CN103214079A - Bidirectional flow internal circulation type PS advanced oxidation reactor and sewage treatment method - Google Patents
Bidirectional flow internal circulation type PS advanced oxidation reactor and sewage treatment method Download PDFInfo
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- 239000010865 sewage Substances 0.000 title claims abstract description 57
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 27
- 230000003647 oxidation Effects 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 18
- 230000002457 bidirectional effect Effects 0.000 title claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 131
- 238000006243 chemical reaction Methods 0.000 claims abstract description 22
- 239000000126 substance Substances 0.000 claims description 43
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 21
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 18
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 claims description 11
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 10
- 239000004744 fabric Substances 0.000 claims description 9
- 239000008139 complexing agent Substances 0.000 claims description 7
- 230000003068 static effect Effects 0.000 claims description 7
- 235000006408 oxalic acid Nutrition 0.000 claims description 6
- 230000000630 rising effect Effects 0.000 claims description 4
- 239000003814 drug Substances 0.000 abstract description 10
- 239000003054 catalyst Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000003795 chemical substances by application Substances 0.000 abstract 3
- 239000003344 environmental pollutant Substances 0.000 abstract 1
- 231100000719 pollutant Toxicity 0.000 abstract 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 17
- 239000002351 wastewater Substances 0.000 description 15
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 150000003254 radicals Chemical class 0.000 description 8
- 239000000975 dye Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000002585 base Substances 0.000 description 5
- 238000006555 catalytic reaction Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 230000004913 activation Effects 0.000 description 4
- 238000009303 advanced oxidation process reaction Methods 0.000 description 4
- 230000015556 catabolic process Effects 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 230000000536 complexating effect Effects 0.000 description 4
- 238000006731 degradation reaction Methods 0.000 description 4
- -1 hydroxyl radical free radical Chemical class 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 230000004044 response Effects 0.000 description 4
- 150000003384 small molecules Chemical class 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910001448 ferrous ion Inorganic materials 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 208000035126 Facies Diseases 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
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- 238000011161 development Methods 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
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- 238000007172 homogeneous catalysis Methods 0.000 description 1
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Abstract
The invention discloses a bidirectional flow internal circulation type PS advanced oxidation reactor and a sewage treatment method. The bidirectional flow internal circulation type PS advanced oxidation reactor comprises a reactor, wherein an inner barrel and an outer barrel which are staggered up and down and are concentric to each other are arranged in the reactor; the upper end of the inner barrel is open; the lower end of the inner barrel is connected with the bottom of a reactor tank; the upper end of the outer barrel is connected with the top of the reactor tank; the lower end of the outer barrel is open; the bottom of the reactor tank is provided with a power-free self-priming backflow system and an umbrella-shaped conical water distributor; the lower end of a catalyst dosing pipe which stretches to the bottom from the top of the reactor tank is correspondingly communicated with an umbrella-shaped conical medicine distributor; the umbrella-shaped conical medicine distributor is positioned in a water-distributing mixed area of the reactor; the reactor also comprises a circular water distribution baffle, a water inlet mixing device and a secondary dosing device. The reactor is small in height-diameter ratio, the reaction space is fully utilized, the capacity load rate is high, the power consumption is low, the unreacted pollutants and agents are repeatedly treated in the power-free backflow system, the agent utilization rate is improved, the agent consumption and energy consumption are reduced, and the cost is reduced.
Description
Technical field
The present invention relates to wastewater treatment equipment and sewage treatment process, relate in particular to a kind of bidirectional flow internal-circulation type PS advanced oxidation reactor and sewage water treatment method.
Background technology
High concentrated organic wastewater is one of difficult problem of Industrial Wastewater Treatment, and it generally has the characteristics that biodegradability is poor, the pollutent relative molecular weight is big.
The prior biological treatment process is to the macromolecule organic pollutant difficult treatment of difficult for biological degradation, and advanced oxidation processes is by producing active extremely strong free radical (hydroxyl radical free radical OH, sulfate radical free radical SO in reaction
4 -Deng), can effectively the macromole hardly degraded organic substance be oxidized to low toxicity or nontoxic small-molecule substance, have the reaction efficiency height, speed of response is fast, organic matter degradation is thorough, characteristics such as applied widely, having a extensive future aspect the high concentrated organic wastewater handling.
In numerous advanced oxidation processes, based on the ferrous catalyzing hydrogen peroxide Fenton oxidation style of OH because of need not external energies such as illumination, High Temperature High Pressure, electric energy, therefore relatively economy such as photochemical oxidation, catalytic wet oxidation, sonochemistry oxidation, electrochemical oxidation, ozone oxidation method, simply be widely studied application.But the Fenton oxidation style is existing some problems aspect the processing high concentrated organic wastewater, comprise: (1) Fenton process need keep pH about 2.5～4 to prevent ferrous precipitation, just can obtain good treatment effect, most of wastewater biochemicals are handled back pH at nearly neutrality or alkaline range, follow-up advanced oxidation is handled need add a large amount of acid in system, cause processing cost higher; (2) aspect ratio is bigger mostly for Fenton's reaction equipment (as fluidized-bed), and hydraulic loss is big, and capacity utilization is low, causes difficulty of construction big, the energy consumption height; (3) inside reactor is difficult to require according to the differential responses stage hydraulics of formation different zones, and short stream easily takes place, and causes the medicament utilising efficiency low; (4) the free ferrous ion is very easily oxidized in the system, and Fe
2+The speed of reaction that homogeneous catalysis produces free radical is exceedingly fast and excessive Fe
2+Can compete free radical with pollutent, cause the local Fe of reactor easily
2+Excessively reduce the free radical that catalysis produces, caused Fe
2+All consumed rapidly and the not effectively catalysis of quilt of oxygenant of other regional areas with free radical, free-radical generating and utilising efficiency are low; (5) remaining oxygenant and catalyzer fail to be recovered and to reuse in the advanced oxidation reaction, cause the medicament waste and form secondary pollution.Based on the sulfate radical free radical
The PS advanced oxidation processes be the high-concentration hardly-degradable organic pollutant removal new technology that development in recent years is got up.Under the neutrallty condition,
Standard oxidationreduction potential (2.5～3.1V) than OH(2.3V) height, and
Active better, intermediate is more stable, and the life-span is longer, so the PS method widened the pH scope of reaction system, and the acid that has reduced Fenton process adds expense.Use small molecules acid complexing agent complexing ferrous ion catalytic activation PS can control free Fe in the solution better
2+Concentration is to guarantee Fe
2+Thereby has free ferrous easily oxidized problem in the system of solubility property solution preferably.
Summary of the invention
The objective of the invention is to overcome the shortcoming and defect of above-mentioned prior art, a kind of bidirectional flow internal-circulation type PS advanced oxidation reactor and sewage water treatment method are provided, in reactor, realize the ferrous catalytic activation PS of complexing advanced oxidation processing high concentrated organic wastewater.
The present invention is achieved through the following technical solutions:
A kind of bidirectional flow internal-circulation type PS advanced oxidation reactor comprises reactor, and this reactor is hollow tank structure, establishes two positions staggered up and down and concentric inner core and urceolus in it; The upper end open of inner core, the lower end of inner core is connected with at the bottom of the reactor tank body; The urceolus upper end is connected the lower ending opening of urceolus with reactor tank body top; Reactor tank body bottom is provided with unpowered self-priming return-flow system and umbrella taper water distributor; Article one, stretch to the catalyzer chemical feed pipe of bottom by reactor tank body top, be positioned at the center of inner core, the corresponding umbrella taper medicine-distributing device that is communicated with in the lower end of catalyzer chemical feed pipe, umbrella taper medicine-distributing device is positioned within the reactor water distribution mixing region, and the other end of catalyzer chemical feed pipe stretches out outside the reactor tank body and connects dosing pump; Barrel at inner core highly locates to be equipped with annular water distribution baffle plate apart from reactor bottom 1/4; Be provided with into water mixing device in inlet area, reactor tank body bottom; The inner core top is provided with the secondary chemicals dosing plant; Be provided with vapor pipe on reactor tank body top corresponding to the position in the urceolus, the exhalant region of reactor tank body is provided with rising pipe.
Described water inlet mixing device comprises sewage water inlet pipe, oxygenant chemical feed pipe and static spiral chip mixing tank; Sewage water inlet pipe and oxygenant chemical feed pipe 90 vertical being connected of degree on horizontal plane; Static spiral chip mixing tank is arranged on sewage water inlet pipe is communicated with the place with the oxygenant chemical feed pipe rear.
Described unpowered return-flow system comprises two inner circulating tubes and water-jet self-priming assembly, and described water-jet self-priming assembly comprises cylindrical hybrid chamber, water inlet convergent jet pipe and water distribution increaser; The height of described cylindrical hybrid chamber is 1/4 of a reactor tank body internal volume height, and diameter is 1/2 of an inner core internal diameter; The tubular axis of described sewage water inlet pipe and cylindrical hybrid chamber bus coincide, and run through the bottom surface of cylindrical hybrid chamber, and the lower end of sewage water inlet pipe connects the water inlet mixing device, and the upper end connects water inlet convergent jet pipe; Described water inlet convergent jet pipe taper angle is in 20 °～30 ° scopes, the pipe range of water inlet convergent jet pipe is 0.67 times of cylindrical hybrid chamber height, the water outlet of water inlet convergent jet pipe is relative with the water-in of water distribution increaser, and the water-in and the reactor bottom surface of water inlet convergent jet pipe are positioned on the same horizontal plane; Described water distribution increaser runs through the bottom of reactor tank body, be communicated with reactor and cylindrical hybrid chamber, the flaring angle of this water distribution increaser is at 10 °～20 °, the water side of water distribution increaser is positioned at umbrella taper water distributor inside, and the awl bottom surface of the feed-water end of water distribution increaser and umbrella taper water distributor is on the same horizontal plane; Described inner circulating tube is 90 ° of bend pipes, and its feed-water end is communicated with the exhalant region of reactor, and the water side is communicated with cylindrical hybrid chamber.
At the bottom of described umbrella taper water distributor and the reactor tank body at a distance of 1cm～6cm, and by stent support ligation device tank base; Umbrella taper medicine-distributing device overlaps in vertical direction with the bus of umbrella taper water distributor, the spacing of staggered 0.5cm～3cm on the vertical direction, forms the current slit.
Described secondary chemicals dosing plant comprises an annular cloth pencil, and two vertical arms and a level are responsible for; On annular cloth pencil, be the centrosymmetry perforate with the center of circle, the aperture vertically downward, the radially two ends of annular cloth pencil are communicated with to hang by two vertical arms respectively is fixed in reactor tank body top, the other end of two vertical arms stretches out outside the reactor tank body, and externally converges the outside dosing tank of back connection by the level person in charge.
The interior circular diameter of described annular water distribution baffle plate is 0.4～0.65 times of the interior circular diameter of inner core.
A kind of sewage water treatment method, carry out according to the following steps:
One, in dosing tank, dispose sewage disposal liquid respectively:
The mass ratio of CODCr in PS solution and the sewage is 6～12:1;
When complexing agent was citric acid, used citric acid and copperas solution mass ratio were 3.5～7:1;
When complexing agent was oxalic acid, used oxalic acid and copperas solution mass ratio were 1.6～3.2:1;
The mass ratio of PS solution and copperas solution is 4.25～8.5:1;
Two, the valve on unlatching sewage water inlet pipe, oxygenant chemical feed pipe and the catalyzer chemical feed pipe, start sewage intake pump, oxygenant dosing pump and catalyzer dosing pump, sewage, sewage disposal liquid are pumped to respectively in the reactor 13, regulate the flow of pump, make the reactor waterpower residence time at 120min;
Three, behind the reaction 70min, open inner circulating tube 5 valves; Reaction 120min, water outlet, promptly finish and dispose of sewage.
The present invention has following advantage and effect with respect to prior art:
By the different waterpower fluidised form features in differential responses stage in umbrella taper water distributor, umbrella taper medicine-distributing device, inner core and the urceolus realization response device, effectively avoid short stream, realize pollutent and fully contacting rapidly of medicament and making full use of of reactor volume;
Inner circulating tube and water-jet self-priming assembly increase hydraulic detention time, realize the recycling of the intact oxygenant of unreacted, save dosing, and make the pollutent that is not degraded obtain oxygenolysis once more;
Unique umbrella taper medicine-distributing device and catalyzer chemical feed pipe, secondary chemicals dosing plant realize the catalyzer ferrous disperse rapidly with control the even and concentration of its concentration in conversion zone suitably and secondary dosing structure realize that a small amount of gradation of catalyzer ferrous adds, reduce the degree of the local excessive ferrous reduction free radical of reaction zone, improve ferrous utilization ratio, improve the efficient of the free-radical oxidn pollutent of catalysis generation simultaneously.Dosage has been saved in improvement by said structure and function, has improved the efficient of the ferrous catalytic activation PS of small molecules acid complexing advanced oxidation processes processing high concentrated organic wastewater, has reduced its cost of disposing of sewage.
Reactor of the present invention is handled at the ferrous activation of complexing PS advanced oxidation and has been solved following technical problem in the high concentrated organic wastewater process:
(1) technical problem that the common aspect ratio of advanced oxidation reactor is big, capacity utilization is low;
(2) technical problem that weak point flows, the medicament utilization ratio is low easily takes place in inside reactor;
(3) the free radical lifetime is short in the reaction process, and reactor is local excessive ferrous with pollutent competition free radical and reduce free base unit weight, causes oxygenant to be failed by effective catalysis, reacts inadequate technical problem;
(4) residual pharmacy fails to be repeated to utilize, and causes the technical problem of secondary pollution.
Description of drawings
Fig. 1 is a bidirectional flow internal-circulation type PS advanced oxidation structure of reactor master synoptic diagram of the present invention.
Fig. 2 is an A-A diagrammatic cross-section among Fig. 1.
Fig. 3 is a B-B diagrammatic cross-section among Fig. 1.
Fig. 4 is a C-C diagrammatic cross-section among Fig. 1.
A dosing of Fig. 5 and secondary dosing are to the PS(dyestuff) waste water COD removal comparison diagram.
Fig. 6 is that the variation of secondary adding consistency relative quantity is removed comparison diagram to PS waste water from dyestuff COD.
Fig. 7 adopts inner circulating tube to handle the effect contrast figure of PS wastewater oxidation degraded.
Embodiment
Below in conjunction with specific embodiment the present invention is done further concrete detailed description the in detail.
Embodiment
A kind of sewage water treatment method, mainly carry out according to the following steps:
One, in dosing tank, dispose sewage disposal liquid respectively:
COD in PS solution and the sewage
CRMass ratio be 6～12:1;
When complexing agent was citric acid, used citric acid and copperas solution mass ratio were respectively 3.5～7:1;
When complexing agent was oxalic acid, used oxalic acid and copperas solution mass ratio were respectively 1.6～3.2:1;
The mass ratio of PS solution and copperas solution is 4.25～8.5:1;
Two, the valve on unlatching sewage water inlet pipe, oxygenant chemical feed pipe and the catalyzer chemical feed pipe, start sewage intake pump, oxygenant dosing pump and catalyzer dosing pump, sewage, sewage disposal liquid are pumped to respectively in the reactor 13, regulate the flow of pump, make the reactor waterpower residence time at 120min;
Three, behind the reaction 70min, open inner circulating tube 5 valves; Reaction 120min, water outlet, promptly finish and dispose of sewage.
Specify above-mentioned implementation process in conjunction with Fig. 1～4:
First kind of embodiment: open secondary chemicals dosing plant 12, it is constant that maintenance catalyst sulfuric acid ferrous adds total amount, with the reaction zone top of part ferrous iron solution shunting by secondary chemicals dosing plant 12 input inner cores 9, ferrous sulfate mass ratio by catalyzer chemical feed pipe 11 and secondary chemicals dosing plant 12 is respectively 1/1, generates sulfate radical free radical SO so that the PS medicament carries out quadric catalysis near secondary chemicals dosing plant 12
4 -Reaction, and secondary degradation of contaminant, the COD after the secondary dosing
CrClearance can improve 8%.
Second kind of embodiment: changing by catalyzer chemical feed pipe 11 is 3/1 with the mass ratio that secondary chemicals dosing plant 12 drops into the catalyst sulfuric acid ferrous iron solution in the reactors, and with waste water from dyestuff COD
CrClearance compares, and the result shows that dosage is 1/1 COD
CrClearance is high by 2%.
A dosing of Fig. 5 and secondary dosing are to the PS(dyestuff) waste water COD removal comparison diagram.
Fig. 6 is that the variation of secondary adding consistency relative quantity is removed comparison diagram to PS waste water from dyestuff COD.
Fig. 7 adopts inner circulating tube to handle the effect contrast figure of PS wastewater oxidation degraded.
Bidirectional flow internal-circulation type PS advanced oxidation reactor of the present invention shown in Fig. 1～4, comprises reactor 13, and this reactor 13 is hollow tank structure, establishes two positions staggered up and down and concentric inner core 9 and urceolus 10 in it; The upper end open of inner core 9, the lower end of inner core 9 is connected with at the bottom of reactor 13 tank bodies; Urceolus 10 upper ends are connected the lower ending opening of urceolus 10 with reactor 13 tank bodies top; Reactor 13 tank base are provided with unpowered self-priming return-flow system and umbrella taper water distributor 7; Article one, stretch to the catalyzer chemical feed pipe 11 of bottom by reactor 13 tank body tops, be positioned at the center of inner core 9, the corresponding umbrella taper medicine-distributing device 8 that is communicated with in the lower end of catalyzer chemical feed pipe 11, umbrella taper medicine-distributing device 8 is positioned within the reactor 13 water distribution mixing regions, and the other end of catalyzer chemical feed pipe 11 stretches out outside reactor 13 tank bodies and connects dosing pump; Barrel at inner core 9 highly locates to be equipped with annular water distribution baffle plate 701 apart from reactor 13 bottoms 1/4; Be provided with into water mixing device in reactor 13 tank base inlet areas; Inner core 9 tops are provided with secondary chemicals dosing plant 12; Be provided with vapor pipe 14 on reactor 13 tank body tops corresponding to the position in the urceolus 10, the exhalant region of reactor 13 tank bodies is provided with rising pipe 15.
Above-mentioned water inlet mixing device comprises sewage water inlet pipe 1, oxygenant chemical feed pipe 2 and static spiral chip mixing tank 201; Sewage water inlet pipe 1 and oxygenant chemical feed pipe 2 90 vertical being connected of degree on horizontal plane; Static spiral chip mixing tank 201 is arranged on sewage water inlet pipe 1 is communicated with the place with oxygenant chemical feed pipe 2 rear.
Above-mentioned unpowered return-flow system comprises two inner circulating tubes 5 and water-jet self-priming assembly, and described water-jet self-priming assembly comprises cylindrical hybrid chamber 4, water inlet convergent jet pipe 3 and water distribution increaser 6; The height of described cylindrical hybrid chamber 4 is 1/4 of reactor 13 tank body internal volume height, and diameter is 1/2 of inner core 9 internal diameters; The tubular axis of described sewage water inlet pipe 1 and cylindrical hybrid chamber 4 buses coincide, and run through the bottom surface of cylindrical hybrid chamber 4, and the lower end of sewage water inlet pipe 1 connects the water inlet mixing device, and the upper end connects water inlet convergent jet pipe 3; Described water inlet convergent jet pipe 3 taper angle are in 20 °～30 ° scopes, the pipe range of water inlet convergent jet pipe 3 is 0.67 times of cylindrical hybrid chamber 4 height, the water outlet of water inlet convergent jet pipe 3 is relative with the water-in of water distribution increaser 6, and the water-in and reactor 13 bottom surfaces of water inlet convergent jet pipe 3 are positioned on the same horizontal plane; Described water distribution increaser 6 runs through the bottom of reactor 13 tank bodies, be communicated with reactor 13 and cylindrical hybrid chamber 4, the flaring angle of this water distribution increaser 6 is at 10 °～20 °, the water side of water distribution increaser 6 is positioned at umbrella taper water distributor 7 inside, and the awl bottom surface of the feed-water end of water distribution increaser 6 and umbrella taper water distributor 7 is on the same horizontal plane; Described inner circulating tube 5 is 90 ° of bend pipes, and its feed-water end is communicated with the exhalant region of reactor 13, and the water side is communicated with cylindrical hybrid chamber 4.
Above-mentioned umbrella taper water distributor 7 with at the bottom of reactor 13 tank bodies at a distance of 1cm～6cm, and by support 702 support and connection reactors 13 tank base; Umbrella taper medicine-distributing device 8 overlaps in vertical direction with the bus of umbrella taper water distributor 7, the spacing of staggered 0.5cm～3cm on the vertical direction, forms the current slit.
Above-mentioned secondary chemicals dosing plant 12 comprises an annular cloth pencil 12-1, and two vertical arm 12-2 and a level are responsible for 12-3; 12-1 is the centrosymmetry perforate with the center of circle on annular cloth pencil, the aperture vertically downward, the radially two ends of annular cloth pencil 12-1 are communicated with to hang by two vertical arm 12-2 respectively is fixed in reactor 13 tank body tops, the other end of two vertical arm 12-2 stretches out outside reactor 13 tank bodies, and is responsible for 12-3 by level and externally converges the outside dosing tank of back connection.
The interior circular diameter of above-mentioned annular water distribution baffle plate 701 is 0.4～0.65 times of inner core 10 interior circular diameters.
In the actual moving process, the waste water from dyestuff that initial COD concentration is 116mg/L is squeezed into sewage water inlet pipe 1 by pump, oxygenant is squeezed into oxygenant chemical feed pipe 2 by pump, sewage and oxygenant mix in sewage water inlet pipe 1, turbulent phenomenon occurring through after the static spiral chip mixing tank 201, mixed effect is reinforced.Then, the sewage that is mixed with oxygenant enters cylindrical hybrid chamber 4, process water inlet convergent jet pipe 3 is accelerated and delivers in the reactor 13 in cylindrical hybrid chamber 4, and then enter umbrella taper water distributor 7 zone and and surface diffusions, reach reactor 13 bottoms and be reflected between the space of the facies basialis pyramidis annulus that flows to umbrella taper water distributor 7 and reactor 13 inner cores 9 walls.Simultaneously, enter between the slit of taper medicine-distributing device 8 and umbrella taper water distributor 7 from the catalyzer citric acid complex copperas solution of catalyzer chemical feed pipe 11 in reactor 13 tops, and diffusion is come rapidly, and the cone base that arrives umbrella taper water distributor 7 forms a ring-shaped liquid film.This layer liquid film be superimposed from the liquid film of umbrella taper water distributor 7 cones because the high pressure of feed water flow, high flow rate and violent turbulent, sewage and the ferrous medicament that is mixed with the PS medicament fully stirs, spreads rapidly and uniform mixing.Sewage after mixing is evenly distributed on the upward flow road water-carrying section, and current are stirred once more when flowing through annular water distribution baffle plate 701, increase turbulence level.Subsequently, sewage continues upwards to flow flow rate of water flow〉0.055m/s, in upward flow formula reaction zone, be turbulent fluidised form, Re 〉 4000, effluent stream is crossed upward flow formula reaction zone, COD behind 12min
CrClearance reaches 51%.Enter down afterwards when the streaming reaction zone because flow velocity reduces to be the transition flow fluidised form, at this moment, flow rate of water flow 0.016＜v＜0.055m/s; 2300 Redox reaction is proceeded in＜Re＜4000, reaches following to streaming reaction zone end reaction device 13 bottoms behind the 70min, at this moment COD
CrClearance reaches 90%.Then, part of contaminated water is because the negative pressure self-priming effect of unpowered return-flow system is inhaled into inner circulating tube 5, further enter in the cylindrical hybrid chamber 4, and merge into one liquid stream from the sewage (containing the PS medicament) of sewage water inlet pipe 1, continue the redox reaction of contaminant degradation; Another part sewage is directly with the exhalant region of flowing through than minimum velocity, flow rate of water flow v＜0.015m/s; Re≤2300; current are laminar flow state; at exhalant region; pollutent is farthest degraded; throw outs such as small amounts of iron mud obtain abundant precipitate and separate and are settled down at the bottom of the reactor tank; discharge by evacuated tube 16, the sewage after being cleaned behind the 60min arrives the reactor tank deck and discharges water outlet COD through rising pipe 15
CrClearance reaches 91%～97%.
As mentioned above, just can realize the present invention preferably.
Embodiments of the present invention are not restricted to the described embodiments; other are any not to deviate from change, the modification done under spirit of the present invention and the principle, substitute, combination, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (7)
1. sewage water treatment method is characterized in that carrying out according to the following steps:
One, in dosing tank, dispose sewage disposal liquid respectively:
COD in PS solution and the sewage
CrMass ratio be 6～12:1;
When complexing agent was citric acid, used citric acid and copperas solution mass ratio were 3.5～7:1;
When complexing agent was oxalic acid, used oxalic acid and copperas solution mass ratio were 1.6～3.2:1;
The mass ratio of PS solution and copperas solution is 4.25～8.5:1;
Two, the valve on unlatching sewage water inlet pipe, oxygenant chemical feed pipe and the catalyzer chemical feed pipe, start sewage intake pump, oxygenant dosing pump and catalyzer dosing pump, sewage, sewage disposal liquid are pumped to respectively in the reactor 13, regulate the flow of pump, make the reactor waterpower residence time at 120min;
Three, behind the reaction 70min, open inner circulating tube 5 valves; Reaction 120min, water outlet, promptly finish and dispose of sewage.
2. bidirectional flow internal-circulation type PS advanced oxidation reactor, it is characterized in that: comprise reactor, this reactor is hollow tank structure, establishes two positions staggered up and down and concentric inner core and urceolus in it; The upper end open of inner core, the lower end of inner core is connected with at the bottom of the reactor tank body; The urceolus upper end is connected the lower ending opening of urceolus with reactor tank body top; Reactor tank body bottom is provided with unpowered self-priming return-flow system and umbrella taper water distributor; Article one, stretch to the catalyzer chemical feed pipe of bottom by reactor tank body top, be positioned at the center of inner core, the corresponding umbrella taper medicine-distributing device that is communicated with in the lower end of catalyzer chemical feed pipe, umbrella taper medicine-distributing device is positioned within the reactor water distribution mixing region, and the other end of catalyzer chemical feed pipe stretches out outside the reactor tank body and connects dosing pump; Barrel at inner core highly locates to be equipped with annular water distribution baffle plate apart from reactor bottom 1/4; Be provided with into water mixing device in inlet area, reactor tank body bottom; The inner core top is provided with the secondary chemicals dosing plant; Be provided with vapor pipe on reactor tank body top corresponding to the position in the urceolus, the exhalant region of reactor tank body is provided with rising pipe.
3. bidirectional flow internal-circulation type PS advanced oxidation reactor according to claim 2 is characterized in that: described water inlet mixing device comprises sewage water inlet pipe, oxygenant chemical feed pipe and static spiral chip mixing tank; Sewage water inlet pipe and oxygenant chemical feed pipe 90 vertical being connected of degree on horizontal plane; Static spiral chip mixing tank is arranged on sewage water inlet pipe is communicated with the place with the oxygenant chemical feed pipe rear.
4. bidirectional flow internal-circulation type PS advanced oxidation reactor according to claim 3, it is characterized in that: described unpowered return-flow system comprises two inner circulating tubes and water-jet self-priming assembly, and described water-jet self-priming assembly comprises cylindrical hybrid chamber, water inlet convergent jet pipe, water distribution increaser; The height of described cylindrical hybrid chamber is 1/4 of a reactor tank body internal volume height, and diameter is 1/2 of an inner core internal diameter; The tubular axis of described sewage water inlet pipe and cylindrical hybrid chamber bus coincide, and run through the bottom surface of cylindrical hybrid chamber, and the lower end of sewage water inlet pipe connects the water inlet mixing device, and the upper end connects water inlet convergent jet pipe; Described water inlet convergent jet pipe taper angle is in 20 °～30 ° scopes, the pipe range of water inlet convergent jet pipe is 0.67 times of cylindrical hybrid chamber height, the water outlet of water inlet convergent jet pipe is relative with the water-in of water distribution increaser, and the water-in and the reactor bottom surface of water inlet convergent jet pipe are positioned on the same horizontal plane; Described water distribution increaser runs through the bottom of reactor tank body, be communicated with reactor and cylindrical hybrid chamber, the flaring angle of this water distribution increaser is at 10 °～20 °, the water side of water distribution increaser is positioned at umbrella taper water distributor inside, and the awl bottom surface of the feed-water end of water distribution increaser and umbrella taper water distributor is on the same horizontal plane; Described inner circulating tube is 90 ° of bend pipes, and its feed-water end is communicated with the exhalant region of reactor, and the water side is communicated with cylindrical hybrid chamber.
5. bidirectional flow internal-circulation type PS advanced oxidation reactor according to claim 2 is characterized in that: at the bottom of described umbrella taper water distributor and the reactor tank body at a distance of 1cm～6cm, and by stent support ligation device tank base; Umbrella taper medicine-distributing device overlaps in vertical direction with the bus of umbrella taper water distributor, the spacing of staggered 0.5cm～3cm on the vertical direction, forms the current slit.
6. bidirectional flow internal-circulation type PS advanced oxidation reactor according to claim 2, it is characterized in that: described secondary chemicals dosing plant comprises an annular cloth pencil, two vertical arms and a level are responsible for; On annular cloth pencil, be the centrosymmetry perforate with the center of circle, the aperture vertically downward, the radially two ends of annular cloth pencil are communicated with to hang by two vertical arms respectively is fixed in reactor tank body top, the other end of two vertical arms stretches out outside the reactor tank body, and externally converges the outside dosing tank of back connection by the level person in charge.
7. bidirectional flow internal-circulation type PS advanced oxidation reactor according to claim 2 is characterized in that: the interior circular diameter of described annular water distribution baffle plate is 0.4～0.65 times of the interior circular diameter of inner core.
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