CN103212284A - 一种联合脱除烟气中的氮氧化物和硫化物的方法及装置 - Google Patents
一种联合脱除烟气中的氮氧化物和硫化物的方法及装置 Download PDFInfo
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- CN103212284A CN103212284A CN2013100846608A CN201310084660A CN103212284A CN 103212284 A CN103212284 A CN 103212284A CN 2013100846608 A CN2013100846608 A CN 2013100846608A CN 201310084660 A CN201310084660 A CN 201310084660A CN 103212284 A CN103212284 A CN 103212284A
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- CN
- China
- Prior art keywords
- flue gas
- desulfurizing tower
- ammonia
- boiler
- ammoniacal liquor
- Prior art date
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- 239000003546 flue gas Substances 0.000 title claims abstract description 92
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 90
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Inorganic materials 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O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title abstract description 49
- 150000003568 thioethers Chemical class 0.000 title 1
- 230000003009 desulfurizing Effects 0.000 claims abstract description 73
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 44
- 238000006477 desulfuration reactions Methods 0.000 claims abstract description 35
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 [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 19
- 229910052813 nitrogen oxides Inorganic materials 0.000 claims abstract description 19
- 239000003245 coal Substances 0.000 claims abstract description 18
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound 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[NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000002485 combustion reactions Methods 0.000 claims abstract description 11
- QXTCFDCJXWLNAP-UHFFFAOYSA-N Mononitrogen monosulfide Chemical compound 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S=[N] QXTCFDCJXWLNAP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000007599 discharging Methods 0.000 claims abstract description 6
- 229910001874 nitric oxide Inorganic materials 0.000 claims abstract 4
- 239000007921 sprays Substances 0.000 claims description 41
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound 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N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 14
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 14
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 14
- 239000007788 liquids Substances 0.000 claims description 13
- 238000000034 methods Methods 0.000 claims description 13
- 238000010521 absorption reactions Methods 0.000 claims description 8
- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reactions Methods 0.000 claims description 8
- 239000007787 solids Substances 0.000 claims description 7
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous Oxide Chemical compound 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[O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- LSNNMFCWUKXFEE-UHFFFAOYSA-M bisulfite Chemical compound 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OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 claims description 4
- 238000002425 crystallisation Methods 0.000 claims description 4
- 239000000047 products Substances 0.000 claims description 4
- 238000007664 blowing Methods 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 238000002309 gasification Methods 0.000 claims description 2
- 230000001105 regulatory Effects 0.000 claims description 2
- 239000011901 water Substances 0.000 claims 7
- 239000003570 air Substances 0.000 claims 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- 239000007789 gases Substances 0.000 abstract description 8
- 238000010531 catalytic reduction reactions Methods 0.000 abstract description 4
- 238000005507 spraying Methods 0.000 abstract description 3
- 238000002347 injection Methods 0.000 abstract 1
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- 238000005516 engineering process Methods 0.000 description 12
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- 235000019738 Limestone Nutrition 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 206010022114 Injury Diseases 0.000 description 1
- NMCUIPGRVMDVDB-UHFFFAOYSA-L Iron(II) chloride Chemical compound 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Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 description 1
- 241000143392 Oar Species 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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Abstract
本发明涉及一种联合脱除烟气中氮氧化物和硫化物的方法,其特征在于:在反应锅炉的炉膛内喷入经气化后的氨水,利用选择性非催化还原法使烟气中的NOX还原为N2,然后烟气进入脱硫塔中,烟气中SO2被加入脱硫塔的氨水吸收,净化后的烟气经烟囱排空。本发明还涉及一种联合脱除烟气中氮氧化物和硫化物的设备,该设备包括(A)用于燃烧煤的燃烧锅炉,锅炉炉膛内设置1个以上的氨水喷射点,(B)脱硫塔,(C)排空装置。
Description
一种联合脱除烟气中的氮氧化物和硫化物的方法及装置
技术领域
[0001] 本发明涉及一种烟气净化技术。特别是涉及一种对工业燃煤燃烧后产生的包含硫化物和氮氧化物(NOx)等成分的烟气的联合脱硫脱硝的净化方法及净化装置。
背景技术
[0002] 二氧化硫(SO2)、硫化氢(H2S)和氮氧化物(NOx)是目前大气污染物中含量较大、影响面较广的气态污染物。它们主要来源于工业燃料煤的燃烧过程,在火力发电厂、金属冶炼厂、炉窑等大型生产企业中会产生大量包含硫化物、氮氧化物在内的废气(俗称烟气)。二氧化硫和氮氧化物形成的硫酸雾、化学烟雾以及酸雨会给生态环境和人类生产生活带来了严重的危害。我国近年来日益恶化空气质量引起社会的普遍关注。据国家环保部最新统计数据显示,2010年我国二氧化硫排放2185万吨,氮氧化物排放量2251万吨。基于我国以煤为主的能源结构目前难以进行根本性改变的现状,我国工业生产中二氧化硫和氮氧化物的排放还会持续增加,环境保护的形势十分严峻,若不尽快推广新型的净化技术来有效控制硫化物和氮氧化物的排放,将直接影响我国大气环境质量和能源行业的可持续发展。随着环保新政策的出台及大气污染物排放标准的修订,二氧化硫和氮氧化物的排放控制将更为严格。
[0003]目前煤化厂、燃煤电厂对烟气脱硫普遍采用石灰石-石膏法,该法具有脱硫效率高、运行可靠、吸收剂利用率高的特点,但该工艺对石灰石需求量大,存在资源消耗大、用水量大、废水二次污染的问题。海水法烟气脱硫利用海水的天然碱度来脱除烟气中的302,该法不产生废物,技术成熟、工艺简单,但受地域条件限制,只能适用于沿海地区工厂。干法脱硫包括炉内喷钙法,该法投资省、占地小、无污水和废酸排出、设备腐蚀小,但该法存在的问题是脱硫效率低、脱硫反应速率较慢,长时间使用需要更新除尘系统。对于煤化厂的焦炉煤气一般采用使用氧化还原催化剂的湿式氧化法,其脱硫效率高且能将硫化氢转化为硫磺,但该法存在碱液消耗大和高浓度还原性废液需要处理的缺点。氨法脱硫是采用氨水做吸收剂除去烟气中的SO2等污染物的烟气净化技术,具有吸收效率高、反应速率快的优点,但是由于氨的价格比石灰石等吸收剂高很多,因此高运行成本是阻碍氨法脱硫工艺获得广泛应用的最大因素。
[0004]目前为了脱除大排量连续型的烟气中的氮氧化物(N0X),一般采用选择性催化还原脱硝技术(Selective Catalytic Reduction, SCR)和选择性非催化还原脱硝技术(Selective Non-Catalytic Reduction, SNCR)。前者具有脱硝效率高、二次污染小的优点,但是存在设备投资大、运行成本高和技术难度大等的问题,尤其安装余热锅炉的系统时易造成余热浪费。后者不用催化剂,设备运行费用也少,但是存在脱硝效率较低、NH3使用量大的问题,难以保证反应温度和停留时间,且由于NH3逃逸容易造成二次污染。
[0005] 由于人们对各种污染物危害程度的认识程度是不断发展的,环保意识是不断提高的,各种环保法规也是逐步出台,造成了目前各种污染治理技术的孤立性,相互之间独立进行,缺乏系统性的整合,往往是为了应对新的环保法规而在原有的设备基础上再另行增加新的净化设备,实际上造成资源和成本上的浪费。此外还存在能耗高、污染治理不彻底的问题。本发明针对以上情况,以全新的角度和系统性的理念,对烟道气中硫化物和氮氧化物进行联合脱除的治理,在治理过程中能量和物料得到最优化的利用。尤其适用于电力、化工、冶金、有色、建材玻璃等大气污染严重的行业。
[0006] 针对以上脱硫脱硝技术中存在的问题,目前很多研究的方向是通过改善脱硫塔结构来提高脱硫效率,如申请号为200820077614.X的发明采用了在脱硫塔体内由上至下设置若干层叶轮状塔盘等结构,但其仍然没能根本上解决设备复杂、投资大的问题。申请号为200710052131.4的发明通过改进烟气进气的方式,使烟气在吸收塔内形成均匀向上的对冲湍流从而烟气与吸收液充分接触来提高脱硫效率,但该方法存在塔内压降增加从而导致鼓风机电耗增加、能耗大的问题。申请号为201010606917.8的发明通过采用低温SCR催化剂移动床的方式脱除烟气中氮氧化物,但低温SCR催化剂由于抗硫抗水性差,目前还处于研发阶段,短期内很难实用化。对于系统性联合脱除氮氧化物和硫化物的技术目前鲜有报道。
[0007] 参考文献:
[0008] 专利文献1:申请号为200820077614.X的中国实用新型专利
[0009] 专利文献2:申请号为20071005213L4的中国发明专利
[0010] 专利文献3:申请号为201010606917.8的中国发明专利
发明内容
[0011] 发明要解决的问题
[0012] 针对上述现有烟气脱硫脱硝方法存在的问题,本发明提供一种对工业燃煤燃烧后产生的包含硫化物和氮氧化物(NOx)等成分的烟气的联合脱硫脱硝的净化方法及净化装置。该净化方法能充分利用现 有工厂(特别是燃煤电厂)已有的脱硫脱硝设备,不额外增加新的净化设备,在燃烧炉内进行选择性非催化还原法脱硝后,烟气再导入脱硫塔脱硫,通过整体性的设计,保证烟气中硫化物和氮氧化物的良好脱除的同时,充分利用物料和能源(进料的氨水计量比控制,烟气的余热用换热器收集并利用),且脱硫塔收集的氨形成硫酸铵固体,供化肥用,既保证资源的充分利用还能避免二次污染。
[0013] 用于解决问题的方案
[0014] 为达以上目的,本发明采用了以下的技术方案:
[0015] (I)一种联合脱除烟气中氮氧化物和硫化物的方法,其特征在于:在反应锅炉的炉膛内喷入经气化后的氨水,利用选择性非催化还原法使烟气中的NOx还原为N2,然后烟气进入脱硫塔中,烟气中SO2被加入脱硫塔内的氨水吸收,净化后的烟气经烟囱排空。
[0016] (2)根据上述(I)所述的方法,其中,氨水经气化后由一个以上喷射点喷入锅炉炉膛,各氨水喷射点分别置于炉膛燃烧器下方低温区域、燃烧器上方高温区域及炉内出口烟道区域中的一处以上。
[0017] (3)根据上述(I)所述的方法,其中,所述锅炉中氨水喷射点区域内的反应温度为700 〜1200。。。
[0018] (4)根据上述(I)所述的方法,其中,所述锅炉中氨水的喷入量以ΝΗ3/Ν0χ的摩尔比计为I〜5。
[0019] (5)根据上述(4)所述的方法,其中,设置ΝΗ3/Ν0χ的摩尔比大于I时,使脱硝过程中未反应的NH3随烟气进入到脱硫塔,在脱硫塔内经除雾器和水洗塔回收作为脱硫剂来用于吸收SO2。
[0020] (6)根据上述(I)所述的方法,其中,将氨气与水以一定比例混合制成反应所需浓度的氨水,浓度控制在3%〜10%的范围内,再由喷氨泵打入脱硫塔底部进行雾化吸收。
[0021] (7)根据上述(6)所述的方法,其中,脱硫塔内氨水喷淋压力在0.8〜1.6MPa之间,满足喷头雾化要求。
[0022] (8)根据上述(6)所述的方法,其中,脱硫塔底吹入压缩空气进行氧化,使塔底混合液中的亚硫酸铵氧化形成硫酸铵,并进行蒸发结晶和固液分离制成硫酸铵产品。
[0023] (9)根据上述(6)所述的方法,其中,脱硫塔顶部安装水洗系统用于洗涤烟气中夹带的NH3,水洗系统顶部装有除雾器以回收烟气中的NH3。
[0024] (10)根据上述(I)所述的方法,其中,脱硝后烟气与脱硫后烟气经烟气换热器换热,前者降低烟气进入脱硫塔时的温度,后者利用前者换热的能量提高烟气排出脱硫塔时的温度。
[0025] (11) 一种联合脱除烟气中氮氧化物和硫化物的设备,其特征在于该设备包括下列部件:
[0026] (A)用于燃烧煤的燃烧锅炉,锅炉炉膛内设置I个以上氨水的喷射点,各氨水喷射点分别置于炉膛燃烧器下方低温区域、燃烧器上方高温区域及炉内出口烟道区域中的一处以上,
[0027] (B)脱硫塔,具有水洗氨气的水洗装置和二氧化硫吸收装置,
[0028] (C)排空装置。
[0029] (12)根据上述(11)的设备,其中燃烧锅炉包括控温装置,其控制氨水喷射点区域内的反应温度为700〜1200°C。
[0030] (13)根据上述(11)的设备,其中氨水喷射装置能以ΝΗ3/Ν0χ的摩尔比计为I〜5进行氨水喷射。
[0031] (14)根据上述(11)的设备,其中脱硫塔包括向其内部喷入氨水的喷氨泵,其将浓度控制在3%〜10%范围、压力控制在0.8〜1.6MPa范围的氨水喷入脱硫塔进行雾化吸收。
[0032] (15)根据上述(11)的设备,其中脱硫塔包括从底部吹入压缩空气的装置,压缩空气使塔底混合液中的亚硫酸铵氧化形成硫酸铵,接着供入到蒸发装置蒸发结晶和分离装置固液分离制成硫酸铵产品。
[0033] (16)根据上述(11)的设备,其中脱硫塔中的水洗系统用于洗涤烟气夹带的见13,水洗系统顶部装有除雾器以回收烟气中的NH3。
[0034] (17)根据上述(11)的设备,其中还包括一个或多个烟气换热器,其可对通入燃烧锅炉的燃烧空气和脱硝后的烟气进行换热,或者对脱硝后的烟气和脱硫后的烟气进行换热。
[0035] 发明的效果
[0036] 1.可以整合现有的生产设备进行联合烟气脱硝脱硫处理,无需增加新的净化装置和净化流程,也无需对目前煤化厂、燃煤电厂等的设备进行整体的更新换代,充分利用了现有的燃烧锅炉和脱硫塔,彻底摆脱了根据不同时间出台环保法规对净化设备进行打补丁式地升级改造的工业设计;[0037] 2.利用燃烧锅炉进行SNCR法脱硝,利用了燃烧锅炉在烧煤过程中产生的热量,并对氨水喷射点区域的反应温度进行控制,该控制可以利用煤本身的燃烧效率和空气进料比进行有效的准确的控制,能保证反应的温度,同时通过在烟气行程上不同的位置设置一个或多个氨水喷射点,保证了烟气有充分时间与氨气接触,脱硝效率相比普通SNCR法脱硝而言得到提高,可达到80%以上。并且该方法无NH3逃逸,避免了 NH3使用过量造成的二次污染,保证环保排放要求;
[0038] 3.采用氨水吸收这种气液法吸收SO2,反应速率快、反应完全、吸收剂利用率高;同时可以回收利用脱硝过程中未反应的NH3 ;
[0039] 4.利用燃烧锅炉这一必要设备进行脱硝处理,不增加另外的脱硝装置,先进行脱硝处理后多余的NH3可直接供入到脱硫装置中得到利用,如此设计使得系统整体的运行费用得到极大降低;
[0040] 5.利用氨水吸收SO2再经氧化得到的脱硫副产品硫酸铵可作为农用肥料,由此避免了 NH3直接排放到空气中或另行增加设备处理过量的NH3,并且物料均得到了充分利用,于环境保护于成本控制都十分有利。
附图说明
[0041] 图1是本发明一个实施形态的联合脱硫脱硝工艺流程示意图。
[0042] 图1中,NI〜N5表示包含氨的气体/液体的走向,Al〜A3、A11、A12是表示导入空气的走向,A4〜10是表示烟气的走向,Wl、W2表示水的引入。
[0043] 图2是表示本发明中NOx脱除效率与ΝΗ3/Ν0χ的摩尔比关系的图。
具体实施方式
[0044] 以下将参考附图详细说明本发明的各种示例性实施例、特征和方面。附图中相同的附图标记表示功能相同或相似的元件。尽管在附图中示出了实施例的各种方面,但是除非特别指出,不必按比例绘制附图。
[0045] 在这里专用的词“示例性”意为“用作例子、实施例或说明性”。这里作为“示例性”所说明的任何实施例不必解释为优于或好于其它实施例。
[0046] 另外,为了更好的说明本发明,在下文的具体实施方式中给出了众多的具体细节。本领域技术人员应当理解,没有这些具体细节,本发明的方案同样可以实施。在另外一些实例中,对于大家熟知的方法、手段和结构未作详细描述,以便于凸显本发明的主旨。
[0047] 本发明的一个具体实施形态中,燃煤电厂已有的设备为燃煤锅炉、脱硫塔、烟囱。燃煤锅炉中导入空气使煤充分燃烧产生热能,即为通常的燃煤电厂的锅炉结构。
[0048] 在燃烧锅炉的炉膛中设置多个氨水喷射点。在煤燃烧发电的同时,将氨水贮槽NI中贮存的氨水经气化后导入压缩泵,再经由喷射点1,2,3,4,5喷入炉膛中。以炉膛为反应器,使氨气在700〜1200°C温度区间,迅速与烟气中的NO5^P O2发生反应,生成氮气和水。由于该反应可在发电的同时进行,因此本发明的净化方法不必单独引起新的NOx净化装置和净化流程,整个净化过程与原有的工业流程有机地整合在一起,有利于能耗和成本的降低,特别适合于旧电厂净化设备的。该过程的反应式为:
[0049] 4N0+4NH3+02 — 4N2+6H20[0050] 2N02+4NH3+02 — 3N2+6H20
[0051] 在氧气不足的情况下,同样能够发生下面的反应:
[0052] N02+N0+2NH3 — 2N2+3H20
[0053] 对于典型燃煤烟气中包含的N0X,NO占95%,NO2占5%,当NH3与NO的摩尔比接近1:1时,理论上NOx的脱除率可以达到90%。但是在实际应用中,反应温度、在最佳温度区域的停留时间、还原剂和烟气的混合程度都会影响脱硝的效率。由于未反应的氨随着烟气排放到大气导致NH3排放超标,会引起二次污染,一般要求氨的逃逸量不超过5 X 10_6或更低。实际应用中,考虑到NH3耗和NH3逃逸,一般ΝΗ3/Ν0χ的摩尔比低于1.05,SNCR设计效率仅为 30% 〜50%ο
[0054] 本发明工艺的特点在于通过提高NH3喷入量以提高ΝΗ3/Ν0χ摩尔比,从而强化上述NOx的还原反应向右进行,而多余的氨逃逸在后端脱硫吸收塔中回收,从而确保脱硫脱硝后排空尾气达到环保要求。本发明的工艺可以将ΝΗ3/Ν0χ摩尔比提高到5,从而大大提高脱硝效率,达到85%以上。虽然提高摩尔比还可以进一步提高脱硝效率到90%,但为了防止未发生反应的氨与系统中的SO3反应生成硫酸铵而在空气预热器上沉积,导致空气预热器的堵塞和腐蚀,优选ΝΗ3/Ν0χ摩尔比控制在2以上5以下,更优选4以上5以下。
[0055] 脱硝后的烟气任选地经除尘器除尘后,经换热器后温度约为50〜100°C,由脱硫塔底部氨水液位上方泵入脱硫塔。此外,将在20〜50°C稀释到5%〜10%浓度的氨水由上方和下方同时喷淋进入脱硫塔,雾化的氨水与烟气中的SO2直接接触进行气-气换热和瞬时化学反应,反应过程为:
[0056] S02+NH3+H20 — NH4HSO3
[0057] 2NH3+H20+S02 — (NH4) 2S03
[0058] (NH4) 2S03+S02+H20 — 2NH4HS03
[0059] 同时从脱硫塔底吹入压缩空气进行氧化,反应过程为:
[0060] 2 (NH4) 2S03+02 — (NH4) 2S04
[0061] 2NH4HS03+02 — NH4HSO4
[0062] 2S02+02 — 2S03
[0063] 通过以上反应除去烟气中的S02。
[0064] 当带有雾沫的气体以一定速度上升通过除雾器时,由于雾沫上升的惯性作用,雾沫与除雾器相碰撞而被附着在除雾器表面上。经除雾器表面上雾沫的扩散、雾沫的重力沉降,使雾沫形成较大的液滴沿着除雾器流下累积,直到聚集的液滴大到其自身产生的重力超过气体的上升力与液体表面张力的合力时,液滴就从除雾器上分离下落。
[0065] 净化后的烟气经除雾器(是在图1中脱硫塔顶打网格线的部分)由塔顶排出。经由烟气换热器与未脱硫的烟气进行换热,使脱硫后的烟气加热至50°C左右,最后由烟®排入大气。
[0066] 吸收SO2后的塔底吸收液中硫酸铵溶液达到一度浓度(>20%)时,由副产物泵送出,经脱水干燥、固液分离获得硫酸铵,作为化肥的原料。
[0067] 下面列出一个在实际生产过程中采用本发明的联合脱硫脱硝净化方法的例子,作为对本发明方案的进一步说明。
[0068] 实施例1[0069] 该例子中,锅炉使用200MW机组。在该例子中,先参考下表I对原料供煤进行分析,按照548225Nm3/h的燃烧空气通入量计算出燃烧产生的NOx的量为432Nm3/h,基于ΝΗ3/Ν0χ的摩尔比=5的进料比经喷射点1,2,3,4,5同时向炉膛内喷入氨。所述NH3的进料量也可以根据未经脱硝处理的烟气测量值进行调节,该烟气测量装置采用常规的测量装置,在图1中省略。喷射氨水时炉内的反应温度为10001:,反应时间(停留时间)为0.58。
[0070] 表1:原料煤质分析
[0071]
[0072] 表2:对煤燃烧后的灰分分析
[0073]
[0074] 表3:锅炉出口烟气卿A5处)参数表
[0075]
[0076] 表4:锅炉出口烟气成分参数表(锅炉BMCR工况/设计煤种,标准状态,实际O2)
[0077]
[0078] 上述脱硝后的气体除尘后经换热器调节至100°C,由脱硫塔底部氨水液位上方泵入脱硫塔,将温度30°C、浓度为10%的氨水由脱硫塔上方和下方同时喷淋进入脱硫塔,喷淋压力在1.5MPa下进行雾化,同时以5000Nm3/h(氧气流速1050Nm3/h)的量向脱硫塔内喷入空气。整个净化过程的脱硝效率是基于锅炉出口烟气NOx浓度与未喷氨情况锅炉出口烟气NOx浓度比之计算,脱硫效率基于排空烟气中SO2与进入脱硫塔前烟气中SO2浓度比值进行计算,结果示于下表5中。
[0079] 表5:脱硝脱硫后烟气参数
[0080]
[0081] 由上述实际的例子可知,采用本发明方法的脱硫脱硝净化工艺,联合脱硫脱硝的效率均良好,其中脱硝效率在85%以上,脱硫效率在90%以上,最后排空气体中的SO2和NOx也达到了目前环保标准允许的水平,且脱硫塔收集的氨形成硫酸铵固体,供化肥用,既保证资源的充分利用还能避免二次污染。
[0082] 此外,在附图1所示的净化装置中,保持其他条件与实施例1相同的情况下,仅改变在燃煤锅炉内的停留时间、脱硫塔空气通入量分别进行试验,按照与实施例1相同的方法测定脱硫脱硝效率,结果分别列于表6和表7中。
[0083] 表6:停留时间对脱硝效率的影响(NH3/N0x=5)
[0084]
[0085] 表7:脱硫塔空气通入量对脱硫效率
[0086]
[0087] 由表6可知,通过延长停留时间,能明显提高脱硝效率。由表7可知,单位时间的空气通入量大的话,脱硫效率也得到提高。
[0088] 以上所述,仅为本发明创造的具体实施方式,但本发明创造的保护范围并不局限于此,可在本技术领域的技术人员所知晓的技术手段和技术常识的范围内适当地合理地进行变化或替换,其都 应涵盖在本发明创造的保护范围之内。
Claims (17)
1.一种联合脱除烟气中氮氧化物和硫化物的方法,其特征在于:在反应锅炉的炉膛内喷入经气化后的氨水,利用选择性非催化还原法使烟气中的NOx还原为N2,然后烟气进入脱硫塔中,烟气中SO2被加入脱硫塔内的氨水吸收,净化后的烟气经烟囱排空。
2.根据权利要求1所述的方法,其中,氨水经气化后由一个以上喷射点喷入锅炉炉膛,各氨水喷射点分别置于炉膛燃烧器下方低温区域、燃烧器上方高温区域及炉内出口烟道区域中的一处以上。
3.根据权利要求1所述的方法,其中,所述锅炉中氨水喷射点区域内的反应温度为700 〜1200。。。
4.根据权利要求1所述的方法,其中,所述锅炉中氨水的喷入量以ΝΗ3/Ν0χ的摩尔比计为I〜5。
5.根据权利要求4所述的方法,其中,设置ΝΗ3/Ν0χ的摩尔比大于I时,使脱硝过程中未反应的NH3随烟气进入到脱硫塔,在脱硫塔内经除雾器和水洗塔回收作为脱硫剂来用于吸收SO2。
6.根据权利要求1所述的方法,其中,将氨气与水以一定比例混合制成反应所需浓度的氨水,浓度控制在3%〜10%的范围内,再由喷氨泵打入脱硫塔底部进行雾化吸收。
7.根据权利要求6所述的方法,其中,脱硫塔内氨水喷淋压力在0.8〜1.6MPa之间,满足喷头雾化要求。
8.根据权利要求6所述的方法,其中,脱硫塔底吹入压缩空气进行氧化,使塔底混合液中的亚硫酸铵氧 化形成硫酸铵,并进行蒸发结晶和固液分离制成硫酸铵产品。
9.根据权利要求6所述的方法,其中,脱硫塔顶部安装水洗系统用于洗涤烟气中夹带的NH3,水洗系统顶部装有除雾器以回收烟气中的NH3。
10.根据权利要求1所述的方法,其中,脱硝后烟气与脱硫后烟气经烟气换热器换热,前者降低烟气进入脱硫塔时的温度,后者利用前者换热的能量提高烟气排出脱硫塔时的温度。
11.一种联合脱除烟气中氮氧化物和硫化物的设备,其特征在于该设备包括下列部件: (A)用于燃烧煤的燃烧锅炉,锅炉炉膛内设置I个以上氨水的喷射点,各氨水喷射点分别置于炉膛燃烧器下方低温区域、燃烧器上方高温区域及炉内出口烟道区域中的一处以上, (B)脱硫塔,具有水洗氨气的水洗装置和二氧化硫吸收装置, (C)排空装置。
12.根据权利要求11的设备,其中燃烧锅炉包括控温装置,其控制氨水喷射点区域内的反应温度为700〜1200°C。
13.根据权利要求11的设备,其中锅炉上的氨水喷射装置能以ΝΗ3/Ν0χ的摩尔比计为I〜5进行氨水喷射。
14.根据权利要求11的设备,其中脱硫塔包括向其内部喷入氨水的喷氨泵,其将浓度控制在3%〜10%范围、压力控制在0.8〜1.6MPa范围的氨水喷入脱硫塔进行雾化吸收。
15.根据权利要求11的设备,其中脱硫塔包括从底部吹入压缩空气的装置,压缩空气使塔底混合液中的亚硫酸铵氧化形成硫酸铵,接着供入到蒸发装置蒸发结晶和分离装置固液分离制成硫酸铵产品。
16.根据权利要求11的设备,其中脱硫塔中的水洗系统用于洗涤烟气夹带的NH3,水洗系统顶部装有除雾器以回收烟气中的NH3。
17.根据权利要求11的设备, 其中还包括一个或多个烟气换热器,其可对通入燃烧锅炉的燃烧空气和脱硝后的烟气进行换热,或者对脱硝后的烟气和脱硫后的烟气进行换热。
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