CN114349246A - Combined treatment method of polycyclic aromatic hydrocarbon wastewater - Google Patents
Combined treatment method of polycyclic aromatic hydrocarbon wastewater Download PDFInfo
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Abstract
The invention discloses a combined treatment method of polycyclic aromatic hydrocarbon wastewater, and relates to a wastewater treatment technology. The method utilizes an ozone and wet oxidation process to treat the polycyclic aromatic hydrocarbon wastewater, thereby realizing standard discharge. The method for treating the polycyclic aromatic hydrocarbon wastewater utilizes the airlift loop reactor to carry out ozone oxidation pretreatment on the polycyclic aromatic hydrocarbon wastewater, thereby improving the biodegradability of the polycyclic aromatic hydrocarbon wastewater. And after pretreatment, wet oxidation is carried out by using a microchannel to degrade the refractory substances. The polycyclic aromatic hydrocarbon wastewater treatment method effectively solves the problems of discharge and treatment of the chemical wastewater, and has the advantages of high wastewater treatment efficiency, stable effect and convenient 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; physical methods, mainly including adsorption, coagulating sedimentation, etc.; the chemical processes are mainly different advanced oxidation processes; the biological method mainly comprises aerobic biological treatment and anaerobic biological treatment.
The advanced oxidation mainly includes an electrochemical oxidation method, a photocatalytic oxidation method, an ozone oxidation method, a fenton oxidation method, and a wet oxidation method. The ozone oxidation method is a wastewater treatment technology for oxidizing organic matters in wastewater by using ozone as an oxidant, and is used for improving B/C and improving biodegradability of wastewater. The preliminary pretreatment of the wastewater with high COD by adopting an ozone oxidation method is a good choice, and the macromolecular organic matters in the wastewater are decomposed into micromolecular organic matters, and the chromaticity of the wastewater is removed.
Chinese patent CN201310047909.8 discloses a method for degrading pentachlorophenol by enhancing ozone oxidation in a microchannel, which utilizes a high-efficiency gas-liquid mass transfer device-microchannel reactor to efficiently remove typical POPs-PCP in water. The treatment process comprises the following steps: (1) the prepared pentachlorophenol dilute solution with a certain concentration enters a microchannel through a high-pressure pump, and ozone is conveyed into the microchannel through another pipeline for reaction; (2) the liquid after the reaction enters a gas-liquid separator for gas-liquid separation. According to the method, the removal rate of pentachlorophenol reaches 100%, but the removal rate of TOC is only about 50%, organic matters in wastewater are not completely degraded, and small molecular organic matters still exist, so that the method is suitable for low-concentration characteristic pollutant wastewater.
Chinese patent CN202011264966.8 discloses an ultrasonic wave H2O2And a microchannel advanced oxidation process and apparatus, which process utilizes H2O2Is an oxidant, and the ultrasonic and the micro-channel cooperate to treat the wastewater. The treatment process comprises the following steps: (1) will be provided withMixing the wastewater to be treated with a hydrogen peroxide solution, and feeding the mixture into a microchannel of a microchannel reactor for reaction; (2) when the intermediate solution is sent into the micro-channel, the oxidation intermediate solution in the micro-channel is subjected to ultrasonic treatment by an ultrasonic generator; (3) and (3) carrying out sewage biochemical treatment on the solution reacted 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 combining electrocatalytic oxidation and multiple catalytic oxidations to treat wastewater with COD of 600 ppm. This patent is only applicable to the treatment of wastewater with low COD content.
In a Master academic paper research on degrading polycyclic aromatic hydrocarbons in printing and dyeing wastewater by ultrasonic-Fenton, 16 polycyclic aromatic hydrocarbon mixed standard solutions are taken as research objects, and the polycyclic aromatic hydrocarbons in the wastewater are degraded by an ultrasonic-Fenton method, wherein the maximum degradation rate can reach 93.2%. 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, wherein the wet oxidation utilizes a microchannel reactor as a reactor. OH generated by ozone follows a hydroxyl radical chain reaction mechanism, macromolecular organic matters in wastewater are decomposed into micromolecular organic matters, and the micromolecular organic matters and organic matters which are difficult to degrade are oxidized into H by wet oxidation in a microchannel2O and CO2. The reaction time is shortened by high mass and heat transfer, and the reaction efficiency is high.
In order to realize the method, the invention adopts the technical scheme that:
a treatment method of polycyclic aromatic hydrocarbon wastewater is carried out according to the following steps:
(1) adjusting the pH value of the polycyclic aromatic hydrocarbon wastewater, and feeding the wastewater after pH adjustment into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the reactor, a gas splitter is arranged at the bottom of the reactor, the wastewater enters the reactor from a downflow zone of the reactor, and the wastewater flows out from a water outlet of the reactor. Sampling and detecting.
(2) Waste water at a water outlet at the bottom of the tower enters the microchannel reactor through the metering pump, is preheated and then enters the reaction zone for 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 the external circulation 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 introduced ozone amount to the COD in the wastewater is 1:1-1:3, preferably 1:1-1: 2.
Wherein the ozone oxidation reaction time is 1-3h, preferably 1-2 h.
Wherein, after the wastewater is pretreated by ozone oxidation, the COD degradation rate of the wastewater reaches 70 to 83 percent.
Wherein the temperature of the preheating zone in the microchannel is 150-200 ℃, preferably 150-180 ℃.
Wherein the temperature of the microchannel reaction zone is 200-250 ℃, preferably 200-230 ℃.
Wherein the flow rate of the wastewater after ozone oxidation entering the micro-channel is 200-300mL/min, preferably 240-260 mL/min.
Wherein the residence time of the microchannel reaction is 0.5-3min, preferably 1-2 min.
Wherein the wet oxidation process is carried out in a tubular reactor with a specific structure, and the reaction system comprises a waste water storage tank and a reactor; the reactor channel structure is one or more of the following combinations: the device comprises a round tube type straight-flow channel structure, a round cake type pulse variable-diameter rectangular flat pipeline structure, an oblique square cake type pulse variable-diameter rectangular flat pipeline structure, a reinforced mixed type round cake type rectangular flat pipeline structure and a heart type channel structure.
The invention has the following advantages: 1. the invention uses the airlift loop reactor to ensure that the fluid in the airlift loop reactor can regularly and circularly flow, strengthens interphase mixing, mass transfer and heat transfer, and has the advantages of low energy consumption, regular internal flow field, good mixing performance, high interphase mass and heat transfer efficiency, good sealing performance, material saving and the like.
2. The method is suitable for high-COD, high-chroma and high-concentration wastewater, does not use a catalyst in the reaction process, and does not introduce new impurity ions.
3. The invention adopts the microchannel 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 for treating polycyclic aromatic hydrocarbon wastewater according to the present invention.
FIG. 2 is a schematic view showing the structure of a loop reactor and a microchannel reactor used in the present invention, wherein 1-an ozone generating device, 2-a waste water storage tank, 3-a gas distributor, 4-a loop reactor, 5 is a metering pump, 6-a preheating zone, 7-a reaction zone, and 8-a waste water collecting zone.
FIG. 3 is a schematic view of a gas distributor used in the present invention.
FIG. 4 is a schematic diagram of the reaction zone structure of the microchannel reactor, wherein 7-1-1 is a reaction zone pipeline, 7-1-2 is a water inlet, and 7-1-3 is a water outlet.
Fig. 5 is one of the internal parts of the microreactor structure shown in fig. 4, wherein a is a direct-current channel, b is a pancake pulse diameter-changing rectangular flat pipeline, c is an oblique-pancake pulse diameter-changing rectangular flat pipeline, d is an enhanced mixed pancake rectangular flat pipeline, and e is a 3g-Heart Cell structure.
Detailed Description
The process is further illustrated below with reference to examples.
The structure of the loop reactor and the microchannel reactor used in the present invention will be described in detail below with reference to FIGS. 2-5!
As shown in figure 2, the wastewater is adjusted to pH and enters a wastewater storage tank (2), a high-pressure metering pump (5) is arranged on a pipeline connecting an outlet of the wastewater storage tank (2) and a liquid inlet of a loop reactor (4), an outlet of an ozone generator (1) is connected with a gas inlet of the loop reactor (4), and a pressure reducing valve, an ozone concentration detector and a gas flow controller are arranged on a connecting pipeline. A gas distributor (3) is arranged above the gas inlet of the loop reactor (4), gas holes on the distributor (3) are uniformly arranged, the loop reactor is divided into an ascending area and a descending area, the water outlet of the loop reactor (4) is connected with the inlet of a micro-channel reactor preheating area (6), a pressure sensor and a metering pump are arranged on a connecting pipeline, and a gas-liquid separation tank is arranged at the tail end outlet of the micro-channel reactor.
Example 1
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 23476mg/L, BOD: 2817mg/L, B/C being 0.12, polycyclic aromatic hydrocarbon content being 1265mg/L) is taken and added into a wastewater storage tank, the pH value is adjusted to 1, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from a gas inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater is 1:1 in the reactor into which the wastewater enters from a downflow zone of the reactor. The reaction time was 1 h.
(2) And (3) the wastewater after reaction flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD of the effluent is 6703mg/L, BOD is 1609mg/L, B/C is 0.24, and the content of polycyclic aromatic hydrocarbon substances is 690 mg/L.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structure combination is an a-direct-current channel and a b-round-cake type pulse variable-diameter rectangular flat pipeline) through a metering pump, the flow rate is 200mL/min, the wastewater enters a reaction zone after being preheated to 150 ℃ for wet oxidation reaction, the temperature of the reaction zone is 200 ℃, and the reaction time in the reaction zone is 0.5 min.
(4) And (3) the waste water after wet oxidation flows out from a water outlet, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 105mg/L, the BOD (biochemical oxygen demand) is 43mg/L, the B/C (carbon/carbon) is 0.41, and the content of polycyclic aromatic hydrocarbon substances is 1.3mg/L, so that the secondary effluent index is reached.
Example 2
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 22954mg/L, BOD: 2525mg/L, B/C: 0.11, polycyclic aromatic hydrocarbon content 1480mg/L) is taken and added into a wastewater storage tank, the pH value is adjusted to 2, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from a gas inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater enters into the reactor from a downflow zone of the reactor is 1: 2. The reaction time was 1.5 h.
(2) And (3) the wastewater after reaction flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 6003mg/L, the BOD (biochemical oxygen demand) is 2041mg/L, the B/C (total carbon) 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 structure combination is an a-direct-current channel and a c-oblique square-cake type pulse variable-diameter rectangular flat pipeline) through a metering pump, the flow rate is 220mL/min, the wastewater enters a reaction zone after being preheated to 160 ℃ for wet oxidation reaction, the temperature of the reaction zone is 210 ℃, and the reaction time in the reaction zone is 1 min.
(4) And (3) the waste water after wet oxidation flows out from a water outlet, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 95mg/L, the BOD (BOD) is 42mg/L, the B/C (B/C) is 0.44, and the content of polycyclic aromatic hydrocarbon substances is 1.3mg/L, so that the secondary effluent standard is achieved.
Example 3
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 30279mg/L, BOD: 4239mg/L, B/C: 0.14, and polycyclic aromatic hydrocarbon content of 1585mg/L) is taken and added into a wastewater storage tank, the pH value is adjusted to 3, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater enters into the reactor from a downflow zone of the reactor is 1: 3. The reaction time was 2 h.
(2) And (3) the wastewater after reaction flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD of the effluent is 6075mg/L, the BOD is 2005mg/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 micro-channel reactor (wherein the structural combination is a b-round cake type pulse diameter-changing rectangular flat pipeline and a c-oblique square cake type pulse diameter-changing rectangular flat pipeline) through a metering pump, the flow rate is 240mL/min, the wastewater enters a reaction zone after being preheated to 170 ℃ for photocatalytic reaction, the temperature of the reaction zone is 220 ℃, and the reaction time in the reaction zone is 1.5 min.
(4) And (3) the waste water after wet oxidation flows out from a water outlet, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 88mg/L, the BOD (BOD) is 40mg/L, the B/C (B/C) is 0.46, and the content of polycyclic aromatic hydrocarbon substances is 0.7mg/L, so that the effluent meets the primary effluent standard.
Example 4
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 31784mg/L, BOD: 3814mg/L, B/C of 0.12 and polycyclic aromatic hydrocarbon content of 1482mg/L) is taken and added into a wastewater storage tank, the pH value is adjusted to 4, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater enters into the reactor from a downflow zone of the reactor is 1: 2. The reaction time was 2.5 h.
(2) And (3) the wastewater after the reaction flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD of the effluent is 6926mg/L, the BOD is 2009mg/L, the B/C is 0.29, and the content of polycyclic aromatic hydrocarbon substances is 134 mg/L.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structure combination is a b-cake type pulse diameter-changing rectangular flat pipeline and a d-enhanced mixed type cake type rectangular flat pipeline) through a metering pump, the flow rate is 260mL/min, the wastewater enters a reaction zone after being preheated to 180 ℃ for photocatalytic reaction, the temperature of the reaction zone is 230 ℃, and the reaction time in the reaction zone is 2 min.
(4) The waste water after photocatalysis flows out through a water outlet, and sampling detection is carried out, wherein the COD (chemical oxygen demand) of the discharged water is 75mg/L, the BOD (biochemical oxygen demand) is 35mg/L, the B/C (chemical oxygen demand) is 0.46, and the content of polycyclic aromatic hydrocarbon substances is 0.7mg/L, so that the first-level water discharge standard is met.
Example 5
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 27634mg/L, BOD: 3592mg/L, and B/C ═ 0.13 polycyclic aromatic hydrocarbon substance content of 1243mg/L) is taken and added into a wastewater storage tank, the pH value is adjusted to 5, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater enters into the reactor from a down-flow area of the reactor is 1: 2. The reaction time was 3 h.
(2) And (3) the reacted wastewater flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 5392mg/L, the BOD (biochemical oxygen demand) is 1564mg/L, the B/C (chemical oxygen demand) is 0.29, and the content of polycyclic aromatic hydrocarbon substances is 106 mg/L.
(3) The wastewater after ozone oxidation enters a micro-channel reactor (wherein the structural combination is a d-enhanced mixed type round cake type rectangular flat pipeline, an e-3g-Heart Cell structure) through a metering pump, the flow rate is 280mL/min, the wastewater enters a reaction zone after being preheated to 190 ℃ for photocatalytic reaction, the temperature of the reaction zone is 240 ℃, and the reaction time in the reaction zone is 2.5 min.
(4) The waste water after photocatalysis flows out through a water outlet, sampling and detecting are carried out, the COD of the effluent is 87mg/L, the BOD is 41mg/L, the B/C is 0.47, and the content of polycyclic aromatic hydrocarbon substances is 0.6mg/L, thereby meeting the first-level effluent standard.
Example 6
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 27673mg/L, BOD: 2767mg/L, B/C is 0.1, the content of polycyclic aromatic hydrocarbon substances is 1283mg/L) is added into a wastewater storage tank, the pH value is adjusted to 2, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater enters into the reactor from a down-flow area of the reactor is 1: 2. The reaction time was 2 h.
(2) And (3) the wastewater after reaction flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 5532mg/L, the BOD (biochemical oxygen demand) is 1826mg/L, the B/C (chemical oxygen demand/carbon) 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 structure combination is a c-oblique square cake type pulse reducing 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 after being preheated to 200 ℃ for photocatalytic reaction, the temperature of the reaction zone is 250 ℃, and the reaction time in the reaction zone is 3 min.
(4) The waste water after photocatalysis flows out through a water outlet, sampling and detecting are carried out, the COD of the effluent is 73mg/L, the BOD is 34mg/L, the B/C is 0.47, and the content of polycyclic aromatic hydrocarbon substances is 0.5mg/L, thereby meeting the first-level effluent standard.
Example 7
(1) Polycyclic aromatic hydrocarbon wastewater (COD: 24037mg/L, BOD: 2404mg/L, B/C of 0.1, polycyclic aromatic hydrocarbon substance content of 1342mg/L) is taken and added into a wastewater storage tank, the pH value is adjusted to 2, the wastewater enters into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the tower, a gas splitter is arranged at the bottom of the tower, and the mass ratio of the introduced ozone to the COD in the wastewater enters into the reactor from a down-flow area of the reactor is 1: 2. The reaction time was 2 h.
(2) And (3) the reacted wastewater flows out from a water outlet at the bottom of the tower, and sampling and detecting are carried out, wherein the COD of the effluent is 4163mg/L, the BOD is 1374mg/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 microchannel reactor (wherein the structure combination is an a-direct-current channel, and the structure of an e-3g-Heart Cell) through a metering pump, the flow rate is 260mL/min, the wastewater enters a reaction zone after being preheated to 160 ℃ for wet oxidation reaction, the temperature of the reaction zone is 220 ℃, and the reaction time in the reaction zone is 2 min.
(4) And (3) the waste water after wet oxidation flows out from a water outlet, and sampling and detecting are carried out, wherein the COD (chemical oxygen demand) of the effluent is 61mg/L, the BOD (biochemical oxygen demand) is 28mg/L, the B/C (carbon dioxide/carbon) is 0.46, and the content of polycyclic aromatic hydrocarbon substances is 0.3mg/L, so that the effluent meets the primary effluent standard.
Claims (10)
1. A treatment method of polycyclic aromatic hydrocarbon wastewater is characterized by comprising the following steps:
(1) adjusting the pH value of the polycyclic aromatic hydrocarbon wastewater, and feeding the wastewater after pH adjustment into an airlift loop reactor through a metering pump, wherein ozone enters from an air inlet at the bottom of the reactor, a gas splitter is arranged at the bottom of the reactor, the wastewater enters the reactor from a downflow zone of the reactor, and the wastewater flows out from a water outlet of the reactor;
(2) waste water at a water outlet at the bottom of the tower enters a microchannel reactor through a metering pump, is preheated and then enters a reaction zone for 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 circulation heat exchange system; and the wastewater is discharged after reaching the standard after detection.
2. The method according to claim 1, wherein the pH is adjusted to 9 to 11, preferably 9 to 10.
3. The method for treating polycyclic aromatic hydrocarbon wastewater according to claim 1, wherein the mass ratio of the ozone amount introduced to the COD in the wastewater is 1:1-1:3, preferably 1:1-1: 2.
4. The method for treating polycyclic aromatic hydrocarbon wastewater according to claim 1, wherein the ozone oxidation reaction time is 1-3h, preferably 1-2 h.
5. The method according to claim 1, wherein the COD degradation rate of the wastewater is 70-83% after the wastewater is pretreated by ozone oxidation.
6. The method as claimed in claim 1, wherein the temperature of the preheating zone in the microchannel is 150-.
7. The method as claimed in claim 1, wherein the temperature of the microchannel reaction zone is 200-250 ℃, preferably 200-230 ℃.
8. The method as claimed in claim 1, wherein the flow rate of the wastewater after ozone oxidation to the micro-channel is 200-300mL/min, preferably 240-260 mL/min.
9. The method for treating polycyclic aromatic hydrocarbon wastewater according to claim 1, wherein the residence time of the microchannel reaction is 0.5-3min, preferably 1-2 min.
10. The method for treating polycyclic aromatic hydrocarbon wastewater as claimed in claim 1, wherein the wet oxidation process is carried out in a tubular reactor with a specific structure, the reaction system comprises a wastewater storage tank, a reactor; the reactor channel structure is one or more of the following combinations: the device comprises a round tube type straight-flow channel structure, a round cake type pulse variable-diameter rectangular flat pipeline structure, an oblique square cake type pulse variable-diameter rectangular flat pipeline structure, a reinforced mixed type round cake type rectangular flat pipeline structure and a heart type channel structure.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114890532A (en) * | 2022-07-12 | 2022-08-12 | 杭州沈氏节能科技股份有限公司 | Spiral casing pipe reactor and micro-channel wet oxidation system |
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| AU1471401A (en) * | 1999-11-05 | 2001-05-14 | University Of Utah Research Foundation | Degradation of polycyclic aromatic hydrocarbons |
| CN200974781Y (en) * | 2006-11-17 | 2007-11-14 | 武汉大学 | Ultrasonic-ozone synergic waste-water treatment device |
| 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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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU1471401A (en) * | 1999-11-05 | 2001-05-14 | University Of Utah Research Foundation | Degradation of polycyclic aromatic hydrocarbons |
| CN200974781Y (en) * | 2006-11-17 | 2007-11-14 | 武汉大学 | Ultrasonic-ozone synergic waste-water treatment device |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114890532A (en) * | 2022-07-12 | 2022-08-12 | 杭州沈氏节能科技股份有限公司 | Spiral casing pipe reactor and micro-channel wet oxidation system |
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