CN114920405B - Efficient deamination device and method for leachate AnMBR effluent of waste incineration plant - Google Patents
Efficient deamination device and method for leachate AnMBR effluent of waste incineration plant Download PDFInfo
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- CN114920405B CN114920405B CN202210580203.7A CN202210580203A CN114920405B CN 114920405 B CN114920405 B CN 114920405B CN 202210580203 A CN202210580203 A CN 202210580203A CN 114920405 B CN114920405 B CN 114920405B
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- 230000009615 deamination Effects 0.000 title claims abstract description 80
- 238000006481 deamination reaction Methods 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000004056 waste incineration Methods 0.000 title claims abstract description 28
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 59
- 238000010438 heat treatment Methods 0.000 claims abstract description 39
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000000523 sample Substances 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 16
- 238000009833 condensation Methods 0.000 claims abstract description 15
- 230000005494 condensation Effects 0.000 claims abstract description 15
- 238000010521 absorption reaction Methods 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000003513 alkali Substances 0.000 abstract description 4
- 239000000149 chemical water pollutant Substances 0.000 abstract description 4
- 239000003814 drug Substances 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 14
- 230000035484 reaction time Effects 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000010494 dissociation reaction Methods 0.000 description 3
- 230000005593 dissociations Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 230000002596 correlated effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000005375 photometry Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- -1 hydrogen ions Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/586—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing ammoniacal nitrogen
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
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- B01D2251/506—Sulfuric acid
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
The invention discloses a high-efficiency deamination device and method for leachate AnMBR effluent of a waste incineration plant, and belongs to the technical field of landfill leachate treatment. The device comprises a water inlet pump, a heating tank, a deamination column, a pressure gauge, a temperature probe, a heating belt, a heating rod, a circulating pump, a vacuum pump, a condensation column and an absorption tank. The leachate AnMBR effluent of the waste incineration plant is preheated to a required temperature from a heating tank, enters a deamination column through a water inlet pump, continuously flows back and circulates in the deamination column through a circulating pump, and is discharged from the bottom of the deamination column after the completion of the circulation; the ammonia-containing steam is sucked out from the top of the deamination column, enters the condensation column to condense the water vapor, and finally enters the absorption tank to absorb the ammonia in the gas and then is discharged. The device is adopted to treat leachate AnMBR effluent of a waste incineration plant, so that ammonia nitrogen removal rate is high, free ammonia in wastewater continuously enters a gas phase and is pumped away under the condition that alkali and vacuum negative pressure are not required to be added, medicament and energy consumption are saved, and cost is reduced.
Description
Technical Field
The invention relates to a high-efficiency deamination device and method for effluent of leachate AnMBR of a waste incineration plant, and belongs to the technical field of landfill leachate treatment.
Background
Although the leachate of the garbage incineration plant adopts an anaerobic membrane bioreactor (Anaerobic Membrane Bioreactor, anMBR) to effectively remove organic pollutants in the leachate of the garbage incineration plant, the effluent contains high-concentration ammonia nitrogen due to further decomposition of nitrogen-containing organic matters in the anaerobic digestion process to generate ammonia nitrogen, and the current emission standard cannot be met.
At present, the leachate deamination process of the garbage incineration plant mostly adopts a multistage nitrification and denitrification process, but the treatment difficulty is higher because the ammonia nitrogen concentration of the AnMBR effluent is higher than 2000 mg/L; in addition, the C/N in the effluent is seriously unbalanced, and a large amount of carbon sources are required to be added in the operation process, so that the problems of large occupied area, high energy consumption, high treatment cost and the like are caused.
The most widely used physicochemical deamination method is a stripping method at present, and has the defects that the pH of the wastewater is higher in the treatment process, and a large amount of alkali is needed to maintain the alkalinity of the wastewater, so that the cost of the medicament is higher; in addition, the air amount used in the stripping method is large, so that the power consumption is high, the operation cost is high, and the like. In view of this, finding a suitable process is necessary for further treatment of ammonia nitrogen in the leachate AnMBR effluent of a waste incineration plant.
Disclosure of Invention
In order to solve the problems of high ammonia nitrogen concentration in the leachate AnMBR effluent of the waste incineration plant, high energy consumption required by the conventional deamination method, high treatment cost and the like; the invention provides a high-efficiency deamination device and method for effluent of leachate AnMBR of a waste incineration plant, which have the advantages of simple process, low cost and good deamination effect.
The technical scheme adopted by the invention is as follows:
a first object of the present invention is to provide a high-efficiency deamination device for effluent of leachate AnMBR of a waste incineration plant, comprising:
the water inlet pump is used for pumping leachate AnMBR of the waste incineration plant into the deamination column for deamination;
a heating tank for heating the AnMBR effluent to a desired temperature;
the deamination column is used for removing high ammonia nitrogen in AnMBR effluent;
and the circulating pump is used for continuously and circularly conveying the wastewater to the deamination column for backflow.
The vacuum pump is used for controlling the vacuum degree of the whole device;
a condensing column for condensing water vapor in the ammonia-containing vapor;
an absorption tank for absorbing ammonia gas;
wherein the water inlet pump is communicated with the right side of the top of the deamination column through a first pipeline Q1; the bottom of the deamination column is connected with the heating tank through a second pipeline Q2, and the top of the deamination column is connected to the lower end of the condensation column through a third pipeline Q3; the top of the condensation column is connected with a vacuum pump through a fourth pipeline Q4; the vacuum pump is connected with the absorption tank through a fifth pipeline Q5; the circulation pump realizes closed circulation through a second pipeline Q2.
Further, the top of the deamination column is provided with a pressure gauge for detecting the pressure so as to ensure the safety of the device.
Further, the column body of the deamination column is provided with a temperature probe and a heating belt for controlling the temperature of the deamination column.
Further, an air inlet and a gas flowmeter are arranged at the bottom of the deamination column so as to control the air inflow.
Further, a heating rod and a temperature probe are arranged in the heating tank to control the water inlet temperature; the temperature of the inlet water is the same as the deamination column temperature.
The second object of the invention is to provide a method for treating landfill leachate AnMBR effluent by a high-efficiency deamination device, which comprises the following treatment steps:
by adopting the efficient deamination device for the AnMBR effluent of the leachate of the waste incineration plant, the AnMBR effluent preheated in the heating tank enters the deamination column from the first pipeline Q1 through the water inlet pump, continuously flows back and circulates in the deamination column through the circulating pump on the second pipeline Q2, ammonia-containing steam obtained through the deamination column reaction enters the condensation column from the top of the deamination column through the third pipeline Q3, and condensed water is discharged through the seventh pipeline Q7; the ammonia-containing gas passes through the fourth pipeline Q4, the vacuum pump, the fifth pipeline Q5, the absorption tank, and the sixth pipeline Q6.
Further, the method for treating the leachate AnMBR effluent of the waste incineration plant specifically comprises the following steps:
(1) When the efficient deamination device is used for treating leachate AnMBR water of a garbage incineration plant, a heating tank is preheated to 40-60 ℃ through a heating rod; the vacuum degree of the vacuum pump is set to be-0.06-0.08 Mpa, the device is operated for 2-6 hours to stop and sample, and the water sample to be detected is obtained;
(2) Measuring the ammonia nitrogen concentration in the water sample to be measured, which is obtained in the step (1), by adopting a Nahner reagent photometry, and calculating the ammonia nitrogen removal rate in the leachate AnMBR effluent sample of the waste incineration plant.
Further, the circulation flow rate in the circulation pump is 20L/h.
Further, the preheating temperature of the heating tank in the step (1) is 60 ℃, and the vacuum degree is-0.08 MPa; the device run time was 4 hours.
Compared with the prior art, the invention has the advantages that:
1. compared with the conventional stripping method, the device can reduce the cost of adding the medicament, reduce the energy consumption and realize the high-efficiency removal of ammonia nitrogen under the condition that alkali and vacuum negative pressure are not required to be added;
2. compared with the leachate deamination process of the waste incineration plant, the device can enable the waste water to circularly flow back in the deamination column, so that the occupied area is obviously reduced, and meanwhile, the deamination efficiency is higher;
3. the absorption tank can play a role in absorbing tail gas, and meanwhile, the waste water is discharged up to the standard.
Drawings
FIG. 1 is an overall schematic diagram of an efficient deamination device for effluent of leachate AnMBR of a waste incineration plant;
FIG. 2 is data of a single factor experiment of the present invention initially performed with temperature as a variable;
FIG. 3 is data of a single factor test of the present invention initially performed with vacuum as a variable;
FIG. 4 is data from a single factor experiment performed initially using time as a variable in accordance with the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be specifically described below with reference to the embodiments and the accompanying drawings.
Reference numerals: the ammonia removal column comprises a water inlet pump 1, a heating tank 2, an ammonia removal column 3, a circulating pump 4, a vacuum pump 5, a temperature probe 6, a temperature probe 7, a condensation column 8, an absorption tank 9, a gas flowmeter 10, a pressure gauge 11, a heating belt 12, a heating belt 13, a heating rod 14, a temperature probe 15, a first pipeline Q1, a second pipeline Q2, a third pipeline Q3, a fourth pipeline Q4, a fifth pipeline Q5, a sixth pipeline Q6 and a seventh pipeline Q7.
Example 1
Fig. 1 is a schematic diagram of the whole efficient deamination device for effluent of leachate AnMBR of a waste incineration plant, which comprises a water inlet pump 1, a heating tank 2, a deamination column 3, a circulating pump 4, a vacuum pump 5, a temperature probe 6, a temperature probe 7, a condensation column 8, an absorption tank 9, a gas flow meter 10, a pressure gauge 11, a heating belt 12, a heating belt 13, a heating rod 14 and a temperature probe 15.
Wherein, the water inlet pump 1 is communicated with the right side of the top of the deamination column 3 through a first pipeline Q1; the bottom of the deamination column 3 is connected with the heating tank 2 through a second pipeline Q2; a heating rod 14 and a temperature probe 15 are arranged in the heating tank 2 and used for controlling the temperature of the heating tank; the top of the deamination column 3 is connected to the lower end of the condensation column 8 through a third pipeline Q3; the top of the deamination column 3 is provided with a pressure gauge 11 for detecting the pressure so as to ensure the safety of the device; the column body of the deamination column 3 is provided with two temperature probes 6 and 7 and two sections of heating belts 12 and 13 for controlling the temperature of the deamination column 3; the bottom of the deamination column 3 is provided with an air inlet and a gas flowmeter 10 to control the air inflow;
wherein, the top of the condensation column 8 is connected with a vacuum pump 5 through a fourth pipeline Q4, and the vacuum pump 5 is connected with an absorption tank 9 through a fifth pipeline Q5; the circulation pump 4 realizes closed circulation through the second pipeline Q2 so as to realize the circulation reflux of the wastewater in the deamination column. The absorption tank 9 is provided with a sixth pipeline Q6 for discharging the residual harmless gas; the condensation column 8 is provided with a seventh line Q7 for discharging condensed water.
The invention relates to a high-efficiency deamination device for leachate AnMBR effluent of a waste incineration plant, which has the working principle that:
after the AnMBR effluent is preheated to a set temperature in a heating tank and the negative pressure of the device reaches a preset value, regulating the circulation flow to 20L/h, regulating the inflow flow of the AnMBR effluent from a first pipeline Q1 through a water inlet pump 1 to enter a deamination column 3, continuously circulating in the deamination column 3 in a reflux way through a circulating pump 4 on a second pipeline Q2, and reacting through the deamination column 3 The obtained ammonia-containing vapor (ammonia, carbon dioxide, water vapor and part of air) enters a condensation column 8 from the top of the deamination column 3 through a third pipeline Q3, and condensed water is discharged through a seventh pipeline Q7; the ammonia-containing mixed gas passes through a fourth pipeline Q4, a vacuum pump 5, a fifth pipeline Q5, an absorption tank 9 (filled with sulfuric acid solution with the concentration of 0.01 mol/L) for absorbing ammonia, and other gases are discharged through a sixth pipeline Q6.
Example 2
A method for treating landfill leachate AnMBR effluent; the method specifically comprises the following steps:
(1) The device of the embodiment 1 is adopted to operate and treat leachate AnMBR effluent (ammonia nitrogen concentration is about 2000 mg/L) of a garbage incineration plant, a heating tank is preheated to 40-60 ℃, the vacuum degree is set to-0.06-0.08 Mpa, the operation is stopped for 2-6 hours, and a water sample is taken and used for measuring the ammonia nitrogen concentration in the sample;
(2) And (3) measuring the ammonia nitrogen concentration in the water sample taken in the step (1) by adopting a Nahner reagent photometry method, and calculating the ammonia nitrogen removal rate in the leachate AnMBR effluent sample of the waste incineration plant.
Under different treatment conditions, the results of the ammonia nitrogen removal rate in the leachate AnMBR effluent of the waste incineration plant are shown in the following table 1:
TABLE 1 ammonia nitrogen removal under different conditions
As is clear from the table, the temperature of the heating tank, the vacuum degree of the vacuum pump and the operation time have a great influence on the removal rate of deamination, and the removal rate can reach 94.53% only when the temperature of the heating tank is set at 60 ℃, the vacuum degree is-0.08 MPa, and the operation time is 4 hours.
Under different conditions, the influence of the ammonia nitrogen removal rate in the leachate AnMBR effluent of the garbage incineration plant is explored.
1. Influence of temperature on deamination
In the deamination process of the device, the ammonia nitrogen in the wastewater is separated and removed mainly depending on two balances: ammonia equilibrium of gas-liquid two-phase and dissociation equilibrium of ammonia in liquid phase, wherein the dissociation equilibrium of liquid phase ammonia is mainly influenced by pH and temperature, and the following formula is shown:
pK a ＝4×10 -8 ×T 3 +9×10 -5 ×T 2 -0.0356×T+10.072
wherein, [ NH ] 3 ]Concentration of free ammonia, [ NH ] 3 +NH 4 + ]Is the total ammonia nitrogen concentration [ H ] + ]The concentration of hydrogen ions is the ionization constant of ammonia nitrogen, and pK a It can be expressed as a function of the reaction temperature T, and it can be seen from the above equation that the higher the temperature and pH, the higher the free ammonia content. Under the condition of no alkali addition, the control temperature becomes a main external influence factor of the concentration change of free ammonia, thereby influencing the deamination efficiency.
The experiment examines the influence of the inlet water temperature on the deamination effect under the conditions of the vacuum degree of-0.07 MPa, the reaction time of 3h, the initial concentration of 2000mg/L and the circulating flow of 20L/h.
The results are shown in FIG. 2, in general NH 4 + The N removal rate is positively correlated with temperature, which is in agreement with the theory of dissociation equilibrium of ammonia. At a temperature of 30 ℃, NH 4 + The removal rate of N is lower and is only 50.4%, which indicates that ionic ammonium in the wastewater is difficult to be converted into molecular ammonia at the condition close to normal temperature; NH at a temperature of between 40 and 60 DEG C 4 + The N removal rate shows a remarkable rising trend, and the ammonia nitrogen removal rate is increased from 55.2% to 76.5%; with the continuous rise of the temperature to 70 ℃, the wastewater reaches the boiling point under the negative pressure condition under the condition, obvious boiling causes flooding phenomenon, and the reactor is not operated conveniently, and NH 4 + The removal rate of N is 77.8%, and the removal rate is increased by only 1.3%. Considering that too high a temperature tends to increase energy consumption, the running cost is increased to lose the application value, and the performance is insufficient when the temperature is too low. Thus, a combination of temperatures in the range [40, 60 ]]In this case, the ammonia nitrogen removal efficiency is the best.
2. Influence of vacuum on deamination
In the deamination process, leachate AnMBR effluent of the waste incineration plant fully contacts with convection air in a deamination column. According to the gas-liquid two-phase ammonia balance theory, the change of the vacuum degree mainly influences the gas-liquid mass transfer process of free ammonia, molecular ammonia in liquid continuously escapes to a gas phase under the action of negative pressure driving, and simultaneously, the ammonia-containing gas is rapidly discharged due to the action of negative pressure suction, and the release of free ammonia in wastewater is promoted by the reduction of the partial pressure of gas-phase ammonia, so that the removal of ammonia nitrogen is promoted.
In order to explore the influence of vacuum degree on the negative pressure in-situ alkalinity deamination of leachate AnMBR effluent of a waste incineration plant, the temperature is controlled to be 50 ℃, the reaction time is controlled to be 3 hours, the initial concentration is 2000mg/L, the circulating flow is controlled to be 20L/h, and the experimental result is shown in figure 3;
as can be seen from FIG. 3, the ammonia nitrogen removal rate is in an overall rising trend along with the increase of the vacuum degree, wherein the ammonia nitrogen removal rate is obviously changed within the vacuum degree range of-0.06 to-0.08 MPa, and is respectively 54.0%, 66.8% and 78.5%. When the vacuum degree is-0.09 MPa, the ammonia nitrogen removal rate is 80.2%, and the ammonia nitrogen removal rate is only increased by 1.7%, which shows that the influence of the continuous improvement of the vacuum degree on the ammonia nitrogen removal rate is weakened; and the ammonia nitrogen removal rate is less than 50% when the vacuum degree is-0.05 MPa, and the removal rate is too low.
3. Effect of time on deamination
Under the conditions that the temperature is 60 ℃, the vacuum degree is 0.08MPa, the initial concentration is 2000mg/L and the circulating flow is 20L/h, the influence of time on the effluent of the leachate AnMBR of the deamination treatment process waste incineration plant is examined; FIG. 4 reflects NH in wastewater 4 + Variation of the N removal rate with the reaction time.
In the whole process, the ammonia nitrogen removal rate is positively correlated with the reaction time, and the removal rate tends to be fast and slow. The ammonia nitrogen removal rate reaches 75.5% in the first 2 hours of deamination, the ammonia nitrogen removal rate continues to rise to 91.6 in 2-4 hours, and the ammonia nitrogen removal rate increases slowly after 4 hours. When the deamination time is 6h, NH 4 + The removal rate of the N reaches 97.8%, the ammonia nitrogen concentration of the effluent is 41.6mg/L, and the C/N ratio of the effluent is good at the moment, so that the method is suitable for subsequent treatment. The deamination time can be flexibly adjusted according to the requirement of the process on the ammonia nitrogen removal rate, but in the experiment, the ammonia nitrogen removal rate is too low when the reaction time is less than 2 hours, the application value is lost, and the operation cost is inevitably increased when the reaction time is too long.
Various changes and modifications may be made by one skilled in the art without departing from the spirit and scope of the invention, and the scope of the invention is therefore to be defined by the appended claims.
Claims (3)
1. A method for treating leachate AnMBR effluent from a waste incineration plant, comprising the steps of:
treating leachate AnMBR effluent of a waste incineration plant by adopting a high-efficiency deamination device; the efficient deamination device comprises a water inlet pump (1), a heating tank (2), a deamination column (3), a circulating pump (4), a vacuum pump (5), a condensation column (8) and an absorption tank (9); the water inlet pump (1) is communicated with the top of the deamination column (3) through a first pipeline (Q1); the bottom of the deamination column (3) is connected with the heating tank (2) through a second pipeline (Q2), and the top of the deamination column (3) is connected to the lower end of the condensation column (8) through a third pipeline (Q3); the top of the condensation column (8) is connected with a vacuum pump (5) through a fourth pipeline (Q4); the vacuum pump (5) is connected with the absorption tank (9) through a fifth pipeline (Q5); the circulating pump (4) realizes closed circulation through a second pipeline (Q2); the top of the deamination column is provided with a pressure gauge (11); the column body of the deamination column (3) is provided with a first temperature probe (6), a second temperature probe (7), a first heating belt (12) and a second heating belt (13);
the method comprises the steps that AnMBR effluent preheated in a heating tank (2) enters a deamination column (3) from a first pipeline (Q1) through a water inlet pump (1), continuously flows back and circulates in the deamination column (3) through a circulating pump on a second pipeline (Q2), ammonia-containing steam obtained through reaction of the deamination column (3) enters a condensation column (8) from the top of the deamination column (3) through a third pipeline (Q3), and condensed water is discharged through a seventh pipeline (Q7); the ammonia-containing mixed gas passes through a vacuum pump (5) through a fourth pipeline (Q4), then enters an absorption tank (9) through a fifth pipeline (Q5) to absorb ammonia, and other gases are discharged through a sixth pipeline (Q6); the preheating temperature of the heating tank (2) is 60 ℃, and the vacuum degree of the vacuum pump (5) is-0.08 MPa; the running time of the device is 4 hours; the circulation flow in the circulation pump (4) is 20L/h; the ammonia nitrogen concentration in the leachate AnMBR effluent of the waste incineration plant is 2000mg/L.
2. Method for treating leachate AnMBR effluent from a waste incineration plant according to claim 1, characterised in that the bottom of the deamination column (3) is provided with an air inlet and a gas flow meter (10).
3. Method for treating leachate AnMBR effluent from waste incineration plants according to claim 1, characterised in that the heating tank (2) is provided with a heating rod (14) and a temperature probe III (15).
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