CN109879510B - Method for recovering ammonia from high ammonia nitrogen wastewater - Google Patents
Method for recovering ammonia from high ammonia nitrogen wastewater Download PDFInfo
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- CN109879510B CN109879510B CN201910307337.XA CN201910307337A CN109879510B CN 109879510 B CN109879510 B CN 109879510B CN 201910307337 A CN201910307337 A CN 201910307337A CN 109879510 B CN109879510 B CN 109879510B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 57
- 239000002351 wastewater Substances 0.000 title claims abstract description 34
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 22
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 60
- 230000009615 deamination Effects 0.000 claims abstract description 31
- 238000006481 deamination reaction Methods 0.000 claims abstract description 31
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 30
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 30
- 238000003763 carbonization Methods 0.000 claims abstract description 19
- 239000011575 calcium Substances 0.000 claims abstract description 17
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims abstract description 16
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 claims abstract description 16
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 16
- 235000012538 ammonium bicarbonate Nutrition 0.000 claims abstract description 16
- 239000001099 ammonium carbonate Substances 0.000 claims abstract description 16
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 229910001425 magnesium ion Inorganic materials 0.000 claims abstract description 10
- 238000011084 recovery Methods 0.000 claims abstract description 10
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 9
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 5
- 239000012808 vapor phase Substances 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 239000002244 precipitate Substances 0.000 claims description 10
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 7
- 229910052791 calcium Inorganic materials 0.000 claims description 7
- 229910052749 magnesium Inorganic materials 0.000 claims description 7
- 239000011777 magnesium Substances 0.000 claims description 7
- 238000005261 decarburization Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims description 5
- 239000002912 waste gas Substances 0.000 claims description 5
- 239000013078 crystal Substances 0.000 claims description 4
- 239000000047 product Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims 1
- 238000005262 decarbonization Methods 0.000 abstract description 17
- 230000000694 effects Effects 0.000 abstract description 4
- 239000010865 sewage Substances 0.000 abstract description 2
- 238000004065 wastewater treatment Methods 0.000 abstract 1
- 238000002425 crystallisation Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000000149 chemical water pollutant Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
本发明公开了一种高氨氮废水氨回收方法，属于污水处理技术领域。该方法步骤为：首先，高氨氮废水通过通入含二氧化碳蒸汽和含氨蒸汽的脱碳塔，除去废水中的钙镁离子，然后通过脱氨塔，在80～90℃下汽提脱氨，废水中的氨氮进入汽相形成高浓度含氨混合蒸汽汇集于脱氨塔顶部，含氨混合蒸汽部分回流至脱碳塔，剩余部分引入冷凝器冷凝后进行气液分离，最后，脱氨塔出水进入后续处理设施进行生化处理，分离出的氨水进入通入含二氧化碳蒸汽的碳化塔形成碳酸氢铵作为回收利用的产品。采用本发明方法对高氨氮废水进行处理及氨回收可以大大提高其脱氨效果和氨回收效率，此外还能防止处理设备结垢。
The invention discloses a method for recovering ammonia from waste water with high ammonia nitrogen, and belongs to the technical field of sewage treatment. The steps of the method are as follows: firstly, the high-ammonia-nitrogen wastewater passes through a decarbonization tower containing steam containing carbon dioxide and ammonia-containing steam to remove calcium and magnesium ions in the waste water, and then passes through the deammonization tower for stripping and deamination at 80-90°C, The ammonia nitrogen in the wastewater enters the vapor phase to form a high-concentration ammonia-containing mixed steam and collects at the top of the deamination tower. Part of the ammonia-containing mixed steam flows back to the decarbonization tower, and the remaining part is introduced into the condenser to condense for gas-liquid separation. Enter the follow-up treatment facility for biochemical treatment, and the separated ammonia water enters the carbonization tower that is fed with carbon dioxide-containing steam to form ammonium bicarbonate as a recycled product. The method of the invention can greatly improve the deammonization effect and ammonia recovery efficiency of high ammonia nitrogen wastewater treatment and ammonia recovery, and can also prevent fouling of treatment equipment.
Description
技术领域technical field
本发明涉及一种高氨氮废水氨回收方法，属于污水处理技术领域。The invention relates to a method for recovering ammonia from waste water with high ammonia nitrogen, and belongs to the technical field of sewage treatment.
背景技术Background technique
目前随着城市人口的迅速增加和人民生活水平的不断提高，我国垃圾渗滤液和市政污泥消化液的产量也随着急剧增加。垃圾渗滤液和市政污泥硝化液中氨氮含量很高，同时总硬度也很高，这使得其较难处理；若不对氨回收，也会造成资源的浪费。At present, with the rapid increase of urban population and the continuous improvement of people's living standards, the output of landfill leachate and municipal sludge digestate in my country has also increased sharply. Landfill leachate and municipal sludge nitrification liquid contain high ammonia nitrogen content and high total hardness, which makes it difficult to handle; if ammonia is not recovered, it will also cause waste of resources.
目前对高氨氮废水进行处理的方法分为生物法和物化法两大类。生物法处理效率不够高，并且氨氮转化成氮气释放，未能资源化利用。物化法中多采用吹脱汽提法，但传统的吹脱汽提法存在脱氨效率低、塔内易结垢、能耗大、成本高等缺陷，国内外相关研究人员一直在寻找一种能提高脱氨效率并且解决塔内结垢等问题的新型高氨氮废水氨回收工艺。At present, the treatment methods of high ammonia nitrogen wastewater are divided into two categories: biological method and physical and chemical method. The efficiency of biological treatment is not high enough, and ammonia nitrogen is converted into nitrogen and released, so it cannot be utilized as a resource. Stripping and stripping are often used in physical and chemical methods, but the traditional stripping and stripping methods have defects such as low ammonia removal efficiency, easy fouling in the tower, high energy consumption, and high cost. Relevant researchers at home and abroad have been looking for an energy A new type of high ammonia nitrogen wastewater ammonia recovery process that improves the efficiency of ammonia removal and solves the problems of fouling in the tower.
发明内容Contents of the invention
针对现有技术中的问题，本发明提供一种高氨氮废水氨回收方法，采用该方法对高氨氮废水进行处理及氨回收可以大大提高其脱氨效果和氨回收效率，此外还能防止处理设备结垢。Aiming at the problems in the prior art, the present invention provides a method for recovering ammonia from high-ammonia-nitrogen wastewater. Using this method to treat and recover ammonia from high-ammonia-nitrogen wastewater can greatly improve its deamination effect and ammonia recovery efficiency. In addition, it can also prevent treatment equipment from Fouling.
为实现以上技术目的，本发明的技术方案是：For realizing above technical purpose, technical scheme of the present invention is:
一种高氨氮废水氨回收方法，步骤为：A method for recovering ammonia from waste water with high ammonia nitrogen, the steps are:
(1)高氨氮废水经预热器预热后泵送至脱碳塔上部，从脱碳塔下部通入含二氧化碳蒸汽和含氨蒸汽，含氨蒸汽包括从脱氨塔回流的含氨蒸汽，废水中的钙镁离子与氨气和二氧化碳反应生成钙镁沉淀物，生成的沉淀物沉淀于脱碳塔底部的储存槽中，通过更换储存槽将钙镁沉淀物排出脱碳塔；(1) High ammonia nitrogen wastewater is preheated by the preheater and pumped to the upper part of the decarbonization tower, and the carbon dioxide-containing steam and ammonia-containing steam are introduced from the lower part of the decarbonization tower. The calcium and magnesium ions in the wastewater react with ammonia and carbon dioxide to form calcium and magnesium precipitates, which are deposited in the storage tank at the bottom of the decarbonization tower, and the calcium and magnesium precipitates are discharged from the decarbonization tower by replacing the storage tank;
(2)脱碳塔出水泵送至脱氨塔上部，从脱氨塔底部通入含二氧化碳的蒸汽，通过负压装置控制脱氨塔为负压状态，在80～90℃下汽提脱氨，废水中的氨氮进入汽相，形成高浓度含氨混合蒸汽汇集于脱氨塔顶部，脱氨塔顶部的含氨混合蒸汽部分回流至脱碳塔，剩余部分引入冷凝器冷凝后进行气液分离，分离出的氨水进入碳化塔；脱氨塔出水进入后续处理设施进行生化处理；(2) The effluent of the decarbonization tower is pumped to the upper part of the deamination tower, and the steam containing carbon dioxide is introduced from the bottom of the deamination tower, and the deamination tower is controlled to be in a negative pressure state through a negative pressure device, and the deamination is stripped at 80-90°C , the ammonia nitrogen in the wastewater enters the vapor phase to form a high-concentration ammonia-containing mixed steam and collects at the top of the deammonization tower. The ammonia-containing mixed steam at the top of the deammonization tower is partially refluxed to the decarbonization tower, and the remaining part is introduced into the condenser for condensation and gas-liquid separation , the separated ammonia enters the carbonization tower; the effluent of the deammonization tower enters the follow-up treatment facility for biochemical treatment;
(3)从碳化塔底部通入含二氧化碳的蒸汽，使二氧化碳与氨水发生反应生成碳酸氢铵，通过设置旁路冷却系统降低碳化塔内液体的温度，使溶解在水中的碳酸氢铵逐渐结晶析出形成碳酸氢铵结晶混合液，碳酸氢铵结晶混合液经离心脱水后得碳酸氢铵产品。(3) Pass carbon dioxide-containing steam from the bottom of the carbonization tower to make carbon dioxide react with ammonia water to generate ammonium bicarbonate. By setting up a bypass cooling system to reduce the temperature of the liquid in the carbonization tower, the ammonium bicarbonate dissolved in water is gradually crystallized. The ammonium bicarbonate crystallization mixed solution is formed, and the ammonium bicarbonate crystallization mixed solution is centrifuged and dehydrated to obtain the ammonium bicarbonate product.
优选地，步骤(1)中所述含二氧化碳蒸汽和含氨蒸汽中二氧化碳与氨气的物质的量比为1:1。Preferably, the substance ratio of carbon dioxide and ammonia in the carbon dioxide-containing steam and ammonia-containing steam in step (1) is 1:1.
优选地，步骤(1)中所述含氨蒸汽还包括从碳化塔回流的部分废气。Preferably, the ammonia-containing steam in step (1) also includes part of the waste gas refluxed from the carbonization tower.
优选地，脱碳塔顶部的气体进入碳化塔底部。Preferably, gas from the top of the decarburization tower enters the bottom of the carbonization tower.
优选地，步骤(2)中脱氨塔出水泵送至预热器进行热量回收后再进深冷器，进一步冷却后排入脱氨出水池，再进入后续处理设施进行生化处理。Preferably, in step (2), the effluent from the deammonization tower is pumped to the preheater for heat recovery, and then enters the cryocooler. After further cooling, it is discharged into the deammonization effluent pool, and then enters the subsequent treatment facility for biochemical treatment.
从以上描述可以看出，本发明具备以下优点：As can be seen from the above description, the present invention has the following advantages:
(1)本发明通过向脱碳塔通入含二氧化碳的蒸汽和从脱氨塔回流的含氨蒸汽，通过二氧化碳和氨气在体系中协同反应产生碳酸根离子，可以在尽可能不破坏废水碱度的情况下与废水中的钙镁离子反应产生碳酸钙和碳酸镁沉淀(Ca2++CO2+2NH3+H2O—>CaCO3+2NH4 +)，此外，二氧化碳和氨气1:1通入能促进沉淀反应正向进行的限度，使钙镁离子的沉淀更加完全。(1) The present invention passes carbon dioxide-containing steam to the decarburization tower and the ammonia-containing steam backflowed from the deammonization tower, and produces carbonate ions through the synergistic reaction of carbon dioxide and ammonia in the system, so as not to destroy the waste water alkali as much as possible. In the case of high temperature, it reacts with calcium and magnesium ions in wastewater to produce calcium carbonate and magnesium carbonate precipitation (Ca 2+ +CO 2 +2NH 3 +H 2 O—>CaCO 3 +2NH 4 + ), in addition, carbon dioxide and ammonia 1 : 1 The limit that can promote the forward progress of the precipitation reaction is introduced, so that the precipitation of calcium and magnesium ions is more complete.
(2)本发明通过在脱碳塔底部附加一节可便携拆卸更换的储存槽，可以诱导钙镁离子在储存槽上沉淀，而且定期更换储存槽可以将钙镁沉淀物排出，从而可以防止钙镁离子在脱碳塔内沉淀结垢。(2) The present invention can induce calcium and magnesium ions to precipitate on the storage tank by attaching a portable, removable and replaceable storage tank at the bottom of the decarburization tower, and regular replacement of the storage tank can discharge the calcium and magnesium precipitates, thereby preventing calcium and magnesium ions from being deposited on the storage tank. Magnesium ions precipitate and scale in the decarburization tower.
(3)本发明通过负压装置控制脱氨塔为负压状态，并向脱氨塔通入含有二氧化碳的蒸汽，在高温(80～90度)下汽提脱氨，废水中的游离氨进入汽相形成高浓度的含氨蒸汽汇集在脱氨塔顶部，其中，负压和高温使得废水中氨的溶解度大大下降，游离态的氨占比大幅度提高，可以大大提高脱氨塔的脱氨效率和脱氨效果，提高氨回收效率，此外，蒸汽中的二氧化碳不仅可以与废水中的碳酸根离子反应(CO2+CO3 2-+H2O—>2HCO3 -)以防止废水中剩余的钙镁离子在脱氨塔内沉淀结垢，而且还可以抑制废水中的碳酸氢根离子在高温下发生的分解反应，以尽可能不破坏废水的碱度，满足脱氨塔需要。(3) The present invention controls the deamination tower to be in a negative pressure state through a negative pressure device, and feeds steam containing carbon dioxide into the deamination tower, stripping and deamination at a high temperature (80-90 degrees), and the free ammonia in the waste water enters The vapor phase forms high-concentration ammonia-containing steam and collects at the top of the deamination tower. The negative pressure and high temperature greatly reduce the solubility of ammonia in the wastewater, and the proportion of free ammonia is greatly increased, which can greatly improve the deamination efficiency of the deamination tower. and deamination effect, improve the efficiency of ammonia recovery, in addition, the carbon dioxide in the steam can not only react with the carbonate ion in the wastewater (CO 2 +CO 3 2- +H 2 O—>2HCO 3 - ) to prevent the remaining Calcium and magnesium ions precipitate and scale in the deamination tower, and can also inhibit the decomposition reaction of bicarbonate ions in the wastewater at high temperature, so as not to destroy the alkalinity of the wastewater as much as possible to meet the needs of the deamination tower.
(4)本发明通过将脱氨塔出水泵送至预热器进行热量回收后再进行后续处理，可以节约能源，通过将碳化塔排出的废气部分回流至脱碳塔进行再利用可以减少要处理的碳化塔排出废气量，降低处理成本。(4) In the present invention, energy can be saved by pumping the effluent from the deamination tower to the preheater for heat recovery before subsequent treatment, and by returning the waste gas discharged from the carbonization tower to the decarbonization tower for reuse, it can reduce the need for treatment The amount of exhaust gas discharged from the carbonization tower reduces the treatment cost.
(5)本发明方法操作过程中无需投加任何污染环境的化学药剂，绿色环保。(5) During the operation of the method of the present invention, there is no need to add any chemical agents that pollute the environment, which is environmentally friendly.
附图说明Description of drawings
图1是本发明方法的流程示意图；Fig. 1 is a schematic flow sheet of the inventive method;
具体实施方式Detailed ways
结合图1，详细说明本发明的一个具体实施例，但不对本发明的权利要求做任何限定。A specific embodiment of the present invention will be described in detail with reference to FIG. 1 , but the claims of the present invention are not limited in any way.
如图1所示，一种高氨氮废水氨回收方法，步骤为：As shown in Figure 1, a kind of high ammonia nitrogen wastewater ammonia recovery method, the steps are:
(1)高氨氮废水经预热器预热后泵送至脱碳塔上部，从脱碳塔下部通入含二氧化碳蒸汽和含氨蒸汽，其中，含二氧化碳蒸汽和含氨蒸汽中二氧化碳与氨气的物质的量比为1:1，含氨蒸汽包括从脱氨塔回流的含氨蒸汽和从碳化塔回流的部分废气，脱碳塔为板式塔，脱碳塔温度为25～45℃，废水流经塔板的过程中与通入的混合蒸汽充分接触并进行热交换，废水中的钙镁离子与氨气和二氧化碳反应生成钙镁沉淀物，生成的沉淀物沉淀于脱碳塔底部的储存槽中，通过更换储存槽将钙镁沉淀物排出脱碳塔；脱碳塔顶部的气体(主要是含二氧化碳的蒸汽)经管道从碳化塔底部进入碳化塔内，其中，脱碳塔顶部的气体也可直接作为废气经处理后排出；脱碳塔出水泵送至脱氨塔上部；(1) High ammonia nitrogen wastewater is preheated by the preheater and pumped to the upper part of the decarbonization tower, and the carbon dioxide-containing steam and ammonia-containing steam are introduced from the lower part of the decarbonization tower, wherein the carbon dioxide and ammonia in the carbon dioxide-containing steam and ammonia-containing steam The amount ratio of the substance is 1:1. The ammonia-containing steam includes the ammonia-containing steam refluxed from the deammonization tower and part of the waste gas refluxed from the carbonization tower. The decarbonization tower is a plate tower. During the process of flowing through the tray, it is in full contact with the mixed steam and performs heat exchange. The calcium and magnesium ions in the wastewater react with ammonia and carbon dioxide to form calcium and magnesium precipitates, which are deposited in the storage at the bottom of the decarbonization tower. In the tank, the calcium and magnesium precipitates are discharged from the decarbonization tower by replacing the storage tank; the gas at the top of the decarbonization tower (mainly steam containing carbon dioxide) enters the carbonization tower from the bottom of the carbonization tower through the pipeline, and the gas at the top of the decarbonization tower It can also be directly discharged as waste gas after treatment; the effluent from the decarbonization tower is pumped to the upper part of the deamination tower;
(2)从脱氨塔底部通入含二氧化碳的蒸汽，通过负压装置控制脱氨塔为负压状态，在80～90℃下汽提脱氨，废水中的氨氮进入汽相，形成高浓度含氨混合蒸汽汇集于脱氨塔顶部，脱氨塔顶部的含氨混合蒸汽(二氧化碳、氨气和蒸汽)部分回流至脱碳塔，剩余部分引入冷凝器冷凝后进行气液分离，分离出的氨水进入碳化塔；脱氨塔出水送至预热器进行热量回收后再进深冷器，进一步冷却后排入脱氨出水池，再进入后续处理设施进行生化处理；(2) The steam containing carbon dioxide is introduced from the bottom of the deamination tower, and the deamination tower is controlled by a negative pressure device to be in a negative pressure state. The ammonia nitrogen in the wastewater enters the vapor phase and forms a high concentration at 80-90°C. The ammonia-containing mixed steam is collected at the top of the deammonization tower, and part of the ammonia-containing mixed steam (carbon dioxide, ammonia and steam) at the top of the deammonization tower is refluxed to the decarburization tower, and the remaining part is introduced into the condenser to condense for gas-liquid separation, and the separated Ammonia water enters the carbonization tower; the effluent from the deamination tower is sent to the preheater for heat recovery, then enters the cryocooler, and after further cooling, it is discharged into the deamination effluent pool, and then enters the subsequent treatment facilities for biochemical treatment;
(3)从碳化塔底部通入含二氧化碳的蒸汽，使二氧化碳与氨水发生反应生成碳酸氢铵，通过设置旁路冷却系统降低碳化塔内液体的温度，使溶解在水中的碳酸氢铵逐渐结晶析出形成碳酸氢铵结晶混合液，将碳酸氢铵结晶混合液泵送至晶浆罐，晶浆罐混合液经离心机离心脱水后得到粉末状碳酸氢铵产品，脱水滤液进入母液池收集后入回收塔然后返回碳化塔再利用。(3) Pass carbon dioxide-containing steam from the bottom of the carbonization tower to make carbon dioxide react with ammonia water to generate ammonium bicarbonate. By setting up a bypass cooling system to reduce the temperature of the liquid in the carbonization tower, the ammonium bicarbonate dissolved in water is gradually crystallized. The ammonium bicarbonate crystallization mixture is formed, and the ammonium bicarbonate crystallization mixture is pumped to the crystal slurry tank, and the crystal slurry tank mixture is centrifuged and dehydrated by a centrifuge to obtain a powdered ammonium bicarbonate product, and the dehydration filtrate is collected in the mother liquor pool and then recycled The tower is then returned to the carbonization tower for reuse.
可以理解的是，以上关于本发明的具体描述，仅用于说明本发明而并非受限于本发明实施例所描述的技术方案。本领域的普通技术人员应当理解，仍然可以对本发明进行修改或等同替换，以达到相同的技术效果；只要满足使用需要，都在本发明的保护范围之内。It can be understood that the above specific descriptions of the present invention are only used to illustrate the present invention and are not limited to the technical solutions described in the embodiments of the present invention. Those of ordinary skill in the art should understand that the present invention can still be modified or equivalently replaced to achieve the same technical effect; as long as the use requirements are met, all are within the protection scope of the present invention.
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