CN220098708U - Wet oxidation reactor - Google Patents
Wet oxidation reactor Download PDFInfo
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- CN220098708U CN220098708U CN202321017459.3U CN202321017459U CN220098708U CN 220098708 U CN220098708 U CN 220098708U CN 202321017459 U CN202321017459 U CN 202321017459U CN 220098708 U CN220098708 U CN 220098708U
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- 238000009279 wet oxidation reaction Methods 0.000 title claims abstract description 43
- 239000002351 wastewater Substances 0.000 claims abstract description 83
- 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 22
- 239000000498 cooling water Substances 0.000 claims description 9
- 239000000919 ceramic Substances 0.000 claims description 7
- 229910001069 Ti alloy Inorganic materials 0.000 claims description 4
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 4
- 239000012982 microporous membrane Substances 0.000 claims description 4
- 239000010936 titanium Substances 0.000 claims description 4
- 229910052719 titanium Inorganic materials 0.000 claims description 4
- 229910001093 Zr alloy Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000002131 composite material Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 23
- 230000000694 effects Effects 0.000 abstract description 11
- 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
- 239000007789 gas Substances 0.000 description 99
- 230000001590 oxidative effect Effects 0.000 description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 18
- 239000007791 liquid phase Substances 0.000 description 16
- 239000007800 oxidant agent Substances 0.000 description 12
- 239000012071 phase Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 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
- 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
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 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
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000356 contaminant Substances 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
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
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; 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 reactor cylinder is provided with a gas condenser; the gas condenser is provided with a tail gas discharge port. The reactor has the advantages of simple structure, capability of realizing reverse flow of gas and liquid without an external circulating pump, good gas-liquid mass transfer effect, high pollutant removal rate and low cost, and is suitable for industrial production.
Description
Technical Field
The utility model relates to a reactor, in particular to a wet oxidation reactor.
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 which has a simple structure, can realize the reverse flow of gas phase and liquid phase without an external circulating pump, has good gas-liquid mass transfer effect, can flexibly regulate and control the liquid level of the liquid phase in the reactor, and has high pollutant removal rate in wastewater.
Disclosure of Invention
The utility model aims to solve the technical problems of the prior art, and provides 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, high pollutant removal rate in wastewater, low cost and suitability for industrial production, and can realize the reverse flow of the gas phase and the liquid phase without an external circulating pump.
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 reactor cylinder body 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 utility model 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 beneficial effects of the utility model 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%, the lower concentration of the pollutants in the produced water is realized, the cost is low, and the method is suitable for industrial production;
(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 of the utility model 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.
Drawings
FIG. 1 is a schematic longitudinal section of a wet oxidation reactor according to example 1 of the present utility model;
FIG. 2 is a top view of a gas distributor (horizontal tube) in a wet oxidation reactor according to example 1 of the present utility model;
FIG. 3 is a top view of a gas distributor (riser) in a wet oxidation reactor according to example 3 of the present utility model;
fig. 4 is a cross-sectional view of fig. 3 at A-A.
Detailed Description
The utility model is further described below with reference to examples and figures.
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 reactor 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 utility model 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 utility model 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.
Claims (5)
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 reactor cylinder body 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 claim 1 or 2, characterized in that: 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 wet oxidation reactor according to claim 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321017459.3U CN220098708U (en) | 2023-04-28 | 2023-04-28 | Wet oxidation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321017459.3U CN220098708U (en) | 2023-04-28 | 2023-04-28 | Wet oxidation reactor |
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| Publication Number | Publication Date |
|---|---|
| CN220098708U true CN220098708U (en) | 2023-11-28 |
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ID=88871756
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321017459.3U Active CN220098708U (en) | 2023-04-28 | 2023-04-28 | Wet oxidation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220098708U (en) |
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2023
- 2023-04-28 CN CN202321017459.3U patent/CN220098708U/en active Active
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