CN210795890U - Ozone catalytic oxidation moving bed reaction device - Google Patents
Ozone catalytic oxidation moving bed reaction device Download PDFInfo
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- CN210795890U CN210795890U CN201921822828.XU CN201921822828U CN210795890U CN 210795890 U CN210795890 U CN 210795890U CN 201921822828 U CN201921822828 U CN 201921822828U CN 210795890 U CN210795890 U CN 210795890U
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- reaction zone
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 113
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 33
- 230000003647 oxidation Effects 0.000 title claims abstract description 31
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 39
- 239000002351 wastewater Substances 0.000 claims abstract description 28
- 239000012159 carrier gas Substances 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000005192 partition Methods 0.000 claims abstract description 21
- 238000004891 communication Methods 0.000 claims abstract description 6
- 239000012530 fluid Substances 0.000 claims abstract description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 238000005273 aeration Methods 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 4
- 229910052723 transition metal Inorganic materials 0.000 claims description 4
- 150000003624 transition metals Chemical class 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 description 11
- 238000006385 ozonation reaction Methods 0.000 description 8
- 238000000034 method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 241001465754 Metazoa Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 230000001699 photocatalysis Effects 0.000 description 1
- 238000007146 photocatalysis Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model provides an ozone catalytic oxidation removes bed reaction unit, include: a reactor having a first reaction zone and a second reaction zone with a partition plate disposed therebetween, the partition plate being sized to place the first reaction zone and the second reaction zone in fluid communication on either side of the partition plate; the water inlet is arranged in a first reaction area of the reactor and used for conveying the wastewater to be treated to the first reaction area; the ozone inlet is arranged in the first reaction zone of the reactor and used for conveying ozone to the first reaction zone; the catalyst inlet is arranged in the second reaction zone of the reactor and conveys the catalyst to the second reaction zone; the carrier gas inlet is arranged in the second reaction area of the reactor and conveys the carrier gas to the second reaction area; wastewater entering the first reaction zone through the water inlet circularly flows between the first reaction zone and the second reaction zone and fully reacts with ozone and the catalyst.
Description
Technical Field
The utility model relates to an ozone catalytic oxidation removes bed reaction unit.
Background
Wastewater containing refractory organics is generated in heavy pollution industries such as steel, dye, chemical industry and the like, and pharmaceutical industry and the like. With the advance of industrialization in China, the discharge amount of refractory organic matters is increasingly increased. However, the conventional sewage treatment process using a biological treatment unit as a main body has difficulty in effectively removing these organic substances, and the entry of these organic substances into the environment undoubtedly poses a serious threat to the environment and the health of human and animals.
Advanced oxidation processes have gained increasing attention in recent years in order to address the problem of the disposal of refractory organics. The advanced oxidation method realizes the high-efficiency removal of refractory organic matters by generating strong oxidant hydroxyl free radicals, and the well-known photocatalysis, ozone, Fenton, electrocatalysis and the like belong to advanced oxidation methods.
The single use of ozone for oxidation has limitations, low solubility of ozone in water, poor mass transfer effect, limited ozone oxidation capacity, large ozone adding amount required for oxidizing refractory organic matters, high operation cost and inapplicability in engineering. In addition, the ozone oxidation has selectivity, the removal efficiency of the ozone oxidation is different from that of organic matters, and particularly, the ozone oxidation has poor removal effect on organic matters such as alkane.
Ozone and a catalyst are combined for catalytic oxidation of ozone, so that the ozone addition amount can be reduced while the ozone oxidation capacity is improved, and the removal rate of Chemical Oxygen Demand (COD) is ensured. In addition, the ozone catalytic oxidation oxidizes organic matters by generating hydroxyl radical, so that the reaction rate is high and the selectivity is low. Unlike conventional ozone oxidation and ozone oxidation using radicals (such as O3/H2O2 or O3/UV), the effect of the ozone catalytic oxidation reaction depends on the activity of the catalyst, and is not affected by the inhibitory effect of compounds capable of capturing radicals, which are generally present in industrial wastewater, so that the effect of the quality of water to be treated on the oxidation effect is also relatively small.
SUMMERY OF THE UTILITY MODEL
The utility model provides an ozone catalytic oxidation removes bed reaction unit, include: a reactor having a first reaction zone and a second reaction zone with a partition plate disposed therebetween, the partition plate being sized to place the first reaction zone and the second reaction zone in fluid communication on either side of the partition plate; the water inlet is arranged in a first reaction area of the reactor and used for conveying the wastewater to be treated to the first reaction area; the ozone inlet is arranged in the first reaction zone of the reactor and used for conveying ozone to the first reaction zone; the catalyst inlet is arranged in the second reaction zone of the reactor and conveys the catalyst to the second reaction zone; and the carrier gas inlet is arranged in the second reaction area of the reactor, the carrier gas is conveyed to the second reaction area, and the wastewater entering the first reaction area through the water inlet circularly flows between the first reaction area and the second reaction area and fully reacts with the ozone and the catalyst.
Advantageously, the water inlet and the ozone inlet are positioned in the first reaction zone such that the flow direction of the wastewater and the flow direction of the ozone are opposite to each other to bring the wastewater into sufficient contact with the ozone.
Advantageously, the reaction device further comprises an ozone diffuser disposed in the first reaction zone and connected to the ozone inlet.
Advantageously, the reaction device further comprises a carrier gas diffuser disposed in the second reaction zone and connected to the carrier gas inlet.
Advantageously, the reaction apparatus further comprises a water discharge port provided in the second reaction zone, and a liquid-solid separation device through which water discharged through the water discharge port passes, the liquid-solid separation device being connected to the catalyst inlet so that the separated catalyst again enters the second reaction zone through the catalyst inlet.
Advantageously, the reaction apparatus further comprises an exhaust port connected to the carrier gas inlet port such that a portion of the gas exhausted through the exhaust port enters the second reaction zone again through the carrier gas inlet port.
Advantageously, the ozone diffuser is an aeration tray.
Advantageously, the carrier gas diffuser is an aeration tray.
Advantageously, the catalyst is supported on silica or granular activated carbon or activated carbon alumina and comprises at least transition metals such as cobalt and copper.
Drawings
The advantages and objects of the present invention will be better understood from the following detailed description of the preferred embodiments of the invention, taken in conjunction with the accompanying drawings. The drawings are not necessarily to scale, emphasis instead being placed upon illustrating the relationship of the various components. In the drawings:
figure 1 shows a schematic view of an ozone catalytic oxidation moving bed reactor according to the present invention.
Fig. 2 shows the effect of removing COD by the catalytic ozonation moving bed reactor according to the present invention, compared with ozonation.
Figure 3 shows the application of the catalytic ozonation moving bed reactor according to the present invention in various industries, compared to ozonation.
Figure 4 shows the amount of ozone transferred when a given COD removal rate is achieved for various industrial applications according to the present invention of an ozone catalytic oxidation moving bed reactor.
Fig. 5 shows a schematic view of an alternative embodiment.
Detailed Description
Various embodiments according to the present invention will be described in detail with reference to the accompanying drawings. Here, it is to be noted that, in the drawings, the same reference numerals are given to constituent parts having substantially the same or similar structures and functions, and repeated description thereof will be omitted. The term "sequentially comprising A, B, C, etc" merely indicates the order of the included elements A, B, C, etc. and does not exclude the possibility of including other elements between a and B and/or between B and C.
The drawings in the present specification are schematic views to assist in explaining the concept of the present invention, and schematically show the shapes of the respective portions and the mutual relationships thereof.
Figure 1 shows a schematic view of an ozone catalytic oxidation moving bed reactor according to the present invention. The reaction device comprises a reactor 1, a water inlet 2, an ozone inlet 11, a catalyst inlet 13 and a carrier gas inlet 9. The reactor 1 is divided into a first reaction zone 5 and a second reaction zone 4, and a partition plate 6 is disposed between the first reaction zone 5 and the second reaction zone 4. As shown in fig. 1, the partition plate partially partitions the first reaction zone and the second reaction zone such that the first reaction zone and the second reaction zone are in fluid communication on both sides of the partition plate, i.e., the partition plate is sized such that the first reaction zone and the second reaction zone are in fluid communication on both sides of the partition plate. In this embodiment, the separator plate is vertically positioned so that the first reaction zone is located on the left side of the separator plate and the second reaction zone is located on the right side of the separator plate, the first and second reaction zones being in fluid communication at the top and bottom of the separator plate.
The water inlet 2 is disposed at the upper portion of the first reaction zone 5, the ozone inlet 11 is disposed at the lower portion of the first reaction zone, and the ozone inlet 11 is connected to an ozone diffuser 10 (e.g., an aeration tray). Thus, the ozone enters the ozone diffuser 10 through the ozone inlet 11, then flows upward uniformly in the form of micro bubbles (which is advantageous for increasing the effective contact area of ozone with wastewater), enters the wastewater at the upper part of the first reaction zone through the water inlet, flows downward, and makes the wastewater and ozone fully contact and react through the reverse flow of wastewater and ozone.
In the second reaction zone, a carrier gas inlet 9 and a catalyst inlet 13 are provided at the lower portion of the second reaction zone, and the carrier gas inlet 9 is further connected to a carrier gas diffuser 8 (e.g., an aeration tray) to diffuse the carrier gas upward, thereby causing the catalyst to form a homogeneous suspension 7 in the second reaction zone. The catalyst takes silicon dioxide or granular activated carbon or activated carbon alumina as a carrier and at least comprises transition metals such as cobalt, copper and the like.
The exhaust port 16 of the reaction device is arranged at the top, and the exhaust port is connected with the ozone destructor 15 on one hand and the carrier gas inlet 9 on the other hand, so that the gas (containing oxygen and ozone) exhausted from the reaction device is converted into oxygen through the ozone destructor and is exhausted, and enters the second reaction area again through the carrier gas inlet 9 on the other hand, the cyclic utilization is realized, and the gas consumption is reduced.
A drain port 3 is also provided at the upper portion of the second reaction zone to drain the treated water (containing water and catalyst). The drain is connected to a liquid-solid separator 12 to separate the catalyst from the drain, and the separated clarified water can be subjected to further processing. The separated catalyst can enter the catalyst inlet again to realize recycling and reduce the consumption of the catalyst.
The operation of the reaction apparatus is described below.
Wastewater enters the first reaction zone through the water inlet and flows downward under the action of gravity. Ozone produced by an ozone generator (not shown) enters the lower portion of the first reaction zone through an ozone inlet and flows uniformly upward through an ozone diffuser, sufficiently contacting the wastewater. The wastewater flows downwards in the first reaction zone, and after reaching the bottom, the wastewater carries ozone to flow below the partition plate and enter the second reaction zone.
The wastewater and ozone flow upward in the second reaction zone. The catalyst enters the lower part of the second reaction zone through the catalyst inlet, the carrier gas enters the lower part of the second reaction zone through the carrier gas inlet, and the catalyst is uniformly mixed into the wastewater under the action of the carrier gas to form catalyst suspension. The wastewater, ozone and the catalyst flow upward together in the second reaction zone, and the catalytic oxidation reaction is fully performed. And one part of water after reaction enters the liquid-solid separator from the water discharge port, the separated catalyst enters the second reaction zone through the catalyst inlet again, and the other part of water after reaction continues to flow upwards and flows into the first reaction zone again when the horizontal plane exceeds the top of the partition plate. In this way, the wastewater flows downward in the first reaction zone and upward in the second reaction zone, constituting a circulation.
According to the utility model discloses an ozone catalytic oxidation compares with traditional ozone oxidation, and the effect of getting rid of the COD is shown as figure 2, can find out from this:
the catalytic ozonation according to the present invention can significantly improve the removal rate of COD, and moreover, with the same COD removal amount, it consumes less ozone and takes less time than the ozone oxidation alone;
conventional ozone oxidation may no longer work in the second stage, while the catalytic ozone oxidation process still shows significant treatment effects in the second stage.
According to the utility model discloses an ozone catalytic oxidation can the wide application in the processing of different industrial waste water, reaches the purpose of high-efficient oxidation. Fig. 3 shows the degradation effect of the organic acid on garbage percolate, waste water in the cosmetics industry, waste water in the automobile industry and waste water in the food industry. In addition, figure 4 table shows that compared with traditional ozone oxidation, reach the given COD removal rate required ozone amount. As can be seen from FIGS. 3 and 4, the catalytic ozonation according to the present invention is superior to the conventional ozonation in oxygen consumption, degradation effect, etc.
In the above embodiment, the partition plates are placed in the vertical direction, but it should be understood that the partition plates may also extend laterally in the reaction apparatus, as schematically shown in fig. 5, and the number of the partition plates is not limited to 1, and a plurality of partition plates may be provided so as to form a plurality of reaction zones for allowing the wastewater, ozone, and catalyst to react sufficiently.
The catalytic ozonation moving bed reactor according to the utility model has the advantages that:
make up for the deficiency of ozone oxidation in wastewater treatment, improve the removal efficiency of COD and reduce the consumption of ozone at the same time;
the carrier gas and the catalyst are recycled, so that the gas consumption and the catalyst consumption are reduced;
the catalyst in the moving bed reactor exists in a suspended state and can be fully contacted with wastewater and ozone.
The technical features disclosed above are not limited to the combinations with other features disclosed, and other combinations between the technical features can be performed by those skilled in the art according to the purpose of the invention to achieve the aim of the invention.
Claims (10)
1. An ozone catalytic oxidation moving bed reaction unit, characterized in that, the reaction unit includes:
a reactor having a first reaction zone and a second reaction zone with a partition plate disposed therebetween, the partition plate being sized to place the first reaction zone and the second reaction zone in fluid communication on either side of the partition plate;
the water inlet is arranged in a first reaction area of the reactor and used for conveying the wastewater to be treated to the first reaction area;
the ozone inlet is arranged in the first reaction zone of the reactor and used for conveying ozone to the first reaction zone;
the catalyst inlet is arranged in the second reaction zone of the reactor and conveys the catalyst to the second reaction zone;
the carrier gas inlet is arranged in the second reaction area of the reactor and conveys the carrier gas to the second reaction area;
wastewater entering the first reaction zone through the water inlet circularly flows between the first reaction zone and the second reaction zone and fully reacts with ozone and the catalyst.
2. The reaction device of claim 1, wherein the water inlet and the ozone inlet are positioned at a position of the first reaction zone such that a flow direction of the wastewater and a flow direction of the ozone are opposite to each other to allow the wastewater to be sufficiently contacted with the ozone.
3. The reactor apparatus of claim 1, further comprising an ozone diffuser disposed in the first reaction zone and connected to the ozone inlet.
4. The reactor of claim 1, further comprising a carrier gas diffuser disposed in the second reaction zone and connected to the carrier gas inlet.
5. The reactor according to claim 1, further comprising a water discharge port provided in the second reaction zone and a liquid-solid separation device through which water discharged through the water discharge port passes, the liquid-solid separation device being connected to the catalyst inlet so that the separated catalyst is again introduced into the second reaction zone through the catalyst inlet.
6. The reaction device of claim 1, further comprising an exhaust port connected to the carrier gas inlet port such that a portion of the gas exhausted through the exhaust port enters the second reaction zone again through the carrier gas inlet port.
7. The reaction device of claim 3 wherein said ozone diffuser is an aeration tray.
8. The reactor of claim 4, wherein said carrier gas diffuser is an aeration tray.
9. The reactor apparatus of claim 1, wherein the catalyst is supported on silica or granular activated carbon or activated alumina and contains at least a transition metal.
10. The reactor apparatus of claim 9 wherein the transition metal is cobalt or copper.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921822828.XU CN210795890U (en) | 2019-10-28 | 2019-10-28 | Ozone catalytic oxidation moving bed reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921822828.XU CN210795890U (en) | 2019-10-28 | 2019-10-28 | Ozone catalytic oxidation moving bed reaction device |
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| Publication Number | Publication Date |
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| CN210795890U true CN210795890U (en) | 2020-06-19 |
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| CN201921822828.XU Active CN210795890U (en) | 2019-10-28 | 2019-10-28 | Ozone catalytic oxidation moving bed reaction device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114940552A (en) * | 2022-06-28 | 2022-08-26 | 电子科技大学中山学院 | Countercurrent aeration internal circulation coupling precipitation separation ozone oxidation reactor |
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2019
- 2019-10-28 CN CN201921822828.XU patent/CN210795890U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114940552A (en) * | 2022-06-28 | 2022-08-26 | 电子科技大学中山学院 | Countercurrent aeration internal circulation coupling precipitation separation ozone oxidation reactor |
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Address after: 3101, 27th Floor, Building 1, Yard 38, East 3rd Ring North Road, Chaoyang District, Beijing, 100026 Patentee after: Suez Environmental Technology (Beijing) Co.,Ltd. Address before: 100026 31 / F, Taikang financial building, building 1, courtyard 38, East Third Ring Road North, Chaoyang District, Beijing Patentee before: Suez Water Treatment Co,.Ltd. |