CN211445356U - Coking wastewater ozone catalytic oxidation advanced treatment unit - Google Patents
Coking wastewater ozone catalytic oxidation advanced treatment unit Download PDFInfo
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- CN211445356U CN211445356U CN201921452956.XU CN201921452956U CN211445356U CN 211445356 U CN211445356 U CN 211445356U CN 201921452956 U CN201921452956 U CN 201921452956U CN 211445356 U CN211445356 U CN 211445356U
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 89
- 239000002351 wastewater Substances 0.000 title claims abstract description 58
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 43
- 238000004939 coking Methods 0.000 title claims abstract description 38
- 230000003647 oxidation Effects 0.000 title claims abstract description 37
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000006243 chemical reaction Methods 0.000 claims abstract description 60
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 238000002347 injection Methods 0.000 claims abstract description 10
- 239000007924 injection Substances 0.000 claims abstract description 10
- 239000000945 filler Substances 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 14
- 239000002245 particle Substances 0.000 claims description 8
- 239000012798 spherical particle Substances 0.000 claims description 8
- 239000004927 clay Substances 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000005245 sintering Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Inorganic materials [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 230000008092 positive effect Effects 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000004925 denaturation Methods 0.000 description 1
- 230000036425 denaturation Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 150000002391 heterocyclic compounds Chemical class 0.000 description 1
- 231100000219 mutagenic Toxicity 0.000 description 1
- 230000003505 mutagenic effect Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Abstract
The utility model relates to a coking wastewater ozone catalytic oxidation advanced treatment unit. The technical scheme is as follows: the processing device is structured as follows: the wastewater delivery water pump (1) is sequentially connected with the first valve (2), the flowmeter (3), the Venturi tube (5), the second valve (6) and the inlet of the wastewater injection pipe (7) through a water pipe, and the throat of the Venturi tube (5) is connected with an ozone generator (4); a wastewater injection pipe (7), a first water distribution plate (8), a first reaction zone (9), a second water distribution plate (10), an ultraviolet lamp (11), a second reaction zone (12), a water outlet weir (13) and a demister (14) are sequentially arranged in a tower body of the ozone reaction tower (15) from bottom to top; the upper part of the ozone reaction tower (15) is provided with a water outlet pipe which is positioned at the bottom of the water outlet weir (13); the tail gas hole at the top of the ozone reaction tower (15) is connected with an ozone destructor (16) through a pipeline. The utility model discloses the catalyst quantity is few, ozone oxidation is efficient, simple structure and running cost are low.
Description
Technical Field
The utility model belongs to the technical field of coking wastewater treatment device. In particular to a coking wastewater ozone catalytic oxidation advanced treatment device.
Background
Coking wastewater is high-concentration organic wastewater generated in the processes of high-temperature dry distillation of coal, recovery of chemical products and refining. The phenol pollutants in the coking wastewater can cause protein denaturation, and the polycyclic aromatic hydrocarbon and the heterocyclic compounds in the wastewater are considered to be carcinogenic and mutagenic substances, and if discharged into a water body, the substances are accumulated in aquatic organisms and enter human bodies through food chains, so that great harm is caused to the health of human bodies. Therefore, in order to protect the natural ecological environment and human health and promote the economic sustainable development, the coking wastewater must be subjected to advanced treatment.
At present, the process of 'pretreatment + biological denitrification + coagulating sedimentation' commonly adopted by coking enterprises is difficult to meet the new national emission requirements, so that the advanced oxidation technology represented by ozone oxidation is rapidly developed and is largely used for the advanced treatment of coking wastewater. The coking wastewater is pretreated and biochemically treated, then is subjected to catalytic oxidation by ozone, and organic pollutants in the wastewater are deeply treated by utilizing the strong oxidizing property of the ozone, so that toxic organic matters in the wastewater can be eliminated and the COD in the wastewater can be reduced. The device changes the common method that the ozone oxidation tower enters water from one side of the tower, improves the gas-water distribution and contact effect, but the oxidation tower is only filled with a section of filler and mainly plays a role in directly oxidizing ozone; also such as a novel ozone oxidation tower (CN207748905U), the device adopts a spiral spray head and a water injector to improve gas-liquid distribution and gas-liquid contact effect, but the device is only filled with a section of filler, and the device still has direct oxidation of ozone; the ozone catalytic oxidation tower type reaction device (CN208776381U) is filled with a section of catalyst and is provided with a circulating water pump, the flow speed of water in a tower body is improved through the circulation of the water, the oxidation efficiency is improved, and the indirect oxidation effect of the catalyst is mainly exerted. In the above technologies, the ozone oxidation tower is only filled with common fillers, so that the oxidation capacity is limited and the requirements of advanced treatment are difficult to meet; or only the catalyst is filled, the catalyst filling bed layer is high, the catalyst usage amount is large, and the cost is high.
Disclosure of Invention
The utility model aims to overcome the defects existing in the prior art, and aims to provide a coking wastewater ozone catalytic oxidation advanced treatment device with less catalyst consumption, simple and compact structure and low operation cost.
In order to achieve the above object, the utility model adopts the following technical scheme: the coking wastewater ozone catalytic oxidation advanced treatment device consists of an ozone generator, a gas-liquid mixing system, an ozone reaction tower and an ozone destructor.
A wastewater injection pipe, a first water distribution plate, a first reaction zone, a second water distribution plate, an ultraviolet lamp, a second reaction zone, a water outlet weir and a demister are sequentially arranged in the tower body of the ozone reaction tower from bottom to top; the upper part of the ozone reaction tower is provided with a water outlet pipe which is positioned at the bottom of the water outlet weir; the top of the ozone reaction tower is provided with a tail gas hole.
The height of the filler in the first reaction zone is 2-3 m, the filler in the first reaction zone is water treatment ceramsite, and the water treatment ceramsite is spherical particles with the particle size of 3-6 mm; the height of the filler in the second reaction zone is 3-5 m, the filler in the second reaction zone is a ceramsite catalyst, and the ceramsite catalyst is spherical particles with the particle size of 3-5 mm.
The gas-liquid mixing system is as follows: the inlet of the wastewater delivery water pump is communicated with the outlet of the coking wastewater through a water pipe, and the outlet of the wastewater delivery water pump is sequentially connected with the outlets of the first valve, the flowmeter, the venturi tube and the second valve through water pipes.
The processing device is structured as follows: the throat of the Venturi tube in the gas-liquid mixing system is connected with an ozone generator; the outlet of the second valve in the gas-liquid mixing system is connected with the inlet of a waste water injection pipe of the ozone reaction tower, and the tail gas hole at the top of the ozone reaction tower is connected with the ozone destructor through a pipeline.
The first water distribution plate is uniformly provided with filter heads, the center distance between the filter heads is 100-120 mm, and the inner diameter of each filter head is 30-50 mm; the first water distribution plate and the second water distribution plate are the same.
The water treatment ceramsite is prepared by granulating, drying and sintering clay.
The ceramsite catalyst is as follows: mixing 35-55 wt% of fly ash, 40-60 wt% of clay and 3-6 wt% of active component, granulating, drying, and sintering at 1000-1080 ℃; the active component is Mn (NO)3)2、Cu(NO3)2More than one of them.
Due to the adoption of the technical scheme, compared with the prior art, the utility model, have following advantage and positive effect:
(1) the device utilizes a conveying water pump 1 to enable coking wastewater to flow through a first valve 2, a flowmeter 3 and a Venturi tube 5, then utilizes vacuum generated by the Venturi tube 5 at a throat to suck ozone, the coking wastewater sucked with the ozone enters a first water distribution plate 8 after being mixed with water through a second valve 6 and a wastewater injection pipe 7, the mixture is uniformly distributed through a filter head, the mixed coking wastewater and the ozone are subjected to ozone oxidation reaction in a first reaction zone 9, the reacted coking wastewater enters a second reaction zone 12 through a second water distribution plate 10, the reacted coking wastewater and a ceramsite catalyst filled in the second reaction zone 12 are subjected to ozone catalytic oxidation reaction, the ozone catalytic oxidation reaction time is 30-50 min, the reacted effluent is discharged through an effluent weir 13, unreacted ozone tail gas is decomposed and harmlessly generated through an ozone destructor 16, and the ozone oxidation efficiency is high.
(2) The device arranges the first reaction zone 9, the second reaction zone 12 and the ultraviolet lamp 11 in an ozone reaction tower 15, and has simple and compact structure and low capital investment.
(3) The device sequentially carries out direct oxidation of ozone and ultraviolet light-assisted catalytic oxidation on the coking wastewater in an ozone reaction tower 15, the ozone utilization rate is higher due to the fact that the direct oxidation of the ozone is firstly utilized and then the ultraviolet light-assisted catalytic oxidation is utilized, the catalyst dosage can be saved by at least 20%, and the operation cost is low.
(4) The device removes most organic matters in the coking wastewater after the coking wastewater is directly oxidized by ozone, generates intermediate products and residual organic matters which are difficult to decompose, and then the coking wastewater is oxidized more thoroughly under the catalytic action of the catalyst through catalytic oxidation of the ozone, so that the COD in the effluent is lower.
Therefore, the utility model has the characteristics of catalyst quantity is few, ozone oxidation is efficient, simple structure is compact and the running cost is low.
Drawings
Fig. 1 is a schematic structural view of the present invention;
fig. 2 is an enlarged schematic view of a structure of the water distribution plate 8 in fig. 1.
Detailed Description
The invention will be described in further detail with reference to the following drawings and specific embodiments, without limiting the scope of the invention.
Example 1
An ozone catalytic oxidation advanced treatment device for coking wastewater. As shown in fig. 1, the treatment apparatus is composed of an ozone generator 4, a gas-liquid mixing system, an ozone reaction tower 15, and an ozone destructor 16.
As shown in fig. 1, a wastewater injection pipe 7, a first water distribution plate 8, a first reaction zone 9, a second water distribution plate 10, an ultraviolet lamp 11, a second reaction zone 12, a water outlet weir 13 and a demister 14 are sequentially arranged in the tower body of the ozone reaction tower 15 from bottom to top; the upper part of the ozone reaction tower 15 is provided with a water outlet pipe which is positioned at the bottom of the water outlet weir 13; the top of the ozone reaction tower 15 is provided with a tail gas hole.
As shown in FIG. 1, the height of the filler in the first reaction zone 9 is 2-2.5 m, the filler in the first reaction zone 9 is water-treated ceramsite, and the water-treated ceramsite is spherical particles with the particle size of 3-5 mm; the height of the filler in the second reaction zone 12 is 3-4 m, the filler in the second reaction zone 12 is a ceramsite catalyst, and the ceramsite catalyst is spherical particles with the particle size of 3-4 mm.
As shown in fig. 1, the gas-liquid mixing system is: the inlet of the wastewater conveying water pump 1 is communicated with the outlet of the coking wastewater through a water pipe, and the outlet of the wastewater conveying water pump 1 is sequentially connected with the outlets of the first valve 2, the flowmeter 3, the Venturi tube 5 and the second valve 6 through water pipes.
As shown in fig. 1, the processing apparatus has a structure in which: the throat of the Venturi tube 5 in the gas-liquid mixing system is connected with an ozone generator 4; the outlet of the second valve 6 in the gas-liquid mixing system is connected with the inlet of the waste water injection pipe 7 of the ozone reaction tower 15, and the tail gas hole at the top of the ozone reaction tower 15 is connected with the ozone destructor 16 through a pipeline.
As shown in fig. 2, the first water distribution plate 8 is uniformly provided with filter heads, the center distance between the filter heads is 100-110 mm, and the inner diameter of the filter heads is 30-40 mm; the first water distribution plate 8 and the second water distribution plate 10 are the same.
The water treatment ceramsite is prepared by granulating, drying and sintering clay.
The ceramsite catalyst is as follows: mixing 35-55 wt% of fly ash, 40-60 wt% of clay and 3-6 wt% of active component, granulating, drying, and sintering at 1000-1080 ℃; the active component is Mn (NO)3)2、Cu(NO3)2More than one of them.
Example 2
An ozone catalytic oxidation advanced treatment device for coking wastewater. The procedure is as in example 1, except for the following parameters:
the height of the filler in the first reaction zone 9 is 2.5-3 m, the filler in the first reaction zone 9 is water treatment ceramsite, and the water treatment ceramsite is spherical particles with the particle size of 4-6 mm;
the height of the filler in the second reaction zone 12 is 4-5 m, the filler in the second reaction zone 12 is a ceramsite catalyst, and the ceramsite catalyst is spherical particles with the particle size of 4-5 mm.
The first water distribution plate 8 is uniformly provided with filter heads, the center distance between the filter heads is 110-120 mm, and the inner diameter of each filter head is 40-50 mm.
Compared with the prior art, the specific implementation mode has the following advantages and positive effects:
(1) the device utilizes a conveying water pump 1 to enable coking wastewater to flow through a first valve 2, a flowmeter 3 and a Venturi tube 5, then utilizes vacuum generated by the Venturi tube 5 at a throat to suck ozone, the coking wastewater sucked with the ozone enters a first water distribution plate 8 after being mixed with water through a second valve 6 and a wastewater injection pipe 7, the mixture is uniformly distributed through a filter head, the mixed coking wastewater and the ozone are subjected to ozone oxidation reaction in a first reaction zone 9, the reacted coking wastewater enters a second reaction zone 12 through a second water distribution plate 10, the reacted coking wastewater and a ceramsite catalyst filled in the second reaction zone 12 are subjected to ozone catalytic oxidation reaction, the ozone catalytic oxidation reaction time is 30-50 min, the reacted effluent is discharged through an effluent weir 13, unreacted ozone tail gas is decomposed and harmlessly generated through an ozone destructor 16, and the ozone oxidation efficiency is high.
(2) The device arranges the first reaction zone 9, the second reaction zone 12 and the ultraviolet lamp 11 in an ozone reaction tower 15, and has simple and compact structure and low capital investment.
(3) The device sequentially carries out direct oxidation of ozone and ultraviolet light-assisted catalytic oxidation on the coking wastewater in an ozone reaction tower 15, the ozone utilization rate is higher due to the fact that the direct oxidation of the ozone is firstly utilized and then the ultraviolet light-assisted catalytic oxidation is utilized, the catalyst dosage can be saved by at least 20%, and the operation cost is low.
(4) The device removes most organic matters in the coking wastewater after the coking wastewater is directly oxidized by ozone, generates intermediate products and residual organic matters which are difficult to decompose, and then the coking wastewater is oxidized more thoroughly under the catalytic action of the catalyst through catalytic oxidation of the ozone, so that the COD in the effluent is lower.
Therefore, the specific embodiment has the characteristics of less catalyst consumption, high ozone oxidation efficiency, simple and compact structure and low operation cost.
Claims (2)
1. The coking wastewater ozone catalytic oxidation advanced treatment device is characterized in that the treatment device consists of an ozone generator (4), a gas-liquid mixing system, an ozone reaction tower (15) and an ozone destructor (16);
a wastewater injection pipe (7), a first water distribution plate (8), a first reaction zone (9), a second water distribution plate (10), an ultraviolet lamp (11), a second reaction zone (12), a water outlet weir (13) and a demister (14) are sequentially arranged in the tower body of the ozone reaction tower (15) from bottom to top; the upper part of the ozone reaction tower (15) is provided with a water outlet pipe which is positioned at the bottom of the water outlet weir (13); the top of the ozone reaction tower (15) is provided with a tail gas hole;
the height of the filler in the first reaction zone (9) is 2-3 m, the filler in the first reaction zone (9) is water treatment ceramsite, and the water treatment ceramsite is spherical particles with the particle size of 3-6 mm; the height of the filler in the second reaction zone (12) is 3-5 m, the filler in the second reaction zone (12) is a ceramsite catalyst, and the ceramsite catalyst is spherical particles with the particle size of 3-5 mm;
the gas-liquid mixing system is as follows: an inlet of the wastewater conveying water pump (1) is communicated with an outlet of coking wastewater through a water pipe, and an outlet of the wastewater conveying water pump (1) is sequentially connected with outlets of the first valve (2), the flowmeter (3), the Venturi tube (5) and the second valve (6) through water pipes;
the processing device is structured as follows: the throat of a Venturi tube (5) in the gas-liquid mixing system is connected with an ozone generator (4); the outlet of the second valve (6) in the gas-liquid mixing system is connected with the inlet of the waste water injection pipe (7) of the ozone reaction tower (15), and the tail gas hole at the top of the ozone reaction tower (15) is connected with the ozone destructor (16) through a pipeline.
2. The coking wastewater ozone catalytic oxidation advanced treatment unit according to claim 1, characterized in that the first water distribution plate (8) is uniformly provided with filter heads, the center distance between the filter heads is 100-120 mm, and the inner diameter of the filter heads is 30-50 mm; the first water distribution plate (8) and the second water distribution plate (10) are the same.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921452956.XU CN211445356U (en) | 2019-09-03 | 2019-09-03 | Coking wastewater ozone catalytic oxidation advanced treatment unit |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921452956.XU CN211445356U (en) | 2019-09-03 | 2019-09-03 | Coking wastewater ozone catalytic oxidation advanced treatment unit |
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| CN211445356U true CN211445356U (en) | 2020-09-08 |
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| CN201921452956.XU Expired - Fee Related CN211445356U (en) | 2019-09-03 | 2019-09-03 | Coking wastewater ozone catalytic oxidation advanced treatment unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112624303A (en) * | 2020-12-29 | 2021-04-09 | 中海油天津化工研究设计院有限公司 | Microbubble supercharging circulation ozone catalytic oxidation reaction device |
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2019
- 2019-09-03 CN CN201921452956.XU patent/CN211445356U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112624303A (en) * | 2020-12-29 | 2021-04-09 | 中海油天津化工研究设计院有限公司 | Microbubble supercharging circulation ozone catalytic oxidation reaction device |
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Granted publication date: 20200908 |