CN105371291A - 烟气余热梯级利用协同脱除so3提高除尘效率的系统 - Google Patents
烟气余热梯级利用协同脱除so3提高除尘效率的系统 Download PDFInfo
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- CN105371291A CN105371291A CN201510755994.2A CN201510755994A CN105371291A CN 105371291 A CN105371291 A CN 105371291A CN 201510755994 A CN201510755994 A CN 201510755994A CN 105371291 A CN105371291 A CN 105371291A
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- heat exchanger
- pressure heater
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- cold
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- 239000000428 dust Substances 0.000 title claims abstract description 31
- 239000000779 smoke Substances 0.000 title abstract description 9
- 239000002918 waste heat Substances 0.000 title abstract description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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- 239000007789 gas Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical group 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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Abstract
本发明涉及一种烟气余热梯级利用协同脱除SO3提高除尘效率的系统。该装置包括锅炉、与锅炉尾部烟道依次连接的脱硝装置、空气预热器、电除尘器、引风机、脱硫吸收塔、烟囱,设置在旁路的低压加热器、高压加热器、换热器,以及设置在各管路上用于流量控制的调节阀和流量泵,空气预热器并联第一旁路,空气预热器与电除尘器之间设有第二旁路,引风机与脱硫吸收塔之间设有第三旁路。本发明遵循能量梯级利用原理,将锅炉烟气分三部分进行余热利用,深度回收了烟气余热;另一方面,本发明可以改变烟气中粉尘的比电阻,提高电除尘的除尘效率,减低烟气中SO3浓度。
Description
技术领域
[0001] 本发明涉及一种燃煤电厂尾部烟气余热利用系统,特别是一种烟气余热梯级利用协同脱除303提尚除尘效率的系统。
背景技术
[0002]目前,针对部分燃煤机组存在排烟温度偏高,排烟热损失大的问题。排烟热损失是锅炉运彳丁中最重要的一项热损失,一般约为5% —12%,占锅炉热损失的60% — 70%,影响排烟热损失的主要因素是排烟温度,一般情况下,排烟温度每增加10°C,排烟热损失增加0.6% — 1%。另外排烟温度高,还会造成飞灰比电阻偏大,导致电除尘的除尘效率下降。传统的烟气余热利用系统(低压省煤器)能量利用效率低,未应用能量梯级利用原理,充分高效回收烟气余热,提高机组热效率;同时随着环保新政策的出台,大部分燃煤火电机组要求实现超低排放要求,通过系统的协同脱除原理是机组能否实现超低排放的关键技术,此发明技术针对现国家最新出台的《关于印发落实煤电节能减排升级与改造行动计划的通知》发改能源2014(2093号)实现燃煤火电机组系统的节能减排的技术方案。
发明内容
[0003] 本发明所要解决的技术问题是提供一种结构设计合理、能够深度回收尾部烟气余热、主要应用于大型电站锅炉排烟温度偏高以及配套执行超低排放的机组的烟气余热梯级利用协同脱除303提高除尘效率的系统。
[0004] 本发明解决上述技术问题所采用的技术方案如下:
[0005] 烟气余热梯级利用协同脱除S03提高除尘效率的系统,包括锅炉、与锅炉尾部烟道依次连接的脱硝装置、空气预热器、电除尘器、引风机、脱硫吸收塔、烟囱,设置在旁路的低压加热器、高压加热器、换热器,以及设置在各管路上用于流量控制的调节阀和流量栗,空气预热器并联第一旁路,第一旁路包括一级换热器、二级换热器、第一高压加热器、第二高压加热器、第三高压加热器,一级换热器通过调节阀及连接管路分别与第二高压加热器的进水口管道和出水口管道连接,二级换热器通过调节阀及连接管路分别与第三高压加热器的进水口管道和出水口管道连接;
[0006] 空气预热器与电除尘器之间设有第二旁路,第二旁路包括三级换热器、第五低压加热器、第八低压加热器,三级换热器设置在空气预热器与电除尘器之间,三级换热器通过调节阀及连接管路分别与第八低压加热器的出水口管道、第五低压加热器的进水口管道连接;
[0007]引风机与脱硫吸收塔之间设有第三旁路,第三旁路包括末级换热器、末级换热器冷一次风管道、末级换热器冷二次风管道,末级换热器设置在引风机与脱硫吸收塔之间,末级换热器、末级换热器冷一次风管道、末级换热器冷二次风管道及调节阀通过循环管路形成闭式循环系统。
[0008] —方面,本发明通过设置第一旁路、第二旁路和第三旁路,遵循能量梯级利用原理,将锅炉烟气分三部分进行余热利用,深度回收了烟气余热;另一方面,本发明可以改变烟气中粉尘的比电阻,提高电除尘的除尘效率,减低烟气中so3浓度;再一方面,本发明通过设置旁路和并联的结构,实现了对大量锅炉尾部烟气和水进行热交换。
[0009] 作为优选,末级换热器分别与末级换热器冷一次风管道、末级换热器冷二次风管道连接,且末级换热器冷一次风管道、末级换热器冷二次风管道为并联结构。其优点在于,烟气的热量在末级换热器进行交换,并分别通过末级换热器冷一次风管道、末级换热器冷二次风管道对冷一次风和冷二次风进行加热,提高热交换效率和能源利用效率,同时提高空气预热器蓄热元件冷端温度,避免空气预热器蓄热原件堵塞问题。
[0010] 作为优选,末级换热器冷一次风管道、末级换热器冷二次风管道分别通过空气预热器与锅炉连接。其优点在于,加热冷一次风和冷二次风,部分替代常规蒸汽暖风器,提高空气预热器蓄热元件冷端温度,避免空气预热器蓄热原件堵塞问题。
[0011] 作为优选,末级换热器利用水作为中间介质,且水介质流向与烟道内烟气流向相反,采用逆流布置方式。其优点在于,水作为中间介质换热效果好,可以更好地进行热交换,使得离开末级换热器的烟气,提高热交换效率;而且价格低,不容易腐蚀,和机组的热力系统容易耦合,补汽加热方便。
[0012] 作为优选,第五低压加热器与第八低压加热器之间还设有N级低压加热器。其优点在于,在第五低压加热器进口的凝结水能够获得更多的热量,升至更高的温度。
[0013] 作为优选,一级换热器、二级换热器为串联结构。其优点在于,在第一旁路中分两级对烟气进行热交换,同时利用二级换热器对较低温的第二高压加热器的进水进行加热,又利用一级换热器对其再次加热,从而获得更高的热交换效率。
[0014] 作为优选,末级加热器热段采用的材料为FPM、UPVC、NBR、CR、EPDM、CPVC、PP、PE或PVDFo其优点在于,采用耐腐蚀的非金属受热段,能够降低脱硫系统入口烟气温度,减少脱硫系统入口减温水使用量,同时减少脱硫系统中石膏浆液的携带,提高脱硫系统的吸尘效率。
[0015] 本发明所述的FPM指氟橡胶,UPVC指未增塑聚氯乙烯,NBR指丁腈橡胶,CR指氯丁橡胶,EPDM指三元乙丙,CPVC指氯化聚氯乙烯,PP指聚丙烯系列(百折胶),PE指聚乙烯,PVDF指聚偏二氟乙烯,这些均为耐腐蚀的非金属材料。
[0016] 本发明的系统流程如下:
[0017] 烟气经过脱硝后温度在30(TC—40(TC,部分烟气通过第一部分空气预热器并联烟道一级换热器、二级换热器的烟气一水换热,加热第一高压加热器和第二高压加热器的进口凝结水;烟气在经过空气预热器后烟气温度在125°C左右,通过第二部分换热器吸收烟气余热,加热第五低压加热器进口凝结水,进入电除尘器前烟气温度能降低到100°C左右;最后烟气通过引风机和吸收塔之间的第三部分末段余热利用装置,末级加热器以水作为中间介质,继续吸收烟气余热,吸收的热量一部分加热冷一次风,一部分加热冷二次风,提高空气预热器的进口风温。烟气进入吸收塔的温度70°C左右,实现烟气余热的梯级高效利用,同时改变烟气量及粉尘比电阻特性,实现协同脱出粉尘及S03,降低烟气的比体积,降低引风机耗电率等。
[0018] 本发明同现有技术相比具有以下优点及效果:
[0019] 1、降低了排烟温度,减少了排烟热损失,提高锅炉效率,实现了烟气余热梯级利用。
[0020] 2、进入电除尘器的烟气温度降低,有效降低飞灰比电阻,提高电除尘器的除尘效率,另外由于烟气温度接近烟气酸露点温度,呈液态的so3易被烟气中的粉尘颗粒吸附,从而被电除尘器脱除,达到协同脱除so3的效果,避免后续环保设备的酸腐蚀。
[0021] 3、烟气换热器的部分热量加热汽轮机凝结水系统,减少汽机抽汽,提高了机组运行的经济性。
[0022] 4、烟气温度降低,烟气量减少,降低引风机电耗,脱硫吸收塔入口烟气温度降低,减少脱硫吸收塔入口减温水量,另外进入脱硫吸收塔内烟气量减少,提高脱硫系统的脱硫效率。
附图说明
[0023] 为了更清楚地说明本发明实施例或现有技术中的技术方案,下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍,显而易见地,下面描述中的附图仅仅是本发明的一些实施例,对于本领域普通技术人员来讲,在不付出创造性劳动的前提下,还可以根据这些附图获得其他的附图。
[0024] 图1为本发明的结构示意图。
[0025] 标号说明:
[0026] 1、锅炉 2、脱硝装置
[0027] 3、空气预热器 4、电除尘器
[0028] 5、引风机 6、脱硫吸收塔
[0029] 7、烟囱 8、一级换热器
[0030] 9、二级换热器 10、三级换热器
[0031] 11、末级换热器 12、末级换热器冷二次风管道段
[0032] 13、末级换热器冷一次风管道段 14、第一高压加热器
[0033] 15、第二高压加热器 16、第三高压加热器
[0034] 17、第五低压加热器 18、第八低压加热器
[0035] 19、流量栗 20、调节阀
具体实施方式
[0036] 下面结合实施例对本发明做进一步的详细说明,以下实施例是对本发明的解释而本发明并不局限于以下实施例。
[0037] 实施例1:
[0038] 如图1所示,本实施例包括锅炉1、顺着锅炉1尾部烟道依次连接的脱硝装置2、空气预热器3、电除尘器4、引风机5、脱硫吸收塔6和烟囱7。在空气预热器3上并联第一旁路,第一旁路由一级换热器8和二级换热器9通过调节阀20及连接管路分别与第二高压加热器15和第三高压加热器16的进水口管道和出水口管道连接组成。在机组高负荷工况下,煤质较差工况下,尤其是燃用劣质燃料如褐煤等燃料,燃料燃烧后烟气量大于空气预热器3设计烟气量工况下,一部分烟气可以通过第一旁路。其中高温烟气段通过一级换热器8加热第一高压加热器14的给水,低温烟气段通过二级换热器9加热第二高压加热器15的给水,实现能量的梯级利用,降低排烟温度,提高经济效益。
[0039] 在空气预热器3和电除尘器4之间布置第二旁路,该第二旁路由三级换热器10分别与第八低压加热器18的出水管道和第五号低压加热器17的进水口管道连接组成。利用空气预热器3出口的烟气余热加热第五低压加热器17进口凝结水温度,作用等同于低低温省煤器。烟气在进入电除尘器4前温度降低到95°C左右,降低电除尘系统飞灰比电阻,提高电除尘器4的除尘效率,另外由于烟气温度接近烟气酸露点温度,呈液态的S03易被烟气中的粉尘颗粒吸附,从而被电除尘器4脱除,达到协同脱除303的效果。通过低低温省煤器降低烟气温度,改变烟气中灰的比电阻特性,提高收尘效率,提高电除尘的除尘效率,同时降低烟气流量,降低引风机5耗电率,提高机组经济效益。
[0040] 在引风机5和脱硫吸收塔6之间布置第三旁路,该第三旁路由末级换热器11、末级换热器冷一次风管道段13、末级换热器冷二次风管道段12及循环管路组成闭式循环系统。其中末级换热器11热段采用耐腐蚀的非金属材料,如FPM、UPVC、NBR、CR、EPDM、CPVC、PP、PE或PVDF。第三旁路能够降低脱硫系统入口烟气温度,减少脱硫系统入口减温水使用量,同时减少脱硫系统中石膏浆液的携带,提高脱硫系统的吸尘效率。
[0041] 另外循环水在末级换热器11吸收烟气热量,升温后在末级换热器冷一次风管道段13和末级换热器冷二次风管道段12分别加热冷一次风和冷二次风,部分替代常规蒸汽暖风器,提高能源利用效率,同时提高空气预热器3蓄热元件冷端温度,避免空气预热器3蓄热原件堵塞问题。
[0042] 调节阀20可根据机组负荷变化,灵活调节调节阀20开度,改变烟气余热利用装置水流量。
[0043] 流量栗19根据需要设置在各管路上,作为水流动力,并与调节阀20配合,用于流量控制。
[0044] 此外,需要说明的是,本说明书中所描述的具体实施例,其零、部件的形状、所取名称等可以不同。凡依本发明专利构思所述的构造、特征及原理所做的等效或简单变化,均包括于本发明专利的保护范围内。本发明所属技术领域的技术人员可以对所描述的具体实施例做各种各样的修改或补充或采用类似的方式替代,只要不偏离本发明的结构或者超越本权利要求书所定义的范围,均应属于本发明的保护范围。
Claims (7)
1.一种烟气余热梯级利用协同脱除so3提高除尘效率的系统,包括锅炉、与锅炉尾部烟道依次连接的脱硝装置、空气预热器、电除尘器、引风机、脱硫吸收塔、烟囱,设置在旁路的低压加热器、高压加热器、换热器,以及设置在各管路上用于流量控制的调节阀和流量栗,其特征是:所述空气预热器并联第一旁路,所述第一旁路包括一级换热器、二级换热器、第一高压加热器、第二高压加热器、第三高压加热器,所述一级换热器通过调节阀及连接管路分别与第二高压加热器的进水口管道和出水口管道连接,所述二级换热器通过调节阀及连接管路分别与第三高压加热器的进水口管道和出水口管道连接; 所述空气预热器与电除尘器之间设有第二旁路,所述第二旁路包括三级换热器、第五低压加热器、第八低压加热器,所述三级换热器设置在空气预热器与电除尘器之间,所述三级换热器通过调节阀及连接管路分别与第八低压加热器的出水口管道、第五低压加热器的进水口管道连接; 所述引风机与脱硫吸收塔之间设有第三旁路,所述第三旁路包括末级换热器、末级换热器冷一次风管道、末级换热器冷二次风管道,所述末级换热器设置在引风机与脱硫吸收塔之间,所述的末级换热器、末级换热器冷一次风管道、末级换热器冷二次风管道及调节阀通过循环管路形成闭式循环系统。
2.根据权利要求1所述的烟气余热梯级利用协同脱除SO 3提高除尘效率的系统,其特征是:所述的末级换热器分别与末级换热器冷一次风管道、末级换热器冷二次风管道连接,且末级换热器冷一次风管道、末级换热器冷二次风管道为并联结构。
3.根据权利要求1所述的烟气余热梯级利用协同脱除SO 3提高除尘效率的系统,其特征是:所述的末级换热器冷一次风管道、末级换热器冷二次风管道分别通过空气预热器与锅炉连接。
4.根据权利要求1至3任一项所述的烟气余热梯级利用协同脱除SO 3提高除尘效率的系统,其特征是:所述的末级换热器利用水作为中间介质,且水介质流向与烟道内烟气流向相反,采用逆流布置方式。
5.根据权利要求1所述的烟气余热梯级利用协同脱除SO 3提高除尘效率的系统,其特征是:所述的第五低压加热器与第八低压加热器之间还设有N级低压加热器。
6.根据权利要求1所述的烟气余热梯级利用协同脱除SO 3提高除尘效率的系统,其特征是:所述的一级换热器、二级换热器为串联结构。
7.根据权利要求1所述的烟气余热梯级利用协同脱除SO 3提高除尘效率的系统,其特征是:所述的末级加热器热段采用的材料为FPM、UPVC、NBR、CR、EPDM、CPVC、PP、PE或PVDF。
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