CN211111579U - Biomembrane biochemical reaction system based on ozone - Google Patents
Biomembrane biochemical reaction system based on ozone Download PDFInfo
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- CN211111579U CN211111579U CN201921624202.8U CN201921624202U CN211111579U CN 211111579 U CN211111579 U CN 211111579U CN 201921624202 U CN201921624202 U CN 201921624202U CN 211111579 U CN211111579 U CN 211111579U
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 284
- 238000005842 biochemical reaction Methods 0.000 title claims abstract description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 123
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 123
- 239000001301 oxygen Substances 0.000 claims abstract description 123
- 239000002351 wastewater Substances 0.000 claims abstract description 90
- 238000005273 aeration Methods 0.000 claims abstract description 69
- 238000011282 treatment Methods 0.000 claims abstract description 58
- 238000000354 decomposition reaction Methods 0.000 claims abstract description 26
- 239000012528 membrane Substances 0.000 claims abstract description 23
- 238000000746 purification Methods 0.000 claims abstract description 18
- 238000007599 discharging Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 82
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 78
- 239000003054 catalyst Substances 0.000 claims description 60
- 239000000945 filler Substances 0.000 claims description 15
- 239000000428 dust Substances 0.000 claims description 10
- 238000005949 ozonolysis reaction Methods 0.000 claims description 9
- 238000012856 packing Methods 0.000 claims description 6
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 5
- 238000011068 loading method Methods 0.000 claims description 5
- 238000003825 pressing Methods 0.000 claims description 5
- 239000013589 supplement Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 46
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 description 34
- 230000003647 oxidation Effects 0.000 description 31
- 230000003197 catalytic effect Effects 0.000 description 19
- 230000015556 catabolic process Effects 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 11
- 238000006731 degradation reaction Methods 0.000 description 11
- 230000006378 damage Effects 0.000 description 10
- 239000007788 liquid Substances 0.000 description 10
- 238000012546 transfer Methods 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 230000002779 inactivation Effects 0.000 description 7
- 238000011049 filling Methods 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 150000002391 heterocyclic compounds Chemical class 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000002957 persistent organic pollutant Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000002894 chemical waste Substances 0.000 description 3
- 125000000623 heterocyclic group Chemical group 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 231100000331 toxic Toxicity 0.000 description 3
- 230000002588 toxic effect Effects 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000005034 decoration Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000007142 ring opening reaction Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005465 channeling Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- Water Supply & Treatment (AREA)
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- Biodiversity & Conservation Biology (AREA)
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Abstract
The utility model discloses a biomembrane biochemical reaction system based on ozone belongs to the waste water treatment field. An ozone reactor which purifies wastewater by using ozone; the oxygen-enriched aeration biological film biochemical reactor is communicated with the ozone generator and is used for carrying out deep purification treatment on the purified wastewater and discharging the wastewater; the ozone decomposition reactor is respectively communicated with the ozone generator and the oxygen-enriched aeration biological membrane biochemical reactor and is used for decomposing the ozone which is not completely reacted after passing through the ozone reactor into oxygen. The utility model provides a low energy consumption, high efficiency, economic waste water deep purification system can make waste water purification discharge to reach standard under lower energy consumption.
Description
Technical Field
The utility model belongs to the waste water treatment field, in particular to biomembrane biochemical reaction system based on ozone for advanced treatment organic waste water.
Background
In order to deal with the increasingly worsened ecological environment, the nation continuously issues more strict environmental protection standards, the requirements for sewage treatment are continuously improved, and along with the rapid development of the industry, the water quantity of industrial wastewater is continuously increased, the components are more and more complex, and the treatment difficulty is more and more high, especially the treatment problem of organic pollutants which are difficult to degrade or have toxic effect on organisms causes great attention, but the organic pollutants are difficult to biodegrade and are also difficult to remove by oxidation with a common oxidant.
In order to achieve the purpose of advanced treatment of organic wastewater, the sewage treatment is generally carried out by adopting an ozone catalytic oxidation mode at present. The ozone catalytic oxidation method is an advanced oxidation technology based on ozone, and the principle is that ozone generates hydroxyl radical OH under the action of a catalyst, wherein OH is second to F in oxidation2The strong oxidant can effectively oxidize refractory organic pollutants. However, the prior art has at least the following problems:
1) the ozone catalytic oxidation technology is low in application economy. For example, the ozone reactor generates channeling and wall flow phenomena, which results in low ozone utilization rate and poor treatment effect; the tail gas ozone destructor can effectively destroy ozone only by high-temperature heating, and the energy consumption is high; the oxygen content (tail oxygen) in the tail gas after the ozonolysis is still more than 80 percent, and the tail gas is basically directly discharged into the atmosphere due to harmlessness, thereby causing a great deal of energy waste.
2) The catalytic oxidation by ozone is not complete for the oxidation of refractory organic matters, and the oxidized small molecular substances are difficult to be further oxidized, so that the simple catalytic oxidation by ozone has certain limitation on the treatment of the organic matters.
Patent CN201620061049.2 has proposed a two-stage ozone catalytic oxidation's effluent treatment plant, and waste water reentries into second grade ozone catalytic oxidation after one-level ozone catalytic oxidation, and ozone tail gas destroys the back direct discharge atmosphere, though this kind of method has improved the treatment degree of organic pollutant in the waste water, can not solve the problem that the ozone utilization ratio is low, and oxygen consumption and equipment investment cost are high moreover.
In order to solve the problem of ozone tail gas utilization, patent CN205603366U proposes that the ozone tail gas after catalytic oxidation by ozone is destroyed and then returned to the upstream biochemical reactor for recycling, although this method reduces the aeration amount of the upstream biochemical reaction and reduces the power consumption, it cannot solve the problem of treating small molecular organic matters in the wastewater after catalytic oxidation by ozone.
SUMMERY OF THE UTILITY MODEL
This patent aims at the not enough of prior art, provides a low energy consumption, high efficiency, and the waste water deep purification technology of economy and the biomembrane biochemical reaction system based on ozone can make waste water purification discharge to reach standard under lower energy consumption.
Namely, the energy consumption of ozone oxidation is reduced while the ring-opening chain-breaking rate is improved by improving the efficiency of ozone oxidation reaction; the ozone tail gas of the ozone catalytic oxidation process is effectively utilized and is treated by the low-energy-consumption decomposition reaction, the ozone tail gas is used as high-concentration oxygen to aerate the biological membrane biochemical reactor, the conventional biological membrane biochemical reactor is optimized to be an oxygen-enriched biological membrane biochemical reactor, the wastewater treatment effect is improved, and the wastewater treatment operation cost is reduced.
The utility model aims at providing a biomembrane biochemical reaction system based on ozone, the utility model provides a technical scheme as follows:
an ozone reactor which purifies wastewater by using ozone;
the oxygen-enriched aeration biological film biochemical reactor is communicated with the ozone generator and is used for carrying out deep purification treatment on the purified wastewater and discharging the wastewater;
the ozone decomposition reactor is respectively communicated with the ozone generator and the oxygen-enriched aeration biological membrane biochemical reactor and is used for decomposing the ozone which is not completely reacted after passing through the ozone reactor into oxygen.
In the technical scheme, ozone (the rest is oxygen) mixed gas enters an ozone reactor together with wastewater, aromatic hydrocarbon organic matters which are difficult to degrade in the wastewater are subjected to ring opening and chain breaking under the action of a catalyst in the ozone reactor to be decomposed into easily degradable organic matters, the wastewater after catalytic oxidation by ozone is discharged from the ozone reactor and then sent to an oxygen-enriched aeration biomembrane biochemical reactor for further biochemical treatment, and the Chemical Oxygen Demand (COD) of the purified wastewater reaches the standard and is discharged. The ozone tail gas which is not completely reacted in the ozone catalytic oxidation reactor is collected and enters the ozone decomposer, the ozone in the tail gas is decomposed into harmless oxygen, then the tail gas rich in oxygen is mixed with pressurized air after being pressurized by the tail gas conveying fan, and the mixture is conveyed to the oxygen-enriched aeration biological film biochemical reactor for aeration, so that the aeration quantity of air can be reduced, the energy consumption is reduced, the oxygen transfer rate of the oxygen-enriched aeration is high, and the biochemical efficiency of organic matters can be improved.
Preferably, the ozone reactor is communicated with an ozone generator, and the ozone generator is used for decomposing pure oxygen to generate a mixed gas of ozone and oxygen.
Preferably, the ozone reactor comprises: the reactor comprises a reactor shell, wherein an ozone distributor, a water inlet distributor, a flow guide support ring, a catalyst support plate, a catalyst layer and a catalyst press plate are sequentially arranged in the reactor shell from bottom to top.
In the technical scheme, pure oxygen is introduced into an ozone generator to generate mixed gas (ozone for short) of ozone and oxygen with the ozone concentration of 8-10%, the ozone is introduced into the bottom of the ozone reactor, and uniform aeration on the interface of the ozone reactor is achieved through an ozone distributor. The wastewater enters the lower part of the reactor and is uniformly distributed on the interface of the ozone reactor through the water inlet distributor, meanwhile, the entering wastewater enters the catalyst layer from bottom to top after being stirred and mixed by ozone aeration at the lower part, passes through the surface of the catalyst in a trickle mode, and on the surface of the catalyst, ozone not only directly oxidizes refractory organic matters to open the ring and break the chain, but also reacts with water to release a large amount of hydroxyl free radicals OH which can directly react with the organic matters in a water phase to degrade the organic matters and are converted into easily degradable short-chain organic matters, even end products of water and carbon dioxide.
Further, preferably, the lower surface of the diversion support ring is an inclined plane, forms an included angle of 120-160 degrees with the inner wall of the ozone reactor and is arranged along the inner wall of the ozone reactor in a circle.
In the technical scheme, the ozone gas close to the wall of the device passes through the inclined plane and then is guided into the catalyst layer, and does not form wall flow along the wall of the device.
Further, preferably, the catalyst supporting plate and the catalyst pressing plate are porous plates, the size of an opening is 2-8 mm, the loss of the catalyst is prevented, the loading amount of the catalyst is 30-70% of the volume of the ozone reactor, if the loading amount of the catalyst is less than 30%, the contact time of the wastewater and the catalyst is too short, and the reaction is incomplete. If the filling amount of the catalyst is higher than 70%, the resistance of the bed layer is increased, and the backwashing is not facilitated.
Preferably, the air outlet of the ozone reactor is communicated with the air inlet of a demister, the water outlet of the demister is communicated with the water return port of the ozone reactor, the air outlet of the demister is communicated with the air inlet of the ozone decomposition reactor, and the demister is used for removing free water.
In the technical scheme, the main component of tail gas after catalytic oxidation of ozone in the ozone reactor is oxygen, and in addition, the tail gas also contains a small amount of unreacted ozone and a small amount of free water, so that the tail gas is discharged out of the ozone reactor, firstly enters a demister to remove the free water, and then enters an ozone decomposer.
Preferably, the inside of the ozonolysis reactor is provided with: gas distributor, catalyst lower backup pad, ozonolysis catalyst layer, catalyst upper support plate.
In the technical scheme, the ozone tail gas for removing the free water mainly comprises oxygen and a small amount of unreacted ozone. Because ozone has a toxic effect on microorganisms, ozone in the ozone tail gas must be destroyed and decomposed into oxygen so as to enter biochemical utilization.
Ozone enters the ozone decomposition reactor, flows through the surface of the ozone decomposition catalyst through the gas distributor, and is decomposed into oxygen on the surface of the ozone decomposition catalyst.
The catalyst upper supporting plate and the catalyst lower supporting plate are preferably porous fixed pressing plates, so that the catalyst is prevented from running off.
Preferably, an air distribution pipe, a water distribution pipe and a biomembrane packing layer are sequentially arranged in the oxygen-enriched aeration biomembrane biochemical reactor from bottom to top;
the inlet of the air distribution pipe is communicated with an air supplement pipe.
In the technical scheme, oxygen decomposed from the ozone reactor is mixed with air introduced into the air supply pipe to form oxygen-enriched air. The wastewater after being oxidized and decomposed by ozone enters the oxygen-enriched aeration biological film biochemical reactor from the water distribution pipe, is uniformly mixed with the oxygen-enriched air, is contacted with a biological film filler filled in the oxygen-enriched aeration biological film biochemical reactor, is further subjected to deep biochemical degradation to form water and carbon dioxide, and is discharged after reaching the standard.
Preferably, the distance between the air distribution pipe and the bottom of the oxygen-enriched aeration biological membrane biochemical reactor is h1, the distance between the water distribution pipe and the air distribution pipe is h2, and the distance between the biological membrane filler layer and the bottom of the oxygen-enriched aeration biological membrane biochemical reactor is h 3; wherein h 1: h 2: h3 is (3-10): (2-5): (6-15); wherein h1 is preferably 300-1000 mm; h2 is preferably 200-500 mm; h3 is preferably 600-1500 mm; the water distribution pipe is arranged above the air distribution pipe, so that waste water can be rapidly mixed by utilizing air flow from the air distribution pipe, and the mass transfer efficiency is improved.
The filling proportion of the filler of the biomembrane filler layer is 30-50% of the tank volume, and the oxygen-enriched concentration in the air in the oxygen-enriched aeration biomembrane biochemical reactor is 23-28%.
In the technical scheme, the water distribution pipe is arranged above the air distribution pipe, so that waste water can be rapidly mixed by utilizing air flow coming out of the air distribution pipe, and the mass transfer efficiency is improved. If the filling proportion of the filler of the biomembrane filler layer is too low, the contact time of the wastewater and the biomembrane filler is short, the treatment effect is poor, the proportion is too high, and the sludge generated by the biomembrane filler is difficult to back flush.
If the oxygen-enriched concentration is too high and the aeration quantity is small, the mass transfer of gas-liquid mixture is not facilitated, otherwise, if the oxygen-enriched concentration is too low, the oxygen-enriched effect cannot be achieved. The COD volume load of the reactor can reach 2-3 kg/m3And d, the biochemical efficiency is higher than 90 percent.
Preferably, the air outlet of the ozone decomposition reactor is communicated with a dust collector, and the dust collector is communicated with the air distribution pipe.
In this technical scheme, the dust collector is arranged in getting rid of the dust in the gas after the purification to ensure the purity of the gas that lets in the gas distribution pipe, can not block up the gas distribution pipe, live time is longer.
The utility model provides a pair of biomembrane biochemical reaction system based on ozone can bring following at least one beneficial effect:
1) the utility model provides a low energy consumption, high efficiency, economic waste water deep purification device can make waste water purify and discharge to reach standard under lower energy consumption.
2) Efficient ozone oxidation: the lower part of the catalyst layer in the ozone catalytic reactor is provided with the flow guide support ring, so that the mixing uniformity and the mass transfer efficiency between gas phase and liquid phase are improved, the wall flow phenomenon of ozone gas is avoided, the loss of ozone is reduced, and the ozone utilization rate and the organic matter treatment efficiency are improved.
3) The normal temperature and pressure ozone destruction technology avoids tail gas heating and reduces the energy consumption of the ozone destruction device.
4) Ozone tail gas enters the fixed biological membrane biochemical reactor, so that dissolved oxygen is improved, the oxygen transfer rate, the biochemical reaction speed and the reaction efficiency are increased, the impact load resistance is high, and the energy consumption of blast aeration is reduced.
Drawings
The above features, technical features, advantages and modes of realisation of an ozone-based bio-membrane bio-chemical reaction system will be further described in the following, in a clearly understandable manner, with reference to the accompanying drawings, which illustrate preferred embodiments.
FIG. 1 is a schematic view of an ozone-based bio-membrane bio-chemical reaction apparatus according to the present invention;
the reference numbers illustrate:
the device comprises an ozone generator 1, an ozone reactor 2, a demister 3, an ozone decomposition reactor 4, an oxygen-enriched aeration biomembrane biochemical reactor 5, an ozone distributor 21, a water inlet distributor 22, a diversion support ring 23, a catalyst support plate 24, a catalyst layer 25, a catalyst press plate 26, a gas distribution pipe 61, a water distribution pipe 62, a gas supplementing pipe 63 and a biomembrane packing layer 64.
Detailed Description
In order to more clearly illustrate embodiments of the present invention or technical solutions in the prior art, specific embodiments of the present invention will be described below with reference to the accompanying drawings. It is obvious that the drawings in the following description are only examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be obtained from these drawings without inventive effort. For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure of the product.
Example 1
The utility model discloses a biomembrane biochemical reaction system based on ozone, as shown in figure 1, include:
an ozone reactor 2, wherein the ozone reactor 2 purifies the wastewater by using ozone;
the oxygen-enriched aeration biological film biochemical reactor 5 is communicated with the ozone generator 1, and the oxygen-enriched aeration biological film biochemical reactor 5 is used for carrying out deep purification treatment on the purified wastewater and discharging the wastewater;
the ozone decomposition reactor 4 is communicated with the ozone generator 1 and the oxygen-enriched aeration biomembrane biochemical reactor 5 respectively, and the ozone decomposition reactor 4 is used for decomposing the ozone which is not completely reacted after passing through the ozone reactor 2 into oxygen.
In this embodiment, the mixed gas of ozone (the rest is oxygen) and wastewater enter the ozone reactor 2 together, under the action of the catalyst in the ozone reactor 2, the non-degradable aromatic hydrocarbon organic matters in the wastewater are opened and broken into easily degradable organic matters, the wastewater after catalytic oxidation by ozone is discharged from the ozone reactor 2, and then sent to the oxygen-enriched aeration biomembrane biochemical reactor 5 for further biochemical treatment, and the purified wastewater reaches the Chemical Oxygen Demand (COD) and is discharged. The ozone tail gas that does not react completely in the ozone catalytic oxidation reactor is collected and is got into ozone decomposer, decomposes the ozone in the tail gas into harmless oxygen, then passes through tail gas conveying fan pressure boost with the pressurized air mixture with this strand of tail gas that is rich in oxygen, delivers to oxygen boosting aeration biomembrane biochemical reactor 5 aeration, not only can reduce the air aeration volume, reduces the energy consumption, and oxygen transfer rate of oxygen boosting aeration is fast simultaneously, can improve the biochemical efficiency of organic matter.
Example 2
As shown in FIG. 1, in this embodiment, in addition to embodiment 1, an ozone reactor 2 is connected to an ozone generator 1, and the ozone generator 1 is used for decomposing pure oxygen to generate a mixed gas of ozone and oxygen.
The ozone reactor 2 includes: the reactor comprises a reactor shell, wherein an ozone distributor 21, a water inlet distributor 22, a diversion support ring 23, a catalyst support plate 24, a catalyst layer 25 and a catalyst press plate 26 are sequentially arranged in the reactor shell from the bottom to the top.
The lower surface of the diversion support ring 23 is an inclined plane, forms an included angle of 120-160 degrees with the inner wall of the ozone reactor 2 and is arranged along the inner wall of the ozone reactor 2 in a circle. So that the ozone gas near the wall passes through the inclined surface and is guided to the inside of the catalyst layer 25 without flowing along the wall.
The catalyst supporting plate 24 and the catalyst pressing plate 26 are porous plates with the opening size of 2-8 mm, so that the loss of the catalyst is prevented, the loading amount of the catalyst is 30-70% of the volume of the ozone reactor 2, if the loading amount of the catalyst is less than 30%, the contact time of the wastewater and the catalyst is too short, and the reaction is incomplete. If the filling amount of the catalyst is higher than 70%, the resistance of the bed layer is increased, and the backwashing is not facilitated.
In this embodiment, pure oxygen is introduced into the ozone generator 1 to generate a mixed gas of ozone and oxygen (referred to as ozone for short) having an ozone concentration of 8 to 10%, and the ozone is introduced into the bottom of the ozone reactor 2 and passes through the ozone distributor 21 to achieve uniform aeration at the interface of the ozone reactor 2. The wastewater enters the lower part of the ozone reactor 2 and is uniformly distributed on the interface of the ozone reactor 2 through the water inlet distributor 22, meanwhile, the entered wastewater enters the catalyst layer 25 from bottom to top after being stirred and mixed by ozone aeration at the lower part, passes through the surface of the catalyst in a trickle mode, on the surface of the catalyst, ozone not only directly oxidizes the organic matters which are difficult to degrade to open the ring and break the chain, but also reacts with water to release a large amount of hydroxyl free radicals OH, which can directly react with the organic matters in a water phase to degrade the organic matters and convert the organic matters into short-chain organic matters which are easy to degrade, even into end products water and carbon dioxide.
Example 3
As shown in fig. 1, in this embodiment, in addition to embodiment 2, the air outlet of the ozone reactor 2 is communicated with the air inlet of the demister 3, the water outlet of the demister 3 is communicated with the water return port of the ozone reactor 2, the air outlet of the demister 3 is communicated with the air inlet of the ozone decomposition reactor 4, and the demister 3 is used for removing free water.
Specifically, the gas outlet of the ozonolysis reactor 4 is communicated with the dust collector, the dust collector is communicated with the gas distribution pipe 61, and the dust collector is used for removing dust in the purified gas, so that the purity of the gas introduced into the gas distribution pipe 61 is ensured, the gas distribution pipe 61 cannot be blocked, and the service life is longer.
In this embodiment, the main component of the tail gas after the catalytic oxidation reaction of ozone is oxygen, and in addition, the tail gas also contains a small amount of unreacted ozone and a small amount of free water, so that the tail gas is discharged from the ozone reactor 2, and then enters the demister 3 to remove the free water, and then enters the ozone decomposition reactor 4.
Example 4
As shown in fig. 1, in this embodiment, in addition to embodiment 1, the ozonolysis reactor 4 is provided with: the gas distributor, the catalyst lower support plate, the ozone decomposition catalyst layer 25, the catalyst upper support plate, and the apparatus structure is not shown in the figure. The ozone tail gas for removing the free water is mainly oxygen and a small amount of unreacted ozone. Because ozone has a toxic effect on microorganisms, ozone in the ozone tail gas must be destroyed and decomposed into oxygen so as to enter biochemical utilization.
In this embodiment, after entering the ozonolysis reactor 4, ozone flows through the surface of the ozonolysis catalyst through the gas distributor, and is decomposed into oxygen on the surface of the ozonolysis catalyst.
The catalyst upper supporting plate and the catalyst lower supporting plate are preferably porous fixed pressing plates, so that the catalyst is prevented from running off.
Example 5
As shown in fig. 1, in this embodiment, on the basis of embodiments 1 to 4, an air distribution pipe 61, a water distribution pipe 62, and a biomembrane packing layer 64 are sequentially disposed from the bottom to the top in the oxygen-enriched aeration biomembrane biochemical reactor 5, and an inlet of the air distribution pipe 61 is communicated with an outlet of the air supplement pipe 63.
In this embodiment, oxygen decomposed from the ozone reactor 2 is mixed with air introduced from the air make-up pipe 63 to be oxygen-enriched air. The wastewater after ozone oxidation and decomposition enters the oxygen-enriched aeration biomembrane biochemical reactor 5 from the water distribution pipe 62, is uniformly mixed with oxygen-enriched air, and then is contacted with the biomembrane packing layer 64, is further subjected to deep biochemical degradation to form water and carbon dioxide, and the wastewater reaches the discharge standard.
Example 6
As shown in fig. 1, in this embodiment, based on embodiment 5, the distance between the air distribution pipe 61 and the bottom of the oxygen-enriched aeration biomembrane biochemical reactor 5 is h1, the distance between the water distribution pipe 62 and the air distribution pipe 61 is h2, and the distance between the biomembrane packing layer 64 and the bottom of the oxygen-enriched aeration biomembrane biochemical reactor 5 is h 3; wherein h 1: h 2: h3 is (3-10): (2-5): (6-15); wherein h1 is preferably 300-1000 mm; h2 is preferably 200-500 mm; h3 is preferably 600-1500 mm; the water distribution pipe is arranged above the air distribution pipe, so that waste water can be rapidly mixed by utilizing air flow from the air distribution pipe, and the mass transfer efficiency is improved.
The filling proportion of the filler of the biomembrane filler layer 64 is 30-50% of the tank volume, if the filling proportion of the filler of the biomembrane filler layer is too low, the contact time of the wastewater and the biomembrane filler is short, the treatment effect is poor, the proportion is too high, and the sludge generated by the biomembrane filler is difficult to back flush. The oxygen-enriched concentration in the air in the oxygen-enriched aeration biomembrane biochemical reactor 5 is 23-28%, if the oxygen-enriched concentration is too high, the aeration quantity is small, the mass transfer of gas-liquid mixture is not facilitated, otherwise, if the oxygen-enriched concentration is too low, the oxygen-enriched effect cannot be achieved. The COD volume load of the reactor can reach 2-3 kg/m3/d, and the biochemical efficiency is higher than 90%.
Example 7
This example discloses the practical use of ozone catalytic oxidation in series with fixed biofilm biochemical reactor devices, as shown in fig. 1, the following treatments and the effects achieved in the process:
the inlet wastewater is two-stage biochemical oil refining wastewater, wherein the COD is 180 mg/L, the two-stage biochemical oil refining wastewater mainly comprises heterocyclic derivatives and polycyclic aromatic hydrocarbons, and the B/C ratio is 0.1.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 40 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 1.2h-1PH is 8, COD of the wastewater after reaction is 80 mg/L, B/C value is 0.62, and energy consumption is 1.28 kw/ton water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane advanced biochemical treatment, namely introducing the reacted wastewater into an oxygen-enriched aeration biological biochemical reactor to carry out oxygen-enriched aeration (oxygen enrichment is 25%) biochemical treatment, wherein the condition in the oxygen-enriched aeration biological biochemical reactor is that the dissolved oxygen in the water is 4.5 mg/L: 8, the COD value of the wastewater subjected to the advanced purification treatment is 18 mg/L, and the energy consumption per ton of water is 0.5 KWh.
Example 7 total energy consumption: 1.7804 KW/ton, COD degradation efficiency: 90%, ozone utilization ratio: greater than 90%.
Comparative example 1
Comparative example 1 is an apparatus used for conventional sewage treatment.
The inlet waste water is two sections of biochemical and petrochemical waste water, COD is 180 mg/L, the main components are heterocyclic derivatives and polycyclic aromatic hydrocarbons, and B/C is less than 0.1.
Ozone oxidation treatment, namely feeding 40 mg/L of ozone and wastewater into an ozone reactor 2 together, and setting the liquid hourly space velocity in the ozone reactor 2 at 1.2h-1PH is 8, COD value of the wastewater after reaction is 120 mg/L, B/C value is 0.48, and energy consumption is 1.6 kw/ton water.
And (3) tail gas ozone destruction treatment: the temperature in the reactor is set to 350 ℃, the pressure is micro-positive pressure (attached heat recovery device), 99% of inactivated tail gas ozone is discharged after reaching the standard (the concentration of the ozone is less than 0.1ppm), and the energy consumption per ton of water is 0.002 KWh.
And (3) biological membrane advanced biochemical treatment, namely introducing the reacted wastewater into the reactor for biological membrane advanced biochemical treatment, wherein the conventional biochemical condition of air aeration is that the dissolved oxygen in the water is 3 mg/L: 8, the COD value of the wastewater subjected to advanced purification treatment is 40 mg/L, and the energy consumption per ton of water is 0.7 KW.
Total energy consumption of comparative example 1: 2.302 KW/ton, COD degradation efficiency: 78%, ozone utilization: less than 30%.
As can be seen from the comparison of example 7 with comparative example 1, the total energy consumption of example 7 is significantly lower than that of comparative example 1, the degradation efficiency is higher, and the ozone utilization rate is also significantly increased.
Example 8
Example 8 is an embodiment of the present invention, as shown in fig. 1:
the inlet wastewater is two-stage biochemical oil refining wastewater, COD is 180 mg/L, the COD is mainly heterocyclic derivatives and polycyclic aromatic hydrocarbons, and B/C is 0.1.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 40 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 0.8h-1PH is 8, COD of the wastewater after reaction is 82 mg/L, B/C value is 0.60, and energy consumption is 1.28 kw/ton water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane deep biochemical treatment, namely introducing the reacted wastewater into the reactor for biological membrane deep biochemical treatment, wherein the conventional biochemical condition of air aeration is that the dissolved oxygen in the water is 5 mg/L: 8, the COD value of the wastewater subjected to deep purification treatment is 16 mg/L, and the energy consumption per ton of water is 0.5 KWh.
The embodiment has the following total energy consumption: 1.7804 KW/ton, COD degradation efficiency: 91%, ozone utilization rate: greater than 90%.
Example 9
Example 9 is an embodiment of the present invention, as shown in fig. 1:
the inlet wastewater is two-stage biochemical post-refining wastewater, COD is 120 mg/L, and the ratio of B/C is 0.05, wherein the COD is mainly heterocyclic compounds and polycyclic aromatic hydrocarbons.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 35 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 0.8h-1The PH value is 7.5, the COD of the waste water after the reaction is 67 mg/L, the B/C value is 0.59, and the energy consumption is 1.12 kw/ton water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane deep biochemical treatment, namely introducing the reacted wastewater into an oxygen-enriched aeration biological biochemical reactor to carry out oxygen-enriched aeration (oxygen enrichment is 26%), wherein the conditions in the oxygen-enriched aeration biological biochemical reactor are that the dissolved oxygen in the water is 5.5 mg/L: 7.5, the COD value of the wastewater subjected to deep purification treatment is 13 mg/L, and the energy consumption per ton of water is 0.48 KWh.
The embodiment has the following total energy consumption: 1.6004 KW/ton, COD degradation efficiency: 89%, ozone utilization ratio: greater than 90%.
Example 10
Example 10 is an embodiment of the present invention, as shown in fig. 1:
the inlet wastewater is two-stage biochemical post-refining wastewater, COD is 150 mg/L, and the ratio of B/C is 0.05, wherein the COD is mainly heterocyclic compounds and polycyclic aromatic hydrocarbons.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 50 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 0.8h-1The PH value is 7.5, the COD of the waste water after the reaction is 68 mg/L, the B/C value is 0.58, and the energy consumption is 1.6 kw/ton water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane advanced biochemical treatment, namely introducing the reacted wastewater into an oxygen-enriched aeration biological biochemical reactor to carry out oxygen-enriched aeration (oxygen enrichment of 27%) biochemical treatment, wherein the conditions in the oxygen-enriched aeration biological biochemical reactor are that the dissolved oxygen in the water is 6 mg/L: 7.5, the COD value of the wastewater subjected to the advanced purification treatment is 15 mg/L, and the energy consumption per ton of water is 0.46 KWh.
The embodiment has the following total energy consumption: 2.0604 KW/ton, COD degradation efficiency: 90%, ozone utilization ratio: greater than 90%.
Example 11
Example 11 is an embodiment of the present invention, as shown in fig. 1:
the inlet waste water is two-stage biochemical chemical waste water, COD is 120 mg/L, and is mainly heterocyclic compound, B/C is less than 0.1.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 35 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 0.8h-1The PH value is 7.5, the COD of the wastewater after the reaction is 50 mg/L, the B/C value is 0.70, and the energy consumption is 1.12 kw/ton of water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane advanced biochemical treatment, namely introducing the reacted wastewater into an oxygen-enriched aeration biological biochemical reactor to carry out oxygen-enriched aeration (oxygen enrichment is 26%), wherein the condition in the oxygen-enriched aeration biological biochemical reactor is that the dissolved oxygen in the water is 6 mg/L: 7.5, the COD value of the wastewater subjected to the advanced purification treatment is 8 mg/L, and the energy consumption per ton of water is 0.48 KWh.
The embodiment has the following total energy consumption: 1.6004 KW/ton, COD degradation efficiency: 93%, ozone utilization rate: greater than 90%.
Example 12
Example 12 is an embodiment of the present invention, as shown in fig. 1:
the inlet waste water is two-stage biochemical chemical waste water, COD is 120 mg/L, and is mainly heterocyclic compound, B/C is less than 0.1.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 30 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 0.8h-1The PH value is 8.5, the COD of the waste water after the reaction is 60 mg/L, the B/C value is 0.70, and the energy consumption is 0.96 kw/ton water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane advanced biochemical treatment, namely introducing the reacted wastewater into an oxygen-enriched aeration biological biochemical reactor to carry out oxygen-enriched aeration (oxygen enrichment is 24 percent) biochemical treatment, wherein the conditions in the oxygen-enriched aeration biological biochemical reactor are that the dissolved oxygen in the water is 4 mg/L: 8.5, the COD value of the wastewater subjected to the advanced purification treatment is 12 mg/L, and the energy consumption per ton of water is 0.5 KWh.
The embodiment has the following total energy consumption: 1.4604 KW/ton, COD degradation efficiency: 90%, ozone utilization ratio: greater than 90%.
Example 13
Example 13 is an embodiment of the present invention, as shown in fig. 1:
the inlet waste water is two-stage biochemical chemical waste water, COD is 150 mg/L, and is mainly heterocyclic compound, B/C is less than 0.1.
Ozone oxidation treatment, namely firstly generating 8-10% ozone in an ozone generator 1, then sending 40 mg/L ozone and wastewater into an ozone reactor 2 together, and setting the hourly space velocity of the liquid in the ozone reactor 2 at 0.5h-1The PH value is 8.5, the COD of the waste water after the reaction is 67 mg/L, the B/C value is 0.69, and the energy consumption is 1.28 kw/ton water.
And (3) tail gas ozone destruction treatment: the tail gas generated in the ozone reactor 2 is firstly introduced into a demister 3 for dewatering, then is introduced into an ozone decomposition reactor 4 for 99 percent inactivation at normal temperature and normal pressure, and then the inactivated ozone tail gas is introduced into an oxygen-enriched aeration biological biochemical reactor as an oxygen source, wherein the energy consumption per ton of water is 0.0004 KWh.
And (3) biological membrane advanced biochemical treatment, namely introducing the reacted wastewater into an oxygen-enriched aeration biological biochemical reactor to carry out oxygen-enriched aeration (oxygen enrichment is 26%), wherein the condition in the oxygen-enriched aeration biological biochemical reactor is that the dissolved oxygen in the water is 6 mg/L: 8.5, the COD value of the wastewater subjected to the advanced purification treatment is 13 mg/L, and the energy consumption per ton of water is 0.48 KWh.
The embodiment has the following total energy consumption: 1.7604 KW/ton, COD degradation efficiency: 91%, ozone utilization rate: greater than 90%.
It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (9)
1. An ozone-based biofilm biochemical reaction system, comprising:
an ozone reactor which purifies wastewater by using ozone;
the oxygen-enriched aeration biological membrane biochemical reactor is communicated with the ozone reactor and is used for carrying out deep purification treatment on the purified wastewater and discharging the wastewater;
the ozone decomposition reactor is respectively communicated with the ozone reactor and the oxygen-enriched aeration biological membrane biochemical reactor, and is used for decomposing the ozone which is not completely reacted after passing through the ozone reactor into oxygen.
2. The ozone-based biofilm biochemical reaction system of claim 1, wherein:
the ozone reactor is communicated with an ozone generator, and the ozone generator is used for decomposing pure oxygen to generate mixed gas of ozone and oxygen.
3. The ozone-based biofilm biochemical reaction system of claim 2, wherein said ozone reactor comprises:
the reactor comprises a reactor shell, wherein an ozone distributor, a water inlet distributor, a flow guide support ring, a catalyst support plate, a catalyst layer and a catalyst press plate are sequentially arranged in the reactor shell from bottom to top.
4. An ozone-based biofilm biochemical reaction system as recited in claim 3, wherein:
the diversion support ring is arranged along the inner wall of the ozone reactor in a circle, and the lower surface of the diversion support ring is an inclined surface and forms an included angle of 120-160 degrees with the inner wall of the ozone reactor;
the catalyst bearing plate and the catalyst pressing plate are porous plates, the size of each opening is 2-8 mm, and the loading amount of the catalyst is 30-70% of the volume of the ozone reactor.
5. An ozone-based biofilm biochemical reaction system as recited in claim 4, wherein:
the air outlet of the ozone reactor is communicated with the air inlet of a demister, the water outlet of the demister is communicated with the water return port of the ozone reactor, the air outlet of the demister is communicated with the air inlet of the ozone decomposition reactor, and the demister is used for removing free water.
6. The ozone-based biofilm biochemical reaction system of claim 1, wherein:
an air distribution pipe, a water distribution pipe and a biomembrane packing layer are sequentially arranged in the oxygen-enriched aeration biomembrane biochemical reactor from bottom to top;
and an air inlet of the air distribution pipe is communicated with an air supplement pipe.
7. An ozone-based biofilm biochemical reaction system as recited in claim 6, wherein:
the distance between the air distribution pipe and the bottom of the oxygen-enriched aeration biomembrane biochemical reactor is h1, the distance between the water distribution pipe and the air distribution pipe is h2, and the distance between the biomembrane filler layer and the bottom of the oxygen-enriched aeration biomembrane biochemical reactor is h 3; wherein h 1: h 2: h3 is 3-10: 2-5: 6-15.
8. An ozone-based biofilm biochemical reaction system as recited in claim 7, wherein:
and the gas outlet of the ozone decomposition reactor is communicated with a dust collector, and the dust collector is communicated with the gas distribution pipe.
9. An ozone-based biofilm biochemical reaction system as recited in claim 8, wherein:
the inside gas inlet of ozone decomposition reactor sets gradually to export: gas distributor, catalyst lower backup pad, ozonolysis catalyst layer, catalyst upper support plate.
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CN116903149A (en) * | 2023-06-09 | 2023-10-20 | 德威华泰科技股份有限公司 | Method for treating biochemical tail water by using biochemical and ozone oxidation coupling reactor device |
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