CN110835136A - Ammonia nitrogen wastewater treatment system and method - Google Patents
Ammonia nitrogen wastewater treatment system and method Download PDFInfo
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- CN110835136A CN110835136A CN201911272211.XA CN201911272211A CN110835136A CN 110835136 A CN110835136 A CN 110835136A CN 201911272211 A CN201911272211 A CN 201911272211A CN 110835136 A CN110835136 A CN 110835136A
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- 238000000034 method Methods 0.000 title claims abstract description 63
- 238000004065 wastewater treatment Methods 0.000 title claims description 24
- 239000002351 wastewater Substances 0.000 claims abstract description 137
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- 239000007788 liquid Substances 0.000 claims abstract description 53
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- 239000000243 solution Substances 0.000 description 42
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- QYDYPVFESGNLHU-KHPPLWFESA-N methyl oleate Chemical compound CCCCCCCC\C=C/CCCCCCCC(=O)OC QYDYPVFESGNLHU-KHPPLWFESA-N 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
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- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 description 1
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- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 1
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 description 1
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- QYDYPVFESGNLHU-UHFFFAOYSA-N elaidic acid methyl ester Natural products CCCCCCCCC=CCCCCCCCC(=O)OC QYDYPVFESGNLHU-UHFFFAOYSA-N 0.000 description 1
- 238000002848 electrochemical method Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 238000009364 mariculture Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 229940073769 methyl oleate Drugs 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid group Chemical group C(CCCCCCC\C=C/CCCCCCCC)(=O)O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
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- 230000002572 peristaltic effect Effects 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
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Classifications
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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
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/008—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for liquid waste
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
-
- 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/10—Liquid waste
- F23G2209/101—Waste liquor
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/50—Intercepting solids by cleaning fluids (washers or scrubbers)
Abstract
The invention provides a system and a method for treating ammonia nitrogen wastewater, wherein the system for treating the ammonia nitrogen wastewater comprises a preheating unit, a multi-effect evaporation unit, a gas-liquid separation unit and a concentrated solution combustion unit; the discharge port of the preheating unit is connected with the feed port of the multi-effect evaporation unit, the exhaust port of the multi-effect evaporation unit is connected with the gas-liquid separation unit, and the liquid outlet of the multi-effect evaporation unit is connected with the concentrated solution combustion unit; the concentrated solution combustion unit comprises a concentrated solution combustion device, a heat exchange device and a tail gas treatment device which are sequentially connected. The invention carries out concentration treatment on the ammonia nitrogen wastewater and burns the concentrated solution, thereby recycling the ammonia nitrogen wastewater.
Description
Technical Field
The invention belongs to the technical field of pollutant treatment, relates to a wastewater treatment system and method, and particularly relates to an ammonia nitrogen wastewater treatment system and method.
Background
Amination refers to a reaction of introducing amino groups into organic compounds, so that wastewater generated by an amination process has the characteristics of high ammonia nitrogen, high COD (chemical oxygen demand) and the like. In the prior art, methods for treating high COD wastewater include physical methods, chemical methods, biological methods and combined treatment methods.
The physical methods include an adsorption method, a coagulation sedimentation method, a membrane filtration method, and the like. For example, CN 109205939 a discloses a method for treating ammonia nitrogen wastewater by using an adsorbent, which comprises the following steps: (1) selecting phosphate, silicate and magnesium salt as raw materials of the adsorbent, uniformly mixing the raw materials into a mixture, adding water into the mixture, and stirring to form a mixed solution; standing the mixed solution for 30-50min, and performing centrifugal separation to form an adsorbent; (2) removing impurities from the ammonia nitrogen wastewater to be treated, and then putting the ammonia nitrogen wastewater after impurity removal into a purification tank; (3) putting the adsorbent into a purification tank, and stirring the ammonia nitrogen wastewater in the purification tank to uniformly mix the adsorbent and the ammonia nitrogen wastewater; (4) aerating to the bottom of the purification tank to fully and uniformly mix the ammonia nitrogen wastewater with the adsorbent; (5) and settling the ammonia nitrogen wastewater in the purification tank.
CN 102976464A discloses a composite ammonia nitrogen remover and a using method thereof, wherein the composite ammonia nitrogen remover comprises the following components in percentage by mass: 53-86% of nano iron particles and 14-47% of isooctanol and/or polyethylene glycol. When treating ammonia nitrogen wastewater, the composite ammonia nitrogen remover is put into the wastewater, mixed evenly and treated.
The method has the advantages of high adsorbent consumption, high regeneration cost and unstable treatment effect.
The chemical method includes catalytic oxidation, electrochemical method, ultrasonic method, incineration method, etc. For example, CN 105502584A discloses a device and a method for removing ammonia nitrogen, nitrite nitrogen and COD in mariculture wastewater. The top end of a reservoir is provided with a water inlet which is communicated with a water outlet at the upper end of an electrochemical reactor, the lower end of the reservoir is provided with a water outlet which is connected with the water inlet at the lower end of the electrochemical reactor through a peristaltic pump; the electrochemical reactor is internally provided with an anode, a bipolar electrode and a cathode in sequence, wherein the anode is connected with the anode of the direct current stabilized power supply, and the cathode is connected with the cathode of the direct current stabilized power supply.
CN 102557355A discloses a method for treating amino-containing compound wastewater by copolymerization extraction, which is carried out at normal temperature and pressure: (1) placing the amino-containing organic wastewater in a copolymerization extraction reaction tower, and adjusting the pH value of the wastewater to 5.7-6.5; (2) adding an extracting agent, wherein the volume ratio of the extracting agent to the wastewater is 1:100-1000, and the catalyst is oleic acid or methyl oleate; (3) carrying out aeration reaction on the wastewater in the reaction tower, wherein the aeration reaction time is 2-6 h; (4) after aeration reaction, standing for 5-30 min; (5) standing, performing liquid-liquid separation, sucking the upper layer reacted extract phase, placing the extract phase in a reduced pressure distillation reaction device, recovering the extractant, and leaving low-concentration organic wastewater.
However, the process for treating wastewater by a pure chemical method is complex, and various additional components are required to be added, so that the cost is high, and the treatment effect is unstable.
For the treatment of high ammonia nitrogen wastewater, the existing treatment method comprises a biological nitrification and denitrification method, breakpoint chlorination, gas stripping, precipitation and an ion exchange method, then the biological method utilizes the metabolism of microorganisms to complete the degradation of organic matters in the wastewater, and has the characteristics of wide application range, large treatment capacity, low operation cost and the like, but is only suitable for treating the organic wastewater with the salt content of less than 5000mg/L, and is difficult to treat the organic wastewater with the high salt content. And the biological method has low treatment efficiency and is not suitable for application scenes with high requirement on treatment efficiency.
Therefore, the system and the method for treating the ammonia nitrogen wastewater have high treatment efficiency and good nitrogen oxide removal effect, and have important significance for improving the treatment effect of the aminated wastewater, reducing the treatment cost of enterprises on the wastewater and improving the economic benefit of the enterprises.
Disclosure of Invention
The invention aims to provide an ammonia nitrogen wastewater treatment system and method, wherein the system is used for concentrating ammonia nitrogen wastewater and carrying out combustion treatment on concentrated solution, so that the ammonia nitrogen wastewater is recycled, and the emission of pollutants is reduced. Moreover, the ammonia nitrogen wastewater treatment system has low treatment cost, can reasonably utilize the energy of each workshop section, has high pollutant removal rate and is beneficial to reducing the environmental load.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the invention provides an ammonia nitrogen wastewater treatment system, which comprises a preheating unit, a multi-effect evaporation unit, a gas-liquid separation unit and a concentrated solution combustion unit.
The discharge port of the preheating unit is connected with the feed port of the multi-effect evaporation unit, the condensate outlet of the multi-effect evaporation unit is connected with the gas-liquid separation unit, and the liquid outlet of the multi-effect evaporation unit is connected with the concentrated liquid combustion unit;
the concentrated solution combustion unit comprises a concentrated solution combustion device, a heat exchange device and a tail gas treatment device which are sequentially connected.
The ammonia nitrogen wastewater flows into the preheating unit for preheating, the preheated ammonia nitrogen wastewater flows into the multi-effect evaporation unit for evaporation and concentration, the concentrated solution flows into the concentrated solution combustion unit for combustion, and the combusted gas is subjected to tail gas treatment after heat exchange, so that the content of nitrogen oxides in the tail gas is reduced. The condensate is recovered after the evaporation gas of multi-effect evaporation is condensed and separated from gas and liquid, so that the resource utilization of the ammonia nitrogen wastewater is realized, the energy consumption is low in the treatment process, and the pollutant removal rate is high.
Preferably, the ammonia nitrogen wastewater is ammonia nitrogen wastewater generated by an amination process.
Preferably, the multi-effect evaporation unit is a three-effect counter-flow evaporator.
Preferably, the preheating unit comprises a heat exchanger.
Preferably, the heat exchanger comprises a shell and tube heat exchanger and/or a plate heat exchanger.
Preferably, the primary preheater of the triple-effect countercurrent evaporator is connected with an external heat source heat supply pipeline, and the external heat source heat supply pipeline is connected with the primary preheater and then connected with the preheating unit.
The invention adopts a triple-effect countercurrent evaporator to evaporate and concentrate preheated ammonia nitrogen wastewater, wherein gas-phase and liquid-phase materials flow in a countercurrent way. The liquid phase direction is as follows: the preheated ammonia nitrogen wastewater firstly enters a triple-effect evaporator, exchanges heat in a triple-effect preheater to raise the temperature, and enters a separation chamber of the triple-effect evaporator for gas-liquid separation; after the ammonia nitrogen wastewater is concentrated to a certain concentration in the triple-effect evaporator, the ammonia nitrogen wastewater is sent into the double-effect evaporator by a triple-effect material transfer pump for evaporation and concentration; and after the ammonia nitrogen wastewater is concentrated to a certain degree in the double-effect evaporator, the ammonia nitrogen wastewater is sent to the single-effect evaporator by the double-effect material transfer pump for evaporation and concentration, and after the ammonia nitrogen wastewater is concentrated to the process requirement, the ammonia nitrogen wastewater is conveyed to the concentrated solution combustion unit by the single-effect material transfer pump.
The gas phase flow direction is as follows: the saturated steam enters a primary preheater for heat exchange and condensation, and the condensate flows into a preheating unit for preheating the ammonia nitrogen wastewater; secondary steam generated by the first-effect evaporator is used as a heat source of the second-effect preheater and is condensed in the second-effect preheater; secondary steam generated by the second-effect evaporator is used as a heat source of the third-effect preheater and is condensed in the third-effect preheater; the secondary steam generated by the triple-effect evaporator is condensed in the condenser, and the condensate flows into the gas-liquid separation unit.
Preferably, a filtering device is arranged at the feed inlet of the preheating unit.
Preferably, the filter device comprises a bag filter and/or a precision filter.
Preferably, the filter device has a filter pore size of 0.5mm or less, for example, 0.1mm, 0.2mm, 0.3mm, 0.4mm or 0.5mm, but not limited to the values recited, and other values not recited within the numerical range are also applicable.
Preferably, the concentrated solution combustion device is a direct-fired furnace.
Preferably, the heat exchange device is a heat exchanger.
The concentrated solution is combusted in the direct combustion furnace, and gas generated by combustion is used as a heat source of the heat exchange device for heat exchange, so that heat generated by combustion of the ammonia nitrogen wastewater is utilized. Meanwhile, the ammonia nitrogen wastewater is beneficial to orderly utilization after being cooled.
Preferably, the heat exchanger comprises a shell and tube heat exchanger and/or a plate heat exchanger.
Preferably, the tail gas treatment device comprises an SCR reactor, a spray tower and a chimney which are connected in sequence.
The concentrated solution is subjected to heat exchange and temperature reduction in the heat exchange device after being combusted, so that the temperature of gas generated by combustion is reduced to meet the reaction temperature of the SCR reactor, such as 250 ℃, 260 ℃, 270 ℃, 280 ℃, 290 ℃, 300 ℃, 310 ℃, 320 ℃, 330 ℃, 340 ℃ or 350 ℃, thereby simplifying the process of tail gas treatment and improving the utilization rate of energy.
Preferably, the connecting pipeline of the multi-effect evaporation unit and the concentrated solution combustion device is a jacket pipeline and/or a heat tracing pipeline.
Preferably, the gas-liquid separation unit comprises a condensate intermediate tank, a gas-liquid separation tank and a vacuumizing device which are connected in sequence.
And a heat source outlet pipeline of the two-effect preheater and a heat source outlet pipeline of the three-effect preheater in the three-effect countercurrent evaporator are respectively and independently connected with the condensate intermediate tank.
And a liquid outlet of a condenser in the triple-effect countercurrent evaporator is connected with the gas-liquid separation tank.
In the double-effect preheater and the triple-effect preheater, secondary steam is condensed after heat exchange, condensate flows into a condensate intermediate tank from a heat source outlet pipeline for primary gas-liquid separation, and then flows into a gas-liquid separation tank for gas-liquid separation. And (4) recovering the condensate for later use, and discharging the non-condensable gas out of the system for non-condensable gas treatment.
And secondary steam of the triple-effect evaporator is condensed by the condenser and then directly flows into the gas-liquid separation tank for gas-liquid separation, condensate is recovered for later use, and non-condensable gas is discharged out of the system for non-condensable gas treatment.
In a second aspect, the invention provides a method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system in the first aspect, wherein the method comprises the following steps:
(1) preheating the ammonia nitrogen wastewater, and performing multi-effect evaporation to obtain an evaporated gas and a concentrated solution;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) burning the concentrated solution obtained in the step (1), and sequentially carrying out heat exchange treatment, SCR denitration treatment and dust removal treatment on the combustion tail gas of the concentrated solution to finish treatment on the ammonia nitrogen wastewater;
the step (2) and the step (3) are not in sequence.
Preferably, the ammonia nitrogen wastewater is ammonia nitrogen wastewater generated by an amination process, the ammonia nitrogen content is 20000-30000mg/L, for example 20000mg/L, 21000mg/L, 22000mg/L, 23000mg/L, 24000mg/L, 25000mg/L, 26000mg/L, 27000mg/L, 28000mg/L, 29000mg/L or 30000mg/L, but not limited to the values listed, and other values not listed in the range of the values are also applicable; the COD is 10000-20000mg/L, for example 10000mg/L, 11000mg/L, 12000mg/L, 13000mg/L, 14000mg/L, 15000mg/L, 16000mg/L, 17000mg/L, 18000mg/L, 19000mg/L or 20000mg/L, but not limited to the values listed, and other values not listed in the numerical range are also applicable.
Preferably, the temperature after preheating in step (1) is 55-60 ℃, for example 55 ℃, 56 ℃, 57 ℃, 58 ℃, 59 ℃ or 60 ℃, but is not limited to the recited values, and other values not recited in the range of values are equally applicable.
The preheating is carried out by using saturated steam, and a person skilled in the art can select proper saturated steam pressure and dosage according to actual needs as long as the preheated ammonia nitrogen wastewater has the temperature of 55-60 ℃, and the invention is not limited to a large extent.
Preferably, the multi-effect evaporation of step (1) is triple-effect counter-current evaporation.
Preferably, in the triple-effect countercurrent evaporation process, the temperature of the single-effect evaporation is 90-110 ℃, for example, 90 ℃, 92 ℃, 95 ℃, 98 ℃, 100 ℃, 102 ℃, 105 ℃, 108 ℃ or 110 ℃, but is not limited to the recited values, and other values in the numerical range are also applicable; absolute pressures of 0.07 to 0.08MPa, for example 0.07MPa, 0.072MPa, 0.075MPa, 0.078MPa or 0.08MPa, but not limited to the values listed, other values not listed in the numerical range also applying; the evaporation amount is 30-35% of the mass of the ammonia nitrogen wastewater, for example, 30%, 31%, 32%, 33%, 34% or 35%, but is not limited to the recited values, and other values not recited in the numerical range are also applicable.
Preferably, in the triple-effect countercurrent evaporation process, the temperature of the double-effect evaporation is 75-90 ℃, for example, 75 ℃, 78 ℃, 80 ℃, 82 ℃, 85 ℃, 88 ℃ or 90 ℃, but the temperature is not limited to the recited values, and other values not recited in the numerical range are also applicable; absolute pressure of 0.035 to 0.045MPa, for example, 0.035MPa, 0.036MPa, 0.037MPa, 0.038MPa, 0.039MPa, 0.040MPa, 0.041MPa, 0.042MPa, 0.043MPa, 0.044MPa or 0.045MPa, but not limited to the values listed, and other values not listed in the numerical range are also applicable; the evaporation amount is 30-35% of the mass of the ammonia nitrogen wastewater, for example, 30%, 31%, 32%, 33%, 34% or 35%, but is not limited to the recited values, and other values not recited in the numerical range are also applicable.
Preferably, in the triple-effect countercurrent evaporation process, the temperature of the triple-effect evaporation is 60-75 ℃, for example, 60 ℃, 62 ℃, 64 ℃, 65 ℃, 66 ℃, 68 ℃, 70 ℃, 72 ℃ or 75 ℃, but not limited to the recited values, and other values not recited in the numerical range are also applicable; absolute pressure of 0.02 to 0.03MPa, for example, 0.02MPa, 0.022MPa, 0.024MPa, 0.025MPa, 0.027MPa, 0.028MPa or 0.03MPa, but not limited to the values listed, and other values not listed in the numerical range are also applicable; the evaporation amount is 25-30% of the mass of the ammonia nitrogen wastewater, for example, 25%, 26%, 27%, 28%, 29% or 30%, but is not limited to the recited values, and other values not recited in the numerical range are also applicable.
Preferably, the heat source of the one-effect evaporation is saturated steam, and the saturated steam provides heat for the one-effect evaporation and then preheats the ammonia nitrogen wastewater.
Preferably, the temperature of the concentrate obtained in step (1) is 88-100 deg.C, such as 88 deg.C, 90 deg.C, 92 deg.C, 94 deg.C, 95 deg.C, 96 deg.C, 98 deg.C or 100 deg.C, but is not limited to the recited values, and other values not recited in the range of values are also applicable.
The invention reduces the load on the combustion furnace during incineration treatment by making the temperature of the concentrated solution be 88-100 ℃, improves the incineration treatment effect, and reduces the content of nitrogen oxides generated during incineration treatment, thereby reducing the burden of subsequent SCR treatment on equipment.
Preferably, the temperature of the incineration treatment in the step (3) is 760-; the residence time is from 2 to 4s, and may be, for example, 2s, 2.5s, 3s, 3.5s or 4s, but is not limited to the values listed, and other values not listed in the numerical range are equally applicable.
The residence time is the residence time of the tail gas after incineration.
Preferably, the temperature of the SCR denitration treatment is 250-350 ℃, for example, 250 ℃, 260 ℃, 270 ℃, 280 ℃, 290 ℃, 300 ℃, 310 ℃, 320 ℃, 330 ℃, 340 ℃ or 350 ℃, but is not limited to the recited values, and other values not recited in the numerical range are also applicable.
The heat exchange treatment is to reduce the temperature of the combustion tail gas of the concentrated solution to the temperature of the SCR denitration treatment through heat exchange, so that the purpose of saving energy is achieved.
The dust removal treatment is carried out by using a spray liquid, but the temperature of the tail gas after the dust removal treatment is 180 ℃, for example, 120 ℃, 130 ℃, 140 ℃, 150 ℃, 160 ℃, 170 ℃ or 180 ℃, so as to eliminate the phenomenon of 'white fog'.
As a preferable technical solution of the method according to the second aspect of the present invention, the method comprises the steps of:
(1) preheating the ammonia nitrogen wastewater to 55-60 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 90-110 ℃, the absolute pressure is 0.07-0.08MPa, and the evaporation amount is 30-35% of the mass of the ammonia nitrogen wastewater; the temperature of the double-effect evaporation is 75-90 ℃, the absolute pressure is 0.035-0.045MPa, and the evaporation capacity is 30-35% of the mass of the ammonia nitrogen wastewater; the temperature of triple effect evaporation is 60-75 ℃, the absolute pressure is 0.02-0.03MPa, and the evaporation capacity is 25-30% of the mass of the ammonia nitrogen wastewater; obtaining the evaporated gas and the concentrated solution with the temperature of 88-100 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) carrying out incineration treatment on the concentrated solution obtained in the step (1) at 760-;
the step (2) and the step (3) are not in sequence.
Compared with the prior art, the invention has the following beneficial effects:
the invention carries out concentration treatment on the ammonia nitrogen wastewater and burns the concentrated solution, thereby recycling the ammonia nitrogen wastewater.
Drawings
FIG. 1 is a schematic structural diagram of an ammonia nitrogen wastewater treatment system provided in embodiment 1 of the present invention.
Wherein: 1, a filtering device; 2, a preheating unit; 31, a one-effect evaporator; 32, a single effect preheater; 41, a double-effect evaporator; 42, a two-effect preheater; 51, a triple effect evaporator; 52, a triple effect preheater; 6, a condenser; 71, a condensate intermediate tank; 72, a gas-liquid separation tank; 81, a direct-fired furnace; 82, a heat exchanger; 83, an SCR reactor; 84, a spray tower; 85, a chimney; and 9, a vacuum pump.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments. It should be understood by those skilled in the art that the examples are only for the understanding of the present invention and should not be construed as the specific limitations of the present invention.
Example 1
The embodiment provides an ammonia nitrogen wastewater treatment system, the structural schematic diagram of ammonia nitrogen wastewater treatment system is shown in figure 1, including: the device comprises a filtering device 1, a preheating unit 2, a three-effect countercurrent evaporator, a gas-liquid separation unit and a concentrated solution combustion unit.
The discharge hole of the preheating unit 2 is connected with the feed inlet of a triple-effect evaporator 51 in the triple-effect countercurrent evaporator, the condensate outlet of the triple-effect evaporator 51 in the triple-effect countercurrent evaporator is connected with the gas-liquid separation unit, and the liquid outlet of a single-effect evaporator 31 in the triple-effect countercurrent evaporator is connected with the concentrated solution combustion unit through a jacket pipeline.
The concentrated solution combustion unit comprises a direct-fired furnace 81, a heat exchanger 82, an SCR reactor 83, a spray tower 84 and a chimney 85 which are connected in sequence. The liquid outlet of the first evaporator 31 in the triple-effect countercurrent evaporator is connected with the direct-fired furnace 81 in the concentrated solution combustion unit through a jacket pipeline.
The preheating unit 2 is a shell-and-tube heat exchanger.
The primary preheater 32 of the triple-effect countercurrent evaporator is connected with an external heat source heat supply pipeline, and the external heat source heat supply pipeline is connected with the primary preheater 32 and then connected with the preheating unit 2, so that after the external heat source provides heat for the primary evaporator 31, heat is provided for the ammonia nitrogen wastewater, and the utilization rate of energy is improved.
The filtering device 1 is a precision filter with a filtering pore diameter of less than 0.5 mm.
The gas-liquid separation unit comprises a condensate intermediate tank 71, a gas-liquid separation tank 72 and a vacuumizing device which are connected in sequence. The heat source outlet pipelines of the two-effect preheater 42 and the three-effect preheater 52 in the three-effect countercurrent evaporator are respectively and independently connected with the condensate intermediate tank 71; the liquid outlet of the condenser 6 in the triple-effect countercurrent evaporator is connected with the gas-liquid separation tank 72. The vacuum pumping device is a vacuum pump 9 and is used for pumping the non-condensable gas in the gas-liquid separation tank 72.
Ammonia nitrogen wastewater filters in filter equipment 1, then flows into preheating unit 2 and preheats, and the ammonia nitrogen wastewater after preheating flows into triple effect adverse current evaporation unit and carries out evaporative concentration, and concentrated concentrate flows into concentrate combustion unit and burns, and gas after the burning carries out tail gas treatment after the heat transfer, reduces the content of nitrogen oxide in the tail gas. The condensate is recovered after the evaporation gas of multi-effect evaporation is condensed and separated from gas and liquid, so that the resource utilization of the ammonia nitrogen wastewater is realized, the energy consumption is low in the treatment process, and the pollutant removal rate is high.
The invention adopts a triple-effect countercurrent evaporator to evaporate and concentrate preheated ammonia nitrogen wastewater, wherein gas-phase and liquid-phase materials flow in a countercurrent way. The liquid phase direction is as follows: the preheated ammonia nitrogen wastewater firstly enters a triple-effect evaporator 51, exchanges heat in a triple-effect preheater 52 to raise the temperature, and enters a separation chamber of the triple-effect evaporator 51 for gas-liquid separation; after the ammonia nitrogen wastewater is concentrated to a certain concentration in the triple-effect evaporator 51, the ammonia nitrogen wastewater is sent into the double-effect evaporator 41 by a triple-effect material transfer pump for evaporation and concentration; after the ammonia nitrogen wastewater is concentrated to a certain degree in the double-effect evaporator 41, the ammonia nitrogen wastewater is sent to the single-effect evaporator 31 by the double-effect material transfer pump for evaporation and concentration, and after the ammonia nitrogen wastewater is concentrated to the process requirement, the ammonia nitrogen wastewater is conveyed to a direct-fired furnace 81 in a concentrated solution combustion unit by the single-effect material transfer pump.
The gas phase flow direction is as follows: the saturated steam enters a primary preheater 32 for heat exchange and condensation, and the condensate flows into a preheating unit 2 for preheating the ammonia nitrogen wastewater; the secondary steam generated by the first-effect evaporator 31 is used as a heat source of the second-effect preheater 42 and is condensed in the second-effect preheater 42; the secondary steam generated by the secondary evaporator 41 is used as a heat source of the triple-effect preheater 52 and is condensed in the triple-effect preheater 52; the secondary steam generated by the triple-effect evaporator 51 is condensed in the condenser 6, and the condensate flows into the gas-liquid separation unit. Wherein, the condensate of the two-effect preheater 42 and the three-effect preheater 52 flows into the condensate intermediate tank 71 and then flows into the gas-liquid separation tank 72; the condensate in the condenser 6 directly flows into the gas-liquid separation tank 72, and the non-condensable gas is recovered by the vacuum pump 9.
Application example 1
The application example provides a method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system provided in the embodiment 1, wherein the ammonia nitrogen wastewater is wastewater generated by an amination process, the ammonia nitrogen content is 24000-26000mg/L, and the COD is 15000-16000 mg/L; the method comprises the following steps:
(1) preheating the ammonia nitrogen wastewater to 58 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 100 ℃, the absolute pressure is 0.075MPa, and the evaporation capacity is 32% of the mass of the ammonia nitrogen wastewater; the temperature of the two-effect evaporation is 80 ℃, the absolute pressure is 0.04MPa, and the evaporation capacity is 32 percent of the mass of the ammonia nitrogen wastewater; the temperature of triple effect evaporation is 65 ℃, the absolute pressure is 0.025MPa, and the evaporation capacity is 27 percent of the mass of the ammonia nitrogen wastewater; obtaining evaporated gas and concentrated solution with the temperature of 91 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) burning the concentrated solution obtained in the step (1) at 810 ℃, wherein the retention time of burning gas is 3s, carrying out heat exchange treatment, SCR denitration treatment and dust removal treatment on the burning tail gas of the concentrated solution in sequence, and discharging the gas after the dust removal treatment from a chimney 85 to finish the treatment of ammonia nitrogen wastewater; the temperature of the SCR denitration treatment is 300 ℃, and the temperature of the gas after the dust removal treatment is 150 ℃;
the step (2) and the step (3) are not in sequence.
The content of nitrogen oxides in the tail gas discharged from the chimney 85 is less than or equal to 100mg/Nm3The content of nitrogen oxides is low, and the ammonia nitrogen wastewater is effectively treated.
Application example 2
The application example provides a method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system provided in the application example 1, wherein the ammonia nitrogen wastewater is wastewater generated by an amination process, the ammonia nitrogen content is 26000-; the method comprises the following steps:
(1) preheating the ammonia nitrogen wastewater to 56 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 95 ℃, the absolute pressure is 0.072MPa, and the evaporation capacity is 31 percent of the mass of the ammonia nitrogen wastewater; the temperature of the two-effect evaporation is 78 ℃, the absolute pressure is 0.038MPa, and the evaporation capacity is 31 percent of the mass of the ammonia nitrogen wastewater; the temperature of the triple effect evaporation is 62 ℃, the absolute pressure is 0.022MPa, and the evaporation capacity is 26 percent of the mass of the ammonia nitrogen wastewater; obtaining the evaporated gas and the concentrated solution with the temperature of 90 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) burning the concentrated solution obtained in the step (1) at 780 ℃ for 2.5s, sequentially carrying out heat exchange treatment, SCR denitration treatment and dust removal treatment on the combustion tail gas of the concentrated solution, and discharging the gas after the dust removal treatment from a chimney 85 to finish the treatment of ammonia nitrogen wastewater; the SCR denitration treatment temperature is 270 ℃, and the gas temperature after the dust removal treatment is 140 ℃;
the step (2) and the step (3) are not in sequence.
The content of nitrogen oxides in the tail gas discharged from the chimney 85 is less than or equal to 100mg/Nm3The content of nitrogen oxides is low, and the ammonia nitrogen wastewater is effectively treated.
Application example 3
The application example provides a method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system provided in the application example 1, wherein the ammonia nitrogen wastewater is wastewater generated by an amination process, the ammonia nitrogen content is 22000-; the method comprises the following steps:
(1) preheating the ammonia nitrogen wastewater to 59 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 105 ℃, the absolute pressure is 0.078MPa, and the evaporation capacity is 33 percent of the mass of the ammonia nitrogen wastewater; the temperature of the two-effect evaporation is 85 ℃, the absolute pressure is 0.042MPa, and the evaporation capacity is 33 percent of the mass of the ammonia nitrogen wastewater; the temperature of triple effect evaporation is 70 ℃, the absolute pressure is 0.027MPa, and the evaporation capacity is 28 percent of the mass of the ammonia nitrogen wastewater; obtaining the evaporated gas and a concentrated solution with the temperature of 95 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) burning the concentrated solution obtained in the step (1) at 850 ℃ for 3.5s, sequentially carrying out heat exchange treatment, SCR denitration treatment and dust removal treatment on the combustion tail gas of the concentrated solution, and discharging the gas after the dust removal treatment from a chimney 85 to finish the treatment of ammonia nitrogen wastewater; the temperature of SCR denitration treatment is 320 ℃, and the temperature of gas after dust removal treatment is 170 ℃;
the step (2) and the step (3) are not in sequence.
The content of nitrogen oxides in the tail gas discharged from the chimney 85 is less than or equal to 100mg/Nm3The content of nitrogen oxides is low, and the ammonia nitrogen wastewater is effectively treated.
Application example 4
The application example provides a method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system provided in the application example 1, wherein the ammonia nitrogen wastewater is wastewater generated by an amination process, the ammonia nitrogen content is 28000-30000mg/L, and the COD is 18000-20000 mg/L; the method comprises the following steps:
(1) preheating the ammonia nitrogen wastewater to 55 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 90 ℃, the absolute pressure is 0.07MPa, and the evaporation capacity is 30% of the mass of the ammonia nitrogen wastewater; the temperature of the double-effect evaporation is 75 ℃, the absolute pressure is 0.035MPa, and the evaporation capacity is 30 percent of the mass of the ammonia nitrogen wastewater; the temperature of triple effect evaporation is 60 ℃, the absolute pressure is 0.02MPa, and the evaporation capacity is 25 percent of the mass of the ammonia nitrogen wastewater; obtaining the evaporated gas and the concentrated solution with the temperature of 88 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) incinerating the concentrated solution obtained in the step (1) at 760 ℃, wherein the retention time of the incineration gas is 2s, sequentially performing heat exchange treatment, SCR denitration treatment and dust removal treatment on the combustion tail gas of the concentrated solution, and discharging the gas after the dust removal treatment from a chimney 85 to finish the treatment of the ammonia nitrogen wastewater; the temperature of the SCR denitration treatment is 250 ℃, and the temperature of the gas after the dust removal treatment is 120 ℃;
the step (2) and the step (3) are not in sequence.
The content of nitrogen oxides in the tail gas discharged from the chimney 85 is less than or equal to 100mg/Nm3The content of nitrogen oxides is low, and the ammonia nitrogen wastewater is effectively treated.
Application example 5
The application example provides a method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system provided in the application example 1, wherein the ammonia nitrogen wastewater is wastewater generated by an amination process, the ammonia nitrogen content is 20000-; the method comprises the following steps:
(1) preheating the ammonia nitrogen wastewater to 60 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 110 ℃, the absolute pressure is 0.08MPa, and the evaporation capacity is 35% of the mass of the ammonia nitrogen wastewater; the temperature of the double-effect evaporation is 90 ℃, the absolute pressure is 0.045MPa, and the evaporation capacity is 35 percent of the mass of the ammonia nitrogen wastewater; the temperature of triple effect evaporation is 75 ℃, the absolute pressure is 0.03MPa, and the evaporation capacity is 30 percent of the mass of the ammonia nitrogen wastewater; obtaining the evaporated gas and the concentrated solution with the temperature of 100 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) carrying out incineration treatment on the concentrated solution obtained in the step (1) at 900 ℃, wherein the retention time of incineration gas is 4s, carrying out heat exchange treatment, SCR denitration treatment and dust removal treatment on the combustion tail gas of the concentrated solution in sequence, and discharging the gas after the dust removal treatment from a chimney 85 to finish the treatment of ammonia nitrogen wastewater; the temperature of the SCR denitration treatment is 350 ℃, and the temperature of the gas after the dust removal treatment is 180 ℃;
the step (2) and the step (3) are not in sequence.
The content of nitrogen oxides in the tail gas discharged from the chimney 85 is less than or equal to 100mg/Nm3The content of nitrogen oxides is low, and the ammonia nitrogen wastewater is effectively treated.
In conclusion, the ammonia nitrogen wastewater is subjected to concentration treatment, and the concentrated solution is combusted, so that the ammonia nitrogen wastewater is recycled, and the system provided by the invention has the advantages of low energy consumption, high pollutant removal rate and positive effect on environmental protection.
The applicant declares that the above description is only a specific embodiment of the present invention, but the scope of the present invention is not limited thereto, and it should be understood by those skilled in the art that any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are within the scope and disclosure of the present invention.
Claims (10)
1. The ammonia nitrogen wastewater treatment system is characterized by comprising a preheating unit, a multi-effect evaporation unit, a gas-liquid separation unit and a concentrated solution combustion unit;
the discharge port of the preheating unit is connected with the feed port of the multi-effect evaporation unit, the condensate outlet of the multi-effect evaporation unit is connected with the gas-liquid separation unit, and the liquid outlet of the multi-effect evaporation unit is connected with the concentrated liquid combustion unit;
the concentrated solution combustion unit comprises a concentrated solution combustion device, a heat exchange device and a tail gas treatment device which are sequentially connected.
2. The ammonia nitrogen wastewater treatment system of claim 1, wherein the multi-effect evaporation unit is a three-effect counter-flow evaporator.
3. The ammonia nitrogen wastewater treatment system according to claim 1 or 2, wherein the preheating unit comprises a heat exchanger;
preferably, the heat exchanger comprises a shell and tube heat exchanger and/or a plate heat exchanger.
4. The ammonia nitrogen wastewater treatment system as set forth in claim 2 or 3, wherein the primary preheater of the triple-effect countercurrent evaporator is connected with an external heat source heat supply pipeline, and the external heat source heat supply pipeline is connected with the primary preheater and then connected with the preheating unit.
5. The ammonia nitrogen wastewater treatment system according to any one of claims 1-4, wherein a filter device is arranged at a feed inlet of the preheating unit;
preferably, the filtration device comprises a bag filter and/or a precision filter;
preferably, the filter device has a filter pore size of 0.5mm or less.
6. The ammonia nitrogen wastewater treatment system according to any one of claims 1-5, wherein the concentrated solution combustion device is a direct-fired furnace;
preferably, the heat exchange device is a heat exchanger;
preferably, the heat exchanger comprises a shell-and-tube heat exchanger and/or a plate heat exchanger;
preferably, the tail gas treatment device comprises an SCR reactor, a spray tower and a chimney which are connected in sequence;
preferably, the connecting pipeline of the multi-effect evaporation unit and the concentrated solution combustion device is a jacket pipeline and/or a heat tracing pipeline.
7. The ammonia nitrogen wastewater treatment system of any one of claims 2 to 6, wherein the gas-liquid separation unit comprises a condensate intermediate tank, a gas-liquid separation tank and a vacuum pumping device which are connected in sequence;
a heat source outlet pipeline of a double-effect preheater and a heat source outlet pipeline of a triple-effect preheater in the triple-effect countercurrent evaporator are respectively and independently connected with the condensate intermediate tank;
and a liquid outlet of a condenser in the triple-effect countercurrent evaporator is connected with the gas-liquid separation tank.
8. A method for treating ammonia nitrogen wastewater by using the ammonia nitrogen wastewater treatment system as defined in any one of claims 1-7, which is characterized by comprising the following steps:
(1) preheating the ammonia nitrogen wastewater, and performing multi-effect evaporation to obtain an evaporated gas and a concentrated solution;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) burning the concentrated solution obtained in the step (1), and sequentially carrying out heat exchange treatment, SCR denitration treatment and dust removal treatment on the combustion tail gas of the concentrated solution to finish treatment on the ammonia nitrogen wastewater;
the step (2) and the step (3) are not in sequence.
9. The method as claimed in claim 8, wherein the ammonia nitrogen wastewater in step (1) is ammonia nitrogen wastewater generated in amination process, the ammonia nitrogen content is 20000-30000mg/L, and the COD is 10000-20000 mg/L;
preferably, the temperature after preheating in the step (1) is 55-60 ℃;
preferably, the multi-effect evaporation of the step (1) is triple-effect countercurrent evaporation;
preferably, in the three-effect countercurrent evaporation process, the temperature of the one-effect evaporation is 90-110 ℃, the absolute pressure is 0.07-0.08MPa, and the evaporation amount is 30-35% of the mass of the ammonia nitrogen wastewater;
preferably, in the three-effect countercurrent evaporation process, the temperature of the two-effect evaporation is 75-90 ℃, the absolute pressure is 0.035-0.045MPa, and the evaporation amount is 30-35% of the mass of the ammonia nitrogen wastewater;
preferably, in the triple-effect countercurrent evaporation process, the triple-effect evaporation temperature is 60-75 ℃, the absolute pressure is 0.02-0.03MPa, and the evaporation capacity is 25-30% of the mass of the ammonia nitrogen wastewater;
preferably, the heat source of the one-effect evaporation is saturated steam, and the saturated steam provides heat for the one-effect evaporation and then preheats the ammonia nitrogen wastewater;
preferably, the temperature of the concentrated solution obtained in the step (1) is 88-100 ℃;
preferably, the temperature of the incineration treatment in the step (3) is 760 and 900 ℃, and the residence time is 2-4 s.
10. Method according to claim 8 or 9, characterized in that it comprises the following steps:
(1) preheating the ammonia nitrogen wastewater to 55-60 ℃, and then carrying out triple-effect countercurrent evaporation, wherein the temperature of the single-effect evaporation is 90-110 ℃, the absolute pressure is 0.07-0.08MPa, and the evaporation amount is 30-35% of the mass of the ammonia nitrogen wastewater; the temperature of the double-effect evaporation is 75-90 ℃, the absolute pressure is 0.035-0.045MPa, and the evaporation capacity is 30-35% of the mass of the ammonia nitrogen wastewater; the temperature of triple effect evaporation is 60-75 ℃, the absolute pressure is 0.02-0.03MPa, and the evaporation capacity is 25-30% of the mass of the ammonia nitrogen wastewater; obtaining the evaporated gas and the concentrated solution with the temperature of 88-100 ℃;
(2) condensing the evaporated gas in the step (1) and then carrying out gas-liquid separation;
(3) carrying out incineration treatment on the concentrated solution obtained in the step (1) at 760-;
the step (2) and the step (3) are not in sequence.
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