CN219603382U - Process system for recycling ammonia nitrogen in sewage treatment - Google Patents
Process system for recycling ammonia nitrogen in sewage treatment Download PDFInfo
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- CN219603382U CN219603382U CN202320043528.1U CN202320043528U CN219603382U CN 219603382 U CN219603382 U CN 219603382U CN 202320043528 U CN202320043528 U CN 202320043528U CN 219603382 U CN219603382 U CN 219603382U
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Abstract
The utility model relates to the technical field of sewage treatment, in particular to a process system for recycling ammonia nitrogen in sewage treatment, which consists of a stripping deamination tower, a cooling tower, a recovery tower, a heat exchange tank, raw water, a pretreatment tank and a deamination effluent cooling tank, wherein the stripping deamination tower carries out deamination treatment, separated ammonia nitrogen mixed gas enters the ammonia recovery tower, cooling water condenses the mixed gas and returns condensate to the stripping deamination tower by utilizing a gas-liquid separator, and gas in the gas-liquid separator enters the ammonia recovery tower for absorption; the utility model solves the problem of low ammonia nitrogen recycling rate of deamination effluent in a stripping rectifying tower, and the technical system provides that ammonia separation efficiency is greatly accelerated by utilizing the principle that the solubility of ammonia in water is reduced under an alkaline high-temperature condition, and raw water can realize cyclic deamination and recycling of ammonia nitrogen, so that the ammonia nitrogen in the raw water effluent is greatly reduced until the emission requirement is met in a continuous deamination-absorption process.
Description
Technical Field
The utility model relates to the technical field of sewage treatment, in particular to a system for recycling ammonia nitrogen in sewage treatment.
Background
In the high ammonia nitrogen concentration percolate treatment process flow, ammonia stripping is generally adopted, and then biological treatment is carried out. The main forms of ammonia stripping at present are an aeration tank stripping method, a stripping tower and a stripping rectifying tower, wherein the former two forms are used more. The aeration tank stripping method is not suitable for treating the high ammonia nitrogen landfill leachate due to small gas-liquid contact area and low stripping efficiency. The stripping method of the stripping tower has higher removal efficiency, but has the defects of high investment and operation cost and difficult treatment of deamination tail gas.
In the existing sewage percolate treatment mode, the stripping rectifying tower can simultaneously meet the problems of high stripping efficiency and low operation cost, but in actual production, the deamination treatment of raw water in the stripping rectifying tower cannot be circularly carried out, and the single deamination treatment cannot ensure the full deamination of the raw water, so that the ammonia nitrogen content of deamination effluent in the stripping rectifying tower is still higher, and the emission requirement cannot be met.
Disclosure of Invention
The utility model aims to solve the defects in the prior art, and provides a process system for recycling ammonia nitrogen in sewage treatment.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
a process system for ammonia nitrogen recycle in sewage treatment, process system by strip deamination tower, ammonia recovery tower, gas-liquid separator, heat transfer jar, pretreatment tank, deamination play water cooling tank and cooling water tower constitute, wherein:
the inner space of the ammonia recovery tower is divided into an absorption section at the top, a condensation section in the middle and a tower kettle at the bottom: the water body circulation is kept between the absorption section at the top and the tower kettle at the bottom through a circulating pump A; the water outlet of the condensing section is communicated with the gas-liquid separator through a pipeline;
the water outlet of the stripping deamination tower is communicated with the sewage water inlet of the heat exchange tank through a liquid pipeline, steam enters the tower from the air inlet of the stripping deamination tower, and the air outlet at the top of the stripping deamination tower is connected with the condensation section through a gas phase pipeline;
the gas outlet of the gas-liquid separator is communicated with the absorption section through a gas phase pipeline, and the liquid outlet of the gas-liquid separator is used for conveying liquid to the liquid inlet at the top of the stripping deamination tower through a reflux pump;
the first cold water pipe of the cold water tower is communicated with the condensing section, and the second cold water pipe of the cold water tower and the heat exchange tank keep bidirectional circulation of water through the circulating pump B;
raw water enters a pretreatment tank and then enters a heat exchange tank through a pipeline, and a deamination sewage outlet of the heat exchange tank is communicated with a deamination effluent cooling tank.
In a preferred technical scheme, the process system further comprises a deamination water outlet tank and an ammonia water storage tank.
In a preferred technical scheme, a sewage outlet of the deamination effluent cooling tank is communicated with the deamination effluent pool through a pipeline, and deamination raw water after cooling enters the deamination effluent pool.
In a preferred technical scheme, be provided with the soft water that is used for absorbing ammonia in the absorption section, carry out the circulation through soft water and absorb ammonia, throw into the aqueous ammonia storage tank after reaching preset concentration.
In a preferred technical scheme, suspended particles in raw water are filtered out through flocculation, precipitation and filtration of the pretreatment tank.
In a preferred technical scheme, the inside of the stripping deamination tower is in a high-temperature alkaline environment, ammonia nitrogen in raw water is separated out through steam, and the ammonia nitrogen enters the ammonia recovery tower.
In a preferred technical scheme, tap water is supplied to the cooling tower.
The beneficial effects of the utility model are as follows:
1. the deamination efficiency is high, raw water can be deaminated for a plurality of times in the whole recycling process system, the raw water can realize cyclic deamination, and ammonia nitrogen in raw water effluent is greatly reduced until the emission requirement is met in the continuous deamination-absorption process, so that the ammonia nitrogen is recycled (high-concentration ammonia water is recycled), and the method has no secondary pollution and is very environment-friendly.
2. The waste heat of the deamination effluent is utilized to carry out waste heat on raw water, so that the utilization rate of heat energy can be improved, and meanwhile, the raw water which just enters the stripping deamination tower has higher temperature, so that the steam consumption can be reduced, and the running cost is saved.
3. The process flow is simple, the occupied area is small, the automation degree is high, and the operation and maintenance are convenient.
In summary, the problem of low ammonia nitrogen recycling rate of deamination effluent in the stripping rectifying tower is solved by the process system provided by the scheme, the ammonia separation efficiency is greatly accelerated by utilizing the principle that the solubility of ammonia in water is reduced under the alkaline high-temperature condition, the raw water can realize cyclic deamination, the ammonia nitrogen is recycled in the continuous deamination-absorption process, and the ammonia nitrogen of the raw water effluent is greatly reduced until the emission requirement is met, so that the process system is quite environment-friendly.
Drawings
FIG. 1 is a block diagram of a process system for ammonia nitrogen recycling in sewage treatment according to the present utility model.
In the figure: 1. stripping deamination tower; 2. an ammonia recovery tower; 21. an absorption section; 22. a condensing section; 23. a tower kettle; 3. a gas-liquid separator; 4. a reflux pump; 5. a heat exchange tank; 6. a pretreatment pool; 7. raw water; 8. deamination effluent cooling tank; 9. steam; 10. deamination effluent pool; 11. a circulating pump A; 12. a circulating pump B; 13. a cooling tower; 14. ammonia water storage tank.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments.
In this embodiment, referring to fig. 1, a process system for ammonia nitrogen recycling in sewage treatment is composed of a stripping deamination tower 1, an ammonia recovery tower 2, a gas-liquid separator 3, a heat exchange tank 5, a pretreatment tank 6, a deamination effluent cooling tank 8 and a cooling tower 13, wherein:
the internal space of the ammonia recovery tower 2 is divided into an absorption section 21 at the top, a condensation section 22 in the middle and a tower kettle 23 at the bottom: the water body circulation is kept between the absorption section 21 at the top and the tower kettle 23 at the bottom through a circulating pump A11; the water outlet of the condensing section 22 is communicated with the gas-liquid separator 3 through a pipeline.
The water outlet of the stripping deamination tower 1 is communicated with the sewage water inlet of the heat exchange tank 5 through a liquid pipeline, steam 9 enters the tower from the air inlet of the stripping deamination tower 1, the inside of the stripping deamination tower 1 is in a high-temperature alkaline environment, ammonia nitrogen in raw water 7 is separated out through the steam 9, and the ammonia nitrogen is conveyed to the condensation section 22 by utilizing a gas phase pipeline arranged at the air outlet at the top of the stripping deamination tower 1.
The gas outlet of the gas-liquid separator 3 is communicated with the absorption section 21 through a gas phase pipeline, and the liquid outlet of the gas-liquid separator 3 conveys liquid to the liquid inlet at the top of the stripping deamination tower 1 through a reflux pump 4;
tap water is supplied to the cooling tower 13, a first cooling water pipe of the cooling tower 13 is communicated with the condensing section 22, and a second cooling water pipe of the cooling tower 13 and the heat exchange tank 5 keep bidirectional circulation of water through the circulating pump B12.
Raw water 7 enters a pretreatment tank 6, and suspended particles in the raw water 7 are filtered out through flocculation, precipitation and filtration of the pretreatment tank 6. And then enters the heat exchange tank 5 through a pipeline, and the deamination sewage outlet of the heat exchange tank 5 is communicated with the deamination effluent cooling tank 8.
Also included in the process system are a deamination effluent tank 10 and an aqueous ammonia storage tank 14, wherein: the sewage outlet of the deamination effluent cooling tank 8 is communicated with the deamination effluent tank 10 through a pipeline, and deamination raw water after cooling enters the deamination effluent tank 10. The absorption section 21 is provided with soft water for absorbing ammonia gas, and the ammonia gas is circularly absorbed by the soft water and is pumped into the ammonia water storage tank 14 after reaching a preset concentration.
The reaction principle of the process system is as follows:
NH 4 + +OH - ＝NH 3 ·H 2 O
NH 3 ·H 2 O＝H 2 O+NH 3 ∈ (high temperature)
In addition, it is particularly desirable to bring the wastewater into intimate contact with the gas at high pH values, thereby reducing the ammonia concentration in the wastewater, the driving force for the mass transfer process being the difference between the partial pressure of ammonia in the gas and the equilibrium partial pressure corresponding to the concentration of ammonia in the wastewater.
The ammonia circulation working principle of the process system is as follows:
raw water 7 enters the stripping deamination tower 1 through the heat exchange tank 5 for deamination treatment, ammonia nitrogen mixed gas enters the condensation section 22 of the ammonia recovery tower 2 after deamination is finished, the condensed gas is converted into liquid to flow into the gas-liquid separator 3, gas-liquid separation is carried out in the gas-liquid separator 3, the separated ammonia gas flows into the absorption section 21 of the ammonia recovery tower 2, soft water in the absorption section 21 is utilized for absorption, and liquid in the gas-liquid separator 3 flows back to the stripping deamination tower 1 through the reflux pump 4 for concentration, and the deamination treatment steps are repeated and continued.
The water circulation working principle of the process system is as follows:
one cold water pipe of the cold water tower 13 is connected to a condensing section 22 of the ammonia recovery tower 2 to cool down and cool down the ammonia nitrogen mixed gas flowing from the stripping deamination tower 1; the other cold water pipe of the cold water tower 13 is conveyed to the heat exchange tank 5, deaminated effluent generated in the stripping deamination tower 1 enters the deamination effluent cooling tank 8 from the heat exchange tank 5, and deaminated effluent in the deamination effluent cooling tank 8 is subjected to heat exchange and cooling by using cooling water introduced from the cold water tower 13, and cooling is completed. The pipelines of the two cold water pipes are separated and are independently subjected to respective cooling operations.
The working principle of the process system is as follows:
raw water 7 enters the pretreatment tank 6 for sedimentation, suspended matters are filtered, and then the raw water 7 is sent to the heat exchange tank 5. In the initial state, no deamination water is discharged from the whole system, so that the middle water/tap water is utilized to preheat the stripping deamination tower 1, and the raw water 7 in the heat exchange tank 5 is sent to the stripping deamination tower 1 after the temperature of the stripping deamination tower 1 is raised to the design temperature; deamination treatment is carried out on raw water 7 by using fresh steam 9, high-temperature deamination effluent enters a heat exchange tank 5 and low-temperature raw water fed from a pretreatment tank 6 is preheated by using waste heat of the high-temperature deamination effluent, so that the high-temperature raw water can be used for temperature raising, and the raw water fed into a stripping deamination tower 1 is ensured to have higher temperature; the high-temperature ammonia nitrogen mixed gas enters a condensing section 22 of the ammonia gas recovery tower 2, the gas is converted into liquid after condensation and flows into a gas-liquid separator 3, ammonia gas is sent into an absorbing section 21 of the ammonia gas recovery tower 2 and absorbed into ammonia water, the ammonia water enters a tower kettle 23, the ammonia water in the tower kettle 23 is conveyed to the absorbing section 21 through a circulating pump A11, so that concentrated ammonia water can be obtained through the circulating operation, and finally the concentrated ammonia water can be pumped into an ammonia water storage tank 14 for storage. The condensed ammonia liquor is refluxed to the stripping deamination tower 1 by a reflux pump 4 for concentration treatment.
The cooling water has two paths, one is used for cooling the ammonia nitrogen mixed gas which enters the condensing section 22 after deamination, liquefying the ammonia nitrogen mixed gas into liquid and then transferring the liquid into the gas-liquid separator 3; and secondly, cooling the deamination effluent in the deamination effluent cooling tank 8, and finally pumping the deamination effluent into the deamination effluent pool 10 for storage after the deamination effluent entering the deamination effluent cooling tank 8 from the heat exchange tank 5 exchanges heat with cooling water and is cooled to a set temperature.
The foregoing is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any person skilled in the art, who is within the scope of the present utility model, should make equivalent substitutions or modifications according to the technical scheme of the present utility model and the inventive concept thereof, and should be covered by the scope of the present utility model.
Claims (7)
1. A process system for ammonia nitrogen recycle in sewage treatment, its characterized in that, process system by strip deamination tower (1), ammonia recovery tower (2), gas-liquid separator (3), heat transfer tank (5), pretreatment tank (6), deamination play water cooling tank (8) and cooling tower (13) constitute, wherein:
the internal space area of the ammonia recovery tower (2) is divided into an absorption section (21) at the top, a condensation section (22) in the middle and a tower kettle (23) at the bottom: the water circulation is kept between the absorption section (21) at the top and the tower kettle (23) at the bottom through a circulating pump A (11); the water outlet of the condensing section (22) is communicated with the gas-liquid separator (3) through a pipeline;
the water outlet of the stripping deamination tower (1) is communicated with the sewage water inlet of the heat exchange tank (5) through a liquid pipeline, steam (9) enters the tower from the air inlet of the stripping deamination tower (1), and the air outlet at the top of the stripping deamination tower (1) is connected with the condensing section (22) through a gas phase pipeline;
the gas outlet of the gas-liquid separator (3) is communicated with the absorption section (21) through a gas phase pipeline, and the liquid outlet of the gas-liquid separator (3) is used for conveying liquid to the top liquid inlet of the stripping deamination tower (1) through a reflux pump (4);
the first cold water pipe of the cold water tower (13) is communicated with the condensing section (22), and the second cold water pipe of the cold water tower (13) and the heat exchange tank (5) keep bidirectional circulation of water through the circulating pump B (12);
raw water (7) enters a pretreatment tank (6) and then enters a heat exchange tank (5) through a pipeline, and a deamination sewage outlet of the heat exchange tank (5) is communicated with a deamination effluent cooling tank (8).
2. The process system for recycling ammonia nitrogen in sewage treatment according to claim 1, wherein the process system further comprises a deamination water outlet tank (10) and an ammonia water storage tank (14).
3. The process system for recycling ammonia nitrogen in sewage treatment according to claim 2, wherein the sewage outlet of the deamination effluent cooling tank (8) is communicated with the deamination effluent pool (10) through a pipeline, and deamination raw water after cooling enters the deamination effluent pool (10).
4. The process system for recycling ammonia nitrogen in sewage treatment according to claim 2, wherein soft water for absorbing ammonia gas is arranged in the absorption section (21), the ammonia gas is circularly absorbed through the soft water, and the ammonia gas is pumped into the ammonia water storage tank (14) after reaching a preset concentration.
5. The process system for ammonia nitrogen recovery in wastewater treatment according to claim 1, characterized in that suspended particles in raw water (7) are filtered out by flocculation, sedimentation and filtration of the pretreatment tank (6).
6. The process system for recycling ammonia nitrogen in sewage treatment according to claim 1, wherein the stripping deamination tower (1) is in a high-temperature alkaline environment, ammonia nitrogen in raw water (7) is separated out through steam (9), and the ammonia nitrogen enters the ammonia recovery tower (2).
7. Process system for ammonia nitrogen recovery in sewage treatment according to claim 1, characterized in that tap water is supplied in the cold water tower (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320043528.1U CN219603382U (en) | 2023-01-09 | 2023-01-09 | Process system for recycling ammonia nitrogen in sewage treatment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320043528.1U CN219603382U (en) | 2023-01-09 | 2023-01-09 | Process system for recycling ammonia nitrogen in sewage treatment |
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| Publication Number | Publication Date |
|---|---|
| CN219603382U true CN219603382U (en) | 2023-08-29 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320043528.1U Active CN219603382U (en) | 2023-01-09 | 2023-01-09 | Process system for recycling ammonia nitrogen in sewage treatment |
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| Country | Link |
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| CN (1) | CN219603382U (en) |
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2023
- 2023-01-09 CN CN202320043528.1U patent/CN219603382U/en active Active
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