CN213790774U - Coking wastewater ammonia recovery purification system - Google Patents
Coking wastewater ammonia recovery purification system Download PDFInfo
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- CN213790774U CN213790774U CN202022604581.3U CN202022604581U CN213790774U CN 213790774 U CN213790774 U CN 213790774U CN 202022604581 U CN202022604581 U CN 202022604581U CN 213790774 U CN213790774 U CN 213790774U
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Abstract
The utility model discloses a coking wastewater ammonia recovery and purification system, which comprises a raw water tank, a negative pressure desorption deamination tower, a condenser, a gas-liquid tank and a purification and purification drying device which are connected in sequence; the purification and drying device comprises at least two purification and drying units which are connected in parallel, wherein each purification and drying unit comprises a primary adsorption tank, a middle-stage adsorption tank and a high-stage adsorption tank which are sequentially connected in series; the bottom of the primary adsorption tank is provided with an air inlet pipe; the air inlet pipe is connected with an air outlet of the air liquid tank; the connecting pipelines among the primary adsorption tank, the middle-stage adsorption tank and the high-stage adsorption tank are all provided with reversing pipes, and the reversing pipes are connected with the connecting pipelines corresponding to the same stage of the other group of purification and drying units; the air outlet pipe at the top of the advanced adsorption box is connected with the vacuum air delivery pipe, and the system has simple structural design, can purify ammonia gas in multiple stages and does not need to be shut down.
Description
Technical Field
The utility model relates to a coking wastewater treatment retrieves the ammonia field, especially relates to a coking wastewater ammonia recovery purification system.
Background
The desulfurization and denitrification process needs ammonia injection, has certain requirements on the purity of ammonia (if the purity of ammonia does not meet the requirements, the desulfurization and denitrification equipment can be adversely affected), and the coal coking wastewater contains a large amount of complex organic matters, oils, cyanides, sulfides and other substances and has the characteristics of high ammonia nitrogen and high alkalinity. The ammonia nitrogen treatment can be realized by the balance of weak acid and weak base radical ions through the gas-liquid interphase partial pressure balance, so that the weak acid and weak base radical ions mutually promote the hydrolysis, and the deamination and the recycling under the in-situ PH (or a very small amount of base) are realized; however, after negative pressure deamination, ammonia-containing steam is moist and contains many impurities, the purity is not up to standard, and the ammonia-containing steam cannot be directly used for desulfurization and denitrification.
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the problem in the prior art and providing a coking wastewater ammonia recovery and purification system which has simple structural design, can purify ammonia in a multistage way and does not need to be shut down.
In order to realize the purpose of the utility model, the technical proposal of the utility model is that:
a coking wastewater ammonia recovery and purification system comprises a raw water tank, a negative pressure desorption deamination tower, a condenser, a gas-liquid tank and a purification and purification drying device which are connected in sequence; the purification and drying device comprises at least two purification and drying units which are connected in parallel, wherein each purification and drying unit comprises a primary adsorption tank, a middle-stage adsorption tank and a high-stage adsorption tank which are sequentially connected in series; the bottom of the primary adsorption tank is provided with an air inlet pipe; the air inlet pipe is connected with an air outlet of the air liquid tank; the connecting pipelines among the primary adsorption tank, the middle-stage adsorption tank and the high-stage adsorption tank are all provided with reversing pipes, and the reversing pipes are connected with the connecting pipelines corresponding to the same stage of the other group of purification and drying units; and the air outlet pipe at the top of the high-grade adsorption box is connected with a vacuum air delivery pipe.
Preferably, the air inlet pipe, the air outlet pipe, the connecting pipeline and the reversing pipe are all provided with control valves.
Preferably, activated carbon adsorption filler or zeolite adsorption filler is arranged in the primary adsorption tank.
Preferably, a primary molecular sieve adsorption filler is arranged in the middle-stage adsorption tank.
Preferably, the advanced adsorption tank is internally provided with advanced molecular sieve adsorption filler.
Preferably, the height ratio of the primary adsorption tank, the middle-stage adsorption tank and the high-stage adsorption tank is 3:2:1 or 1:1: 1.
The utility model has the advantages that:
firstly, the method comprises the following steps: the negative pressure steam stripping process is used, the steam consumption is low, the negative pressure steam stripping process is used, the operation temperature is low, and the problem of corrosion caused by high chloride ion content in raw water is solved;
secondly, the method comprises the following steps: the purification and purification drying unit is internally provided with a primary adsorption tank, a middle-grade adsorption tank and a high-grade adsorption tank in series, and the ammonia-containing steam is subjected to multi-stage adsorption, purification and drying treatment, so that the treatment effect is good, and the recycling standard can be met;
thirdly, the method comprises the following steps: the purification and purification drying units are arranged in two groups and are connected in parallel, one group is used for standby, and the machine does not need to be stopped.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
FIG. 2 is a schematic view of a purification and drying apparatus.
In the figure: 10 is raw water tank, 20 is negative pressure analysis deamination tower, 30 is condenser, 40 is gas liquid tank, 50 is purification drying device, 51 is purification drying unit, 51.1 is primary adsorption tank, 51.2 is middle stage adsorption tank, 51.3 is high stage adsorption tank, 52 is inlet pipe, 53 is connecting pipe, 54 is reversing pipe, 55 is outlet pipe, 60 is control valve.
Detailed Description
The technical solution in the embodiment of the present invention is clearly and completely described below with reference to the accompanying drawings.
A coking wastewater ammonia recovery and purification system comprises a raw water tank 10, a negative pressure desorption deamination tower 20, a condenser 30, a gas liquid tank 40 and a purification and purification drying device 50 which are connected in sequence; the purification and drying device 50 comprises at least two purification and drying units 51 connected in parallel, wherein each purification and drying unit 51 comprises a primary adsorption tank 51.1, a middle-stage adsorption tank 51.2 and a high-stage adsorption tank 51.3 which are sequentially connected in series; an air inlet pipe 52 is arranged at the bottom of the primary adsorption tank 51.1; the gas inlet pipe 52 is connected with a gas outlet of the gas-liquid tank 40; the connecting pipelines 53 among the primary adsorption tank 51.1, the middle-stage adsorption tank 51.2 and the high-stage adsorption tank 51.3 are all provided with reversing pipes 54, and the reversing pipes 54 are connected with the connecting pipelines 53 corresponding to the same stage of the other group of purification and drying units 51; and an air outlet pipe 55 at the top of the high-grade adsorption tank 51.3 is connected with a vacuum air conveying pipe.
Preferably, the air inlet pipe 52, the air outlet pipe 55, the connecting pipeline 53 and the reversing pipe 54 are all provided with control valves 60, and the control valves 60 are connected with a PLC control system, so that the whole adsorption tank can be switched for use; one or two adsorption tanks can be switched independently, and the flexibility is high.
Preferably, activated carbon adsorption packing or zeolite adsorption packing is arranged in the primary adsorption tank 51.1.
Preferably, the middle-stage adsorption tank 51.2 is internally provided with primary molecular sieve adsorption filler.
Preferably, the advanced adsorption tank 51.3 is internally provided with advanced molecular sieve adsorption filler.
Preferably, the height ratio of the primary adsorption tank 51.1, the middle-stage adsorption tank 51.2 and the high-stage adsorption tank 51.3 is 3:2:1 or 1:1: 1.
The negative pressure analysis deamination tower 20 can use a distillation tower plate, a self-cleaning mechanism and a distillation tower for preventing distillation scaling disclosed in Chinese patent CN209679534U, and can effectively prevent scaling by utilizing the distillation tower to carry out negative pressure ammonia distillation, so that shutdown cleaning is not needed, a negative pressure steam stripping process is used, the steam consumption is low, the operation temperature is low, and the problem of corrosion caused by high raw water chloride ions is solved.
The described embodiments are only some, but not all embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Claims (6)
1. The utility model provides a coking wastewater ammonia recovery purification system which characterized in that: comprises a raw water tank (10), a negative pressure desorption deamination tower (20), a condenser (30), a gas-liquid tank (40) and a purification and drying device (50) which are connected in sequence; the purification and drying device (50) comprises at least two purification and drying units (51) connected in parallel, wherein each purification and drying unit (51) comprises a primary adsorption tank (51.1), a middle-stage adsorption tank (51.2) and a high-stage adsorption tank (51.3) which are sequentially connected in series; an air inlet pipe (52) is arranged at the bottom of the primary adsorption tank (51.1); the air inlet pipe (52) is connected with an air outlet of the gas-liquid tank (40); the connecting pipelines (53) among the primary adsorption tank (51.1), the middle-stage adsorption tank (51.2) and the high-stage adsorption tank (51.3) are all provided with reversing pipes (54), and the reversing pipes (54) are connected with the connecting pipelines (53) corresponding to the same stage of the other group of purification and drying units (51); an air outlet pipe (55) at the top of the high-grade adsorption tank (51.3) is connected with a vacuum air conveying pipe.
2. The coking wastewater ammonia gas recovery and purification system according to claim 1, which is characterized in that: and the air inlet pipe (52), the air outlet pipe (55), the connecting pipeline (53) and the reversing pipe (54) are all provided with control valves (60).
3. The coking wastewater ammonia gas recovery and purification system according to claim 1, which is characterized in that: and active carbon adsorption filler or zeolite adsorption filler is arranged in the primary adsorption tank (51.1).
4. The coking wastewater ammonia gas recovery and purification system according to claim 1, which is characterized in that: and primary molecular sieve adsorption filler is arranged in the middle-stage adsorption tank (51.2).
5. The coking wastewater ammonia gas recovery and purification system according to claim 1, which is characterized in that: and a high-grade molecular sieve adsorption filler is arranged in the high-grade adsorption box (51.3).
6. The coking wastewater ammonia gas recovery and purification system according to claim 1, which is characterized in that: the height ratio of the primary adsorption tank (51.1), the middle-stage adsorption tank (51.2) and the high-stage adsorption tank (51.3) is 3:2:1 or 1:1: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022604581.3U CN213790774U (en) | 2020-11-12 | 2020-11-12 | Coking wastewater ammonia recovery purification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022604581.3U CN213790774U (en) | 2020-11-12 | 2020-11-12 | Coking wastewater ammonia recovery purification system |
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| Publication Number | Publication Date |
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| CN213790774U true CN213790774U (en) | 2021-07-27 |
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| CN202022604581.3U Active CN213790774U (en) | 2020-11-12 | 2020-11-12 | Coking wastewater ammonia recovery purification system |
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| CN (1) | CN213790774U (en) |
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- 2020-11-12 CN CN202022604581.3U patent/CN213790774U/en active Active
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