CN209778320U - A heat coupling system for pressurized deacidification and ammonia distillation - Google Patents
A heat coupling system for pressurized deacidification and ammonia distillation Download PDFInfo
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- CN209778320U CN209778320U CN201920189231.XU CN201920189231U CN209778320U CN 209778320 U CN209778320 U CN 209778320U CN 201920189231 U CN201920189231 U CN 201920189231U CN 209778320 U CN209778320 U CN 209778320U
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 276
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 136
- 238000004821 distillation Methods 0.000 title claims abstract description 84
- 238000010168 coupling process Methods 0.000 title claims abstract description 14
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 13
- 230000008878 coupling Effects 0.000 title claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 43
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 24
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 24
- 239000007791 liquid phase Substances 0.000 claims abstract description 22
- 239000002351 wastewater Substances 0.000 claims abstract description 22
- 239000002253 acid Substances 0.000 claims abstract description 7
- 239000003513 alkali Substances 0.000 claims abstract description 6
- 238000001704 evaporation Methods 0.000 claims abstract 8
- 230000008020 evaporation Effects 0.000 claims abstract 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000012856 packing Methods 0.000 claims description 6
- 230000003009 desulfurizing effect Effects 0.000 claims 1
- 238000003795 desorption Methods 0.000 abstract description 12
- 238000011084 recovery Methods 0.000 abstract description 4
- 230000009467 reduction Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 27
- 238000000034 method Methods 0.000 description 17
- 238000006477 desulfuration reaction Methods 0.000 description 16
- 230000023556 desulfurization Effects 0.000 description 16
- 230000008569 process Effects 0.000 description 15
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 7
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- 238000000605 extraction Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000003034 coal gas Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- AQGDXJQRVOCUQX-UHFFFAOYSA-N N.[S] Chemical compound N.[S] AQGDXJQRVOCUQX-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
Description
技术领域technical field
本实用新型涉及焦炉煤气净化技术领域，尤其涉及一种加压脱酸蒸氨热量耦合的系统。The utility model relates to the technical field of coke oven gas purification, in particular to a heat coupling system for pressurized deacidification and ammonia distillation.
背景技术Background technique
氨水法脱硫工艺是一种用于脱除荒煤气中硫化氢的常见工艺。该工艺以煤气中的氨为碱源，以含氨水溶液为洗涤介质，采用氨硫联合洗涤(吸收)工艺脱除煤气中的硫化氢。该法由洗涤装置和脱酸蒸氨装置组成了吸收和解吸的工艺主体，并使氨和硫化氢的洗涤和汽提解吸装置紧密结合在一起。吸收单元中，由脱酸蒸氨装置返回含氨较高的脱酸贫液和汽提水吸收荒煤气中的氨和硫化氢，形成含氨和硫化氢的富液，以达到脱除荒煤气中硫化氢的目的。解吸单元中，富液通过脱酸蒸氨装置解吸得到的脱酸贫液和汽提水(蒸氨废水的一部分)送回洗涤装置循环使用。Ammonia water desulfurization process is a common process for removing hydrogen sulfide in raw coal gas. The process uses the ammonia in the gas as the alkali source, uses the ammonia-containing aqueous solution as the washing medium, and adopts the ammonia-sulfur combined washing (absorption) process to remove the hydrogen sulfide in the gas. The main body of the absorption and desorption process is composed of a washing device and a deacidification and ammonia distillation device, and the washing and stripping desorption devices of ammonia and hydrogen sulfide are closely combined. In the absorption unit, the deacidification lean liquid with high ammonia content and the stripping water returned by the deacidification and ammonia distillation device absorb the ammonia and hydrogen sulfide in the raw coal gas, and form a rich liquid containing ammonia and hydrogen sulfide to achieve the removal of raw coal gas The purpose of hydrogen sulfide. In the desorption unit, the deacidified lean liquid and stripped water (a part of the ammonia distillation wastewater) obtained by desorption of the rich liquid through the deacidification and ammonia distillation device are sent back to the washing device for recycling.
氨法脱硫工艺相比于其它脱硫工艺，仅以水为洗涤介质、煤气中氨为碱源的吸收法脱硫，不产生脱硫废液，具有总体煤气净化流程短、投资低的优点。但是，现有工艺中解吸单元(脱酸蒸氨)将氨气和硫化氢一同解吸，解吸出的气体经氨分解后进行硫回收。此过程中，可以作为最终化学产品的氨被当成杂质直接分解，未能得到有效回收。同时，富液解吸过程能耗偏大、操作费用偏高。由于塔底需求热量大，通常采用蒸汽直接通入塔底的方式进行供热，这也导致了该工艺废水量偏大的缺点。Compared with other desulfurization processes, the ammonia desulfurization process only uses water as the washing medium and ammonia in the gas as the alkali source for absorption desulfurization, does not produce desulfurization waste liquid, and has the advantages of short overall gas purification process and low investment. However, in the existing process, the desorption unit (deacidification and ammonia distillation) desorbs ammonia and hydrogen sulfide together, and the desorbed gas undergoes sulfur recovery after decomposition of ammonia. In this process, ammonia, which can be used as the final chemical product, is directly decomposed as an impurity and cannot be effectively recovered. At the same time, the energy consumption and operating cost of the rich liquid desorption process are relatively high. Due to the large demand for heat at the bottom of the tower, steam is usually passed directly into the bottom of the tower for heat supply, which also leads to the disadvantage of a large amount of wastewater in the process.
目前配套氨水法脱硫过程的脱酸蒸氨，为有效回收氨产品并且增加贫液氨硫比可以采用加压脱酸蒸氨的工艺方法。通过提高富液解吸压力，分步解吸完成氨产品的回收的同时，提高贫液质量，增加脱硫效果。但是，该工艺仍然存在能耗高、操作费用高、废水量偏大的问题。At present, the deacidification and ammonia distillation supporting the ammonia water desulfurization process can adopt the process of pressurized deacidification and ammonia distillation in order to effectively recover ammonia products and increase the ammonia-sulfur ratio of lean liquid. By increasing the desorption pressure of the rich liquid, the recovery of the ammonia product is completed through step-by-step desorption, and at the same time, the quality of the lean liquid is improved and the desulfurization effect is increased. However, this process still has the problems of high energy consumption, high operating costs, and a large amount of wastewater.
发明内容Contents of the invention
本实用新型提供了一种加压脱酸蒸氨热量耦合的系统，在保证富液解吸压力能够实现分步解吸完成氨产品的回收的同时，进一步提高蒸氨塔塔顶压力，使蒸氨塔塔顶温度高于脱酸塔塔底温度，用蒸氨塔顶冷凝器的热量为脱酸塔塔底供热，通过合理的温度制度进行热量耦合，从而达到节能减排的目的。The utility model provides a heat-coupling system for pressurized deacidification and steaming of ammonia. While ensuring that the desorption pressure of the rich liquid can realize step-by-step desorption to complete the recovery of ammonia products, the pressure at the top of the ammonia distillation tower is further increased to make the ammonia distillation tower The temperature at the top of the tower is higher than the bottom temperature of the deacidification tower, and the heat from the top condenser of the ammonia distillation tower is used to supply heat to the bottom of the deacidification tower, and the heat coupling is carried out through a reasonable temperature system, so as to achieve the purpose of energy saving and emission reduction.
为了达到上述目的，本实用新型采用以下技术方案实现：In order to achieve the above object, the utility model adopts the following technical solutions to realize:
一种加压脱酸蒸氨热量耦合的系统，包括脱酸塔、蒸氨塔、泵、冷凝器、换热器、再沸器和阀门；所述脱酸塔的顶部设有酸气排出口，上部设混合液入口，中部设贫液侧线采出口，下部设蒸氨气体入口及气液相返回口，底部设氨水排出口；其中混合液入口连接换热器的第一换热介质出口，换热器的第一换热介质入口连接脱硫塔富液输送管道和剩余氨水输送管道；脱酸塔的贫液侧线出口与换热器的第二换热介质入口连接，换热器的第二换热介质出口连接贫液输送管道；所述蒸氨塔的顶部设蒸氨气体出口，上部设氨水入口及冷凝液入口，中部设碱液入口，底部设气液相入口及蒸氨废水出口；所述脱酸塔的氨水排出口和泵的入口连接，泵的出口分别连接蒸氨塔的氨水入口和冷凝器的第一换热介质入口，冷凝器的第一换热介质出口连接脱酸塔的气液相返回口；蒸氨塔的蒸氨气体出口通过一路管道与冷凝器的第二换热介质入口连接，通过另一路管道连接脱酸塔的蒸氨气体入口，且与蒸氨气体入口连接的管路上设阀门；冷凝器的第二换热介质出口连接氨气产品管道，冷凝器的冷凝液出口连接蒸氨塔的冷凝液入口；蒸氨塔的蒸氨废水出口与蒸氨废水管道连接，蒸氨废水管道通过分支管道与再沸器的入口连接，再沸器的出口与蒸氨塔的气液相入口连接，分支管道下游的蒸氨废水管道另外连接汽提水输送管道。A system for heat coupling of pressurized deacidification and ammonia distillation, including a deacidification tower, an ammonia distillation tower, a pump, a condenser, a heat exchanger, a reboiler and a valve; the top of the deacidification tower is provided with an acid gas outlet , the upper part is provided with a mixed liquid inlet, the middle part is provided with a lean liquid side line extraction outlet, the lower part is provided with an ammonia distilled gas inlet and a gas-liquid phase return port, and the bottom is provided with an ammonia water outlet; the mixed liquid inlet is connected to the first heat exchange medium outlet of the heat exchanger, The first heat exchange medium inlet of the heat exchanger is connected to the rich liquid delivery pipeline of the desulfurization tower and the remaining ammonia water delivery pipeline; the lean liquid side line outlet of the deacidification tower is connected to the second heat exchange medium inlet of the heat exchanger, and the second heat exchange medium inlet of the heat exchanger The outlet of the heat exchange medium is connected to the poor liquid delivery pipeline; the top of the ammonia distillation tower is provided with an ammonia distillation gas outlet, the upper part is provided with an ammonia water inlet and a condensate inlet, the middle part is provided with a lye inlet, and the bottom is provided with a gas-liquid phase inlet and an ammonia distillation waste water outlet; The ammonia water outlet of the deacidification tower is connected to the inlet of the pump, and the outlet of the pump is respectively connected to the ammonia water inlet of the ammonia distillation tower and the first heat exchange medium inlet of the condenser, and the first heat exchange medium outlet of the condenser is connected to the deacidification tower The gas-liquid phase return port of the ammonia distillation tower; the ammonia distillation gas outlet of the ammonia distillation tower is connected to the second heat exchange medium inlet of the condenser through a pipeline, and the ammonia distillation gas inlet of the deacidification tower is connected through another pipeline, and connected to the ammonia distillation gas inlet A valve is provided on the connected pipeline; the second heat exchange medium outlet of the condenser is connected to the ammonia gas product pipeline, and the condensate outlet of the condenser is connected to the condensate inlet of the ammonia distillation tower; the ammonia distillation wastewater outlet of the ammonia distillation tower is connected to the ammonia distillation wastewater pipeline Connection, the ammonia distillation wastewater pipeline is connected to the inlet of the reboiler through a branch pipeline, the outlet of the reboiler is connected to the gas-liquid phase inlet of the ammonia distillation tower, and the ammonia distillation wastewater pipeline downstream of the branch pipeline is additionally connected to the stripped water delivery pipeline.
所述脱酸塔在位于混合液入口与贫液侧线采出口之间、贫液侧线采出口与蒸氨气体入口之间的2段塔体内分别设置多层填料或塔盘。The deacidification tower is provided with multiple layers of packing or trays in the two-stage tower body located between the mixed liquid inlet and the lean liquid side-line extraction outlet, and between the lean liquid side-line extraction outlet and the ammonia distillation gas inlet.
所述蒸氨塔在位于氨水入口与碱液入口之间、碱液入口与气液相入口之间的2段塔体内分别设置多层填料或塔盘。In the ammonia distillation tower, multiple layers of packing or trays are respectively arranged in the two-stage tower bodies located between the ammonia water inlet and the lye inlet, and between the lye inlet and the gas-liquid phase inlet.
与现有技术相比，本实用新型的有益效果是：Compared with the prior art, the beneficial effects of the utility model are:
1)通过提高蒸氨塔塔顶压力，使得蒸氨塔塔顶温度高于脱酸塔塔底温度，在蒸氨塔冷凝器完成浓缩氨气的同时，还作为脱硫塔的再沸器对脱硫塔进行供热；1) By increasing the pressure at the top of the ammonia distillation tower, the temperature at the top of the ammonia distillation tower is higher than the bottom temperature of the deacidification tower. While the ammonia distillation tower condenser completes the concentration of ammonia, it also acts as a reboiler for the desulfurization tower to desulfurize tower for heating;
2)通过热量耦合的方式，降低系统蒸汽消耗，同时使蒸氨塔塔底再沸器所需面积减少；采用蒸汽间接加热的方式，降低废水排量。2) Through heat coupling, the steam consumption of the system is reduced, and at the same time, the area required for the reboiler at the bottom of the ammonia distillation tower is reduced; the indirect steam heating method is used to reduce the waste water discharge.
附图说明Description of drawings
图1是本实用新型所述加压脱酸蒸氨热量耦合的工艺的流程图。Fig. 1 is a flow chart of the heat-coupling process of pressurized deacidification and ammonia distillation described in the present invention.
图中：1.脱酸塔 11.酸气排出口 12.混合液入口 13.贫液侧线采出口 14.蒸氨气体入口 15.气液相返回口一 16.氨水排出口 2.蒸氨塔 21.蒸氨气体出口 22.氨水入口23.冷凝液入口 24.碱液入口 25.气液相入口 26.蒸氨废水出口 3.换热器 4.泵 5.冷凝器 6.再沸器 7.阀门In the figure: 1. Deacidification tower 11. Acid gas outlet 12. Mixed liquid inlet 13. Lean liquid side line extraction outlet 14. Ammonia distillation gas inlet 15. Gas-liquid phase return port 16. Ammonia water outlet 2. Ammonia distillation tower 21. Ammonia distillation gas outlet 22. Ammonia water inlet 23. Condensate inlet 24. Alkaline liquor inlet 25. Gas-liquid phase inlet 26. Ammonia distillation waste water outlet 3. Heat exchanger 4. Pump 5. Condenser 6. Reboiler 7 .valve
具体实施方式Detailed ways
下面结合附图对本实用新型的具体实施方式作进一步说明：The specific embodiment of the utility model will be further described below in conjunction with accompanying drawing:
如图1所示，本实用新型所述一种加压脱酸蒸氨热量耦合的系统，包括脱酸塔1、蒸氨塔2、泵4、冷凝器5、换热器3、再沸器6和阀门7；所述脱酸塔1的顶部设有酸气排出口11，上部设混合液入口12，中部设贫液侧线采出口13，下部设蒸氨气体入口14及气液相返回口15，底部设氨水排出口16；其中混合液入口12连接换热器3的第一换热介质出口，换热器3的第一换热介质入口连接脱硫塔富液输送管道和剩余氨水输送管道；脱酸塔1的贫液侧线出口13与换热器3的第二换热介质入口连接，换热器3的第二换热介质出口连接贫液输送管道；所述蒸氨塔2的顶部设蒸氨气体出口21，上部设氨水入口22及冷凝液入口23，中部设碱液入口24，底部设气液相入口25及蒸氨废水出口26；所述脱酸塔1的氨水排出口16和泵4的入口连接，泵4的出口分别连接蒸氨塔2的氨水入口22和冷凝器5的第一换热介质入口，冷凝器5的第一换热介质出口连接脱酸塔1的气液相返回口15；蒸氨塔2的蒸氨气体出口21通过一路管道与冷凝器5的第二换热介质入口连接，通过另一路管道连接脱酸塔1的蒸氨气体入口14，且与蒸氨气体入口14连接的管路上设阀门7；冷凝器5的第二换热介质出口连接氨气产品管道，冷凝器5的冷凝液出口连接蒸氨塔2的冷凝液入口23；蒸氨塔2的蒸氨废水出口26与蒸氨废水管道连接，蒸氨废水管道通过分支管道与再沸器6的入口连接，再沸器6的出口与蒸氨塔2的气液相入口25连接，分支管道下游的蒸氨废水管道另外连接汽提水输送管道。As shown in Figure 1, a pressurized deacidification and ammonia distillation heat coupling system described in the utility model includes a deacidification tower 1, an ammonia distillation tower 2, a pump 4, a condenser 5, a heat exchanger 3, and a reboiler 6 and valve 7; the top of the deacidification tower 1 is provided with an acid gas discharge port 11, the upper part is provided with a mixed liquid inlet 12, the middle part is provided with a lean liquid side line extraction outlet 13, and the lower part is provided with an ammonia distillation gas inlet 14 and a gas-liquid phase return port 15. An ammonia water outlet 16 is provided at the bottom; the mixed liquid inlet 12 is connected to the first heat exchange medium outlet of the heat exchanger 3, and the first heat exchange medium inlet of the heat exchanger 3 is connected to the desulfurization tower rich liquid delivery pipeline and the remaining ammonia water delivery pipeline The lean liquid side line outlet 13 of the deacidification tower 1 is connected with the second heat exchange medium inlet of the heat exchanger 3, and the second heat exchange medium outlet of the heat exchanger 3 is connected with the lean liquid delivery pipeline; the top of the ammonia distillation tower 2 Ammonia gas outlet 21 is established, ammonia inlet 22 and condensate inlet 23 are established in the top, lye inlet 24 is established in the middle, gas-liquid phase inlet 25 and ammonia wastewater outlet 26 are established in the bottom; ammonia outlet 16 of the deacidification tower 1 It is connected with the inlet of pump 4, and the outlet of pump 4 is respectively connected with the ammonia water inlet 22 of ammonia distillation tower 2 and the first heat exchange medium inlet of condenser 5, and the first heat exchange medium outlet of condenser 5 is connected with the gas of deacidification tower 1. The liquid phase return port 15; the ammonia distillation gas outlet 21 of the ammonia distillation tower 2 is connected with the second heat exchange medium inlet of the condenser 5 through one pipeline, and the ammonia distillation gas inlet 14 of the deacidification tower 1 is connected through another pipeline, and connected with A valve 7 is arranged on the pipeline connected to the ammonia gas inlet 14; the second heat exchange medium outlet of the condenser 5 is connected to the ammonia gas product pipeline, and the condensate outlet of the condenser 5 is connected to the condensate inlet 23 of the ammonia distillation tower 2; The ammonia distillation wastewater outlet 26 of 2 is connected with the ammonia distillation wastewater pipeline, and the ammonia distillation wastewater pipeline is connected with the inlet of the reboiler 6 through a branch pipeline, and the outlet of the reboiler 6 is connected with the gas-liquid phase inlet 25 of the ammonia distillation tower 2, and the branch The ammonia distillation wastewater pipeline downstream of the pipeline is additionally connected to the stripping water delivery pipeline.
所述脱酸塔1在位于混合液入口12与贫液侧线采出口13之间、贫液侧线采出口13与蒸氨气体入口14之间的2段塔体内分别设置多层填料或塔盘。The deacidification tower 1 is provided with multiple layers of packing or trays in the two-stage tower body located between the mixed liquid inlet 12 and the lean liquid side draw outlet 13, and between the lean liquid side draw outlet 13 and the ammonia distillation gas inlet 14.
所述蒸氨塔2在位于氨水入口22与碱液入口24之间、碱液入口24与气液相入口25之间的2段塔体内分别设置多层填料或塔盘。The ammonia distillation tower 2 is provided with multiple layers of packing or trays in the two-stage tower body between the ammonia water inlet 22 and the lye inlet 24, and between the lye inlet 24 and the gas-liquid phase inlet 25.
本实用新型所述一种加压脱酸蒸氨热量耦合的系统的工艺过程如下：The technical process of a system of pressurized deacidification and steam ammonia heat coupling described in the utility model is as follows:
1)由脱硫塔来的富液与剩余氨水混合，经换热器3与脱酸塔贫液换热后进入脱酸塔1顶部；脱酸塔1顶部通过加压操作抑制氨气逸出，使脱酸塔1塔顶酸气产品中仅含有少量氨气；1) The rich liquid from the desulfurization tower is mixed with the remaining ammonia water, and then enters the top of the deacidification tower 1 after heat exchange with the lean liquid of the deacidification tower by the heat exchanger 3; Only a small amount of ammonia is contained in the acid gas product at the top of the deacidification tower 1;
2)酸气由脱酸塔1顶部逸出，脱酸塔1侧线采出的贫液与脱硫塔富液及剩余氨水换热后，返回脱硫塔循环使用；2) The acid gas escapes from the top of the deacidification tower 1, and the lean liquid extracted from the side line of the deacidification tower 1 exchanges heat with the rich liquid of the desulfurization tower and the remaining ammonia water, and returns to the desulfurization tower for recycling;
3)蒸氨塔2顶部压力大于脱酸塔1底部压力，脱酸塔1塔底液相经过泵4增压后，一部分进入蒸氨塔2顶部进行蒸氨处理，另外一部分进入蒸氨塔2顶的冷凝器5进行加热，加热后的气液相返回脱酸塔1底部；3) The pressure at the top of ammonia distillation tower 2 is greater than the pressure at the bottom of deacidification tower 1. After the liquid phase at the bottom of deacidification tower 1 is pressurized by pump 4, part of it enters the top of ammonia distillation tower 2 for ammonia distillation treatment, and the other part enters ammonia distillation tower 2 The condenser 5 on the top is heated, and the gas-liquid phase after heating returns to the bottom of the deacidification tower 1;
4)蒸氨塔2顶部蒸氨气体逸出后一部分进入塔顶冷凝器5进行冷凝浓缩处理，另外一部分经过阀门7调节返回脱酸塔1底部作为脱酸塔1底部热源；4) Part of the ammonia distillation gas escapes from the top of the ammonia distillation tower 2 enters the top condenser 5 for condensation and concentration treatment, and the other part is regulated by the valve 7 and returned to the bottom of the deacidification tower 1 as a heat source at the bottom of the deacidification tower 1;
5)蒸氨塔2顶部蒸氨气体经冷凝器5浓缩后，气相逸出成为氨产品，液相返回蒸氨塔2作为回流；5) After the ammonia distillation gas at the top of the ammonia distillation tower 2 is concentrated by the condenser 5, the gas phase escapes to become an ammonia product, and the liquid phase returns to the ammonia distillation tower 2 as reflux;
6)蒸氨塔2中部加入碱液用于脱除固定氨，蒸氨塔2底部通过再沸器6提供热量，蒸氨塔2底部排出的蒸氨废水一部分返回脱硫工段用作脱硫洗氨的汽提水，同时对脱硫塔供热。6) Lye is added to the middle of the ammonia distillation tower 2 to remove fixed ammonia, the bottom of the ammonia distillation tower 2 is provided with heat through the reboiler 6, and part of the ammonia distillation waste water discharged from the bottom of the ammonia distillation tower 2 is returned to the desulfurization section for desulfurization and washing of ammonia. The water is stripped and heat is supplied to the desulfurization tower at the same time.
以上所述，仅为本实用新型较佳的具体实施方式，但本实用新型的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本实用新型揭露的技术范围内，根据本实用新型的技术方案及其实用新型构思加以等同替换或改变，都应涵盖在本实用新型的保护范围之内。The above is only a preferred embodiment of the utility model, but the scope of protection of the utility model is not limited thereto. The equivalent replacement or change of the new technical solution and the concept of the utility model shall be covered by the protection scope of the utility model.
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| WO2020164341A1 (en) * | 2019-02-11 | 2020-08-20 | 中冶焦耐(大连)工程技术有限公司 | Process and system for thermal coupling of pressurized deacidification and ammonia distillation |
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