CN103771625A - Device and method for treating pulping wastewater by Fenton catalytic oxidation method - Google Patents
Device and method for treating pulping wastewater by Fenton catalytic oxidation method Download PDFInfo
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- CN103771625A CN103771625A CN201410035540.3A CN201410035540A CN103771625A CN 103771625 A CN103771625 A CN 103771625A CN 201410035540 A CN201410035540 A CN 201410035540A CN 103771625 A CN103771625 A CN 103771625A
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Abstract
The invention discloses a device and method for treating pulping wastewater by a Fenton catalytic oxidation method. The device comprises a water collecting tank, a catalytic oxidation tower, a neutralization tank, a coagulative precipitation tower, a clean water tank and a medicament preparation system, wherein a balance regulating tank at the top of the catalytic oxidation tower is connected with the water collecting tank through a pipeline; the balance regulating tank is connected with a water distribution pipe at the bottom of a fluidized catalytic reaction column of the catalytic oxidation tower through a pipeline; a circulating water outlet tank is connected with the water distribution pipe through a pipeline; the neutralization tank is connected with a water distribution pipe of the coagulative precipitation tower through a pipeline; an outlet water tank is arranged on the external wall of the upper part of the coagulative precipitation tower, and the top of the coagulative precipitation tower is connected with the outlet water tank through an overflow port. The method comprises the steps of carrying out balance regulating treatment, carrying out fluidized catalytic oxidation treatment, carrying out coagulative precipitation and purifying. According to the device and the method, by using efficient mass transfer efficiency under fluidized conditions, a relatively high wastewater treatment effect is achieved under the condition that the dosage of hydrogen peroxide and ferrous ions is relatively low, so that the wastewater treatment efficiency is increased, and meanwhile, the amount of generated sludge is reduced.
Description
Technical field
The present invention relates to a kind of pulp and paper effluent treatment method, be specifically related to a kind of device and method of Fenton catalytic oxidation processing pulp-making waste-water.
Background technology
Pulp and paper industry is one of important source of waste water and pollutant emission.Current, generally take the technique of one-level materialization processing and two stage biological treatment combination to process paper-making effluent, effectively reduce the pollution load of waste water.But, in pulp-making waste-water, contain the organism of certain density difficult for biological degradation, suppress the effect of biological treatment, cause waste water can not reach national emission standard after two stage biological is processed, still contain the organism of higher concentration, thereby must carry out further advanced treatment, to alleviate the impact on receiving water body and ecotope.
Fenton catalytic oxidation is that employing ferrous ion is catalyzer, in reaction system, ferrous ion catalyzing hydrogen peroxide decomposes generation hydroxyl radical free radical OH, again by OH be oxidized, organic pollutant in mineralising waste water, thereby reach the object of the pollutent in remarkable removal waste water.Fenton catalytic oxidation comprises in fact two continuous steps: under sour environment, ferrous ion catalyzing hydrogen peroxide decomposes generation OH, by the organism in OH oxidative degradation, mineralising, removal waste water; Then, regulate the pH value of reaction system to alkalescence, iron ion generates molysite deposition flco under alkaline condition, removes organic pollutant, suspended substance and other pollutents in waste water by the mode of absorption, coagulation, precipitation.Fenton catalytic oxidation is in current engineering, to apply more high-level oxidation technology, have the advantages that speed of response is fast, reaction conditions is gentle and treatment effect is good, become degraded and removed one of major technique of the refractory organic in waste water, there is stable good result.But traditional Fenton catalyzed oxidation technology exists the problem that chemicals usage is large, processing cost is high, and in treating processes, has produced a large amount of mud.
Summary of the invention
The object of the invention is to overcome the deficiency that existing common Fenton oxidation technology exists, a kind of device and method that reduces chemicals usage, minimizing chemical sludge output, improves the Fenton catalytic oxidation processing pulp-making waste-water of waste water treatment efficiency is provided.
Object of the present invention is achieved through the following technical solutions:
Fenton catalytic oxidation is processed the device of pulp-making waste-water, comprises water collecting basin 1, catalyzed oxidation tower 6, neutralization tank 19, coagulating sedimentation tower 23, clean water basin 25 and medicament preparation system 26;
The balanced regulating tank 7 at described catalyzed oxidation tower 6 tops is connected with water collecting basin 1 by pipeline; Described balanced regulating tank 7 with on the connecting tube of water collecting basin 1, be provided with the first water pump 2, the first line mixer 3, second pipe mixing tank 4 and the under meter 5 that are connected successively;
Described the first line mixer 3 is connected with the outlet of the acid solution storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the first described line mixer 3 and the acid solution storagetank outlet of medicament preparation system 26, be provided with volume pump 28;
Described second pipe mixing tank 4 is connected with the outlet of the catalyzer storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the catalyzer storagetank outlet of described second pipe mixing tank 4 and medicament preparation system 26, be provided with volume pump 27;
Described balanced regulating tank 7 is connected with the water distributor 11 of fluidization catalytic reaction post 12 bottoms of catalyzed oxidation tower 6 by pipeline; Described balanced regulating tank 7 with on the connecting tube of water distributor 11, be provided with the under meter 9, the second water pump 8 and the 3rd line mixer 10 that are connected successively;
Described the 3rd line mixer 10 is connected with the outlet of the hydrogen peroxide storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the 3rd described line mixer 10 and the hydrogen peroxide storagetank outlet of medicament preparation system 26, be provided with volume pump 29;
The external wall of upper portion of described fluidization catalytic reaction post 12 is provided with and recycles tank 17, recycles tank 17 and is connected with water distributor 11 by pipeline; On the described connecting tube that recycles tank 17 and water distributor 11, be provided with the under meter 16 and the water circulating pump 15 that are connected successively; The described tank 17 that recycles is also connected with the water-in of neutralization tank 19 by outlet conduit 35, is also provided with under meter 18 on outlet conduit 35;
Described neutralization tank 19 is connected with the water distributor of coagulating sedimentation tower 23 by pipeline, on the connecting tube of described neutralization tank 19 and the water distributor of coagulating sedimentation tower 23, is provided with the 3rd water pump 21 and the 4th line mixer 22 that are connected successively;
In described neutralization tank 19, be provided with whipping appts 20, neutralization tank 19 is connected with the outlet of the alkali lye storagetank of medicament preparation system 26 by pipeline, and on connecting tube, is provided with volume pump 30;
Described the 4th line mixer 22 is connected with the outlet of the flocculation agent storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the 4th described line mixer 22 and the flocculation agent storagetank outlet of medicament preparation system 26, be provided with volume pump 31;
In described coagulating sedimentation tower 23 external wall of upper portion, be provided with effluent trough 24, coagulating sedimentation tower 23 tops are connected with effluent trough 24 by overflow port;
Described effluent trough 24 is connected with clean water basin 25 by rising pipe 36, and effluent trough 24 is also connected with clean water basin 25 by upflow tube 37;
In described balanced regulating tank 7, be provided with several piece dividing plate separated from one another;
In the fluidization catalytic reaction post 12 of described catalyzed oxidation tower 6, be also provided with fluidic plate 13 and particle input port 32, it is characterized in that adding solid granule 14 by particle input port 32 to fluidization catalytic reaction post 12; Be further characterized in that described fluidic plate 13 is for being provided with the porous fanning strip of taper hole;
Described coagulating sedimentation tower 23 is provided with fluidization reaction zone, flco reaction of propagation district, flco separation and precipitation area, mud enrichment region and the clarification pool of circulation successively.
Described balanced regulating tank 7 is connected with water collecting basin 1 by upflow tube 33, and the described tank 17 that recycles is connected with water collecting basin 1 by upflow tube 34.
Fenton catalytic oxidation is processed the method for pulp-making waste-water, it is characterized in that comprising the following steps and processing condition:
1 balanced adjusting processed: the waste water in water collecting basin 1 is transported to the balanced regulating tank 7 at catalyzed oxidation tower 6 tops by the first water pump 2, adds successively H simultaneously by the first line mixer 3 and second pipe mixing tank 4
2sO
4with with pending water in the COD mass ratio FeSO that is 1.5～2.5:1
47H
2o.In balanced regulating tank 7, be provided with several piece dividing plate separated from one another, waste water successively by each dividing plate, makes waste water, H with pulling flow type
2sO
4and FeSO
47H
2o obtains fully, evenly mixes in by line mixer 3,4 and balanced regulating tank 7.Waste water is 10～15 minutes in the residence time of balanced regulating tank 7, and the pH of exit waste water is 3～4.
2 fluidized catalytic oxide treatment: adopt the second water pump 8 to deliver into the water distributor 11 of fluidization catalytic reaction post 12 bottoms by pipeline through the balanced waste water of processing that regulates, simultaneously by the 3rd line mixer 10 add with pending water in the COD mass ratio hydrogen peroxide that is 1.5～3.5:1, drop into solid granule 14 by particle input port 32 to fluidization catalytic reaction post 12; The waste water flowing out from water distributor 11 upwards flows in the bottom of fluidization catalytic reaction post 12 with certain flow velocity, makes solid granule 14 be fluidized state, carries out fluidized catalytic oxidizing reaction; And the fluidic plate 13 that fluidization catalytic reaction post 12 bottoms arrange makes waste water present the flow states such as turbulent flow, mixed flow, whirlpool, effectively strengthen the fluidization degree of fluidization catalytic reaction post 12 bottoms, be conducive to organism, hydrogen peroxide, H in waste water
2sO
4and FeSO
47H
2the rapid mixing of O, reaction, improved the speed of catalytic oxidation.
Waste water arrives the top of fluidization catalytic reaction post 12 after fluidized catalytic oxide treatment, along with the increase of flow cross-sectional area, on waste water, Flow Velocity declines, the movement velocity of solid granule 14 constantly declines, and last waste water separates with solid granule by effluent weir and overflows to and recycle tank 17;
Recycle part water in tank 17 delivers into fluidization catalytic reaction post 12 bottoms through pipeline water distributor 11 by water circulating pump 15, mix with the waste water from balanced regulating tank 7, to maintain the upper Flow Velocity of waste water in fluidization reaction column 12, make the abundant fluidization of solid granule; Another part water recycling in tank 17 enters neutralization tank 19 by the effluent weir overflow at top;
In described step 2, waste water passes through successively the processing of strong fluidization hybrid reaction district, fluidized catalytic oxidation reaction zone and solid-liquid displacement zone in the fluidization catalytic reaction post 12 of catalyzed oxidation tower 6.
3 coagulating sedimentation and purification: the waste water through catalytic oxidation treatment enters neutralization tank 19 by recycling tank 17, volume pump 30 adds alkali lye in neutralization tank simultaneously, regulates pH value to 7.5～8 of waste water.Then, be transported to the water distributor of coagulating sedimentation tower 23 through pipeline by the 3rd water pump 21, enter the fluidization reaction zone of coagulating sedimentation tower 23, in waste water, add flocculation agent by the 4th line mixer 22 simultaneously; In wastewater volume, the add-on of flocculation agent is 1.5～2mg/L.In fluidization reaction zone, micro-floccule starts to form, and maintains certain current lift velocity, makes micro-floccule in fluidized state, makes waste water fully mix, contact, react with flocculation agent;
Enter flco reaction of propagation district from fluidization reaction zone waste water out, the flow velocity of waste water declines, and fluidization weakens gradually, and micro-floccule is phase mutual coagulation under flocculation agent effect, forms larger flco and starts to sink; Then, waste water enters flco separation and precipitation area;
In flco separation and precipitation area, the flow velocity that waste water rises further declines, flco sinks to mud enrichment region gradually, form precipitation concentrated gradually at reactor bottom, and waste water flow to the clarification pool at coagulating sedimentation tower 23 tops on slowly, enter effluent trough 24 by overflow weir overflow, then be transported to clean water basin 25 by pipeline 35, complete the Fenton catalytic oxidation treatment process of waste water.
Compared with prior art, tool has the following advantages in the present invention:
1, the present invention utilizes fluidized catalytic oxidation technology to replace traditional Fenton oxidizing process, utilize efficient mass-transfer efficiency under fluidization condition, realize the higher position reason effect of waste water under lower hydrogen peroxide and ferrous ion dosage condition, improve the efficiency of wastewater treatment, reduced the growing amount of mud simultaneously.Waste water passes through successively the processing of strong fluidization hybrid reaction district, fluidized catalytic oxidation reaction zone and solid-liquid displacement zone in catalytic oxidation unit, make waste water and Fenton reagent under fluidization condition fully, evenly mix, carry out fluidised catalytic oxidation, effectively improve the speed of mass-transfer efficiency and chemical reaction, improved the effect of Organic Pollutants in Wastewater oxidative degradation; Can reduce Fenton using amount of reagent, reduce the output of mud in later stage coagulation process simultaneously.
2, the waste water after fluidized catalytic oxidizing reaction of the present invention under fluidization condition and alkali lye, flocculation agent carry out fully, evenly mix, reaction, has effectively improved the efficiency of mass transfer, has strengthened the effect of coagulating waste water precipitation; On the other hand, waste water has been realized the object of coagulation, precipitation, purification in coagulating sedimentation tower simultaneously, has effectively improved the efficiency of wastewater treatment, has shortened the flow process of wastewater treatment.
3, hydrogen peroxide of the present invention joins in reaction system progressively, continuously, effectively maintain stable, higher concentration of hydrogen peroxide in fluidized catalytic oxidizing tower, guarantee the generation of hydroxyl radical free radical continuous and effective, guarantee higher catalytic oxidation speed, can effectively reduce the decomposition of hydrogen peroxide, reduce the demand of hydrogen peroxide simultaneously.
Accompanying drawing explanation
Fig. 1 is the schematic diagram that this Fenton catalytic oxidation is processed the method for pulp-making waste-water.
Embodiment
Below in conjunction with drawings and Examples, the invention will be further described, but the scope of protection of present invention is not limited to the scope that embodiment explains.
As shown in Figure 1, a kind of Fenton catalytic oxidation is processed the device of pulp-making waste-water, comprises water collecting basin 1, catalyzed oxidation tower 6, neutralization tank 19, coagulating sedimentation tower 23, clean water basin 25 and medicament preparation system 26; Medicament preparation system is prepared and/or has been stored acid, catalyzer, alkali, flocculant solution and hydrogen peroxide, and is joined in waste water and gone by volume pump respectively.
The balanced regulating tank 7 at catalyzed oxidation tower 6 tops is connected with water collecting basin 1 by pipeline; On the connecting tube of water collecting basin 1 and balanced regulating tank 7, be provided with the first water pump 2, the first line mixer 3, second pipe mixing tank 4 and the first flow meter 5 that connect successively; The first line mixer 3 is connected with the outlet of the acid solution storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the acid solution storagetank outlet of the first line mixer 3 and medicament preparation system 26, be provided with the second volume pump 28; Second pipe mixing tank 4 is connected with the outlet of the catalyzer storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the catalyzer storagetank outlet of second pipe mixing tank 4 and medicament preparation system 26, be provided with the first volume pump 27;
Balanced regulating tank 7 is connected with the water distributor 11 of fluidization catalytic reaction post 12 bottoms of catalyzed oxidation tower 6 by pipeline; On the connecting tube of balanced regulating tank 7 and water distributor 11, be provided with the second under meter 9, the second water pump 8 and the 3rd line mixer 10 that are connected successively; The 3rd line mixer 10 is connected with the outlet of the hydrogen peroxide storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the hydrogen peroxide storagetank outlet of the 3rd line mixer 10 and medicament preparation system 26, be provided with the 3rd volume pump 29;
The external wall of upper portion of fluidization catalytic reaction post 12 is provided with and recycles tank 17, recycles tank 17 and is connected with water distributor 11 by pipeline; Recycle on the connecting tube of tank 17 and water distributor 11 and be provided with the 3rd under meter 16 and the water circulating pump 15 that are connected successively; Recycle tank 17 and be also connected with the water-in of neutralization tank 19 by outlet conduit 35, on outlet conduit 35, be also provided with the 4th under meter 18;
Neutralization tank 19 is connected with the water distributor of coagulating sedimentation tower 23 by pipeline, on the connecting tube of neutralization tank 19 and the water distributor of coagulating sedimentation tower 23, is provided with the 3rd water pump 21 and the 4th line mixer 22 that are connected successively; In neutralization tank 19, be provided with whipping appts 20, neutralization tank 19 is connected with the outlet of the alkali lye storagetank of medicament preparation system 26 by pipeline, and on connecting tube, is provided with the 4th volume pump 30; The 4th line mixer 22 is connected with the outlet of the flocculation agent storagetank of medicament preparation system 26 by pipeline; On the connecting tube of the flocculation agent storagetank outlet of the 4th line mixer 22 and medicament preparation system 26, be provided with the 5th volume pump 31;
In coagulating sedimentation tower 23 external wall of upper portion, be provided with effluent trough 24, coagulating sedimentation tower 23 tops are connected with effluent trough 24 by overflow port; Effluent trough 24 is connected with clean water basin 25 by rising pipe 36, and effluent trough 24 is also connected with clean water basin 25 by the 3rd upflow tube 37;
In balanced regulating tank 7, be provided with several piece dividing plate separated from one another;
In the fluidization catalytic reaction post 12 of catalyzed oxidation tower 6, be also provided with fluidic plate 13 and particle input port 32, add solid granule 14 by particle input port 32 to fluidization catalytic reaction post 12; Fluidic plate 13 is for being provided with the porous fanning strip of taper hole;
Coagulating sedimentation tower 23 is provided with fluidization reaction zone, flco reaction of propagation district, flco separation and precipitation area, mud enrichment region and the clarification pool of circulation successively.
Balanced regulating tank 7 is connected with water collecting basin 1 by the first upflow tube 33, recycles tank 17 and is connected with water collecting basin 1 by the second upflow tube 34.
The present embodiment process southern weedtree slurry D0/C ?the waste water of (EO) PD1 bleaching effluent after acidication and Wastewater Treated by Activated Sludge Process, the COD of waste water
crfor 350mg/L, BOD
5for 55mg/L, colourity is 490C.U..
The Fenton catalytic oxidation of application said apparatus is processed the method for pulp-making waste-water, comprises the following steps and processing condition:
1) balanced adjusting processed: the waste water in water collecting basin 1 is transported to the balanced regulating tank 7 at catalyzed oxidation tower 6 tops by the first water pump 2, adds respectively H simultaneously by the first line mixer 3 and second pipe mixing tank 4
2sO
4and FeSO
47H
2o.In balanced regulating tank 7, be provided with several piece dividing plate separated from one another, waste water successively by each dividing plate, makes waste water, H with pulling flow type
2sO
4and FeSO
47H
2o obtains fully, evenly mixes in by the first line mixer 3, second pipe mixing tank 4 and balanced regulating tank 7; Waste water is 10～15 minutes in the residence time of balanced regulating tank 7; By pending wastewater volume, FeSO
47H
2the add-on of O is 875mg/L.
2) fluidized catalytic oxide treatment: adopt the second water pump 8 to deliver into the water distributor 11 of fluidization catalytic reaction post 12 bottoms by pipeline through the balanced waste water of processing that regulates, add hydrogen peroxide by the 3rd line mixer 10 simultaneously, in wastewater volume, the add-on control of superoxol in waste water is 1225mg/L; Drop into fluidization catalytic reaction post 12 the small-particle quartz sand 14 that particle diameter is 0.5～1.5mm by particle input port 32; The waste water flowing out from water distributor 11 upwards flows in the bottom of fluidization catalytic reaction post 12 with the flow velocity of 45～65m/h, makes small-particle quartz sand 14 be fluidized state, carries out fluidized catalytic oxidizing reaction; And the fluidic plate 13 that fluidization catalytic reaction post 12 bottoms arrange makes waste water present the flow states such as turbulent flow, mixed flow, whirlpool, effectively strengthen the fluidization degree of fluidization catalytic reaction post 12 bottoms, be conducive to organism, hydrogen peroxide, H in waste water
2sO
4and FeSO
47H
2the rapid mixing of O, reaction, improved the speed of catalytic oxidation.
Waste water arrives the top of fluidization catalytic reaction post 12 after fluidized catalytic oxide treatment, along with the increase of flow cross-sectional area, on waste water, Flow Velocity declines, and the movement velocity of quartz sand particle 14 constantly declines, and last waste water separates with quartz sand by effluent weir and overflows to and recycle tank 17;
Recycle part (1/2 ?2/3 quality) water in tank 17 delivers into fluidization catalytic reaction post 12 bottoms through pipeline water distributor 11 by water circulating pump 15, mix with the waste water from balanced regulating tank 7, to maintain the upper Flow Velocity of waste water in fluidization reaction column 12, make the abundant fluidization of small-particle quartz sand; Another part water (1/3 ?1/2 quality) recycling in tank 17 enters neutralization tank 19 by the effluent weir overflow at top;
Waste water passes through successively the processing of strong fluidization hybrid reaction district, fluidized catalytic oxidation reaction zone and solid-liquid displacement zone in the fluidization catalytic reaction post 12 of catalyzed oxidation tower 6.
3) coagulating sedimentation and purification: enter neutralization tank 19, the four volume pumps 30 add sodium hydroxide solution in neutralization tank 19 by recycling tank 17 through the waste water of catalytic oxidation treatment.Then, be transported to the water distributor of coagulating sedimentation tower 23 by the 3rd water pump 21 through pipeline, enter the fluidization reaction zone of coagulating sedimentation tower 23, in waste water, add flocculation agent polyacrylamide by the 4th line mixer 22, in wastewater volume, the add-on of polyacrylamide is 1.5mg/L; In fluidization reaction zone, micro-floccule starts to form, and maintains current lift velocity for (25～45) m/h, makes micro-floccule in fluidized state, makes waste water fully mix, contact, react with flocculation agent;
Enter flco reaction of propagation district from fluidization reaction zone waste water out, the flow velocity of waste water declines, and fluidization weakens gradually, and micro-floccule is phase mutual coagulation under flocculation agent effect, forms larger flco and starts to sink; Then, waste water enters flco separation and precipitation area; In flco separation and precipitation area, the flow velocity that waste water rises further declines, flco sinks down into mud enrichment region gradually, form precipitation concentrated gradually at reactor bottom, and waste water flow to the clarification pool at coagulating sedimentation tower 23 tops on slowly, enter effluent trough 24 by overflow weir overflow, then be transported to clean water basin 25 by rising pipe 36, complete the Fenton catalytic oxidation treatment process of waste water.
After testing, after processing, the COD of waste water
crfor 75mg/L, colourity is 80C.U..And take conventional Fenton treatment process, the COD of processed waste water
cr120 ?between 150mg/L, colourity be 120 ?170C.U., and processing cost is higher.
The present embodiment except following with embodiment 1: the device that a kind of Fenton catalytic oxidation is processed pulp-making waste-water for the treatment of southern weedtree slurry D0/C ?the waste water of (EO) PD1 bleaching effluent after acidication and Wastewater Treated by Activated Sludge Process, the COD of waste water
crfor 310mg/L, colourity is 530C.U.; In the present embodiment, in wastewater volume, FeSO
47H
2the add-on of O is 465mg/L, and hydrogen peroxide add-on is 930mg/L, and the add-on of polyacrylamide is 1.8mg/L.After treatment, the COD of waste water
crfor 95mg/L, colourity is 100C.U..And take conventional Fenton treatment process, the COD of processed waste water
cr120 ?between 150mg/L, colourity be 120 ?170C.U., and processing cost is higher.
Embodiment 3
The present embodiment except following with embodiment 1: the device that a kind of Fenton catalytic oxidation is processed pulp-making waste-water for the treatment of certain tobacco sheet enterprise waste water generated during paper-making process reconstituted-tobacco production through UASB and SBR waste water after treatment, the COD of waste water
crfor 550mg/L, colourity is 1900C.U.; In the present embodiment, in wastewater volume, FeSO
47H
2the add-on of O is 1100mg/L, and hydrogen peroxide add-on is 825mg/L, and the add-on of polyacrylamide is 2.0mg/L.After treatment, the COD of waste water
crfor 180mg/L, colourity is 280C.U..And take conventional Fenton treatment process, the COD of processed waste water
cr230 ?between 260mg/L, colourity be 400 ?480C.U., and processing cost is higher.
Claims (5)
1.Fenton catalytic oxidation is processed the device of pulp-making waste-water, it is characterized in that, comprises water collecting basin, catalyzed oxidation tower, neutralization tank, coagulating sedimentation tower, clean water basin and medicament preparation system; The balanced regulating tank of catalyzed oxidation top of tower is connected with water collecting basin by pipeline; On the connecting tube of water collecting basin and balanced regulating tank, be provided with the first water pump, the first line mixer, second pipe mixing tank and the first flow meter that connect successively; The first line mixer is connected with the outlet of the acid solution storagetank of medicament preparation system by pipeline; On the connecting tube of the acid solution storagetank outlet of the first line mixer and medicament preparation system, be provided with the second volume pump; Second pipe mixing tank is connected with the outlet of the catalyzer storagetank of medicament preparation system by pipeline; On the connecting tube of the catalyzer storagetank outlet of second pipe mixing tank and medicament preparation system, be provided with the first volume pump;
Described balanced regulating tank is connected with the water distributor of the fluidization catalytic reaction column bottom of catalyzed oxidation tower by pipeline; On the connecting tube of balanced regulating tank and water distributor, be provided with the second under meter, the second water pump and the 3rd line mixer that are connected successively; The 3rd line mixer is connected with the outlet of the hydrogen peroxide storagetank of medicament preparation system by pipeline; On the connecting tube of the hydrogen peroxide storagetank outlet of the 3rd line mixer and medicament preparation system, be provided with the 3rd volume pump;
The external wall of upper portion of described fluidization catalytic reaction post is provided with and recycles tank, recycles tank and is connected with water distributor by pipeline; Recycle on the connecting tube of tank and water distributor and be provided with the 3rd under meter and the water circulating pump being connected successively; Recycle tank and be also connected with the water-in of neutralization tank by outlet conduit, on outlet conduit, be also provided with the 4th under meter;
Described neutralization tank is connected with the water distributor of coagulating sedimentation tower by pipeline, on the connecting tube of neutralization tank and the water distributor of coagulating sedimentation tower, is provided with the 3rd water pump and the 4th line mixer that are connected successively; In neutralization tank, be provided with whipping appts, neutralization tank is connected with the outlet of the alkali lye storagetank of medicament preparation system by pipeline, and on connecting tube, is provided with the 4th volume pump; The 4th line mixer is connected with the outlet of the flocculation agent storagetank of medicament preparation system by pipeline; On the connecting tube of the flocculation agent storagetank outlet of the 4th line mixer and medicament preparation system, be provided with the 5th volume pump;
In described coagulating sedimentation tower external wall of upper portion, be provided with effluent trough, coagulating sedimentation top of tower is connected with effluent trough by overflow port; Effluent trough is connected with clean water basin by rising pipe, and effluent trough is also connected with clean water basin by the 3rd upflow tube;
In the fluidization catalytic reaction post of described catalyzed oxidation tower, be also provided with fluidic plate and particle input port;
Described balanced regulating tank is connected with water collecting basin by the first upflow tube.
2. Fenton catalytic oxidation according to claim 1 is processed the device of pulp-making waste-water, it is characterized in that, is provided with several piece dividing plate separated from one another in described balanced regulating tank.
3. Fenton catalytic oxidation according to claim 1 is processed the device of pulp-making waste-water, it is characterized in that, described fluidic plate is the porous fanning strip that is provided with taper hole.
4. Fenton catalytic oxidation according to claim 1 is processed the device of pulp-making waste-water, it is characterized in that, described in recycle tank and be connected with water collecting basin by the second upflow tube.
Application rights require 1 ?the Fenton catalytic oxidation that installs described in 4 any one process the method for pulp-making waste-water, it is characterized in that comprising the following steps and processing condition:
1) balanced adjusting processed: the waste water in water collecting basin is transported to the balanced regulating tank of catalyzed oxidation top of tower by the first water pump, adds respectively H simultaneously by the first line mixer and second pipe mixing tank
2sO
4and FeSO
47H
2o; Waste water is 10～15 minutes in the residence time of balanced regulating tank; The FeSO adding
47H
2in O and pending water, COD mass ratio is 1.5～2.5:1; The pH of exit waste water is 3～4;
2) fluidized catalytic oxide treatment: adopt the second water pump to deliver into the water distributor of fluidization catalytic reaction column bottom by pipeline through the balanced waste water of processing that regulates, by the 3rd line mixer add with pending water in the COD mass ratio hydrogen peroxide that is 1.5～3.5:1, drop into fluidization catalytic reaction post the small-particle quartz sand that particle diameter is 0.5～1.5mm by particle input port; The waste water flowing out from water distributor upwards flows in the bottom of fluidization catalytic reaction post with the flow velocity of 45～65m/h, makes small-particle quartz sand be fluidized state, carries out fluidized catalytic oxidizing reaction; Waste water arrives the top of fluidization catalytic reaction post after fluidized catalytic oxide treatment, and waste water separates by effluent weir and overflows to and recycle tank with quartz sand; Recycle part water in tank delivers into fluidization catalytic reaction column bottom through pipeline water distributor by water circulating pump, mix with the waste water from balanced regulating tank, to maintain the upper Flow Velocity of waste water in fluidization reaction column, make the abundant fluidization of small-particle quartz sand; Another part water recycling in tank enters neutralization tank by the effluent weir overflow at top;
3) coagulating sedimentation and purification: the waste water through catalytic oxidation treatment enters neutralization tank by recycling tank, and the 4th volume pump adds sodium hydroxide solution in neutralization tank, pH value to 7.5～8 of adjusting waste water; Then, be transported to the water distributor of coagulating sedimentation tower by the 3rd water pump through pipeline, enter the fluidization reaction zone of coagulating sedimentation tower, add flocculation agent polyacrylamide by the 4th line mixer in waste water, the add-on of polyacrylamide is 1.5～2mg/L; In fluidization reaction zone, micro-floccule starts to form, and maintains current lift velocity for (25～45) m/h; Enter flco reaction of propagation district from fluidization reaction zone waste water out, the flow velocity of waste water declines, and fluidization weakens gradually, and micro-floccule is phase mutual coagulation under flocculation agent effect, forms larger flco and starts to sink; Then, waste water enters flco separation and precipitation area; In flco separation and precipitation area, the flow velocity that waste water rises further declines, flco sinks down into mud enrichment region gradually, form precipitation concentrated gradually at reactor bottom, on waste water, flow to the clarification pool of coagulating sedimentation top of tower, enter effluent trough by overflow weir overflow, then be transported to clean water basin by rising pipe, complete the Fenton catalytic oxidation treatment process of waste water.
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| CN201410035540.3A CN103771625B (en) | 2014-01-24 | 2014-01-24 | Device and method for treating pulping wastewater by Fenton catalytic oxidation method |
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|---|---|---|---|
| CN201410035540.3A CN103771625B (en) | 2014-01-24 | 2014-01-24 | Device and method for treating pulping wastewater by Fenton catalytic oxidation method |
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| CN103771625A true CN103771625A (en) | 2014-05-07 |
| CN103771625B CN103771625B (en) | 2014-12-31 |
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| CN104445743A (en) * | 2014-12-15 | 2015-03-25 | 王全勇 | Two-stage catalytic oxidation wastewater treatment system |
| CN105000718A (en) * | 2015-08-11 | 2015-10-28 | 湛江晨鸣浆纸有限公司 | Pulp paper wastewater treatment process |
| CN105268487A (en) * | 2014-07-24 | 2016-01-27 | 艾特克控股集团有限公司 | Preparation method and applications of supported iron oxide catalyst carrier |
| CN106315992A (en) * | 2016-10-14 | 2017-01-11 | 华南理工大学 | Papermaking-process reconstituted tobacco wastewater advanced treatment device and wastewater treatment method thereof |
| CN106348536A (en) * | 2016-10-14 | 2017-01-25 | 华南理工大学 | Fenton synergistic ozone wastewater treatment device and wastewater treatment method thereof |
| CN106365348A (en) * | 2016-10-14 | 2017-02-01 | 华南理工大学 | Fenton cooperated ozone fluidized catalytic oxidation waste water treatment device and waste water treatment method thereof |
| CN106430826A (en) * | 2016-10-14 | 2017-02-22 | 华南理工大学 | Efficient wastewater treatment device for papermaking process tobacco leaf regeneration and wastewater treatment method thereof |
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| CN107311338A (en) * | 2016-04-26 | 2017-11-03 | 中国石油化工股份有限公司 | A kind of processing method of glycol production waste water |
| CN108117196A (en) * | 2018-02-01 | 2018-06-05 | 北京桑德环境工程有限公司 | Leather waste water advanced treatment system and method |
| CN108178361A (en) * | 2016-12-08 | 2018-06-19 | 中国科学院大连化学物理研究所 | The reverse osmosis combined treatment process for generating strong brine in a kind of coal chemical industrial waste water reuse |
| CN114772795A (en) * | 2022-05-25 | 2022-07-22 | 福建省金皇环保科技有限公司 | Catalytic oxidation coagulating sedimentation integrated sewage treatment process |
| CN115571969A (en) * | 2022-11-10 | 2023-01-06 | 华夏碧水环保科技股份有限公司 | Fenton reactor |
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| CN105268487A (en) * | 2014-07-24 | 2016-01-27 | 艾特克控股集团有限公司 | Preparation method and applications of supported iron oxide catalyst carrier |
| CN105268487B (en) * | 2014-07-24 | 2018-03-02 | 艾特克控股集团有限公司 | A kind of preparation method and applications of loading type ferric oxide catalyst carrier |
| CN104445743A (en) * | 2014-12-15 | 2015-03-25 | 王全勇 | Two-stage catalytic oxidation wastewater treatment system |
| CN105000718A (en) * | 2015-08-11 | 2015-10-28 | 湛江晨鸣浆纸有限公司 | Pulp paper wastewater treatment process |
| CN107311338A (en) * | 2016-04-26 | 2017-11-03 | 中国石油化工股份有限公司 | A kind of processing method of glycol production waste water |
| CN106315992A (en) * | 2016-10-14 | 2017-01-11 | 华南理工大学 | Papermaking-process reconstituted tobacco wastewater advanced treatment device and wastewater treatment method thereof |
| CN106430826A (en) * | 2016-10-14 | 2017-02-22 | 华南理工大学 | Efficient wastewater treatment device for papermaking process tobacco leaf regeneration and wastewater treatment method thereof |
| CN106365348A (en) * | 2016-10-14 | 2017-02-01 | 华南理工大学 | Fenton cooperated ozone fluidized catalytic oxidation waste water treatment device and waste water treatment method thereof |
| CN106348536A (en) * | 2016-10-14 | 2017-01-25 | 华南理工大学 | Fenton synergistic ozone wastewater treatment device and wastewater treatment method thereof |
| CN108178361A (en) * | 2016-12-08 | 2018-06-19 | 中国科学院大连化学物理研究所 | The reverse osmosis combined treatment process for generating strong brine in a kind of coal chemical industrial waste water reuse |
| CN107055860A (en) * | 2017-01-15 | 2017-08-18 | 丽中环境工程科技（上海）有限公司 | A kind of multidimensional multiphase Fenton sewage disposal systems and its application |
| CN108117196A (en) * | 2018-02-01 | 2018-06-05 | 北京桑德环境工程有限公司 | Leather waste water advanced treatment system and method |
| CN114772795A (en) * | 2022-05-25 | 2022-07-22 | 福建省金皇环保科技有限公司 | Catalytic oxidation coagulating sedimentation integrated sewage treatment process |
| CN114772795B (en) * | 2022-05-25 | 2024-01-02 | 福建省金皇环保科技有限公司 | Catalytic oxidation coagulation precipitation integrated sewage treatment process |
| CN115571969A (en) * | 2022-11-10 | 2023-01-06 | 华夏碧水环保科技股份有限公司 | Fenton reactor |
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