CN114349246B - Combined treatment method of polycyclic aromatic hydrocarbon wastewater - Google Patents
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- 239000002351 wastewater Substances 0.000 title claims abstract description 127
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 42
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 29
- 230000003647 oxidation Effects 0.000 claims abstract description 26
- 238000009279 wet oxidation reaction Methods 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 230000035484 reaction time Effects 0.000 claims description 19
- 238000001514 detection method Methods 0.000 claims description 16
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 230000015556 catabolic process Effects 0.000 claims description 3
- 238000006731 degradation reaction Methods 0.000 claims description 3
- 239000000126 substance Substances 0.000 abstract description 19
- 238000004065 wastewater treatment Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 2
- 239000010865 sewage Substances 0.000 abstract description 2
- 238000005070 sampling Methods 0.000 description 15
- 239000007789 gas Substances 0.000 description 14
- 239000007788 liquid Substances 0.000 description 7
- IZUPBVBPLAPZRR-UHFFFAOYSA-N pentachlorophenol Chemical compound OC1=C(Cl)C(Cl)=C(Cl)C(Cl)=C1Cl IZUPBVBPLAPZRR-UHFFFAOYSA-N 0.000 description 6
- 230000001699 photocatalysis Effects 0.000 description 4
- 238000013032 photocatalytic reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000007146 photocatalysis Methods 0.000 description 3
- 238000010170 biological method Methods 0.000 description 2
- 230000000593 degrading effect Effects 0.000 description 2
- 230000016507 interphase Effects 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 238000000053 physical method Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000002604 ultrasonography Methods 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical group [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000013259 porous coordination polymer Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000012086 standard solution Substances 0.000 description 1
- 238000009210 therapy by ultrasound Methods 0.000 description 1
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Abstract
The invention discloses a combined treatment method of polycyclic aromatic hydrocarbon wastewater, and relates to the wastewater treatment technology. The method utilizes an ozone and wet oxidation process to treat the polycyclic aromatic hydrocarbon wastewater, thereby realizing standard emission. According to the treatment method of the polycyclic aromatic hydrocarbon wastewater, the air-lift type loop reactor is utilized for carrying out ozone oxidation pretreatment on the polycyclic aromatic hydrocarbon wastewater, so that the biodegradability of the polycyclic aromatic hydrocarbon wastewater is improved. After pretreatment, the micro-channels are used for wet oxidation to degrade the substances difficult to degrade. The polycyclic aromatic hydrocarbon wastewater treatment method effectively solves the problems of discharge and treatment of the chemical wastewater, has high sewage treatment efficiency and stable effect, and is convenient for popularization and use.
Description
Technical Field
The invention relates to a method for treating polycyclic aromatic hydrocarbon wastewater by combining ozone oxidation and wet oxidation, belonging to the wastewater treatment technology.
Background
At present, polycyclic aromatic hydrocarbon wastewater is mainly divided into a physical method, a chemical method and a biological method; the physical method mainly comprises adsorption, coagulating sedimentation and the like; the chemical method is mainly a different advanced oxidation method; the biological method mainly comprises aerobic biological treatment and anaerobic biological treatment.
The advanced oxidation mainly comprises an electrochemical oxidation method, a photocatalytic oxidation method, an ozone oxidation method, a Fenton oxidation method and a wet oxidation method. Wherein the ozone oxidation method is a wastewater treatment technology for oxidizing organic matters in wastewater by using ozone as an oxidant, and the biodegradability of the wastewater is improved for improving B/C. The ozone oxidation method is a good choice for preliminary pretreatment of the wastewater with high COD, and can decompose macromolecular organic matters in the wastewater into micromolecular organic matters and remove chromaticity of the wastewater.
Chinese patent CN201310047909.8 discloses a method for degrading pentachlorophenol by enhanced ozone oxidation in a microchannel, which uses a microchannel reactor, which is a high-efficiency gas-liquid mass transfer device, to efficiently remove typical POPs-PCPs in water. The treatment process comprises the following steps: (1) The prepared pentachlorophenol dilute solution with certain concentration enters a micro-channel through a high-pressure pump, and ozone is conveyed into the micro-channel through another pipeline to react; (2) And the reacted liquid enters a gas-liquid separator for gas-liquid separation. The method has the advantages that the pentachlorophenol removal rate reaches 100%, but the TOC removal rate is only about 50%, the organic matters in the wastewater are not completely degraded, and the wastewater still contains small molecular organic matters, and is suitable for low-concentration characteristic pollutant wastewater.
Chinese patent CN202011264966.8 discloses an advanced oxidation method and apparatus for ultrasound, H 2O2 and micro-channel, which uses H 2O2 as oxidant, and the ultrasound and micro-channel cooperate to treat waste water. The treatment process comprises the following steps: (1) Mixing wastewater to be treated with hydrogen peroxide solution, and sending the mixed wastewater into a micro-channel of a micro-channel reactor for reaction; (2) The oxidation intermediate liquid in the micro-channel is subjected to ultrasonic treatment through an ultrasonic generator while being fed into the micro-channel; (3) And (3) carrying out sewage biochemical treatment on the solution obtained after the reaction in the step (2). The method uses an ultrasonic generator, is difficult to operate, is difficult to control the reaction rate, and is not suitable for treating a large amount of wastewater.
Chinese patent CN104909504a discloses a method for treating high-salt high-COD organic wastewater, which uses a method of combining electrocatalytic oxidation with various catalytic oxidation to treat wastewater having a COD of 600 ppm. This patent is only applicable to wastewater treatment with low COD content.
In the research of degrading polycyclic aromatic hydrocarbon in printing and dyeing wastewater in the university of Guangdong industry Kong Minyi of the university of Shuoshi, 16 kinds of polycyclic aromatic hydrocarbon mixed standard solutions are taken as research objects, and the maximum degradation rate of the polycyclic aromatic hydrocarbon in the wastewater can reach 93.2% by adopting an ultrasonic-Fenton method. However, the method is only carried out in an ideal system at present, and the actual wastewater has complex components and is not applied to the actual wastewater.
Disclosure of Invention
The invention provides a treatment method of polycyclic aromatic hydrocarbon wastewater, which combines ozone oxidation and wet oxidation, and the wet oxidation uses a microchannel reactor as a reactor. The OH generated by ozone follows a hydroxyl radical chain reaction mechanism to decompose macromolecular organic matters in the wastewater into micromolecular organic matters, and the micromolecular organic matters and refractory organic matters are oxidized into H 2 O and CO 2 by wet oxidation in a micro-channel. The reaction time is shortened through high mass and heat transfer, and the reaction efficiency is high.
In order to realize the method, the invention adopts the following technical scheme:
the treatment method of the polycyclic aromatic hydrocarbon wastewater comprises the following steps:
(1) And regulating the pH of the polycyclic aromatic hydrocarbon wastewater, and enabling the wastewater after regulating the pH to enter an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, the wastewater enters the reactor from a flow-down area of the reactor, and the wastewater flows out from a water outlet of the reactor. And (5) sampling and detecting.
(2) Waste water at the water outlet of the bottom of the tower enters the microchannel reactor through the metering pump to be preheated and then enters the reaction zone to carry out wet oxidation reaction, the flow rate is controlled by adjusting the metering pump, so that the reaction residence time is controlled, and the reaction temperature is controlled by an external circulating heat exchange system. And the wastewater is discharged after reaching the standard after detection.
Wherein the pH is adjusted to 9-11, preferably 9-10.
Wherein the mass ratio of the ozone to COD in the wastewater is 1:1-1:3, preferably 1:1-1:2.
Wherein the ozone oxidation reaction time is 1-3 hours, preferably 1-2 hours.
Wherein after the wastewater is pretreated by ozone oxidation, the COD degradation rate of the wastewater reaches 70-83%.
Wherein the temperature of the preheating zone in the microchannel is 150-200deg.C, preferably 150-180deg.C.
Wherein the temperature of the microchannel reaction zone is 200-250deg.C, preferably 200-230deg.C.
Wherein the flow rate of the wastewater subjected to ozone oxidation entering the micro-channel is 200-300mL/min, preferably 240-260mL/min.
Wherein the residence time of the microchannel reaction is 0.5-3min, preferably 1-2min.
Wherein the wet oxidation process is carried out in a tubular reactor with a specific structure, and the reaction system comprises a wastewater storage tank and a reactor; the reactor channel structure is one or more of the following combinations: round tube type direct current channel structure, round cake type pulse variable diameter type rectangular flat pipeline structure, inclined Fang Bing type pulse variable diameter type rectangular flat pipeline structure, reinforced mixed round cake type rectangular flat pipeline structure and heart type channel structure.
The invention has the following advantages: 1. the invention uses the airlift loop reactor to enable the fluid in the reactor to regularly circulate, strengthens inter-phase mixing, mass transfer and heat transfer, and has the advantages of low energy consumption, regular internal flow field, good mixing performance, high inter-phase mass transfer and heat transfer efficiency, good sealing performance, material saving and the like.
2. The invention is applicable to high COD, high chroma and high concentration waste water, and no catalyst is used in the reaction process and no new impurity ion is introduced.
3. The invention adopts the micro-channel reactor, increases the mass and heat transfer effect in the reaction process, shortens the reaction process, reduces the reaction time and improves the reaction efficiency.
Drawings
FIG. 1 is a process flow diagram of the treatment of polyaromatic wastewater in accordance with the present invention.
FIG. 2 is a schematic diagram of the loop reactor and the microchannel reactor used in the present invention, wherein the 1-ozone generating device, the 2-wastewater storage tank, the 3-gas distributor, the 4-loop reactor, 5 is a metering pump, 6-preheating zone, 7-reaction zone, 8-wastewater collection zone.
FIG. 3 is a schematic diagram of a gas distributor used in the present invention.
FIG. 4 is a schematic illustration of the reaction zone structure of a microchannel reactor wherein 7-1-1 is the reaction zone conduit, 7-1-2 is the water inlet, and 7-1-3 is the water outlet.
FIG. 5 shows one of the internal parts of the microreactor structure described in FIG. 4, wherein a is a DC channel, b is a pancake-type pulse-diameter-variable rectangular flat tube, c is an oblique pancake-type pulse-diameter-variable rectangular flat tube, d is a reinforced hybrid pancake-type rectangular flat tube, and e is a 3g-HEART CELL structure.
Detailed Description
The method is further illustrated in the following examples.
The construction of the loop reactor and the microchannel reactor used in the present invention will be described in detail below in connection with FIGS. 2-5-!
As shown in fig. 2, the pH of the wastewater is regulated to enter a wastewater storage tank (2), a high-pressure metering pump (5) is arranged on a pipeline connecting the outlet of the wastewater storage tank (2) with the liquid inlet of a loop reactor (4), the outlet of an ozone generator (1) is connected with the air inlet of the loop reactor (4), and a pressure reducing valve, an ozone concentration detector and a gas flow controller are arranged on the connected pipeline. A gas distributor (3) is arranged above the gas inlet of the loop reactor (4), the gas holes on the distributor (3) are uniformly arranged, the loop reactor is divided into an upflow zone and a downflow zone, the water outlet of the loop reactor (4) is connected with the inlet of a preheating zone (6) of the microchannel reactor, a pressure sensor and a metering pump are arranged on the connecting pipeline, and a gas-liquid separation tank is arranged at the tail end outlet of the microchannel reactor.
Example 1
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 23476mg/L, BOD:2817mg/L, B/C=0.12 and polycyclic aromatic hydrocarbon substance content=1265mg/L) into a wastewater storage tank, regulating the pH to be 1, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to the COD in the wastewater is 1:1 in the reactor entering from a downflow area of the reactor. The reaction time was 1h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD=6703 mg/L, BOD=1609 mg/L, B/C=0.24 and the content of polycyclic aromatic hydrocarbon substances=690 mg/L of the effluent are carried out.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structural combination is an a-DC channel and a b-discus type pulse variable diameter rectangular flat pipeline) through a metering pump, the flow rate is 200mL/min, the wastewater enters a reaction zone for wet oxidation reaction after being preheated to 150 ℃, the temperature of the reaction zone is 200 ℃, and the reaction time in the reaction zone is 0.5min.
(4) The wastewater after wet oxidation flows out from the water outlet, sampling and detection are carried out, at the moment, the COD of the effluent is=105 mg/L, BOD is=43 mg/L, B/C is=0.41, and the content of polycyclic aromatic hydrocarbon substances is=1.3 mg/L, so that the secondary effluent index is reached.
Example 2
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 22954mg/L, BOD:2525mg/L, B/C=0.11, polycyclic aromatic hydrocarbon content of 1480 mg/L) into a wastewater storage tank, regulating the pH value to 2, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to COD in the wastewater is 1:2 in the reactor entering from a downflow zone of the reactor. The reaction time was 1.5h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD of the effluent is=6003 mg/L, the BOD is=2041 mg/L, the B/C is=0.34, and the content of polycyclic aromatic hydrocarbon substances is=101 mg/L.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structural combination is an a-DC channel and a c-oblique Fang Bing type pulse variable diameter rectangular flat pipeline) through a metering pump, the flow speed is 220mL/min, the wastewater enters a reaction zone for wet oxidation reaction after being preheated to 160 ℃, the temperature of the reaction zone is 210 ℃, and the reaction time of the reaction zone is 1min.
(4) The wastewater after wet oxidation flows out from the water outlet, sampling and detection are carried out, at the moment, the COD=95 mg/L, BOD=42 mg/L, B/C=0.44 and the content of polycyclic aromatic hydrocarbon substances=1.3 mg/L of the wastewater reach the secondary effluent standard.
Example 3
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 30279mg/L, BOD:4239mg/L, B/C=0.14, polycyclic aromatic hydrocarbon content of 1585 mg/L) into a wastewater storage tank, adjusting the pH to 3, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to the COD in the wastewater is 1:3 in the reactor entering from a downflow area of the reactor. The reaction time was 2h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD of the effluent is=6075 mg/L, the BOD is=2005 mg/L, the B/C is=0.33, and the content of polycyclic aromatic hydrocarbon substances is=121 mg/L.
(3) The wastewater after ozone oxidation enters a microchannel reactor (wherein the structural combination is a b-round cake type pulse variable diameter rectangular flat pipeline, a c-inclined Fang Bing type pulse variable diameter rectangular flat pipeline) through a metering pump, the flow speed is 240mL/min, the wastewater enters a reaction zone for photocatalytic reaction after being preheated to 170 ℃, the temperature of the reaction zone is 220 ℃, and the reaction time in the reaction zone is 1.5min.
(4) The wastewater after wet oxidation flows out from the water outlet, sampling and detection are carried out, at the moment, the COD of the effluent is 88mg/L, BOD is 40mg/L, B/C is 0.46, and the content of polycyclic aromatic hydrocarbon substances is 0.7mg/L, thereby meeting the primary effluent standard.
Example 4
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 31784mg/L, BOD:3814mg/L, B/C=0.12 and polycyclic aromatic hydrocarbon content of 1482 mg/L) into a wastewater storage tank, adjusting the pH to 4, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to COD in the wastewater is 1:2 in the reactor entering from a downflow area of the reactor. The reaction time was 2.5h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD=6926mg/L, BOD=2009 mg/L, B/C=0.29 and the content of polycyclic aromatic hydrocarbon substances=134 mg/L are obtained.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structural combination is a b-round cake type pulse variable diameter rectangular flat pipeline and a d-reinforced mixed round cake type rectangular flat pipeline) through a metering pump, the flow rate is 260mL/min, the wastewater enters a reaction zone for photocatalytic reaction after being preheated to 180 ℃, the temperature of the reaction zone is 230 ℃, and the reaction time of the reaction zone is 2min.
(4) The wastewater after photocatalysis flows out from the water outlet, sampling and detection are carried out, at the moment, the COD of the effluent is=75 mg/L, BOD is=35 mg/L, B/C is=0.46, and the content of polycyclic aromatic hydrocarbon substances is=0.7 mg/L, thereby meeting the primary effluent standard.
Example 5
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 27634mg/L, BOD:3592mg/L, B/C=0.13 polycyclic aromatic hydrocarbon content is 1243 mg/L) into a wastewater storage tank, adjusting the pH to 5, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to COD in the wastewater is 1:2 in the reactor entering from a downflow area of the reactor. The reaction time was 3h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD=5392 mg/L, BOD=1564 mg/L, B/C=0.29 and the content of polycyclic aromatic hydrocarbon substances=106 mg/L of the effluent are carried out.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structural combination is a d-reinforced mixed round cake type rectangular flat pipeline, e-3g-HEART CELL structure) through a metering pump, the flow rate is 280mL/min, the wastewater enters a reaction zone for photocatalytic reaction after being preheated to 190 ℃, the temperature of the reaction zone is 240 ℃, and the reaction time in the reaction zone is 2.5min.
(4) The wastewater after photocatalysis flows out from the water outlet, sampling and detection are carried out, at the moment, the COD of the effluent is=87 mg/L, BOD is=41 mg/L, B/C is=0.47, and the content of polycyclic aromatic hydrocarbon substances is=0.6 mg/L, thereby meeting the primary effluent standard.
Example 6
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 27673mg/L, BOD:2767mg/L, B/C=0.1, polycyclic aromatic hydrocarbon content of 1283 mg/L) into a wastewater storage tank, adjusting pH to 2, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to COD in the wastewater is 1:2 in the reactor entering from a downflow area of the reactor. The reaction time was 2h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD of the effluent is=5532 mg/L, the BOD is=1826 mg/L, the B/C is=0.33, and the content of polycyclic aromatic hydrocarbon substances is=103 mg/L.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structural combination is a c-inclined Fang Bing type pulse variable diameter rectangular flat pipeline, an e-3g-HEART CELL structure) through a metering pump, the flow rate is 300mL/min, the wastewater enters a reaction zone for photocatalytic reaction after being preheated to 200 ℃, the temperature of the reaction zone is 250 ℃, and the reaction time of the reaction zone is 3min.
(4) The wastewater after photocatalysis flows out from the water outlet, sampling and detection are carried out, at the moment, the COD=73 mg/L, BOD=34 mg/L, B/C=0.47 and the polycyclic aromatic hydrocarbon substance content=0.5 mg/L of the wastewater meet the primary effluent standard.
Example 7
(1) Adding polycyclic aromatic hydrocarbon wastewater (COD: 24037mg/L, BOD:2404mg/L, B/C=0.1, polycyclic aromatic hydrocarbon content of 1342 mg/L) into a wastewater storage tank, adjusting pH to 2, and feeding the wastewater into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, and the mass ratio of the ozone to COD in the wastewater is 1:2 in the reactor entering from a downflow area of the reactor. The reaction time was 2h.
(2) And the reacted wastewater flows out from a water outlet at the bottom of the tower, sampling and detection are carried out, and at the moment, the COD of the effluent is=4163 mg/L, the BOD is=1374 mg/L, the B/C is=0.33, and the content of polycyclic aromatic hydrocarbon substances is=107 mg/L.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structure combination is a-DC channel and e-3g-HEART CELL structure) through a metering pump, the flow rate is 260mL/min, the wastewater enters a reaction zone for wet oxidation reaction after being preheated to 160 ℃, the temperature of the reaction zone is 220 ℃, and the reaction time in the reaction zone is 2min.
(4) The wastewater after wet oxidation flows out from the water outlet, sampling and detection are carried out, at the moment, the COD of the effluent is=61 mg/L, BOD is=28 mg/L, B/C is=0.46, and the content of polycyclic aromatic hydrocarbon substances is=0.3 mg/L, thereby meeting the primary effluent standard.
Claims (8)
1. A treatment method of polycyclic aromatic hydrocarbon wastewater is characterized by comprising the following steps:
(1) Regulating the pH of the polycyclic aromatic hydrocarbon wastewater, and enabling the wastewater after regulating the pH to enter an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas separator is arranged at the bottom of the tower, the wastewater enters the reactor from a downflow area of the reactor, and the wastewater flows out from a water outlet of the reactor;
Wherein the pH is adjusted to 4;
Wherein the mass ratio of the ozone to COD in the wastewater is 1:1-1:3;
(2) Waste water at the water outlet of the bottom of the tower enters a microchannel reactor through a metering pump to be preheated and then enters a reaction zone to carry out wet oxidation reaction, the flow rate is controlled through adjusting the metering pump, so that the reaction residence time is controlled, and the reaction temperature is controlled by an external circulating heat exchange system; the wastewater is discharged after reaching the standard after detection;
The ozone oxidation reaction time is 1-3h,
Wherein the temperature of the preheating zone in the micro-channel is 150-200 ℃,
Wherein the temperature of the micro-channel reaction zone is 200-250 ℃,
Wherein the reaction residence time of the micro-channel is 1-2min,
Wherein the wet oxidation process is carried out in a tubular reactor with a specific structure, and the reaction system comprises a wastewater storage tank and a reactor; the reactor channel structure is a combination of a round cake type pulse variable diameter rectangular flat pipeline structure and an enhanced mixed round cake type rectangular flat pipeline structure.
2. The method for treating wastewater containing polycyclic aromatic hydrocarbon according to claim 1, wherein the mass ratio of ozone to COD in the wastewater is 1:1 to 1:2.
3. The method for treating wastewater containing polycyclic aromatic hydrocarbon according to claim 1, wherein the ozone oxidation reaction time is 1-2 hours.
4. The method for treating polycyclic aromatic hydrocarbon wastewater according to claim 1, wherein the COD degradation rate of the wastewater after the wastewater is pretreated by ozone oxidation is up to 70-83%.
5. The method for treating wastewater containing polycyclic aromatic hydrocarbon according to claim 1, wherein the preheating zone in the microchannel is at a temperature of 150-180 ℃.
6. The method for treating wastewater containing polycyclic aromatic hydrocarbon according to claim 1, wherein the temperature of the reaction zone of the microchannel is 200-230 ℃.
7. The method for treating wastewater containing polycyclic aromatic hydrocarbon according to claim 1, wherein the flow rate of the wastewater subjected to ozone oxidation entering the microchannel is 240-260mL/min.
8. The method for treating wastewater containing polycyclic aromatic hydrocarbon according to claim 1, wherein the residence time of the microchannel reaction is 1 to 2 minutes.
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| CN202164194U (en) * | 2011-08-16 | 2012-03-14 | 北京市环境保护科学研究院 | Polycyclic aromatic hydrocarbon type polluted soil waste washing liquid treatment system |
| CN113173654A (en) * | 2021-04-01 | 2021-07-27 | 常州大学 | Wet oxidation combined treatment method for aromatic hydrocarbon-containing wastewater |
| CN113582457A (en) * | 2021-08-10 | 2021-11-02 | 山东理工大学 | Treatment method and treatment system for semi-coke wastewater |
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