CN103359896B - A treatment, regeneration and cyclic utilization method for tobacco sheet production wastewater - Google Patents
A treatment, regeneration and cyclic utilization method for tobacco sheet production wastewater Download PDFInfo
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- CN103359896B CN103359896B CN201310341316.2A CN201310341316A CN103359896B CN 103359896 B CN103359896 B CN 103359896B CN 201310341316 A CN201310341316 A CN 201310341316A CN 103359896 B CN103359896 B CN 103359896B
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- 230000008929 regeneration Effects 0.000 title abstract description 3
- 238000011069 regeneration method Methods 0.000 title abstract description 3
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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention relates to a treatment, regeneration and cyclic utilization method for tobacco sheet production wastewater. The method comprises steps of slag removal, chemical decalcification, air floatation, anaerobic treatment, electrolysis, A/O treatment, secondary electrolysis, membrane treatment/aeration biological filter biochemical treatment, third electrolysis, desalination in sequence to obtain reclaimed water. The method combines a chemical decalcification technology, a biochemical technology, an electrochemical technology, a BAF technology and a membrane technology. The method has low cost and high efficiency. 75%-85% of the tobacco sheet production wastewater can be regenerated, cycled and utilized after being treated, thereby reducing wastewater discharge, protecting the environment from being polluted by the wastewater, reducing water resource waste, and allowing the cost of the recycled water to be lower than the cost of tap water. The method is economic and reasonable, and can produce good economic benefit.
Description
Technical field
The present invention relates to a kind of processing and recycling utilization method of tobacco sheet factory effluent, particularly relate to a kind of tobacco sheet factory effluent based on chemical decalcification technology, Measurement for Biochemistry, electrochemical techniques, BAF technology and membrane technique and processing and the recycling utilization method of tobacco factory effluent, belong to the water pollution control field of environmental engineering.
Background technology
Tobacco leaf is in the time producing, and raw material can not be utilized completely, and tobacco is from preliminary working to making the production process of cigarette, can produce the particle that accounts for greatly former cigarette material total amount 1/3, and these tobacco particles cannot directly be made cigarette product as raw material again.The comprehensive utilization that produces, realizes particle in order to reduce waste material, tobacco sheet technology is arisen at the historic moment.Tobacco sheet, having another name called reconstituted tobacco (Reconstituted Tobacco), is to utilize the tobacco materials such as offal, offal, tobacco cut to make sheet or thread reconstituted product for raw material, is used as cigarette filler, reduce the tar content in cigarette, reduce the Health hazard that smoking brings to human body.The use of tobacco sheet has the tobacco quality of raising, reduces cigarette cost, saves the plurality of advantages such as raw materials consumption, resource reutilization.Roll-in method, thick slurry method and paper process are the main production methods of current tobacco sheet.Compare with thick slurry method thin slice with roll-in method, paper process thin slice has obvious advantage: reduce production of cigarettes cost, constant product quality, filling value and becomes high, the resistance to machining property of silk rate good, improved the combustionvelocity of cigarette and reduced releasing content of coke tar, product plasticity-is high and more easily process, and is effective technique of current production " health type " cigarette.Just because of papermaking thin slice have advantages of roll-in method and thick slurry method incomparable, therefore all obtained extensive popularization at home and abroad.
The general character of the existing paper waste of waste water producing in tobacco sheets by paper making method production process is as contained a large amount of fibers, have again that tobacco wastewater colourity is high, biodegradability is poor simultaneously, contain features such as the disadvantageous nicotine of microorganism growth, tar and the high 150～500mg/L of calcium-magnesium content in waste water, main contamination index is as following table:
| Sequence number | Project | Index |
| 1 | Chemical oxygen demand (COD) (COD Cr） | 1500~25000mg/L |
| 2 | Five-day BOD (BOD 5） | 600~10000mg/L |
| 3 | Suspended substance (SS) | 700~15000mg/L |
| 4 | PH value | 5.5~6.5 |
| 5 | Colourity | 1000 ~ 25000 times |
| 6 | Water temperature | 45~65℃ |
| 7 | Ca 2+ | 150~500 mg/L |
Waste strength fluctuation is simultaneously larger, COD
crfrom 1500～25000mg/L, SS is from 700～15000mg/L, and nicotine and tar suppress microorganism growth, and the high reactor fouling that causes of calcium-magnesium content can not normally move, and belongs to the difficult organic waste water of high density.
Chinese patent CN1683261A discloses a kind for the treatment of process of papermaking method tobacco sheet production wastewater, i.e. the treatment process of the tobacco sheet factory effluent of coagulation air-float+aerobic oxidation+mechanical filter.
Chinese patent CN102276093A discloses a kind for the treatment of process of papermaking method tobacco sheet production wastewater, and this technique comprises the following steps: by factory effluent, by grid coarse filtration, gravity flow enters wastewater equalization pond; By lift pump by the waste water lifting in wastewater equalization pond to adding Ca-diatom soil series compound flocculating agent reaction 5-10min in coagulator, then add bodied ferric sulfate, polyacrylamide separating agent enters the reaction of static reaction pond, the reaction times is 50-60min; Be to pump in ultrasonic micro-electrolysis reactor after slant acidity by the pH regulator of the organic waste water of lower concentration, jointly react by ultrasonic wave and micro-electrolysis, make Chemical Oxygen Demand in Wastwater material rapid-digestion, the reaction times is 30-60min; Again by waste water process charcoal absorption and quartz sand filtration; The mud that equalizing tank and static reaction pond workshop section are produced uses as solid fuel after overlapping screwed sludge dewatering equipment is processed.
In Chinese patent CN10133045A, disclose papermaking method tobacco sheet production wastewater and to three-stage filtration, be back to respectively again slurrying workshop section through one, reuse water adopts the method that is regularly thrown into sewage works, but factory effluent loops back for the production of affecting greatly thin slice quality.
Chinese patent CN1683261A discloses papermaking method tobacco sheet production wastewater and has first removed wherein suspended solid through coagulating treatment, By Bubble-floating Method, then sends into aeration tank and remove by aerobic microbiological the method for most COD material.
Above method all has certain effect to the processing of tobacco sheet factory effluent, but exist, technical process is long, facility investment is large, floor space is large, the defects such as working cost height, more seriously owing to containing a large amount of calcium in waste water, directly cause a large amount of foulings of biochemical treatment system and film separating system, system cannot normally be moved, and existing wastewater processing technology waste discharge after treatment can not reach emission standard, let alone recycling utilization.
Summary of the invention
The object of the invention is to for existingly in existing tobacco production wastewater treatment method establishing that long, the standby investment of technical process is large, floor space is large, working cost is high, biochemical treatment system and film processing system be because fouling can not normally move, waste discharge after treatment is not up to standard, cannot recycling utilization etc. defect, providing a kind of combines based on chemical decalcification technology, Measurement for Biochemistry, electrochemical techniques, BAF technology and membrane technique, cost is lower, usefulness is higher, makes it the treatment process of the tobacco factory effluent of recycling utilization.
The processing of tobacco sheet factory effluent of the present invention and recycling utilization method comprise the following steps:
(1) slagging-off
Tobacco sheet factory effluent enters mechanical coarse rack water collecting basin after pipeline is collected, coarse rack is set in pond, cursory thing thick in sewage is isolated to removal, then pass through lift pump, tobacco sheet factory effluent is promoted in rotating machinery fine grid machine, further remove the suspended substance of most of insolubility in water by the filtration of filter screen, generation every slag packing outward transport, waste water passes through chemical decalcification processing;
(2) chemical decalcification
Water outlet after slagging-off first flows into equalizing tank through pipeline, enter again one-level decalcification reaction tank, under agitation first add sodium hydroxide solution or the saturated clear liquor of lime adjust pH to 8.5～9.5 of 300 ~ 900mg/L through chemicals dosing plant, remove after false hardness (supercarbonate), enter secondary decalcification reaction tank, pass into the gas that in step (4) anaerobic treatment, UASB anaerobic pond produces, make CO in gas
2react with calcium ions and magnesium ions and generate carbonate deposition, or add the Na of 200 ~ 800mg/L
2cO
3make pH value to 8～9, carbonate reacts with calcium ions and magnesium ions and generates carbonate deposition, enters preliminary sedimentation tank precipitation 3～4 hours;
(3) air supporting
The supernatant liquor of preliminary sedimentation tank pumps into filtration unit, obtain filtrate and precipitation, filtrate flows into coagulation basin, under agitation condition, first add the PAC of 5 ~ 10mg/L, the negatively charged ion polyphenyl alkene acid amides (PAM) that finally adds 2 ~ 3mg/L, enters air flotation pool and carries out dissolved air flotation after reacting completely, filtering-depositing and scum silica frost (being mud) are sent in sludge sump through pump and pipeline, finally in sludge dehydration device, carry out filtering separation, air flotation pool water outlet enters anaerobic pond; Described filtration unit is the one of centrifugal filter, vacuum filter or pressure filter;
(4) anaerobic treatment
Air flotation pool water outlet promotes and enters UASB anaerobic pond through lift pump, in process UASB anaerobic pond, under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane, organic acid is resolved into methane and carbon dioxide, the methane and carbon dioxide producing imports the secondary decalcification reaction tank in the chemical decalcification of step (2) after gas collector is collected, after secondary decalcification reaction tank purifies, reclaim biogas in gas holder, waste water enters step (5); The time of anaerobic treatment processing is 44～56 hours.
(5) electrolysis
The water outlet of UASB anaerobic pond enters electrolysis machine a and carries out electrolysis, and the adjacent two interelectrode voltages of electrolysis machine a are 2～12V, and current density is 30～260mA/cm
2;
(6) A/O processes
Electrolysis water outlet enters anoxic pond successively, Aerobic Pond and second pond, and the part mud of second pond is back to anoxic pond by reflux pump, utilize anoxic, under the alternating action of aerobic microbiological, can carry out denitrogenation dephosphorizing, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD, in Aerobic Pond, evenly fill up a large amount of biological suspended packings, for providing, aerobic microbiological perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface, be provided with aeration aerating stirring system in Aerobic Pond bottom, sewage is carried out to oxygenation, make the dissolved oxygen in water maintain 2～4 mg/L, the effect that simultaneously utilizes gas to rise, suspended substance in pond is more fully contacted with water, in addition by the agitaion of gas and clear water back flushing, can effectively wash away the aging microbial film of filling surface growth, impel biomembranous update, make microbial film maintain higher activity,
(7) re-electrolysis
Second pond water outlet enters electrolysis machine b and carries out electrolysis again, and electrolysis machine b is adjacent, and two interelectrode voltages are 2～6V, and current density is 20～200mA/cm
2;
(8) film is processed or BAF biochemistry (BAF biochemistry)
Waste water after re-electrolysis enters membrane treatment appts or BAF, by filtering separation or the oxidation degradation effect of membrane treatment appts, waste water is purified, and further removes COD, SS and ammonia nitrogen, is purified waste water; Described membrane treatment appts is the one of membrane bioreactor (MBR device) or ultra-filtration equipment;
(9) three electrolysis
Waste water is after film processing or BAF biochemical treatment, and water outlet is processed through electrolysis machine c again, can further remove colourity, and waste water is carried out to sterilization and disinfection;
(10) desalination
Waste water after three electrolysis enters desalting plant, separates to obtain water-dialyzing and condensed water, and water-dialyzing enters reuse water basin, and a condensed water part flow to the equalizing tank in the chemical decalcification of step (2) by back of pipeline, and remainder discharges through discharge channel; Described desalting plant is the one of reverse osmosis system, nanofiltration system, electrodialysis or capacitive adsorption deionizing system;
(11) sludge treatment
The mud that during UASB anaerobic pond in filtration unit in preliminary sedimentation tank, step (3) air supporting in the chemical decalcification of step (2) and air flotation pool, step (4) anaerobic treatment, step (6) A/O process, anoxic pond, Aerobic Pond and second pond and step (8) membrane treatment appts or BAF biochemical treatment produce all enters sludge sump by pipeline, then make reducing sludge volume through the dehydration of sludge filter press, after dehydration, mud cake carries out burning disposal, and filtrate is back to the equalizing tank in the chemical decalcification of step (2).
The second step of the chemical decalcification of step (2) is that the biogas (containing methane, carbonic acid gas, hydrogen sulfide, sulfur alcohol compound, ammonia etc.) that UASB anaerobic pond is produced leads to secondary decalcification pond, makes CO in gas
2react with calcium ions and magnesium ions and generate when carbonate deposition, hydrogen sulfide in biogas, sulfur alcohol compound, ammonia etc. reacts with calcium ions and magnesium ions, make biogas also obtain purification, and the biogas after purification can be collected in further utilization in gas holder.
Air supporting described in step (3) air supporting is the one of gas distribution By Bubble-floating Method, electric floating method, biology and chemical floatation treatment, dissolved air flotation.
Filtration described in step (3) air supporting is the one of centrifuging, vacuum filtration or press filtration; The whizzer working speed of centrifuging is 3000～5000 revs/min; The filter cloth aperture of vacuum filtration and press filtration is less than 5 μ m.
Electrolysis machine a, electrolysis machine b and the electrolysis machine c of step (5), step (7) and step (9) are equipped with power supply and electrolyzer, and the electrode materials in described electrolyzer is the one in graphite, titanium, iron, aluminium, zinc, copper, lead, nickel, molybdenum, chromium, alloy and nano-catalytic inert material; The top layer of described nano-catalytic noble electrode is coated with the metal oxide inertia catalyst coatings that crystal grain is 10～35nm, and the substrate of described nano-catalytic noble electrode is titanium plate or plastic plate.
The membrane module of the described MBR device of step (8) is the one of hollow fiber film assembly or plate film assembly; Hollow fiber film assembly is the one in Pvdf Microporous Hollow Fiber Membrane assembly, polypropylene hollow fiber membrane assembly, ps hollow fiber uf membrane assembly, polyethersulfone assembly, polyacrylonitrile assembly and PVC hollow fiber membrane assembly, membrane pore size is 0.10～0.2 μ m, operating pressure is-1～-50kPa, and working temperature is 5～45 DEG C; Described ultra-filtration equipment is the one of immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000～100000MWCO, working conditions is: normal temperature～45 DEG C, the operating pressure of immersion ultrafiltration is-1～-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3～300kPa.
Reverse osmosis membrane assembly in the described reverse osmosis system of step (10) is rolled membrane module, mould material is cellulose acetate film or composite membrane in organic membrane, the molecular weight cut-off of mould material is 50～200MWCO, entrance pressure can be 6.0～45.0bar, go out to press and can be 4.5～33.5 bar, working temperature is 20～45 DEG C, and optimum temps is 25～35 DEG C; Nanofiltration membrane component in described nanofiltration system is the one of tubular membrane component, rolled membrane module or plate film assembly, and operating pressure is 6～45bar, and working temperature is 20～45 DEG C, and optimum temps is 25～35 DEG C; Described electrodialytic working conditions is operating voltage pressure 0.5～3.0 kg/cm
2, operating voltage 50～250V, strength of current 1～3A; The working conditions of described capacitive adsorption deionizing system is that volts DS is 110V～2 × 10
6v, strength of current is less than or equal to 1A.
Waste water is as shown in table 1 through the above effect of processing:
The present invention compared with the prior art, has following outstanding advantages:
(1) remove after false hardness (supercarbonate) by the one-level decalcification reaction of chemical decalcification system, through secondary decalcification reaction tank, carbonate is reacted with calcium ions and magnesium ions again and generate carbonate deposition, then in coagulation basin carbonate deposition de-steady, flocculate mutually with the coagulant aids such as negatively charged ion polyphenyl alkene acid amides (PAM), be gathered into thick alumina blossom particles, in preliminary sedimentation tank, settle down, high-concentration Ca, magnesium ion in final effective elimination tobacco sheet factory effluent, clearance reaches 50 ~ 90%, reduce water hardness, make Ca
2+lower than 80 mg/L, prevent reactor fouling, ensure that follow-up biochemical treatment, electrolysis process and desalinating process are smooth, steady running.
(2), after chemical decalcification, after centrifugation or vacuum filtration or press filtration, the COD in waste water is dropped to below 7000mg/L.
(3) after UASB system for anaerobic treatment is processed, the index such as COD, BOD in waste water significantly reduces, and the gas of generation imports the secondary decalcification reaction tank in chemical decalcification after gas collector is collected, and makes CO in gas
2react with calcium ions and magnesium ions and generate carbonate deposition, on the one hand CO in gas recovery
2, gas is utilized effectively; Remove the H in gas by secondary decalcification reaction tank on the other hand
2s, Purge gas, biogas is collected and is utilized or high altitude discharge by gas holder again.
(3) after slagging-off and the processing of chemical decalcification system, the SS clearance in waste water reaches more than 95%, and the SS in equalizing tank greatly reduces, and avoids the deposition of mud in equalizing tank, alleviates and moves at ordinary times clear mud workload.
(4) the strong oxidizing property free radical producing by nano-catalytic electrolysis makes the biochemical macromolecular cpd open loop of the difficulty chain rupture in waste water, become can be biochemical small molecules, further improve B/C value, improve the condition of follow-up biochemical treatment, and remove colourity and the stink in waste water, reduce the indexs such as ammonia nitrogen, COD.
(5) through A/O biochemistry pool, by the alternating action of anaerobic-aerobic, can carry out denitrogenation dephosphorizing to sewage.
(6) after BAF biochemical treatment, thoroughly decompose pollutant in water by the oxygenolysis of aerobic microbiological, make stable effluent quality, qualified discharge.
(7) tobacco sheet factory effluent is through processing, and 75%～85% can recycling utilization, has both reduced discharge of wastewater, avoid waste water environmental pollution, reduce again water resource waste, can also make the recirculated water cost of regeneration lower than tap water price, economical rationality, produces good economic benefit.
Brief description of the drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
The present invention is the design to tobacco sheet production wastewater treatment method completing after the composition to existing tobacco sheet factory effluent, character and existing processing scheme are goed deep into the comparative study of system, it is by the integrated use of the methods such as chemical decalcification, biochemistry, electrochemistry, BAF, membrane technique, thereby forms a kind of processing and recycling utilization method that is particularly suitable for tobacco sheet factory effluent.
1 explanation the specific embodiment of the present invention with reference to the accompanying drawings.
Embodiment 1
The processing of 20 ton per day tobacco sheet factory effluents and recycling utilization method.
Described tobacco sheet factory effluent water-quality guideline is as shown in table 2 after measured.
(1) slagging-off
Tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in pond, cursory thing thick in sewage is isolated to removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, tobacco sheet factory effluent is promoted in rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in water by the filtration of filter screen, what produce transports outward every slag packing, and waste water is through chemical decalcification processing.
(2) chemical decalcification
Water outlet after slagging-off first flows into equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, under agitation first add the sodium hydroxide solution adjust pH to 8.5 of 600mg/L through chemicals dosing plant, remove after false hardness (supercarbonate), enter secondary decalcification reaction tank 5, pass into the gas that in step (4) anaerobic treatment, UASB anaerobic pond 10 produces, make CO in gas
2react with calcium ions and magnesium ions and generate carbonate deposition, adjust pH to 8.0, enters preliminary sedimentation tank 6 and carries out precipitate and separate after reacting completely, and sedimentation time is 4 hours, processes the calcium ions and magnesium ions in waste water thereby remove tobacco, and clearance reaches 84%, reduces water hardness, makes Ca
2+concentration is less than 80 mg/L, prevents that follow-up equipment, facility are because of too high Ca
2+fouling;
(3) air supporting
Supernatant liquor in preliminary sedimentation tank 6 pumps in filtration unit 7 through lift pump 23, the present embodiment adopts whizzer, centrifugation under the rotating speed of 4200 revs/min, obtain filtrate and precipitation, filtrate flows into coagulation basin 8, under agitation condition, first add the PAC of 10mg/L, finally add the negatively charged ion polyphenyl alkene acid amides (PAM) of 2mg/L, after reacting completely, enter air flotation pool 9 and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in sludge sump 20 through pump and pipeline, finally in sludge dehydration device 21, carry out filtering separation, air flotation pool 9 water outlets pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion,
(4) anaerobic treatment
Air flotation pool 9 water outlets enter UASB anaerobic pond 10 through lift pump 24 liftings and carry out anaerobic treatment 56 hours, in process UASB anaerobic pond 10, under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane, organic acid are resolved into methane and carbon dioxide; The methane and carbon dioxide producing, after gas collector 27 is collected, reclaims biogas in biogas storage tank 28 after purifying; Waste water enters step (5).
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make the biochemical macromolecular cpd open loop of difficulty in waste water chain rupture simultaneously, become can be biochemical small molecules, further improve B/C value, improve the condition of follow-up biochemical treatment; The adjacent two interelectrode voltages of electrolysis machine a11 are 2V, and current density is 260mA/cm
2.
(6) A/O processes
Electrolysis water outlet enters anoxic pond 12, Aerobic Pond 13 and second pond 14 successively, and the part mud of second pond 14 is back to anoxic pond 12 by reflux pump, utilize under the alternating action of anoxic, aerobic microbiological and can carry out denitrogenation dephosphorizing, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD; Aerobic Pond 13 is interior evenly fills up a large amount of biological suspended packings, perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface for aerobic microbiological provides.Be provided with aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out to oxygenation, make the dissolved oxygen in water maintain 2～4 mg/L, the effect that simultaneously utilizes gas to rise, suspended substance in pond is more fully contacted with water, in addition by the agitaion of gas and clear water back flushing, can effectively wash away the aging microbial film of filling surface growth, impel biomembranous update, make microbial film maintain higher activity.
(7) re-electrolysis
Second pond 14 water outlets enter electrolysis machine b15 and carry out electrolysis again, make to be difficult to biochemical larger molecular organics through electrolysis generation open loop chain scission in waste water, are converted into and are easy to biochemical small organic molecule, improve B/C; When electrolysis, adjacent two interelectrode voltages are 6V, and current density is 20mA/cm
2.
(8) BAF biochemistry (BAF biochemistry)
Waste water after re-electrolysis enters BAF 16, by oxidation degradation effect, waste water is purified, and further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
Waste water is after BAF 16 biochemical treatments, and water outlet is promoted to electrolysis machine c17 by lift pump 25 and processes, and can further remove colourity, and waste water is carried out to sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters desalting plant 30 through working shaft 29, the present embodiment adopts reverse osmosis unit, separate to obtain water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, a condensed water part flow to the equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder discharges through discharge channel 18;
(11) sludge treatment
In air flotation pool in preliminary sedimentation tank, step (3) air supporting in the chemical decalcification of step (2), step (4) anaerobic treatment UASB anaerobic pond 10, step (6) A/O process in the mud that produces of anoxic pond 12, Aerobic Pond 13 and second pond 14 and 16 biochemical treatments of step (8) BAF all enter sludge sump 20 by pipeline, then make reducing sludge volume through the dehydration of sludge dehydration device 21, after dehydration, mud cake carries out burning disposal, and filtrate is back to the equalizing tank 3 in the chemical decalcification of step (2).
The each operation of process effect after treatment is as table 3
Reuse water water-quality guideline is as shown in table 4 after measured.
Embodiment 2
The processing of 50 ton per day tobacco sheet factory effluents and recycling utilization method.
Described tobacco sheet factory effluent water-quality guideline is as shown in table 5 after measured.
(1) slagging-off
Tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in pond, cursory thing thick in sewage is isolated to removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, tobacco sheet factory effluent is promoted in rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in water by the filtration of filter screen, what produce transports outward every slag packing, and waste water is through chemical decalcification processing.
(2) chemical decalcification
Water outlet after slagging-off first flows into equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, under agitation first add the saturated settled solution of 900mg/L lime adjust pH to 9.5 through chemicals dosing plant, remove after false hardness (supercarbonate), enter secondary decalcification reaction tank 5, add the Na of 400mg/L
2cO
3adjust pH to 8.5, makes carbonate react with calcium ions and magnesium ions and generates carbonate deposition, enters preliminary sedimentation tank 6 and carry out precipitate and separate after reacting completely, sedimentation time is 3 hours, processes the calcium ions and magnesium ions in waste water thereby remove tobacco, and clearance reaches 83.3%, reduce water hardness, make Ca
2+concentration is less than 50 mg/L, prevents that follow-up equipment, facility are because of too high Ca
2+fouling;
(3) air supporting
Supernatant liquor in preliminary sedimentation tank 6 pumps into filtration unit 7 through lift pump 23, the present embodiment adopts in vacuum filter, filtering separation under-0.3MPa vacuum condition, filter cloth aperture is less than 5um, obtain filtrate and precipitation, filtrate flows into coagulation basin 8, under agitation condition, first add the PAC of 5mg/L, finally add the negatively charged ion polyphenyl alkene acid amides (PAM) of 3mg/L, after reacting completely, enter air flotation pool 9 and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in sludge sump 20 through pump and pipeline, finally in sludge dehydration device 21, carry out filtering separation, air flotation pool 9 water outlets pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion,
(4) anaerobic treatment
Air flotation pool 9 water outlets enter UASB anaerobic pond 10 through lift pump 24 liftings and carry out anaerobic treatment 44 hours, in process UASB anaerobic pond 10, under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane, organic acid are resolved into methane and carbon dioxide; The methane and carbon dioxide producing, after gas collector 27 is collected, reclaims biogas in biogas storage tank 28 after purifying; Waste water enters step (5).
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make the biochemical macromolecular cpd open loop of difficulty in waste water chain rupture simultaneously, become can be biochemical small molecules, further improve B/C value, improve the condition of follow-up biochemical treatment; The adjacent two interelectrode voltages of electrolysis machine a11 are 8V, and current density is 150mA/cm
2.
(6) A/O processes
Electrolysis water outlet enters anoxic pond 12, Aerobic Pond 13 and second pond 14 successively, and the part mud of second pond 14 is back to anoxic pond 12 by reflux pump, utilize under the alternating action of anoxic, aerobic microbiological and can carry out denitrogenation dephosphorizing, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD; Aerobic Pond 13 is interior evenly fills up a large amount of biological suspended packings, perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface for aerobic microbiological provides.Be provided with aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out to oxygenation, make the dissolved oxygen in water maintain 2～4 mg/L, the effect that simultaneously utilizes gas to rise, suspended substance in pond is more fully contacted with water, in addition by the agitaion of gas and clear water back flushing, can effectively wash away the aging microbial film of filling surface growth, impel biomembranous update, make microbial film maintain higher activity.
(7) re-electrolysis
Second pond 14 water outlets enter electrolysis machine b15 and carry out electrolysis again, make to be difficult to biochemical larger molecular organics through electrolysis generation open loop chain scission in waste water, are converted into and are easy to biochemical small organic molecule, improve B/C; When electrolysis, adjacent two interelectrode voltages are 4V, and current density is 100mA/cm
2.
(8) MBR processes
Waste water after re-electrolysis enters membrane treatment appts 16, and the present embodiment adopts MBR device, is separated waste water is purified with membrane filtration by oxidation degradation effect, further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
Waste water is after the biochemical treatment of MBR device, and water outlet is promoted to electrolysis machine c17 by lift pump 25 and processes, and can further remove colourity, and waste water is carried out to sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters nanofiltration device 30 through working shaft 29, separate to obtain water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, and a condensed water part flow to the equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder discharges through discharge channel 18.
(11) sludge treatment
In air flotation pool 9 in preliminary sedimentation tank 6, step (3) air supporting in the chemical decalcification of step (2), step (4) anaerobic treatment UASB anaerobic pond 10, step (6) A/O process in the mud that produces of anoxic pond 12, Aerobic Pond 13 and second pond 14 and the biochemical treatment of step (8) MBR device all enter sludge sump 20 by pipeline, then make reducing sludge volume through the dehydration of sludge dehydration device 21, after dehydration, mud cake carries out burning disposal, and filtrate is back to the equalizing tank 3 in the chemical decalcification of step (2).
The each operation of process effect after treatment is as table 6
Reuse water water-quality guideline is as shown in table 7 after measured.
Embodiment 3
The processing of 10 ton per day tobacco sheet factory effluents and recycling utilization method.
Described tobacco sheet factory effluent water-quality guideline is as shown in table 8 after measured.
(1) slagging-off
Tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in pond, cursory thing thick in sewage is isolated to removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, tobacco sheet factory effluent is promoted in rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in water by the filtration of filter screen, what produce transports outward every slag packing, and waste water is through chemical decalcification processing.
(2) chemical decalcification
Water outlet after slagging-off first flows into equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, under agitation first add the saturated settled solution of 300mg/L lime adjust pH to 9.0 through chemicals dosing plant, remove after false hardness (supercarbonate), enter secondary decalcification reaction tank 5, add the Na of 200mg/L
2cO
3adjust pH to 9.0, makes carbonate react with calcium ions and magnesium ions and generates carbonate deposition, enters preliminary sedimentation tank 6 and carry out precipitate and separate after reacting completely, sedimentation time is 3.5 hours, processes the calcium ions and magnesium ions in waste water thereby remove tobacco, and clearance reaches 87.5%, reduce water hardness, make Ca
2+concentration is less than 50 mg/L, prevents that follow-up equipment, facility are because of too high Ca
2+fouling;
(3) air supporting
Supernatant liquor in preliminary sedimentation tank 6 pumps in filtration unit 7 through lift pump 23, the present embodiment adopts pressure filter, filtering separation in pressure filter, filter cloth aperture is less than 5um, obtain filtrate and precipitation, filtrate flows into coagulation basin 8, under agitation condition, first add the PAC of 8mg/L, finally add the negatively charged ion polyphenyl alkene acid amides (PAM) of 2.5mg/L, after reacting completely, enter air flotation pool 9 and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in sludge sump 20 through pump and pipeline, finally in sludge dehydration device 21, carry out filtering separation, air flotation pool 9 water outlets pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion,
(4) anaerobic treatment
Air flotation pool 9 water outlets enter UASB anaerobic pond 10 through lift pump 24 liftings and carry out anaerobic treatment 50 hours, in process UASB anaerobic pond 10, under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane, organic acid are resolved into methane and carbon dioxide; The methane and carbon dioxide producing, after gas collector 27 is collected, reclaims biogas in biogas storage tank 28 after purifying; Waste water enters step (5).
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make the biochemical macromolecular cpd open loop of difficulty in waste water chain rupture simultaneously, become can be biochemical small molecules, further improve B/C value, improve the condition of follow-up biochemical treatment; The adjacent two interelectrode voltages of electrolysis machine a11 are 12V, and current density is 30mA/cm
2.
(6) A/O processes
Electrolysis water outlet enters anoxic pond 12, Aerobic Pond 13 and second pond 14 successively, and the part mud of second pond 14 is back to anoxic pond 12 by reflux pump, utilize under the alternating action of anoxic, aerobic microbiological and can carry out denitrogenation dephosphorizing, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD; Aerobic Pond 13 is interior evenly fills up a large amount of biological suspended packings, perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface for aerobic microbiological provides.Be provided with aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out to oxygenation, make the dissolved oxygen in water maintain 2～4 mg/L, the effect that simultaneously utilizes gas to rise, suspended substance in pond is more fully contacted with water, in addition by the agitaion of gas and clear water back flushing, can effectively wash away the aging microbial film of filling surface growth, impel biomembranous update, make microbial film maintain higher activity.
(7) re-electrolysis
Second pond 14 water outlets enter electrolysis machine b15 and carry out electrolysis again, make to be difficult to biochemical larger molecular organics through electrolysis generation open loop chain scission in waste water, are converted into and are easy to biochemical small organic molecule, improve B/C; When electrolysis, adjacent two interelectrode voltages are 2V, and current density is 200mA/cm
2.
(8) uf processing
Waste water after re-electrolysis enters membrane treatment appts 16, and the present embodiment adopts ultra-filtration equipment, is separated waste water is purified by ultrafiltration membrance filter, further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
Waste water is after ultra-filtration equipment is processed, and water outlet is promoted to electrolysis machine c17 by lift pump 25 and processes, and can further remove colourity, and waste water is carried out to sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters desalting plant 30 through working shaft 29, the present embodiment adopts capacitive adsorption deionizing desalting plant, separate to obtain water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, a condensed water part flow to the equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder discharges through discharge channel 18.
(11) sludge treatment
In air flotation pool 9 in preliminary sedimentation tank 6, step (3) air supporting in the chemical decalcification of step (2), step (4) anaerobic treatment UASB anaerobic pond 10, step (6) A/O process in anoxic pond 12, Aerobic Pond 13 and second pond 14 process the mud producing and all enter sludge sump 20 by pipeline, then make reducing sludge volume through the dehydration of sludge dehydration device 21, after dehydration, mud cake carries out burning disposal, and filtrate is back to the equalizing tank 3 in the chemical decalcification of step (2).
The each operation of process effect after treatment is as table 9
Reuse water water-quality guideline is as shown in table 10 after measured.
Embodiment 4
The processing of 100 ton per day tobacco sheet factory effluents and recycling utilization method.
Described tobacco sheet factory effluent water-quality guideline is as shown in table 11 after measured.
(1) slagging-off
Tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in pond, cursory thing thick in sewage is isolated to removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, tobacco sheet factory effluent is promoted in rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in water by the filtration of filter screen, what produce transports outward every slag packing, and waste water is through chemical decalcification processing.
(2) chemical decalcification
Water outlet after slagging-off first flows into equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, under agitation first add 900mg/LNaOH solution adjust pH to 9.5 through chemicals dosing plant, remove after false hardness (supercarbonate), enter secondary decalcification reaction tank 5, add the Na of 800mg/L
2cO
3adjust pH to 9.0, makes carbonate react with calcium ions and magnesium ions and generates carbonate deposition, enters preliminary sedimentation tank 6 and carry out precipitate and separate after reacting completely, sedimentation time is 3 hours, processes the calcium ions and magnesium ions in waste water thereby remove tobacco, and clearance reaches 66.7%, reduce water hardness, make Ca
2+concentration is less than 50 mg/L, prevents that follow-up equipment, facility are because of too high Ca
2+fouling;
(3) air supporting
Supernatant liquor in preliminary sedimentation tank 6 pumps into filtration unit 7 through lift pump 23, the present embodiment adopts in whizzer, centrifugation under the rotating speed of 5000 revs/min, obtain filtrate and precipitation, filtrate flows into coagulation basin 8, under agitation condition, first add the PAC of 8mg/L, finally add the negatively charged ion polyphenyl alkene acid amides (PAM) of 2.5mg/L, after reacting completely, enter air flotation pool 9 and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in sludge sump 20 through pump and pipeline, finally in sludge dehydration device 21, carry out filtering separation, air flotation pool 9 water outlets pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion,
(4) anaerobic treatment
Air flotation pool 9 water outlets enter UASB anaerobic pond 10 through lift pump 24 liftings and carry out anaerobic treatment 48 hours, in process UASB anaerobic pond 10, under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane, organic acid are resolved into methane and carbon dioxide; The methane and carbon dioxide producing, after gas collector 27 is collected, reclaims biogas in biogas storage tank 28 after purifying; Waste water enters step (5).
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make the biochemical macromolecular cpd open loop of difficulty in waste water chain rupture simultaneously, become can be biochemical small molecules, further improve B/C value, improve the condition of follow-up biochemical treatment; The adjacent two interelectrode voltages of electrolysis machine a11 are 8V, and current density is 120mA/cm
2.
(6) A/O processes
Electrolysis water outlet enters anoxic pond 12, Aerobic Pond 13 and second pond 14 successively, and the part mud of second pond 14 is back to anoxic pond 12 by reflux pump, utilize under the alternating action of anoxic, aerobic microbiological and can carry out denitrogenation dephosphorizing, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD; Aerobic Pond 13 is interior evenly fills up a large amount of biological suspended packings, perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface for aerobic microbiological provides.Be provided with aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out to oxygenation, make the dissolved oxygen in water maintain 2～4 mg/L, the effect that simultaneously utilizes gas to rise, suspended substance in pond is more fully contacted with water, in addition by the agitaion of gas and clear water back flushing, can effectively wash away the aging microbial film of filling surface growth, impel biomembranous update, make microbial film maintain higher activity.
(7) re-electrolysis
Second pond 14 water outlets enter electrolysis machine b15 and carry out electrolysis again, make to be difficult to biochemical larger molecular organics through electrolysis generation open loop chain scission in waste water, are converted into and are easy to biochemical small organic molecule, improve B/C; When electrolysis, adjacent two interelectrode voltages are 4V, and current density is 150mA/cm
2.
(8) uf processing
Waste water after re-electrolysis enters membrane treatment appts 16, and the present embodiment adopts ultra-filtration equipment, is separated waste water is purified by ultrafiltration membrance filter, further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
Waste water is after ultra-filtration equipment is processed, and water outlet is promoted to electrolysis machine c17 by lift pump 25 and processes, and can further remove colourity, and waste water is carried out to sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters desalting plant 30 through working shaft 29, the present embodiment adopts electrodialysis unit, separate to obtain water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, a condensed water part flow to the equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder discharges through discharge channel 18.
(11) sludge treatment
In air flotation pool 9 in preliminary sedimentation tank 6, step (3) air supporting in the chemical decalcification of step (2), step (4) anaerobic treatment UASB anaerobic pond 10, step (6) A/O process in anoxic pond 12, Aerobic Pond 13 and second pond 14 process the mud producing and all enter sludge sump 20 by pipeline, then make reducing sludge volume through the dehydration of sludge dehydration device 21, after dehydration, mud cake carries out burning disposal, and filtrate is back to the equalizing tank 3 in the chemical decalcification of step (2).
The each operation of process effect after treatment is as table 12
Reuse water water-quality guideline is as shown in table 13 after measured.
Above are only the specific embodiment of the present invention, but design concept of the present invention is not limited to this, allly utilizes this design to carry out the change of unsubstantiality to the present invention, all should belong to the behavior of invading protection domain of the present invention.
Claims (10)
1. the processing of tobacco sheet factory effluent and recycling utilization method, it comprises the following steps:
(1) slagging-off
Tobacco sheet factory effluent enters mechanical coarse rack water collecting basin after pipeline is collected, coarse rack is set in pond, cursory thing thick in sewage is isolated to removal, then pass through lift pump, tobacco sheet factory effluent is promoted in rotating machinery fine grid machine, further remove the suspended substance of most of insolubility in water by the filtration of filter screen, generation every slag packing outward transport, waste water passes through chemical decalcification processing;
(2) chemical decalcification
Water outlet after slagging-off first flows into equalizing tank through pipeline, enter again one-level decalcification reaction tank, under agitation first add sodium hydroxide solution or the saturated clear liquor of lime adjust pH to 8.5～9.5 of 300 ~ 900mg/L through chemicals dosing plant, remove after false hardness supercarbonate, enter secondary decalcification reaction tank, pass into the gas that in step (4) anaerobic treatment, UASB anaerobic pond produces, make CO in gas
2react with calcium ions and magnesium ions and generate carbonate deposition, or add the Na of 200 ~ 800mg/L
2cO
3make pH value to 8～9, carbonate reacts with calcium ions and magnesium ions and generates carbonate deposition, enters preliminary sedimentation tank precipitation 3～4 hours;
(3) air supporting
The supernatant liquor of preliminary sedimentation tank pumps into filtration unit and carries out filtering separation, obtain filtrate and precipitation, filtrate flows into coagulation basin, under agitation condition, first add the PAC of 5 ~ 10mg/L, finally add the anionic polyacrylamide of 2 ~ 3mg/L, after reacting completely, enter air flotation pool and carry out dissolved air flotation, filtering-depositing and scum silica frost are sent in sludge sump through pump and pipeline, finally in sludge dehydration device, carry out filtering separation, air flotation pool water outlet enters anaerobic pond, described filtration is centrifuging, the one of vacuum filtration or press filtration, the whizzer working speed of centrifuging is 3000～5000 revs/min, the filter cloth aperture of vacuum filtration and press filtration is less than 5 μ m,
(4) anaerobic treatment
Air flotation pool water outlet promotes and enters UASB anaerobic pond through lift pump, in process UASB anaerobic pond, under the absorption of anerobe, the oxygen bacterium of holding concurrently, fermentation, the acting in conjunction of product methane, organic acid is resolved into methane and carbon dioxide, the methane and carbon dioxide producing imports the secondary decalcification reaction tank in the chemical decalcification of step (2) after gas collector is collected, after purifying, secondary decalcification reaction tank reclaims biogas in gas holder, waste water enters step (5), and the time of anaerobic treatment is 44～56 hours;
(5) electrolysis
The water outlet of UASB anaerobic pond enters electrolysis machine a and carries out electrolysis, and the adjacent two interelectrode voltages of electrolysis machine a are 2～12V, and current density is 30～260mA/cm
2;
(6) A/O processes
Electrolysis water outlet enters anoxic pond successively, Aerobic Pond and second pond, and the part mud of second pond is back to anoxic pond by reflux pump, utilize anoxic, under the alternating action of aerobic microbiological, can carry out denitrogenation dephosphorizing, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD, in Aerobic Pond, evenly fill up a large amount of biological suspended packings, for providing, aerobic microbiological perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface, be provided with aeration aerating stirring system in Aerobic Pond bottom, sewage is carried out to oxygenation, make the dissolved oxygen in water maintain 2～4 mg/L, the effect that simultaneously utilizes gas to rise, suspended substance in pond is more fully contacted with water, in addition by the agitaion of gas and clear water back flushing, effectively the aging microbial film of filling surface growth is washed away, impel biomembranous update, make microbial film maintain higher activity,
(7) re-electrolysis
Second pond water outlet enters electrolysis machine b and carries out electrolysis again, and electrolysis machine b is adjacent, and two interelectrode voltages are 2～6V, and current density is 20～200mA/cm
2;
(8) film is processed or BAF biochemistry
Waste water after re-electrolysis enters membrane treatment appts or BAF, filtering separation or oxidation degradation effect by membrane treatment appts purify waste water, further remove COD, SS and ammonia nitrogen, be purified waste water, described membrane treatment appts is the one of MBR device or ultra-filtration equipment;
(9) three electrolysis
Waste water is after film processing or BAF biochemical treatment, and water outlet is processed through electrolysis machine c again, can further remove colourity, and waste water is carried out to sterilization and disinfection;
(10) desalination
Waste water after three electrolysis enters desalting plant, separate to obtain water-dialyzing and condensed water, water-dialyzing enters reuse water basin, a condensed water part flow to the equalizing tank in the chemical decalcification of step (2) by back of pipeline, remainder discharges through discharge channel, and described desalting plant is the one of reverse osmosis system, nanofiltration system, electrodialysis or capacitive adsorption deionizing system;
(11) sludge treatment
The mud that anoxic pond, Aerobic Pond and second pond during air flotation pool in preliminary sedimentation tank, step (3) air supporting in the chemical decalcification of step (2), the UASB anaerobic pond in step (4) anaerobic treatment, step (6) A/O process and step (8) membrane treatment appts or BAF biochemical treatment produce all enters sludge sump by pipeline, then make reducing sludge volume through the dehydration of sludge dehydration device, after dehydration, mud cake carries out burning disposal, and filtrate is back to the equalizing tank in the chemical decalcification of step (2).
2. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, is characterized in that: described in step (3) air supporting, air supporting is the one of gas distribution By Bubble-floating Method, electric floating method, biology and chemical floatation treatment, dissolved air flotation.
3. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, it is characterized in that: electrolysis machine a, electrolysis machine b and the electrolysis machine c of step (5), step (7) and step (9) are equipped with power supply and electrolyzer, the electrode in described electrolyzer is the one in graphite, titanium, iron, aluminium, zinc, copper, lead, nickel, molybdenum, chromium, alloy and nano-catalytic noble electrode.
4. the processing of tobacco sheet factory effluent as claimed in claim 3 and recycling utilization method, it is characterized in that: the top layer of described nano-catalytic noble electrode is coated with the metal oxide inertia catalyst coatings that crystal grain is 10～35nm, and the substrate of described nano-catalytic noble electrode is titanium plate or plastic plate.
5. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, is characterized in that: the membrane module of the described MBR device of step (8) is the one of hollow fiber film assembly or plate film assembly; Hollow fiber film assembly is the one in Pvdf Microporous Hollow Fiber Membrane assembly, polypropylene hollow fiber membrane assembly, ps hollow fiber uf membrane assembly, polyethersulfone assembly, polyacrylonitrile assembly and PVC hollow fiber membrane assembly, membrane pore size is 0.10～0.2 μ m, operating pressure is-1～-50kPa, and working temperature is 5～45 DEG C.
6. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, it is characterized in that: the described ultra-filtration equipment of step (8) is the one of immersion ultrafiltration, pillar ultrafiltration, tubular type ultrafiltration, spiral wound or plate-type hyperfiltration, molecular weight cut-off is 1000～100000MWCO, working conditions is: normal temperature～45 DEG C, the operating pressure of immersion ultrafiltration is-1～-50kPa, and the operating pressure of pillar ultrafiltration, tubular type ultrafiltration, spiral wound and plate-type hyperfiltration is 3～300kPa.
7. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, it is characterized in that: the reverse osmosis membrane assembly in the described reverse osmosis system of step (10) is rolled membrane module, mould material is cellulose acetate film or composite membrane in organic membrane, the molecular weight cut-off of mould material is 50～200MWCO, entrance pressure is 6.0～45.0bar, going out to press is 4.5～33.5 bar, and working temperature is 20～45 DEG C.
8. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, it is characterized in that: the nanofiltration membrane component in the described nanofiltration system of step (10) is the one of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 6～45bar, and working temperature is 20～45 DEG C.
9. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, is characterized in that: the described electrodialytic working conditions of step (10) is: operating voltage pressure 0.5～3.0 kg/cm
2, operating voltage 50～250V, strength of current 1～3A.
10. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, is characterized in that: the working conditions of the described capacitive adsorption deionizing system of step (10) is that volts DS is 110V～2 × 10
6v, strength of current is less than or equal to 1A.
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| US11563229B1 (en) | 2022-05-09 | 2023-01-24 | Rahul S Nana | Reverse electrodialysis cell with heat pump |
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| WO2014190874A1 (en) * | 2013-05-31 | 2014-12-04 | 波鹰(厦门)科技有限公司 | Apparatus and method for treating tobacco sheet production wastewater |
| CN104230127B (en) * | 2014-10-17 | 2016-03-23 | 安徽中烟再造烟叶科技有限责任公司 | The technique of biogas is prepared in reforged tobacco wastewater process |
| CN104291531A (en) * | 2014-10-25 | 2015-01-21 | 吴玲玲 | Sewage treatment method and sewage treatment device |
| CN105399287B (en) * | 2015-12-30 | 2019-01-22 | 北京赛科康仑环保科技有限公司 | A kind of organic wastewater with difficult degradation thereby integrated treatment and Zero discharge treatment method and its system |
| CN107467706A (en) * | 2017-01-17 | 2017-12-15 | 云南中烟再造烟叶有限责任公司 | The method for reducing water-soluble chemical oxygen demand in papermaking-method reconstituted tobaccos production plain boiled water |
| CN107487875A (en) * | 2017-08-24 | 2017-12-19 | 上海烟草集团有限责任公司 | A kind of papermaking-method reconstituted tobaccos are manufactured paper with pulp white water recycling handling process |
| CN108341518A (en) * | 2018-02-12 | 2018-07-31 | 安徽江淮汽车集团股份有限公司 | A kind of high concentration phosphatization wastewater treatment method |
| CN110589991B (en) * | 2019-09-10 | 2020-11-27 | 同济大学 | Method for removing calcium ions in high-concentration organic wastewater |
| CN111592098B (en) * | 2020-05-27 | 2021-04-27 | 山东膜源水净化科技股份有限公司 | MBR membrane biological reaction device |
| US11502323B1 (en) | 2022-05-09 | 2022-11-15 | Rahul S Nana | Reverse electrodialysis cell and methods of use thereof |
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