CN112694163A - Method for quenching waste water of catalytic wet-type acrylonitrile oxidation device - Google Patents
Method for quenching waste water of catalytic wet-type acrylonitrile oxidation device Download PDFInfo
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- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
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- 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
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- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
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- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- 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
Abstract
The invention relates to a method for catalytically wet-oxidizing acrylonitrile device quenching wastewater, which mainly solves the problems of high energy consumption and serious environmental pollution when acrylonitrile device quenching wastewater is treated by the prior art. The invention adopts the following steps: the technical scheme that the acrylonitrile device quenching wastewater raw material and oxygen enter a catalytic wet oxidation reaction zone after heat exchange, and are subjected to low-pressure isothermal catalytic wet oxidation reaction and high-pressure adiabatic catalytic wet oxidation in sequence to obtain the treated material better solves the problem and can be used in industrial application of acrylonitrile device quenching wastewater treatment.
Description
Technical Field
The invention relates to a method for quenching wastewater in a catalytic wet-type acrylonitrile oxidation device.
Background
Acrylonitrile (AN) is AN important basic organic raw material and is widely used in the field of manufacturing chemical products such as synthetic fibers, synthetic rubbers, synthetic resins, and the like. At present, the main process for producing acrylonitrile in China is a propylene ammoxidation method, namely, propylene, ammonia gas and air are used as main raw materials, acrylonitrile is obtained under certain reaction conditions and the action of a catalyst, and simultaneously, a byproduct, namely ethylene, is producedNitrile, hydrocyanic acid, and the like. In the above-mentioned acrylonitrile production process, plant waste water mainly comprising quench waste water and refined waste water is generated, and these waste waters are highly toxic, highly colored and complex in composition. Wherein the quenched wastewater is more difficult to treat due to higher COD value. The quenching waste water is divided into one-section type and two-section type process quenching waste water according to different types of the quenching tower. The process wastewater of the one-section type quenching tower only has one stream of wastewater, and the wastewater is treated by concentration, incineration and sulfuric acid recovery. The two-section type quench tower process wastewater generates two wastewater streams, namely upper-section ammonium sulfate wastewater and lower-section tower kettle wastewater, the upper-section wastewater is concentrated to recover ammonium sulfate, condensate generated in the process returns to the upper section of the quench tower, and mother liquor and the lower-section wastewater of the quench tower are concentrated together and then are subjected to incineration treatment. The defects of the incineration method for treating the quenching wastewater are as follows: on one hand, the incineration belongs to a high energy consumption process; on the other hand, the incineration process will produce SO2、NOXAnd the like, and causes pollution to the environment. Therefore, the development of a method for effectively treating the quenching wastewater of the acrylonitrile device ensures that the treated wastewater meets the environmental protection requirement and the realization of the green production of the acrylonitrile device is very important.
Wet oxidation is a technology developed in the 50 s of the 20 th century for treating toxic, harmful and high-concentration organic wastewater. The method is to oxidize organic pollutants into CO in a liquid phase by taking air or pure oxygen as an oxidant under the conditions of high temperature (125-320 ℃) and high pressure (0.5-20 MPa)2And inorganic substances such as water and the like or small molecular organic substances. The method has the advantages of wide application range, high treatment efficiency, high oxidation rate, less secondary pollution, low energy consumption, small occupied area and the like. On the basis of wet oxidation technology, the developed catalytic wet oxidation technology is to add a high-efficiency and stable catalyst designed according to the composition of wastewater in the traditional wet oxidation process. The technology can greatly improve the oxidation efficiency, shorten the reaction residence time, reduce the temperature and pressure required by the reaction and reduce the production cost. CN1166574C discloses a method for treating industrial wastewater with high sulfur content, which comprises diluting wastewater, and treating wastewater by wet oxidation and electric multiphase catalytic oxidationAfter the two technologies are combined and applied, the total removal rate of COD of the organic wastewater reaches 89.6% -92.32%. The method needs a set of electrolytic oxidation device besides the wet oxidation device, and has complex process flow and high operation cost. CN106865860A discloses an energy recovery type wastewater catalytic wet oxidation treatment device and a wastewater treatment method, the method comprises the steps of mixing a homogeneous catalyst and wastewater, obtaining primary treated water and secondary treated water through a first reaction tower and a second reaction tower respectively, evaporating the secondary treated water through an MVR evaporator to obtain crystal salt, condensed water and a distilled mother liquor containing the homogeneous catalyst, wherein the condensed water enters a third reaction tower filled with the heterogeneous catalyst for further treatment, and finally obtaining liquid phase water meeting the emission standard. In the method, an MVR evaporator is required to treat the second treatment water, and the treatment, the recycling and the like of the homogeneous catalyst increase the complexity of the whole process flow and have high investment and operation cost. CN1167089A discloses a process for the treatment of acrylonitrile plant wastewater by first evaporating the wastewater to produce a gas stream containing steam, ammonia and volatile organic compounds, and then passing the gas stream into a catalytic reactor to convert it at elevated temperature to a mixture containing hydrogen, nitrogen and carbon dioxide. The method can only treat volatile substances in the wastewater and cannot treat high polymers and high-boiling-point organic matters. CN106348421A discloses a continuous wet oxidation process for degrading high-concentration organic wastewater and equipment thereof, the method comprises the steps of firstly exchanging heat between raw wastewater and treated wastewater, then mixing the heated wastewater with an oxidant, then feeding the mixture into a reactor for oxidation reaction, and feeding the treated wastewater into a separation process after exchanging heat and cooling. The method adopts a homogeneous catalyst, so that the separation of the treated wastewater is complex; in addition, when the COD concentration of the wastewater is high, the excessive heat generated by the reaction can cause a large amount of reaction wastewater to be vaporized, the heat loss is large, and the reaction effect is influenced. CN106380021A discloses a wet oxidation treatment system and method for high-concentration organic wastewater, which comprises the steps of firstly pretreating raw material wastewater, mixing the pretreated raw material wastewater with oxygen heated by heat exchange after heat exchange and heating, feeding the mixture into a reaction system, feeding reaction discharge materials into a reaction system after heat exchange and coolingA gas-liquid separation system. The COD removal rate of the method is low, and similarly, when the COD concentration of the treated wastewater is high, a large amount of reaction wastewater in the reactor is vaporized, the heat loss is large, and the reaction effect is influenced. CN107572651A discloses a method and a device for treating industrial wastewater by multistage wet oxidation, wherein the method comprises the steps of sequentially carrying out primary oxidation, secondary oxidation and tertiary oxidation on the industrial wastewater, the temperature of the primary oxidation is lower than that of the secondary oxidation, the temperature of the secondary oxidation is lower than that of the tertiary oxidation, and the tertiary oxidation supplies heat for the secondary oxidation and the primary oxidation in sequence. The method has complex reaction process and low COD removal rate. CN108455719A discloses a high-concentration organic wastewater wet oxidation treatment system and a treatment method, wherein wastewater and oxygen are introduced into a reactor with heating and stirring functions for oxidation reaction, and the reaction discharge material is cooled and then enters a gas-liquid separation system. The reaction device of the method is complex and discontinuous in wastewater treatment.
Disclosure of Invention
The invention relates to a method for quenching wastewater in a catalytic wet-type acrylonitrile oxidation device. The invention aims to solve the technical problems of high energy consumption and serious environmental pollution when the quenching wastewater is treated in the prior art. Provides a new method for treating quenching wastewater in the acrylonitrile production process. When the method is used for treating the quenching wastewater, the method has the characteristics of simple process flow, high COD removal rate, full heat utilization, environmental protection and high economic benefit.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: the process of quenching waste water in catalytic wet acrylonitrile oxidizing apparatus includes the following steps:
mixing a quenching wastewater raw material of an acrylonitrile device with a first stream of oxygen-containing gas (preferably oxygen), and then entering a catalytic wet oxidation reaction zone to obtain a treated material;
the catalytic wet oxidation reaction zone comprises two catalytic wet oxidation reactors, namely a catalytic wet oxidation isothermal reactor and a catalytic wet oxidation adiabatic reactor, and the wastewater raw material sequentially passes through the isothermal reactor and the adiabatic reactor;
the reaction discharge of the isothermal reactor enters a first gas-liquid separation tank for separation, a condensate obtained by cooling a gas-phase material at the top of the first gas-liquid separation tank is mixed with a liquid-phase material at the bottom of the first gas-liquid separation tank, and then the condensate is mixed with a second stream of oxygen-containing gas (preferably oxygen) and then enters an adiabatic reactor;
the reaction temperature of the isothermal reactor is 200-260 ℃, and the reaction pressure is 3-7 MPaG;
the inlet temperature of the adiabatic reactor is 190-250 ℃, and the reaction pressure is 7-13 MPaG;
the air input amount of oxygen in the first strand of oxygen-containing gas is 50-90% of the total air input amount of oxygen in the first strand of oxygen-containing gas and the second strand of oxygen-containing gas.
In the technical scheme, the acrylonitrile device quenching wastewater raw material is mixed with the first stream of oxygen-containing gas and then enters the catalytic wet oxidation reaction zone after heat exchange (preferably after heat exchange by a feeding and discharging heat exchanger).
In the technical scheme, the gas-phase material at the top of the first gas-liquid separation tank is cooled and then enters the second gas-liquid separation tank, and the condensate is obtained at the bottom of the second gas-liquid separation tank.
In the technical scheme, the COD value of the quenching wastewater raw material is 80000 mg/L-300000 mg/L, and the removal rate of COD after catalytic wet oxidation treatment is more than 95%.
In the technical scheme, the inner tube side of the catalytic wet oxidation isothermal reactor is a heat removing medium, the shell side is filled with a catalyst, and the quenching wastewater is subjected to catalytic wet oxidation reaction on the shell side.
In the technical scheme, the reaction temperature of the catalytic wet oxidation isothermal reactor is more preferably 210-250 ℃, and the reaction pressure is more preferably 4-6 MPaG.
In the technical scheme, the reaction volume space velocity of the catalytic wet oxidation isothermal reactor is preferably 0.2-1.5 h-1。
When entering a catalytic wet oxidation reaction zone, the quenched wastewater firstly enters an isothermal reactor, and most organic pollutants in the quenched wastewater are removed through isothermal reaction under relatively low pressure, so that the COD value of the quenched wastewater is greatly reduced. And then the isothermal reaction discharge enters an adiabatic reactor, and the residual organic pollutants in the quenching wastewater are removed through adiabatic reaction at relatively high pressure. By combining and optimizing the low-pressure isothermal reaction and high-pressure adiabatic reaction process technology, the high removal rate of organic pollutants in the quenching wastewater is realized, and the operation severity and the investment cost of the device are greatly reduced.
In the technical scheme, the reaction temperature of the catalytic wet oxidation adiabatic reactor is more preferably 200-240 ℃, and the reaction pressure is more preferably 8-12 MPaG.
In the technical scheme, the reaction volume space velocity of the catalytic wet oxidation adiabatic reactor is preferably 1.0-2.0 h-1。
In the above technical scheme, the air input amount of oxygen in the first strand of oxygen-containing gas is more preferably 60-85% of the total air input amount of oxygen in the first strand of oxygen-containing gas and the second strand of oxygen-containing gas.
In the technical scheme, the air input of the oxygen is 1.1-1.3 times of the theoretical oxygen consumption required by the COD value of the raw material quenching wastewater.
In the technical scheme, the catalyst filled in the isothermal reactor and the adiabatic reactor is at least one of a composite metal oxide catalyst and a noble metal supported catalyst.
In the acrylonitrile process, the COD value of acrylonitrile quenching wastewater is higher than that of other wastewater, and the treatment difficulty is higher.
The invention treats the quenching wastewater of the acrylonitrile device by adopting the catalytic wet oxidation technology, thereby avoiding the problems of high energy consumption and serious environmental pollution when the quenching wastewater is treated by adopting the traditional incineration method; by applying two reaction processes of low-pressure isothermal reaction and high-pressure adiabatic reaction, the heat exchange of feeding and discharging and the whole process flow are optimized, and the air inflow of oxygen entering an isothermal reactor and an adiabatic reactor is distributed and regulated, so that the reaction effect of catalytic wet oxidation is improved, the investment cost of the device is greatly reduced while the high-COD value wastewater treatment is realized; in addition, the whole process of treating the wastewater by catalytic wet oxidation is ensured to be in a stable and controllable state, the process is simple, the COD removal rate is high, the environmental protection and economic benefits are high, the industrialization is easy to realize, and a better technical effect is obtained.
Drawings
FIG. 1 is a schematic diagram of the process flow of the method for quenching wastewater in the catalytic wet-type acrylonitrile oxidation device.
In fig. 1, 1 is a raw material of quenched wastewater, 2 is oxygen, 3 is a heat removal medium, 4 is an isothermal reaction discharge material, 5 is a gas-phase discharge material of a first gas-liquid separation tank, 6 is a liquid-phase discharge material of the first gas-liquid separation tank, 7 is a noncondensable gas at the top of a second gas-liquid separation tank, 8 is a liquid-phase discharge material of the second gas-liquid separation tank, 9 is an adiabatic reaction discharge material, 10 is a noncondensable gas at the top of a third gas-liquid separation tank, 11 is a liquid-phase discharge material of the third gas-liquid separation tank, R1 and R2 are respectively a catalytic wet oxidation isothermal reactor and a catalytic wet oxidation adiabatic reactor, E1 is a charge and discharge heat exchanger, E2 is a first discharge cooler, E3 is a steam generator or a heat recovery device, E4 is a second discharge cooler, and D1, D2 and D3 are respectively a first gas-liquid separation tank.
According to the flow shown in figure 1, the raw material 1 of the quenching wastewater and a part of gas in the oxygen 2 are mixed and then enter a charging and discharging heat exchanger E1, and enter the shell side of a catalytic wet oxidation isothermal reactor R1 from the bottom after heat exchange and temperature rise. The heat released by the reaction is removed by the heat removing medium 3 in the pipe path R1. The isothermal reaction output 4 enters a first gas-liquid separation tank D1. And the gas phase discharge 5 of the first gas-liquid separation tank enters a second gas-liquid separation tank D2 after being cooled by a first discharge cooler E2. And (3) discharging non-condensable gas 7 from the top of the D2, mixing a liquid phase discharge 8 of a second gas-liquid separation tank obtained from the bottom with a liquid phase discharge 6 of a first gas-liquid separation tank and the rest of oxygen, and then feeding the mixture into the catalytic wet oxidation adiabatic reactor R2 from the bottom. And the adiabatic reaction discharge 9 enters a third gas-liquid separation tank D3 after sequentially passing through a feed and discharge heat exchanger E1 for heat exchange and temperature reduction, a steam generator or a heat recoverer E3 for heat recovery and a second discharge cooler E4 for cooling. The non-condensable gas 10 is discharged from the top of the D3, and the liquid phase discharged from the bottom 11 is discharged to the outside as treated wastewater.
The present invention will be further described with reference to specific examples, but the scope of the present invention is not limited to the scope covered by the examples.
Detailed Description
[ example 1 ]
As shown in figure 1, the COD value of the quenched wastewater raw material is 285320mg/L, the reaction temperature of the isothermal reactor in the catalytic wet oxidation reaction zone is 250 ℃, the reaction pressure is 7.0MPaG, and the volume space velocity is 0.3h-1The catalyst is composite metal oxide catalyst Al2O3(ii) a The inlet temperature of the adiabatic reactor is 230 ℃, the inlet pressure is 12.0MPaG, and the volume space velocity is 1.0h-1The loaded catalyst is a noble metal supported catalyst Pd/Al2O3(ii) a The air input of the oxygen is 1.2 times of the theoretical oxygen consumption required by the COD value of the raw material of the quenching wastewater; the oxygen amount entering from the front of the feeding and discharging heat exchanger and the front of the adiabatic reactor is respectively 90 percent and 10 percent of the total air input amount; the COD removal rate of the obtained quenched wastewater was 95.8%.
[ example 2 ]
As shown in figure 1, the COD value of the quenched wastewater raw material is 237166mg/L, the reaction temperature of the isothermal reactor in the catalytic wet oxidation reaction zone is 240 ℃, the reaction pressure is 6.5MPaG, and the volume space velocity is 0.5h-1The catalyst is composite metal oxide catalyst Al2O3(ii) a The inlet temperature of the adiabatic reactor is 225 ℃, the inlet pressure is 11.2MPaG, and the volume space velocity is 1.2h-1The loaded catalyst is a composite metal oxide catalyst Pd/Al2O3(ii) a The air input of the oxygen is 1.2 times of the theoretical oxygen consumption required by the COD value of the raw material of the quenching wastewater; the oxygen amount entering from the front of the feeding and discharging heat exchanger and the front of the adiabatic reactor is 85 percent and 15 percent of the total air input amount respectively; the COD removal rate of the obtained quenched wastewater was 96.3%.
[ example 3 ]
As shown in figure 1, the COD value of the quenched wastewater raw material is 192074mg/L, the reaction temperature of the isothermal reactor in the catalytic wet oxidation reaction zone is 235 ℃, the reaction pressure is 6.0MPaG, and the volume space velocity is 1.5h-1The loaded catalyst is a composite metal oxide catalyst ZrO2(ii) a The inlet temperature of the adiabatic reactor is 210 ℃, the inlet pressure is 10.5MPaG, and the volume space velocity is 2.0h-1The loaded catalyst is a composite metal oxide catalyst ZrO2(ii) a The air input of the oxygen is 1.1 times of the theoretical oxygen consumption required by the COD value of the raw material of the quenching wastewater; the oxygen amount entering from the front of the feeding and discharging heat exchanger and the front of the adiabatic reactor is 85 percent and 15 percent of the total air input amount respectively; the COD removal rate of the obtained quenched wastewater was 95.2%.
[ example 4 ]
As shown in figure 1, the COD value of the quenched wastewater raw material is 156833mg/L, the reaction temperature of the isothermal reactor in the catalytic wet oxidation reaction zone is 230 ℃, the reaction pressure is 5.5MPaG, and the volume space velocity is 1.2h-1The catalyst is composite metal oxide catalyst Al2O3(ii) a The inlet temperature of the adiabatic reactor was 205 ℃, the inlet pressure was 9.8MPaG, and the volume space velocity was 1.8h-1The loaded catalyst is a composite metal oxide catalyst ZrO2(ii) a The air input of the oxygen is 1.1 times of the theoretical oxygen consumption required by the COD value of the raw material of the quenching wastewater; the oxygen amount entering from the front of the feeding and discharging heat exchanger and the front of the adiabatic reactor is respectively 80 percent and 20 percent of the total air input amount; the COD removal rate of the obtained quenched wastewater was 96.1%.
[ example 5 ]
As shown in figure 1, the COD value of the quenched wastewater raw material is 129578mg/L, the reaction temperature of the isothermal reactor in the catalytic wet oxidation reaction zone is 220 ℃, the reaction pressure is 4.5MPaG, and the volume space velocity is 1.0h-1The loaded catalyst is a noble metal supported catalyst Ru/ZrO2(ii) a The inlet temperature of the adiabatic reactor was 205 ℃, the inlet pressure was 8.5MPaG, and the volume space velocity was 1.5h-1The loaded catalyst is a composite metal oxide catalyst ZrO2(ii) a The air input of the oxygen is 1.3 times of the theoretical oxygen consumption required by the COD value of the raw material of the quenching wastewater; the oxygen amount entering from the front of the feeding and discharging heat exchanger and the front of the adiabatic reactor is respectively 75 percent and 25 percent of the total air input amount; the COD removal rate of the obtained quenched wastewater was 97.4%.
[ example 6 ]
As shown in figure 1, the COD value of the quenched wastewater raw material is 81724mg/L, the reaction temperature of the isothermal reactor in the catalytic wet oxidation reaction zone is 210 ℃, the reaction pressure is 3.0MPaG, and the volume space velocity is 0.8h-1Loaded with catalystThe agent is noble metal loaded catalyst Pd/ZrO2(ii) a The inlet temperature of the adiabatic reactor is 200 ℃, the inlet pressure is 7.5MPaG, and the volume space velocity is 1.2h-1The loaded catalyst is a noble metal supported catalyst Pd/Al2O3(ii) a The air input of the oxygen is 1.3 times of the theoretical oxygen consumption required by the COD value of the raw material of the quenching wastewater; the oxygen amount entering from the front of the feeding and discharging heat exchanger and the front of the adiabatic reactor is respectively 55 percent and 45 percent of the total air input amount; the COD removal rate of the obtained quenched wastewater was 97.7%.
[ COMPARATIVE EXAMPLE 1 ]
The conditions and procedures of example 6 were followed, with the other operating conditions being maintained, and the catalytic wet oxidation reaction zone contained only one adiabatic reactor. The COD removal rate of the quenched waste water obtained at this time was 65.3%.
[ COMPARATIVE EXAMPLE 2 ]
The process was carried out under the conditions and in the same manner as in example 6, except that the isothermal reactor was placed in the catalytic wet oxidation zone before the adiabatic reactor, and the wastewater was passed through the adiabatic reactor and the isothermal reactor in this order. At the moment, a feeding heater is required to be added between the feeding and discharging heat exchanger and the adiabatic reactor to make up for the problem that the raw material wastewater cannot be preheated to the inlet temperature required by the adiabatic reaction due to the lower outlet temperature of the isothermal reactor. Not only increases the equipment investment, but also needs 52kW extra heat per ton of quenched wastewater.
[ COMPARATIVE EXAMPLE 3 ]
According to the conditions and procedures of example 6, other operating conditions were kept unchanged, the reaction temperature of the isothermal reactor was 195 ℃ and the inlet pressure of the adiabatic reactor was 6.5MPaG, at which time the COD removal rate of the obtained quenched wastewater was 88.5%.
Claims (10)
1. The process of quenching waste water in catalytic wet acrylonitrile oxidizing apparatus includes the following steps:
mixing a quenching wastewater raw material of an acrylonitrile device with a first stream of oxygen-containing gas (preferably oxygen), and then entering a catalytic wet oxidation reaction zone to obtain a treated material;
the catalytic wet oxidation reaction zone comprises two catalytic wet oxidation reactors, namely a catalytic wet oxidation isothermal reactor and a catalytic wet oxidation adiabatic reactor, and the wastewater raw material sequentially passes through the isothermal reactor and the adiabatic reactor;
the reaction discharge of the isothermal reactor enters a first gas-liquid separation tank for separation, a condensate obtained by cooling a gas-phase material at the top of the first gas-liquid separation tank is mixed with a liquid-phase material at the bottom of the first gas-liquid separation tank, and then the condensate is mixed with a second stream of oxygen-containing gas (preferably oxygen) and then enters an adiabatic reactor;
the reaction temperature of the isothermal reactor is 200-260 ℃, and the reaction pressure is 3-7 MPaG;
the inlet temperature of the adiabatic reactor is 190-250 ℃, and the reaction pressure is 7-13 MPaG;
the air input amount of oxygen in the first strand of oxygen-containing gas is 50-90% of the total air input amount of oxygen in the first strand of oxygen-containing gas and the second strand of oxygen-containing gas.
2. The method for quenching waste water of a catalytic wet oxidation acrylonitrile device according to claim 1, wherein the raw material of the quenching waste water of the acrylonitrile device is mixed with the first stream of oxygen-containing gas and then enters the catalytic wet oxidation reaction zone after heat exchange (preferably after heat exchange by a feed and discharge heat exchanger).
3. The method for quenching wastewater of a catalytic wet acrylonitrile oxidation device according to claim 1, wherein the gas phase material at the top of the first gas-liquid separation tank is cooled and then enters the second gas-liquid separation tank, and a condensate is obtained at the bottom of the second gas-liquid separation tank.
4. The method for rapid cooling waste water of catalytic wet oxidation acrylonitrile device as claimed in claim 1, wherein COD value of raw material of rapid cooling waste water of acrylonitrile device is 80000 mg/L-300000 mg/L.
5. The method for quenching wastewater of a catalytic wet oxidation acrylonitrile device according to claim 1, wherein the tube side in the isothermal reactor is a heat removal medium, and the shell side is filled with a catalyst.
6. The method for quenching wastewater of a catalytic wet-type acrylonitrile oxidation device according to claim 1, wherein the reaction temperature of the isothermal reactor is 210-250 ℃, the reaction pressure is 4-6 MPaG, and/or the reaction volume space velocity is 0.2-1.5 h-1。
7. The method for quenching wastewater of a catalytic wet acrylonitrile oxidation device according to claim 1, wherein the reaction temperature of the adiabatic reactor is 200-240 ℃ and/or the reaction pressure is 8-12 MPa; and/or the space velocity of the reaction volume is 1.0-2.0 h-1。
8. The method for quenching wastewater of a catalytic wet-type acrylonitrile oxidation device according to claim 1, wherein the air input amount of oxygen in the first stream of oxygen-containing gas is 60-85% of the total air input amount of oxygen in the first stream of oxygen-containing gas and the second stream of oxygen-containing gas.
9. The method for quenching wastewater of a catalytic wet oxidation acrylonitrile device according to claim 1, wherein the amount of oxygen gas input is 1.1-1.3 times of the theoretical oxygen consumption required by the COD value of the raw quenching wastewater.
10. The method for quenching wastewater of a catalytic wet oxidation acrylonitrile unit as claimed in claim 1, wherein the isothermal reactor and the adiabatic reactor are both filled with a catalyst selected from at least one of a composite metal oxide catalyst and a noble metal supported catalyst.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115490356A (en) * | 2022-08-31 | 2022-12-20 | 湖北泰盛化工有限公司 | Glyphosate mother liquor wet oxidation treatment system and oxidation treatment method |
| CN116675364A (en) * | 2023-05-16 | 2023-09-01 | 江苏立业环境科技有限公司 | Treatment process for treating acrylonitrile sewage |
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| CN115490356B (en) * | 2022-08-31 | 2023-10-31 | 湖北泰盛化工有限公司 | Wet oxidation treatment system and oxidation treatment method for glyphosate mother liquor |
| CN116675364A (en) * | 2023-05-16 | 2023-09-01 | 江苏立业环境科技有限公司 | Treatment process for treating acrylonitrile sewage |
| CN116675364B (en) * | 2023-05-16 | 2023-10-20 | 江苏立业环境科技有限公司 | Treatment process for treating acrylonitrile sewage |
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