CN106823730B - Ammonia desulfurization system capable of preventing ammonia from escaping - Google Patents
Ammonia desulfurization system capable of preventing ammonia from escaping Download PDFInfo
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Abstract
Description
技术领域Technical field
本发明涉及烟气处理领域，尤其涉及一种防止氨逃逸的氨法脱硫系统。The invention relates to the field of flue gas treatment, and in particular to an ammonia desulfurization system that prevents ammonia from escaping.
背景技术Background technique
氨法脱硫技术以水溶液中NH3和SO2的反应为基础，在烟气脱硫塔的吸收段将烟气中的SO2吸收，得到脱硫中间产品亚硫酸铵或亚硫酸氢铵的水溶液，在脱硫系统的循环槽，鼓入压缩空气进行亚硫酸铵的氧化反应，将亚硫酸铵直接氧化成硫酸铵溶液。在脱硫塔的浓缩段，利用高温烟气的热量将硫酸铵溶液浓缩，得到含有一定固含量的硫酸铵浆液，浆液经旋流器浓缩、离心分离、干燥、包装等工序，得到硫酸铵产品。反应方程式如下：Ammonia desulfurization technology is based on the reaction of NH 3 and SO 2 in aqueous solution. The SO 2 in the flue gas is absorbed in the absorption section of the flue gas desulfurization tower to obtain an aqueous solution of desulfurization intermediate product ammonium sulfite or ammonium bisulfite. The circulation tank of the desulfurization system blows in compressed air to carry out the oxidation reaction of ammonium sulfite, and directly oxidizes ammonium sulfite into ammonium sulfate solution. In the concentration section of the desulfurization tower, the ammonium sulfate solution is concentrated using the heat of high-temperature flue gas to obtain an ammonium sulfate slurry containing a certain solid content. The slurry undergoes cyclone concentration, centrifugal separation, drying, packaging and other processes to obtain ammonium sulfate products. The reaction equation is as follows:
SO2 + NH3 + H2O = NH4HSO3 SO 2 + NH 3 + H 2 O = NH 4 HSO 3
SO2 + 2NH3 + H2O = (NH4)2SO3 SO 2 + 2NH 3 + H 2 O = (NH 4 ) 2 SO 3
SO2 + (NH4)2SO3 + H2O = 2NH4HSO3 SO 2 + (NH 4 ) 2 SO 3 + H 2 O = 2NH 4 HSO 3
NH3 + NH4HSO3 =2 (NH4)2SO3 NH 3 + NH 4 HSO 3 =2 (NH 4 ) 2 SO 3
2 (NH4)2SO3 + O2 = 2 (NH4)2SO4 2 (NH 4 ) 2 SO 3 + O 2 = 2 (NH 4 ) 2 SO 4
氨法脱硫是一种高效、低耗能的湿法脱硫方式，脱硫过程是气液相反应，反应速率快，吸收剂利用率高，能保持脱硫效率95~99%。 氨在水中的溶解度超过20%。氨法具有丰富的原料。氨法以氨为原料，其形式可以是液氨、氨水和碳铵。氨法的最大特点是 SO2的可资源化，可将污染物SO2回收成为高附加值的(NH4)2SO4，这是一种优良的氮肥，在我国具有很好的市场前景。Ammonia desulfurization is a high-efficiency, low-energy-consuming wet desulfurization method. The desulfurization process is a gas-liquid phase reaction with a fast reaction rate, high absorbent utilization rate, and can maintain a desulfurization efficiency of 95~99%. The solubility of ammonia in water exceeds 20%. The ammonia method has abundant raw materials. The ammonia method uses ammonia as raw material, which can be in the form of liquid ammonia, ammonia water and ammonium bicarbonate. The biggest feature of the ammonia method is the resource utilization of SO 2 , which can recover pollutant SO 2 into high value-added (NH 4 ) 2 SO 4 , which is an excellent nitrogen fertilizer and has good market prospects in China.
目前，国内氨法脱硫技术普遍存在脱硫剂消耗大、氨逃逸严重、气溶胶难以消除、亚硫酸铵氧化慢、硫酸铵结晶难等问题，这些问题的存在制约了氨法脱硫技术的进一步推广应用，其中氨逃逸现象是指脱硫喷淋塔出口的游离氨气的超标排放。解决氨法脱硫氨逃逸的途径主要是通过提高亚硫酸铵氧化率、改变加氨点、控制脱硫液pH值等措施来降低脱硫尾气携带氨，这些途径只能尽量拦截脱硫尾气携带氨，不能从根本上解决问题。At present, domestic ammonia desulfurization technology has common problems such as high desulfurization agent consumption, serious ammonia escape, difficulty in eliminating aerosols, slow oxidation of ammonium sulfite, and difficulty in crystallization of ammonium sulfate. The existence of these problems has restricted the further promotion and application of ammonia desulfurization technology. , where ammonia slip phenomenon refers to the excessive emission of free ammonia at the outlet of the desulfurization spray tower. The way to solve the problem of ammonia escape from ammonia-based desulfurization is mainly to reduce the ammonia carried by the desulfurization tail gas by increasing the ammonium sulfite oxidation rate, changing the ammonia addition point, controlling the pH value of the desulfurization liquid and other measures. These ways can only intercept the ammonia carried by the desulfurization tail gas as much as possible, but cannot from the desulfurization tail gas. Solve the problem fundamentally.
发明内容Contents of the invention
本发明所要解决的技术问题是针对上述的技术现状而提供一种防止氨逃逸的氨法脱硫系统，将水吸收脱硫过程的H2SO3溶液用过氧化氢催化氧化为稀H2SO4溶液，并在脱硫喷淋塔出口之前进行喷淋，将逃逸的氨气吸收，从根本上解决氨逃逸问题，为氨法脱硫的应用推广扫除障碍。The technical problem to be solved by the present invention is to provide an ammonia desulfurization system that prevents ammonia from escaping in view of the above technical status quo, and uses hydrogen peroxide to catalytically oxidize the H 2 SO 3 solution in the water absorption desulfurization process into a dilute H 2 SO 4 solution. , and spray before the outlet of the desulfurization spray tower to absorb the escaped ammonia, fundamentally solving the problem of ammonia escape and clearing obstacles for the application and promotion of ammonia desulfurization.
本发明解决上述技术问题所采用的技术方案为一种防止氨逃逸的氨法脱硫系统，其特征在于：所述的系统由：第一吸收塔1，单向阀2，氧化器3，第一离心泵4，第二离心泵5，过氧化氢储罐6，第三离心泵7，第二吸收塔8组成；所述的第一吸收塔1和第二吸收塔8为结构相同的塔器，所述塔器的顶部设置有出风口a，底部设置有排渣口f，所述塔器的内部从上往下依次设置有除雾器b、上层喷头c和下层喷头d；所述塔器的侧面设置有进风口e，所述进风口e的位置低于下层喷头d；所述的氧化器3为一内装填有催化剂的管道，所述的催化剂的材质为二氧化锰；所述第一吸收塔1的出风口a通过第一管路与第二吸收塔8的进风口e连通，所述第一吸收塔1的底部还设有水进口；所述第一离心泵4的进口通过第二管路与第一吸收塔1的底部连通，离心泵4的出口通过第三管路与第一三通的第一个口连通，第一三通的第二个口通过第四管路与第一吸收塔1的下层喷头d连通，第一三通的第三个口通过第五管路与第二三通的第一个口连通，第二三通的第二个口通过第六管路与第一吸收塔1的上层喷头c连通；第二三通的第三个口通过第七管路与第三三通的第一个口连通，在第七管路上设置有单向阀2，且单向阀2的通路方向为从第二三通往第三三通；第三三通的第二个口通过第八管路与第二离心泵5的出口连通，第二离心泵5的进口通过第九管路与过氧化氢储罐6的底部连通；第三三通的第三个口通过第十管路与氧化器3的一端连通，氧化器3的另一端通过第十一管路与第四三通的第一个口连通；第四三通的第二个口通过第十二管路与第二吸收塔8的上层喷头c连通，第四三通的第三个口通过第十三管路与第一四通的第一个口连通，第一四通的第二个口通过第十四管路与第二吸收塔8的下层喷头d连通，第一四通的第三个口通过第十五管路与第三离心泵7的出口连通，第一四通的第四个口为硫酸铵溶液出口；第三离心泵7的进口通过第十六管路与第二吸收塔8的底部连通；第二吸收塔8的底部还设置有液氨进口和氧化空气进口。The technical solution adopted by the present invention to solve the above technical problems is an ammonia desulfurization system that prevents ammonia from escaping. It is characterized in that: the system consists of: a first absorption tower 1, a one-way valve 2, an oxidizer 3, a first It consists of a centrifugal pump 4, a second centrifugal pump 5, a hydrogen peroxide storage tank 6, a third centrifugal pump 7, and a second absorption tower 8; the first absorption tower 1 and the second absorption tower 8 are towers with the same structure. , the top of the tower is provided with an air outlet a, and the bottom is provided with a slag discharge port f. The interior of the tower is provided with a demister b, an upper layer nozzle c, and a lower layer nozzle d in order from top to bottom; the tower An air inlet e is provided on the side of the device, and the position of the air inlet e is lower than the lower nozzle d; the oxidizer 3 is a pipe filled with a catalyst, and the material of the catalyst is manganese dioxide; The air outlet a of the first absorption tower 1 is connected to the air inlet e of the second absorption tower 8 through the first pipeline. The bottom of the first absorption tower 1 is also provided with a water inlet; the inlet of the first centrifugal pump 4 The second pipe is connected to the bottom of the first absorption tower 1. The outlet of the centrifugal pump 4 is connected to the first port of the first tee through the third pipe. The second port of the first tee is connected to the fourth pipe. The road is connected to the lower nozzle d of the first absorption tower 1, the third port of the first tee is connected to the first port of the second tee through the fifth pipe, and the second port of the second tee is connected through the fifth pipe. The sixth pipeline is connected to the upper nozzle c of the first absorption tower 1; the third port of the second tee is connected to the first port of the third tee through the seventh pipeline, and a one-way Valve 2, and the passage direction of the one-way valve 2 is from the second three-way to the third three-way; the second port of the third three-way is connected to the outlet of the second centrifugal pump 5 through the eighth pipeline, and the second centrifugal pump 5 The inlet of the pump 5 is connected to the bottom of the hydrogen peroxide storage tank 6 through the ninth pipe; the third port of the third tee is connected to one end of the oxidizer 3 through the tenth pipe, and the other end of the oxidizer 3 is connected through the tenth pipe. The eleventh pipeline is connected to the first port of the fourth tee; the second port of the fourth tee is connected to the upper nozzle c of the second absorption tower 8 through the twelfth pipeline; the third port of the fourth tee The first port is connected to the first port of the first four-way through the thirteenth pipe, and the second port of the first four-way is connected to the lower nozzle d of the second absorption tower 8 through the fourteenth pipe. The third port of the first four-way is connected to the outlet of the third centrifugal pump 7 through the fifteenth pipeline. The fourth port of the first four-way is the ammonium sulfate solution outlet; the inlet of the third centrifugal pump 7 passes through the sixteenth pipeline. It is connected with the bottom of the second absorption tower 8; the bottom of the second absorption tower 8 is also provided with a liquid ammonia inlet and an oxidation air inlet.
本发明的一种防止氨逃逸的氨法脱硫系统的基本工作过程如下：含SO2的烟气从第一吸收塔1的进风口e进入塔内向上流动，塔底的H2SO3水溶液由第一离心泵4输送，一部分被输送至第一吸收塔1的上层喷头c和下层喷头d，并在塔内喷淋而下与向上流动的烟气进行吸收，烟气中的部分SO2气体和大部分的烟气颗粒物被吸收，在第一吸收塔1的塔底部得到混有颗粒物的H2SO3水溶液，颗粒物在重力的作用下从排渣口f排出，水从进水口补充；在第一吸收塔1内吸收后的烟气穿过除雾器b脱除雾滴，后从第一吸收塔1的出风口a排出，再通过第一管路进入第二吸收塔8，并在第二吸收塔8内从下往上流动；由第一离心泵4输送的另一部分H2SO3水溶液，通过第七管路输送至第三三通；过氧化氢储罐6中的过氧化氢水溶液由第二离心泵5输送至第三三通与H2SO3水溶液混合得到混合液，混合液进入氧化器3内发生氧化反应，混合液中H2SO3溶液被氧化成H2SO4溶液并进入第四三通；第二吸收塔8底部的吸收液（主要成分为(NH4)2SO4 、(NH4)2SO3、NH4HSO3的溶液）通过第三离心泵7输送，输送的吸收液的第一部分进入第二吸收塔8的下层喷头d并在塔内喷淋而下，输送的吸收液的第二部分通过第一四通的第四个口去硫酸铵结晶系统，输送的吸收液的第三部分进入第四三通并与H2SO4溶液混合后得到酸性喷淋液进入第二吸收塔8的下层喷头c在塔内喷淋而下；在第二吸收塔8的内部下层喷头d喷淋而下的吸收液与烟气接触吸收了绝大部分的SO2并有一部分氨气逃逸，在第二吸收塔8的内部上层喷头c喷淋而下的酸性喷淋液吸收逃逸的氨，这样就控制住了氨的逃逸，净化烟气从第二吸收塔8的出风口a排出；氧化空气从第二吸收塔8底部的氧化空气进口进入塔底部，将 (NH4)2SO3氧化成(NH4)2SO4；液氨从第二吸收塔8底部的液氨进口加入，以维持塔底吸收液的碱性。The basic working process of an ammonia desulfurization system to prevent ammonia escape of the present invention is as follows: flue gas containing SO 2 enters the tower from the air inlet e of the first absorption tower 1 and flows upward, and the H 2 SO 3 aqueous solution at the bottom of the tower is The first centrifugal pump 4 delivers a part of it to the upper nozzle c and the lower nozzle d of the first absorption tower 1, and is sprayed down and absorbed in the upward flowing flue gas in the tower. Part of the SO 2 gas in the flue gas Most of the flue gas particles are absorbed, and an H 2 SO 3 aqueous solution mixed with particles is obtained at the bottom of the first absorption tower 1. The particles are discharged from the slag discharge port f under the action of gravity, and water is replenished from the water inlet; The absorbed flue gas in the first absorption tower 1 passes through the demister b to remove mist droplets, and then is discharged from the air outlet a of the first absorption tower 1, and then enters the second absorption tower 8 through the first pipeline, and is The second absorption tower 8 flows from bottom to top; another part of the H 2 SO 3 aqueous solution transported by the first centrifugal pump 4 is transported to the third tee through the seventh pipeline; the peroxide in the hydrogen peroxide storage tank 6 The hydrogen aqueous solution is transported to the third tee by the second centrifugal pump 5 and mixed with the H 2 SO 3 aqueous solution to obtain a mixed liquid. The mixed liquid enters the oxidizer 3 to undergo an oxidation reaction, and the H 2 SO 3 solution in the mixed liquid is oxidized into H 2 SO 4 solution and enters the fourth tee; the absorption liquid at the bottom of the second absorption tower 8 (the solution whose main components are (NH 4 ) 2 SO 4 , (NH 4 ) 2 SO 3 , NH 4 HSO 3 ) passes through the third centrifugal pump 7 is transported. The first part of the transported absorption liquid enters the lower nozzle d of the second absorption tower 8 and is sprayed down in the tower. The second part of the transported absorption liquid passes through the fourth port of the first four-way to remove ammonium sulfate. In the crystallization system, the third part of the transported absorption liquid enters the fourth tee and is mixed with the H 2 SO 4 solution to obtain an acidic spray liquid that enters the lower nozzle c of the second absorption tower 8 and is sprayed down in the tower; The absorption liquid sprayed down from the inner lower nozzle d of the second absorption tower 8 contacts with the flue gas and absorbs most of the SO 2 and a part of the ammonia gas escapes, and is sprayed down from the upper nozzle c inside the second absorption tower 8 The acidic spray liquid absorbs the escaped ammonia, thus controlling the escape of ammonia, and the purified flue gas is discharged from the air outlet a of the second absorption tower 8; the oxidation air enters the bottom of the tower from the oxidation air inlet at the bottom of the second absorption tower 8 , (NH 4 ) 2 SO 3 is oxidized into (NH 4 ) 2 SO 4 ; liquid ammonia is added from the liquid ammonia inlet at the bottom of the second absorption tower 8 to maintain the alkalinity of the absorption liquid at the bottom of the tower.
本发明的有益效果是：将第一吸收塔得到的H2SO3溶液用过氧化氢氧化成H2SO4溶液，并与第二吸收塔的吸收液混合以维持第二吸收塔上层喷淋液的酸性，利用该酸性喷淋液吸收控制逃逸的氨气，从根本上解决了氨法脱硫过程氨逃逸的问题。The beneficial effects of the present invention are: oxidize the H 2 SO 3 solution obtained from the first absorption tower with hydrogen peroxide into the H 2 SO 4 solution, and mix it with the absorption liquid from the second absorption tower to maintain the upper layer spraying of the second absorption tower. The acidic spray liquid is used to absorb and control the escaped ammonia gas, which fundamentally solves the problem of ammonia escape in the ammonia desulfurization process.
附图说明Description of the drawings
图1是本发明的一种防止氨逃逸的氨法脱硫系统的流程示意图。Figure 1 is a schematic flow diagram of an ammonia desulfurization system that prevents ammonia from escaping according to the present invention.
其中：1为第一吸收塔，2为单向阀，3为氧化器，4为第一离心泵，5为第二离心泵，6为过氧化氢储罐，7为第三离心泵，8为第二吸收塔，a为出风口，b为除雾器，c为上层喷头，d为下层喷头，e为进风口，f为排渣口。Among them: 1 is the first absorption tower, 2 is the one-way valve, 3 is the oxidizer, 4 is the first centrifugal pump, 5 is the second centrifugal pump, 6 is the hydrogen peroxide storage tank, 7 is the third centrifugal pump, 8 is the second absorption tower, a is the air outlet, b is the mist eliminator, c is the upper nozzle, d is the lower nozzle, e is the air inlet, and f is the slag discharge port.
具体实施方式Detailed ways
需要说明的是，在不冲突的情况下，本申请中的实施例及实施例中的特征可以相互组合。下面将参考附图1通过实施例对本发明作进一步详细描述。It should be noted that, as long as there is no conflict, the embodiments and features in the embodiments of this application can be combined with each other. The present invention will be described in further detail below through embodiments with reference to Figure 1 .
实施例1Example 1
一种防止氨逃逸的氨法脱硫系统由第一吸收塔1，单向阀2，氧化器3，第一离心泵4，第二离心泵5，过氧化氢储罐6，第三离心泵7，第二吸收塔8组成；所述的第一吸收塔1和第二吸收塔8为结构相同的塔器，所述塔器的顶部设置有出风口a，底部设置有排渣口f，所述塔器的内部从上往下依次设置有除雾器b、上层喷头c和下层喷头d；所述塔器的侧面设置有进风口e，所述进风口e的位置低于下层喷头d；所述的氧化器3为一内装填有催化剂的管道，所述的催化剂的材质为二氧化锰；所述第一吸收塔1的出风口a通过第一管路与第二吸收塔8的进风口e连通，所述第一吸收塔1的底部还设有水进口；所述第一离心泵4的进口通过第二管路与第一吸收塔1的底部连通，离心泵4的出口通过第三管路与第一三通的第一个口连通，第一三通的第二个口通过第四管路与第一吸收塔1的下层喷头连通，第一三通的第三个口通过第五管路与第二三通的第一个口连通，第二三通的第二个口通过第六管路与第一吸收塔1的上层喷头c连通；第二三通的第三个口通过第七管路与第三三通的第一个口连通，在第七管路上设置有单向阀2，且单向阀2的通路方向为从第二三通往第三三通；第三三通的第二个口通过第八管路与第二离心泵5的出口连通，第二离心泵5的进口通过第九管路与过氧化氢储罐6的底部连通；第三三通的第三个口通过第十管路与氧化器3的一端连通，氧化器3的另一端通过第十一管路与第四三通的第一个口连通；第四三通的第二个口通过第十二管路与第二吸收塔8的上层喷头c连通，第四三通的第三个口通过第十三管路与第一四通的第一个口连通，第一四通的第二个口通过第十四管路与第二吸收塔8的下层喷头d连通，第一四通的第三个口通过第十五管路与第三离心泵7的出口连通，第一四通的第四个口为硫酸铵溶液出口；第三离心泵7的进口通过第十六管路与第二吸收塔8的底部连通；第二吸收塔8的底部还设置有液氨进口和氧化空气进口。An ammonia desulfurization system that prevents ammonia from escaping consists of a first absorption tower 1, a one-way valve 2, an oxidizer 3, a first centrifugal pump 4, a second centrifugal pump 5, a hydrogen peroxide storage tank 6, and a third centrifugal pump 7 , consisting of a second absorption tower 8; the first absorption tower 1 and the second absorption tower 8 are towers with the same structure. The top of the tower is provided with an air outlet a, and the bottom is provided with a slag discharge port f, so The interior of the tower is provided with a demister b, an upper nozzle c and a lower nozzle d in sequence from top to bottom; an air inlet e is provided on the side of the tower, and the position of the air inlet e is lower than the lower nozzle d; The oxidizer 3 is a pipeline filled with a catalyst, and the catalyst is made of manganese dioxide; the air outlet a of the first absorption tower 1 passes through the first pipeline and the inlet of the second absorption tower 8 The tuyere e is connected, and the bottom of the first absorption tower 1 is also provided with a water inlet; the inlet of the first centrifugal pump 4 is connected with the bottom of the first absorption tower 1 through a second pipeline, and the outlet of the centrifugal pump 4 passes through the second pipeline. The third pipeline is connected to the first port of the first tee, the second port of the first tee is connected to the lower nozzle of the first absorption tower 1 through the fourth pipeline, and the third port of the first tee is connected to The fifth pipeline is connected to the first port of the second tee, and the second port of the second tee is connected to the upper nozzle c of the first absorption tower 1 through the sixth pipeline; the third port of the second tee The port is connected to the first port of the third tee through the seventh pipeline. A one-way valve 2 is provided on the seventh pipeline, and the passage direction of the one-way valve 2 is from the second third to the third tee; The second port of the third tee is connected to the outlet of the second centrifugal pump 5 through the eighth pipe, and the inlet of the second centrifugal pump 5 is connected to the bottom of the hydrogen peroxide storage tank 6 through the ninth pipe; The third port of the fourth tee is connected to one end of the oxidizer 3 through the tenth pipe, and the other end of the oxidizer 3 is connected to the first port of the fourth tee through the eleventh pipe; The first port is connected to the upper nozzle c of the second absorption tower 8 through the twelfth pipeline, and the third port of the fourth tee is connected to the first port of the first four-way through the thirteenth pipeline. The second port of the first four-way is connected to the lower nozzle d of the second absorption tower 8 through the fourteenth pipeline, and the third port of the first four-way is connected to the outlet of the third centrifugal pump 7 through the fifteenth pipeline. The fourth port of the four-way is the ammonium sulfate solution outlet; the inlet of the third centrifugal pump 7 is connected to the bottom of the second absorption tower 8 through the sixteenth pipeline; the bottom of the second absorption tower 8 is also provided with a liquid ammonia inlet and oxidizing air inlet.
本发明的一种防止氨逃逸的氨法脱硫系统的基本工作过程如下：含SO2的烟气从第一吸收塔1的进风口e进入塔内向上流动，塔底的H2SO3水溶液由第一离心泵4输送，一部分被输送至第一吸收塔1的上层喷头c和下层喷头d，并在塔内喷淋而下与向上流动的烟气进行吸收，烟气中的部分SO2气体和大部分的烟气颗粒物被吸收，在第一吸收塔1的塔底部得到混有颗粒物的H2SO3水溶液，颗粒物在重力的作用下从排渣口f排出，水从进水口补充；在第一吸收塔1内吸收后的烟气穿过除雾器b脱除雾滴，后从第一吸收塔1的出风口a排出，再通过第一管路进入第二吸收塔8，并在第二吸收塔8内从下往上流动；由第一离心泵4输送的另一部分H2SO3水溶液，通过第七管路输送至第三三通；过氧化氢储罐6中的过氧化氢水溶液由第二离心泵5输送至第三三通与H2SO3水溶液混合得到混合液，混合液进入氧化器3内发生氧化反应，混合液中H2SO3溶液被氧化成H2SO4溶液并进入第四三通；第二吸收塔8底部的吸收液（主要成分为(NH4)2SO4 、(NH4)2SO3、NH4HSO3的溶液）通过第三离心泵7输送，输送的吸收液的第一部分进入第二吸收塔8的下层喷头d并在塔内喷淋而下，输送的吸收液的第二部分通过第一四通的第四个口去硫酸铵结晶系统，输送的吸收液的第三部分进入第四三通并与H2SO4溶液混合后得到酸性喷淋液进入第二吸收塔8的下层喷头c在塔内喷淋而下；在第二吸收塔8的内部下层喷头d喷淋而下的吸收液与烟气接触吸收了绝大部分的SO2并有一部分氨气逃逸，在第二吸收塔8的内部上层喷头c喷淋而下的酸性喷淋液吸收逃逸的氨，这样就控制住了氨的逃逸，净化烟气从第二吸收塔8的出风口a排出；氧化空气从第二吸收塔8底部的氧化空气进口进入塔底部，将 (NH4)2SO3氧化成(NH4)2SO4；液氨从第二吸收塔8底部的液氨进口加入，以维持塔底吸收液的碱性。The basic working process of an ammonia desulfurization system to prevent ammonia escape of the present invention is as follows: flue gas containing SO 2 enters the tower from the air inlet e of the first absorption tower 1 and flows upward, and the H 2 SO 3 aqueous solution at the bottom of the tower is The first centrifugal pump 4 delivers a part of it to the upper nozzle c and the lower nozzle d of the first absorption tower 1, and is sprayed down and absorbed in the upward flowing flue gas in the tower. Part of the SO 2 gas in the flue gas Most of the flue gas particles are absorbed, and an H 2 SO 3 aqueous solution mixed with particles is obtained at the bottom of the first absorption tower 1. The particles are discharged from the slag discharge port f under the action of gravity, and water is replenished from the water inlet; The absorbed flue gas in the first absorption tower 1 passes through the demister b to remove mist droplets, and then is discharged from the air outlet a of the first absorption tower 1, and then enters the second absorption tower 8 through the first pipeline, and is The second absorption tower 8 flows from bottom to top; another part of the H 2 SO 3 aqueous solution transported by the first centrifugal pump 4 is transported to the third tee through the seventh pipeline; the peroxide in the hydrogen peroxide storage tank 6 The hydrogen aqueous solution is transported to the third tee by the second centrifugal pump 5 and mixed with the H 2 SO 3 aqueous solution to obtain a mixed liquid. The mixed liquid enters the oxidizer 3 to undergo an oxidation reaction, and the H 2 SO 3 solution in the mixed liquid is oxidized into H 2 SO 4 solution and enters the fourth tee; the absorption liquid at the bottom of the second absorption tower 8 (the solution whose main components are (NH 4 ) 2 SO 4 , (NH 4 ) 2 SO 3 , NH 4 HSO 3 ) passes through the third centrifugal pump 7 is transported. The first part of the transported absorption liquid enters the lower nozzle d of the second absorption tower 8 and is sprayed down in the tower. The second part of the transported absorption liquid passes through the fourth port of the first four-way to remove ammonium sulfate. In the crystallization system, the third part of the transported absorption liquid enters the fourth tee and is mixed with the H 2 SO 4 solution to obtain an acidic spray liquid that enters the lower nozzle c of the second absorption tower 8 and is sprayed down in the tower; The absorption liquid sprayed down from the inner lower nozzle d of the second absorption tower 8 contacts with the flue gas and absorbs most of the SO 2 and a part of the ammonia gas escapes, and is sprayed down from the upper nozzle c inside the second absorption tower 8 The acidic spray liquid absorbs the escaped ammonia, thus controlling the escape of ammonia, and the purified flue gas is discharged from the air outlet a of the second absorption tower 8; the oxidation air enters the bottom of the tower from the oxidation air inlet at the bottom of the second absorption tower 8 , (NH 4 ) 2 SO 3 is oxidized into (NH 4 ) 2 SO 4 ; liquid ammonia is added from the liquid ammonia inlet at the bottom of the second absorption tower 8 to maintain the alkalinity of the absorption liquid at the bottom of the tower.
以上所述仅为本发明的优选实施例而已，并不用于限制本发明，对于本领域的技术人员来说，本发明可以有各种更改和变化。凡在本发明的精神和原则之内，所作的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。The above descriptions are only preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and changes. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention shall be included in the protection scope of the present invention.
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