CN117088444A - High ammonia nitrogen organic wastewater treatment system and method - Google Patents
High ammonia nitrogen organic wastewater treatment system and method Download PDFInfo
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- CN117088444A CN117088444A CN202311100107.9A CN202311100107A CN117088444A CN 117088444 A CN117088444 A CN 117088444A CN 202311100107 A CN202311100107 A CN 202311100107A CN 117088444 A CN117088444 A CN 117088444A
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- tank
- evaporation
- organic wastewater
- acid
- ammonia nitrogen
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- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims abstract description 15
- 238000001704 evaporation Methods 0.000 claims abstract description 164
- 230000008020 evaporation Effects 0.000 claims abstract description 155
- 239000007788 liquid Substances 0.000 claims abstract description 102
- 239000002253 acid Substances 0.000 claims abstract description 83
- 230000001105 regulatory effect Effects 0.000 claims abstract description 73
- 239000002351 wastewater Substances 0.000 claims abstract description 33
- 238000005406 washing Methods 0.000 claims abstract description 30
- 239000003513 alkali Substances 0.000 claims abstract description 17
- 239000012452 mother liquor Substances 0.000 claims description 39
- 238000001556 precipitation Methods 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 9
- 239000006228 supernatant Substances 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 5
- 238000001514 detection method Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 36
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 abstract description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 4
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 abstract description 4
- 229910052921 ammonium sulfate Inorganic materials 0.000 abstract description 4
- 235000011130 ammonium sulphate Nutrition 0.000 abstract description 4
- 235000019270 ammonium chloride Nutrition 0.000 abstract description 3
- 230000001376 precipitating effect Effects 0.000 abstract 1
- 239000012141 concentrate Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000003750 conditioning effect Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000004021 humic acid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
Abstract
The invention provides a high ammonia nitrogen organic wastewater treatment system, which comprises an evaporation tank and a collecting assembly, wherein concentrated liquid discharged from the evaporation tank is led to the collecting assembly for treatment, and the treatment system further comprises: the acid regulating tank is used for regulating the pH value of the high ammonia nitrogen organic wastewater, and the wastewater after the pH value is regulated enters the evaporation tank for evaporation; and the steam exhausted from the evaporating tank enters the washing tank and is washed by alkali liquor, and the steam exhausted from the washing tank is collected. In the invention, the organic wastewater with high ammonia nitrogen is firstly introduced into the acid regulating tank for regulating acid, ammonia nitrogen is converted into ammonium sulfate or ammonium chloride, ammonia gas is prevented from precipitating in the evaporation process, and meanwhile, the steam discharged from the evaporation tank is cleaned by alkali liquor, so that low-boiling-point organic matters in the steam can be collected, and the COD of produced water is ensured to reach the emission standard.
Description
Technical Field
The invention relates to wastewater treatment, in particular to a high ammonia nitrogen organic wastewater treatment system and a method.
Background
In recent years, the evaporation system is widely applied in the field of wastewater treatment, can realize separation of water molecules, salts and pollutants in wastewater, has better water quality, and aims at the phenomena that the produced water of the conventional evaporation system is high in ammonia nitrogen and COD (chemical oxygen demand) exceeding standard and the water yield of the system is low due to the fact that the produced water of the conventional evaporation system is close to the produced water of high-salt high-ammonia nitrogen and high-organic wastewater.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a high ammonia nitrogen organic wastewater treatment system and a method.
The invention is realized in the following way:
the embodiment of the invention provides a high ammonia nitrogen organic wastewater treatment system, which comprises an evaporation tank and a collecting assembly, wherein concentrated liquid discharged from the evaporation tank is led to the collecting assembly for treatment, and the treatment system further comprises:
the acid regulating tank is used for regulating the pH value of the high ammonia nitrogen organic wastewater, and the wastewater after the pH value is regulated enters the evaporation tank for evaporation;
and the steam exhausted from the evaporating tank enters the washing tank and is washed by alkali liquor, and the steam exhausted from the washing tank is collected.
Further, the washing tank comprises a tank body and a flow guide pipe arranged in the tank body, an upper port of the flow guide pipe is communicated with an exhaust port of the evaporation tank, the tank body is divided into an upper space and a lower space through a demister, the flow guide pipe extends from the upper space to the lower space, a lower port of the flow guide pipe is communicated with the lower space, a spray pipe is arranged in the flow guide pipe, and alkali liquor in the lower space is extracted by the spray pipe and sprayed into the flow guide pipe through the circulation pipe.
Further, the evaporator comprises a heat exchanger, and the deposition concentrate at the bottom of the evaporator is led into the heat exchanger for heat exchange.
Further, the steam discharged from the washing tank is processed by the compressor and then enters the heat exchanger for heat exchange.
Further, a liquid level sensor and a pH value sensor are arranged in the acid regulating tank;
the high liquid level and the low liquid level of the acid regulating tank are preset, when the liquid level is not higher than the low liquid level, the acid regulating tank starts feeding, and when the liquid level reaches the high liquid level, the feeding is stopped; and a stirring piece is arranged in the acid regulating tank, and organic wastewater and acid liquor are mixed through the stirring piece when the pH value is regulated.
Further, the acid regulating tank is used for intermittently regulating acid;
when the liquid level is not higher than the low liquid level, organic wastewater is introduced into the acid regulating tank, the stirring piece starts stirring, quantitative strong acid is introduced into the acid regulating tank, and when the detection data of the pH value sensor is smaller than the set fluctuation range in a certain time, the quantitative strong acid is introduced into the acid regulating tank again until the pH value of the liquid in the acid regulating tank is a target value.
Further, stopping feeding when the liquid level of the evaporation tank is higher than a set value and the temperature of the evaporation tank is lower than the set value; when the temperature of the evaporation tank reaches a set value and the liquid level of the evaporation tank is lower than the set value, starting feeding; and the fluctuation range of the liquid level in the evaporation tank is regulated by regulating the opening of the feeding regulating valve.
Further, the evaporation tanks are provided with two groups, the two groups of evaporation tanks are divided into a first-stage evaporation tank and a second-stage evaporation tank, liquid in the acid regulating tank enters the first-stage evaporation tank for evaporation treatment, concentrated liquid discharged from the first-stage evaporation tank enters the second-stage evaporation tank for continuous evaporation treatment, concentrated liquid discharged from the second-stage evaporation tank enters the collecting assembly, and gas discharged from the first-stage evaporation tank and gas discharged from the second-stage evaporation tank enter the washing tower for cleaning.
Further, the collecting component comprises a mother liquor precipitation tank and a mother liquor recycling tank, wherein the mother liquor precipitation tank collects concentrated liquor discharged from the evaporation tank, the mother liquor recycling tank collects clear liquor discharged from the mother liquor precipitation tank, and the clear liquor in the mother liquor recycling tank is recycled to the evaporation tank;
when the density of the supernatant of the mother liquor precipitation tank is measured to be smaller than a set value, and the liquid level of the mother liquor return tank is measured to be smaller than the set value, the mother liquor precipitation tank discharges the supernatant to the mother liquor return tank, and when the evaporation tank discharges the concentrated liquid to the mother liquor precipitation tank, the mother liquor return tank stops discharging the supernatant to the evaporation tank.
The embodiment of the invention also provides a method for treating the high ammonia nitrogen organic wastewater, which comprises the following steps:
introducing the organic wastewater into an acid regulating tank to regulate the pH value, and introducing the liquid after the pH value into an evaporation tank for evaporation treatment;
the steam discharged from the evaporating pot enters the washing pot for cleaning, and the gas discharged from the washing pot is collected; and the concentrated liquid discharged from the evaporating pot enters the collecting component to be cooled and crystallized.
The invention has the following beneficial effects:
in the treatment system, firstly, high ammonia nitrogen organic wastewater is introduced into an acid regulating tank for acid regulation, ammonia nitrogen is converted into ammonium sulfate or ammonium chloride, and ammonia gas precipitation in the evaporation process is avoided; in addition, after the liquid with acid regulated enters the evaporation tank to evaporate, the generated steam enters the washing tank to be washed, so that low-boiling-point organic matters in the steam can be collected, and the COD (chemical oxygen demand) emission of produced water can be achieved.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a high ammonia nitrogen organic wastewater treatment system according to an embodiment of the present invention.
Detailed Description
The following description of the embodiments of the present invention 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 invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Referring to fig. 1, an embodiment of the present invention provides a high ammonia nitrogen organic wastewater treatment system, which includes an evaporation tank 1, a collection assembly 2, an acid conditioning tank 3, and a washing tank 4.
The organic wastewater with high ammonia nitrogen is introduced into the acid regulating tank 3, the strong acid in the acid storage tank 5 can be introduced into the acid regulating tank 3 through the acid adding pump 51, the strong acid in the acid storage tank 5 can be sulfuric acid or hydrochloric acid, and the like, the organic wastewater and the strong acid are mixed in the acid regulating tank 3, chemical reaction can occur between the organic wastewater and the strong acid, ammonia nitrogen in the organic wastewater is converted into ammonium sulfate or ammonium chloride, and liquid in the acid regulating tank 3 is introduced into the evaporation tank 1 through the feed pump 61 for evaporation treatment; and in the evaporation process, the steam discharged from the evaporation tank 1 enters the washing tank 4 and is cleaned by alkali liquor, so that low-temperature boiling point organic matters can be absorbed into the alkali liquor, COD (chemical oxygen demand) of the cleaned steam after condensation cannot exceed the standard, the concentrated solution at the bottom of the evaporation tank 1 can be specifically determined by adopting the solution density after the concentrated solution is concentrated to a certain degree, such as a densimeter is additionally arranged, the concentrated solution at the bottom of the evaporation tank 1 is discharged to the collecting assembly 2 after the concentration is detected by the densimeter to reach a set value, and the concentrated solution can be subjected to post-treatment by the collecting assembly 2.
According to the invention, when the evaporation treatment is adopted for the organic wastewater with high ammonia nitrogen, the acid regulation is carried out in advance, the organic wastewater is evaporated in an acidic environment, ammonia nitrogen in the organic wastewater is converted into ammonium sulfate or ammonium hydrochloride, the ammonia precipitation in the evaporation process can be avoided, in addition, the low-boiling-point organic matters carried in the steam can be effectively treated after the steam discharged from the evaporation tank 1 is washed by alkali liquor, and the COD content exceeding the standard after the washed steam is condensed is avoided.
The structure of refining wash tank 4, including jar body 41 and honeycomb duct 42, be provided with defroster 43 in jar body 41, defroster 43 separates jar body 41 into upper and lower two parts, specifically upper space 411 and lower space 412, foretell honeycomb duct 42 passes defroster 43, defroster 43 adopts folded plate structure, its part is located upper space 411, part is located lower space 412, of course honeycomb duct 42 and upper space 411 are not linked together, its lower port stretches into lower space 412 and communicates with lower space 412, the upper port of honeycomb duct 42 communicates with the gas vent of evaporation tank 1, from this evaporation tank 1 exhaust steam gets into in honeycomb duct 42, get into wash tank 4's lower space 412 by honeycomb duct 42 again. In addition, a spray pipe 44 is arranged in the guide pipe 42, alkali liquid can be atomized and sprayed into the guide pipe 42 through the spray pipe 44, so that low-boiling-point organic matters contained in absorbed steam can be eliminated, the residual steam can enter the upper space 411 through the demister 43 and can be condensed and collected, generally, the treatment system is provided with a water production tank 7, and the steam discharged from the washing tank 4 is condensed and then collected in the water production tank 7. The water producing tank 7 is matched with a water producing pump 71, the water producing pump 71 is interlocked with the liquid level of the water producing tank 7, when the liquid level of the water producing tank 7 is higher than a set value (such as 0.8 m), a water producing regulating valve 72 is opened, the water producing pump 71 is opened, and when the liquid level fluctuation of the water producing tank 7 is within a set range (+0.05-0.1 m), the feeding of the evaporation tank 1 is increased.
In optimizing the above embodiment, the washing tank 4 is provided with the circulation pipe 45, one end of the circulation pipe 45 is communicated with the spray pipe 44, the other end of the circulation pipe 45 extends to the lower space 412, alkali liquor is generally accumulated in the lower space 412, the other end of the circulation pipe 45 extends into the alkali liquor, the alkali liquor is pumped to the spray pipe 44 through the circulation pump 451 on the circulation pipe 45, and the liquid discharged from the flow guide pipe 42 is recycled to the lower space 412. For the spray pipes 44, at least three groups are arranged in the guide pipe 42 and are sequentially arranged at intervals along the length direction of the guide pipe 42, for example, four groups are arranged, the distance between two adjacent groups is 0.5m, the spraying direction of each spray pipe 44 is the same as the steam flow direction entering the guide pipe 42, all the spray pipes adopt rotary steaming nozzles, all the spray pipes are close to the upper port of the guide pipe 42, and the atomized alkali liquid and the steam in the guide pipe 42 can be fully mixed. In addition, at least part of the flow guiding tube 42 extends out of the upper space 411, and each of the spraying tubes 44 is located at the area of the flow guiding tube 42 extending out of the upper space 411. A pH sensor is also provided in the lower space 412 for detecting the pH of the liquid in the lower space 412, specifically, when the liquid level of the wash tank 4 is high to a set value range (e.g., 0.8-1 m) and the temperature of the wash tank 4 is set to a set value (e.g., 60 °), the circulation pump 451 is turned on, when the pH of the wash tank 4 is reduced to 10, the liquid alkali pump is automatically started, when the pH of the wash tank 4 is increased to 13, and the liquid alkali pump is automatically stopped.
In a preferred scheme, the treatment system further comprises a heat exchanger 8, and the concentrated solution deposited at the bottom of the evaporation tank 1 is led into the heat exchanger 8 for heat exchange. In this embodiment, the concentrated solution deposited at the bottom of the evaporation tank 1 is led into the heat exchanger 8 through the forced circulation pump 81 to exchange heat, and after the temperature rises, the concentrated solution is returned back into the evaporation tank 1 through the return pipe. In general, the forced circulation pump 81 is used for extracting the liquid at the bottom of the evaporation tank 1, and the return pipe guides the liquid after heat exchange and temperature rising into the evaporation tank 1, and the guiding position is higher than the extracting position of the forced circulation pump 81, so that on one hand, the evaporation efficiency in the evaporation tank 1 can be improved through heat exchange and temperature rising, and on the other hand, the liquid in the evaporation tank 1 can flow, especially the liquid with higher density at the bottom of the evaporation tank 1. Since the feeding temperature is lower than the liquid temperature led in by the guide pipe, the feeding port of the evaporation tank 1 is arranged above the led-in position of the return pipe, and the evaporation efficiency in the evaporation tank 1 can be improved.
Continuing to optimize the embodiment, the steam discharged from the washing tank 4 is treated by the compressor 82 and then enters the heat exchanger 8 for heat exchange. In this embodiment, the heat exchange medium in the heat exchanger 8 is the steam discharged from the wash tank 4, which is compressed by the compressor 82 and then heated, and cooled and condensed into liquid after heat exchange by the heat exchanger 8, and then collected into the water producing tank 7. The treatment system is further vacuumized through the water ring vacuum pump 83, so that the heat exchanger 8, the washing tank 4, the evaporation tank 1 and the like form a certain vacuum degree, the water ring vacuum pump 83 is interlocked with the treatment system pressure and the vacuum regulating valve 831, when the treatment system negative pressure is smaller than a set value, the opening degree of the vacuum regulating valve 831 is increased, when the system negative pressure is larger than the set value, the opening degree of the vacuum regulating valve 831 is reduced, and the treatment system pressure is controlled by the vacuum regulating valve 831 to be repeatedly regulated, so that the evaporation temperature of the treatment system is maintained within a set range (such as-80 kpa), the operation energy consumption of the treatment system is greatly reduced, meanwhile, calcium sulfate and humic acid are not easy to precipitate at a lower evaporation temperature, the scaling risk of the treatment system is reduced, and the mechanical cleaning period of the treatment system is prolonged. The water ring vacuum pump 83 is communicated with the heat exchanger 8 through a pipeline, and is particularly communicated with a steam flow path in the heat exchanger 8, so that when the water ring vacuum pump 83 works, steam in the heat exchanger 8 is pumped into a pipeline corresponding to the water ring vacuum pump 83 along with air, and the heat exchanger is additionally arranged on the pipeline, so that heat exchange between the pipeline and a feed flow path of the evaporation tank 1 can be realized, the steam in the pipeline is cooled and condensed into liquid after heat exchange, and then the liquid is collected into the water production tank 7. The produced water in the produced water tank 7 can also exchange heat with the feeding flow path of the evaporation tank 1, namely the liquid after acid adjustment needs to enter the evaporation tank 1 after twice heat exchange, and specifically comprises the following steps: the heat exchange is carried out with the produced water in the produced water tank 7, and then the heat exchange is carried out again with the pipeline corresponding to the water ring vacuum pump 83, so that the overall heat utilization rate of the treatment system is improved.
In one embodiment, a liquid level sensor and a pH value sensor are disposed in the acid adjusting tank 3, a high liquid level and a low liquid level of the acid adjusting tank 3 are preset, and when the liquid level is not higher than the low liquid level, the acid adjusting tank 3 starts feeding, and when the high liquid level is reached, the feeding is stopped. In addition, during the pH adjustment, the organic wastewater and the acid solution are mixed by the stirring member 31. Specifically, the intermittent acid regulation is adopted, when the liquid level is not higher than the low liquid level, the organic wastewater is introduced into the acid regulation tank 3, the stirring piece 31 starts stirring, then the quantitative strong acid is introduced into the acid regulation tank 3, and when the detection data of the pH value sensor is smaller than the set fluctuation range within a certain time, the quantitative strong acid is introduced into the acid regulation tank 3 again until the pH value of the liquid in the acid regulation tank 3 is the target value. When the liquid level of the acid regulating tank 3 is lower than 1m, the feeding is started, when the liquid level of the acid regulating tank 3 is higher than 5m, the feeding is stopped, the acid regulating tank 3 adopts an intermittent feeding and discharging mode, for example, a 150 square/day system is processed, three times of feeding can be adopted, namely, the effective volume of the acid regulating tank 3 can be designed to be 50 square, after the feeding of the acid regulating tank 3 is completed, the acid regulating tank 3 starts to regulate the acid, firstly, the stirrer is started, then the acid adding pump 51 is started, the acid adding pump 51 is stopped for 10 minutes after 10 seconds or 15 seconds of operation, the acid regulating tank 3 starts to regulate the acid for the second time after no fluctuation in 1 minute, the acid adding pump 51 is stopped for 10 minutes after 10 seconds or 15 seconds of operation, and the pH value of the acid regulating tank 3 starts to push inwards in sequence until the pH value of the acid regulating tank 3 reaches a set value, and the acid adding pump 51 is stopped. The adoption of the acid regulating mode can effectively avoid the problem that the pH value sensor is used for measuring data time delay and cannot feed back in time, and the intermittent feeding mode can effectively avoid the problem that the fluctuation of the water quality of the running feeding cannot accurately control the pH value. When the acid conditioning process is finished, the transfer pump 32 is started to input feed liquid into the feed tank 6, then the acid conditioning of the second batch is started, the feed tank 6 stores the acid-conditioned liquid, and the evaporation tank 1 pumps the liquid from the feed tank 6 through the feed pump 61.
In one embodiment, when the liquid level in the evaporation tank 1 is higher than the set value and the temperature in the evaporation tank 1 is lower than the set value, the feed pump 61 stops drawing liquid from the feed tank 6; when the temperature of the evaporation tank 1 reaches the set value and the liquid level of the evaporation tank 1 is lower than the set value, the feed pump 61 starts to operate, and the fluctuation range of the liquid level in the evaporation tank 1 is adjusted by adjusting the opening of the feed adjusting valve 62. Specifically, when the liquid level of the evaporation tank 1 is higher than a set value (e.g., 0.8 m) while the temperature of the evaporation tank 1 is lower than the set value (e.g., 60 °), the feed pump 61 is stopped, and the feed regulating valve 62 is closed, when the temperature of the evaporation tank 1 reaches the set value while the liquid level of the evaporation tank 1 is lower than the set value, the feed regulating valve 62 is opened, the feed pump 61 is opened, when the liquid level fluctuation of the evaporation tank 1 is within a set range (±0.01 to- - ±0.02 m), the opening of the feed regulating valve 62 is increased, and when the liquid level fluctuation of the evaporation tank 1 is within the set range (+0.05 to- +0.1 m), the opening of the feed regulating valve 62 is decreased, and the adjustment is repeated, so that the liquid level fluctuation of the evaporation tank 1 is within the set range (±0.05 m). When the discharge densitometer 13 of the evaporation tank 1 measures the density to be more than 1.4g/cm 3 When the liquid level of the collecting assembly 2 is lower than the set value (such as 5 m), the discharging adjusting valve 11 is opened, the discharging pump 12 is opened, the discharging flow is adjusted repeatedly to reach the set value (such as 0.5 square/hour), and when the discharging density meter 13 measures the density to be less than 1.3g/cm 3 When the discharge pump 12 is turned off, the discharge regulating valve 11 is turned off.
In the preferred scheme, the evaporation tank 1 is provided with two groups, the two groups of evaporation tanks 1 form two-stage evaporation, in particular to a first-stage evaporation tank 1 and a second-stage evaporation tank 1, liquid in the feeding tank 6 enters the first-stage evaporation tank 1 through the feeding pump 61 for evaporation treatment, and concentrated liquid discharged from the first-stage evaporation tank 1 enters the second-stage evaporation tank 1 for subsequent evaporationAnd (3) continuing the evaporation treatment, wherein the concentrated solution discharged from the primary evaporation tank 1 enters the secondary evaporation tank 1 to continue the evaporation treatment, the concentrated solution discharged from the secondary evaporation tank 1 enters the collecting assembly 2, and the steam discharged from the primary evaporation tank 1 and the secondary evaporation tank 1 enters the washing tank 4 to be washed. In this embodiment, when the components of the organic wastewater are complex, a two-stage evaporation mode is adopted, that is, the concentrated solution discharged from the first-stage evaporation tank 1 is not directly discharged into the collecting assembly 2, and enters the second-stage evaporation tank 1 for secondary evaporation concentration. The two-stage evaporation tank 1 and the one-stage evaporation tank 1 are both matched with heat exchangers 8, steam discharged from the washing tank 4 enters the two heat exchangers 8 after being compressed, and liquid in the evaporation tank 1 enters the corresponding heat exchangers 8 for heat exchange. The density of the solution measured by the discharge densitometer 13 of the secondary evaporation tank 1 is more than 1.3g/cm 3 When the liquid level of the secondary evaporation tank 1 is lower than a set value (such as 1.5 m), the discharging regulating valve 11 is opened, the discharging pump 12 is opened, and the solution is led into the collecting assembly 2.
Refining collection subassembly 2, including mother liquor precipitation tank 21 and mother liquor feed back jar 22, mother liquor precipitation tank 21 collects evaporation tank 1 and discharges the concentrate, when adopting the second grade evaporation, mother liquor precipitation tank 21 collects the second grade evaporation tank 1 and discharges the concentrate, high concentration concentrate separates out the salinity in mother liquor precipitation tank 21, mother liquor feed back jar 22 collects mother liquor precipitation tank 21 exhaust clear solution, and retrieve mother liquor feed back jar 22 clear solution to evaporation tank 1 through feed back pump 221, the preferred embodiment is leading into evaporation tank 1 after it is leading into heat exchanger 8 again. The mother liquor precipitation tank 21 is provided with heat exchange cooling, after the concentrated liquor enters the mother liquor precipitation tank 21, the temperature of the mother liquor is reduced to normal temperature by circulating cooling water, salt in the concentrated liquor is separated out by crystallization, and when the density of the supernatant liquid of the mother liquor precipitation tank 21 is measured by the feed back densimeter 211 to be smaller than a set value, such as 1.1g/cm 3 When the liquid level of the mother liquor recycle tank 22 is lower than a set value (such as 0.5 m), the recycle regulating valve 222 is opened, and when the discharge densimeter 13 measures that the density is higher than 1.3g/cm 3 At the time, that is, when the evaporation tank 1 discharges the concentrated water to the mother liquor precipitation tank 21, the feed back pump 221 is turned off.
The embodiment of the invention also provides a method for treating the high ammonia nitrogen organic wastewater, which adopts the treatment system to treat the high ammonia nitrogen organic wastewater, and comprises the following specific steps:
the organic wastewater is led into an acid regulating tank 3 to regulate the pH value, and the liquid after the pH value is led into an evaporation tank 1 to be evaporated;
the steam discharged from the evaporation tank 1 enters the washing tank 4 for washing, and the gas discharged from the washing tank 4 is collected; and the concentrated liquid discharged from the evaporation tank 1 enters the collecting component 2 to be cooled and crystallized.
In the method, the organic wastewater is subjected to acid regulation firstly, the organic wastewater is subjected to evaporation treatment through an evaporation tank 1 in an acidic environment, steam discharged from the evaporation tank 1 is subjected to alkali liquor cleaning through a washing tank 4, the cleaned steam is compressed by a compressor 82 and then heated, so that the heated steam can be introduced into a heat exchanger 8 to exchange heat with liquid at the bottom of the evaporation tank 1, the condensed steam is collected in a water production tank 7, concentrated liquid discharged from the evaporation tank 1 is subjected to heat exchange and temperature reduction in a mother liquor precipitation tank 21 to precipitate salt therein, and supernatant liquid is reintroduced into the evaporation tank 1 for re-evaporation. By the treatment method, on one hand, the exceeding of COD of the produced water in the water producing tank 7 can be avoided, on the other hand, the water producing rate of the whole treatment system can be ensured, and the evaporation process of the evaporation tank 1 is controlled by adopting the combination of air pressure, temperature, density, liquid level, pH value and the like, so that the efficient and stable operation of the evaporation tank is ensured.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Claims (10)
1. The utility model provides a high ammonia nitrogen organic wastewater treatment system, includes evaporation tank and collection subassembly, evaporation tank discharge thick liquid leads to collection subassembly and handles, its characterized in that still includes:
the acid regulating tank is used for regulating the pH value of the high ammonia nitrogen organic wastewater, and the wastewater after the pH value is regulated enters the evaporation tank for evaporation;
and the steam exhausted from the evaporating tank enters the washing tank and is washed by alkali liquor, and the steam exhausted from the washing tank is collected.
2. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 1, wherein: the washing tank comprises a tank body and a flow guide pipe arranged in the tank body, wherein the upper port of the flow guide pipe is communicated with an exhaust port of the evaporation tank, the tank body is divided into an upper space and a lower space through a demister, the flow guide pipe extends from the upper space to the lower space, the lower port of the flow guide pipe is communicated with the lower space, a spray pipe is arranged in the flow guide pipe, and alkali liquor in the lower space is extracted by the spray pipe and sprayed into the flow guide pipe through a circulation pipe.
3. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 1, wherein: the evaporator comprises a heat exchanger, wherein concentrated solution deposited at the bottom of the evaporating pot is led into the heat exchanger for heat exchange.
4. A high ammonia nitrogen organic wastewater treatment system as defined in claim 3, wherein: and the steam discharged from the washing tank is processed by the compressor and then enters the heat exchanger for heat exchange.
5. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 1, wherein: a liquid level sensor and a pH value sensor are arranged in the acid regulating tank;
the high liquid level and the low liquid level of the acid regulating tank are preset, when the liquid level is not higher than the low liquid level, the acid regulating tank starts feeding, and when the liquid level reaches the high liquid level, the feeding is stopped; and a stirring piece is arranged in the acid regulating tank, and organic wastewater and acid liquor are mixed through the stirring piece when the pH value is regulated.
6. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 5, wherein: the acid regulating tank is used for intermittently regulating acid;
when the liquid level is not higher than the low liquid level, organic wastewater is introduced into the acid regulating tank, the stirring piece starts stirring, quantitative strong acid is introduced into the acid regulating tank, and when the detection data of the pH value sensor is smaller than the set fluctuation range in a certain time, the quantitative strong acid is introduced into the acid regulating tank again until the pH value of the liquid in the acid regulating tank is a target value.
7. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 1, wherein: stopping feeding when the liquid level of the evaporation tank is higher than a set value and the temperature of the evaporation tank is lower than the set value; when the temperature of the evaporation tank reaches a set value and the liquid level of the evaporation tank is lower than the set value, starting feeding; and the fluctuation range of the liquid level in the evaporation tank is regulated by regulating the opening of the feeding regulating valve.
8. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 1, wherein: the evaporation tanks are provided with two groups, the two groups of evaporation tanks are divided into a first-stage evaporation tank and a second-stage evaporation tank, liquid in the acid regulating tank enters the first-stage evaporation tank for evaporation treatment, concentrated liquid discharged from the first-stage evaporation tank enters the second-stage evaporation tank for continuous evaporation treatment, concentrated liquid discharged from the second-stage evaporation tank enters the collecting assembly, and gas discharged from the first-stage evaporation tank and the second-stage evaporation tank all enter the washing tower for washing.
9. The high ammonia nitrogen organic wastewater treatment system as claimed in claim 1, wherein: the collecting assembly comprises a mother liquor precipitation tank and a mother liquor recycling tank, wherein the mother liquor precipitation tank collects concentrated liquor discharged from the evaporation tank, the mother liquor recycling tank collects clear liquid discharged from the mother liquor precipitation tank, and the clear liquid in the mother liquor recycling tank is recycled to the evaporation tank;
when the density of the supernatant of the mother liquor precipitation tank is measured to be smaller than a set value, and the liquid level of the mother liquor return tank is measured to be smaller than the set value, the mother liquor precipitation tank discharges the supernatant to the mother liquor return tank, and when the evaporation tank discharges the concentrated liquid to the mother liquor precipitation tank, the mother liquor return tank stops discharging the supernatant to the evaporation tank.
10. The method for treating the high ammonia nitrogen organic wastewater is characterized by comprising the following steps of:
introducing the organic wastewater into an acid regulating tank to regulate the pH value, and introducing the liquid after the pH value into an evaporation tank for evaporation treatment;
the steam discharged from the evaporating pot enters the washing pot for cleaning, and the gas discharged from the washing pot is collected; and the concentrated liquid discharged from the evaporating pot enters the collecting component to be cooled and crystallized.
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