CN115583716A - Serial ozone catalytic oxidation sewage treatment system and method - Google Patents
Serial ozone catalytic oxidation sewage treatment system and method Download PDFInfo
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- CN115583716A CN115583716A CN202210493715.XA CN202210493715A CN115583716A CN 115583716 A CN115583716 A CN 115583716A CN 202210493715 A CN202210493715 A CN 202210493715A CN 115583716 A CN115583716 A CN 115583716A
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 272
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 119
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 112
- 239000010865 sewage Substances 0.000 title claims abstract description 63
- 230000003647 oxidation Effects 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 96
- 238000012544 monitoring process Methods 0.000 claims abstract description 38
- 238000010992 reflux Methods 0.000 claims abstract description 35
- 238000011001 backwashing Methods 0.000 claims abstract description 19
- 239000005416 organic matter Substances 0.000 claims abstract description 18
- 238000010521 absorption reaction Methods 0.000 claims abstract description 13
- 239000003054 catalyst Substances 0.000 claims description 41
- 238000011010 flushing procedure Methods 0.000 claims description 19
- 238000006555 catalytic reaction Methods 0.000 claims description 16
- 238000006385 ozonation reaction Methods 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 10
- 238000013461 design Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000012856 packing Methods 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 238000004065 wastewater treatment Methods 0.000 claims 2
- 230000035939 shock Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 28
- 230000000694 effects Effects 0.000 description 7
- 239000010842 industrial wastewater Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- -1 carrier Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 210000005056 cell body Anatomy 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000306 component Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 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
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/23—O3
- C02F2209/235—O3 in the gas phase
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a serial ozone catalytic oxidation sewage treatment system and a method, wherein the system comprises: the ozone generation subsystem is connected with the ozone dosing subsystem through an ozone gas supply pipe provided with an ozone concentration online monitoring subsystem; the ozone adding subsystem is connected to the inside of the ozone catalytic oxidation reaction tank; a water inlet flowmeter and an organic matter concentration online monitoring subsystem are sequentially arranged on a water inlet pipeline of the ozone catalytic oxidation reaction tank; the reflux subsystem is connected between the water outlet pipeline of the ozone catalytic oxidation reaction tank and the ozone adding subsystem; the back washing gas subsystem and the tail gas absorption subsystem are respectively connected with the ozone catalytic oxidation reaction tank. This system is through being provided with organic matter concentration on-line monitoring subsystem, ozone concentration on-line monitoring subsystem and backward flow subsystem, is convenient for according to the COD of intaking of handling sewage, corresponds the control and throws the volume to the ozone in the ozone catalytic oxidation reaction tank, avoids ozone extravagant, promotes the ozone utilization ratio, sets up back washing gas subsystem, has promoted shock resistance.
Description
Technical Field
The invention relates to the field of advanced treatment of degradation-resistant sewage, in particular to a serial ozone catalytic oxidation sewage treatment system and method.
Background
At present, with the continuous increase of sewage projects in industrial parks and the stricter sewage discharge standards, more and more sewage treatment plants need to add advanced oxidation processes so as to achieve the purpose of standard discharge of COD of effluent. The catalytic ozonation process has the advantages of good COD removal effect, low operation cost, simplicity and convenience in operation, no sludge generation and the like in the aspect of removing refractory organic matters in industrial parks and industrial wastewater, can realize continuous water feeding or intermittent operation, is not limited by engineering scale and regions, has wide application range and has wide application prospect.
The traditional catalytic ozonation process has the disadvantages of low ozone dissolution efficiency in sewage, short ozone contact time and the like, so that the mass transfer efficiency of ozone in water is influenced, and finally the overall effect of the catalytic ozonation process is not ideal. Especially for the treatment of industrial wastewater containing refractory organic matters in the inlet water and with high concentration, in order to reach the sewage discharge standard, a large amount of ozone is usually added to remove COD in the sewage, and if the mass transfer efficiency of the ozone in the water is low, the early investment and the later operation cost are inevitably overhigh. In addition, the COD of the industrial wastewater at the upstream in the sewage treatment process of the ozone catalysis process has large variation fluctuation, so that impact load is caused, the effluent COD is easy to reach the standard, and sewage plants face environmental protection penalties. Therefore, how to relieve the impact load caused by the large fluctuation of the COD of the industrial wastewater in the traditional ozone catalytic oxidation process section is a problem to be solved urgently.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The invention aims to provide a series ozone catalytic oxidation sewage treatment system and a method, which are convenient for improving the impact load resistance of an ozone catalytic oxidation process, further ensure the catalytic oxidation effect of ozone and well solve the technical problems in the prior art.
The purpose of the invention is realized by the following technical scheme:
the embodiment of the invention provides a serial ozone catalytic oxidation sewage treatment system, which comprises:
the system comprises an ozone generation subsystem, an ozone concentration online monitoring subsystem, an ozone feeding subsystem, a water inlet flow meter, an organic matter concentration online monitoring subsystem, an ozone catalytic oxidation reaction tank, a back flushing gas subsystem, a back flow meter, a back flow pump, a back flow clean water tank, an ozone feeding pipe and a tail gas absorption subsystem; wherein, the first and the second end of the pipe are connected with each other,
the air supply port of the ozone generation subsystem is connected with the air inlet of the ozone adding subsystem through an ozone air supply pipe provided with the ozone concentration online monitoring subsystem;
an ozone adding pipe of the ozone adding subsystem is connected to the ozone catalytic oxidation reaction tank;
the water inlet flowmeter and the organic matter concentration online monitoring subsystem are sequentially arranged on a water inlet pipeline of the ozone catalytic oxidation reaction tank;
the return clean water tank is connected with a water outlet pipe at the tail end of the ozone catalytic oxidation reaction tank, and is connected with a water inlet of the ozone adding subsystem through a pipeline which is sequentially provided with the return pump and the return flowmeter;
the back-flushing gas subsystem is connected with the bottom in the ozone catalytic oxidation reaction tank;
and the tail gas absorption subsystem is connected with the top in the ozone catalytic oxidation reaction tank.
The embodiment of the invention also provides a serial ozone catalytic oxidation sewage treatment method, and the serial ozone catalytic oxidation sewage treatment system comprises:
sewage enters an ozone catalytic oxidation reaction tank of the system through a water inlet pipeline;
ozone generated by an ozone generation subsystem of the system is added into the ozone catalytic oxidation reaction tank through an ozone adding subsystem of the system, the sewage is subjected to ozone catalytic oxidation reaction, and tail gas after reaction is treated by a tail gas absorption subsystem and then is discharged;
one part of effluent of the ozone catalytic oxidation reaction tank is discharged after reaching the standard through an effluent pipeline, and the other part of effluent enters a reflux subsystem of the system through a pipeline and flows back into the ozone catalytic oxidation reaction tank through the reflux subsystem for further oxidation reaction;
in the process of ozone catalytic oxidation reaction, displaying the concentration COD of refractory organic matters entering the sewage on line through an organic matter concentration online monitoring subsystem of the system, if the concentration COD of the refractory organic matters entering the sewage is confirmed to be lower than an original design value, shutting down the backflow subsystem, and simultaneously reducing the ozone generation amount of the ozone generation subsystem according to the ozone concentration online monitoring subsystem;
if the concentration COD of the refractory organic matters entering the sewage is higher than the original design value, the reflux subsystem is opened, and the ozone generation amount of the ozone generation subsystem is increased according to the ozone concentration online monitoring subsystem;
and when the suspended matters entering the sewage exceed a preset value, opening a back-flushing gas subsystem of the system, and performing gas-water back-flushing on a catalyst packed bed in the ozone catalytic oxidation reaction tank.
Compared with the prior art, the serial ozone catalytic oxidation sewage treatment system and the serial ozone catalytic oxidation sewage treatment method have the beneficial effects that:
the treatment system is convenient to correspondingly control the ozone adding amount in the ozone catalytic oxidation reaction tank according to the inlet water COD of the treated sewage, so that the ozone waste is avoided, the ozone utilization rate is improved, and the ozone catalytic oxidation process is more flexibly and efficiently operated; the anti-impact capability of the catalytic ozonation process is improved by arranging the back-flushing gas subsystem in the catalytic ozonation reaction tank.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the description below are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of a tandem ozone catalytic oxidation sewage treatment system according to an embodiment of the present invention.
Fig. 2 is a schematic diagram of the first packed catalyst bed of the catalytic ozonation reaction tank according to an embodiment of the present invention.
Detailed Description
The technical scheme in the embodiment of the invention is clearly and completely described below by combining the specific content of the invention; it is to be understood that the described embodiments are merely exemplary of the invention, and are not intended to limit the invention to the particular forms disclosed. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present invention without making any creative effort, shall fall within the protection scope of the present invention.
The terms that may be used herein are first described as follows:
the term "and/or" means that either or both can be achieved, for example, X and/or Y means that both cases include "X" or "Y" as well as three cases including "X and Y".
The terms "comprising," "including," "containing," "having," or other similar terms of meaning should be construed as non-exclusive inclusions. For example: including a feature (e.g., material, component, ingredient, carrier, formulation, material, dimension, part, component, mechanism, device, step, process, method, reaction condition, processing condition, parameter, algorithm, signal, data, product, or article, etc.) that is not specifically recited, should be interpreted to include not only the specifically recited feature but also other features not specifically recited and known in the art.
The term "consisting of 8230% \8230%," consisting of 8230indicates the exclusion of any technical characteristic elements not explicitly listed. If used in a claim, the term shall render the claim closed except for the usual impurities associated therewith which do not include the technical features other than those explicitly listed. If the term occurs in only one clause of the claims, it is defined only as specifically listed in that clause, and elements recited in other clauses are not excluded from the overall claims.
Unless expressly stated or limited otherwise, the terms "mounted," "connected," and "secured," etc., are to be construed broadly, as for example: can be fixedly connected, can also be detachably connected or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms herein can be understood by those of ordinary skill in the art as appropriate.
When concentrations, temperatures, pressures, dimensions, or other parameters are expressed as ranges of values, the ranges are to be understood as specifically disclosing all ranges formed from any pair of upper, lower, and preferred values within the range, regardless of whether ranges are explicitly recited; for example, if a numerical range of "2 to 8" is recited, then that numerical range should be interpreted to include ranges such as "2 to 7," "2 to 6," "5 to 7," "3 to 4 and 6 to 7," "3 to 5 and 7," "2 and 5 to 7," and the like. Unless otherwise indicated, the numerical ranges recited herein include both the endpoints thereof and all integers and fractions within the numerical range.
The terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," and the like are used in an orientation or positional relationship that is indicated based on the orientation or positional relationship shown in the drawings for ease of description and simplicity of description only, and are not intended to imply or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting herein.
The serial ozone catalytic oxidation sewage treatment system and method provided by the invention are described in detail below. Details which are not described in detail in the embodiments of the invention belong to the prior art which is known to the person skilled in the art. The examples of the present invention, in which specific conditions are not specified, were carried out according to the conventional conditions in the art or conditions suggested by the manufacturer. The reagents or instruments used in the examples of the present invention are not specified by manufacturers, and are all conventional products available by commercial purchase.
As shown in fig. 1, an embodiment of the present invention provides a serial ozone catalytic oxidation sewage treatment system and method, including:
the system comprises an ozone generation subsystem 1, an ozone concentration online monitoring subsystem 2, an ozone adding subsystem 3, a water inlet flow meter 4, an organic matter concentration online monitoring subsystem 5, an ozone catalytic oxidation reaction tank 6, a back flushing gas subsystem 8, a reflux flow meter 9, a reflux pump 10, a reflux clean water tank 11, an ozone adding pipe 12 and a tail gas absorption subsystem 11; wherein the content of the first and second substances,
the air supply port of the ozone generation subsystem 1 is connected with the air inlet of the ozone adding subsystem 3 through an ozone supply pipe 10 provided with the ozone concentration online monitoring subsystem 2;
the ozone adding pipe 12 of the ozone adding subsystem 3 is connected to the inside of the ozone catalytic oxidation reaction tank 6;
the water inlet flow meter 4 and the organic matter concentration online monitoring subsystem 5 are sequentially arranged on a water inlet pipeline A of the ozone catalytic oxidation reaction tank 6;
the return clean water tank 11 is connected with a water outlet pipeline B at the tail end of the ozone catalytic oxidation reaction tank 6, and the return clean water tank 11 is connected with a water inlet of the ozone dosing subsystem 3 through a pipeline which is sequentially provided with the return pump 10 and the return flowmeter 9;
the back flushing subsystem 8 is connected with the bottom in the ozone catalytic oxidation reaction tank 6;
and the tail gas absorption subsystem 11 is connected with the top in the ozone catalytic oxidation reaction tank 6.
In the system, a first overflow wall, a first guide wall, a second overflow wall, a second guide wall and a third overflow wall are sequentially arranged in the ozone catalytic oxidation reaction tank 6 from front to back at intervals;
the upper end of the first overflow wall is provided with a first upper water passing opening;
a second lower water passing opening is formed in the lower portion of the first guide wall, and a first-stage ozone catalytic reaction area provided with a first catalyst packed bed is arranged between the first guide wall and the second overflow wall;
the upper end of the second overflow wall is provided with a third upper water passing hole;
a fourth lower water passing opening is formed in the lower portion of the second guide wall, and a second-stage ozone catalytic reaction area provided with a second catalyst packed bed is arranged between the second guide wall and the third overflow wall;
the upper end of the third overflow wall is a fifth upper water passing hole;
the bottom of the tail end of the ozone catalytic oxidation reaction tank 6 is provided with the water outlet pipeline B.
Above-mentioned ozone catalytic oxidation reaction tank 6 of this kind of structure can increase the reaction dwell time of ozone and sewage in the cell body owing to the crisscross setting of mouth of a river is crossed to upper and lower to owing to be two-stage structure ozone catalytic reaction district, increase with the mixed effect of ozone, promote the utilization efficiency of ozone.
Referring to fig. 2, in the above system, the first catalyst packed bed and the second catalyst packed bed are the same in structure and each comprises:
a water distribution device 61, a supporting layer 62 and a catalyst filler layer 63 which are arranged from bottom to top in sequence.
In the system, the height of the bearing layer 62 is 0.3-0.45 m; the height of the catalyst filler layer 63 is 0.5-3 m.
In the system, the catalyst filler layer is a filler layer composed of a metal-loaded spherical molecular sieve catalyst.
In the system, the ozone catalytic oxidation reaction tank 6 is a square tank body.
In the system, the ozone adding pipe 12 of the ozone adding subsystem 3 comprises a first ozone adding branch pipe and a second ozone adding branch pipe, wherein the first ozone adding branch pipe penetrates through the second lower water passing hole to be arranged at the bottom in the first-stage ozone catalytic reaction zone and is positioned below the first catalyst packed bed;
and the second ozone adding branch pipe penetrates through the fourth lower water passing hole to be arranged at the bottom in the second-stage ozone catalytic reaction zone and is positioned below the second catalyst packed bed.
In the system, the tail end of the first ozone adding branch pipe is a sharp nozzle air outlet, and the included angle between the sharp nozzle air outlet and the horizontal line is-10 degrees to 10 degrees;
the tail end of the second ozone adding branch pipe is a sharp nozzle air outlet, and an included angle between the sharp nozzle air outlet and the horizontal line is-10 degrees to 10 degrees. The first ozone adding branch pipe and the second ozone adding branch pipe with the tail ends being the air outlets of the sharp nozzles can play a certain role in pressurization, the ozone adding efficiency is improved, the air outlets of the sharp nozzles and the horizontal line are arranged in the direction of an included angle of-10 degrees to 10 degrees, the uniform flow state distribution of ozone in an ozone catalytic reaction area can be guaranteed, and the catalytic oxidation effect of ozone is improved.
Referring to fig. 1 and 2, in the above system, the back flush subsystem 8 includes:
a backwash air pump 81, a backwash pipeline 82 and two backwash air distribution devices 83; wherein the content of the first and second substances,
a backwash gas distribution device 83 is disposed below the first catalyst packed bed;
another backwash gas distribution device 83 is arranged below the second catalyst packed bed;
the backwashing air pump 81 is connected with two backwashing air distribution devices 83 through the backwashing pipeline 82.
The back flushing subsystem 8 can conveniently back flush the first catalyst packed bed and the second catalyst packed bed by air-water combination, and improve the impact resistance of the ozone catalytic oxidation reaction tank 6 to water inlet change.
The ozone adding subsystem 3 adopts a multi-stage jet ozone adding device, and can improve the ozone adding mixing efficiency.
The reflux sub-system 9 comprises: a reflux flow meter 93, a reflux pump 92, a reflux clean water tank 91 and a reflux pipeline 94; wherein the content of the first and second substances,
the water inlet end of the return clean water tank 91 is connected with a water outlet pipeline at the tail end of the ozone catalytic oxidation reaction tank 6;
and the water outlet of the return clean water tank 91 is connected with the water inlet of the ozone adding subsystem 3 through a return pipeline 94 which is sequentially provided with the return pump 92 and the return flowmeter 93. Such a return subsystem can monitor the return flow rate via a return flow meter 93, and can control the return flow rate or shut down the return system via a return pump 92.
The embodiment of the invention also provides a serial ozone catalytic oxidation sewage treatment method, and the serial ozone catalytic oxidation sewage treatment system comprises:
sewage enters an ozone catalytic oxidation reaction tank 6 of the system through a water inlet pipeline;
ozone generated by an ozone generation subsystem 1 of the system is added into the ozone catalytic oxidation reaction tank 6 through an ozone adding subsystem 3 of the system, the sewage is subjected to ozone catalytic oxidation reaction, and tail gas after the reaction is treated by a tail gas absorption subsystem 11 and then is discharged;
one part of the effluent of the ozone catalytic oxidation reaction tank 6 is discharged after reaching the standard through an effluent pipeline B, and the other part of the effluent enters a reflux subsystem 9 of the system through a pipeline and flows back into the ozone catalytic oxidation reaction tank 6 through a reflux pipeline of the reflux subsystem 9 to further carry out oxidation reaction;
in the process of the ozone catalytic oxidation reaction, the concentration COD of the difficultly-degraded organic matters entering the sewage is displayed on line through an online organic matter concentration monitoring subsystem 5 of the system, if the concentration COD of the difficultly-degraded organic matters entering the sewage is confirmed to be lower than an original design value, the backflow subsystem 9 is stopped, and meanwhile, the ozone generation amount of the ozone generation subsystem 1 is reduced according to the online ozone concentration monitoring subsystem 2;
if the concentration COD of the refractory organic matters entering the sewage is higher than the original design value, the reflux subsystem 9 is opened, and the ozone generation amount of the ozone generation subsystem 1 is increased according to the ozone concentration online monitoring subsystem 2;
when the suspended matter in the sewage exceeds the preset value, a back flushing subsystem 8 of the system is opened, and the first and second catalyst packed beds in the ozone catalytic oxidation reaction tank 6 are subjected to air-water back flushing.
In summary, according to the system and the method provided by the embodiment of the invention, the online organic matter concentration monitoring subsystem is arranged on the water inlet pipeline of the ozone catalytic oxidation reaction tank, the online ozone concentration monitoring subsystem is arranged on the ozone gas supply pipe of the ozone generation subsystem, and the treatment system is matched with the reflux subsystem arranged on the ozone catalytic oxidation reaction tank, so that the ozone adding amount in the ozone catalytic oxidation reaction tank can be correspondingly controlled according to the inlet water COD of the treated sewage, the ozone waste is avoided, the ozone utilization rate is improved, and the ozone catalytic oxidation process can be operated more flexibly and efficiently; the anti-impact capability of the catalytic ozonation process is improved by arranging the back-flushing gas subsystem in the catalytic ozonation reaction tank.
In order to more clearly show the technical solutions and the technical effects provided by the present invention, the following detailed description of the tandem type ozone catalytic oxidation sewage treatment system and method provided by the embodiments of the present invention is provided by specific embodiments.
Examples
As shown in fig. 1, an embodiment of the present invention provides a serial ozone catalytic oxidation sewage treatment system, including: the system comprises an ozone generation subsystem 1, an ozone concentration online monitoring subsystem 2, an ozone adding subsystem 3, a water inlet flowmeter 4, an organic matter concentration online monitoring subsystem 5, an ozone catalytic oxidation reaction tank 6, a backflow subsystem 9, an ozone adding pipe 12 and a tail gas absorption subsystem 11; the whole system layout pipeline comprises: water inlet and outlet pipelines, an ozone pipeline, an ozone tail gas pipeline, a back flush gas circuit pipeline and a backflow pipeline.
The ozone catalytic oxidation reaction tank 6 is made of concrete, and other parts of the device are made of 316L stainless steel or other ozone corrosion resistant materials.
The ozone catalytic oxidation reaction tank 6 is a square tank body, and is internally provided with a first overflow wall 71, a first guide wall 74, a second overflow wall 72, a second guide wall 75 and a third overflow wall 73 which are sequentially arranged from front to back at intervals to be divided into a two-stage ozone catalytic reaction area, namely a first ozone catalytic reaction area and a second ozone catalytic reaction area, wherein the first ozone catalytic reaction area is internally provided with a first catalyst packed bed, and the second ozone catalytic reaction area is internally provided with a second catalyst packed bed;
the first catalyst packed bed and the second catalyst packed bed have the same structure and are composed of a water distribution device 61, a supporting layer 62 and a catalyst packing layer 63 which are arranged from bottom to top in sequence; preferably, the filler of the catalyst filler layer is a metal-loaded spherical molecular sieve catalyst, and the filler has basically no abrasion consumption, is more stable and has better catalytic effect.
The front end of the ozone catalytic oxidation reaction tank 6 is connected with a water inlet pipeline, and the tail end of the ozone catalytic oxidation reaction tank is connected with a water outlet pipeline.
The ozone generating subsystem 1 is an oxygen source ozone generator system capable of monitoring the flow of ozone gas produced.
The ozone concentration on-line monitoring subsystem 2 can monitor the concentration of ozone generated by the ozone generation subsystem 1 in real time.
The ozone adding subsystem 3 adopts a multi-stage jet ozone adding device, and can realize the efficient dissolution of ozone in water in a short time.
The inflow flowmeter 4 is positioned at the foremost end of the inflow pipeline and can monitor the inflow flow in real time on line.
The organic matter concentration on-line monitoring subsystem 5 is positioned at the rear end of the water inlet flow meter 4 and can monitor the concentration of organic pollutants in inlet water on line.
The filling height of the bearing layer 62 in the ozone catalytic oxidation reaction tank 6 is 0.3-0.45 m; the filling height of the catalyst filler layer 63 is 0.5-3 m.
The ozone adding pipe 12 comprises two branches, namely a first ozone adding branch pipe and a second ozone adding branch pipe, the tail ends of the first ozone adding branch pipe and the second ozone adding branch pipe are sharp nozzle air outlets, and the included angle between each sharp nozzle air outlet and the horizontal line ranges from-10 degrees to 10 degrees.
The reflux subsystem 9 mainly comprises a reflux flowmeter 9, a reflux pump 10, a reflux clean water tank 11 and a reflux pipeline, and the reflux flow is adjusted by adjusting the reflux pump 10 to change the reflux ratio, so that part of the effluent of the ozone catalytic oxidation reaction tank 6 can be refluxed into the tank, the retention time of the sewage in the system is prolonged, and the COD removal efficiency of the sewage is improved. The reflux ratio is controlled within the range of 0.4 to 0.8.
The backwashing subsystem 8 is composed of a backwashing air pump 81, a backwashing pipeline 82 and two backwashing air distribution devices 83, one backwashing air distribution device 83 is arranged at the bottom of each catalyst packed bed, and the two backwashing air distribution devices 83 are connected with the backwashing air pump 81 through the backwashing pipeline 82, so that when the content of the suspended matters in the inlet water exceeds a preset value, the first and second catalyst packed beds are subjected to air-water backwashing, and the impact resistance of the ozone catalytic oxidation reaction tank 6 is improved.
The tail gas absorption system 11 collects ozone tail gas through an ozone tail gas pipeline at the top of the ozone catalytic oxidation reaction tank 6, can treat residual ozone tail gas in the ozone catalytic oxidation reaction tank 6, and prevents the direct discharge of the ozone tail gas from causing air pollution.
The working principle of the sewage measuring system is as follows:
sewage enters through a water inlet pipeline, the concentration of refractory organic matters is displayed on line by the online organic matter concentration monitoring subsystem and then enters the catalytic ozonation reaction tank, ozone generated by the ozone generation subsystem is added into the catalytic ozonation reaction tank through the ozone adding subsystem, catalytic ozonation reaction is carried out in the tank, the COD concentration of the sewage is reduced, meanwhile, the refractory organic matters are converted into degradable organic matters through advanced oxidation, and the biodegradability of the sewage is improved. And the tail gas after reaction is treated by a tail gas absorption system and then is exhausted.
The water discharged from the ozone catalytic oxidation reaction tank can be divided into two paths, one path of water is discharged after reaching the standard through a water outlet pipeline, the other path of water can enter a backflow clean water tank through a backflow pipeline, the backflow clean water tank is connected with the ozone catalytic oxidation reaction tank through a pipeline, and the water in the clean water tank can flow back into the ozone catalytic oxidation reaction tank through a backflow pump for further oxidation.
The arrangement of the ozone concentration on-line monitoring subsystem, the organic matter concentration on-line monitoring subsystem and the backflow subsystem enables the treatment process to be flexibly and efficiently operated. When the COD of the inlet water monitored by the online organic matter concentration monitoring subsystem is lower than an original design value, the reflux subsystem can be shut down, and the ozone generation amount of the ozone generation system is reduced, so that the ozone adding amount is saved; when the COD concentration of the inlet water monitored by the organic matter concentration online monitoring subsystem is higher than the original design value, the ozone adding amount of the ozone catalytic oxidation reaction tank is increased through the ozone generation subsystem and the ozone concentration online monitoring subsystem, and meanwhile, the reflux subsystem can be opened to increase the retention time of ozone, so that the COD removal effect of the ozone catalytic oxidation is improved, and the COD removal rate of the whole process is correspondingly improved. When the content of the suspended matters in the inlet water is too high to cause impact load, the backwashing subsystem can be opened to carry out air-water backwashing on the filler of the catalyst packed bed.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims. The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information forms the prior art already known to a person skilled in the art.
Claims (10)
1. A serial-type ozone catalytic oxidation sewage treatment system is characterized by comprising:
the system comprises an ozone generation subsystem (1), an ozone concentration online monitoring subsystem (2), an ozone adding subsystem (3), a water inlet flow meter (4), an organic matter concentration online monitoring subsystem (5), an ozone catalytic oxidation reaction tank (6), a back flushing gas subsystem (8), a backflow subsystem (9), an ozone adding pipe (10) and a tail gas absorption subsystem (11); wherein the content of the first and second substances,
the air supply port of the ozone generation subsystem (1) is connected with the air inlet of the ozone dosing subsystem (3) through an ozone air supply pipe (10) provided with the ozone concentration online monitoring subsystem (2);
an ozone adding pipe (12) of the ozone adding subsystem (3) is connected into the ozone catalytic oxidation reaction tank (6);
the water inlet flowmeter (4) and the organic matter concentration online monitoring subsystem (5) are sequentially arranged on a water inlet pipeline of the ozone catalytic oxidation reaction tank (6);
the water inlet end of the backflow subsystem (9) is connected with a water outlet pipeline at the tail end of the ozone catalytic oxidation reaction tank (6), and the water outlet end of the backflow subsystem (9) is connected with the water inlet of the ozone adding subsystem (3);
the back flushing subsystem (8) is connected with the bottom in the ozone catalytic oxidation reaction tank (6);
and the tail gas absorption subsystem (11) is connected with the top in the ozone catalytic oxidation reaction tank (6).
2. The series ozone catalytic oxidation sewage treatment system of claim 1, wherein a first overflow wall, a first guide wall, a second overflow wall, a second guide wall and a third overflow wall are sequentially arranged in the ozone catalytic oxidation reaction tank (6) from front to back at intervals;
the upper end of the first overflow wall is provided with a first upper water passing opening;
a second lower water passing opening is formed in the lower portion of the first guide wall, and a first-stage ozone catalytic reaction area provided with a first catalyst packed bed is arranged between the first guide wall and the second overflow wall;
the upper end of the second overflow wall is provided with a third upper water passing hole;
a fourth lower water passing opening is formed in the lower portion of the second guide wall, and a second-stage ozone catalytic reaction area provided with a second catalyst packed bed is arranged between the second guide wall and the third overflow wall;
the upper end of the third overflow wall is a fifth upper water passing hole;
the bottom of the tail end of the ozone catalytic oxidation reaction tank (6) is provided with the water outlet pipeline.
3. The in-line ozone catalytic oxidation wastewater treatment system of claim 1, wherein the first and second packed catalyst beds are identical in composition and each comprise:
a water distribution device (61), a supporting layer (62) and a catalyst packing layer (63) which are arranged from bottom to top in sequence.
4. The serial ozone catalytic oxidation sewage treatment system of claim 3, wherein the height of the supporting layer (62) is 0.3-0.45 m; the height of the catalyst filler layer (63) is 0.5-3 m.
5. The serial-type ozone catalytic oxidation sewage treatment system of claim 3 wherein the catalyst packing layer is a packing layer composed of metal-loaded spherical molecular sieve catalyst.
6. The series ozone catalytic oxidation sewage treatment system according to claim 3, wherein the ozone catalytic oxidation reaction tank (6) is a square tank body.
7. The series-connection type ozone catalytic oxidation sewage treatment system according to any one of claims 2 to 6, wherein the ozone adding pipe (12) of the ozone adding subsystem (3) comprises a first ozone adding branch pipe and a second ozone adding branch pipe, the first ozone adding branch pipe penetrates through the second lower water passing port to be arranged at the bottom of the first-stage ozone catalytic reaction zone and is positioned below the first catalyst packed bed;
and the second ozone adding branch pipe penetrates through the fourth lower water passing hole to be arranged at the bottom in the second-stage ozone catalytic reaction zone and is positioned below the second catalyst packed bed.
8. The series ozone catalytic oxidation sewage treatment system of claim 7, wherein the end of the first ozone adding branch pipe is a sharp nozzle air outlet, and the included angle between the sharp nozzle air outlet and the horizontal line is-10 degrees to 10 degrees;
the tail end of the second ozone adding branch pipe is a sharp nozzle air outlet, and an included angle between the sharp nozzle air outlet and the horizontal line is-10 degrees to 10 degrees.
9. The in-line ozonation catalytic oxidation wastewater treatment system according to any one of claims 2 to 6, wherein the back flush gas subsystem (8) comprises:
a back-flushing air pump (81), a back-flushing pipeline (82) and two back-flushing air distribution devices (83); wherein the content of the first and second substances,
a backwash gas distribution device (83) is arranged below the first catalyst packed bed;
another back-flushing gas distribution device (83) is arranged below the second catalyst packed bed;
the backwashing air pump (81) is respectively connected with the two backwashing air distribution devices (83) through the backwashing pipeline (82);
the ozone adding subsystem (3) adopts a multi-stage jet flow ozone adding device;
the recirculation subsystem (9) comprises: a reflux flowmeter (93), a reflux pump (92), a reflux clean water tank (91) and a reflux pipeline (94); wherein the content of the first and second substances,
the water inlet end of the return clean water tank (91) is connected with a water outlet pipeline at the tail end of the ozone catalytic oxidation reaction tank (6);
and the water outlet of the return clean water tank (91) is connected with the water inlet of the ozone dosing subsystem (3) through a return pipeline (94) which is sequentially provided with the return pump (92) and the return flowmeter (93).
10. A serial ozone catalytic oxidation sewage treatment method, characterized in that, the serial ozone catalytic oxidation sewage treatment system of any claim 1 to 9 is adopted, comprising:
sewage enters an ozone catalytic oxidation reaction tank (6) of the system through a water inlet pipeline;
ozone generated by an ozone generation subsystem (1) of the system is added into the ozone catalytic oxidation reaction tank (6) through an ozone adding subsystem (3) of the system to carry out ozone catalytic oxidation reaction on sewage, and tail gas after reaction is treated by a tail gas absorption subsystem (11) and then is discharged;
one part of effluent of the ozone catalytic oxidation reaction tank (6) is discharged after reaching the standard through an effluent pipeline, and the other part of effluent enters a reflux subsystem (9) of the system through a pipeline and flows back into the ozone catalytic oxidation reaction tank (6) through the reflux subsystem (9) to further carry out oxidation reaction;
in the process of the catalytic oxidation reaction of ozone, the concentration COD of the difficultly-degraded organic matters entering the sewage is displayed on line through an online organic matter concentration monitoring subsystem (5) of the system, if the concentration COD of the difficultly-degraded organic matters entering the sewage is confirmed to be lower than an original design value, the backflow subsystem (9) is stopped, and meanwhile, the ozone generation amount of the ozone generation subsystem (1) is reduced according to the online ozone concentration monitoring subsystem (2);
if the concentration COD of the refractory organic matters entering the sewage is higher than the original design value, the reflux subsystem (9) is opened, and the ozone generation amount of the ozone generation subsystem (1) is increased according to the ozone concentration online monitoring subsystem (2);
when the content of suspended matters in the entering sewage exceeds a preset value, a back flushing gas subsystem (8) of the system is opened, and the first catalyst packed bed and the second catalyst packed bed in the ozone catalytic oxidation reaction tank (6) are subjected to gas-water back flushing.
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