High-temperature ammonia-nitrogen wastewater treatment device

Abstract

The utility model provides a high-temperature ammonia-nitrogen wastewater treatment device. The high-temperature ammonia-nitrogen wastewater treatment device comprises a pipeline mixer, a negative pressure deamination tower, a condenser, a gas-liquid separation tank, a gas cooler, a pH regulating tank, a liquid cooler, a filter, a gaseous membrane material liquid deamination unit, an acid liquor circulating tank, a vacuum pump, a gaseous membrane material gas deamination unit, an ammonium sulfate circulating tank and an ammonium sulfate concentrated liquor tank which are sequentially connected in series. The high-temperature ammonia-nitrogen wastewater enters a negative-pressure deamination tower for deamination after being subjected to alkali adjustment through a pipeline mixer, and stronger ammonia water is obtained for reuse; ammonia-containing feed liquid at the tower bottom and ammonia-containing tail gas at the tower top respectively enter a gaseous membrane feed liquid deamination unit and a gaseous membrane feed gas deamination unit for deamination; a byproduct ammonium sulfate solution of the gaseous membrane material liquid deamination unit is used as absorption liquid of the gaseous membrane material gas deamination unit, and an ammonium sulfate concentrated solution is obtained and reused. The waste heat of the high-temperature ammonia-nitrogen wastewater is fully utilized, ammonia nitrogen in the high-temperature ammonia-nitrogen wastewater can be removed to reach the standard, ammonia resources are recycled in the form of concentrated ammonia water and concentrated ammonium sulfate, and the process is energy-saving, efficient and free of secondary pollution.

Description

Technical Field

[0001] This utility model relates to the field of industrial wastewater treatment, specifically a high-temperature ammonia nitrogen wastewater treatment device. Background Technology

[0002] High-temperature ammonia nitrogen wastewater is commonly generated during production processes in industries such as petrochemicals, coal chemicals, power plants, and non-ferrous metal smelting. This type of wastewater typically has a temperature between 60°C and 80°C, with ammonia nitrogen concentrations ranging from several hundred milligrams per liter (mg / L) to several thousand milligrams per liter, and sometimes even reaching tens of thousands of milligrams per liter. Ammonia nitrogen is a major environmental pollutant, and due to its toxicity and destructive impact on aquatic ecosystems, it is one of the most difficult pollutants to degrade and remove. How to efficiently treat high-temperature ammonia nitrogen wastewater while achieving energy conservation and resource utilization is a crucial research topic in the field of industrial wastewater treatment. Currently, the main technologies for treating high-temperature ammonia nitrogen wastewater include biochemical methods, physical methods, and chemical methods.

[0003] However, most of these technologies require wastewater to be cooled to room temperature before treatment, resulting in wasted heat energy and a lack of energy-saving treatment processes that can fully utilize waste heat. Furthermore, existing technologies typically suffer from high operating costs, limited treatment efficiency, and difficulties in meeting emission standards for tail gas or effluent. While stripping-absorption or distillation technologies can achieve high-temperature feed treatment, they still have many shortcomings. Traditional stripping-absorption processes are inefficient in removing ammonia nitrogen, and the effluent often fails to meet direct discharge standards. For example, patent CN215627338U discloses a composite high-temperature ammonia nitrogen stripping tower, which improves the efficiency of ammonia nitrogen stripping-absorption through the recycling of stripping air and a radially arranged multi-layer packing box design. However, this technology has complex internal components, high maintenance difficulty, and higher power consumption and operating costs than ordinary stripping-absorption towers. On the other hand, distillation technologies generally operate at higher temperatures and pressures, resulting in higher equipment investment and operating energy consumption. Although negative pressure ammonia removal technology can reduce system energy consumption to some extent and quickly collect ammonia from wastewater, it is prone to problems such as substandard ammonia nitrogen wastewater effluent or the need for secondary treatment of ammonia-containing tail gas during operation. For example, patent CN221777633U discloses an ammonia removal device for high-temperature, high-salinity ammonia nitrogen wastewater. While its structure is relatively simple and operation is convenient, the simple design of the absorption device results in low ammonia removal efficiency and unsatisfactory tail gas treatment, easily leading to excessive ammonia nitrogen levels in the emitted air. Furthermore, gaseous membrane separation technology, as a highly efficient and energy-saving wastewater and waste gas treatment technology, has attracted attention due to its mild operating conditions and high selectivity. However, this technology is typically suitable for ambient temperature processes, with the feed liquid or gas temperature not exceeding 45°C, thus lacking applicability for treating high-temperature ammonia nitrogen wastewater.

[0004] In summary, existing high-temperature ammonia nitrogen wastewater treatment technologies all have varying degrees of shortcomings, including high energy consumption, low ammonia removal efficiency, and difficulty in meeting standards for tail gas and effluent treatment. There is an urgent need for a resource-based treatment technology for ammonia nitrogen wastewater that can directly feed at high temperatures, has high treatment efficiency, a simple structure, and low operating costs, in order to overcome the deficiencies of existing technologies and further improve the treatment effect of high-temperature ammonia nitrogen wastewater. Utility Model Content

[0005] The purpose of this invention is to provide a high-temperature ammonia nitrogen wastewater treatment device that combines negative pressure deammoniation with gaseous membrane liquid deammoniation and gaseous membrane gas deammoniation. After negative pressure deammoniation, the high-temperature ammonia nitrogen wastewater is treated to obtain concentrated ammonia water for reuse. For the ammonia-containing liquid at the bottom of the negative pressure deammoniation tower that does not meet the standards, gaseous membrane liquid deammoniation is used to remove the ammonia nitrogen, so that the ammonia in the ammonia-containing liquid meets the discharge standards. The ammonium sulfate solution, which is an acidic byproduct of gaseous membrane liquid deammoniation, is used as the absorbent for gaseous membrane gas deammoniation to absorb the ammonia-containing tail gas at the top of the negative pressure deammoniation. The tail gas that meets the ammonia nitrogen standards is released into the air, and the concentrated ammonium sulfate solution is obtained for reuse.

[0006] To achieve the above objectives, this utility model proposes the following technical solution: a high-temperature ammonia nitrogen wastewater treatment device, comprising:

[0007] The system includes a pipeline mixer and a negative pressure ammonia removal tower. The pipeline mixer has a high-temperature ammonia nitrogen wastewater inlet, an alkali inlet, and a discharge outlet. The negative pressure ammonia removal tower has a high-temperature liquid inlet on the upper side wall, a steam inlet on the lower side wall, a gas outlet at the top, a reflux liquid inlet at the top, and a liquid outlet at the bottom. The discharge outlet is connected to the high-temperature liquid inlet of the negative pressure ammonia removal tower via a pipeline. A pH meter is installed on the pipeline. The gas outlet at the top of the tower is connected to a condenser. The condensate is sent to the negative pressure ammonia removal tower for further treatment via the reflux liquid inlet. Non-condensable gases are extracted by a vacuum pump. The liquid outlet at the bottom of the tower is connected to the inlet of a pH adjustment tank. The outlet of the pH adjustment tank is connected to the inlet of a liquid cooler. The outlet of the liquid cooler is connected to the inlet of a filter.

[0008] A gaseous membrane ammonia removal unit comprises several gaseous membrane modules connected in series or parallel. The unit has an ammonia-containing liquid inlet at the bottom of the tube side and a liquid outlet (II) at the top of the tube side; a sulfuric acid absorbent inlet at the bottom of the shell side and a completed absorption liquid outlet (I) at the top of the shell side. The ammonia-containing liquid inlet is connected to the filtrate outlet of a filter via a pipeline, and the ammonia-compliant liquid is discharged through liquid outlet (II). The sulfuric acid absorbent inlet is connected to the acid outlet of an acid circulation tank, and the completed absorption liquid outlet (I) is connected to the inlets of an ammonium sulfate circulation tank and an acid circulation tank, respectively. A pH meter, valve K3, and valve K4 are installed on the pipeline.

[0009] The gaseous membrane material ammonia removal unit comprises several gaseous membrane modules connected in series or parallel. The gaseous membrane material ammonia removal unit has a gas inlet at the top of the tube side, a gas outlet at the bottom of the tube side, an absorbent inlet at the bottom of the shell side, and a completed absorbent outlet at the top of the shell side. The gas inlet is connected to the gas outlet of a vacuum pump via a pipeline, and the nitrogen-compliant material gas is discharged through gas outlet. The absorbent inlet is connected to the outlet of the ammonium sulfate circulation tank, and the completed absorbent outlet is connected to the inlet of the ammonium sulfate circulation tank and the inlet of the ammonium sulfate concentrate tank via pipelines. A pH meter, valve K5, and valve K6 are installed on the pipelines.

[0010] Furthermore, in this invention, the inner wall of the negative pressure deammoniation tower is provided with an anti-scaling layer.

[0011] Furthermore, in this invention, the gaseous membrane component of the gaseous membrane material deammoniation unit is a hollow fiber membrane component, made of a hollow fiber microporous hydrophobic membrane with an inner diameter greater than 1 mm.

[0012] Furthermore, in this utility model, the condensate from the condenser is connected to the gas-liquid separator and the reflux inlet at the top of the negative pressure ammonia removal tower via a pipeline. The reflux pipeline is equipped with an ammonia nitrogen meter, valve K1, a concentrated ammonia water collection pipeline, and valve K2. The non-condensable gas is cooled by a gas cooler and then extracted by a vacuum pump into the gaseous membrane material ammonia removal unit.

[0013] Furthermore, in this invention, the pH adjustment tank is equipped with a pH meter, an alkali inlet, an outlet, and a stirring device.

[0014] Furthermore, in this utility model, the filter is provided with a feed inlet, a filtrate outlet, and a filter residue outlet; after the feed liquid is filtered by the filter, filtrate and filter residue are obtained. The filtrate enters the gaseous membrane feed liquid deammoniation unit, and the filter residue is transported off-site for treatment.

[0015] Furthermore, in this utility model, the filter is one or a combination of several of the following: pressure filtration, fiber filtration, bag filtration, multi-media filtration, security filtration, microfiltration, tubular ultrafiltration, and ultrafiltration.

[0016] Furthermore, in this invention, both the acid circulation tank and the ammonium sulfate circulation tank are equipped with pH meters for detecting the acidity of the feed solution.

[0017] Furthermore, in this utility model, the inlet and outlet pipes of the ammonia-containing liquid in the gaseous membrane deammoniation unit, and the inlet and outlet pipes of the gaseous membrane deammoniation unit are all equipped with ammonia nitrogen meters for detecting ammonia nitrogen concentration.

[0018] Furthermore, in this utility model, the pipeline mixer, negative pressure deammoniation tower, condenser, gas-liquid separator, gas cooler, pH adjustment tank, liquid cooler, filter, gaseous membrane material deammoniation unit, acid circulation tank, vacuum pump, gaseous membrane material gas deammoniation unit, ammonium sulfate circulation tank, and ammonium sulfate concentrate tank are all connected by matching liquid transfer pumps, pipelines, valves, and instruments. All liquid transfer pumps are equipped with pressure gauges for measuring hydraulic pressure on the pipelines downstream.

[0019] Process principle:

[0020] High-temperature ammonia nitrogen wastewater, after being adjusted to alkaline pH, directly enters the negative pressure ammonia removal tower. Under alkaline conditions, ionic NH4 in the wastewater... + The ammonia gas is converted into free NH3 and accumulates at the top of the negative pressure ammonia removal tower. It is then extracted, condensed, and converted into concentrated ammonia water for collection and reuse. The ammonia-containing liquid at the bottom of the tower is pH adjusted, heat exchanged, and filtered. It is then deammonerated using a gaseous membrane to obtain a liquid with compliant ammonia nitrogen levels, which is discharged. The byproduct ammonium sulfate solution is acidic and is used as the absorbent for the ammonia-containing tail gas at the top of the tower. Ammonia nitrogen in the tail gas of the negative pressure ammonia removal tower is removed using a gaseous membrane. The ammonia-compliant gas is then discharged into the air, and the concentrated ammonium sulfate solution is obtained for reuse.

[0021] Gaseous membrane technology can be used to remove ammonia nitrogen from liquid or gaseous feeds. While the principles are the same, the application devices, especially the core gaseous membrane module, differ in structure and operation. For ammonia-containing liquid feeds, the pH needs to be pre-adjusted to alkaline, followed by filtration. The filtered clear liquid then enters the gaseous membrane unit. Under alkaline conditions, volatile ammonia in the liquid diffuses through the micropores of the hydrophobic gaseous membrane wall and is absorbed by the sulfuric acid absorbent on the other side, forming ammonium sulfate, thus removing ammonia nitrogen from the liquid. For ammonia-containing gaseous feeds, the ammonia directly enters the gaseous membrane unit. Volatile ammonia in the gas permeates through the micropores of the hydrophobic gaseous membrane wall and is absorbed by the acidic absorbent on the other side, forming ammonium salts, thus removing ammonia nitrogen from the gas. Compared to gaseous membrane modules used for liquid ammonia removal, those used for gaseous ammonia removal employ hollow fiber membranes with larger inner diameters and higher fiber strength to ensure higher throughput at lower operating pressures.

[0022] Beneficial effects: The technical solution of this application has the following technical effects:

[0023] 1. After the high-temperature ammonia nitrogen wastewater is adjusted for alkali by the pipeline mixer, it directly enters the negative pressure ammonia removal tower for ammonia removal. There is no need for a preheater or reboiler. It makes full use of the original wastewater heat, reduces equipment investment, and lowers heat energy consumption.

[0024] 2. A negative pressure ammonia removal tower is used to remove most of the ammonia nitrogen from the high-temperature ammonia nitrogen wastewater, and concentrated ammonia water is obtained for reuse; a gaseous membrane liquid ammonia removal unit removes ammonia nitrogen from the bottom liquid of the negative pressure ammonia removal tower, so that the liquid meets the discharge standards; a gaseous membrane gas ammonia removal unit removes ammonia nitrogen from the tail gas at the top of the tower, so that the tail gas meets the venting standards, and concentrated ammonium sulfate solution is obtained for reuse; thus, the high-temperature ammonia nitrogen wastewater meets the treatment standards, and ammonia nitrogen in the original wastewater is recovered in the form of concentrated ammonia water and concentrated ammonium sulfate solution, respectively, realizing the reuse of ammonia resources.

[0025] 3. The ammonium sulfate solution produced as a byproduct of the gaseous membrane ammonia removal unit is used as the absorbent in the gaseous membrane ammonia removal unit. The two share a storage tank, which not only solves the problem of neutralizing and reprocessing the ammonium sulfate solution produced as a byproduct of gaseous membrane wastewater ammonia removal, but also reduces equipment investment.

[0026] 4. The gaseous membrane material ammonia removal unit is used instead of the conventional absorption tower, which has a higher absorption efficiency for ammonia-containing tail gas and saves more on equipment investment and operating costs.

[0027] 5. A two-step alkali adjustment scheme, consisting of initial alkali adjustment using a pipeline mixer and secondary alkali adjustment using a pH adjustment tank, is adopted to replace the initial alkali adjustment before the negative pressure ammonia removal tower. This not only avoids the need for high-temperature resistant filtration devices before the negative pressure ammonia removal tower, which would increase equipment investment, reduce feed liquid temperature, and negatively affect the negative pressure ammonia removal effect, but also reduces the feed turbidity of the negative pressure ammonia removal tower while meeting the feed pH requirements of both the negative pressure ammonia removal tower and the gaseous membrane feed liquid ammonia removal unit, thus preventing scaling and clogging in the negative pressure ammonia removal tower.

[0028] 6. A two-step cooling scheme using a condenser and a gas cooler is adopted to replace the deep cooling of the condenser. This not only ensures the temperature of the reflux liquid entering the negative pressure deammoniation tower and reduces heat source consumption, but also provides the gas with a suitable temperature for the gaseous membrane material deammoniation unit. Overall, the cold source consumption is greatly reduced, resulting in greater energy savings.

[0029] 7. This utility model uses energy-saving and high-efficiency devices such as negative pressure ammonia removal tower, gaseous membrane wastewater ammonia removal unit, and gaseous membrane waste gas ammonia removal unit as the main components, making the high-temperature ammonia nitrogen wastewater treatment device energy-saving and efficient as a whole.

[0030] It should be understood that all combinations of the foregoing concepts and the additional concepts described in more detail below can be considered as part of the utility model subject matter of this disclosure, provided that such concepts do not contradict each other.

[0031] The foregoing and other aspects, embodiments, and features of the present invention will be more fully understood from the following description in conjunction with the accompanying drawings. Other additional aspects of the present invention, such as features and / or beneficial effects of exemplary embodiments, will become apparent from the following description or may be learned through practice of specific embodiments according to the teachings of the present invention. Attached Figure Description

[0032] The accompanying drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component shown in the various figures may be denoted by the same reference numeral. For clarity, not every component is labeled in each figure. Embodiments of various aspects of the present invention will now be described by way of example and with reference to the accompanying drawings, wherein:

[0033] Figure 1 This is a schematic diagram of the structure of this utility model.

[0034] In the diagram, the meanings of the labels are as follows: 1. Pipeline mixer; 2. Negative pressure ammonia removal tower; 3. Condenser; 4. Gas-liquid separator; 5. Gas cooler; 6. pH adjustment tank; 7. Liquid cooler; 8. Filter; 9. Gaseous membrane feed ammonia removal unit; 10. Acid circulation tank; 11. Vacuum pump; 12. Gaseous membrane feed gas ammonia removal unit; 13. Ammonium sulfate circulation tank; 14. Ammonium sulfate tank; K1, K2, K3, K4, K5, and K6 are all valves.

[0035] 1.1 Feed inlet; 1.2 Addition port; 1.3 Discharge port; 2.1 High-temperature liquid inlet; 2.2 Steam inlet; 2.3 Gas outlet one; 2.4 Reflux liquid inlet; 2.5 Liquid outlet one; 9.1 Ammonia-containing liquid inlet; 9.2 Liquid outlet two; 9.3 Sulfuric acid absorbent inlet; 9.4 Completed absorption liquid outlet one; 12.1 Gas inlet; 12.2 Absorbent liquid inlet; 12.3 Gas outlet two; 12.4 Completed absorption liquid outlet two; Detailed Implementation

[0036] To better understand the technical content of this utility model, specific embodiments are described below in conjunction with the accompanying drawings. Various aspects of this utility model are described in this disclosure with reference to the accompanying drawings, which illustrate numerous illustrative embodiments. The embodiments of this disclosure are not necessarily defined to include all aspects of this utility model. It should be understood that the various concepts and embodiments described above, as well as those described in more detail below, can be implemented in any of many ways, because the concepts and embodiments disclosed in this utility model are not limited to any particular implementation. Furthermore, some aspects of this utility model can be used alone or in any suitable combination with other aspects disclosed in this utility model.

[0037] like Figure 1As shown, the high-temperature ammonia nitrogen wastewater treatment device of this embodiment includes a pipeline mixer 1, a negative pressure ammonia removal tower 2, a condenser 3, a gas-liquid separator 4, a gas cooler 5, a pH adjustment tank 6, a liquid cooler 7, a filter 8, a gaseous membrane material liquid ammonia removal unit 9, an acid circulation tank 10, a vacuum pump 11, a gaseous membrane material gas ammonia removal unit 12, an ammonium sulfate circulation tank 13, and an ammonium sulfate concentrate tank 14, all connected in series. The above devices are connected by matching liquid transfer pumps, pipelines, valves and instruments. The pipeline mixer 1 is equipped with a high-temperature ammonia nitrogen wastewater inlet 1.1, an alkali solution dosing inlet 1.2, and a discharge outlet 1.3; the negative pressure ammonia removal tower 2 has a high-temperature liquid inlet 2.1 on the upper side wall, a steam inlet 2.2 on the lower side wall, a gas outlet 1 2.3 at the top, a reflux liquid inlet 2.4 at the top, and a liquid outlet 1 2.5 at the bottom; the gaseous membrane liquid ammonia removal unit 9 has an ammonia-containing liquid inlet 9.1 at the bottom of the tube side, a liquid outlet 2 9.2 at the top of the tube side, a sulfuric acid absorbent inlet 9.3 at the bottom of the shell side, and a completed absorption liquid outlet 1 9.4 at the top of the shell side; the gaseous membrane gas ammonia removal unit 12 has a gas inlet 12.1 at the bottom of the tube side, a gas outlet 2 12.3 at the bottom of the tube side, an absorbent inlet 12.2 at the bottom of the shell side, and a completed absorption liquid outlet 2 12.4 at the top of the shell side.

[0038] The specific process is as follows: High-temperature ammonia nitrogen wastewater enters the pipeline mixer 1 through the feed inlet 1.1 and alkaline solution enters through the dosing inlet 1.2. In the pipeline mixer 1, the high-temperature ammonia nitrogen wastewater is adjusted to alkalinity. The pH value is detected by the pH meter on the pipeline connecting the discharge outlet 1.3 and the high-temperature feed inlet 2.1. The amount of alkaline solution added to the pipeline mixer 1 is adjusted to adjust the pH of the high-temperature ammonia nitrogen wastewater to about 10, which meets the feed requirements of the negative pressure ammonia removal tower 2. At the same time, the turbidity of the feed to the negative pressure ammonia removal tower 2 is reduced as much as possible. The inner wall of the negative pressure ammonia removal tower 2 is equipped with an anti-scaling layer to further ensure that scaling, clogging and other adverse phenomena do not easily occur in the negative pressure ammonia removal tower 2.

[0039] The high-temperature ammonia nitrogen feed liquid entering the negative pressure ammonia removal tower 2 flows downward through the distributor. The steam, which serves as the heating source, diffuses upward from the bottom of the tower through the distributor. After the two come into contact, mass and heat transfer occur. The liquid continues to flow downward to the bottom outlet 2.5 and is discharged. The ammonia in the feed liquid escapes into the water as ammonia gas and is discharged upward from the top gas outlet 2.3 into the condenser 3. The condensate is separated by the gas-liquid separator 4 and the liquid is returned to the negative pressure ammonia removal tower 2 for further treatment. The non-condensable gas is extracted by the vacuum pump 11 through the gas cooler 5, thereby maintaining the negative pressure inside the tower. The temperature of the ammonia-containing tail gas extracted by the vacuum pump 11 is controlled to not exceed 45°C by controlling the cooling water circulation of the gas cooler 5.

[0040] Condenser 3 is connected in sequence to gas-liquid separator 4 and reflux inlet 2.4 at the top of negative pressure ammonia removal tower 2 via pipelines. The liquid reflux pipeline is equipped with an ammonia nitrogen meter, valve K1, concentrated ammonia water collection pipeline and valve K2. The reflux solution is returned to negative pressure ammonia removal tower 2 by judging the ammonia nitrogen concentration and controlling the opening and closing of the pipeline valves. When the concentration detected by the ammonia nitrogen meter is lower than the set concentration, valve K2 is closed and valve K1 is opened, and the reflux liquid enters the negative pressure ammonia removal tower. When the concentration detected by the ammonia nitrogen meter reaches the set concentration, valve K1 is closed and valve K2 is opened, and concentrated ammonia water is collected.

[0041] The ammonia-containing liquid discharged from the bottom outlet of the negative pressure ammonia removal tower 2 (at point 2.5) is connected to the inlet of the pH adjustment tank 6. The pH adjustment tank 6 is also equipped with a pH meter, an alkali inlet, an outlet, and a stirring device. By adding alkali, the pH of the liquid is adjusted to be greater than 11, and impurities such as calcium and magnesium ions are precipitated.

[0042] The outlet of pH adjustment tank 6 is connected to the inlet of liquid cooler 7, and the outlet of liquid cooler 7 is connected to the inlet of filter 8. By controlling the cooling water circulation of liquid cooler 7, the outlet temperature of pH adjustment tank 6 is reduced to room temperature, not exceeding 45°C, so as to provide a suitable temperature of feed liquid for gaseous membrane ammonia removal unit.

[0043] Filter 8 is equipped with a feed inlet, a filtrate outlet, and a filter residue outlet. After the feed liquid is filtered by filter 8, filtrate and filter residue are obtained. The filtrate enters the gaseous membrane feed liquid ammonia removal unit 9, and the filter residue is transported off-site for disposal. Filter 8 is one or a combination of several of the following: pressure filtration, fiber filtration, bag filtration, multi-media filtration, security filtration, microfiltration, tubular ultrafiltration, and ultrafiltration. It is used to filter and remove solid particulate impurities from wastewater, ensuring the feed liquid is clear and preventing subsequent membrane clogging.

[0044] The gaseous membrane ammonia removal unit 9 includes several gaseous membrane modules connected in series or parallel. The filtrate produced by the filter 8 enters the tube side of the gaseous membrane ammonia removal unit 9 through the feed inlet 9.1, while the sulfuric acid absorbent enters the shell side of the gaseous membrane ammonia removal unit 9 through the absorbent inlet 9.2. Volatile ammonia molecules in the feed diffuse through the micropores of the gaseous membrane wall, and at the membrane-absorbent interface and in the acidic absorbent, H+ molecules are absorbed. + A reaction occurs, removing ammonia from the feed solution. An ammonia nitrogen detector is installed at the outlet pipe; feed solutions meeting ammonia nitrogen standards are discharged through feed solution outlet 9.3. The absorbed ammonium sulfate solution is discharged from outlet 9.4 and connected via pipes to ammonium sulfate circulation tank 13 and acid circulation tank 10. These pipes are equipped with a pH meter, valve K3, and valve K4. The pH readings and valve opening / closing control whether the ammonium sulfate solution returns to acid circulation tank 10. When pH < 2, valve K3 is opened and valve K4 is closed, returning the solution to acid circulation tank 10 for reuse as an acidic absorbent. When pH > 2, valve K4 is opened and valve K3 is closed, allowing the solution to enter ammonium sulfate circulation tank 13.

[0045] The ammonium sulfate produced by the gaseous membrane ammonia removal unit 9 is acidic and is used as the absorbent in the gaseous membrane ammonia removal unit 12 for the absorption of ammonia-containing tail gas in the negative pressure ammonia removal tower 2. This ensures that the ammonia in the tail gas meets the standards while increasing the concentration of the ammonium sulfate solution, which is beneficial for the reuse of the ammonium sulfate solution. At the beginning of the unit's operation, sulfuric acid solution needs to be added to the ammonium sulfate circulation tank 13 to ensure that the ammonia-containing tail gas in the negative pressure ammonia removal tower 2 meets the standards.

[0046] The gaseous membrane material ammonia removal unit 12 includes several gaseous membrane modules arranged in series or parallel. Vacuum pump 11 extracts gas, which enters the tube side of the gaseous membrane material ammonia removal unit 12 through a pipeline and gas inlet 12.1. Acidic ammonium sulfate solution enters the shell side of the gaseous membrane material ammonia removal unit 12 from the outlet of ammonium sulfate circulation tank 13 through absorbent inlet 12.2. Ammonia molecules in the ammonia-containing tail gas pass through the micropores of the gaseous membrane wall and react with H+ in the acidic absorbent on the other side. + A reaction occurs, thereby removing ammonia from the feed gas. The gas outlet pipe is equipped with an ammonia nitrogen detector. Feed gas with ammonia nitrogen levels meeting the standard is discharged through feed outlet 12.3. The outlet of the absorption liquid is connected to the inlet of ammonium sulfate circulation tank 13 and the inlet of ammonium sulfate concentrate tank 14 through pipes. The pipes are equipped with a pH meter, valve K5, and valve K6. When the pH of the feed liquid is <5, valve K5 is opened and valve K6 is closed, and the feed liquid enters ammonium sulfate circulation tank 13. When the pH of the feed liquid is >5, valve K6 is opened and valve K5 is closed, and the feed liquid enters ammonium sulfate concentrate tank 14.

[0047] The gaseous membrane module of the gaseous membrane deammoniation unit 2 is a hollow fiber membrane module. The hollow fiber membrane is a microporous hydrophobic membrane with an inner diameter greater than 1 mm, and the membrane material is polypropylene (PP), polytetrafluoroethylene (PTFE), etc. The number and arrangement of the gaseous membrane modules are directly related to the gas throughput and ammonia concentration.

[0048] All standard parts used in this application can be purchased from the market, and can be customized according to the description and drawings. The specific connection methods of each part adopt conventional methods such as bolts, rivets, and welding that are mature in the prior art. The machinery, parts and equipment adopt conventional models in the prior art. The control method is automatic control through a controller. The control circuit of the controller can be implemented by simple programming by those skilled in the art and is common knowledge in the field. Since this application is mainly used to protect mechanical devices, the control method and circuit connection will not be explained in detail in this application.

[0049] Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Those skilled in the art to which this invention pertains can make various modifications and refinements without departing from the spirit and scope of the present invention. Therefore, the scope of protection of this invention shall be determined by the claims.

Claims

1. A high-temperature ammonia nitrogen wastewater treatment device, characterized in that, The application relates to a high-temperature ammonia-nitrogen wastewater treatment device, which comprises the following components: a pipeline mixer (1) and a negative pressure ammonia removal tower (2), the pipeline mixer (1) is provided with a high-temperature ammonia-nitrogen wastewater feeding port (1.1), an alkali feeding port (1.2) and a discharging port (1.3), the negative pressure ammonia removal tower (2) is provided with a high-temperature feed liquid inlet (2.1) at the upper part of the side wall, a steam inlet (2.2) at the lower part of the side wall, a gas outlet (2.3) at the top, a reflux liquid inlet (2.4) at the top and a feed liquid outlet (2.5) at the bottom, the discharging port (1.3) is connected with the high-temperature feed liquid inlet (2.1) of the negative pressure ammonia removal tower (2) through a pipeline, a pH meter is arranged on the pipeline, the gas outlet (2.3) at the top is connected with a condenser (3), condensed liquid is treated again in the negative pressure ammonia removal tower (2) through the reflux liquid inlet (2.4), and non-condensed gas is extracted through a vacuum pump (11); the feed liquid outlet (2.5) at the bottom is connected with a water inlet of a pH adjusting tank (6), a discharging port of the pH adjusting tank (6) is connected with a feeding port of a liquid cooler (7), and a discharging port of the liquid cooler (7) is connected with a feeding port of a filter (8); a gaseous membrane feed liquid ammonia removal unit (9), the gaseous membrane feed liquid ammonia removal unit (9) comprises a plurality of gaseous membrane assemblies arranged in series or in parallel, the gaseous membrane feed liquid ammonia removal unit (9) is provided with a feed liquid inlet (9.1) at the bottom of the tube side, a feed liquid outlet (9.3) at the top of the tube side, a sulfuric acid absorption liquid inlet (9.2) at the bottom of the shell side and an absorption completed liquid outlet (9.4) at the top of the shell side; the feed liquid inlet (9.1) is connected with a filtrate outlet of the filter (8) through a pipeline, ammonia standard liquid is discharged through the feed liquid outlet (9.3); the sulfuric acid absorption liquid inlet (9.2) is connected with an acid outlet of an acid liquid circulating tank (10), the absorption completed liquid outlet (9.4) is connected with feeding inlets of an ammonium sulfate circulating tank (13) and the acid liquid circulating tank (10) respectively, and a pH meter, a valve K3 and a valve K4 are arranged on the pipeline; a gaseous membrane feed gas ammonia removal unit (12), the gaseous membrane feed gas ammonia removal unit (12) comprises a plurality of gaseous membrane assemblies arranged in series or in parallel, the gaseous membrane feed gas ammonia removal unit (12) is provided with a gas inlet (12.1) at the top of the tube side, a gas outlet (12.3) at the bottom of the tube side, an absorption liquid inlet (12.2) at the bottom of the shell side and an absorption completed liquid outlet (12.4) at the top of the shell side; the gas inlet (12.1) is connected with a gas outlet of the vacuum pump (11) through a pipeline, nitrogen standard gas is discharged through the gas outlet (12.3); the absorption liquid inlet (12.2) is connected with a discharging port of the ammonium sulfate circulating tank (13), the absorption completed liquid outlet (12.4) is connected with feeding inlets of the ammonium sulfate circulating tank (13) and the ammonium sulfate concentrated liquid tank (14) through pipelines respectively, and a pH meter, a valve K5 and a valve K6 are arranged on the pipelines.

2. The high-temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: An antifouling layer is arranged on the inner wall of the negative pressure ammonia removal tower (2).

3. The high-temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The gaseous membrane assembly of the gaseous membrane feed gas ammonia removal unit (12) is a hollow fiber membrane assembly which is made of a hollow fiber microporous hydrophobic membrane with an inner diameter greater than 1 mm.

4. The high-temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The condensed liquid of the condenser (3) is connected with the reflux liquid inlet (2.4) of the top of the negative pressure deamination tower (2) through a pipeline, and an ammonia nitrogen meter, a valve K1, a concentrated ammonia water collection pipeline and a valve K2 are arranged on the reflux pipeline; the non-condensable gas is cooled by the gas cooler (5) and then is extracted by the vacuum pump (11) to enter the gaseous membrane material gas deamination unit (12).

5. The high temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The pH adjusting tank (6) is provided with a pH meter, an alkali feeding port, a discharge port and a stirring device.

6. The high temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The filter (8) is provided with a feeding port, a filtrate outlet and a filter residue outlet; after the material liquid is filtered by the filter (8), the filtrate is obtained and is fed into the gaseous membrane material liquid deamination unit (9), and the filter residue is transported out for treatment.

7. The high temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The filter (8) is one or a combination of several of pressure filtration, fiber filtration, bag type filtration, multi-medium filtration, security filtration, microfiltration, tubular ultrafiltration and ultrafiltration.

8. The high temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The acid liquid circulating tank (10) and the ammonium sulfate circulating tank (13) are each provided with a pH meter for detecting the acidity of the material liquid.

9. The high temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The feeding pipeline and the discharge pipeline of the gaseous membrane material liquid deamination unit (9) and the gas inlet pipeline and the gas outlet pipeline of the gaseous membrane material gas deamination unit (12) are each provided with an ammonia nitrogen meter for detecting the ammonia nitrogen concentration.

10. The high temperature ammonia-nitrogen wastewater treatment device according to claim 1, characterized in that: The pipeline mixer (1), the negative pressure deamination tower (2), the condenser (3), the gas-liquid separation tank (4), the gas cooler (5), the pH adjusting tank (6), the liquid cooler (7), the filter (8), the gaseous membrane material liquid deamination unit (9), the acid liquid circulating tank (10), the vacuum pump (11), the gaseous membrane material gas deamination unit (12), the ammonium sulfate circulating tank (13) and the ammonium sulfate concentrated liquid tank (14) are connected through matched liquid conveying pumps, pipelines, valves and instruments, and a pressure meter for measuring the liquid pressure is arranged on the pipeline after each liquid conveying pump.

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