CN202973140U - 一种高效烟气净化和余热利用系统 - Google Patents
一种高效烟气净化和余热利用系统 Download PDFInfo
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- CN202973140U CN202973140U CN2012205661844U CN201220566184U CN202973140U CN 202973140 U CN202973140 U CN 202973140U CN 2012205661844 U CN2012205661844 U CN 2012205661844U CN 201220566184 U CN201220566184 U CN 201220566184U CN 202973140 U CN202973140 U CN 202973140U
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- Prior art keywords
- flue gas
- heat exchanger
- outlet
- entrance
- except
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 239000003546 flue gas Substances 0.000 title claims abstract description 78
- 239000002918 waste heat Substances 0.000 title claims abstract description 21
- 238000000746 purification Methods 0.000 title abstract description 6
- 238000010521 absorption reactions Methods 0.000 claims abstract description 65
- 238000010438 heat treatment Methods 0.000 claims abstract description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound data:image/svg+xml;base64,<?xml version='1.0' encoding='iso-8859-1'?>
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- 238000009833 condensation Methods 0.000 abstract description 4
- 230000005494 condensation Effects 0.000 abstract description 2
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- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Inorganic materials 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- 238000004140 cleaning Methods 0.000 description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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- 239000000126 substance Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000004642 transportation engineering Methods 0.000 description 1
- 238000005429 turbidity Methods 0.000 description 1
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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
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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
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
本实用新型公开了一种燃煤锅炉的高效烟气净化和余热利用系统,包括空气预热器(1)、除SO3器(2)、静电除尘器(3)、湿法脱硫塔(4)和吸收式热泵,吸收式热泵包括发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)和溶液热交换器(9)。在空气预热器(1)和静电除尘器(3)之间布置除SO3器(2),除SO3器(2)热媒出口与吸收式热泵的发生器(5)入口相连,热媒入口与吸收式热泵的发生器(5)出口相连。除SO3器能将烟气温度降低到酸露点以下,促进SO3冷凝和余热回收,下游的静电除尘器可高效脱除SO3和颗粒物,除SO3器回收的余热引入吸收式热泵系统,将余热再利用成高品质热产品和生活热水。该烟气净化和余热利用系统能同时高效脱除SO3、颗粒物,回收烟气废热,在各种煤质和工况条件下均能稳定运行。
Description
一种高效烟气净化和余热利用系统
技术领域
[0001] 本实用新型涉及一种燃煤锅炉高效烟气净化和余热利用系统,能高效脱除烟气中的SO3、烟尘,并有效利用锅炉尾部排烟余热。
背景技术
[0002] 我国是燃煤大国,煤炭消费占一次能源总量70%以上。煤炭燃烧的同时排放大量空气污染物,据统计,燃煤S02、NOx、颗粒物排放量分别占全国总排放量的90%、67%和70%。这些污染物中S02、N0x呈酸性,与颗粒物结合并沉降形成酸雨,2010年我国酸雨面积140万平方公里,占国土面积14%,部分地区出现严重的区域性复合污染。继十一五把燃煤S02作为社会经济发展的约束性指标以来,十二五把S02、NOx作为约束性指标,并将消减目标确定为8%和10% ο
[0003] 在控制燃煤大气污染的措施中,常用静电除尘器除尘、湿式石灰石-石膏法脱硫。图1为常规的燃煤锅炉烟气净化系统,包括空气预热器1、静电除尘器2、烟气换热器(GGH)
3、SO2吸收塔4。烟气离开锅炉后进入空气预热器,部分烟气余热被回收用于加热空气,从空预器出来的烟气温度大概在130-150°C,保证后端静电除尘器不受酸腐蚀,除尘后烟气通过气气换热器(一般为回转式GGH)进入吸收塔脱硫,GGH可以回收原烟气余热,将净烟气加热到80°C以上。
[0004] 这种常规系统在实践中存在几个弊端:
[0005] 首先,静电除尘器利用电晕荷电,使带电粒子在电场中迁移到集尘板,并通过振打清灰被捕集。由于粒子的荷电量主要取决于粒径,粒径在0.15 μ m以下的粒子主要通过扩散荷电,荷电过程缓慢,粒径在0.5 μ m的粒子主要通过电场荷电,粒径在0.15-0.5 μ m之间的粒子,要同时考虑两种荷电作用。因此亚微米粒径的颗粒物荷电量小、迁移速度慢,很容易穿透静电除尘器。另外,静电除尘器效果还受烟尘颗粒的比电阻影响,其工作的最佳比电阻区间为104-5X KTQ/cm,高于5X ΚΓΩ/^πι的颗粒物称为高比电阻烟尘,因为比电阻高,到集尘板上之后放电速度慢,在集尘板上形成一个带电粉尘层,导致粉尘层到集尘板产生电势差,严重时可以击穿粉尘层内空气,产生火花放电(也称反电晕),火花放电改变了静电除尘器的伏安特性曲线,限制其最高工作电压,降低了静电除尘器的除尘效率。由于上述原因,静电除尘器的出口烟尘最多只能降低到100mg/Nm3,即便经过脱硫,烟囱出口处烟尘浓度仍然在30mg/Nm3以上,很难满足日渐严格的环保标准,对高灰份、高比电阻的粉尘,除尘效率更差。
[0006] 其次,煤炭中的硫在燃烧时,绝大部分氧化成SO2,但也有一小部分继续氧化成SO3,如果锅炉尾部加装选择性催化还原NOx装置(简称SCR),催化剂中的活性组分在还原NOx的同时能继续将SO2氧化成SO3,燃煤烟气中S03含量一般在S02的2_3%之间。SO3在温度低于酸露点的时候将冷凝产生硫酸酸露,其酸露点与S03浓度和水含量有关,一般烟气中酸露点在110-150°C之间。硫酸酸露对尾部烟道、吸收塔及其配件产生严重腐蚀,另外,SO3结露形成的酸雾属于亚微米颗粒物, 可以穿过吸收塔排放到大气中,当S03浓度超过3ppm,即可使烟囱处的烟羽呈蓝色,影响浊度,另一方面,含硫酸的烟羽落地后产生酸沉降,对地面植被造成损害并破坏动物和人体的呼吸系统。为了防止酸腐蚀,静电除尘器必须在酸露点之上工作,其后烟道和吸收塔必须使用昂贵的防腐材料,增加了整个系统的投资和运行成本。
[0007] 最后,回转式GGH的漏风率一般在1%左右,即使少量原烟气泄露进入烟囱也会造成环保不达标,而且GGH在运行中普遍存在堵塞、腐蚀等问题,需要经常停机清洗,由于环保部门要求脱硫与主机同时起停,这就意味着锅炉主机也要同时停运,从而造成较大的经济损失。
[0008] 针对以上问题,本实用新型专利提供一套高效的烟气净化和余热利用系统,具有先进的自动调节系统,能够
[0009] I)实现高效脱除SO3和烟尘
[0010] 2 )在各种煤质条件稳定运行
[0011] 3)提供更灵活的余热利用方案
发明内容
[0012] 本实用新型所要解决的问题是,提高传统静电除尘器的除尘效率,高效脱除烟气中的三氧化硫,并提供余热回收利用方案,达到节能减排的双重作用。本实用新型的实质,是在静电除尘器之前加设除S03器,该除S03器一方面降低烟气温度,提高静电除尘器的除尘效率,另一方面,通过冷凝吸附高效脱除烟气中的S03,同时可以将烟气中回收的余热进行综合利用。为实现上述目的,图2提供了本实用新型的第一烟气处理工艺,该烟气净化和余热利用系统包括空气预热器(I)、除SO3器(2)、静电除尘器(3)、湿法脱硫塔(4)、吸收式热泵,吸收式热泵包含发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)、溶液热交换器(9)。除S03器布置在空气预热器和静电除尘器之间,能高效脱除烟气中的S03 ;除S03器热媒入口与吸收式热泵发生器的管程出口相连,热媒出口与吸收式热泵发生器的管程入口相连。进一步地,除S03器热媒水的出、入口安装调节阀和旁路阀,用于调节热媒水流入除S03器的流量。进一步地,除S03器内部安装吹灰器,根据除S03器出入口压差和入口灰浓度,调节吹灰频率和时间。进一步地,从烟气回收的余热引入第二类吸收式热泵,利用回收余热做驱动热源,溴化锂做吸收剂,水做制冷剂,制取高品质热产品,同时输出生活热水。
[0013] 该系统具有如下特点:在烟气净化方面,将除SO3器放在静电除尘器之前,使烟气温度降低到90-100°C,由于烟尘比电阻对温度敏感,降温后比电阻降低,而且温度降低处理烟气体积缩小、流速降低,飞灰颗粒的表观迁移速度提高,除尘性能得到改善,颗粒物浓度离开静电除尘器时可低于50mg/Nm3,经吸收塔脱硫后可低于20mg/Nm3 ;其次,烟气温度低于酸露点,SO3将优先冷凝在烟尘颗粒表面,并随烟尘一起在静电除尘器中脱除,除SO3效率可达到95%以上;另外,管式换热器替代回转式换热器,管内流动热媒水,有效解决了因回转式GGH泄露造成的排放不达标问题;最后,由于电除尘器性能提高,三电场静电除尘器可具有五电场的除尘效果,节省了投资和运行费用,同时吸收塔入口烟气温度降低减少了吸收塔的蒸发水量,具有减少投资、消减排放、节能降耗等多重优势。
[0014] 在系统稳定性方面,除SO3器热媒水出口和入口调节阀,以及除S03器内部的吹灰器,可以保证不同煤质和工况条件下烟气净化和余热利用系统都能稳定运行。当锅炉负荷降低,排烟温度下降,为了保证除SO3器出口烟气温度稳定,可减少热媒水入口流量;当锅炉排烟温度过高,为保证除SO3器出口烟气温度稳定,可打开入口调节阀,补充冷媒;当燃烧高灰煤,可根据入口灰浓度调整吹灰器频次和吹灰时间。
[0015] 在余热利用方面,充分利用锅炉的中、低温余热资源,使用吸收式热泵系统的发生器、冷凝器、蒸发器、吸收器和溶液热交换器,从废烟气中制取高品质热产品和生活热水。该系统用锅炉烟气从150°C到90°C的热量做驱动热源,用溴化锂溶液做吸收剂,水做冷剂,在热泵系统内产生吸收液循环和冷剂循环,将驱动热源的热量转移产生高品质热产品和生活用水。由于溴化锂沸点为1265°C,水的沸点为100°C,溴化锂稀溶液被加热时,稀溶液将沸腾并释放大量水分变为浓溶液,所产生的水蒸气冷剂依次在冷凝器中放热,在蒸发器中吸热,最后流入吸收器,被发生器来的溴化锂浓溶液吸收产生稀溶液,再次返回发生器。通过溶液循环和冷剂循环,即可将烟气中的中、低温余热转变成高品质的高温热产品和中温生活用热水。
[0016] 图3提供了本实用新型的第二烟气处理工艺,工艺实质与第一烟气处理工艺相似,但回收的烟气余热引入吸收式热泵,以及冷凝器和干燥机组成的干燥系统,干燥脱硫石膏。该高效烟气净化和余热利用系统包括空气预热器(I)、除303器(2)、静电除尘器(3)、湿法脱硫塔(4)、干燥机(10)和吸收式热泵,吸收式热泵包含发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)、溶液热交换器(9)。除SO3器置于空气预热器和静电除尘器之间,能高效脱除烟气中的S03。进一步地,除S03器回收的余热作驱动热源,溴化锂做吸收剂,水做冷剂,产生过的高温水在冷凝器和干燥机中循环,干燥脱硫副产物,同时吸收器中产生生活热水。
[0017] 图4提供了本实用新型的第三烟气处理工艺,工艺实质与第一烟气处理工艺相似,但回收的余热引入后端的S02吸收解吸工艺,用于加热富SO2的胺溶液,促进SO2的解吸。该高效烟气净化和余热利用系统由空气预热器(I)、除303器(2)、静电除尘器(3)、SO2吸收塔(4)、SO2解吸塔(5)、余热换热器(6)、热交换器(7)、SO2浓缩室(8)组成。除SO3器置于空气预热器和静电除尘器之间,能高效脱除烟气中S03。S02吸收塔中吸收了 S02的富胺溶液通过热交换器7进入S02解吸塔,解吸后的贫胺溶液一部分流入余热换热器6,与除S03器回收的烟气余热进行换热,然后返回S02解吸塔,另一部分经热交换器7返回S02吸收塔,循环利用。
[0018] 图5提供了本实用新型的第四烟气处理工艺,工艺实质与第一烟气处理工艺相似,但回收的热量引入后端的烟气脱CO2工艺,用于加热富CO2的胺液,促进CO2的解吸。该高效烟气净化和余热利用系统由空气预热器(I)、除SO3器(2)、静电除尘器(3)、烟气脱硫装置(4 )、CO2吸收塔(5 )、CO2解吸塔(6 )、余热换热器(7 )、热交换器(8 )、CO2浓缩室(9 )组成。除SO3器置于空气预热器和静电除尘器之间,烟气经除S03器降温脱S03后,依次进入静电除尘器和烟气脱硫装置,除尘脱硫后烟气进入C02吸收塔脱C02后排放。吸收了 C02的富胺溶液,通过热交换器7进入C02解吸塔,解吸后的贫胺溶液一部分流入余热换热器7,与除S03器回收的烟气余热进行换热,然后返回C02解吸塔,另一部分经热交换器8返回C02吸收塔,循环利用。
[0019] 附图说明
[0020] 附图1为常规的烟气净化系统示意图
[0021] 附图2为第一处理工艺的烟气净化和余热利用系统示意图[0022] 附图3为第二处理工艺的烟气净化和余热利用系统示意图
[0023] 附图4为第三处理工艺的烟气净化和余热利用系统示意图
[0024] 附图5为第四处理工艺的烟气净化和余热利用系统示意图
[0025] 具体实施方式
[0026] 下面将参照附图描述本实用新型发明的具体实施例。
[0027] 第一实施例:
[0028] 本实用新型专利的第一实施例如图2所示,烟气离开燃煤锅炉,先进入空气预热器(1),降温到130-150°C之后进入除303器(2),在除SO3器内部,烟气温度继续降低到90-100°C,烟气中的SO3冷凝,其后的静电除尘器(3)不但高效收尘,还能将冷凝在烟尘颗粒表面的SO3除掉,烟气经湿法脱硫塔(4)后从烟囱排放。除SO3器的热媒入口与吸收式热泵的发生器(5)管程出口相连,热媒出口与吸收式热泵的发生器(5)管程入口相连,与常规系统图1的不同在于将除SO3器放在空气预热器与静电除尘器之间,且除SO3器安装出、入口和旁路调节阀、吹灰器,且除SO3器回收的热量用于供热,除SO3器出、入口须至少安装烟气温度传感器和压力传感器。
[0029] 前述的除SO3器可用水做热媒。由于空气预热器来的烟气含尘量大,烟尘颗粒粒径在20〜30 μ m左右,其总比表面积远远大于烟道和换热器表面积,当烟气温度降低到酸露点,烟气中SO3将优先冷凝在具有较大比表面积的烟尘颗粒表面,有效避免了除SO3器内部硫酸腐蚀问题。
[0030] 前述的出、入口和旁路调节阀,应根据除SO3器入口温度传感器的烟温调节阀门开度,保证出口烟气温度不高于设定的最高温度。前述的吹灰器,应根据除SO3器出、入口差压数据调整吹灰频度和持续时间。
[0031] 前述的吸收式热泵,从除SO3器回收的热量引入发生器,溴化锂稀溶液受热后沸腾,不断蒸发浓缩成为浓溶液并产生高温水蒸汽,浓溶液经溶液热交换器进入吸收器,水蒸气经冷凝器放热、蒸发器吸热后也进入吸收器,被溴化锂浓溶液吸收产生稀溶液,再次返回发生器,在吸收器和发生器之间装有溶液热交换器,实现浓溶液和稀溶液之间的换热。前述的吸收式热泵,生活水进入吸收器管程,吸热增温后返回供生活热水管路;供热回水进入冷凝器管程,放热降温后返回供热管路;冷却水进入蒸发器入口管程,冷却后离开蒸发器出口管程。为保持设备的真空度,前述的吸收式热泵使用前需进行气密性检查,为防止腐蚀,需控制溴化锂浓度变化不超过其结晶浓度。
[0032] 第二实施例:
[0033] 下面结合图3说明本发明的第二实施例。除SO3器(2)热媒入口与吸收式热泵的发生器(5)管程出口相连,热媒出口与发生器(5)的管程入口相连,干燥机(10)入口与冷凝器(6)管程出口相连,干燥机(10)出口与冷凝器(6)管程入口相连;冷却水入口与蒸发器管程入口相连,冷却水出口与蒸发器管程出口相连;生活水与吸收器管程入口相连,加热后离开吸收器管程出口,用于供生活热水。脱硫石膏副产物进入干燥机,从冷凝器来的高温热水烘干石膏,携带水份的湿空气从干燥机排出,热水降温后返回冷凝器。
[0034] 本实施例与第一实施例的相似之处在于都将除SO3器置于空气预热器和静电除尘器之间,都能将烟气从130-150°C降温到90-100°C,回收的余热都用来制取生活热水,都在除SO3器安装出入口和旁路调节阀、吹灰器等保证系统稳定运行。但是本实施例的特点是将冷凝器和干燥机相连,用于干燥脱硫副产物。
[0035] 与第一实施例相同,除S03器热媒可选用水。由于烟气中S03在温度低于酸露点时将优先冷凝在比表面积大的烟尘颗粒表面上,有效避免了除S03器内部酸腐蚀问题。
[0036] 本实施例能干燥脱硫石膏,减少石膏排放量,方便石膏运输和石膏产品的生产。因为即能回收废热产生生活热水,又能深加工石膏产品,具有显著的节能效果。
[0037] 第三实施例:
[0038] 下面结合图4说明本发明的第三实施例。除SO3器热媒入口与余热换热器(6)管程出口相连,热媒出口与余热换热器(6)管程入口相连;静电除尘器(3)烟气出口与S02吸收塔(4)烟气入口相连,S02吸收塔(4)烟气出口接烟囱入口 ;S02吸收塔(4)胺液出口与S02解吸塔(5)胺液入口相连,S02解吸塔(5)胺液出口 一部分与余热交换器(6)壳程相连,一部分与S02吸收塔(4)胺液入口相连,余热换热器(6)壳程出口与S02解吸塔(5)相连。
[0039] 烟气经空气预热器(I)降温、除303器(2)回收废热、静电除尘器(3)除SO3、除尘之后,进入SO2吸收塔(4),S02被其中的胺溶液吸收,干净烟气排至烟囱,富SO2的胺溶液经过热交换器(7)后进入SO2解吸塔(5),在高温下SO2解吸并从塔顶排出至SO2浓缩室(8),贫胺溶液从SO2解吸塔(5)塔底排出,一部分经由余热换热器(6)返回SO2解吸塔(5),从除SO3器回收的热量在此处用于加热胺液,促进SO2的解吸,另一部分贫胺溶液经过热交换器
(7)返回SO2吸收塔(4),形成封闭循环。
[0040] 本实施例与第一实施例的相同之处在于都将除SO3器置于空气预热器和静电除尘器之间,都能将烟气温度从130-150°C降低到90-100°C,且都在除SO3器安装调节阀、吹灰器等保证系统稳定运行。但本实施例将回收的废热引入烟气制硫酸工艺,用于加热胺液,促进SO2的解吸。
[0041] 前述的余热换热器6也可以置于S02解吸塔内,直接加热从解吸塔上部喷淋下来的富S02胺溶液。
[0042] 前述的除S03器热媒可选用水。采取与第一实施例相同的技术手段保证除S03器内部不发生酸腐蚀问题。
[0043] 本实施例可实现烟气废热再利用,并节省烟气脱硫制硫酸工艺所需要的大量蒸汽。
[0044] 第四实施例:
[0045] 下面结合图5说明本发明的第四实施例。本实施例中,除SO3器(2)热媒入口与余热交换器(7 )管程出口相连,除S03器(2 )热媒出口与余热交换器(7 )管程入口相连;湿法脱硫塔(4)烟气入口与静电除尘器(3 )出口相连,烟气出口与CO2吸收塔(5 )烟气入口相连,CO2吸收塔(5)烟气出口与烟囱入口相连;C02吸收塔(5)胺液出口与CO2解吸塔(6)胺液入口相连,CO2解吸塔(6 )胺液出口 一部份与余热换热器(7 )壳程入口相连,一部份与CO2吸收塔(5)胺液入口相连,余热换热器(7)壳程出口与CO2解吸塔(6)相连。
[0046] 烟气经空气预热器(I)降温、除SO3器(2)回收余热、静电除尘器(3)除尘、湿法脱硫塔(4)脱硫之后,进入CO2吸收塔(5),烟气中的CO2被胺溶液吸收,脱碳后烟气排入烟囱。富CO2的胺溶液经过热交换器(8)后进入CO2解吸塔(6),在高温下CO2解吸并从塔顶排出至CO2浓缩室(9),贫胺溶液从塔底排出,一部分经由余热换热器(7)返回CO2解吸塔(6),从除SO3器回收的热量在此处用于加热胺液,促进CO2的解吸,另一部分贫胺溶液经过热交换器(8)返回CO2吸收塔(5),形成封闭循环。
[0047] 本实施例与第一实施例相似之处在于,都将除SO3器置于空气预热器和静电除尘器之间,都能将烟气温度从130-150°C降低到90-100°C,且都在除SO3器安装调节阀和吹灰器等保证系统稳定运行。但本实施例将除SO3器回收的废热引入烟气脱CO2工艺,用于促进胺液解吸CO2。
[0048] 前述的余热加热器也可置于CO2解吸塔内,用除SO3器回收的余热直接加热从解吸塔上部喷淋下来的富CO2胺溶液。
[0049] 前述的除303器热媒可选用水,实用与第一实施例相同的技术手段防止除503器内部的酸腐蚀问题。
[0050] 本实施例可实现烟气废热再利用,并节省烟气脱碳工艺所需大量蒸汽。
[0051] 应注意的是,本文所公开的实施例仅描述了本发明的优选实施例,但决不以任何方式限制本实用新型专利的范围。本领域技术人员能够从上文的指导内容,在不脱离本实用新型专利的范围和实质的情况下,根据实际需要对本实用新型专利所公开的各实施例进行的各种组合和变形,均在本实用新型专利的保护范围内。
Claims (9)
1.一种高效烟气净化和余热利用系统,包括空气预热器(I)、除S03器(2)、静电除尘器(3)、湿法脱硫塔(4)和吸收式热泵,吸收式热泵包含发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)和溶液热交换器(9),该系统特征在于:除S03器布置在空气预热器和静电除尘器之间,能高效脱除烟气中S03 ;除S03器热媒入口与吸收式热泵的发生器的管程出口相连,热媒出口与吸收式热泵的发生器管程入口相连。
2.根据权利要求1所述的高效烟气净化和余热利用系统,其特征是:在除S03器(2)热媒水的出、入口安装调节阀。
3.根据权利要求1所述的高效烟气净化和余热利用系统,其特征是:在除S03器(2)内部安装吹灰器,可调节吹灰频率和持续时间。
4.如权利要求1所述的高效烟气净化和余热利用系统,其特征是:吸收式热泵包含发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)和溶液热交换器(9),利用除S03器(2)回收余热做驱动热源,溴化锂做吸收剂,水做冷剂,制取高品质热产品,同时输出生活热水。
5.一种高效烟气净化和余热利用系统,包括空气预热器(I)、除S03器(2)、静电除尘器(3)、湿法脱硫塔(4)、干燥机(10)和吸收式热泵,吸收式热泵包含发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)和溶液热交换器(9),该系统特征在于:除S03器置于空气预热器和静电除尘器之间,能高效脱除烟气中的S03 ;除503器热媒入口与吸收式热泵的发生器管程出口相连,热媒出口与发生器的管程入口相连。
6.根据权利要求5所述的高效烟气净化和余热利用系统,其特征是:吸收式热泵包含发生器(5)、冷凝器(6)、蒸发器(7)、吸收器(8)和溶液热交换器(9),用除S03器(2)回收的余热作驱动热源,溴化锂做吸收剂,水做冷剂,高温水在冷凝器和干燥机中循环,干燥脱硫副产物,吸收器中产生生活热水。
7.一种高效烟气净化和余热利用系统,包括空气预热器(I)、除S03器(2)、静电除尘器(3 )、S02吸收塔(4 )、 S02解吸塔(5 )、余热换热器(6 ),热交换器(7 )、S02浓缩室(8 ),其特征在于: 1)除S03器置于空气预热器和静电除尘器之间,能高效脱除烟气中S03 ; 2)除S03器热媒入口与余热换热器管程出口相连,热媒出口与余热换热器管程入口相连; 3)静电除尘器出口与S02吸收塔烟气入口相连,S02吸收塔烟气出口接烟囱入口 ; 4) S02吸收塔胺液出口经热交换器(7)与S02解吸塔胺液入口相连,S02解吸塔胺液出口一部份与余热交换器壳程入口相连,一部份经热交换器(7)与S02吸收塔胺液入口相连,余热换热器壳程出口与S02解吸塔相连。
8.一种高效烟气净化和余热利用系统,包括空气预热器(I)、除S03器(2)、静电除尘器(3 )、烟气脱硫装置(4 )、C02吸收塔(5 )、C02解吸塔(6 )、余热换热器(7 )、热交换器(8 )、C02浓缩室(9)组成,其特征在于: 1)除S03器置于空气预热器和静电除尘器之间,能高效脱除烟气中S03 ; 2)除S03器热媒入口与余热交换器管程出口相连,除S03器热媒出口与余热交换器管程入口相连; 3)烟气脱硫装置入口与静电除尘器出口相连,出口与C02吸收塔烟气入口相连,C02吸收塔烟气出口与烟囱入口相连;
9.C02吸收塔胺液出口经热交换器(8)与C02解吸塔胺液入口相连,C02解吸塔胺液出口一部份与余热换热器壳程入口相连,一部份经热交换器(8)与C02吸收塔胺液入口相连,余热换热器壳程出口与C02解吸 塔相连。
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