量，起动容易和负荷应性良好。与现有技术中煤气化气在400-450℃除尘，脱硫后在燃烧室燃烧，燃气轮机和汽轮机复合发电情况相比，本发明送电端效率可提高约2%左右。
图1为本发明第1实施例所用装置示意图。
图2为本发明第2实施例所用装置示意图。
图3为本发明第3实施例所用装置示意图。
图4为现有气化燃烧方法示意图。
图5为现有气化发电方法示意图。

Claims (4)

1、气化燃烧方法，其特征在于将燃料和脱硫剂及空气送入流化床气化炉内，上述燃料一部分气化，生成的可燃气同时导入燃烧室，上述流化床气化炉内未气化剩余燃料与脱硫剂一起导入流化床燃烧炉，用另外供给的空气燃烧，生成的燃烧气导入上述燃烧室，该燃烧室中上述可燃气用上述燃烧气和另外送入的空气燃烧。
2、权利要求1的方法，其特征在于流化床气化炉，流化床燃烧炉及燃烧室中送入的总空气量控制为维持燃烧室温度所必须的空气量。
3、权利要求2的方法，其特征在于对上述流化床直接送入的空气量进行控制以将该流化床气化炉的温度维持在规定值内，对上述流化床燃烧炉中直接送入的空气量进行控制以将该流化床燃烧炉的温度维持在规定值内，而燃烧室中直接送入的空气量为按上述总空气量减去上述流化床气化炉和上述流化床燃烧炉中直接送入的空气量所得之差送入的空气量。
4、气化发电方法，其特征在于：将燃料和脱硫剂及空气送入流化床气化炉内，上述燃料一部分气化，生成的可燃气同时导入燃烧室，上述流化床气化炉内未气化剩余燃料与脱硫剂一起导入流化床燃烧炉，用另外供给的空气燃烧，生成的燃烧气导入上述燃烧室，该燃烧室中上述可燃气用上述燃烧气和另外送入的空气燃烧，用该燃烧气驱动燃气轮机，并用该燃气轮机排出的燃烧气产生的蒸汽驱动汽轮机，这两种涡轮机分别使发电机运转而进行发电。
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CN105754661A (zh) * 2015-05-23 2016-07-13 刘全胜 一种不间断自动控制的生物质燃气发电装置
CN107841346A (zh) * 2017-11-01 2018-03-27 浙江大学 煤炭空气部分气化热电燃气多联产装置及方法

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CN100386413C (zh) * 2006-01-17 2008-05-07 东北大学 煤高温气化高温贫氧燃烧一体化***
CN105754661A (zh) * 2015-05-23 2016-07-13 刘全胜 一种不间断自动控制的生物质燃气发电装置
CN107841346A (zh) * 2017-11-01 2018-03-27 浙江大学 煤炭空气部分气化热电燃气多联产装置及方法

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DE69100679T2 (de) 1994-04-28
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EP0468357B1 (en) 1993-11-24
EP0468357A1 (en) 1992-01-29
CN1022061C (zh) 1993-09-08

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