Pretreatment system for phenol ammonia semi-coke wastewater

Abstract

The utility model discloses a pretreatment system for phenol ammonia semi-coke wastewater. The pretreatment system comprises an electric flocculation air flotation machine, a coalescence oil removal device, an ammonia nitrogen stripping device, an extraction tower, an ozone oxidation device and a biochemical treatment device, the water outlet end of a wastewater incoming pipeline is communicated with a water inlet of an electric flocculation air flotation machine, a water outlet of the electric flocculation air flotation machine is communicated with a water inlet of a coalescence oil removal device through a pipeline, a water outlet of the coalescence oil removal device is communicated with a water inlet of an adjusting tank through a pipeline, and a water outlet of the adjusting tank is communicated with a water inlet of an ammonia nitrogen stripping device through a pipeline. A water outlet of the ammonia nitrogen stripping device is communicated with a water inlet of the pipeline mixer through a pipeline, a water outlet of the pipeline mixer is communicated with a feed liquid inlet of the extraction tower, a feed liquid outlet of the extraction tower is communicated with a water inlet of the ozone oxidation device through a pipeline, and a water outlet of the ozone oxidation device is communicated with a water inlet of the biochemical treatment device through a pipeline; the method has the advantages that an ammonium sulfate salt solution and a phenol sodium salt solution can be produced as byproducts, and economic benefits can be improved by sale.

Description

Technical field:

[0001] The utility model relates to a wastewater pretreatment system, in particular to a phenol-ammonia-blue charcoal wastewater pretreatment system. Background technology:

[0002] With the rapid development of the coal chemical industry, water pollution has become more and more serious. In actual projects, most phenol-ammonia charcoal wastewater treatment is still in its early stages. Due to the high cost of investment and treatment, some companies directly use phenol-ammonia charcoal wastewater for quenching. In this way, the concentration of pollutants in the circulating wastewater is getting higher and higher, making the entire plant area filled with pungent odors, which is more harmful to the ecological environment. Although a small number of companies have their own wastewater treatment facilities, due to their treatment processes or equipment, the treated effluent cannot meet the prescribed emission standards. Since the amount of this part of wastewater is large, if it is discharged without qualified treatment, it will cause great pollution to the surrounding water ecology. At the same time, because it contains high concentrations of oil, phenol, ammonia and other substances, it not only causes great pollution to the ecosystem, but also poses a threat to humans in severe cases. When conventional phenol-ammonia charcoal wastewater is used to remove emulsified oil by chemical demulsification, a large amount of chemical demulsifiers are required, and the cost of wastewater treatment is greatly increased. Utility model content:

[0003] In order to solve the above problems, the purpose of the utility model is to provide a pretreatment system for phenol-ammonia blue charcoal wastewater.

[0004] The utility model is implemented by the following technical solutions:

[0005] A pretreatment system for phenol-ammonia blue charcoal wastewater, comprising an electric flocculation flotation machine, a coalescence oil removal device, an ammonia nitrogen stripping device, an extraction tower, an ozone oxidation device and a biochemical treatment device;

[0006] The water outlet end of the wastewater pipeline is connected to the water inlet of the electric flocculation flotation machine, the water outlet of the electric flocculation flotation machine is connected to the water inlet of the coalescence and oil removal device through a pipeline, the water outlet of the coalescence and oil removal device is connected to the water inlet of the regulating tank through a pipeline, the water outlet of the regulating tank is connected to the water inlet of the ammonia nitrogen stripping device through a pipeline, the water outlet of the ammonia nitrogen stripping device is connected to the water inlet of the pipeline mixer through a pipeline, the water outlet of the pipeline mixer is connected to the feed liquid inlet of the extraction tower, the feed liquid outlet of the extraction tower is connected to the water inlet of the ozone oxidation device through a pipeline, and the water outlet of the ozone oxidation device is connected to the water inlet of the biochemical treatment device through a pipeline;

[0007] The outlet of the alkali liquid tank is communicated with the water inlet of the regulating tank through a pipeline, and the outlet of the sulfuric acid storage tank is communicated with the pipeline mixer through a pipeline.

[0008] Furthermore, the coalescence and oil removal device includes a closed oil removal cylinder, a sewage outlet is provided at the bottom of the oil removal cylinder, a coalescence device is fixedly provided in the middle of the oil removal cylinder, and a water inlet is provided on the side wall of the oil removal cylinder below the coalescence device; an oil discharge port and an exhaust port are respectively provided on the top of the oil removal cylinder, and the position height of the exhaust port is higher than the position height of the oil discharge port; a water outlet is provided on the side wall of the upper part of the oil removal cylinder; the oil discharge port is connected to the liquid inlet at the bottom of the visual oil collector through a pipeline, and an oil outlet is provided on the top of the visual oil collector.

[0009] Furthermore, a flow stabilizing baffle is provided in the oil removal cylinder above the coalescing device and below the water outlet, and a plurality of through holes are opened on the flow stabilizing baffle.

[0010] Furthermore, the coalescing device comprises a horizontally arranged fixing plate, the fixing plate is sealed and fixedly connected to the inner wall of the oil removal cylinder; a plurality of water holes are opened on the fixing plate;

[0011] A coalescing filter cartridge is fixedly provided at each water passage hole, the bottom end of the coalescing filter cartridge is fixedly connected to the fixing plate around the corresponding water passage hole, and the top end of the coalescing filter cartridge is a closed structure.

[0012] Furthermore, the water outlet of the electro-flocculation air flotation machine is connected to the water inlet ends of at least two release pipes arranged horizontally and in parallel, the release pipes are straight pipes, and the water outlet direction of the release pipes is tangent to the inner wall of the oil removal cylinder;

[0013] Water inlets corresponding to the positions of the release pipes and equal in number are provided on the side wall of the oil removal cylinder, and the water outlet ends of the release pipes are connected to the water inlets of the oil removal cylinder in a one-to-one correspondence.

[0014] Furthermore, the ammonia nitrogen stripping device comprises a blower and two stripping towers arranged in series;

[0015] The water outlet of the regulating tank is connected to the water inlet of the first-stage stripping tower through a pipeline, the water outlet of the first-stage stripping tower is connected to the water inlet of the second-stage stripping tower through a pipeline, and the water outlet of the second-stage stripping tower is connected to the water inlet of the pipeline mixer through a pipeline;

[0016] The air outlet of the fan is connected to the air inlet of the second-stage stripping tower through a pipeline, and the air outlet of the second-stage stripping tower is connected to the air inlet of the first-stage stripping tower through a pipeline.

[0017] Furthermore, the air outlet of the first-stage stripping tower is connected to the air inlet of the sulfuric acid absorption tower through a pipeline, and the liquid outlet at the bottom of the sulfuric acid absorption tower is connected to the inlet of the ammonium sulfate storage tank through a pipeline.

[0018] Furthermore, the extractant outlet of the extraction tower is connected to the feed liquid inlet of the stripping tower through a pipeline, and the feed liquid outlet of the stripping tower is connected to the inlet of the sodium phenol salt storage tank through a pipeline.

[0019] Advantages of the utility model:

[0020] Under the action of microbubbles, the electro-flocculation flotation machine can remove floating oil and part of the emulsified dispersed oil through processes such as aggregation, flotation, and scraping. The COD removal rate is about 14%, and the petroleum removal rate is about 65%. The coalescence oil removal device can discharge the separated floating oil from the upper oil collector, and the impurities are gathered at the bottom. The sewage outlet is opened regularly to discharge the impurities. The total petroleum substances in the treated water can be removed by more than 85%. The utility model can also produce ammonium sulfate salt solution and sodium phenol salt solution as by-products, which can improve the economic benefits of the enterprise through external sales. Description of the drawings:

[0021] Figure 1 is a schematic diagram of system connection of this embodiment;

[0022] Figure 2 This is a schematic diagram of the structure of the coalescence oil removal device in this embodiment;

[0023] Figure 3 for Figure 2 AA section view in.

[0024] In the figure: an electro-flocculation flotation machine 1, a coalescence oil removal device 2, an oil removal cylinder 21, a sewage outlet 22, a fixing plate 23, a water hole 24, a coalescence filter cartridge 25, a visual oil collector 26, an exhaust port 27, a water outlet 28, a release pipe 29, a flow stabilizing baffle 210, a through hole 211, a regulating tank 3, an ammonia nitrogen stripping device 4, a stripping tower 41, a fan 42, a sulfuric acid absorption tower 5, an ammonium sulfate storage tank 6, an extraction tower 7, a stripping tower 8, an ozone oxidation device 9, a biochemical treatment device 10, a wastewater pipeline 11, a pipeline mixer 12, an alkali solution tank 13, a sulfuric acid storage tank 14, and a sodium phenol salt storage tank 15. Specific implementation method:

[0025] like Figures 1 to 3 A pretreatment system for phenol-ammonia blue charcoal wastewater shown includes an electric flocculation flotation machine 1, a coalescence oil removal device 2, an ammonia nitrogen stripping device 4, an extraction tower 7, an ozone oxidation device 9 and a biochemical treatment device 10;

[0026] In this embodiment, the coalescence oil removal device 2 includes a closed oil removal cylinder 21, a sewage outlet 22 is provided at the bottom of the oil removal cylinder 21, a coalescence device is fixedly provided in the middle of the oil removal cylinder 21, and a water inlet is provided on the side wall of the oil removal cylinder 21 below the coalescence device; an oil discharge port and an exhaust port 27 are provided at the top of the oil removal cylinder 21, respectively, and the position height of the exhaust port 27 is higher than the position height of the oil discharge port; a water outlet 28 is provided on the side wall of the upper part of the oil removal cylinder 21; the oil discharge port is connected to the liquid inlet at the bottom of the visual oil collector 26 through a pipeline, and an oil outlet is provided at the top of the visual oil collector 26. A flow stabilizing baffle 210 is provided in the oil removal cylinder 21 above the coalescence device and below the water outlet 28, and a plurality of through holes 211 are provided on the flow stabilizing baffle 210.

[0027] The coalescing device includes a horizontally arranged fixed plate 23, which is sealed and fixedly connected to the inner wall of the oil removal cylinder 21; a plurality of water holes 24 are opened on the fixed plate 23; a coalescing filter cartridge 25 is fixedly arranged at each water hole 24, and the bottom end of the coalescing filter cartridge 25 is fixedly connected to the fixed plate 23 around the corresponding water hole 24, and the top end of the coalescing filter cartridge 25 is a closed structure.

[0028] The outlet of the wastewater pipeline 11 is connected to the water inlet of the electro-flocculation flotation machine 1, and the water outlet of the electro-flocculation flotation machine 1 is connected to the water inlet of at least two horizontal and parallel release pipes 29, the release pipes 29 are straight pipes, and the water outlet direction of the release pipes 29 is tangent to the inner wall of the oil removal cylinder 21; the side wall of the oil removal cylinder 21 is provided with water inlets corresponding to the positions of the release pipes 29 and equal in number, and the water outlet ends of the release pipes 29 are connected to the water inlets of the oil removal cylinder 21 one by one. The water outlet 28 of the coalescence oil removal device 2 is connected to the water inlet of the regulating tank 3 through a pipeline. The ammonia nitrogen stripping device 4 includes a blower 42 and two stripping towers 41 arranged in series; the water outlet of the regulating tank 3 is connected to the water inlet of the first-stage stripping tower 41 through a pipeline, the water outlet of the first-stage stripping tower 41 is connected to the water inlet of the second-stage stripping tower 41 through a pipeline, and the water outlet of the second-stage stripping tower 41 is connected to the water inlet of the pipeline mixer 12 through a pipeline; the air outlet of the blower 42 is connected to the air inlet of the second-stage stripping tower 41 through a pipeline, and the air outlet of the second-stage stripping tower 41 is connected to the air inlet of the first-stage stripping tower 41 through a pipeline. The air outlet of the first-stage stripping tower 41 is connected to the air inlet of the sulfuric acid absorption tower 5 through a pipeline, and the liquid outlet at the bottom of the sulfuric acid absorption tower 5 is connected to the inlet of the ammonium sulfate storage tank 6 through a pipeline.

[0029] The water outlet of the pipeline mixer 12 is connected to the feed liquid inlet of the extraction tower 7, the feed liquid outlet of the extraction tower 7 is connected to the water inlet of the ozone oxidation device 9 through a pipeline, and the water outlet of the ozone oxidation device 9 is connected to the water inlet of the biochemical treatment device 10 through a pipeline; the extractant outlet of the extraction tower 7 is connected to the feed liquid inlet of the stripping tower 8 through a pipeline, and the feed liquid outlet of the stripping tower 8 is connected to the inlet of the sodium phenol salt storage tank 15 through a pipeline.

[0030] The outlet of the alkali liquid tank 13 is communicated with the water inlet of the regulating tank 3 through a pipeline, and the outlet of the sulfuric acid storage tank 14 is communicated with the pipeline mixer 12 through a pipeline.

[0031] Job Description:

[0032] The phenol-ammonia charcoal wastewater first enters the electric flocculation flotation machine 1 and stays there for 30 minutes. Under the action of microbubbles, floating oil and part of the emulsified dispersed oil can be removed through processes such as aggregation, flotation and scraping. The COD removal rate is about 14%, and the petroleum removal rate is about 65%.

[0033] The wastewater after flotation oil removal enters the coalescence oil removal device 2. The water-blocking separation material has different wettability to the liquid. The two phases show different wetting angles on the contact surface. The oil droplets are attracted in large quantities and coarsened, so that the tiny oil particles can aggregate and grow on the surface of the separation material. When the difference in the wetting angles of the two phases in the liquid on the same surface is greater than 70 degrees, the oil droplets will float off the surface of the separation material, thereby achieving the purpose of separation. The separated floating oil is discharged from the upper visual oil collector 26, impurities gather at the bottom, and the sewage outlet 22 is opened regularly to discharge impurities. The wastewater is discharged from the outlet 28. The total petroleum substances in the water discharged from the coalescence oil removal device 2 can be removed by more than 85%.

[0034] The phenol-ammonia blue charcoal wastewater treated by coalescence and oil removal is adjusted to pH 10.5-11.5 by the regulating tank 3, and heated to 40°C at the same time. Then it is pumped into the liquid distributor of the stripping tower 41, and the air enters the air inlet below the tower body of the ammonia nitrogen stripping tower 41 under the action of the fan 42. The air blows out the free ammonia, and the water falls into the bottom of the tower and is transported to the second-stage stripping tower 41 by the feed pump to circulate this process to form a secondary stripping. In this system, the air first enters the second-stage stripping tower 41, and then enters the bottom of the first-stage stripping tower 41 from the top of the tower, and countercurrently exchanges with the phenol-ammonia blue charcoal wastewater entering the second stage from the first stage, which can improve the stripping removal rate. After stripping, the gas is led to the sulfuric acid absorption tower 5 by the pipeline; the absorption tower circulates and sprays the sulfuric acid absorption liquid, absorbs ammonia, generates about 20% ammonium sulfate, enters the ammonium sulfate storage tank 6 for temporary storage, and obtains ammonium sulfate salt after subsequent evaporation and crystallization, which can be sold, thereby improving the economic benefits. The gas absorbed by the sulfuric acid absorption tower 5 meets the emission standards, and the removal rate of ammonia nitrogen in the phenol ammonia blue charcoal wastewater after ammonia evaporation by the ammonia nitrogen stripping device 4 is about 80%.

[0035] After ammonia evaporation, the phenol-containing wastewater is added with sulfuric acid through the pipeline mixer 12 to adjust the pH to 5-6, and then pumped into the extraction tower 7. After dephenolation, the wastewater is discharged from the extraction tower 7. The phenol-containing extractant in the extraction tower 7 flows into the stripping tower 8 by gravity, and at the same time, 15% concentration of liquid alkali enters the stripping tower 8 to perform stripping and alkali washing on the phenol-containing extractant. The extractant after alkali washing returns to the extraction tower 7 for further extraction. The alkali solution can be recycled for 3-4 times (depending on the material conditions on site). After stripping, the phenol sodium salt solution with a concentration of more than 10% is temporarily stored in the phenol sodium salt storage tank 15, which can be sold for the production of crude phenol to improve economic benefits.

[0036] The dephenolized wastewater discharged from the extraction tower 7 enters the ozone oxidation device 9 for oxidation treatment for 1 hour, which can reduce the COD content in the wastewater and decompose some macromolecules into small molecules to increase the BOD / COD ratio and improve the efficiency of the subsequent biochemical system. By introducing ozone from the bottom, the oxidation of organic matter also has a secondary flotation effect, which can entrain suspended matter to rise to the surface of the water body for discharge.

[0037] The phenol-ammonia blue charcoal wastewater after ozone oxidation treatment enters the biochemical treatment device 10. The biochemical treatment device 10 adopts the "anoxic + aerobic" process, which is stable in operation, easy to operate, low in energy consumption, and has few structures. It is very effective in removing COD and ammonia nitrogen. The wastewater enters the anoxic tank together with the internal return sludge from the aerobic tank through a pump. Under anaerobic conditions, NO3--N in the return sludge undergoes denitrification reaction with the organic matter in the anoxic tank, and NO3--N is reduced to N2 and removed. The sludge return of the aerobic tank ensures that there are sufficient numbers of microorganisms in the anoxic tank and the aerobic tank, and the anoxic tank obtains the nitrate produced by nitrification in the aerobic tank. At the same time, it ensures that the anoxic tank denitrification provides sufficient carbon source so that denitrification can be carried out in the anoxic tank. The effluent after denitrification can be further degraded and nitrified by BOD in the aerobic tank. The effluent from the anoxic pool directly enters the aerobic pool. Under aerobic conditions, the biological flora has a strong COD degradation ability. At the same time, the nitrifying bacteria have a high concentration and a good nitrification effect, which can nitrify a large amount of ammonia nitrogen into nitrate nitrogen. Under the action of the aerobic pool, a large amount of organic matter and ammonia nitrogen are oxidized and degraded by microorganisms.

[0038] After being treated by the biochemical treatment device 10, the pretreatment of the phenol-ammonia blue charcoal wastewater is completed, and the effluent enters the subsequent deep treatment system.

[0039] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A pretreatment system for phenol-ammonia blue charcoal wastewater, characterized in that: It includes an electro-flocculation flotation machine, a coalescence oil removal device, an ammonia nitrogen stripping device, an extraction tower, an ozone oxidation device, and a biochemical treatment device; The water outlet end of the wastewater pipeline is connected to the water inlet of the electric flocculation flotation machine, the water outlet of the electric flocculation flotation machine is connected to the water inlet of the coalescence and oil removal device through a pipeline, the water outlet of the coalescence and oil removal device is connected to the water inlet of the regulating tank through a pipeline, the water outlet of the regulating tank is connected to the water inlet of the ammonia nitrogen stripping device through a pipeline, the water outlet of the ammonia nitrogen stripping device is connected to the water inlet of the pipeline mixer through a pipeline, the water outlet of the pipeline mixer is connected to the feed liquid inlet of the extraction tower, the feed liquid outlet of the extraction tower is connected to the water inlet of the ozone oxidation device through a pipeline, and the water outlet of the ozone oxidation device is connected to the water inlet of the biochemical treatment device through a pipeline; The outlet of the alkali liquid tank is communicated with the water inlet of the regulating tank through a pipeline, and the outlet of the sulfuric acid storage tank is communicated with the pipeline mixer through a pipeline.

2. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 1, characterized in that: The coalescence and oil removal device includes a closed oil removal cylinder, a sewage outlet is provided at the bottom of the oil removal cylinder, a coalescence device is fixedly provided in the middle of the oil removal cylinder, and a water inlet is provided on the side wall of the oil removal cylinder below the coalescence device; an oil discharge port and an exhaust port are respectively provided on the top of the oil removal cylinder, and the position height of the exhaust port is higher than the position height of the oil discharge port; a water outlet is provided on the side wall of the upper part of the oil removal cylinder; the oil discharge port is connected to the liquid inlet at the bottom of the visual oil collector through a pipeline, and an oil outlet is provided on the top of the visual oil collector.

3. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 2, characterized in that: A flow stabilizing baffle is arranged in the oil removal cylinder above the coalescing device and below the water outlet, and a plurality of through holes are opened on the flow stabilizing baffle.

4. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 2, characterized in that: The coalescing device comprises a horizontally arranged fixed plate, the fixed plate is sealed and fixedly connected to the inner wall of the oil removal cylinder; a plurality of water holes are opened on the fixed plate; A coalescing filter cartridge is fixedly provided at each water passage hole, the bottom end of the coalescing filter cartridge is fixedly connected to the fixing plate around the corresponding water passage hole, and the top end of the coalescing filter cartridge is a closed structure.

5. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 2, characterized in that: The water outlet of the electric flocculation air flotation machine is connected to the water inlet ends of at least two release pipes arranged horizontally and in parallel, the release pipes are straight pipes, and the water outlet direction of the release pipes is tangent to the inner wall of the oil removal cylinder; Water inlets corresponding to the positions of the release pipes and equal in number are provided on the side wall of the oil removal cylinder, and the water outlet ends of the release pipes are connected to the water inlets of the oil removal cylinder in a one-to-one correspondence.

6. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 1, characterized in that: The ammonia nitrogen stripping device comprises a blower and two stripping towers arranged in series; The water outlet of the regulating tank is connected to the water inlet of the first-stage stripping tower through a pipeline, the water outlet of the first-stage stripping tower is connected to the water inlet of the second-stage stripping tower through a pipeline, and the water outlet of the second-stage stripping tower is connected to the water inlet of the pipeline mixer through a pipeline; The air outlet of the fan is connected to the air inlet of the second-stage stripping tower through a pipeline, and the air outlet of the second-stage stripping tower is connected to the air inlet of the first-stage stripping tower through a pipeline.

7. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 6, characterized in that: The air outlet of the first-stage stripping tower is connected to the air inlet of the sulfuric acid absorption tower through a pipeline, and the liquid outlet at the bottom of the sulfuric acid absorption tower is connected to the inlet of the ammonium sulfate storage tank through a pipeline.

8. A pretreatment system for phenol-ammonia blue charcoal wastewater according to claim 1, characterized in that: The extractant outlet of the extraction tower is connected to the feed liquid inlet of the stripping tower through a pipeline, and the feed liquid outlet of the stripping tower is connected to the inlet of the sodium phenol salt storage tank through a pipeline.

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