CN201454383U - 碳酸氢铵干法热解制氨的烟气脱硝装置 - Google Patents
碳酸氢铵干法热解制氨的烟气脱硝装置 Download PDFInfo
- Publication number
- CN201454383U CN201454383U CN2009201092147U CN200920109214U CN201454383U CN 201454383 U CN201454383 U CN 201454383U CN 2009201092147 U CN2009201092147 U CN 2009201092147U CN 200920109214 U CN200920109214 U CN 200920109214U CN 201454383 U CN201454383 U CN 201454383U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- pyrolysis
- flue gas
- ammonium bicarbonate
- air
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 52
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 239000003546 flue gas Substances 0.000 title claims abstract description 28
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 title claims abstract description 19
- PRKQVKDSMLBJBJ-UHFFFAOYSA-N Ammonium carbonate Chemical compound 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N.N.OC(O)=O PRKQVKDSMLBJBJ-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 235000012538 ammonium bicarbonate Nutrition 0.000 title claims abstract description 19
- 239000001099 ammonium carbonate Substances 0.000 title claims abstract description 19
- 239000000843 powder Substances 0.000 claims abstract description 23
- 238000010790 dilution Methods 0.000 claims abstract description 8
- 229920002456 HOTAIR Polymers 0.000 claims description 13
- 238000005507 spraying Methods 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 5
- 239000003638 reducing agent Substances 0.000 abstract description 18
- 238000004642 transportation engineering Methods 0.000 abstract description 13
- 239000007788 liquid Substances 0.000 abstract description 6
- 238000004090 dissolution Methods 0.000 abstract description 5
- 238000002347 injection Methods 0.000 abstract 2
- 239000007924 injection Substances 0.000 abstract 2
- 241000273930 Brevoortia tyrannus Species 0.000 abstract 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea Chemical compound 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- 239000004202 carbamide Substances 0.000 description 28
- 235000011114 ammonium hydroxide Nutrition 0.000 description 12
- 230000000694 effects Effects 0.000 description 8
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- 238000009924 canning Methods 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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Abstract
本实用新型公开了属于火电厂烟气脱硝系统领域的一种碳酸氢铵干法热解制氨的烟气脱硝装置。由送粉风机、文丘利混合器、热解炉、缓冲罐、调节阀、氨气空气混合器依次串联后连接至与锅炉的烟气管道连接的喷氨格栅；喷氨格栅连接SCR反应器，SCR反应器再通过空气预热器和热解炉相连；碳酸氢铵粉仓通过给粉机与文丘利混合器连接；氨气空气混合器还与稀释风机连接。本装置采用碳酸氢铵干法热解，避免了设置溶解系统，简化系统设计，节省设备占地面积，进一步提高了经济性，避免了液氨及氨水等还原剂在运输存储方面的安全隐患，整个脱硝装置简洁，高效。
Description
碳酸氢铵干法热解制氨的烟气脱硝装置
技术领域
[0001] 本实用新型属于火电厂烟气脱硝技术领域，特别涉及一种碳酸氢铵干法热解制氨
的烟气脱硝装置。 技术背景
[0002] 火力发电厂排放出的烟气含有N0X，严重污染环境。日益严格的环保法规要求新建 火力发电机组必须安装脱硝系统。常用的烟气脱硝技术一般是将脱硝还原剂制备出氨气， 再将氨气通过喷氨格栅喷入到烟气中。在催化剂的作用下，N0X被氨气还原成N2。 [0003] 火力发电厂烟气脱硝系统常用的还原剂有液氨、氨水及尿素。液氨具有高毒性，采 用液氨作为还原剂必须对液氨的储存、运输和使用进行严格的规范。液氨通过液氨卸料压 縮机进入储存罐，随后进入蒸发器，在蒸汽加热作用下气化变成氨气，氨气再通过空气稀释 后送入烟气中脱硝。该脱硝系统需要设置液氨卸料压縮机，液氨储存罐和液氨蒸发器。 [0004] 采用氨水作为还原剂，是将25%的含氨水溶液通过加热装置使其蒸发，形成氨气 和水蒸汽，随后氨气被空气稀释后送入烟气中脱硝，该脱硝系统需要匹配大型的氨水存储 设备及氨水蒸发器。
[0005] 采用尿素作为还原剂，常见的有热解法和水解法制氨，尿素水解法是将尿素溶于 水中，尿素溶液受热析出的氨气经过空气稀释后送入烟气中脱硝。尿素热解法则是雾化后 的尿素溶液在加热条件下析出氨气，氨气经过空气稀释后送入烟气中脱硝。采用尿素作为 还原剂的脱硝系统，需要设置固体尿素存储系统、尿素溶解系统以及尿素水解或热解系统。 [0006] 火力发电厂烟气脱硝系统常用的还原剂有液氨、氨水及尿素。在这三种脱硝还原 剂中，液氨的投资、运输和事业成本为三者最低，但氨是国家规定的乙类危险品，在液氨的 运输和储存过程中都存在一定的危险性，液氨的运输和储存都需要国家有关部门的审批和 准许。液氨的储存量超过40吨即可被列为重大危险源，在其储存和运输过程中一旦发生事 故，其后果往往不堪设想。在国外，很多电站仅允许使用铁路运输液氨。液氨的高毒性使得 其工业应用存在较大的安全隐患。
[0007] 脱硝所用氨水的质量百分比一般为20%〜30%，较液氨安全，但是氨水也是一种 危险性物质，具有毒性和腐蚀性，低浓度的氨气剌激眼睛、皮肤和鼻子，而且运输体积大，运 输成本相对纯氨高，且氨水需要大型存储设备。其脱硝系统复杂，占地面积大，系统能耗高， 经济性差。
[0008] 尿素是一种固体物质，安全无害，运行存储方便。但是尿素溶液对容器具有腐蚀 性，系统增加了尿素溶解系统，系统变的更复杂。尿素制氨需要先制备成低浓度的尿素溶液 < 10%，在高温高压条件下进行，系统能耗高，设备占地面积大。尿素分解产物中可能含有 联二脲等聚合物，易与飞灰一起形成SCR催化剂层的堵塞，甚至造成催化剂的中毒。尿素作 为还原剂有潮解问题，尿素溶液要加添加剂，添加剂在管道和罐中容易产生沉淀，且尿素添 加剂长期影响SCR催化剂使用寿命。
[0009] 碳酸氢铵常温常压下以固态存在，所以与液氨和氨水相比，碳酸氢铵在储存和运输方面不存在安全问题；与尿素相比，碳酸氢铵分解温度低，可采用干法热解，脱硝系统经 济性更好。因此，从安全性和经济性角度考虑，碳酸氢铵适合作为烟气脱硝系统的还原剂。 因此，本发明提出了碳酸氢铵干法热解制氨的烟气脱硝工艺及其系统。
发明内容，
[0010] 本实用新型的目的是针对现有技术中液氨、氨水及尿素。液氨具有高毒性， [0011] 采用液氨作为还原剂必须对液氨的储存、运输和使用都存在安全隐患，必须进行
严格的规范处理，同时，设备复杂，运行成本高等不足而提供一种碳酸氢铵干法热解制氨的 烟气脱硝装置，其特征在于，所述碳酸氢铵干法热解制氨的烟气脱硝装置，由送粉风机1、文
丘利混合器4、热解炉5、缓冲罐6、调节阀7、氨气空气混合器9依次串联后连接至与锅炉12 的烟气管道连接的喷氨格栅11 ;喷氨格栅11连接SCR反应器10， SCR反应器10再通过空 气预热器13和热解炉5相连；碳酸氢铵粉仓2通过给粉机3与文丘利混合器4连接。 [0012] 所述氨气空气混合器9还与稀释风机8连接。
[0013] 所述热解炉为立式圆罐，热解炉体5. 4下部分布了四根热空气引入管5. 1和2根 碳酸氢铵气流引入管5. 2，顶部布置一根引出管5. 3。
[0014] 所述热解炉体5. 4的高度，以确保气体在炉内有0. 4〜0. 6秒的停留时间为准。 [0015] 所述四根热空气引入管轴线与立式圆罐截面轴线有10度的偏斜。 [0016] 本实用新型的有益效果是本脱硝工艺采用碳酸氢铵作为还原剂，运输储存方便安 全，经济性好，避免了液氨及氨水等还原剂在运输、存储方面存在的安全隐患，鉴于碳酸氢 铵易于分解，并且由于混合气体温度保持在175t:以上，则碳酸氢铵可以在短时间内分解， 分解率可以达到100%。采用碳酸氢铵干法热解，避免了设置溶解系统，经济性优于尿素还 原剂，整个脱硝系统简洁，高效。
附图说明
[0017] 图1为碳酸氢铵干法热解制氨的烟气脱硝系统图。
[0018] 图2为热解炉示意图。
[0019] 图3为热空气引入管布置截面。
[0020] 图4为碳酸氢铵喷射管布置截面。
具体实施方式
[0021] 本实用新型提供一种碳酸氢铵干法热解制氨的烟气脱硝装置。下面结合附图，具 体对本实用新型说明如下：
[0022] 在图1所示的碳酸氢铵干法热解制氨的烟气脱硝装置图中，由送粉风机1、文丘利 混合器4、热解炉5、缓冲罐6、调节阀7、氨气空气混合器9依次串联后连接至与锅炉12的 烟气管道连接的喷氨格栅11 ;喷氨格栅11连接SCR反应器10， SCR反应器10再通过空气 预热器13和热解炉5相连；碳酸氢铵粉仓2通过给粉机3与文丘利混合器4连接；氨气空 气混合器9还与稀释风机8连接。
[0023] 所述热解炉为立式圆罐，热解炉体5. 4的高度，以确保气体在炉内有0. 4〜0. 6秒 的停留时间为准。热解炉体5. 4下部分布了与空气引入管轴线与立式圆罐截面轴线有10度的偏斜的四根热空气引入管5. 1 (如图3所示），使得热空气进入热解炉后具有一定旋转 强度，炉内流场充满度好，热解炉内温度分布均匀。和2根碳酸氢铵气流弓I入管5. 2 (如图 1、4所示），顶部布置一根引出管5. 3 ;碳酸氢铵气流引入管5. 2对称分布在热解炉的四根 热空气引入管5. 1上方（如图2所示），使热空气对碳酸氢铵粉末具有良好的依托作用，防 止碳酸氢铵粉末沉积在热解炉底部；碳酸氢铵气流混合物与热空气在此处相互混合，共同 向上流动，在热空气的作用下碳酸氢铵分解成氨气、二氧化碳和水蒸气。 [0024] 碳酸氢铵粉末直接通过罐装车送入碳酸氢铵粉仓2内储存，碳酸氢铵粉仓2下的 给粉机3根据烟气中N0X的量来改变给粉量，将碳酸氢铵粉末送入文丘利混合器4，碳酸氢 铵粉末被送粉风机1吹来的风经过立式圆罐热解炉体5. 4下部分布的2根碳酸氢铵气流引 入管5. 2输送到热解炉5内，空气预热器13送入的热空气从热解炉体5. 4下部分布的四根 热空气引入管5. l进入热解炉5(如图2所示）内加热碳酸氢铵粉末，分析纯级别的碳酸氢 铵最低的分解温度在8(TC以上，普通碳酸氢铵因为含有杂质，实际分解温度为35°C -60°C。 采用30(TC以上的空气来热解碳酸氢铵粉末，且保证热解炉出口气流温度在175t:以上，则 碳酸氢铵可以在O. 1〜0.4秒时间内分解，分解率可以达到100%，分解出氨气、二氧化碳和 水，热解后的混合气体流通过热解炉顶部的一根引出管5. 3入到缓冲罐，经过调节阀7进入 氨气空气混合器9，并由稀释风机8稀释，稀释后的混合气体通过与锅炉12的烟气管道连接 的喷氨格栅11进入SCR反应器10，在催化剂的作用下，氨气将NOx还原成N2。其中，混合 气体的温度需要保持在175t:以上，以避免氨气与二氧化碳低温下发生逆向反应生成氨基 甲酸盐，为了保持混合气体温度，在缓冲罐6内设置起加热作用的蒸汽管道，以保持混合气 体的温度，使得碳酸氢铵充分热解；
[0025] 所说碳酸氢铵含氨量为21.5%，尿素含氨量为56. 7% 。 2009年5月国内碳酸氢铵 的平均价格在480元/吨左右，尿素的平均销售价格在1800元/吨左右。每生成1公斤氨 气，采用碳酸氢铵作为还原剂，需要花费2. 23元；而采用尿素作为还原剂，则需要花费3. 17 元。明显，碳酸氢铵作为还原剂比尿素更为经济。且碳酸氢铵分解温度低，鉴于碳酸氢铵易 于分解，避免了设置溶解系统，简化了系统设计，节省了设备占地面积，进一步提高了经济 性和安全性。整个脱硝系统简洁，高效，进一步提高了经济性。
Claims (5)
- 一种碳酸氢铵干法热解制氨的烟气脱硝装置，其特征在于，所述碳酸氢铵干法热解制氨的烟气脱硝装置，由送粉风机(1)、文丘利混合器(4)、热解炉(5)、缓冲罐(6)、调节阀(7)、氨气空气混合器(9)依次串联后连接至与锅炉(12)的烟气管道连接的喷氨格栅(11)；喷氨格栅(11)连接SCR反应器(10)，SCR反应器(10)再通过空气预热器(13)和热解炉(5)相连；碳酸氢铵粉仓(2)通过给粉机(3)与文丘利混合器(4)连接。
- 2. 根据权利要求1所述碳酸氢铵干法热解制氨的烟气脱硝装置，其特征在于，所述氨 气空气混合器（9)还与稀释风机（8)连接。
- 3. 根据权利要求1所述碳酸氢铵干法热解制氨的烟气脱硝装置，其特征在于，所述热 解炉为立式圆罐，热解炉体（5.4)下部分布了四根热空气引入管（5. 1)和2根碳酸氢铵气 流引入管（5. 2)，顶部布置一根引出管（5. 3)。
- 4. 根据权利要求3所述碳酸氢铵干法热解制氨的烟气脱硝装置，其特征在于，所述热 解炉体（5. 4)的高度，以确保气体在炉内有0. 4〜0. 6秒的停留时间为准。
- 5. 根据权利要求1所述碳酸氢铵干法热解制氨的烟气脱硝装置，其特征在于，所述四 根热空气引入管轴线与立式圆罐截面轴线有10度的偏斜。
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| CN102068904A (zh) * | 2010-12-10 | 2011-05-25 | 中电投远达环保工程有限公司 | 直喷尿素法scr烟气脱硝工艺及装置 |
| CN101574616B (zh) * | 2009-06-08 | 2011-09-07 | 叶力平 | 碳酸氢铵干法热解制氨的烟气脱硝工艺及其系统 |
| CN105893768A (zh) * | 2016-04-07 | 2016-08-24 | 上海电气电站环保工程有限公司 | 对燃煤锅炉脱硝装置中的催化剂活性估计的方法 |
| CN106606928A (zh) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | 蒸汽裂解生产低碳烯烃产生的裂解烟气的脱硝方法 |
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| CN101574616B (zh) * | 2009-06-08 | 2011-09-07 | 叶力平 | 碳酸氢铵干法热解制氨的烟气脱硝工艺及其系统 |
| CN102068904A (zh) * | 2010-12-10 | 2011-05-25 | 中电投远达环保工程有限公司 | 直喷尿素法scr烟气脱硝工艺及装置 |
| CN102068904B (zh) * | 2010-12-10 | 2013-10-02 | 中电投远达环保工程有限公司 | 直喷尿素法scr烟气脱硝工艺及装置 |
| CN106606928A (zh) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | 蒸汽裂解生产低碳烯烃产生的裂解烟气的脱硝方法 |
| CN105893768A (zh) * | 2016-04-07 | 2016-08-24 | 上海电气电站环保工程有限公司 | 对燃煤锅炉脱硝装置中的催化剂活性估计的方法 |
| CN105893768B (zh) * | 2016-04-07 | 2018-10-09 | 上海电气电站环保工程有限公司 | 对燃煤锅炉脱硝装置中的催化剂活性估计的方法 |
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