Anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas.

Abstract

This utility model relates to an anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas. The reactor body includes an absorption zone and a crystallization zone from top to bottom, with the crystallization zone and the absorption zone connected. The absorption zone is located above the liquid surface, and the crystallization zone is located below the liquid surface. The top of the absorption zone has a tail gas outlet, and the bottom of the crystallization zone has a crystal slurry outlet. An external Venturi reaction zone is located below the absorption zone of the reactor body, connected to the reactor body. The Venturi reaction zone has an inlet for the ammonia-containing waste gas and an inlet for the circulating absorbent liquid. The external Venturi reaction zone forms a primary absorption, reducing the intensity of the absorption reaction within the reactor and significantly improving the anti-clogging capability.

Description

Technical Field

[0001] This utility model relates to the field of chemical environmental protection, and in particular to an anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas in the field of wastewater treatment. Background Technology

[0002] In the production processes of chemical plants and environmental protection facilities such as synthetic ammonia, gold beneficiation agent synthesis, coal gas purification, acidic water vapor extraction and phenol-ammonia recovery, ammonia-containing waste gas of varying concentrations is generated. The composition is complex, the concentration is high, and the differences are significant. The recovery of ammonia-containing waste gas into valuable and qualified products is technically challenging, and it is even more difficult to achieve emission standards for tail gas after treatment of high-concentration ammonia-containing waste gas. Due to the malodorous nature of ammonia, once the emission exceeds the standard, it will cause serious environmental accidents. However, ammonia has a high added value, so the treatment and resource recycling of ammonia-containing waste gas has significant economic and environmental value.

[0003] Resource recovery of ammonia-containing waste gas can yield liquid ammonia, ammonia water, and ammonium salts. However, due to absorption equilibrium limitations, direct absorption of ammonia-containing waste gas with water to generate ammonia water often results in low concentrations, making it difficult to utilize directly. Further concentration or purification processes such as distillation are typically required to recover high-concentration ammonia water or liquid ammonia. This process is complex, costly, and the ammonia concentration in the tail gas remains high after absorption, making it difficult to meet emission standards. Resource recovery of ammonia-containing waste gas into ammonium salts, such as ammonium sulfate, ammonium phosphate, ammonium chloride, and ammonium carbonate, offers advantages such as shorter processes, complete absorption, and high product purity. The products can be directly used in agricultural fertilizers. However, because high-concentration ammonia-containing waste gas reacts with acid in a crystallization process, the reaction is rapid, leading to high supersaturation concentrations. This can easily cause scaling and blockage in the reactor, resulting in frequent reactor cleaning and severely impacting normal production.

[0004] Existing technologies for treating ammonia-containing waste gas mainly include physical absorption, chemical absorption, catalytic decomposition, catalytic aerobic decomposition, and biodegradation. However, due to the high concentration of ammonia-containing waste gas (≥1%v), the treatment processes span both chemical and environmental protection fields. For example, physical absorption and chemical absorption have long treatment processes, are highly corrosive, and the exhaust gas is difficult to meet standards. Catalytic decomposition and catalytic aerobic decomposition have high operating temperatures, high fuel gas consumption, and high treatment costs. Biodegradation is difficult to meet the treatment requirements for high-concentration ammonia-containing waste gas, and often requires a combination of multiple processes, resulting in problems such as long process chains, large investments, and high operating costs.

[0005] Chinese patent document CN218339413U discloses a system for preparing ammonium sulfate by ammonia stripping and absorption of ammonia-containing waste gas. The system includes an ammonia absorption tower with a gas phase outlet at the top, a liquid phase outlet at the bottom, a dilute sulfuric acid inlet on the top side, and an ammonia-containing waste gas inlet on the bottom side. The absorption tower is equipped with a spray device inside for spraying dilute sulfuric acid introduced through the dilute sulfuric acid inlet. A cooler is also included, with its outlet connected to the dilute sulfuric acid inlet of the absorption tower. The cooler's inlet is connected to the liquid phase outlet at the bottom of the absorption tower via a sulfuric acid circulation pump. This technical solution uses absorption towers of the same diameter, and all reactions occur within the absorption tower; therefore, it cannot prevent blockage inside the absorption tower after prolonged use.

[0006] Chinese patent document CN210057881U discloses an apparatus for preparing ammonium sulfate by ammonia stripping and absorption of ammonia-containing waste gas. Its structure includes a sulfuric acid diluent, a sulfuric acid storage tank, a sulfuric acid transfer pump, a first mixer, a second mixer, a bottom circulation pump, a top circulation pump, a bottom cooler, a top cooler, an ammonia absorption tower, and a pH meter. The sulfuric acid diluent dilutes concentrated sulfuric acid into dilute sulfuric acid, which is then transported to the first and second mixers to form a mixed solution, which is then transported to the ammonia absorption tower. The ammonia-containing waste gas enters the ammonia absorption tower and is absorbed by the acidic mixed solution. The absorbed liquid is extracted and circulated, and dilute sulfuric acid is continuously added to adjust the pH value of the mixed solution. Simultaneously, a portion of the absorbed liquid is concentrated through evaporation to form ammonium sulfate crystals. This technical solution uses absorption towers of the same diameter, and all reactions occur within the absorption tower, which cannot prevent blockage inside the absorption tower after prolonged use.

[0007] Therefore, it is necessary to propose an anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas. This reactor is highly integrated, small in size, and achieves separation of the absorption zone and crystallization zone within a single reactor, ensuring efficient absorption of high-concentration ammonia-containing waste gas. The absorption zone has a low solid content and is not prone to clogging. Utility Model Content

[0008] The technical problem to be solved by this utility model is to provide an anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas. It has high integration and small size, and the absorption zone and crystallization zone are separated in a single reactor to ensure efficient absorption of high-concentration ammonia-containing waste gas. The absorption zone has low solid content, is not prone to clogging, and has strong anti-crystallization clogging performance.

[0009] To address the aforementioned technical issues, the present invention provides the following solution: an anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas, comprising a reactor body. The reactor body, from top to bottom, includes an absorption zone and a crystallization zone, which are connected. The absorption zone is located above the liquid surface, and the crystallization zone is located below the liquid surface. The top of the absorption zone has a tail gas outlet, and the bottom of the crystallization zone has a crystal slurry outlet. The reactor body has an externally mounted Venturi reaction zone located below the absorption zone, which is connected to the reactor body. The Venturi reaction zone has an ammonia-containing waste gas inlet and a circulating absorbent inlet.

[0010] The reactor employing the above technical solution features a vertical structure with high integration and small volume. The upper part is the absorption zone, and the lower part is the crystallization zone. A Venturi reaction zone is then set up outside the reactor to form a primary absorption, reducing the intensity of the absorption reaction within the reactor and significantly improving anti-clogging capability. Separation of the crystallization and absorption zones is achieved within a single reactor. Overflow is used to control the solids content of the circulating absorbent, enhancing the absorption zone's resistance to crystallization clogging and greatly improving absorption efficiency. Supersaturation control measures are implemented in the crystallization zone, resulting in high-quality crystals with uniform particle size and large size, facilitating concentration and separation. Simultaneously, the reactor maximizes the use of reaction heat to minimize the reliance on external heat, resulting in energy conservation and environmental protection. The technology is stable and reliable, with low investment and operating / maintenance costs. The higher the ammonia concentration in the ammonia gas or ammonia-containing waste gas, the higher the recovery value.

[0011] Preferably, the outlet of the Venturi reaction zone is connected to the reactor body through an inclined tube, so that the ammonia-containing waste gas entering the Venturi reaction zone is absorbed and reacted with the sulfuric acid-containing circulating absorbent liquid, and then enters the reactor body through the inclined tube at the outlet of the Venturi reaction zone.

[0012] Preferably, the downward tilt angle of the inclined tube is set to 20~70°, so that after the ammonia-containing waste gas enters the reactor body, it collides and bounces with the liquid surface of the crystallization zone, and then rises to the top of the reactor body.

[0013] Preferably, the downward tilt angle of the inclined tube is set to 40~60°.

[0014] Preferably, the absorption zone is provided with at least one absorption spray layer, and the crystallization zone is provided with at least one pulse spray layer. The absorption spray layer is provided for the ammonia gas to be absorbed by countercurrent contact with the circulating absorbent containing sulfuric acid; the pulse spray layer utilizes a portion of the circulating absorbent or mother liquor to pulse-impact and flush the bottom area, maintaining the fluidity of the crystals, removing small crystal nuclei from the crystal surface, and forming larger, more regular crystals to further prevent precipitation and blockage.

[0015] Preferably, the anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas is equipped with a reaction circulation pump, a second circulating absorbent inlet is provided at the upper part of the absorption zone, and a circulating absorbent outlet is provided at the upper part of the crystallization zone. The first circulating absorbent inlet, the second circulating absorbent inlet, and the circulating absorbent outlet are connected to the reaction circulation pump to form an external circulation.

[0016] In the above technical solution, the solid content of the circulating absorbent in the absorption zone is ≤3%, preferably ≤1%, which can reduce the risk of blockage in the absorption zone and reduce wear on the pipe nozzles. In the crystallization zone, supersaturation control measures are implemented to optimize the circulating absorbent volume and pulse flow rate, control the slurry flow rate, and minimize fluctuations in supersaturation concentration, thereby achieving high-quality crystals with uniform particle size, large particle size, and easy concentration and separation. The clear liquid with low solid content at the top of the crystallization zone overflows from the circulating absorbent outlet to the outside of the reactor as circulating absorbent, with a solid content ≤3%, preferably ≤1%. After being buffered by a circulating tank, pressurized by a reaction circulation pump, and supplemented with sulfuric acid, it is sent to circulating absorbent inlet one to enter the Venturi reaction zone for reaction, and to circulating absorbent inlet two to enter the multi-layer absorption spray layer for spray absorption; simultaneously, the pH of the circulating absorbent is controlled at 4~5.5. In addition, a portion of the circulating absorbent with low solid content is sent to the bottom of the crystallization zone, where it is pulsed to maintain the fluidity of the crystals, prevent large ammonium sulfate particles from precipitating and clogging the crystals, and remove small crystal nuclei from the crystal surface to form larger and more regular crystals.

[0017] Preferably, the circulating pump is connected to a circulating tank, and a pulse pump is installed at the outlet of the circulating tank. The outlet of the pulse pump is connected to the pulse liquid inlet of the pulse spray layer. The pulse spray layer is provided with vertically downward nozzles, which are evenly distributed and cover the bottom plate of the impact bottom head. The flow rate of the pulse spray layer to the flow rate of the crystal slurry discharge is 1~3, preferably 2~3.

[0018] Preferably, a variable diameter section is provided between the crystallization zone and the absorption zone, and the diameter ratio of the crystallization zone to the absorption zone is 1.2 to 1.4; the end cap at the bottom of the crystallization zone is an elliptical end cap or a constricted flat-bottom end cap, and the solid content of the slurry in the crystallization zone is controlled at 5% to 50%, preferably 10% to 25%. The elliptical end cap or constricted flat-bottom end cap is used to enhance the pulse impact effect.

[0019] Preferably, the upper part of the absorption zone is further provided with at least one layer of demisters, which are located above the absorption spray layer. The number of absorption spray layers is 1 to 4, wherein the distance between the bottommost absorption spray layer and the liquid surface is not less than 3 times the spacing between the absorption spray layers. A manhole is also provided above the demister. Depending on the ammonia concentration in the ammonia-containing waste gas, 1 to 4 spray layers can be set, and 1 to 2 layers of demisters can be set at the top of the reactor. This design offers high flexibility and allows for precise control of absorption efficiency. The distance between the bottommost absorption spray layer and the liquid surface is not less than 3 times the spacing between the absorption spray layers, ensuring a sufficiently large clearance at the bottom of the absorption zone, allowing the ammonia-containing waste gas to be dispersed and evenly distributed, and providing sufficient reaction time with the falling absorption liquid. Preferably, the distance between the bottommost absorption spray layer and the liquid surface is greater than or equal to 5m.

[0020] Preferably, the crystallization zone is provided with at least one thermometer port, at least one density meter port, at least one sight glass, at least one pH meter port, a spare port, and a second manhole. Both the absorption zone and the crystallization zone are provided with at least one remote level gauge port, and the absorption zone is also provided with a third manhole. The thermometer port, remote level gauge port, sight glass, pH meter port, spare port, and manhole are provided as needed, such as above or / and below the demister and spray layer, to facilitate manual cleaning and maintenance of internal components.

[0021] Compared with the prior art, the beneficial effects of this utility model are:

[0022] (1) The reactor has a reasonable structure and adopts a vertical structure. The reactor has an external Venturi reaction zone at the inlet. Ammonia and sulfuric acid-containing circulating absorbent form a primary absorption. The upper part of the reactor is set with an absorption zone and the lower part with a crystallization zone. The solid content of the circulating absorbent is controlled by overflow, which improves the equipment's anti-crystallization and clogging performance, and the absorption efficiency is high. The quality of the obtained ammonium sulfate crystals is high. At the same time, the heat of reaction is used as much as possible to reduce the use of external heat, which is energy-saving and environmentally friendly. The technology is stable and reliable, and the investment and operation and maintenance costs are low. The higher the ammonia concentration in the ammonia or ammonia-containing waste gas, the higher the recovery value.

[0023] (2) The pulse circulating fluid velocity is increased by the pulse nozzle to form an impact flow, which impacts larger ammonium sulfate particles to further prevent precipitation and blockage at the bottom of the crystallization zone; the bottom end cap of the crystallization zone is set as an elliptical end cap or a constricted flat end cap to enhance the pulse impact effect;

[0024] (3) Other components are provided in different locations of the reactor as needed. The crystallization zone is equipped with a thermometer port, a remote level gauge port, multiple sight glasses, a pH meter port, and a spare port. The absorption zone and the crystallization zone are equipped with manholes as needed, such as the demister and the area above and below the spray layer, to facilitate manual cleaning and maintenance of internal components.

[0025] (4) The reactor can treat ammonia-containing waste gas with an ammonia concentration of 1%v~100%v. The ammonia recovery rate can reach more than 98%, and even more than 99.9%. Pretreatment devices can be set up according to the different sources of ammonia-containing waste gas and different impurity components. The pretreatment devices include, but are not limited to, dust removal, pre-washing, heating or cooling, to meet the normal operation of the reactor and the quality of ammonium sulfate products. It has a wide range of applications. It realizes the resource recovery of high-concentration ammonia-containing waste gas into ammonium sulfate, improves the quality of ammonium sulfate products, has a high ammonia recovery rate, solves the problem of reactor blockage in solid and crystallizing reactors, and has no waste gas, waste liquid or solid waste discharge during the treatment process, realizing long-term stable operation of the device.

[0026] (5) The reactor has a novel and safe structure and can operate stably for a long time; and the reactor structure is simple and easy to maintain. Attached Figure Description

[0027] The technical solution of this utility model is further described below with reference to the accompanying drawings:

[0028] Figure 1 This is a schematic diagram of the anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to this utility model;

[0029] Wherein: 1-Crystallization zone; 2-Thermometer port; 3-Variable diameter section; 4-Reactor body; 5-Venturi reaction zone; 501-Inclined tube; 6-Ammonia-containing waste gas inlet; 7-Circulating absorbent inlet one; 8-Absorption zone; 9-Demister; 10-Tail gas outlet; 11-Manhole one; 12-Absorption spray layer; 13-Circulating absorbent inlet two; 14-Remote level gauge port (lower port); 15-Circulating absorbent outlet; 16, 27, 28-Sight glasses; 17-pH meter port; 18-Pulse spray layer; 19-Pulse liquid inlet; 20-Spare port; 21-Crystal slurry outlet; 22-Bottom end cap; 23, 29-Density meter port; 24-Manhole two; 25-Manhole three; 26-Remote level gauge port (upper port). Detailed Implementation

[0030] To enhance understanding of this utility model, it will be described in further detail below with reference to the accompanying drawings and embodiments. These embodiments are only used to explain this utility model and do not limit the scope of protection of this utility model.

[0031] Example 1: As Figure 1As shown, this anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas includes a reactor body 4. The reactor body 4 comprises, from top to bottom, an absorption zone 8 and a crystallization zone 1, which are connected. The absorption zone 8 is located above the liquid surface, and the crystallization zone 1 is located below the liquid surface. The top of the absorption zone 8 has a tail gas outlet 10, and the bottom of the crystallization zone 1 has a crystal slurry outlet 21. The reactor body 4 has an externally mounted Venturi reaction zone 5 located below the absorption zone 8, which is connected to the reactor body 4. The Venturi reaction zone 5 is equipped with an ammonia-containing waste gas inlet 6 and a circulating absorbent liquid inlet 7. The outlet of the Venturi reaction zone 5 is connected to the reactor body 4 through an inclined tube 501, so that the ammonia-containing waste gas entering the Venturi reaction zone 5 is absorbed and reacted with the sulfuric acid-containing circulating absorbent liquid, and then enters the reactor body 4 through the inclined tube 501 at the outlet of the Venturi reaction zone 5. The downward inclination angle of the inclined tube 501 is set to 20~70°, so that after the ammonia-containing waste gas enters the reactor body 4, it collides with the liquid surface of the crystallization zone 1 and bounces back, rising to the top of the reactor body 4.

[0032] The absorption zone 8 is provided with at least one absorption spray layer 12, and the crystallization zone 1 is provided with at least one pulse spray layer 18. The absorption spray layer 12 is provided for the ammonia gas to be absorbed by countercurrent contact with the circulating absorption liquid containing sulfuric acid; the pulse spray layer 18 is provided to use a portion of the circulating absorption liquid or mother liquor to perform pulse impact, flush the bottom area, maintain the fluidity of the crystals, remove small crystal nuclei on the crystal surface, and form larger and more regular crystals to further prevent precipitation and blockage.

[0033] The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas is equipped with a reaction circulation pump. The upper part of the absorption zone 8 is provided with a second circulation absorption liquid inlet 13, and the upper part of the crystallization zone 1 is provided with a circulation absorption liquid outlet 15. The first circulation absorption liquid inlet 7, the second circulation absorption liquid inlet 13, and the circulation absorption liquid outlet 15 are connected to the reaction circulation pump to form an external circulation.

[0034] The circulating pump is connected to a circulating tank, and a pulse pump is installed at the outlet of the circulating tank. The outlet of the pulse pump is connected to the pulse liquid inlet 19 of the pulse spray layer 18. The pulse spray layer 18 is equipped with vertically downward nozzles, which are evenly distributed and cover the bottom plate of the impact bottom head 22. The ratio of the flow rate of the pulse spray layer 18 to the flow rate of the crystal slurry discharge is 1~3.

[0035] The solid content of the circulating absorbent in absorption zone 8 is ≤3%, preferably ≤1%, which reduces the risk of blockage in the absorption zone and reduces wear on the pipe nozzles. In crystallization zone 1, supersaturation control measures are implemented to optimize the circulating absorbent volume and pulse flow rate, control the slurry flow rate, and minimize fluctuations in supersaturation concentration, thereby achieving high-quality crystals with uniform particle size, large particle size, and easy concentration and separation. The clear liquid with low solid content at the top of crystallization zone 1 overflows from the circulating absorbent outlet 15 to the outside of the reactor as circulating absorbent, with a solid content ≤3%, preferably ≤1%. After being buffered by a circulating tank, pressurized by a reaction circulation pump, and supplemented with sulfuric acid, it is sent to circulating absorbent inlet 7 to enter the Venturi reaction zone 5 for reaction, and to circulating absorbent inlet 13 to enter the multi-layer absorption spray layer 12 for spray absorption; simultaneously, the pH of the circulating absorbent is controlled at 4~5.5. In addition, a portion of the circulating absorbent with low solid content is sent to the bottom of crystallization zone 1, and the bottom area is pulsed to maintain the fluidity of the crystals, prevent large particles of ammonium sulfate from precipitating and clogging the crystals, and at the same time remove the small crystal nuclei on the crystal surface to form larger and more regular crystals.

[0036] A variable diameter section 3 is provided between the crystallization zone 1 and the absorption zone 8, and the diameter ratio of the crystallization zone 1 to the absorption zone 8 is 1.2~1.4; the end cap at the bottom of the crystallization zone 1 is an elliptical end cap or a constricted flat-bottom end cap, and the solid content of the slurry in the crystallization zone 1 is controlled at 5~50%; the elliptical end cap or constricted flat-bottom end cap is set to enhance the pulse impact effect.

[0037] The upper part of the absorption zone 8 is also provided with at least one layer of demister 9, which is located above the absorption spray layer 12. The absorption spray layer 12 has 1 to 4 layers, and the distance between the bottommost absorption spray layer 12 and the liquid surface is not less than 3 times the spacing of the absorption spray layers 12. A manhole 11 is also provided above the demister 9.

[0038] The crystallization zone is equipped with a thermometer port 2, two density meters (density meters 23 and 29 respectively), three sight glasses (sight glasses 16, 27 and 28 respectively), a pH meter port 17, a spare port 20 and a second manhole 24. The absorption zone 8 is equipped with a remote liquid level gauge port (upper port) 26, the crystallization zone 1 is equipped with a remote liquid level gauge port (lower port) 14, and the absorption zone is also equipped with a third manhole 25.

[0039] Example 2: The difference from Example 1 is that the downward tilt angle of the inclined tube 501 in this example is set to 40~60°; the solid content of the slurry in the crystallization zone 1 is controlled at 10~25%; the ratio of the flow rate of the pulse spray layer to the flow rate of the crystal slurry discharge is 2~3; and the distance between the bottommost absorption spray layer and the liquid surface is greater than or equal to 5m.

[0040] In addition, depending on the source of the ammonia-containing waste gas and the different impurity components, a pretreatment device can be set up. The pretreatment device includes, but is not limited to, dust removal, pre-washing, heating or cooling, in order to meet the normal operation of the reactor and the quality of the ammonium sulfate product.

[0041] The specific steps for the recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas using an anti-clogging reactor are as follows:

[0042] Ammonia-containing waste gas enters the Venturi reaction zone 5 through ammonia-containing waste gas inlet 6, where it is absorbed and reacted with the sulfuric acid-containing circulating absorbent sprayed in through circulating absorbent inlet 1. The gas then enters the reactor body 4 through the inclined pipe 501 at the outlet of the Venturi reaction zone 5. After colliding with the liquid surface in the crystallization zone 1 and rebounding, it rises to the top of the reactor body 4. During this ascent, it flows countercurrently and reacts with the sulfuric acid-containing circulating absorbent sprayed by the multi-layer absorption spray layer 12 in the absorption zone 8, generating ammonium sulfate. After absorption, the tail gas is demisted by the demister 9 and discharged through the tail gas outlet 10. The clear liquid with low solid content in the upper part of the crystallization zone 1 overflows from the circulating absorbent outlet 15 to the outside of the reactor as circulating absorbent. After being buffered by a circulating tank, pressurized by a reaction circulation pump, and supplemented with sulfuric acid, it is sent to the circulating absorbent inlet 1 to enter the Venturi reaction zone for reaction, and to the circulating absorbent inlet 2 13 to enter the multi-layer absorption spray layer 12 for spray absorption. Simultaneously, a portion of the circulating absorbent is drawn from the circulation tank, pressurized by a pulse pump, and sent to the pulse liquid inlet 19 into the pulse spray layer 18. The pulse nozzles increase the flow rate of the circulating liquid, creating an impact flow that impacts larger ammonium sulfate particles, preventing them from settling and clogging at the bottom of the crystallization zone 1. The diameter ratio of the crystallization zone 1 to the absorption zone 8 is 1.2~1.4, with a variable diameter section between them. The bottom end cap 22 of the crystallization zone 1 is either an elliptical end cap or a constricted flat-bottom end cap to enhance the pulse impact effect. The ammonium sulfate slurry containing larger particles at the bottom of the crystallization zone 1 is discharged from the reactor through the slurry outlet.

[0043] The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas has the following characteristics:

[0044] 1) The reactor features high integration and small size. Its vertical structure and external Venturi reaction zone form a primary absorption stage, reducing the intensity of the absorption reaction within the reactor and significantly improving anti-clogging capabilities. Separation of the crystallization and absorption zones is achieved within a single reactor, with the absorption zone at the top and the crystallization zone at the bottom. Overflow is used to control the solids content of the circulating absorbent, enhancing the absorption zone's resistance to crystallization clogging and greatly improving absorption efficiency. Supersaturation control measures in the crystallization zone result in high-quality crystals with uniform particle size and large particle size, facilitating concentration and separation.

[0045] 2) The reactor adopts a spray reactor, in which ammonia gas is absorbed by countercurrent contact with the circulating absorbent containing sulfuric acid. The number of spray layers in the absorption zone is designed according to the ammonia concentration in the inlet gas, and can be 1 to 4 layers. The design has a high degree of freedom and the absorption efficiency can be precisely controlled.

[0046] 3) The crystallization zone is the area for crystal growth, purification, and separation. It is equipped with a pulse spray layer, which uses a portion of the circulating absorbent or mother liquor to perform pulse impact, flushing the bottom area, maintaining the fluidity of the crystals, removing small crystal nuclei from the crystal surface, and forming larger and more regular crystals; the ratio of the washing spray flow rate to the crystal slurry discharge flow rate is 1~3.

[0047] 4) The pulse spray layer is equipped with vertically downward nozzles that are evenly distributed and cover the bottom plate of the impact head;

[0048] 5) The diameter ratio of the crystallization zone to the absorption zone is 1.2 to 1.4, and a variable diameter section is set between them. The bottom end cap of the crystallization zone is set as an elliptical end cap or a constricted flat bottom end cap to enhance the pulse impact effect.

[0049] For those skilled in the art, the specific embodiments are merely exemplary descriptions of the present invention. Obviously, the specific implementation of the present invention is not limited to the above-described manner. Any non-substantial improvements made using the inventive concept and technical solution of the present invention, or the direct application of the inventive concept and technical solution to other situations without modification, are all within the protection scope of the present invention.

Claims

1. A clog-resistant reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas, characterized in that, The reactor body includes an absorption zone and a crystallization zone from top to bottom, which are connected to each other. The absorption zone is located above the liquid surface, and the crystallization zone is located below the liquid surface. The top of the absorption zone has a tail gas outlet, and the bottom of the crystallization zone has a crystal slurry outlet. The reactor body has an externally mounted Venturi reaction zone at the lower part of the absorption zone, which is connected to the reactor body. The Venturi reaction zone has an ammonia-containing waste gas inlet and a circulating absorbent inlet.

2. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 1, characterized in that, The outlet of the Venturi reaction zone is connected to the reactor body through an inclined tube, so that the ammonia-containing waste gas entering the Venturi reaction zone is absorbed and reacted with the sulfuric acid-containing circulating absorbent liquid, and then enters the reactor body through the inclined tube at the outlet of the Venturi reaction zone.

3. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 2, characterized in that, The downward tilt angle of the inclined tube is set to 20~70°, so that after the ammonia-containing waste gas enters the reactor body, it collides with the liquid surface of the crystallization zone and bounces back, rising to the top of the reactor body.

4. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 3, characterized in that, The downward tilt angle of the inclined tube is set to 40~60°.

5. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 3, characterized in that, The absorption zone is provided with at least one absorption spray layer; the crystallization zone is provided with at least one pulse spray layer.

6. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 5, characterized in that, The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas is equipped with a reaction circulation pump. The upper part of the absorption zone is provided with a second circulation absorbent inlet, and the upper part of the crystallization zone is provided with a circulation absorbent outlet. The first circulation absorbent inlet, the second circulation absorbent inlet, and the circulation absorbent outlet are connected to the reaction circulation pump to form an external circulation.

7. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 6, characterized in that, The circulating pump is connected to a circulating tank, and a pulse pump is installed at the outlet of the circulating tank. The outlet of the pulse pump is connected to the pulse liquid inlet of the pulse spray layer. The pulse spray layer is equipped with vertically downward nozzles, which are evenly distributed and cover the bottom plate of the impact bottom head. The ratio of the flow rate of the pulse spray layer to the flow rate of the crystal slurry discharge is 1~3.

8. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 6, characterized in that, A variable diameter section is provided between the crystallization zone and the absorption zone, and the diameter ratio of the crystallization zone to the absorption zone is 1.2 to 1.4; the end cap at the bottom of the crystallization zone is an elliptical end cap or a constricted flat-bottom end cap; the solid content of the slurry in the crystallization zone is controlled at 5 to 50%.

9. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 6, characterized in that, The upper part of the absorption zone is also provided with at least one layer of demister, which is located above the absorption spray layer. The number of layers of the absorption spray layer is 1 to 4, wherein the distance between the bottommost absorption spray layer and the liquid surface is not less than 3 times the spacing of the absorption spray layers; a manhole is also provided above the demister.

10. The anti-clogging reactor for the resource recovery and preparation of ammonium sulfate from high-concentration ammonia-containing waste gas according to claim 6, characterized in that, The crystallization zone is equipped with at least one thermometer port, at least one density meter port, at least one sight glass, at least one pH meter port, a spare port, and a second manhole. Both the absorption zone and the crystallization zone are equipped with at least one remote liquid level gauge port. The absorption zone is also equipped with a third manhole.

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