Acetylene slag cement denitration ammonia escape control and utilization system

Abstract

The invention belongs to the technical field of cement kiln flue gas treatment, and particularly relates to a carbide slag cement denitration ammonia escape control and utilization system, and a modification method of the carbide slag cement denitration ammonia escape control and utilization system comprises the following steps: changing a drying crusher into an indirect dryer, indirectly exchanging heat between flue gas at an outlet of a preheater and carbide slag, and drying the flue gas at an outlet of the indirect dryer; a waste gas outlet of the indirect dryer is connected with an inlet of the ammonia gas absorption device, and an outlet of the ammonia gas absorption device is communicated with a drying medium outlet of the indirect dryer. The invention provides a carbide slag cement denitration ammonia escape control and utilization system.

Description

Technical Field

[0001] This invention belongs to the field of cement kiln flue gas treatment technology, and in particular relates to a system for controlling and utilizing ammonia escape from denitrification in carbide slag cement. Background Technology

[0002] Nitrogen oxides (NOx) are an inevitable pollutant emitted during cement production, causing immeasurable pollution to the environment and human health. Ammonia-based denitrification technology is a commonly used method in cement kilns, encompassing SNCR and SCR technologies. Both technologies operate on the principle of reacting ammonia with NOx in flue gas to produce nitrogen and water under suitable reaction conditions. However, in actual operation, denitrification systems are prone to issues such as uneven mixing of flue gas and ammonia, and significant delays in the control of the ammonia injection system, leading to excessive ammonia escape. To ensure that NOx emissions from the chimney meet standards, the denitrification control system typically uses the NOx concentration at the chimney as the control quantity, while the ammonia injection point is set within a suitable temperature range. This time lag between the two points causes the automatic control system to fail to accurately and promptly control the ammonia injection amount in response to changes in background NOx levels, resulting in fluctuations in NOx emission concentrations and even exceeding standards. To mitigate the risk of excessive NOx emissions, the margin for ammonia water usage is often increased, which further increases ammonia escape concentration and causes secondary pollution.

[0003] Compared to traditional limestone cement plants, carbide slag cement plants have a higher risk of excessive ammonia escape during their production process. The reasons are as follows: Carbide slag cement plants utilize kiln tail gas to dry and crush raw materials—carbide slag. Carbide slag originates from the waste residue after acetylene gas is obtained through the hydrolysis of calcium carbide. During the drying and crushing process, ammonia gas is released, increasing the amount of ammonia escape from the chimney. Tests have shown that ammonia escape from the carbide slag drying process is tens to hundreds of times greater than that from the denitrification system. Therefore, carbide slag cement plants need to pay closer attention to the management of ammonia generated during the carbide slag drying process.

[0004] A patent (CN118594214A) discloses a control system and method for ammonia escape emission in denitrification. The method includes: processing system operating data to obtain denoised operating data; filling in the denoised operating data to obtain a system operating dataset; processing the operating dataset using a concentration prediction model to obtain a concentration prediction output value; processing the flue gas denitrification dataset using a deviation prediction model to obtain a deviation output value; obtaining a corrected nitrogen oxide concentration and the required ammonia injection amount based on the concentration prediction output value and the deviation output value; collecting ammonia escape concentration and second nitrogen oxide concentration using a monitoring device; determining the first reactant requirement based on the second nitrogen oxide concentration and nitrogen oxide emission limits; and determining the second reactant requirement based on the ammonia concentration and ammonia escape standard limits. This method achieves ammonia escape emission control, reduces ammonia escape and air pollution, and improves the stability and safety of the denitrification system. A patented ammonia slip control device for a denitrification system (CN211928434U) includes an ammonia slip detection device and a control device. The ammonia slip detection device is fixed at the outlet of the denitrification system, and its ammonia slip output terminal is electrically connected to the ammonia slip input terminal of the control device. It also includes a slow-release adsorbent injection device, which is fixed at the inlet of the denitrification system. This slow-release adsorbent injection device includes a flow regulating solenoid valve and a nozzle. The outlet of the flow regulating solenoid valve is connected to the inlet of the nozzle via a pipeline. The inlet of the flow regulating solenoid valve is connected to the outlet of a slow-release adsorbent storage device, which stores nano-slow-release adsorbent. The outlet of the nozzle faces the interior of the denitrification system's inlet flue.

[0005] The patent CN117065570A discloses a method and system for controlling ammonia injection in denitrification based on accurate measurement of ammonia slip. The method includes the following steps: dividing the SCR inlet flue into ammonia injection control zones and dividing the SCR outlet flue into the same number of sampling zones; setting judgment conditions; and if the judgment conditions are met, adjusting the ammonia slip concentration deviation or NO concentration at the SCR outlet. x The concentration deviation determines whether ammonia injection adjustment is needed; otherwise, the sampling area and catalyst are purged or the flue gas temperature is increased.

[0006] However, the aforementioned documents and patents have a series of problems and shortcomings: 1. The aforementioned literature and patents are all aimed at ammonia denitrification systems, with the goal of improving ammonia utilization and reducing ineffective ammonia injection. However, the main ammonia emissions from carbide slag cement plants come from the ammonia in the raw materials. The aforementioned literature and patents cannot solve the problem of ammonia in the raw materials, are not suitable for the production process of carbide slag cement, and cannot solve the problem of ammonia escape from carbide slag cement plants.

[0007] 2. The existing method of adding solid ammonia adsorbent has three problems: ① The problem of low gas-solid adsorption efficiency, limited adsorption time, and ineffective utilization of the adsorbent's adsorption capacity; ② If the solid adsorbent is to be recovered separately, separate dust collectors and other equipment are required, and the disposal of the solid adsorbent that has adsorbed ammonia also becomes a new problem; ③ If the solid adsorbent is not recovered separately, it will be returned to the production system along with the kiln ash and released again. Circulating in the production system does not solve the problem. If the kiln ash is not returned to the production system, it will result in waste of the kiln ash. The same problem of disposing of ammonia-containing kiln ash also exists.

[0008] 3. The raw material for carbide slag comes from the upstream chlor-alkali plant. Affected by the production of the chlor-alkali plant and the filter press plant, the output of carbide slag fluctuates. Therefore, the amount of ammonia gas dried by the drying and crushing machine also varies. As a result, the ammonia concentration in the flue gas fluctuates greatly, and the above solution cannot adapt to the problem of fluctuating ammonia release from carbide slag. Summary of the Invention

[0009] The purpose of this application is to provide a system for controlling and utilizing ammonia escape from denitrification in carbide slag cement, in order to solve the technical problems in the prior art.

[0010] The technical solution adopted in this application embodiment to solve the technical problems existing in the prior art is as follows: A method for modifying a calcium carbide slag cement denitrification ammonia escape control and utilization system, the method comprising the following steps: The dryer and crusher is replaced with an indirect dryer, in which the flue gas at the outlet of the preheater exchanges heat indirectly with the carbide slag, the exhaust gas outlet of the indirect dryer is connected to the inlet of the ammonia absorption device, and the outlet of the ammonia absorption device is connected to the drying medium outlet of the indirect dryer.

[0011] The embodiments of this application may also employ the following technical solutions: In the above-mentioned modification method of the denitrification ammonia escape control and utilization system of carbide slag cement, the ammonia absorption device further includes an absorption liquid tank and a condensation absorption tower. The absorption liquid tank is connected to the top of the condensation absorption tower through a circulating pump, the bottom of the condensation absorption tower is connected to an ammonia blower, and the ammonia blower is connected to the exhaust gas outlet of the indirect dryer.

[0012] In the above-mentioned modification method of the denitrification ammonia escape control and utilization system for carbide slag cement, the top of the condensation absorption tower is further connected to the drying medium outlet of the indirect dryer through a pipeline, and a flue gas analyzer is installed on the pipeline.

[0013] In the above-mentioned modification method for the denitrification and ammonia escape control and utilization system of carbide slag cement, the bottom of the condensation absorption tower is further connected to the absorption liquid pool.

[0014] A system for controlling and utilizing ammonia escape in denitrification of carbide slag cement, wherein the system is modified by any of the above-mentioned modification methods for the system for controlling and utilizing ammonia escape in denitrification of carbide slag cement.

[0015] In the aforementioned denitrification and ammonia escape control and utilization system for carbide slag cement, further, the drying medium inlet of the indirect dryer is connected to the primary cyclone separator, the drying medium outlet of the indirect dryer is connected to the tail dust collector via a high-temperature fan, the outlet of the ammonia absorption device is connected to the tail dust collector, so that the mixed gas exiting the ammonia absorption device is mixed with the flue gas exiting the preheater after indirect heat exchange for dust removal, and the discharge port of the indirect dryer is connected to the carbide slag dry powder silo.

[0016] In the aforementioned denitrification and ammonia escape control and utilization system for carbide slag cement, the exhaust outlet of the indirect dryer is connected to the inlet of the cyclone dust collector, the outlet of the cyclone dust collector is connected to the inlet of the ammonia absorption device, and the discharge port of the cyclone dust collector is connected to the dry powder silo of carbide slag.

[0017] A process for controlling and utilizing ammonia escape in denitrification of calcium carbide slag cement, wherein the process employs the aforementioned calcium carbide slag cement denitrification ammonia escape control and utilization system.

[0018] In the above-mentioned process for controlling and utilizing ammonia escape in denitrification of calcium carbide slag cement, the process further includes the following steps: The calcium carbide slag and the flue gas at the preheater outlet exchange heat indirectly, and the calcium carbide slag and the flue gas at the preheater outlet do not come into contact. The mixed gas containing water vapor and ammonia produced by carbide slag enters the ammonia absorption device, and the mixed gas exiting the ammonia absorption device is mixed with the flue gas from the preheater outlet after indirect heat exchange.

[0019] In the above-mentioned process for controlling and utilizing ammonia escape in denitrification of carbide slag cement, the ammonia absorption device further adopts the absorption liquid circulation to absorb ammonia in the mixed gas. The absorption liquid is one or more of hydrochloric acid, sulfuric acid, and nitric acid. When the pH value of the absorption liquid reaches 6.5~7, the absorption liquid is saturated and the absorption liquid is replaced.

[0020] One or more technical solutions provided in the embodiments of this application have at least the following beneficial effects: 1. In this invention, the flue gas does not come into contact with carbide slag, and the ammonia gas is absorbed first and then mixed with the flue gas, which reduces the amount of ammonia escape into the flue gas system from the source, which is conducive to reducing the ammonia escape concentration in the chimney and meets environmental protection standards.

[0021] 2. The main source of ammonia escape in carbide slag cement plants is the drying of carbide slag. The liquid absorption method is highly efficient and greatly reduces the amplitude of ammonia entering the production flue gas system, which helps to reduce the fluctuation range of ammonia escape concentration in the chimney.

[0022] 3. This invention adopts indirect operation, so the water vapor and ammonia generated during drying do not mix with the drying flue gas and are not diluted by the drying flue gas. The concentration of pollutants (ammonia) is high and the amount of flue gas to be treated is small, which reduces the difficulty of treatment and equipment specifications. There is no secondary pollution, no waste ammonia-containing adsorbent is generated, no kiln ash is wasted, and the construction and operation costs are low.

[0023] 4. This invention reduces ammonia escape into the flue gas system at the source, while also turning waste ammonia into a resource, utilizing the ammonia from the carbide slag cement plant, thus generating certain economic benefits.

[0024] 5. Traditional calcium carbide slag drying and crushing systems use direct drying, where dry calcium carbide slag powder flows with the drying flue gas and is collected by a calcium carbide slag cyclone separator, then temporarily stored in a calcium carbide slag powder silo. In contrast, indirect drying generates less waste gas, and the dry calcium carbide slag powder does not flow with the flue gas, allowing it to be directly transported to the calcium carbide slag powder silo. This eliminates the need for large-scale calcium carbide slag cyclones suitable for high air volumes and high dust concentrations, reducing equipment investment. Attached Figure Description

[0025] The technical solutions of the embodiments of this application will be further described in detail below with reference to the accompanying drawings. However, it should be understood that these drawings are designed for illustrative purposes only and are not intended to limit the scope of this application. In addition, unless otherwise specified, these drawings are only intended to conceptually illustrate the structural construction described herein and are not necessarily drawn to scale.

[0026] Figure 1 This is a common process for producing cement using calcium carbide slag. Figure 2 This is a schematic diagram of the denitrification ammonia escape control system for carbide slag cement in Example 1; Figure 3 This is a schematic diagram of the denitrification ammonia escape control system for carbide slag cement in Example 3.

[0027] In the picture: 1. Primary cyclone separator; 2. Preheater outlet flue gas; 3. Dehydrated carbide slag; 4. Drying crusher; 5. Carbide slag cyclone separator; 6. Carbide slag dry powder silo; 7. High-temperature fan; 8. Tail exhaust dust collector; 9. Tail exhaust fan; 10. Chimney; 11. Rotary indirect dryer; 12. Ammonia blower; 13. Condensation absorption tower; 14. Absorption liquid tank; 15. Circulating pump; 16. Flue gas analyzer; 17. Cyclone dust collector. Detailed Implementation

[0028] To better understand the above technical solutions, the following will provide a detailed explanation of the technical solutions in conjunction with the accompanying drawings and specific implementation methods.

[0029] Example 1 As per the instruction manual Figure 1 As shown, existing calcium carbide slag cement production plants use a drying crusher 4 to dry calcium carbide slag 3 from the chlor-alkali workshop. The preheater outlet flue gas 2 from the primary preheater 1 and the calcium carbide slag 3 from the chlor-alkali workshop flow concurrently into the drying crusher 4, where they mix and transfer heat. The moisture content of the calcium carbide slag is reduced from 30%~35% to approximately 1%. After heat exchange, the dry calcium carbide slag powder is transported with the flue gas to a calcium carbide slag cyclone dust collector 5 for collection and then temporarily stored in a calcium carbide slag silo 6. The flue gas is then sent to a tail exhaust dust collector 8 for dust collection by a high-temperature fan 7 and a tail exhaust fan 9 before being discharged through a chimney 10. During the drying process in the drying crusher 4, a large amount of water vapor and ammonia from the calcium carbide slag mix and enter the flue gas, flowing with the flue gas and ultimately being discharged into the atmosphere.

[0030] This embodiment involves the modification of an existing carbide slag cement production plant. (See attached instruction manual.) Figure 2 As shown, the direct heat exchange drying crusher 4 is replaced with an indirect heat exchange drying machine. In this embodiment, the indirect drying machine can be a rotary indirect drying machine 11. In the rotary indirect drying machine 11, the high-temperature preheater outlet flue gas and the material being dried do not come into contact with each other. Preferably, the dehydrated carbide slag 3 and the high-temperature preheater outlet flue gas 2 in the rotary indirect drying machine 11 flow in opposite directions. The included angle of the rotary kiln in the rotary indirect drying machine 11 should be 3~6°. Components such as fins can be added inside the rotary indirect drying machine 11 to increase heat exchange efficiency and promote the turning of the material (dehydrated carbide slag).

[0031] This embodiment also includes an ammonia absorption device. The mixed gas containing water vapor and ammonia generated from carbide slag enters the ammonia absorption device, and the mixed gas is high-humidity, high-ammonia flue gas. The condensation absorption tower 13 of the ammonia absorption device is the place where the high-humidity, high-ammonia flue gas is condensed and ammonia is absorbed. Preferably, the absorbent and the high-humidity, high-ammonia flue gas in the condensation absorption tower 13 operate in a countercurrent manner. Packing is provided to increase absorption efficiency, and a demister is installed at the top of the condensation absorption tower. The operating temperature is controlled below 70°C.

[0032] The absorbent in the condensation absorption tower 13 can be one or more of hydrochloric acid, sulfuric acid, and nitric acid.

[0033] Furthermore, in this embodiment, the absorbent is circulated using a circulating pump. A pH testing device and an absorbent discharge pipe are installed in the absorbent tank 14. When the pH value of the absorbent reaches 6.5-7, it is considered saturated. The saturated absorbent is then discharged and new absorbent is injected. The saturated absorbent is then concentrated to produce fertilizer.

[0034] After passing through the ammonia absorption device, the mixed gas is mixed with the flue gas from the preheater outlet after passing through the flue gas analyzer 16. The flue gas analyzer 16 tests for ammonia and oxygen. The circulation pump 15 is a variable frequency pump. Under the control of the flue gas analyzer 16 test results and the control system, the circulation flow rate is changed to ensure that the ammonia concentration at the outlet of the condensation absorption tower 13 reaches the set value.

[0035] Example 2 This embodiment includes the following steps: the high-temperature preheater outlet flue gas 2 from the primary cyclone 1 exchanges heat with the dehydrated carbide slag 3 from the upstream chlor-alkali workshop in a rotary indirect dryer 11. After heat utilization, the preheater outlet flue gas 2 enters the tail exhaust dust collector 8 for dust removal under the action of the high-temperature fan 7 and the tail exhaust fan 13, and is then discharged from the chimney 10.

[0036] The moisture content of the dehydrated carbide slag is reduced from 30%~35% to below 1%, and the dried carbide slag is sent to the carbide slag dry powder silo 6 for later use.

[0037] The dehydrated carbide slag 3 is heated in the rotary indirect dryer 11, releasing water vapor and ammonia to form high-humidity, high-ammonia flue gas. Driven by the ammonia blower 12, this flue gas enters the condensation absorption tower 13, where it comes into contact with the absorbent liquid, cools and condenses, and absorbs the ammonia. After contacting the high-humidity, high-ammonia flue gas in the condensation absorption tower 13, the absorbent liquid returns to the absorbent liquid pool 14 and re-enters the condensation absorption tower 13 for recycling under the action of the circulating pump 15. After the high-humidity, high-ammonia flue gas passes through the condensation absorption tower 13 to reduce moisture and ammonia, it is sent to the pipeline before the tail-end dust collector 8 and mixes with the preheater outlet flue gas 2 after passing through the rotary indirect dryer 11. After purification by the tail-end dust collector 8, it is discharged into the atmosphere.

[0038] Among them, the temperature of the flue gas 2 at the outlet of the high-temperature preheater is generally 550~700℃, which is related to the number of preheater stages in the plant. The dehydrated carbide slag 3 comes from the upstream chlor-alkali workshop. After being dehydrated by a filter press, the moisture content of the dehydrated carbide slag 3 is 30%~35%.

[0039] Example 3 As per the instruction manual Figure 3 As shown, in this embodiment, based on embodiment one, the exhaust outlet of the indirect dryer 11 is connected to the cyclone dust collector 17, the exhaust port of the cyclone dust collector 17 is connected to the inlet of the ammonia fan 12, and the discharge port of the cyclone dust collector 17 is connected to the carbide slag dry powder silo 6.

[0040] Working principle: Since it is an indirect drying process, the amount of flue gas from the ammonia blower 12 is very small. The flue gas mainly consists of water vapor and ammonia from the drying process, as well as some air leaking in. Therefore, the air velocity inside the indirect dryer 11 is very low. Most of the dried carbide slag powder is discharged through the outlet of the indirect dryer 11. A small portion of the carbide slag powder is carried out by the flue gas. By setting up a cyclone dust collector 17, the carbide slag powder carried out by the flue gas can be collected. Since the carbide slag cyclone discharge pipe is connected to the carbide slag dry powder silo 6, the collected carbide slag powder enters the carbide slag dry powder silo 6.

[0041] Example 4 A certain calcium carbide slag cement plant has an SNCR (Synthetic Non-Combustion Catalytic Reduction) denitrification system installed. To achieve ultra-low emissions of nitrogen oxides and ammonia escaping from flue gas and to utilize the ammonia escaping, the equipment was modified. The modification process is as follows: The high-temperature preheater outlet flue gas 2 from the primary cyclone separator 1 exchanges heat with the dehydrated carbide slag 3 from the upstream chlor-alkali plant in a rotary indirect dryer 11. After heat utilization, the preheater outlet flue gas enters the tail exhaust dust collector 8 for dust removal under the action of the high-temperature fan 7 and the tail exhaust fan 13, and is then discharged from the chimney 10. The moisture content of the dehydrated carbide slag is reduced from 30%~35% to below 1%, and the dried carbide slag is sent to the carbide slag dry powder silo 6 for later use. The high-humidity, high-ammonia flue gas formed by the dehydrated carbide slag being heated and releasing water vapor and ammonia in the rotary indirect dryer 11 is then introduced into the countercurrent condensation absorption tower 13 by the ammonia fan 12, where it contacts the absorbent liquid to cool down and absorb ammonia. After contacting the high-humidity, high-ammonia flue gas in the condensation absorption tower 13, 1% dilute sulfuric acid returns to the absorbent liquid pool 14 and re-enters the condensation absorption tower 13 for recycling under the action of the circulating pump 15.

[0042] The plant uses 1% dilute sulfuric acid as the absorbent, and the flow rate of the circulating pump is controlled by a flue gas analyzer at the outlet of the condensation absorption tower to ensure that the ammonia slip concentration is <8 mg / m³. 3 This ensures that ammonia emissions from the chimney meet standards. The plant has installed a pH testing device and an absorbent discharge pipeline in the absorbent pool. When the pH value of the absorbent reaches 6.8, it is considered saturated. The saturated absorbent is then discharged to the granulation tower to produce ammonium sulfate, and a new 1% concentration of dilute sulfuric acid absorbent is injected.

[0043] In summary, this invention provides a system for controlling and utilizing ammonia escape during denitrification in carbide slag cement.

[0044] The above embodiments have provided a detailed description of the present invention, but the content described is only a preferred embodiment of the present invention and should not be considered as limiting the scope of the present invention. All equivalent variations and improvements made within the scope of the present invention should still fall within the patent coverage of the present invention.

Claims

1. A method for revamping a calcium carbide slag cement denitration ammonia escape control and utilization system, characterized in that: The modification method of the calcium carbide slag cement denitration ammonia escape control and utilization system comprises the following steps: The drying crusher is changed into an indirect dryer, the preheater outlet flue gas is indirectly exchanged with the calcium carbide slag, the indirect dryer waste gas outlet is connected with the ammonia gas absorption device inlet, and the ammonia gas absorption device outlet is communicated with the indirect dryer drying medium outlet.

2. The method for revamping a calcium carbide sludge cement denitration ammonia escape control and utilization system according to claim 1, characterized in that: The ammonia gas absorption device comprises an absorption liquid pool and a condensation absorption tower, the absorption liquid pool is connected with the condensation absorption tower top through a circulating pump, the condensation absorption tower bottom is connected with an ammonia gas fan, and the ammonia gas fan is connected with the indirect dryer waste gas outlet.

3. The method for revamping a calcium carbide sludge cement denitration ammonia escape control and utilization system according to claim 2, characterized in that: The condensation absorption tower top is connected with the indirect dryer drying medium outlet through a pipeline, and a flue gas analyzer is arranged on the pipeline.

4. The method for revamping a calcium carbide sludge cement denitration ammonia escape control and utilization system according to claim 2, characterized in that: The condensation absorption tower bottom is connected with the absorption liquid pool.

5. A calcium carbide slag cement denitration ammonia escape control and utilization system, characterized in that: The calcium carbide slag cement denitration ammonia escape control and utilization system is modified by the modification method of the calcium carbide slag cement denitration ammonia escape control and utilization system according to any one of claims 2-4.

6. The carbide slag cement denitration ammonia escape control and utilization system according to claim 5, characterized in that: The drying medium inlet of the indirect dryer is connected with a primary cyclone, the drying medium outlet of the indirect dryer is connected with a tailing dust collector through a high-temperature fan, the ammonia gas absorption device outlet is connected with the tailing dust collector, so that the mixed gas discharged from the ammonia gas absorption device is mixed with the preheater outlet flue gas after indirect exchange and then is dusted, and the indirect dryer discharge outlet is connected with a calcium carbide slag dry powder warehouse.

7. The carbide slag cement denitration ammonia escape control and utilization system according to claim 6, characterized in that: The indirect dryer waste gas outlet is connected with a cyclone dust collector air inlet, the cyclone dust collector air outlet is connected with the ammonia gas absorption device inlet, and the cyclone dust collector discharge outlet is connected with the calcium carbide slag dry powder warehouse.

8. A calcium carbide slag cement denitration ammonia escape control and utilization process, characterized in that: The calcium carbide slag cement denitration ammonia escape control and utilization process adopts the calcium carbide slag cement denitration ammonia escape control and utilization system according to claim 6.

9. The carbide cement denitration ammonia escape control and utilization process of claim 8, wherein: The calcium carbide slag cement denitration ammonia escape control and utilization process comprises the following steps: The calcium carbide slag is indirectly exchanged with the preheater outlet flue gas, and the calcium carbide slag does not contact the preheater outlet flue gas; The mixed gas containing water vapor and ammonia generated by the calcium carbide slag enters the ammonia gas absorption device, and the mixed gas discharged from the ammonia gas absorption device is mixed with the preheater outlet flue gas after indirect exchange.

10. The carbide cement denitration ammonia escape control and utilization process of claim 9, wherein: The ammonia gas absorption device uses absorption liquid to circulate and absorb ammonia in the mixed gas, the absorption liquid is one or more of hydrochloric acid, sulfuric acid and nitric acid, the absorption liquid is saturated when the absorption liquid PH value reaches 6.5-7, and the absorption liquid is replaced.

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