CN105481177A - Low-consumption nitrification and denitrification coal chemical wastewater advanced treatment device - Google Patents
Low-consumption nitrification and denitrification coal chemical wastewater advanced treatment device Download PDFInfo
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- CN105481177A CN105481177A CN201510992643.3A CN201510992643A CN105481177A CN 105481177 A CN105481177 A CN 105481177A CN 201510992643 A CN201510992643 A CN 201510992643A CN 105481177 A CN105481177 A CN 105481177A
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/889—Manganese, technetium or rhenium
- B01J23/8892—Manganese
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
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Abstract
The invention discloses a low-consumption nitrification and denitrification coal chemical wastewater advanced treatment device, comprising a catalytic oxidation pond, an oxidation stabilization pond and a rear biochemical BAF pond, wherein the catalytic oxidation pond is filled with ozone-catalytic particles in a static bed form, and a comprehensive dilution tank is provided with a charging hole and a stirrer; the ozone-catalytic particles are prepared from 88.7-91.3 parts of activated aluminium oxide particles, 1.2-1.5 parts of copper oxide, 4-7 parts of polyethylene glycol, 1.5-2 parts of polyvinyl alcohol, 0.8-1 part of titanium dioxide, 0.3-0.5 part of hydroxyl propyl cellulose and 0.2-0.4 part of manganese dioxide; the lower part and the upper part of an aerobic tank in the rear biochemical BAF pond are respectively provided with a lower sieve plate and an upper sieve plate, the lower sieve plate, the upper sieve plate and the side wall of the aerobic tank form an aerobic cavity, and a plurality of aerobic activated sludge particles and a plurality of second masson pines as a filler are arranged in the aerobic cavity. The low-consumption nitrification and denitrification coal chemical wastewater advanced treatment device oxidizes a macromolecular organic matter hard to degrade into a micromolecular organic matter easy to biochemically treat, and the biochemical property of effluent is further improved.
Description
Technical field
The present invention relates to a kind of low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus, belong to technical field of waste water processing.
Background technology
Domestic coal-producing gasification factory mostly adopts the strange gas-made technology in Shandong, and the Wastewater Pollutant that this technique produces is dense, and organic components is complicated, mainly contain phenolic compound, polycyclc aromatic compound, the heterogeneous ring compound of nitrogenous, oxygen, sulphur and fats chemical combination, toxicity is large, difficult for biological degradation.If coal gas wastewater will cause serious pollution to ecotope without dealing carefully with discharge beyond standards, therefore how effectively to administer coal gas wastewater, realizing discharged wastewater met the national standard becomes an international difficult problem.
At present, the ammonia nitrogen of high density and phenol are the Focal point and difficult points of coal gasification waste water water treatment, coal gasification waste water is after pre-treatment and biochemical treatment, ammonia nitrogen and most of organism are effectively removed, but still containing certain hardly degraded organic substance and suspended substance in waste water, need just can reach discharge and reuse requirement by advanced treatment.The further treatment technique applied both at home and abroad has advanced oxidation processes, absorption method, coagulant sedimentation and membrane separation technique, and above-mentioned wastewater processing technology still exists a lot of problem on outlet effect and running cost.Mostly rest on the small-scale test stage to the research of coal gasification waste water treatment technology at present, most of scholar is carrying out applied research for monotechnics, studies seldom the coupling technique of materializing strategy and biochemical treatment.
Summary of the invention
The object of the invention is to provide a kind of low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus, this low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus working cost is low, simple to operate, stable, and obtain the object of efficient degradation organic pollutant, the petroleum chemical industry height saline sewage advanced treatment under low cost and qualified discharge can be realized.
For achieving the above object, the technical solution used in the present invention is: a kind of low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus, described treatment process is based on a special processor, this special processor comprises catalyzed oxidation pond, oxidation-stabilized pond, rear biochemical BAF pond, clean water basin, dilute comprehensive tank, pretreated primary BAF pond, pre-treatment secondary BAF pond and outlet sump, the comprehensive tank of described dilution, pretreated primary BAF pond, pre-treatment secondary BAF pond is connected by leading portion transfer conduit successively with outlet sump, described catalyzed oxidation pond, oxidation-stabilized pond, rear biochemical BAF pond is connected by back segment transfer conduit successively with clean water basin, it is inner that described outlet sump and catalyzed oxidation pond are connected to catalyzed oxidation pond by inlet channel,
It is inner that one ozonizer is connected to catalyzed oxidation pond by gas pipeline, described clean water basin are provided with prosopyle, posticum, the prosopyle of described clean water basin is connected by back segment transfer conduit with rear biochemical BAF pond, described clean water basin are connected to a backwashing pump one end, it is inner that this backwashing pump the other end is connected to catalyzed oxidation pond, rear biochemical BAF pond by back segment reflux line, described catalyzed oxidation pond is filled with ozone catalytic particle with fixed bed form, and the comprehensive tank of described dilution is provided with charging opening and agitator;
Described rear biochemical BAF pond comprises anaerobic pond, Aerobic Pond further, and the top of described anaerobic pond is connected by intervalve with the bottom of Aerobic Pond, and the bottom of described anaerobic pond is connected with sewage water inlet pipe, and the top of described Aerobic Pond is connected with water shoot;
Described anaerobic pond bottom, top are separately installed with lower supporting plate, upper backup pad, this lower supporting plate, upper backup pad and anaerobic pond sidewall form anaerobism cavity, be placed with several anaerobic activated sludge particles and some first Pinus massoniana Lamb as filler in described anaerobism cavity, in several anaerobic activated sludge particles described, part anaerobic activated sludge particle is positioned at the first Pinus massoniana Lamb on the surface;
Described Aerobic Pond bottom, top are separately installed with lower sieve plate, upper sieve plate, this lower sieve plate, upper sieve plate and Aerobic Pond sidewall form aerobic cavity, be placed with several aerobic activated sludge particles and some second Pinus massoniana Lamb as filler in described aerobic cavity, in several aerobic activated sludge particles described, part aerobic activated sludge particle is positioned at the second Pinus massoniana Lamb on the surface;
Described Aerobic Pond is vertically provided with the aeration cylinder of sieve plate under an embedding, upper sieve plate centre, one aeration head is positioned at bottom aeration cylinder, one is positioned at aeration cylinder for the oxygen hose transmitting oxygen and is connected to described aeration head, and described aerobic activated sludge particle and the second Pinus massoniana Lamb are between Aerobic Pond sidewall and aeration cylinder;
The top of described aeration cylinder is provided with back window portion, and this back window portion is positioned at above upper sieve plate, and this back window portion side surface has been uniformly distributed circumferentially several fenestras;
Described ozone catalytic particle is made up of the component of following weight part:
Particle diameter is the activated alumina particle 88.7 ~ 91.3 parts of 2 ~ 4mm,
Cupric oxide 1.2 ~ 1.5 parts,
Polyoxyethylene glycol 4 ~ 7 parts,
Polyvinyl alcohol 1.5 ~ 2 parts,
Titanium dioxide 0.8 ~ 1 part,
Hydroxypropylcellulose 0.3 ~ 0.5 part,
Manganse Dioxide 0.2 ~ 0.4 part;
Be that the activated alumina particle 88.7 ~ 91.3 parts of 2 ~ 4mm mixes with cupric oxide 1.2 ~ 1.5 parts, polyoxyethylene glycol 4 ~ 7 parts, polyvinyl alcohol 1.5 ~ 2 parts, titanium dioxide 0.8 ~ 1 part, hydroxypropylcellulose 0.3 ~ 0.5 part, Manganse Dioxide 0.2 ~ 0.4 part in stirring mixer by described particle diameter, make the cupric oxide after Homogeneous phase mixing 1.2 ~ 1.5 parts, polyoxyethylene glycol 4 ~ 7 parts, polyvinyl alcohol 1.5 ~ 2 parts, titanium dioxide 0.8 ~ 1 part, hydroxypropylcellulose 0.3 ~ 0.5 part, Manganse Dioxide 0.2 ~ 0.4 part be covered in described activated alumina particle surface and form catalyzer mother bulb; Again catalyzer mother bulb is carried out drying successively, roasting obtains described loaded catalyst.
The technical scheme improved further in technique scheme is as follows:
As preferably, also comprise the backwash settling tank, leading portion supernatant liquid pool and the pre-treatment backwashing pump that connect successively, described backwash settling tank is connected to pretreated primary BAF pond, pre-treatment secondary BAF pond by the first pipeline, second pipe, and described pre-treatment backwashing pump is connected to pretreated primary BAF pond, pre-treatment secondary BAF pond by leading portion reflux line.
As preferably, described ozonizer is connected to the bottom in catalyzed oxidation pond by gas pipeline.
As preferably, in described step 3, under 100 ~ 120 DEG C of conditions, time of drying is 4 ~ 6 hours.
As preferably, in described step 4, under 350 ~ 520 DEG C of conditions, roasting time is 7 ~ 9 hours.
Because technique scheme is used, the present invention compared with prior art has following advantages and effect:
1, low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus of the present invention, its catalytic ozonation technology compares other chemical oxidization methods, speed of reaction is rapid, produce the hydroxyl radical free radical of non-selectivity active in a large number, multiple pollutant in oxidized waste water, improve the biodegradability of waste water, oxidation water outlet enters internal recycle BAF, in the filtration of biological bed, under biofloculation and biological adsorption effect, the materials such as the organism contained in waste water are by further by adsorption and oxidation, the advantage of effectively with low cost in conjunction with biochemical treatment and the advanced oxidation high efficiency of the method, improve the feasibility of the dense water depth process of RO, secondly, improve the tolerance to coal chemical industry sewage, make in the catalytic oxidation treatment process to coal chemical industry sewage, the hydroxyl radical free radical that catalyst ozone generation is active, keeps good effect to the removal of waste water COD, decolouring, de-stench, degraded toxic pollutant and the biodegradability that improves waste water.
2, low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus of the present invention, macromole hardly degraded organic substance is oxidized to the easy biochemical organism of small molecules by it, and then the biochemical of water outlet is improved, by rear biochemical internal recycle BAF system, mineralising is carried out to the organism in water again, final outflow water is less than 30mg/L, embodies the economy of this combination process, high efficiency.
3, the present invention is used for the advanced treatment device of petrochemical complex height saline sewage qualified discharge, it increases internal recycle can significantly improve O pond synchronous nitration and denitrification efficiency, thus the removal effect that improve TN, also assures that the double oxygen environment in A pond carbon source abundance and A pond simultaneously, A pond denitrifying bacteria is played a role efficiently, the low total nitrogen of further raising, the total clearance of total nitrogen is about more than 92%; Secondly, it adopts Pinus massoniana Lamb elastic filler: 3 D elastic filler has screened several corrosion resistants in polyolefins and polymeric amide, high temperature resistant, ageing-resistant fine quality, be mixed with the auxiliary agents such as hydrophilic, absorption, heat resistanceheat resistant oxygen, adopt special wire drawing, strand hair technique, strand is interted solid at corrosion resistant, on the axial cord of high strength, make strand spatially evenly distributed radiation regimes, filler evenly can be unfolded and is abound with by stereoscopic and omnibearing in effective area, and surface-area is large, and biofilm is rapid, and adhesion not conglomeration, make gas, water, microbial film obtain fully mixed oozing and contact exchange; Secondly, by Pinus massoniana Lamb biofilm, the working cost that the specific denitrifying bacteria in A pond and O pond and nitrifier save sludge reflux in traditional A/O technique can be turned out.
Accompanying drawing explanation
Accompanying drawing 1 be treatment process of the present invention based on special processor structural representation;
Accompanying drawing 2 is the local structure schematic diagram of accompanying drawing 1;
Accompanying drawing 3 is rear biochemical BAF pool structure schematic diagram in accompanying drawing 1.
In above accompanying drawing: 1, catalyzed oxidation pond; 2, oxidation-stabilized pond; 3, rear biochemical BAF pond; 4, clean water basin; 41, prosopyle; 42, posticum; 51, leading portion transfer conduit; 52, back segment transfer conduit; 6, lift pump; 7, inlet channel; 8, ozonizer; 9, gas pipeline; 10, back segment reflux line; 11, backwashing pump; 12, ozone catalytic particle; 15, pretreated primary BAF pond; 16, pre-treatment secondary BAF pond; 17, outlet sump; 18, comprehensive tank is diluted; 181, charging opening; 182, agitator; 19, backwash settling tank; 201, the first pipeline; 202, backwash settling tank; 21, leading portion supernatant liquid pool; 22, pre-treatment backwashing pump; 23, leading portion reflux line; 31, anaerobic pond; 32, Aerobic Pond; 33, intervalve; 34, sewage water inlet pipe; 35, water shoot; 36, lower supporting plate; 37, upper backup pad; 38, anaerobism cavity; 39, anaerobic activated sludge particle; 40, the first Pinus massoniana Lamb; 41, lower sieve plate; 42, upper sieve plate; 43, aerobic cavity; 44, aerobic activated sludge particle; 45, the second Pinus massoniana Lamb; 46, aeration cylinder; 47, aeration head; 48, oxygen hose; 49, back window portion; 50, fenestra.
Embodiment
Below in conjunction with embodiment, the invention will be further described:
Embodiment 1 ~ 4: a kind of low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus, described treatment process is based on a special processor, this special processor comprises catalyzed oxidation pond 1, oxidation-stabilized pond 2, rear biochemical BAF pond 3, clean water basin 4, dilutes comprehensive tank 18, pretreated primary BAF pond 15, pre-treatment secondary BAF pond 16 and outlet sump 17, the comprehensive tank 18 of described dilution, pretreated primary BAF pond 15, pre-treatment secondary BAF pond 16 are connected by leading portion transfer conduit 51 successively with outlet sump 17
Described catalyzed oxidation pond 1, oxidation-stabilized pond 2, rear biochemical BAF pond 3 are connected by back segment transfer conduit 52 successively with clean water basin 4, and it is inner that described outlet sump 17 and catalyzed oxidation pond 1 are connected to catalyzed oxidation pond 1 by inlet channel 7,
It is inner that one ozonizer 8 is connected to catalyzed oxidation pond 1 by gas pipeline 9, described clean water basin 4 are provided with prosopyle 41, posticum 42, the prosopyle 41 of described clean water basin 4 is connected by back segment transfer conduit 52 with rear biochemical BAF pond 3, described clean water basin 4 are connected to backwashing pump 11 one end, it is inner that this backwashing pump 11 the other end is connected to catalyzed oxidation pond 1, rear biochemical BAF pond 3 by back segment reflux line 10, described catalyzed oxidation pond 1 is filled with ozone catalytic particle 12 with fixed bed form, and the comprehensive tank 18 of described dilution is provided with charging opening 181 and agitator 182;
Described rear biochemical BAF pond 3 comprises anaerobic pond 31, Aerobic Pond 32 further, the top of described anaerobic pond 31 is connected by intervalve 33 with the bottom of Aerobic Pond 32, the bottom of described anaerobic pond 31 is connected with sewage water inlet pipe 34, and the top of described Aerobic Pond 32 is connected with water shoot 35;
Described anaerobic pond 31 bottom, top are separately installed with lower supporting plate 36, upper backup pad 37, this lower supporting plate 36, upper backup pad 37 and anaerobic pond 31 sidewall form anaerobism cavity 38, be placed with several anaerobic activated sludge particles 39 and some first Pinus massoniana Lamb 40 as filler in described anaerobism cavity 38, in several anaerobic activated sludge particles 39 described, part anaerobic activated sludge particle 39 is positioned at the first Pinus massoniana Lamb 40 on the surface;
Described Aerobic Pond 32 bottom, top are separately installed with lower sieve plate 41, upper sieve plate 42, this lower sieve plate 41, upper sieve plate 42 and Aerobic Pond 32 sidewall form aerobic cavity 43, be placed with several aerobic activated sludge particles 44 and some second Pinus massoniana Lamb 45 as filler in described aerobic cavity 43, in several aerobic activated sludge particles 44 described, part aerobic activated sludge particle 44 is positioned at the second Pinus massoniana Lamb 45 on the surface;
Described Aerobic Pond 32 is vertically provided with the aeration cylinder 46 of sieve plate 41 under an embedding, upper sieve plate 42 centre, one aeration head 47 is positioned at bottom aeration cylinder 46, one is positioned at aeration cylinder 46 for the oxygen hose 48 transmitting oxygen and is connected to described aeration head 47, and described aerobic activated sludge particle 44 and the second Pinus massoniana Lamb 45 are between Aerobic Pond 32 sidewall and aeration cylinder 46;
The top of described aeration cylinder 46 is provided with back window portion 49, and this back window portion 49 is positioned at above upper sieve plate 42, and this back window portion 49 side surface has been uniformly distributed circumferentially several fenestras 50;
Described ozone catalytic particle 12 is made up of the component of following weight part, as shown in table 1:
Table 1
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | |
| Activated alumina particle | 90 parts | 89.5 parts | 89 parts | 91 parts |
| Cupric oxide 1.2 ~ 1.5 parts | 1.25 part | 1.4 part | 1.2 part | 1.3 part |
| Polyoxyethylene glycol 4 ~ 7 parts | 5.2 part | 6 parts | 4.5 part | 6.2 part |
| Polyvinyl alcohol 1.5 ~ 2 parts | 1.5 part | 1.8 part | 2 parts | 1.6 part |
| Titanium dioxide 0.8 ~ 1 part | 1 part | 0.9 part | 0.95 part | 0.8 part |
| Hydroxypropylcellulose 0.3 ~ 0.5 part | 0.45 part | 0.38 part | 0.5 part | 0.35 part |
| Manganse Dioxide 0.2 ~ 0.4 part | 0.3 part | 0.2 part | 0.25 part | 0.32 part |
Described activated alumina particle particle diameter is 2 ~ 4mm;
Be that the activated alumina particle 88.7 ~ 91.3 parts of 2 ~ 4mm mixes with cupric oxide 1.2 ~ 1.5 parts, polyoxyethylene glycol 4 ~ 7 parts, polyvinyl alcohol 1.5 ~ 2 parts, titanium dioxide 0.8 ~ 1 part, hydroxypropylcellulose 0.3 ~ 0.5 part, Manganse Dioxide 0.2 ~ 0.4 part in stirring mixer by described particle diameter, make the cupric oxide after Homogeneous phase mixing 1.2 ~ 1.5 parts, polyoxyethylene glycol 4 ~ 7 parts, polyvinyl alcohol 1.5 ~ 2 parts, titanium dioxide 0.8 ~ 1 part, hydroxypropylcellulose 0.3 ~ 0.5 part, Manganse Dioxide 0.2 ~ 0.4 part be covered in described activated alumina particle surface and form catalyzer mother bulb; Again catalyzer mother bulb is carried out drying successively, roasting obtains described loaded catalyst.
Also comprise the backwash settling tank 19, leading portion supernatant liquid pool 21 and the pre-treatment backwashing pump 22 that connect successively, described backwash settling tank 19 is connected to pretreated primary BAF pond 15, pre-treatment secondary BAF pond 16 by the first pipeline 201, second pipe 201, and described pre-treatment backwashing pump 22 is connected to pretreated primary BAF pond 15, pre-treatment secondary BAF pond 16 by leading portion reflux line 23.
Above-mentioned ozonizer 8 is connected to the bottom in catalyzed oxidation pond 1 by gas pipeline 9.
In above-mentioned steps three, under 100 ~ 120 DEG C of conditions, time of drying is 5 hours; In above-mentioned steps four, under 350 ~ 520 DEG C of conditions, roasting time is 8 hours.
Ozone catalytic particulate catalytic effect assessment of the present invention, experimental technique and data are in table 2:
In the test of dynamic continuous flow catalytic ozonation, catalyst amounts is 1.5L, ozone dosage 100mg/L, hydraulic detention time 1h, utilizes gas meter to control ozone dosage, by peristaltic pump continuum micromeehanics in experiment.After running 3 cycle catalytic effect stabilities, repeatedly sampling and measuring COD, averages.
Experiment condition: dynamic continuous flow operational mode, ozone dosage 100mg/L, HRT=1h.
Water inlet source: the dense water of certain factory RO, COD is about 350mg/L, and TDS is 3500mg/L.
From table 2, data are known, relative to Zhonghai Asphalt's conventional alumina ozone catalyst, the dense water of resistance to high salt ozone catalyst catalyzed oxidation RO, be 100mg/L at ozone dosage, hydraulic detention time is under 1h operational conditions, COD clearance is up to 34.2%, and ozone efficiency is 1.1, is far superior to conventional ozone catalyst.
Low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus of the present invention, working process is as follows, comprises the steps:
(1) coal chemical industry sewage squeezes into internal recycle BAF system by pump, and sewage promotes along aeration tube, then through biological bed, forms cycling stream.The flow velocity of packing layer inside reaches 20 ~ 30m/h, improve the mass transfer velocity between microbial film and aqueous phase, improve treatment efficiency and the impact resistance of reactor, the air water short circuit phenomenon simultaneously preventing the channel directly formed packing layer aeration to cause occurs.By pretreated BAF system can degrade by biochemical component to coal chemical industry sewage, thus reduce bio-chemical effluent COD;
(2) biochemical pre-treatment water outlet gravity flow enters catalytic ozonation, rear biochemical internal recycle BAF coupling technique treatment system, first this system utilizes ozone to carry out catalytic oxidation, utilize ozone oxidation part refractory organic, make larger molecular organics be oxidized to small organic molecule, the biodegradability of pre-treatment water outlet can be improved simultaneously;
(3) catalytic ozonation water outlet enters rear biochemical internal recycle BAF advanced treatment system, and this biochemical reaction tank utilizes the mushroom of domestication to carry out biological degradation to the small organic molecule of ozone oxidation water outlet, and water outlet COD is reduced further.
Wherein, in order to ensure the microorganism growth in pre-treatment IRBAF device in step (1), total dissolved solid concentration is controlled 1.3% to 2.5%;
In step (2) in catalytic ozonation technique, control ozone dosage and be not more than 100mg/L, to meet rear biochemical internal recycle BAF demand.In catalytic ozonation pond, catalyzer exists as a fixed bed, the present embodiment catalyzer is metal ion loaded catalyst, hydroxyl radical free radical can be produced by catalysis ozone, reduce the activation energy of hydroxyl radical free radical oxidizing reaction simultaneously, the organism of difficult degradation in phenol-containing wastewater is removed by mineralising.
In step (3), catalytic ozonation water outlet gravity flow enters rear biochemical internal recycle BAF advanced treatment system, utilizes microorganism to carry out biological degradation to the organism after catalytic ozonation, to reduce processing cost.
The water quality analysis data of embodiment implemented by table 3
When influent COD is 1100-1300mg/L, be less than 120mg/L through the water outlet of pre-treatment IRBAF biochemical system, COD clearance is up to 90%, and internal recycle BAF reactor is to the high efficiency of high saliferous phenolic wastewater as can be seen here; For the waste water difficult for biological degradation after pre-treatment biochemical treatment, adopt catalytic ozonation high-level oxidation technology, metal ion loaded catalyst catalysis ozone is utilized to produce the hydroxyl radical free radical of strong oxidizing property, the organism of bio-refractory is oxidized, on the one hand by mineralization of organic material can be reduced water outlet COD, learn that water outlet COD is less than 60mg/L by table 3; Macromole hardly degraded organic substance can be oxidized to the easy biochemical organism of small molecules on the other hand, and then the biochemical of water outlet is improved.Carry out mineralising by rear biochemical internal recycle BAF system to the organism in water again, final outflow water is less than 30mg/L, embodies the economy of this combination process, high efficiency.
Above-described embodiment, only for technical conceive of the present invention and feature are described, its object is to person skilled in the art can be understood content of the present invention and implement according to this, can not limit the scope of the invention with this.All equivalences done according to spirit of the present invention change or modify, and all should be encompassed within protection scope of the present invention.
Claims (5)
1. a low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus, this special processor comprises catalyzed oxidation pond (1), oxidation-stabilized pond (2), rear biochemical BAF pond (3), clean water basin (4), dilutes comprehensive tank (18), pretreated primary BAF pond (15), pre-treatment secondary BAF pond (16) and outlet sump (17), the comprehensive tank of described dilution (18), pretreated primary BAF pond (15), pre-treatment secondary BAF pond (16) and outlet sump (17) are connected by leading portion transfer conduit (51) successively
Described catalyzed oxidation pond (1), oxidation-stabilized pond (2), rear biochemical BAF pond (3) and clean water basin (4) are connected by back segment transfer conduit (52) successively, and it is inner that described outlet sump (17) and catalyzed oxidation pond (1) are connected to catalyzed oxidation pond (1) by inlet channel (7);
It is inner that one ozonizer (8) is connected to catalyzed oxidation pond (1) by gas pipeline (9), described clean water basin (4) are provided with prosopyle (41), posticum (42), the prosopyle (41) of described clean water basin (4) is connected by back segment transfer conduit (52) with rear biochemical BAF pond (3), described clean water basin (4) are connected to a backwashing pump (11) one end, this backwashing pump (11) the other end is connected to catalyzed oxidation pond (1) by back segment reflux line (10), rear biochemical BAF pond (3) is inner, described catalyzed oxidation pond (1) is filled with ozone catalytic particle (12) with fixed bed form, the comprehensive tank of described dilution (18) is provided with charging opening (181) and agitator (182),
Described rear biochemical BAF pond (3) comprises anaerobic pond (31), Aerobic Pond (32) further, the top of described anaerobic pond (31) is connected by intervalve (33) with the bottom of Aerobic Pond (32), the bottom of described anaerobic pond (31) is connected with sewage water inlet pipe (34), and the top of described Aerobic Pond (32) is connected with water shoot (35);
Described anaerobic pond (31) bottom, top are separately installed with lower supporting plate (36), upper backup pad (37), this lower supporting plate (36), upper backup pad (37) and anaerobic pond (31) sidewall form anaerobism cavity (38), be placed with several anaerobic activated sludge particles (39) and some first Pinus massoniana Lamb (40) as filler in described anaerobism cavity (38), in several anaerobic activated sludge particles (39) described, part anaerobic activated sludge particle (39) is positioned at the first Pinus massoniana Lamb (40) on the surface;
Described Aerobic Pond (32) bottom, top are separately installed with lower sieve plate (41), upper sieve plate (42), this lower sieve plate (41), upper sieve plate (42) and Aerobic Pond (32) sidewall form aerobic cavity (43), be placed with several aerobic activated sludge particles (44) and some second Pinus massoniana Lamb (45) as filler in described aerobic cavity (43), in several aerobic activated sludge particles (44) described, part aerobic activated sludge particle (44) is positioned at the second Pinus massoniana Lamb (45) on the surface;
Described Aerobic Pond (32) is vertically provided with the aeration cylinder (46) of sieve plate (41) under an embedding, upper sieve plate (42) centre, one aeration head (47) is positioned at aeration cylinder (46) bottom, one is positioned at aeration cylinder (46) for the oxygen hose (48) transmitting oxygen and is connected to described aeration head (47), and described aerobic activated sludge particle (44) and the second Pinus massoniana Lamb (45) are positioned between Aerobic Pond (32) sidewall and aeration cylinder (46);
The top of described aeration cylinder (46) is provided with back window portion (49), and this back window portion (49) is positioned at upper sieve plate (42) top, and this back window portion (49) side surface has been uniformly distributed circumferentially several fenestras (50);
Described ozone catalytic particle (12) is made up of the component of following weight part:
Particle diameter is the activated alumina particle 88.7 ~ 91.3 parts of 2 ~ 4mm,
Cupric oxide 1.2 ~ 1.5 parts,
Polyoxyethylene glycol 4 ~ 7 parts,
Polyvinyl alcohol 1.5 ~ 2 parts,
Titanium dioxide 0.8 ~ 1 part,
Hydroxypropylcellulose 0.3 ~ 0.5 part,
Manganse Dioxide 0.2 ~ 0.4 part;
Be that the activated alumina particle 88.7 ~ 91.3 parts of 2 ~ 4mm mixes with cupric oxide 1.2 ~ 1.5 parts, polyoxyethylene glycol 4 ~ 7 parts, polyvinyl alcohol 1.5 ~ 2 parts, titanium dioxide 0.8 ~ 1 part, hydroxypropylcellulose 0.3 ~ 0.5 part, Manganse Dioxide 0.2 ~ 0.4 part in stirring mixer by described particle diameter, make the cupric oxide after Homogeneous phase mixing 1.2 ~ 1.5 parts, polyoxyethylene glycol 4 ~ 7 parts, polyvinyl alcohol 1.5 ~ 2 parts, titanium dioxide 0.8 ~ 1 part, hydroxypropylcellulose 0.3 ~ 0.5 part, Manganse Dioxide 0.2 ~ 0.4 part be covered in described activated alumina particle surface and form catalyzer mother bulb; Again catalyzer mother bulb is carried out drying successively, roasting obtains described loaded catalyst.
2. low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus according to claim 1, it is characterized in that: also comprise the backwash settling tank (19), leading portion supernatant liquid pool (21) and the pre-treatment backwashing pump (22) that connect successively, described backwash settling tank (19) is connected to pretreated primary BAF pond (15), pre-treatment secondary BAF pond (16) by the first pipeline (201), second pipe (201), and described pre-treatment backwashing pump (22) is connected to pretreated primary BAF pond (15), pre-treatment secondary BAF pond (16) by leading portion reflux line (23).
3. low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus according to claim 1, is characterized in that: described ozonizer (8) is connected to the bottom of catalyzed oxidation pond (1) by gas pipeline (9).
4. low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus according to claim 1, is characterized in that: in described step 3, under 100 ~ 120 DEG C of conditions, time of drying is 4 ~ 6 hours.
5. low consumption nitration denitrification coal chemical industry sewage advanced treatment apparatus according to claim 1, is characterized in that: in described step 4, under 350 ~ 520 DEG C of conditions, roasting time is 7 ~ 9 hours.
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