CN117263356A - Wet oxidation reactor and use method thereof - Google Patents
Wet oxidation reactor and use method thereof Download PDFInfo
- Publication number
- CN117263356A CN117263356A CN202310482055.XA CN202310482055A CN117263356A CN 117263356 A CN117263356 A CN 117263356A CN 202310482055 A CN202310482055 A CN 202310482055A CN 117263356 A CN117263356 A CN 117263356A
- Authority
- CN
- China
- Prior art keywords
- gas
- reactor
- wastewater
- reactor cylinder
- cylinder
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000009279 wet oxidation reaction Methods 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000002351 wastewater Substances 0.000 claims abstract description 200
- 230000001590 oxidative effect Effects 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 194
- 239000012528 membrane Substances 0.000 claims description 42
- 229910052751 metal Inorganic materials 0.000 claims description 24
- 239000002184 metal Substances 0.000 claims description 24
- 229910000990 Ni alloy Inorganic materials 0.000 claims description 21
- 229910052760 oxygen Inorganic materials 0.000 claims description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 20
- 239000001301 oxygen Substances 0.000 claims description 20
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims description 16
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 13
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 10
- 239000004155 Chlorine dioxide Substances 0.000 claims description 8
- 235000019398 chlorine dioxide Nutrition 0.000 claims description 8
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 7
- 239000000919 ceramic Substances 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 7
- 239000012982 microporous membrane Substances 0.000 claims description 4
- 229910001069 Ti alloy Inorganic materials 0.000 claims description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 3
- 239000010936 titanium Substances 0.000 claims description 3
- 229910052719 titanium Inorganic materials 0.000 claims description 3
- 229910001093 Zr alloy Inorganic materials 0.000 claims description 2
- 239000002131 composite material Substances 0.000 claims description 2
- 239000010935 stainless steel Substances 0.000 claims description 2
- 229910001220 stainless steel Inorganic materials 0.000 claims description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims 3
- 230000000694 effects Effects 0.000 abstract description 13
- 239000003344 environmental pollutant Substances 0.000 abstract description 9
- 231100000719 pollutant Toxicity 0.000 abstract description 9
- 238000009776 industrial production Methods 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 29
- 239000007791 liquid phase Substances 0.000 description 16
- 208000028659 discharge Diseases 0.000 description 13
- 239000007800 oxidant agent Substances 0.000 description 13
- 239000012071 phase Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 9
- 238000001514 detection method Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 230000009471 action Effects 0.000 description 4
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- 239000000356 contaminant Substances 0.000 description 3
- 239000010842 industrial wastewater Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- XDTRNDKYILNOAP-UHFFFAOYSA-N phenol;propan-2-one Chemical compound CC(C)=O.OC1=CC=CC=C1 XDTRNDKYILNOAP-UHFFFAOYSA-N 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- 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
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
Landscapes
- 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
A wet oxidation reactor and method of use thereof, the reactor comprising: a wastewater inlet is formed in one side of the upper part of the reactor cylinder; the waste water outlet at the bottom of the reactor cylinder is connected with a pneumatic lifting pipe, and the tail part of the pneumatic lifting pipe is provided with a waste water outlet; the middle part of the pneumatic lifting pipe is provided with an emptying port; gas distributors are arranged at the lower parts in the reactor cylinder body and the pneumatic lifting pipe; the gas distributor is provided with gas inlets at the outside of the reactor cylinder or the pneumatic lifting pipe respectively; the top of the reaction cylinder is provided with a gas condenser; the gas condenser is provided with a tail gas discharge port. The use method is that the waste water to be treated is injected, a reactor cylinder and a gas distributor in a pneumatic lifting pipe are started at the same time, oxidizing gas is aerated, and the waste water is discharged after oxidation reaction. The reactor has the advantages of simple structure, realization of reverse flow of gas and liquid without an external circulating pump, good gas-liquid mass transfer effect and high pollutant removal rate. The method is simple, low in cost and suitable for industrial production.
Description
Technical Field
The invention relates to a reactor and a using method thereof, in particular to a wet oxidation reactor and a using method thereof.
Background
Wet oxidation (WAO) technology is a typical wastewater heat treatment technology, i.e. oxidation of organic matter in wastewater to CO with an oxidant at high temperature and high pressure 2 And water, thereby achieving the purpose of removing pollutants. The reaction mechanism of WAO is that under the conditions of high temperature and high pressure, oxygen in the air generates strong oxidative OH free radical on the surface of the catalyst, and organic pollutant and poison containing N, S and the like are directly oxidized into CO 2 And H 2 O and N 2 、SO 4 2－ Harmless substances such as the like; NO solid waste is generated in the process, and NO dioxin and NO are generated x 、SO 2 And secondary pollution waste gas. Meanwhile, the oxidation reaction heat can be fully utilized in the reaction process, self-heating balance is realized, and the energy conservation is good. WAO has the advantages of high removal rate, low operation cost, strong adaptability, no secondary pollution, simple flow, small occupied area and the like, and is paid attention to.
In the current wet oxidation reactor, the gas phase and the liquid phase both adopt the flow form of parallel flow in the same direction, after the gas phase is blown into the liquid phase of the reactor, the oxidant (generally oxygen) is gradually consumed along with the progress of the reaction, so that the partial pressure of the oxidant in the gas phase is gradually reduced closer to the outlet of the reactor, the concentration of the dissolved oxidant in the liquid phase at the water outlet end is very low, a large amount of refractory substances such as micromolecular acid formed by oxidation reaction exist in the water outlet end, and the substances can be degraded only under the condition of high oxidant concentration, so that the concentration of pollutants such as COD in the produced water of wet oxidation is still higher by adopting the mode of parallel flow of the gas phase and the liquid phase.
In addition, the current wet oxidation reactor adopts perforated pipes as gas distributors, the diameters of gas bubbles which are bulged out of the perforated pipes are large, the sizes of the gas bubbles are uneven, and the gas content is low, so that the gas-liquid mass transfer effect is poor, and the utilization rate of the oxidant is not high.
CN208150968U discloses an oxidation reaction tower with countercurrent gas-liquid, however, the countercurrent mode is realized by an external liquid-phase circulating pump, which is not suitable for the application scenario of wet oxidation at high temperature and high pressure.
CN113967448A discloses an internal circulation catalytic wet oxidation reactor and a water treatment system, which realizes the air-lift internal circulation of wastewater by arranging a guide cylinder, thereby improving the gas-liquid mass transfer effect. However, partial back mixing of the wastewater in the internal circulation reactor can result in low removal of contaminants from the produced water.
CN102513040a discloses a ceramic membrane microporous gas distributor. However, the distribution of the gas in the liquid is realized by the cross-flow in the distributor, and the gas distributor cannot be applied to a case where the gas distributor is a dead-end bubbling type of a wet oxidation reactor.
CN112340916a discloses a wet oxidation strengthening interface system, in which 2 liquid ejectors and 2 micro-interface generators for air intake are arranged in the reactor, so that high-efficiency mass transfer of gas and liquid can be realized. However, the internal structure of the reactor is very complicated, and the wastewater inlet is located close to the bottom discharge port and above the inlet micro-interface generator, the residence time of wastewater in the reactor is short, most of the gas is mixed with the dead water at the lower side of the reactor, which is unfavorable for the reaction of the gas with the pollution in the wastewater, and the reactor needs to intermittently discharge the cleaned wastewater from the bottom.
CN210855425U discloses a chemical sewage wet oxidation reactor, in which 1 vertical air pipe and 2-5 horizontal annular air pipes are arranged, which can increase the oxygen supply range in the reactor; meanwhile, a circulating pipeline and a circulating liquid pump are arranged, so that turbulent flow is generated in the material liquid, and the material is further fully contacted with oxygen. However, the water inlet and the overflow port of the reactor are both arranged at the top, and the reactor is provided with a circulating pipe, so that the material and the compressed air in the reactor generate mixed flow, and the removal rate of the reactor is lower than that of a plug flow reactor with water inlet and outlet at two ends; the circulating liquid pump is additionally arranged, the circulating liquid pump operates under high temperature and high pressure conditions, the service life of the circulating liquid pump is short, and the operating energy consumption of the circulating liquid pump is high; the annular air pipe is provided with a plurality of air holes, and the air holes are in the form of a common perforated pipe gas distributor, so that the diameters of generated air bubbles are large, and the gas-liquid mass transfer effect is not high.
Therefore, it is needed to find a wet oxidation reactor with simple structure, good gas-liquid mass transfer effect, flexible regulation and control of liquid level of liquid phase in the reactor and high removal rate of pollutants in wastewater, and a use method thereof, wherein the reverse flow of gas phase and liquid phase can be realized without an external circulating pump.
Disclosure of Invention
The invention aims to solve the technical problems of overcoming the defects in the prior art and providing the wet oxidation reactor which has the advantages of simple structure, good gas-liquid mass transfer effect, flexible regulation and control of the liquid level of the liquid phase in the reactor and high removal rate of pollutants in wastewater, and can realize the reverse flow of gas phase and liquid phase without an external circulating pump.
The invention further aims to solve the technical problems of overcoming the defects in the prior art and providing a use method of the wet oxidation reactor, which is simple to operate, low in cost and suitable for industrial production.
The technical scheme adopted for solving the technical problems is as follows: a wet oxidation reactor comprising: a wastewater inlet is formed in one side of the upper part of the reactor cylinder; the waste water outlet at the bottom of the reactor cylinder is connected with a pneumatic lifting pipe, and the tail part of the pneumatic lifting pipe is provided with a waste water outlet; an evacuation port is arranged at the lowest part of the pneumatic lifting pipe; the lower parts in the reactor cylinder and the pneumatic lifting pipe are respectively provided with a gas distributor; the gas distributor is provided with gas inlets at the outside of the reactor cylinder or the air lift pipe respectively; the top of the reaction cylinder is provided with a gas condenser; and the gas condenser is provided with a tail gas discharge port. In the wet oxidation reactor, the gas phase and the liquid phase in the reactor cylinder body flow reversely, waste water is fed into the reactor from a waste water inlet at the upper part, flows into a pneumatic lifting pipe from the bottom and flows out from a waste water outlet, the concentration of an oxidant at the waste water outlet end is higher than that at the waste water inlet end, gas is fed into a plurality of gas distributors at the lower part in the reactor cylinder body, and is cooled by a gas condenser at the top of the reactor cylinder body and then is discharged from a tail gas discharge port. The design of countercurrent flow of the gas phase and the liquid phase in the reactor cylinder body relieves the dilution of nitrogen and carbon dioxide in lower-layer gas to oxygen in upper-layer gas, and the closer to the waste water outlet, the higher the partial pressure of the gas phase oxidant in the waste water outlet is, namely the higher the concentration of the oxidant in the waste water outlet is than that in the waste water inlet, and solves the problems of low concentration of the dissolved oxidant in the liquid phase of the water outlet and higher concentration of pollutants such as water production COD (chemical oxygen demand) of wet oxidation. The tail gas discharged from the tail gas discharge port on the condenser can be sent to the next working procedure together with the wastewater from the wastewater discharge port, or the tail gas can be circularly introduced into the gas distributor again according to the reduction degree of the tail gas. The evacuation port is used for evacuating the wastewater in the reactor when the equipment is deactivated.
The wet oxidation reactor of the invention has the working procedures that: the waste water to be treated is injected from a waste water inlet, a gas distributor in a reactor cylinder and a pneumatic lifting pipe is started simultaneously, oxidizing gas is aerated, the waste water reacts with the oxidizing gas in the reactor cylinder, the oxidized waste water is further oxidized by the oxidizing gas in the pneumatic lifting pipe, and meanwhile, the oxidized waste water is discharged under the actions of increasing gas content and reducing density and the difference of the heights of a waste water outlet and the waste water inlet.
Preferably, the number of the gas distributor groups in the reactor cylinder is n,3n-2 is less than or equal to the height meter number of the reactor cylinder, and n is an integer which is more than or equal to 1.
Preferably, when there are two or more gas distributors, the uppermost gas distributor is 300-2500 mm (more preferably 1000-2000 mm) lower than the height of the wastewater inlet, and the height of the lowermost gas distributor of one or two or more gas distributors from the bottom of the reactor cylinder is 30-300 mm.
Preferably, the gas distributor is a conventional perforated tube gas distributor or a microporous membrane gas distributor.
Preferably, the microporous membrane is an inorganic membrane.
Preferably, the inorganic film is made of one or a combination of several of metal film, ceramic film or metal and ceramic composite film. More preferably, the metal film is a nickel alloy metal film. The inorganic film can disperse the gas in the liquid phase into micro bubbles, and the bubbles are distributed more uniformly, so that the mass transfer effect is better.
Preferably, the inorganic membrane is in the form of a tubular membrane and/or a flat sheet membrane.
Preferably, the tubular membranes are arranged in a vertical or horizontal manner in the reactor cylinder, and the tubular membranes are arranged in a vertical manner in the air lift pipe.
Preferably, the projections between adjacent tubular films do not overlap. The arrangement may make the gas distribution more uniform.
Preferably, when the tubular membrane is horizontal, the tubular membrane is disposed on the main gas inlet pipe parallel to the cross section of the reactor cylinder, and the tail end of the tubular membrane is 5 to 50mm (more preferably 6 to 30 mm) from the inner wall of the reactor cylinder.
Preferably, when the tubular membrane is vertical, the tubular membrane is disposed on the main gas inlet pipe parallel to the axial direction of the reactor cylinder or the gas lift pipe, and the length of the tubular membrane is 20 to 800mm (more preferably 100 to 500 mm).
Preferably, the tubular membrane has a diameter of 10 to 80mm and a pore diameter of 0.1 to 20 μm (more preferably 0.1 to 10 μm, still more preferably 0.1 to 5 μm). The tail end of each tubular membrane is sealed by a blind plate, and the other end of each tubular membrane is connected with a main air inlet pipe.
Preferably, the membrane in the flat membrane is disc-shaped, and the edge of the membrane is 5-50 mm away from the inner wall of the reactor cylinder. The bottom of the disc is connected with the main air inlet pipe.
Preferably, the air lifting pipe is internally provided with more than or equal to 1 group of gas distributors, and the height of the lowest layer of gas distributors from the bottom of the reactor cylinder body is 30-300 mm. The oxidative gas is blown into the air-lift pipe by the gas distributor, and the waste water density in the air-lift pipe is lower than the water density in the reactor cylinder body under the high gas content by the air-lift action of the blown oxidative gas, and the principle of the U-shaped communicating pipe ensures that the waste water flows from bottom to top.
Preferably, the diameter of the air lift tube is less than or equal to 1/10 of the diameter of the reactor cylinder. More preferably, the diameter of the air-lift tube is 25 to 120mm (more preferably 30 to 80 mm).
Preferably, the elevation of the wastewater outlet is-500 to +1000 mm (more preferably 0 to 300 mm) lower than the elevation of the wastewater inlet. The height difference of the waste water outlet and the waste water inlet and the air outlet quantity of the air distributor in the air lift pipe are controlled, so that the difference is generated between the air content and the density of the waste water in the air lift pipe and the waste water in the reactor, and the control of the liquid level in the reactor is realized. The height of the liquid level in the reactor determines the residence time of the wastewater in the reactor, and influences the removal effect of pollutants in the wastewater.
Preferably, the wastewater inlet is 200-500 mm lower than the top of the reactor cylinder.
Preferably, the height to diameter ratio of the reactor cylinder is 4-20:1 (more preferably 6-15:1). The larger the height-diameter ratio is, the higher the gas content is, and the better the gas-liquid mass transfer effect is, however, the larger the height-diameter ratio is, the more the material consumption of the reactor is increased, and the investment of the reactor is increased.
Preferably, the reactor cylinder is made of stainless steel, nickel alloy, zirconium alloy or titanium alloy.
Preferably, the condenser is provided with a cooling water inlet and a cooling water outlet. The condenser cools the flowing gas through cooling water or low-temperature raw water, and realizes condensation of water vapor, and the condensed water flows back to the reactor.
Preferably, the condenser is made of titanium coil pipes with diameters of 6-50 mm and lengths of 1-30 m.
The technical scheme adopted by the invention for further solving the technical problems is as follows: a method for using wet oxidation reactor features that the waste water to be treated is injected from waste water inlet, the gas distributor in reactor cylinder and air lift tube is started, oxidizing gas is aerated, and after oxidizing reaction, the waste water is discharged up to standard or ready to be treated by biochemical system.
Preferably, the COD concentration of the wastewater to be treated is 2000-200000 mg/L (more preferably 10000-150000 mg/L), and the ammonia nitrogen concentration is 200-50000 mg/L (more preferably 500-15000 mg/L). The wastewater treated by the method is derived from industrial wastewater of phenol-acetone devices or industrial wastewater of hydrogen peroxide of caprolactam devices in chemical enterprises.
Preferably, the oxidizing gas and the treatmentGas-liquid ratio Nm of wastewater treatment 3 /m 3 2 to 160:1 (more preferably 10 to 100:1, still more preferably 20 to 60:1), and the gas flow rate in the air-lift tube is 1 to 10 times (more preferably 1 to 6 times, still more preferably 1 to 3 times) the gas flow rate in the reactor vessel. The gas-liquid ratio is the ratio of the flow rate of gas to the flow rate of liquid under the internal standard condition of the reactor, the amount of the oxidant can be ensured to be in a proper range by controlling the gas-liquid ratio, the waste of the excessive gas-liquid ratio is avoided, the economy is not realized, and the excessive low gas-liquid ratio is insufficient for oxidizing the organic matters in the wastewater. The gas flow rate in the air lift tube is greater than that in the reactor cylinder to ensure that the gas content in the air lift tube is greater than that in the reactor cylinder.
Preferably, the temperature of the oxidation reaction is 180 to 320 ℃ (more preferably 200 to 290 ℃, still more preferably 230 to 275 ℃), the pressure is 0.5 to 12.0MPa (more preferably 2 to 10MPa, still more preferably 4 to 8 MPa), and the wastewater residence time is 0.2 to 5.0 hours (more preferably 0.5 to 4.0 hours, still more preferably 1.5 to 3.5 hours). The cost is low under the reaction condition, and the condition that the removal rate is insufficient due to overhigh temperature, overhigh pressure or overlong residence time is avoided, otherwise, the operation cost is too high.
Preferably, the oxidizing gas in the reactor cylinder is one or more of air, oxygen, ozone-containing air, chlorine dioxide-containing air and the like. The oxygen comprises oxygen-enriched pure oxygen, and the volume concentration of the oxygen-enriched oxygen is more than 21 percent.
Preferably, the oxidizing gas in the air lift pipe is one or more of pure oxygen, ozone-containing air, chlorine-containing air or chlorine dioxide-containing air.
Preferably, the concentration of the ozone-containing air, chlorine-containing air or chlorine dioxide-containing air is 50-5000 mg/Nm 3 (more preferably 80 to 1000 mg/Nm) 3 ）。
Preferably, when the gas distributors in the reactor cylinder or the air lift pipe are in a plurality of groups, the same oxidizing gas is introduced or oxidizing gas with gradually increased oxidizing property is introduced from top to bottom. For example, when the gas distributor of the reactor cylinder is three layers, the uppermost layer is filled with air, the middle layer is filled with air, oxygen-enriched or pure oxygen, and the lowermost layer is filled with oxygen-enriched or pure oxygen.
The beneficial effects of the invention are as follows:
(1) The gas phase and the liquid phase in the wet oxidation reactor reversely flow, and the upward flow of wastewater at the bottom of the reactor in the air lift pipe is realized by the air lift effect and the principle of the U-shaped communicating pipe, so that an external circulating pump is not needed; the concentration of the oxidant in the wastewater outlet is higher than that in the wastewater inlet, so that the problems of low concentration of the dissolved oxidant in the liquid phase of the water outlet and high concentration of pollutants such as COD (chemical oxygen demand) of produced water of wet oxidation are solved, the removal rate of COD in the wastewater can be up to 99.53%, the removal rate of ammonia nitrogen can be up to 99.55%, and the lower concentration of the pollutants in the produced water is realized;
(2) The wet oxidation reactor adopts a plurality of groups of gas distributors and selects the inorganic membrane for aeration, so that gas in a liquid phase is dispersed into micro bubbles, the bubbles are distributed more uniformly, and the mass transfer effect is better;
(3) The wet oxidation reactor controls the elevation difference of the wastewater outlet and the wastewater inlet and the air outlet quantity of the air distributor in the air lift pipe, so that the air content and the density of the wastewater in the air lift pipe and the wastewater in the reactor are different, and the flexible control of the liquid level in the reactor is realized;
(4) The method of the invention has simple operation and low cost, and is suitable for industrial production.
Drawings
FIG. 1 is a schematic longitudinal section of a wet oxidation reactor according to example 1 of the present invention;
FIG. 2 is a top view of a gas distributor (horizontal tube) in a wet oxidation reactor according to example 1 of the present invention;
FIG. 3 is a top view of a gas distributor (riser) in a wet oxidation reactor according to example 3 of the present invention;
fig. 4 is a cross-sectional view of fig. 3 at A-A.
Detailed Description
The invention is further described below with reference to examples and figures.
The wastewater 1 used in the embodiment of the invention is derived from industrial wastewater of phenol-acetone devices of certain chemical enterprises, the COD concentration is 15000mg/L, and the ammonia nitrogen concentration is 800mg/L; the wastewater 2 is derived from the wastewater produced by the caprolactam device of a certain chemical enterprise, the COD concentration is 92000mg/L, and the ammonia nitrogen concentration is 1800mg/L; the materials or reagents used in the examples of the present invention, unless otherwise specified, were obtained from conventional commercial sources.
Wet oxidation reactor example 1
As shown in fig. 1 and 2, a wet oxidation reactor includes: a reactor cylinder 1 (titanium alloy TA10 material, diameter 540mm and height 5000 mm), wherein a wastewater inlet 1-1 is arranged at one side of the upper part of the reactor cylinder 1; the waste water outlet 1-2 at the bottom of the reactor cylinder 1 is connected with a pneumatic lifting pipe 2, and the tail part of the pneumatic lifting pipe 2 is provided with a waste water outlet 2-1; an evacuation port 2-2 is arranged at the lowest part of the pneumatic lifting pipe 2; the lower part in the reactor cylinder body 1 is provided with 2 groups of horizontal tubular nickel alloy metal film gas distributors 3, and the lower part in the air lifting pipe 2 is provided with 1 group of vertical tubular nickel alloy metal film gas distributors 3; the gas distributor 3 is provided with gas inlets 1-3 and 2-3 outside the reactor cylinder 1 or the air lift pipe 2 respectively; the top of the reaction cylinder 1 is provided with a gas condenser 4; the gas condenser 4 is provided with a tail gas discharge port 4-1; the condenser 4 is provided with a cooling water inlet 4-2 and a cooling water outlet 4-3;
in 2 groups of horizontal tubular nickel alloy metal film gas distributors 3 in the reactor cylinder 1, the height of the uppermost gas distributor 3 from the bottom of the reactor cylinder 1 is 3000mm, the height of the lowermost gas distributor 3 from the bottom of the reactor cylinder 1 is 150mm, 10 tubular nickel alloy metal films 3-1 are arranged in each group of horizontal tubular nickel alloy metal film gas distributors 3, the diameter is 60mm, the aperture is 0.2 mu m, projections between adjacent tubular nickel alloy metal films 3-1 are not overlapped, the cross section of the reactor cylinder 1 is parallel to the main air inlet pipe 3-2, and the tail end of each tubular nickel alloy metal film 3-1 is 10mm from the inner wall of the reactor cylinder 1;
in the 1-group vertical type tubular nickel alloy metal film gas distributor 3 in the pneumatic lifting pipe 2, 2 tubular nickel alloy metal films 3-1 are totally arranged, the diameter is 15mm, the aperture is 0.2 mu m, the length is 150mm, projections between adjacent tubular nickel alloy metal films 3-1 are not overlapped, and the projections are parallel to the axial direction of the pneumatic lifting pipe 2 and are arranged on the main gas inlet pipe 3-2;
the tail end of each tubular nickel alloy metal film 3-1 is sealed by a blind plate, and the other end of each tubular nickel alloy metal film is connected with a main air inlet pipe 3-2;
the height of the gas distributor 3 in the air lift pipe 2 from the bottom of the reactor cylinder 1 is 150mm, and the diameter of the air lift pipe 2 is 32mm; the height of the waste water outlet 2-1 from the bottom of the reactor cylinder 1 is 4500mm; the height from the wastewater inlet 1-1 to the bottom of the reactor cylinder 1 is 4500mm; the condenser 4 is made of titanium coil pipes with the diameter of 15mm and the length of 2 m.
The working process of the wet oxidation reactor of the embodiment of the invention is as follows: the waste water to be treated is injected from a waste water inlet 1-1, a gas distributor 3 in a reactor cylinder 1 and a pneumatic lifting pipe 2 is started at the same time, oxidizing gas is aerated, the waste water reacts with the oxidizing gas in the reactor cylinder 1, the oxidized waste water is further oxidized by the oxidizing gas in the pneumatic lifting pipe 2, and meanwhile, the oxidized waste water is discharged under the actions of increasing gas content and reducing density.
Wet oxidation reactor example 2
This embodiment differs from embodiment 1 only in that: 2 groups of horizontal tubular nickel alloy metal film gas distributors 3 are arranged at the lower part in the reactor cylinder 1; 10 tubular nickel alloy metal films 3-1 with a diameter of 50mm and a pore diameter of 2 μm are arranged in each group of horizontal tubular nickel alloy metal film gas distributors 3. Example 1 was followed.
The wet oxidation reactor of the present embodiment operates as in example 1.
Wet oxidation reactor example 3
As shown in fig. 3 and 4, this embodiment differs from embodiment 1 only in that: the height of the reactor cylinder 1 is 4000mm; the diameter of the air lift pipe 2 is 40mm; the reactor is characterized in that a reactor cylinder 1 is internally provided with 1 group of vertical tubular nickel alloy metal film gas distributors 3, 44 tubular nickel alloy metal films 3-1 are totally arranged, the diameter is 15mm, the aperture is 0.2 mu m, the length is 150mm, projections between adjacent tubular nickel alloy metal films 3-1 are not overlapped, and the projections are parallel to the axial direction of the reactor cylinder 1 and are arranged on a main gas inlet pipe 3-2; the height of the gas distributor 3 from the bottom of the reactor cylinder 1 is 100mm; the height of the waste water outlet 2-1 from the bottom of the reactor cylinder 1 is 3500mm; the height of the wastewater inlet 1-1 from the bottom of the reactor cylinder 1 is 3600mm. Example 1 was followed.
The wet oxidation reactor of the present embodiment operates as in example 1.
Wet oxidation reactor example 4
This embodiment differs from embodiment 1 only in that: the height of the waste water outlet 2-1 from the bottom of the reactor cylinder 1 is 4700mm; the height from the wastewater inlet 1-1 to the bottom of the reactor cylinder 1 is 4800mm; the lower part in the reactor cylinder 1 is provided with 2 groups of horizontal tubular ceramic membrane gas distributors 3, the diameter of the tubular ceramic membrane is 20mm, and the aperture is 0.1 mu m. Example 1 was followed.
The working process of the wet oxidation reactor of the embodiment of the invention is as follows: the waste water to be treated is injected from a waste water inlet 1-1, a gas distributor 3 in a reactor cylinder 1 and a pneumatic lifting pipe 2 is started at the same time, oxidizing gas is aerated, the waste water reacts with the oxidizing gas in the reactor cylinder 1, the oxidized waste water is further oxidized by the oxidizing gas in the pneumatic lifting pipe 2, meanwhile, the oxidized waste water is discharged under the action of the elevation difference of a gas content rate and a density reduction, and a waste water outlet 2-1 and the waste water inlet 1-1.
Method of Using Wet Oxidation reactor example 1
The wastewater 1 to be treated was injected at a flow rate of 400L/h from the wastewater inlet of example 1 of the wet oxidation reactor, and simultaneously the reactor cylinder and the gas distributor in the air lift tube were started to be exposed to the oxidizing gas, wherein the gas distributor at the upper layer in the reactor cylinder had an inflow rate of 8Nm 3 Air/h, gas distributor inlet flow rate of lower layer of 2Nm 3 Oxygen per h (volume concentration 99.5%) and gas sparger inlet flow rate in the gas lift tube of 0.05Nm 3 Air containing ozone per hour (concentration of ozone 80mg/Nm 3 ) At 260 ℃ and under the pressure of 6MPa,after oxidation reaction (the retention time of the wastewater is 2.2 h), the wastewater is discharged after reaching the standard.
The gas content of the wastewater in the reactor cylinder is 23% and the gas content of the wastewater in the air lift pipe is 32% through the detection of a differential pressure method, so that the density of the wastewater in the air lift pipe is smaller than that of the wastewater in the reactor cylinder, and the wastewater can spontaneously flow out from a wastewater outlet at the bottom of the reactor cylinder through the air lift pipe.
The water quality analyzer with Ha Xiduo parameters detects that the concentrations of COD and ammonia nitrogen in the wastewater discharged from the wastewater outlet are 230mg/L and 3.6mg/L respectively, and the wastewater meets the three-level discharge requirements of the integrated wastewater discharge standard (GB 8978-1996) and the removal rates are 98.42% and 99.55% respectively.
Method of Using Wet Oxidation reactor example 2
The wastewater 1 to be treated is injected from the wastewater inlet of the wet oxidation reactor example 2 at a flow rate of 350L/h, and simultaneously the reactor cylinder and the gas distributor in the air lift pipe are started to be exposed to oxidizing gas, wherein the inlet flow rate of the gas distributor positioned at the upper layer in the reactor cylinder is 8Nm 3 Air/h, gas distributor inlet flow rate of lower layer of 5Nm 3 Air/h, gas distributor inlet flow in the gas lift tube of 0.05Nm 3 After oxidation reaction (residence time of wastewater is 2.5 h) of pure oxygen (volume concentration is 99.9%) at 260 ℃ and pressure of 6MPa, the wastewater is ready to enter a biochemical system for treatment.
The gas content of the wastewater in the reactor cylinder is 26% and the gas content of the wastewater in the air lift pipe is 33% through the detection of a differential pressure method, so that the density of the wastewater in the air lift pipe is smaller than that of the wastewater in the reactor cylinder, and the wastewater can spontaneously flow out from a wastewater outlet at the bottom of the reactor cylinder through the air lift pipe.
The water quality analyzer with Ha Xiduo parameters detects that the concentration of COD and ammonia nitrogen in the wastewater discharged from the wastewater outlet is 1287mg/L and 94.4mg/L respectively, and the biochemical index (COD/BOD) 5 ) B/c=0.42, meets the water inlet index requirement of the biochemical system, and has the removal rates of 91.42% and 88.20% respectively.
Method of Using Wet Oxidation reactor example 3
The wastewater 1 to be treated is injected from the wastewater inlet of the wet oxidation reactor example 3 at a flow rate of 315L/h, and simultaneously a gas distributor in a reactor cylinder and a gas lift pipe is started to expose oxidizing gas, wherein the gas distributor in the reactor cylinder has an inlet flow rate of 7.8Nm 3 Air/h, gas distributor inlet flow in the gas lift tube of 0.05Nm 3 Air containing ozone per hour (concentration of ozone 80mg/Nm 3 ) After oxidation reaction (residence time of wastewater is 2.2 h) is carried out at 260 ℃ and under the pressure of 6MPa, the wastewater is ready to enter a biochemical system for treatment.
The gas content of the wastewater in the reactor cylinder is 21% and the gas content of the wastewater in the air lift pipe is 33.5% detected by a differential pressure method, so that the density of the wastewater in the air lift pipe is less than that of the wastewater in the reactor cylinder, and the wastewater can spontaneously flow out from a wastewater outlet at the bottom of the reactor cylinder through the air lift pipe.
The water quality analyzer with Ha Xiduo parameters detects that the concentration of COD and ammonia nitrogen in the wastewater discharged from the wastewater outlet is 1567mg/L and 147mg/L respectively, and the biochemical index (COD/BOD) 5 ) B/c=0.39, meets the water inflow index requirement of the biochemical system, and has the removal rate of 89.55% and 81.63% respectively.
Method of Using Wet Oxidation reactor example 4
The wastewater 1 to be treated is injected from the wastewater inlet of the wet oxidation reactor example 4 at a flow rate of 280L/h, and simultaneously the reactor cylinder and the gas distributor in the air lift pipe are started to be exposed to oxidizing gas, wherein the inlet flow rate of the gas distributor positioned at the upper layer in the reactor cylinder is 8Nm 3 Air/h, gas distributor inlet flow rate of lower layer of 2Nm 3 Oxygen per h (volume concentration 99.5%) and gas sparger inlet flow rate in the gas lift tube of 0.05Nm 3 And (3) carrying out oxidation reaction (the retention time of the wastewater is 3.4 h) on the pure oxygen per hour (the volume concentration is 99.5%) at 257 ℃ and the pressure is 5.5MPa, and then discharging the wastewater after reaching the standard.
The gas content of the wastewater in the reactor cylinder is 24% and the gas content of the wastewater in the air lift pipe is 34% through the detection of a differential pressure method, so that the density of the wastewater in the air lift pipe is smaller than that of the wastewater in the reactor cylinder, and the wastewater can spontaneously flow out from a wastewater outlet at the bottom of the reactor cylinder through the air lift pipe.
The water quality analyzer with Ha Xiduo parameters detects that the concentrations of COD and ammonia nitrogen in the wastewater discharged from the wastewater discharge port are 272mg/L and 78mg/L respectively, and meet the three-level discharge requirements of the Integrated wastewater discharge Standard (GB 8978-1996), and the removal rates are 98.18% and 90.23% respectively.
Method of Using Wet Oxidation reactor example 5
The wastewater 1 to be treated was injected at a flow rate of 400L/h from the wastewater inlet of example 1 of the wet oxidation reactor, and simultaneously the reactor cylinder and the gas distributor in the air lift tube were started to be exposed to the oxidizing gas, wherein the gas distributor at the upper layer in the reactor cylinder had an inflow rate of 8Nm 3 Air/h, gas distributor inlet flow rate of lower layer of 2Nm 3 Industrial oxygen enrichment per h (volume concentration 40%), gas sparger feed rate in the air-lift tube was 0.08Nm 3 Air containing chlorine dioxide/h (concentration of chlorine dioxide 500 mg/Nm) 3 ) And (3) performing oxidation reaction (the retention time of the wastewater is 2.2 h) at 270 ℃ and under the pressure of 6.5MPa, and discharging the wastewater after reaching the standard.
The gas content of the wastewater in the reactor cylinder is 23% and the gas content of the wastewater in the air lift pipe is 35% through the detection of a differential pressure method, so that the density of the wastewater in the air lift pipe is smaller than that of the wastewater in the reactor cylinder, and the wastewater can spontaneously flow out from a wastewater outlet at the bottom of the reactor cylinder through the air lift pipe.
The water quality analyzer with Ha Xiduo parameters detects that the concentrations of COD and ammonia nitrogen in the wastewater discharged from the wastewater outlet are 95mg/L and 44mg/L respectively, which meet the secondary discharge requirements of the Integrated wastewater discharge Standard (GB 8978-1996) and the removal rates are 99.36% and 94.50% respectively.
Method of Using Wet Oxidation reactor example 6
This embodiment differs from embodiment 1 only in that: the wastewater to be treated is wastewater 2; the oxidation reaction was carried out at 275℃and a pressure of 8 MPa. Example 1 was followed.
The gas content of the wastewater in the reactor cylinder is 23% and the gas content of the wastewater in the air lift pipe is 32% through the detection of a differential pressure method, so that the density of the wastewater in the air lift pipe is smaller than that of the wastewater in the reactor cylinder, and the wastewater can spontaneously flow out from a wastewater outlet at the bottom of the reactor cylinder through the air lift pipe.
The water quality analyzer with Ha Xiduo parameters detects that the concentrations of COD and ammonia nitrogen in the wastewater discharged from the wastewater discharge port are 430mg/L and 296mg/L respectively, and the wastewater meets the three-level discharge requirements of the Integrated wastewater discharge Standard (GB 8978-1996) and the removal rates are 99.53% and 83.56% respectively.
Wet oxidation reactor comparative example 1
This comparative example differs from example 1 only in that: the waste water outlet 1-2 is changed into a waste water inlet, the waste water inlet 1-1 is changed into a waste water outlet, and the air lifting pipe 2 is removed. Example 1 was followed.
Comparative example 1 of use method of wet oxidation reactor
Injecting waste water 1 to be treated into the wet oxidation reactor from the waste water inlet of the wet oxidation reactor from the comparative example 1 at a flow rate of 295L/h, simultaneously starting a gas distributor in the reactor cylinder body, and exposing the waste water to oxidizing gas, wherein the inlet flow rate of the gas distributor positioned at the upper layer in the reactor cylinder body is 8Nm 3 Air/h, gas distributor inlet flow rate of lower layer of 2Nm 3 The oxidation reaction was carried out with oxygen per hour (oxygen concentration: 99.5%) at 260℃and a pressure of 6MPa (wastewater retention time: 3.0 hours), and then wastewater was discharged.
The gas content of the wastewater in the reactor cylinder body is 25 percent by the detection of a differential pressure method.
The water quality analyzer with Ha Xiduo parameters detects that the concentrations of COD and ammonia nitrogen in the wastewater discharged from the wastewater outlet are 2646mg/L and 338mg/L respectively, the wastewater does not meet the requirements of the three-level discharge standard of the integrated wastewater discharge standard (GB 8978-1996) on COD not more than 500mg/L, and the removal rates are 82.36% and 57.74% respectively. It is understood that the mass transfer effect and the contaminant removal rate of the conventional gas-liquid co-current flow method are significantly lower than those of the gas-liquid countercurrent method of example 1 under the same reaction conditions.
Use method of wet oxidation reactor comparative example 2
This comparative example differs from example 1 only in that: the gas distributor in the air riser is not activated.
The gas content of the waste water in the reactor cylinder is 23% and the gas content of the waste water in the air lift pipe is 0% through the detection of a differential pressure method, so that the density of the waste water in the air lift pipe is higher than that of the waste water in the reactor cylinder, and the waste water can only flow out from the top of the reactor cylinder along with the gas through a tail gas discharge port on a gas condenser, but cannot flow upwards through the air lift pipe from a waste water outlet at the bottom of the reactor cylinder to be discharged.
The water quality analyzer with Ha Xiduo parameters detects that the concentration of COD and ammonia nitrogen in the wastewater discharged from the wastewater outlet is 3260mg/L and 585mg/L respectively, which does not meet the requirements of the three-level discharge standard of wastewater comprehensive discharge standard (GB 8978-1996) on COD not more than 500mg/L and the biochemical index (COD/BOD) 5 ) B/c=0.25, which does not meet the water inflow index requirement of the biochemical system, and the removal rates are 78.27% and 26.88% respectively. It is understood that the mass transfer effect and the contaminant removal rate of the conventional gas-liquid parallel flow method can be achieved only under the same reaction conditions without using the gas distributor of the air lift pipe, and are significantly lower than those of the gas-liquid countercurrent method of example 1.
Claims (6)
1. A wet oxidation reactor comprising: reactor barrel, its characterized in that: a wastewater inlet is formed in one side of the upper part of the reactor cylinder; the waste water outlet at the bottom of the reactor cylinder is connected with a pneumatic lifting pipe, and the tail part of the pneumatic lifting pipe is provided with a waste water outlet; an evacuation port is arranged at the lowest part of the pneumatic lifting pipe; the lower parts in the reactor cylinder and the pneumatic lifting pipe are respectively provided with a gas distributor; the gas distributor is provided with gas inlets at the outside of the reactor cylinder or the air lift pipe respectively; the top of the reaction cylinder is provided with a gas condenser; and the gas condenser is provided with a tail gas discharge port.
2. The wet oxidation reactor according to claim 1, wherein: the number of the gas distributor groups in the reactor cylinder is n, the number of the gas distributor groups in the reactor cylinder is 3n-2 which is less than or equal to the height meter number of the reactor cylinder, and n is an integer which is more than or equal to 1; when two or more layers of gas distributors exist, the height of the uppermost layer of gas distributor is 300-2500 mm lower than the height of the wastewater inlet, and the height of the lowermost layer of gas distributor of one layer of gas distributor or two or more layers of gas distributors from the bottom of the reactor cylinder is 30-300 mm; the gas distributor is a common perforated pipe gas distributor or a microporous membrane gas distributor; the microporous membrane is an inorganic membrane; the inorganic membrane is made of one or a combination of a plurality of metal membranes, ceramic membranes or metal and ceramic composite membranes; the inorganic membrane is in the form of a tubular membrane and/or a flat membrane; the tubular membrane is arranged in a vertical or horizontal mode in the reactor cylinder body, and the tubular membrane is arranged in a vertical mode in the pneumatic lifting pipe; the projections between adjacent tubular films are not overlapped; when the tubular membrane is horizontal, the tubular membrane is arranged on the main air inlet pipe in parallel with the section of the reactor cylinder, and the tail end of the tubular membrane is 5-50 mm away from the inner wall of the reactor cylinder; when the tubular membrane is vertical, the tubular membrane is arranged on the main air inlet pipe in parallel to the axial direction of the reactor cylinder or the air lifting pipe, and the length of the tubular membrane is 20-800 mm; the diameter of the tubular membrane is 10-80 mm, and the aperture is 0.1-20 mu m; the membrane in the flat membrane is disc-shaped, and the edge of the membrane is 5-50 mm away from the inner wall of the reactor cylinder.
3. A wet oxidation reactor according to claim 1 or 2, characterized in that: the pneumatic lifting pipe is internally provided with more than or equal to 1 group of gas distributors, and the height of the lowest gas distributor from the bottom of the reactor cylinder body is 30-300 mm; the diameter of the air lift pipe is less than or equal to 1/10 of the diameter of the reactor cylinder; the elevation of the wastewater outlet is lower than that of the wastewater inlet by-500 to minus 1000mm; the wastewater inlet is 200-500 mm lower than the top of the reactor cylinder.
4. A wet oxidation reactor according to any one of claims 1 to 3, wherein: the height-diameter ratio of the reactor cylinder is 4-20:1; the reactor cylinder body is made of stainless steel, nickel alloy, zirconium alloy or titanium alloy; the condenser is provided with a cooling water inlet and a cooling water outlet; the condenser is made of titanium coil pipes with the diameter of 6-50 mm and the length of 1-30 m.
5. A method of using the wet oxidation reactor according to claim 1 to 4, wherein: and (3) injecting the wastewater to be treated into the reactor through a wastewater inlet, simultaneously starting a reactor cylinder and a gas distributor in the air lift pipe, exposing oxidizing gas, and performing oxidation reaction to obtain the wastewater which is discharged up to the standard or ready to enter a biochemical system for treatment.
6. A method of using a wet oxidation reactor according to claim 5, wherein: the COD concentration of the wastewater to be treated is 2000-200000 mg/L, and the ammonia nitrogen concentration is 200-50000 mg/L; gas-liquid ratio Nm of oxidizing gas and wastewater to be treated 3 /m 3 Is 2-160:1, and the gas flow rate in the air lift pipe is 1-10 times of the gas flow rate in the reactor cylinder; the temperature of the oxidation reaction is 180-320 ℃, the pressure is 0.5-12.0 MPa, and the residence time of the wastewater is 0.2-5.0 h; the oxidizing gas in the reactor cylinder is one or more of air, oxygen, air containing ozone, air containing chlorine gas or air containing chlorine dioxide; the oxidizing gas in the air lift pipe is one or more of pure oxygen, air containing ozone, air containing chlorine gas or air containing chlorine dioxide; the concentration of the air containing ozone, chlorine gas or chlorine dioxide is 50-5000 mg/Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the When the gas distributors in the reactor cylinder or the air lifting pipe are in a plurality of groups, the same oxidizing gas is introduced or the oxidizing gas with gradually increased oxidizing property is introduced from top to bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310482055.XA CN117263356A (en) | 2023-04-28 | 2023-04-28 | Wet oxidation reactor and use method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310482055.XA CN117263356A (en) | 2023-04-28 | 2023-04-28 | Wet oxidation reactor and use method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN117263356A true CN117263356A (en) | 2023-12-22 |
Family
ID=89201509
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310482055.XA Pending CN117263356A (en) | 2023-04-28 | 2023-04-28 | Wet oxidation reactor and use method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117263356A (en) |
-
2023
- 2023-04-28 CN CN202310482055.XA patent/CN117263356A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20040211723A1 (en) | Membrane supported bioreactor for municipal and industrial wastewater treatment | |
| CN104828926A (en) | Wastewater advanced treatment equipment and method for catalytic ozonation membrane reactor | |
| WO2023173715A1 (en) | Ozone catalytic oxidation and flotation integrated system and method for using same | |
| CN103112991A (en) | Coking wastewater treatment system and coking wastewater treatment method | |
| CN113735245B (en) | Method for catalytic oxidation of sewage by ozone | |
| CN110526527B (en) | Biological membrane biochemical reaction system based on ozone and wastewater purification process | |
| CN212151749U (en) | High-efficient ozone catalytic oxidation processing apparatus of high salt waste water | |
| CN114426382B (en) | Ozone oxidation treatment process for ship oil stain wastewater | |
| CN102616995B (en) | A kind of catalytic ozonation of reverse osmosis concentrated water and biochemical composite handling arrangement and application method thereof | |
| CN102219326B (en) | Oxidation nanofiltration membrane reactor | |
| CN211770809U (en) | High-pollution degradation-resistant wastewater efficient treatment device | |
| CN117263356A (en) | Wet oxidation reactor and use method thereof | |
| CN220098708U (en) | Wet oxidation reactor | |
| CN220684912U (en) | Full quantitative treatment system for leachate | |
| CN110668552B (en) | Ozone synergistic micro hydrogen peroxide catalytic device and method | |
| CN114349246B (en) | Combined treatment method of polycyclic aromatic hydrocarbon wastewater | |
| CN110862196A (en) | High-efficiency treatment method, treatment device and application of high-pollution refractory wastewater | |
| CN203173936U (en) | Coking waste water oxidation and biochemical treatment equipment | |
| CN203173917U (en) | Coking waste water coal tar treatment equipment | |
| CN211111264U (en) | Biological fluidized bed reactor and wastewater treatment device | |
| CN210133954U (en) | Continuous reactor for treating wet desulphurization wastewater | |
| CN221440480U (en) | Catalytic wet oxidation reactor and reaction system | |
| CN210237220U (en) | Device for treating wastewater by catalytic oxidation of ozone | |
| CN217895264U (en) | Oxygen-enriched oxidation and carbon dioxide capture device for organic pollutants in wastewater | |
| CN217868452U (en) | Three-phase fluidized bed reaction device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |