CN108059232B - Method for purifying waste water - Google Patents
Method for purifying waste water Download PDFInfo
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- CN108059232B CN108059232B CN201711358019.3A CN201711358019A CN108059232B CN 108059232 B CN108059232 B CN 108059232B CN 201711358019 A CN201711358019 A CN 201711358019A CN 108059232 B CN108059232 B CN 108059232B
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- 239000002351 wastewater Substances 0.000 title claims abstract description 113
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 119
- 230000003197 catalytic effect Effects 0.000 claims abstract description 116
- 230000003647 oxidation Effects 0.000 claims abstract description 65
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 48
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- 239000002994 raw material Substances 0.000 claims abstract description 36
- 239000008213 purified water Substances 0.000 claims abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 50
- 238000000926 separation method Methods 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 13
- 238000005273 aeration Methods 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 10
- 230000000903 blocking effect Effects 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 27
- 238000003795 desorption Methods 0.000 abstract 1
- 239000012530 fluid Substances 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 4
- 239000006260 foam Substances 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical group O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- -1 pharmacy Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The application of this division provides a method for purifying waste water, raw materials waste water gets into catalytic oxidation reactor from catalytic oxidation reactor's bottom entry, ozone gets into catalytic oxidation reactor from catalytic oxidation reactor's top ozone entry, raw materials waste water and ozone through mixing many times, after the reaction in catalytic oxidation reactor, the qualified purified water of processing flows out catalytic oxidation reactor by the purified water export, the gas after the reaction is accomplished flows out catalytic oxidation reactor by the exhaust vent, COD's desorption efficiency can reach more than 80%. The catalytic oxidation reactor of the invention is particularly suitable for purifying methanol-containing wastewater.
Description
The application is divisional application with the application number of 201711096677X, the application date of 2017, 11 and 9, and the name of the invention, namely a catalytic oxidation reactor for purifying wastewater and a purification method thereof.
Technical Field
The invention relates to a method for purifying waste water, which is particularly suitable for purifying waste water containing methanol.
Background
Methanol is an important chemical product and raw material, has rich resources, and is one of the important energy sources in the future. However, methanol is toxic to microorganisms, aquatic organisms and human bodies, and is widely used as an organic pollutant in production wastewater of basic organic synthesis, plastics, artificial fibers, pharmacy, ion exchange resin, petrochemical industry, forestry chemical industry, sulfate pulp and the like.
At present, the treatment of the methanol wastewater mainly comprises a physical treatment method, a chemical treatment method and a biological treatment method. The chemical treatment method has the characteristics of simple flow, wide concentration range of the treated wastewater, large treatment capacity, short treatment time and the like, and is widely applied to practical industrial application. The chemical oxidant for treating the methanol wastewater by adopting a chemical method comprises ozone, chlorine oxidant and the like. When the methanol wastewater is treated by ozone, the intermediate product is formaldehyde, and the final product is CO2. After the methanol wastewater with the mass concentration of 5000mg/L is subjected to a one-step catalytic oxidation process, the removal rate can reach more than 80%.
However, how to further improve the efficiency of the catalytic oxidation wastewater treatment technology becomes one of the bottlenecks in the fields of wide application of the catalytic oxidation technology and wastewater treatment. In order to meet the increasing demand of wastewater treatment and treat high-concentration wastewater by a chemical method, the performance of a catalytic oxidation catalyst is generally continuously improved by technical personnel in the field, meanwhile, the design of a catalytic oxidation reactor is more inclined to an integrated design, how to achieve the optimal energy utilization efficiency of different heat absorption and release processes in the reactor by optimizing the logistics and energy flow distribution of a system, and meanwhile, a reaction system is more miniaturized and integrated, so that the energy efficiency of the whole system is improved, and the method is the fundamental premise of the practicability of the catalytic oxidation wastewater treatment technology.
Disclosure of Invention
The invention aims to provide a catalytic oxidation reactor for purifying wastewater, which can solve the following problems: firstly, the reactor can be started and the normal operation of the reactor can be automatically maintained under the conditions of normal temperature and no external heat supply; secondly, the method is suitable for treating wastewater with different concentrations according to the use requirements; and thirdly, multiple functions of heat exchange, reaction, mixing, separation and the like are integrated, the compactness of the whole catalytic oxidation reactor is improved, and the miniaturization of the reactor is realized.
In order to achieve the purpose, the invention adopts the technical scheme that: a catalytic oxidation reactor for purifying waste water is a three-layer sleeve type tower structure; the catalytic oxidation reactor is sequentially provided with a tail gas emission control area, a waste water preheating area and a catalytic oxidation reaction area from outside to inside; a catalytic oxidation catalyst is filled in the catalytic oxidation reaction zone; the catalytic oxidation reaction zone comprises a pre-reaction zone, a gas-liquid buffer zone, a main reaction zone and a post-reaction zone from top to bottom in sequence, a liquid distributor is arranged above the pre-reaction zone, the gas-liquid buffer zone is arranged above the main reaction zone, a gas-liquid redistributor is arranged above the gas-liquid buffer zone, a gas-liquid separation zone is arranged below the bottom of the catalytic oxidation reactor, a purified water outlet is arranged below the gas-liquid separation zone, an ozone inlet is arranged at the top of the catalytic oxidation reactor, a wastewater inlet is arranged below one side of the catalytic oxidation reactor, and a tail gas discharge port is arranged above one side of the catalytic oxidation reactor.
The invention also aims to protect the method for purifying the wastewater, which comprises the following specific steps: raw material wastewater enters a wastewater preheating zone from a wastewater inlet at the bottom of the catalytic oxidation reactor, is preheated to 60-90 ℃ by the wastewater preheating zone, and enters a catalytic oxidation reaction zone through a liquid distributor after being preheated; ozone with a corresponding proportion is introduced into the catalytic oxidation reactor from the ozone inlet, the ozone enters the catalytic oxidation reaction zone through the ozone distributor, the ozone and the raw material wastewater are subjected to three times of mixing and catalytic reaction to enable the raw material wastewater to reach the purified water standard and are discharged through the purified water outlet, reaction tail gas enters the tail gas discharge control zone through the gas-liquid separation zone to continue the catalytic oxidation reaction, and the tail gas reaching the standard is discharged out of the catalytic oxidation reactor through the tail gas discharge port after passing through the foam barrier net.
The catalytic oxidation reactor integrates gas distribution, gas-liquid mixing, gas-liquid back mixing, preheating and catalytic oxidation reaction, and has high energy efficiency. The catalytic oxidation reactor is divided into a tail gas emission control area, a waste water preheating area, a catalytic oxidation reaction area and other different functional areas. The tail gas emission control area ensures that the ozone content in the emitted tail gas reaches the standard; the waste water preheating zone can absorb the reaction heat generated in the catalytic oxidation reaction zone, and the raw material waste water in the waste water preheating zone is preheated to 60-90 ℃ while the temperature of the catalytic oxidation reaction zone is effectively controlled; the raw material wastewater in the wastewater preheating zone and the fluid in the catalytic oxidation reaction zone adopt a convection flow mode, so that the heat exchange efficiency between the raw material wastewater and the fluid in the catalytic oxidation reaction zone can be greatly improved. The whole catalytic oxidation reaction zone can be divided into a pre-reaction zone, a main reaction zone and a reaction zone, three-section catalytic oxidation reaction is adopted, and each section of reaction zone is filled with a catalytic oxidation catalyst. When the catalytic oxidation reactor is started, a small amount of raw materials and ozone are mixed for many times and enter different reaction areas, so that the whole reactor is started at normal temperature without any external heat supply.
The air inlet mode of the ozone adopts multi-section feeding, so that the concentration distribution of the ozone in the axial direction of the catalytic oxidation reaction zone is ensured; meanwhile, a unidirectional aeration device is adopted at the inlet part of each section of ozone, so that the concentration distribution of the ozone in the radial direction of the catalytic oxidation reaction zone is ensured. Through the adjustment of the ozone distributor and the total amount of the inlet, the wastewater with different concentrations can be treated.
The invention adopts the countercurrent flow among the material flows in the catalytic oxidation reactor, the heat exchange integration between the wastewater preheating zone and the catalytic oxidation reaction zone, and the design of the internal gas-liquid separation zone and the gas-liquid distributor to reasonably control and manage the supply and exchange of the energy between the fluid heat exchange and the reaction, thereby improving the compactness of the whole catalytic oxidation reactor, realizing the miniaturization of the reactor and greatly improving the energy efficiency of the whole system.
Drawings
FIG. 1 is a schematic view of a catalytic oxidation reactor for purifying wastewater;
FIG. 2 is an enlarged view of a portion of FIG. 1B;
FIG. 3 is a schematic view of the internal flow of a catalytic oxidation reactor for purifying wastewater;
FIG. 4 is an experimental result of a catalytic oxidation reactor for purifying wastewater according to the present invention.
The device comprises an ozone inlet 1, an ozone inlet 2, a wastewater inlet 3, a tail gas discharge port 4, a purified water outlet 5, a catalyst observation port 6, a gas-liquid disturbance device 7, raw material wastewater distribution ports A and 8, raw material wastewater distribution ports B and 9, a one-way aeration valve 10, a liquid blocking screen 11, a reactor fixing frame 12, a foam blocking net 13, an ozone distributor 14, a liquid distributor 15, a one-way aeration device 16, a gas-liquid redistributor 17, the bottom of a catalytic oxidation reactor, a catalytic oxidation reaction zone, B, a wastewater preheating zone, c, a tail gas discharge control zone, d, a pre-reaction zone, e, a main reaction zone, f, a post-reaction zone, g, a gas-liquid separation zone, h and a gas-liquid buffer zone.
Detailed Description
The invention will be described in more detail below with reference to the accompanying figures 1 to 4 and the specific examples, without limiting the scope of the invention.
As shown in figure 1, a catalytic oxidation reactor for purifying waste water, which is a three-layer sleeve type tower structure; the catalytic oxidation reactor is sequentially provided with a tail gas emission control area c, a waste water preheating area b and a catalytic oxidation reaction area a from outside to inside;
the catalytic oxidation reaction zone a sequentially comprises a pre-reaction zone d, a main reaction zone e and a post-reaction zone f from top to bottom, a liquid distributor 14 is arranged above the pre-reaction zone d, a gas-liquid buffer zone h is arranged above the main reaction zone e, and a gas-liquid redistributor 16 is arranged above the gas-liquid buffer zone h; the top of the catalytic oxidation reactor is provided with an ozone inlet 1, and an ozone distributor 13 is vertically arranged inside the catalytic oxidation reaction zone a and below the ozone inlet 1; the ozone distributor 13 is also provided with a one-way aeration device 15. The gas outlet direction of the one-way aeration device 15 is in opposite contact with the raw material wastewater, so that the gas and the liquid are fully mixed.
A gas-liquid separation zone g is arranged below the bottom 17 of the catalytic oxidation reactor, and a purified water outlet 4 is arranged below the gas-liquid separation zone g; a liquid blocking screen 10 is arranged above the gas-liquid separation area g, and a one-way aeration valve 9 is arranged below the tail gas emission control area c. A raw material wastewater distribution port A7 and a raw material wastewater distribution port B8 are arranged in the wastewater inlet 2, the raw material wastewater distribution port A7 is connected with the tail gas emission control area c, and the raw material wastewater distribution port B8 is connected with the wastewater preheating area B. The two raw material waste waters will also be mixed in the off-gas emission control zone c and will be uniformly fed into the catalytic oxidation reaction zone a by the liquid distributor 14. A catalytic oxidation catalyst is arranged in the tail gas emission control area c, and a gas-liquid disturbance device 6 is arranged to ensure that gas and liquid are fully mixed; and a catalyst observation port 5 is also arranged in the tail gas emission control area c, so that the catalyst can be periodically sampled and analyzed. A bottom waste water inlet 2 is arranged below one side of the catalytic oxidation reactor, and a tail gas discharge port 3 is arranged above one side of the catalytic oxidation reactor. According to the different requirements of users on COD discharge concentration in the wastewater, the method can be realized by adjusting the flow of ozone at the ozone inlet 1.
The specific method for purifying the wastewater by using the catalytic oxidation reactor comprises the following steps:
(1) the raw material wastewater enters a wastewater preheating zone b from a bottom wastewater inlet 2 of the catalytic oxidation reactor. When the wastewater purification process is stable, in the wastewater preheating zone b, the raw wastewater can absorb the reaction heat generated by the oxidation of the wastewater and ozone in the catalytic oxidation reaction zone a, and the raw wastewater in the wastewater preheating zone b is preheated to 60-90 ℃ while the temperature of the catalytic oxidation reaction zone a is effectively controlled. The raw material wastewater in the wastewater preheating zone b and the fluid in the catalytic oxidation reaction zone a adopt a convection flow mode, so that the heat exchange efficiency between the raw material wastewater and the fluid can be greatly improved.
(2) The wastewater preheated by the wastewater preheating zone b enters the catalytic oxidation reaction zone a through the liquid distributor 14.
(3) After raw material wastewater enters the catalytic oxidation reaction zone a, the raw material wastewater firstly infiltrates the pre-reaction zone d, the main reaction zone e and the post-reaction zone f layer by layer, then enters the gas-liquid separation zone g through the bottom 17 of the catalytic oxidation reactor, and liquid flows out of the catalytic oxidation reactor through the purified water outlet 4.
(4) After the catalytic oxidation reaction zone a is soaked in the raw material wastewater, ozone with a corresponding proportion is introduced from an ozone inlet 1 of the catalytic oxidation reactor, and the ozone passes through an ozone distributor 13 and enters each designated area of the corresponding catalytic oxidation reaction zone a in different areas.
(5) Ozone uniformly enters a catalytic oxidation reaction zone a through a one-way aeration device 15, and is in countercurrent contact with raw material wastewater at the upper part of a pre-reaction zone d, and enters the pre-reaction zone d after being fully mixed, so that the first catalytic oxidation reaction is carried out on the surface of a catalyst.
(6) The wastewater after the first catalytic oxidation reaction is in countercurrent contact with the second section of ozone, and after the wastewater is fully mixed, the mixing of the ozone and the wastewater is enhanced by a gas-liquid redistributor 16, and then the wastewater enters a gas-liquid buffer zone h.
(7) And (4) passing through the gas-liquid buffer zone h, uniformly feeding the fully mixed wastewater and ozone into the main reaction zone e, and carrying out a secondary catalytic oxidation reaction on the surface of the catalyst.
(8) And the wastewater after the second catalytic oxidation reaction is in countercurrent contact with the third section of ozone, the wastewater is fully mixed and then enters a post-catalytic oxidation reaction zone f, the unreacted substances in the wastewater part complete the third catalytic oxidation reaction in the post-catalytic oxidation reaction zone f, and the unreacted substances pass through a gas-liquid separation zone g and then flow out of the catalytic oxidation reactor through a purified water outlet 4 after reaching the purified water standard.
(9) The reaction tail gas after the three catalytic oxidation reactions is subjected to gas-liquid separation in a gas-liquid separation zone g, passes through a liquid blocking screen 10 designed on the upper layer, and enters a tail gas emission control zone c through a one-way aeration valve 9. In the tail gas emission control area c, the reaction tail gas continuously carries out catalytic oxidation reaction with partial waste water entering from the raw material waste water distribution port A7, and the tail gas passes through the foam blocking net 12 and flows out of the catalytic oxidation reactor from the tail gas emission port 3 after reaching the emission standard.
The experimental result of the catalytic oxidation reactor for purifying wastewater of the present invention is shown in fig. 3, and a catalytic oxidation reactor filled with 1 cubic meter of catalyst is installed according to the structural design of fig. 1, when the hydraulic load is 2-3m3/m2H, the COD removal rate and the time curve show that the catalytic oxidation reactor has obvious COD removal effect, can achieve stable operation within 20 hours from starting operation, and has the catalytic removal efficiency of more than 80 percent. The catalytic oxidation reactor of the invention is particularly suitable for purifying methanol-containing wastewater.
The above description is only for the purpose of creating a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution and the inventive concept of the present invention within the technical scope of the present invention.
Claims (1)
1. A method for purifying waste water, characterized in that,
(1) raw material wastewater enters a wastewater preheating zone (b) from a wastewater inlet (2) at the bottom of the catalytic oxidation reactor to be preheated, after the wastewater purification process is stable, the raw material wastewater absorbs the reaction heat generated by the oxidation of the wastewater and ozone in a catalytic oxidation reaction zone (a) in the wastewater preheating zone (b), and the raw material wastewater in the wastewater preheating zone (b) is preheated to 60-90 ℃ while the temperature of the catalytic oxidation reaction zone (a) is controlled;
(2) the raw material wastewater preheated by the wastewater preheating zone (b) enters the catalytic oxidation reaction zone (a) through a liquid distributor (14);
(3) after raw material wastewater enters a catalytic oxidation reaction zone (a), infiltrating a pre-reaction zone (d), a main reaction zone (e) and a post-reaction zone (f) layer by layer, then entering a gas-liquid separation zone (g) through the bottom (17) of a catalytic oxidation reactor, and enabling liquid to flow out of the catalytic oxidation reactor through a purified water outlet (4);
(4) after the raw material wastewater is soaked in the catalytic oxidation reaction zone (a), ozone with a corresponding proportion is introduced from an ozone inlet (1) of the catalytic oxidation reactor, the ozone passes through an ozone distributor (13), enters the catalytic oxidation reaction zone (a), and enters each designated zone of the corresponding catalytic oxidation reaction zone (a) in a subarea manner;
(5) ozone uniformly enters a catalytic oxidation reaction zone (a) through a one-way aeration device (15), is in countercurrent contact with raw material wastewater at the upper part of a pre-reaction zone (d), is fully mixed and then enters the pre-reaction zone (d), and is subjected to a first catalytic oxidation reaction on the surface of a catalyst; the volume ratio of the catalytic oxidation catalyst to the reactor is (1:3) - (1: 5);
(6) the wastewater after the first catalytic oxidation reaction is in countercurrent contact with the second section of ozone, and after the wastewater is fully mixed, the mixing of the ozone and the wastewater is enhanced by a gas-liquid redistributor (16), and then the wastewater enters a gas-liquid buffer area (h);
(7) after passing through the gas-liquid buffer zone (h), the fully mixed wastewater and ozone uniformly enter the main reaction zone (e) to perform a second catalytic oxidation reaction on the surface of the catalyst;
(8) the wastewater after the second catalytic oxidation reaction is in countercurrent contact with a third section of ozone, the wastewater and the third section of ozone are fully mixed and then enter a reaction zone (f) after catalytic oxidation, and the unreacted substances in the wastewater part complete the third catalytic oxidation reaction in the post-reaction zone (f) to reach the purified water standard and are discharged through a purified water outlet (4);
(9) after gas-liquid separation of reaction tail gas in a gas-liquid separation zone (g), the reaction tail gas enters a tail gas emission control zone (c) through a one-way aeration valve (9) through a liquid blocking screen (10) to continue catalytic oxidation reaction, and is discharged out of the catalytic oxidation reactor after reaching the standard; part of the raw material wastewater entering from the raw material wastewater distribution port A (7) and reaction tail gas continue to perform catalytic oxidation reaction, and the raw material wastewater is discharged from the catalytic oxidation reactor through the tail gas discharge port (3) after reaching the standard.
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| CN201711358019.3A CN108059232B (en) | 2017-11-09 | 2017-11-09 | Method for purifying waste water |
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| CN201711096677.XA CN107601645B (en) | 2017-11-09 | 2017-11-09 | A kind of catalyst oxidation reactor and its purification method purifying waste water |
| CN201711358019.3A CN108059232B (en) | 2017-11-09 | 2017-11-09 | Method for purifying waste water |
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| CN108751380A (en) * | 2018-06-19 | 2018-11-06 | 怀化学院 | A kind of processing method of phase chromatography-use methanol waste water |
| CN111362336B (en) * | 2020-03-31 | 2021-02-26 | 南京大学 | Device for treating high-concentration organic wastewater by catalytic hydrothermal gasification |
| CN114229988B (en) * | 2021-12-28 | 2023-07-25 | 大连大学 | Catalytic oxidation reactor suitable for purifying printing and dyeing wastewater |
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| DE3363127D1 (en) * | 1982-02-09 | 1986-05-28 | Bbc Brown Boveri & Cie | Method and apparatus for treating a liquid with a gas |
| CA1220320A (en) * | 1984-02-10 | 1987-04-14 | Majesty (Her) In Right Of Canada As Represented By Atomic Energy Of Canada Limited/L'energie Atomique Du Canada Limitee | Method of producing sulphuric acid from sulphur dioxide and apparatus therefor |
| KR100615434B1 (en) * | 2004-09-14 | 2006-08-28 | 안미옥 | The cylindrical reactor in a body for dissolving ozone in water and separating sludge by floatation |
| US7504030B2 (en) * | 2007-03-30 | 2009-03-17 | Richard Melvin Hall | Acid mine water demineralizer |
| CN202007178U (en) * | 2011-03-08 | 2011-10-12 | 北京市环境保护科学研究院 | CH-B (chemical-biological) water treatment technique integrated device |
| JP2013136045A (en) * | 2011-11-28 | 2013-07-11 | Ricoh Co Ltd | Apparatus and method for treatment of waste liquid |
| CN204097234U (en) * | 2014-08-26 | 2015-01-14 | 北京国中科创环境科技有限责任公司 | A kind of organic wastewater with difficult degradation thereby treatment system |
| CN204454717U (en) * | 2014-12-22 | 2015-07-08 | 安徽工程大学 | Effluent treatment plant |
| CN205527942U (en) * | 2016-01-25 | 2016-08-31 | 英诺伟霆（北京）环保技术有限公司 | Inner loop ozone catalytic unit |
| CN206109022U (en) * | 2016-09-12 | 2017-04-19 | 河北莫兰斯环境科技股份有限公司 | Cephalo pharmacy wastewater systems is handled in catalysis ozonization circulation |
| CN206188475U (en) * | 2016-11-08 | 2017-05-24 | 江门市三清环境技术工程有限公司 | Ozone oxidation reactor |
| CN206447630U (en) * | 2016-11-28 | 2017-08-29 | 山东利源海达环境工程有限公司 | Integrated ozone catalyzing oxidizing degrading tank |
| CN107285524B (en) * | 2017-08-07 | 2020-11-20 | 北京化工大学 | Coupling type heterogeneous catalysis ozone efficient advanced sewage treatment method and device |
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| CN108059232A (en) | 2018-05-22 |
| CN107601645A (en) | 2018-01-19 |
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