CN111635086A - Zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater and treatment process thereof - Google Patents
Zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater and treatment process thereof Download PDFInfo
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- CN111635086A CN111635086A CN202010672849.9A CN202010672849A CN111635086A CN 111635086 A CN111635086 A CN 111635086A CN 202010672849 A CN202010672849 A CN 202010672849A CN 111635086 A CN111635086 A CN 111635086A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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Abstract
The invention belongs to the technical field of sewage treatment, and discloses a zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater. The PH of the wastewater containing ammonia nitrogen is adjusted to 10-13 by adding alkali, the ammonia nitrogen in the wastewater is converted into free ammonia NH3, then large particles and insoluble suspended matters generated by the alkali adding reaction are separated by precipitation, the supernatant enters a deamination nitrogen membrane group, free ammonia diffuses out through membrane pores to form an ammonium salt solution with an absorption liquid outside the membrane, the absorption liquid is adjusted to be neutral by the PH, distilled water and ammonium salt are separated by evaporation crystallization, the ammonium salt can realize product level recycling, the deamination wastewater can reach the discharge standard, the investment operation cost is low, the operation is stable, the energy consumption is low, the problem of secondary pollution is avoided, the resource utilization of the wastewater containing ammonia nitrogen and the zero discharge of the wastewater containing ammonia nitrogen are realized, and the method is worthy of popularization.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater and a treatment process thereof.
Background
With the rapid development of industry and agriculture, the content of ammonia nitrogen in wastewater generated by industries such as chemical fertilizers, coking, petrifaction, pharmacy, foods, refuse landfills and the like is over standard gradually, the ammonia nitrogen in the wastewater is a main reason for water body nutrition and environmental pollution, the ammonia nitrogen is a main object for polluting a water body, and a large amount of oxygen is consumed during the oxidation and decomposition of the ammonia nitrogen, so that the content of dissolved oxygen in the water is reduced, the normal growth of aquatic animals is threatened, and even death can be caused. Ammonia nitrogen is oxidized into nitrite nitrogen under the action of microorganisms, and then the nitrite nitrogen is combined with protein to generate nitrosamine, and if the nitrosamine enters a human body through aquatic organisms, carcinogenic and teratogenic threats exist. Therefore, the national requirements require that ammonia nitrogen-containing wastewater can be discharged only after being subjected to ammonia nitrogen removal treatment and meeting the discharge indexes of ammonia nitrogen-containing wastewater in the current relevant environmental protection standards in China, such as the surface water environment quality standard, the underground water environment quality standard, the sewage comprehensive discharge standard and the relevant industry type water pollutant discharge standard.
Various ammonia nitrogen removal technologies adopted at present comprise a chemical method, a biological method, a physical method, a physicochemical biological combination method and other processes for treating ammonia nitrogen in wastewater, and most of the methods have the problems of investment, operation cost, secondary pollution and the like.
Disclosure of Invention
1. Technical problem to be solved
Aiming at the problems in the prior art, the invention aims to provide a zero discharge system for producing ammonium salt from ammonia-nitrogen-containing wastewater and a treatment process thereof, belonging to a physicochemical combination method, and having the advantages of low investment and operation cost, stable operation and low energy consumption.
2. Technical scheme
In order to solve the above problems, the present invention adopts the following technical solutions.
A zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater comprises a PH regulating zone I, a precipitation separation zone, a sand filtering zone, an ammonia nitrogen removal membrane zone, a PH regulating zone II and an evaporation crystallization zone which are sequentially communicated through pipelines;
the PH adjusting area comprises a raw material tank, the raw material tank is communicated with a PH adjusting tank through a pipeline, a raw material conveying pump is arranged on the pipeline connecting the raw material tank with the PH adjusting tank, a first alkali liquor tank is arranged on one side of the PH adjusting tank, the first alkali liquor tank is communicated with the PH adjusting tank through a pipeline, and a first alkali liquor conveying pump is arranged on the pipeline connecting the PH adjusting tank with the first alkali liquor tank;
the sedimentation separation zone comprises an inclined plate sedimentation tank, the PH adjusting tank is communicated with the inclined plate sedimentation tank, the bottom of the inclined plate sedimentation tank is communicated with a sludge conveying pipe, a sludge conveying pump is arranged on the sludge conveying pipe, and one end of the sludge conveying pipe, which is far away from the inclined plate sedimentation tank, is communicated with a filter press;
the sand filtration zone comprises a buffer tank, the buffer tank is communicated with the inclined plate sedimentation tank through a pipeline, the output end of the buffer tank is communicated with a sand filtration tank through a pipeline, a buffer delivery pump is arranged on the pipeline connecting the buffer tank and the sand filtration tank, the output end of the sand filtration tank is communicated with a middle buffer tank through a pipeline, and an MBR membrane group is arranged in the middle buffer tank;
the ammonia nitrogen removal membrane group comprises an ammonia nitrogen removal membrane group, the input end of the ammonia nitrogen removal membrane group is communicated with the MBR membrane group through a pipeline, a cache delivery pump is arranged on the pipeline connecting the ammonia nitrogen removal membrane group and the MBR membrane group, the input end of the ammonia nitrogen removal membrane group is communicated with an absorption liquid pipe, an absorption liquid pump is arranged on the absorption liquid pipe, one end, far away from the ammonia nitrogen removal membrane group, of the absorption liquid pipe is communicated with an absorption liquid tank, and the output end of the ammonia nitrogen removal membrane group is communicated with an ammonia nitrogen removal wastewater discharge pipe;
the pH adjusting area II comprises an ammonium salt water storage tank, a second alkali liquor tank is arranged on one side of the ammonium salt water storage tank and is communicated with the ammonium salt water storage tank through a pipeline, and a second alkali liquor delivery pump is arranged on the pipeline through which the second alkali liquor tank is communicated with the ammonium salt water storage tank;
the evaporative crystallization area comprises a heater, a crystallization separator, a steam compressor and a distilled water tank, the heater is connected with an ammonium salt water storage tank through a pipeline, an ammonium salt water delivery pump is arranged on the ammonium salt water storage tank and a pipeline connected with the heater, the crystallization separator and the steam compressor are connected through a pipeline, the distilled water tank is connected with the heater through a pipeline, the distilled water discharge pipe is communicated with the output end of the distilled water tank, the distilled water delivery pump is arranged on the distilled water discharge pipe, the output end of the crystallization separator is communicated with a return pipe, a heating circulating pump is arranged on the return pipe, the output end of the crystallization separator is communicated with a discharge pipe, the discharge pipe is provided with a discharge pump, and one end of the discharge pipe, far away from the crystallization separator, is.
Preferably, a stirrer is arranged in the pH adjusting tank.
The invention aims to solve another technical problem of providing a treatment process of a zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater, which comprises the following steps:
s1, PH regulation: conveying the ammonia nitrogen-containing wastewater in the raw material tank into the PH regulating tank through a raw material conveying pump, simultaneously adding alkali liquor in a first alkali liquor tank into the PH regulating tank through a first alkali liquor conveying pump, controlling the ratio of the alkali liquor to ammonia nitrogen in the ammonia nitrogen-containing wastewater to be 1:1.3, uniformly stirring by using a stirrer, and regulating the PH to be 11-13 so as to convert most of the ammonia nitrogen into free gaseous ammonia NH 3;
s2, coagulating sedimentation; after the pH of the wastewater containing ammonia nitrogen is regulated and stabilized, the wastewater enters the inclined plate sedimentation tank, the flow speed of the wastewater is controlled to be 0.5-5mm/s, large particles and insoluble suspended matters formed by the sewage after the alkali is added enter a sedimentation tank, are separated by gravity sedimentation, are pumped out of sludge by a sludge conveying pump, are treated by a filter press and then are discharged out of a system, and supernatant enters a sand filtration zone;
s3, sand filtration: the supernatant enters the sand filtering area, is treated by the sand filtering tank and reduces the concentration of suspended solid in the wastewater to below 10 ppm;
s4, MBR membrane filtration: the wastewater treated in the step S3 enters an intermediate buffer tank and is filtered by an MBR membrane group, so that the concentration of suspended solid in the wastewater is reduced to below 1ppm, and the ammonia nitrogen removal membrane is prevented from being blocked;
s5, deamination nitrogen film: the ammonia nitrogen is treated in the step S4 and then is conveyed into a ammonia nitrogen removal film of the ammonia nitrogen removal film group through the buffer conveying pump, meanwhile, absorption liquid in an absorption liquid tank is introduced to the outer side of the ammonia nitrogen removal film through an absorption liquid pump, free gaseous ammonia NH3 in the wastewater enters the absorption liquid through the film wall to form an ammonium salt solution together with the absorption liquid, and the wastewater after ammonia nitrogen removal is discharged out of the system through an ammonia nitrogen removal wastewater discharge pipe;
s6, PH regulation: conveying the ammonium salt solution formed in the step S5 into the ammonium salt water storage tank through a pipeline, adding alkali liquor in a second alkali liquor tank into the ammonium salt water storage tank through a second alkali liquor conveying pump, and enabling the acidic ammonium salt solution PH to be neutral and then enter an evaporation crystallization area;
s7, evaporative crystallization: and (4) allowing the wastewater with the PH adjusted in the step S6 to enter an evaporative crystallization area for evaporative crystallization, separating inorganic ammonium salt in the wastewater by using a centrifugal machine, wherein the ammonium salt can be prepared into a product for recycling, and discharging distilled water out of the system through a distilled water discharge pipe.
Preferably, the pH adjustment in step S1 is performed by using sodium hydroxide or Ca (OH) with a concentration of 10-35%2The pH of the alkaline solution or the two solutions is adjusted in stages.
Preferably, the absorption liquid in step S5 is a mixture of one or more of sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, hydrofluoric acid, and oxalic acid with a concentration of 5% to 25%.
Preferably, the membrane component of the deammoniation and nitrogen removal membrane group is a hydrophobic microporous hollow fiber membrane, and the membrane material is a high polymer material and comprises one or a mixture of polytetrafluoroethylene, polypropylene and polyethylene.
Preferably, in step S6, the PH adjustment is performed by using an ammonia solution with a concentration of 5% to 25%.
Preferably, the evaporative crystallization adopts a multi-effect evaporative crystallization or MVR evaporative crystallization system.
3. Advantageous effects
Compared with the prior art, the invention has the advantages that:
(1) the method comprises the steps of firstly, carrying out PH regulation on raw water, and regulating ammonia nitrogen and sodium hydroxide in the raw water to ensure that the raw water has stable alkalinity, most of the ammonia nitrogen in the wastewater is converted into free gaseous ammonia NH3 to exist, and impurities and insoluble suspended matters in the raw water can form precipitates and insoluble suspended matters with the sodium hydroxide;
(2) impurities in raw water after water quality adjustment and precipitates generated by reaction are subjected to coagulating sedimentation for further separation, and SS of overflow supernatant is subjected to primary separation;
(3) the method further reduces the SS of the overflowed supernatant fluid, ensures the continuous operation of the subsequent process, further filters most suspended matters through sand filtration to control the SS of the effluent to be below 10ppm, and further filters the effluent to enter an MBR membrane;
(4) the invention adopts the MBR membrane filtering unit as a security system of the deamination nitrogen membrane, reduces SS in the wastewater to 1ppm, and ensures that the deamination nitrogen membrane is not blocked;
(5) the invention adopts the ammonia nitrogen removal membrane technology, does not adopt the traditional blowing process, can reduce the investment and the operation cost, has high removal rate of the ammonia nitrogen of the effluent, does not have the problem of secondary pollution, adopts the ammonia nitrogen removal membrane method to isolate the influence of the water quality of the original water on the absorption liquid, thereby ensuring the quality of the ammonium salt and ensuring that the ammonium salt can reach the product grade;
(6) the method adopts a PH (potential of hydrogen) adjustment technology, adopts ammonia water for adjusting the PH of the acidic absorption liquid, and is also used for ensuring the quality of the formed ammonium salt solution, and the PH value is adjusted to ensure the stable operation of a subsequent evaporator;
(7) according to the invention, an MVR forced circulation evaporation crystallization technology is adopted, inorganic ammonium salt in the wastewater is separated by a centrifuge after an ammonium salt solution is evaporated to reach a saturated solution, the ammonium salt can be recycled at a product level, and evaporated distilled water can reach the standard after being cooled and then is discharged;
in conclusion, the zero discharge system and the treatment process for producing ammonium salt from ammonia nitrogen-containing wastewater belong to a physicochemical combination method, have the advantages of low investment and operation cost, stable operation, low energy consumption and no secondary pollution, realize the resource utilization of ammonia nitrogen-containing wastewater and the zero discharge of ammonia nitrogen-containing wastewater, and are worthy of popularization.
Drawings
FIG. 1 is a system diagram of the present invention;
FIG. 2 is a process flow diagram of the present invention.
The reference numbers in the figures illustrate:
1. a raw material tank; 2. a pH adjusting tank; 3. a raw material delivery pump; 4. a first lye tank; 5. a stirrer; 6. a first alkali liquor delivery pump; 7. a sloping plate sedimentation tank; 8. a sludge delivery pump; 9. a filter press; 10. a buffer tank; 11. a sand filtration tank; 12. a buffer delivery pump; 13. an intermediate buffer tank; 14. MBR membrane group; 15. a deamination nitrogen membrane group; 16. a buffer delivery pump; 17. an absorption liquid pump; 18. an absorption liquid tank; 19. a discharge pipe for the ammonia nitrogen wastewater; 20. an ammonium salt water storage tank; 21. a second lye tank; 22. a second lye delivery pump; 23. a heater; 24. a crystallization separator; 25. a vapor compressor; 26. a distilled water tank; 27. a distilled water discharge pipe; 28. a distilled water delivery pump; 29. heating the circulating pump; 30. a discharge pump; 31. a centrifuge; 32. ammonium salt water delivery pump.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention; it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments, and all other embodiments obtained by those skilled in the art without any inventive work are within the scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", "top/bottom", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "disposed," "sleeved/connected," "connected," and the like are to be construed broadly, e.g., "connected," which may be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Referring to fig. 1-2, a zero discharge system for ammonium salt production from ammonia nitrogen-containing wastewater comprises a PH adjusting zone i, a precipitation separation zone, a sand filtration zone, a deamination nitrogen membrane zone, a PH adjusting zone ii and an evaporation crystallization zone which are sequentially communicated through a pipeline;
the PH adjusting area comprises a raw material tank 1, the raw material tank 1 is communicated with a PH adjusting pool 2 through a pipeline, a raw material conveying pump 3 is arranged on the pipeline connecting the raw material tank 1 and the PH adjusting pool 2, a first alkali liquor tank 4 is arranged on one side of the PH adjusting pool 2, the first alkali liquor tank 4 is communicated with the PH adjusting pool 2 through a pipeline, a first alkali liquor conveying pump 6 is arranged on the pipeline connecting the PH adjusting pool 2 and the first alkali liquor tank 4, and a PH meter is arranged in the PH adjusting pool 2, so that the actual PH value is fed back;
the precipitation separation zone comprises an inclined plate precipitation tank 7, the PH adjusting tank 2 is communicated with the inclined plate precipitation tank 7, the bottom of the inclined plate precipitation tank 7 is communicated with a sludge conveying pipe, a sludge conveying pump 8 is arranged on the sludge conveying pipe, and one end of the sludge conveying pipe, which is far away from the inclined plate precipitation tank 7, is communicated with a filter press 9;
the sand filtering area comprises a buffer tank 10, the buffer tank 10 is communicated with the inclined plate precipitation tank 7 through a pipeline, the output end of the buffer tank 10 is communicated with a sand filtering tank 11 through a pipeline, a buffer delivery pump 12 is arranged on the pipeline connecting the buffer tank 10 and the sand filtering tank 11, the output end of the sand filtering tank 11 is communicated with an intermediate buffer tank 13 through a pipeline, and an MBR membrane group 14 is arranged in the intermediate buffer tank 13;
the deammoniation nitrogen membrane module comprises a deammoniation nitrogen membrane module 15, the input end of the deammoniation nitrogen membrane module 15 is communicated with an MBR membrane module 14 through a pipeline, a cache delivery pump 16 is arranged on the pipeline connecting the deammoniation nitrogen membrane module 15 and the MBR membrane module 14, the input end of the deammoniation nitrogen membrane module 15 is communicated with an absorption liquid pipe, an absorption liquid pump 17 is arranged on the absorption liquid pipe, one end, far away from the deammoniation nitrogen membrane module 15, of the absorption liquid pipe is communicated with an absorption liquid tank 18, the output end of the deammoniation nitrogen membrane module 15 is communicated with a deammoniation nitrogen wastewater discharge pipe 19, and an ammonia nitrogen monitoring device;
the PH adjusting area II comprises an ammonium salt water storage tank 20, a second alkali liquor tank 21 is arranged on one side of the ammonium salt water storage tank 20, the second alkali liquor tank 21 is communicated with the ammonium salt water storage tank 20 through a pipeline, and a second alkali liquor delivery pump 22 is arranged on the pipeline through which the second alkali liquor tank 21 is communicated with the ammonium salt water storage tank 20;
the evaporative crystallization area comprises a heater 23, a crystallization separator 24, a vapor compressor 25 and a distilled water tank 26, the heater 23 is connected with an ammonium salt water storage tank 20 through a pipeline, an ammonium salt water delivery pump 32 is arranged on the pipeline connecting the ammonium salt water storage tank 20 and the heater 23, the crystallization separator 24 and the vapor compressor 25 are connected through a pipeline, the distilled water tank 26 is connected with the heater 23 through a pipeline, the output end of the distilled water tank 26 is communicated with a distilled water discharge pipe 27, the distilled water discharge pipe 27 is provided with a distilled water delivery pump 28, the output end of the crystallization separator 24 is communicated with a return pipe, the return pipe is provided with a heating circulating pump 29, the output end of the crystallization separator 24 is communicated with a discharge pipe, the discharge pipe is provided with a discharge pump 30, and one end of the discharge pipe.
Further, a stirrer 5 is arranged in the pH adjusting tank 2.
The invention aims to solve another technical problem of providing a treatment process of a zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater, which comprises the following steps:
s1, PH regulation: conveying the ammonia nitrogen-containing wastewater in the raw material tank 1 into a PH adjusting tank 2 through a raw material conveying pump 3, simultaneously adding alkali liquor in a first alkali liquor tank 4 into the PH adjusting tank 2 through a first alkali liquor conveying pump 6, controlling the ratio of the alkali liquor to ammonia nitrogen in the ammonia nitrogen-containing wastewater to be 1:1.3, uniformly stirring by using a stirrer 5, adjusting the PH to 11-13, and converting most of the ammonia nitrogen into free gaseous ammonia NH 3;
s2, coagulating sedimentation; after the pH of the wastewater containing ammonia nitrogen is regulated and stabilized, the wastewater enters an inclined plate sedimentation tank 7, the flow speed of the wastewater is controlled to be 0.5-5mm/s, large particles and insoluble suspended matters formed by the sewage after the addition of alkali enter a sedimentation tank, are separated by gravity sedimentation, sludge is pumped out by a sludge delivery pump 8, is treated by a filter press 9 and then is discharged out of a system, and supernatant enters a sand filtration zone;
s3, sand filtration: the supernatant fluid enters a sand filtering area and is treated by a sand filtering tank 11, and the concentration of suspended solid in the wastewater is reduced to below 10 ppm;
s4, MBR membrane filtration: the wastewater treated in the step S3 enters an intermediate buffer tank 13 and is filtered by an MBR membrane group 14, so that the concentration of suspended solid in the wastewater is reduced to below 1ppm, and the ammonia nitrogen removal membrane is prevented from being blocked;
s5, deamination nitrogen film: the ammonia nitrogen removal wastewater is treated in the step S4 and then is conveyed into the ammonia nitrogen removal membrane of the ammonia nitrogen removal membrane group 15 through the buffer conveying pump 16, meanwhile, absorption liquid in the absorption liquid tank 18 is introduced to the outer side of the ammonia nitrogen removal membrane through the absorption liquid pump 17, free gaseous ammonia NH3 in the wastewater enters the absorption liquid through the membrane wall and forms an ammonium salt solution with the absorption liquid, the wastewater after ammonia nitrogen removal is discharged out of the system through the ammonia nitrogen removal wastewater discharge pipe 19, and the working principle of the ammonia nitrogen removal membrane is based on the hydrophobicity and air permeability of a hollow fiber membrane, namely, the desorption process of the characteristic that gas can permeate the membrane surface but liquid cannot permeate the membrane under certain conditions.
S6, PH regulation: conveying the ammonium salt solution formed in the step S5 into an ammonium salt water storage tank 20 through a pipeline, simultaneously adding alkali liquor in a second alkali liquor tank 21 into the ammonium salt water storage tank 20 through a second alkali liquor conveying pump 22, and enabling the acidic ammonium salt solution PH to enter an evaporation crystallization area after being neutralized;
s7, evaporative crystallization: and (4) allowing the wastewater with the PH adjusted in the step S6 to enter an evaporative crystallization area for evaporative crystallization, separating inorganic ammonium salt in the wastewater by using a centrifuge 31, wherein the ammonium salt can be prepared into a product for recycling, and discharging distilled water out of the system through a distilled water discharge pipe 27.
Further, step S1PH is to adjust the concentration of sodium hydroxide or Ca (OH) with the concentration of 10-35%2The pH of the alkaline solution or the two solutions is adjusted in stages.
Further, in the step S5, the absorption liquid is a mixture of one or more of sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, hydrofluoric acid, and oxalic acid with a concentration of 5% to 25%.
Further, the membrane module of the deammoniation and denitrification membrane module 15 is a hydrophobic microporous hollow fiber membrane, and the membrane material is a high molecular material, including one or more of polytetrafluoroethylene, polypropylene, and polyethylene.
Further, in step S6PH, an ammonia solution with a concentration of 5% to 25% is used.
Furthermore, the evaporative crystallization adopts a multi-effect evaporative crystallization or MVR evaporative crystallization system.
The working principle is as follows: the ammonia nitrogen-containing wastewater generated in the production process is firstly collected into a raw material tank 1, the wastewater is pumped into a PH regulating pool 2 through a raw material conveying pump 3, alkali liquor in a first alkali liquor tank 4 is added into the PH regulating pool 2 through a first alkali liquor conveying pump 6, the raw liquor is uniformly mixed under the stirring of a stirrer 5 in the PH regulating pool 2, the actual PH value is fed back through PH meter time, the PH value is stabilized between 10 and 13, the wastewater is pumped into an inclined plate precipitation tank 7 through a conveying pump, large particles and insoluble suspended matters generated by reaction with the alkali liquor are settled to the bottom of the pool through gravity, supernatant is pumped into a nitrogen membrane group 15 through the conveying pump, free NH3 reaches the outer side of the membrane through membrane holes and forms an ammonium salt solution with absorption liquid, the wastewater after ammonia nitrogen removal passes through a ammonia nitrogen-containing wastewater discharge pipe 19, an outlet ammonia nitrogen monitoring device monitors the water quality in real time and reaches the standard discharge, the ammonium salt solution enters an ammonium salt, and adjusting the pH value to be neutral, pumping the pH value into an evaporative crystallization area through an ammonium salt water delivery pump 32 for evaporative crystallization, removing inorganic salt to prepare ammonia fertilizer, and discharging distilled water up to the standard to realize resource utilization of the ammonia nitrogen-containing wastewater.
The foregoing is only a preferred embodiment of the present invention; the scope of the invention is not limited thereto. Any person skilled in the art should be able to cover the technical scope of the present invention by equivalent or modified solutions and modifications within the technical scope of the present invention.
Claims (8)
1. The utility model provides an contain ammonia nitrogen waste water production ammonium salt zero discharge system which characterized in that: comprises a PH adjusting area I, a precipitation separation area, a sand filtering area, a deamination nitrogen film area, a PH adjusting area II and an evaporation crystallization area which are sequentially communicated through pipelines;
the PH adjusting area comprises a raw material tank (1), the raw material tank (1) is communicated with a PH adjusting tank (2) through a pipeline, a raw material conveying pump (3) is arranged on the pipeline connecting the raw material tank (1) and the PH adjusting tank (2), a first alkali liquor tank (4) is arranged on one side of the PH adjusting tank (2), the first alkali liquor tank (4) is communicated with the PH adjusting tank (2) through a pipeline, and a first alkali liquor conveying pump (6) is arranged on the pipeline connecting the PH adjusting tank (2) and the first alkali liquor tank (4);
the sedimentation separation zone comprises an inclined plate sedimentation tank (7), the PH adjusting tank (2) is communicated with the inclined plate sedimentation tank (7), the bottom of the inclined plate sedimentation tank (7) is communicated with a sludge conveying pipe, a sludge conveying pump (8) is arranged on the sludge conveying pipe, and one end of the sludge conveying pipe, which is far away from the inclined plate sedimentation tank (7), is communicated with a filter press (9);
the sand filtration area comprises a buffer tank (10), the buffer tank (10) is communicated with an inclined plate precipitation tank (7) through a pipeline, the output end of the buffer tank (10) is communicated with a sand filtration tank (11) through a pipeline, a buffer delivery pump (12) is arranged on the pipeline connecting the buffer tank (10) and the sand filtration tank (11), the output end of the sand filtration tank (11) is communicated with a middle buffer tank (13) through a pipeline, and an MBR membrane group (14) is arranged in the middle buffer tank (13);
the ammonia nitrogen removal membrane group comprises an ammonia nitrogen removal membrane group (15), the input end of the ammonia nitrogen removal membrane group (15) is communicated with an MBR membrane group (14) through a pipeline, a cache delivery pump (16) is arranged on the pipeline connecting the ammonia nitrogen removal membrane group (15) and the MBR membrane group (14), the input end of the ammonia nitrogen removal membrane group (15) is communicated with an absorption liquid pipe, an absorption liquid pump (17) is arranged on the absorption liquid pipe, one end, far away from the ammonia nitrogen removal membrane group (15), of the absorption liquid pipe is communicated with an absorption liquid tank (18), and the output end of the ammonia nitrogen removal membrane group (15) is communicated with an ammonia nitrogen removal wastewater discharge pipe (19);
the PH adjusting area II comprises an ammonium salt water storage tank (20), a second alkali liquor tank (21) is arranged on one side of the ammonium salt water storage tank (20), the second alkali liquor tank (21) is communicated with the ammonium salt water storage tank (20) through a pipeline, and a second alkali liquor conveying pump (22) is arranged on the pipeline through which the second alkali liquor tank (21) is communicated with the ammonium salt water storage tank (20);
the evaporative crystallization area comprises a heater (23), a crystallization separator (24), a steam compressor (25) and a distilled water tank (26), the heater (23) is connected with an ammonium salt water storage tank (20) through a pipeline, an ammonium salt water delivery pump (32) is arranged on the pipeline connecting the ammonium salt water storage tank (20) and the heater (23), the crystallization separator (24) and the steam compressor (25) are connected through a pipeline, the distilled water tank (26) is connected with the heater (23) through a pipeline, the output end of the distilled water tank (26) is communicated with a distilled water discharge pipe (27), the distilled water discharge pipe (27) is provided with a distilled water delivery pump (28), the output end of the crystallization separator (24) is communicated with a return pipe, the return pipe is provided with a heating circulating pump (29), the output end of the crystallization separator (24) is communicated with a discharge pipe, the discharge pipe is provided with a discharge pump (30), and one end of the discharge pipe, which is far away from the crystallization separator (24), is communicated with a centrifugal machine (31).
2. The system for zero discharge of ammonium salt production from ammonia-nitrogen containing wastewater according to claim 1, characterized in that: and a stirrer (5) is arranged in the PH adjusting tank (2).
3. The treatment process of the zero discharge system for producing ammonium salt from ammonia nitrogen-containing wastewater according to claims 1-2, characterized in that: the method comprises the following steps:
s1, PH regulation: conveying the ammonia nitrogen-containing wastewater in the raw material tank (1) into the PH adjusting tank (2) through a raw material conveying pump (3), simultaneously adding alkali liquor in a first alkali liquor tank (4) into the PH adjusting tank (2) through a first alkali liquor conveying pump (6), controlling the ratio of the alkali liquor to ammonia nitrogen in the ammonia nitrogen-containing wastewater to be 1:1.3, uniformly stirring by using a stirrer (5), and adjusting the PH to 11-13 to convert most of the ammonia nitrogen into free gaseous ammonia NH 3;
s2, coagulating sedimentation; after the pH value of the wastewater containing ammonia nitrogen is regulated and stabilized, the wastewater enters an inclined plate sedimentation tank (7), the flow speed of the wastewater is controlled to be 0.5-5mm/s, large particles and insoluble suspended matters formed by the sewage after the alkali is added enter a sedimentation tank for separation through gravity sedimentation, sludge is pumped out through a sludge delivery pump (8), the sludge is discharged out of a system after being treated by a filter press (9), and supernatant enters a sand filtration zone;
s3, sand filtration: the supernatant enters the sand filtering area, is treated by the sand filtering tank (11) and reduces the concentration of suspended solid in the wastewater to below 10 ppm;
s4, MBR membrane filtration: the wastewater treated in the step S3 enters an intermediate buffer tank (13) and is filtered by an MBR membrane group (14), so that the concentration of suspended solid in the wastewater is reduced to below 1ppm, and the ammonia nitrogen removal membrane is prevented from being blocked;
s5, deamination nitrogen film: the ammonia nitrogen is treated in the step S4 and then is conveyed into a ammonia nitrogen removal film of the ammonia nitrogen removal film group (15) by the buffer conveying pump (16), meanwhile, absorption liquid in the absorption liquid tank (18) is introduced into the outer side of the ammonia nitrogen removal film by the absorption liquid pump (17), free gaseous ammonia NH3 in the wastewater enters the absorption liquid through the film wall to form an ammonium salt solution with the absorption liquid, and the wastewater after ammonia nitrogen removal is discharged out of the system through an ammonia nitrogen removal wastewater discharge pipe (19);
s6, PH regulation: conveying the ammonium salt solution formed in the step S5 into the ammonium salt water storage tank (20) through a pipeline, simultaneously adding alkali liquor in a second alkali liquor tank (21) into the ammonium salt water storage tank (20) through a second alkali liquor conveying pump (22), and entering an evaporation crystallization area after the pH value of the acidic ammonium salt solution is neutral;
s7, evaporative crystallization: and (3) the wastewater with the PH adjusted in the step S6 enters an evaporative crystallization area for evaporative crystallization, inorganic ammonium salt in the wastewater is separated by a centrifuge (31), the ammonium salt can be made into a product for recycling, and distilled water is discharged out of the system through a distilled water discharge pipe (27).
4. The treatment process of the zero discharge system for producing ammonium salt from ammonia-nitrogen containing wastewater according to claim 3, characterized in that: step S1 the pH adjustment is performed by using 10-35% sodium hydroxide or Ca (OH)2The pH of the alkaline solution or the two solutions is adjusted in stages.
5. The treatment process of the zero discharge system for producing ammonium salt from ammonia-nitrogen containing wastewater according to claim 3, characterized in that: and step S5, the absorption liquid is one or more of sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, hydrofluoric acid and oxalic acid with the concentration of 5% -25%.
6. The treatment process of the zero discharge system for producing ammonium salt from ammonia-nitrogen containing wastewater according to claim 3, characterized in that: the membrane component of the deammoniation and nitrogen removal membrane group (15) is a hydrophobic microporous hollow fiber membrane, and the membrane material is a high polymer material and comprises one or a mixture of polytetrafluoroethylene, polypropylene and polyethylene.
7. The treatment process of the zero discharge system for producing ammonium salt from ammonia-nitrogen containing wastewater according to claim 3, characterized in that: in the step S6, an ammonia solution with a concentration of 5% -25% is used for pH adjustment.
8. The treatment process of the zero discharge system for producing ammonium salt from ammonia-nitrogen containing wastewater according to claim 3, characterized in that: the evaporative crystallization adopts a multi-effect evaporative crystallization or MVR evaporative crystallization system.
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