CN103359896A - 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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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, the processing and the recycling utilization method that 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 tobacco factory effluent belong to the water pollution control field of environmental engineering.
Background technology
Tobacco leaf is when producing, and raw material can not be utilized completely, and tobacco to the production process of making cigarette, can produce the particle that accounts for greatly former cigarette material total amount 1/3 from preliminary working, and these tobacco particles can't directly be made cigarette product as raw material again.The comprehensive utilization that produces, realizes particle in order to reduce waste material, the 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, as cigarette filler, reduce the tar content in the cigarette, reduce the Health hazard that smoking brings to human body.The use of tobacco sheet has the tobacco quality of raising, reduces the 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, the paper process thin slice has obvious advantage: reduce production of cigarettes cost, constant product quality, filling value and becomes that the silk rate is high, anti-machining property is good, improved the combustionvelocity of cigarette and has reduced releasing content of coke tar, product plasticity-is high and more easily process, and is effective technique of present production " health type " cigarette.Have roll-in method and the incomparable advantage of thick slurry method just because of the papermaking thin slice, therefore all obtained extensive popularization at home and abroad.
The general character of the existing paper waste of waste water that produces in the tobacco sheets by paper making method production process is as containing a large amount of fibers, have again simultaneously that tobacco wastewater colourity is high, biodegradability is relatively poor, contain to characteristics such as the disadvantageous nicotine of microorganism growth, tar and the high 150～500mg/L of calcium-magnesium content main contamination index such as following table in the waste water:
| Sequence number | Project | Index |
| 1 | Chemical oxygen demand (COD) (COD Cr） | 1500~25000mg/ |
| 2 | Five-day BOD (BOD 5） | 600~10000mg/ |
| 3 | Suspended substance (SS) | 700~15000mg/L |
| 4 | The pH value | 5.5~6.5 |
| 5 | Colourity | 1000 ~ 25000 |
| 6 | Water temperature | 45~65 |
| 7 | Ca 2+ | 150~500 mg/L |
Simultaneously waste strength fluctuation is larger, COD
CrFrom 1500～25000mg/L, SS is from 700～15000mg/L, and nicotine and tar suppress microorganism growth, and the calcium-magnesium content height causes reactor fouling normally not 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 may further comprise the steps: by the grid coarse filtration, gravity flow enters wastewater equalization pond with factory effluent; By lift pump the waste water lifting in the wastewater equalization pond is added Ca-diatom soil series compound flocculating agent reaction 5-10min to the coagulator, then add bodied ferric sulfate, the polyacrylamide separating agent enters the reaction of static reaction pond, the reaction times is 50-60min; Be to pump in the ultrasonic micro-electrolysis reactor after the slant acidity with the pH regulator of the organic waste water of lower concentration, jointly react by ultrasonic wave and little electrolysis that make Chemical Oxygen Demand in Wastwater material rapid-digestion, the reaction times is 30-60min; Again with waste water process charcoal absorption and quartz sand filtration; After processing through overlapping screwed sludge dewatering equipment, uses as solid fuel in the mud that equalizing tank and static reaction pond workshop section are produced.
Disclose papermaking method tobacco sheet production wastewater among the Chinese patent CN10133045A and to three-stage filtration, be back to respectively again slurrying workshop section through one, reuse water adopts the method that regularly is thrown into sewage works, but factory effluent loops back for the production of affecting greatly the thin slice quality.
Chinese patent CN1683261A discloses papermaking method tobacco sheet production wastewater and has removed wherein suspended solid through coagulating treatment, By Bubble-floating Method first, then sends into the most COD material is removed in the aeration tank by aerobic microbiological method.
Above method all has certain effect to the processing of tobacco sheet factory effluent, technical process is long, facility investment is large, floor space is large but exist, the defectives such as working cost height, more seriously owing to contain a large amount of calcium in the waste water, directly cause a large amount of foulings of biochemical treatment system and film separating system, system can't normally move, and the waste discharge after existing wastewater processing technology is processed can not reach emission standard, let alone recycling utilization.
Summary of the invention
The object of the invention is to for existingly in the existing tobacco production wastewater treatment method establish 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 the processing is not up to standard, can't recycling utilization etc. defective, 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 may further comprise the steps:
(1) slagging-off
The tobacco sheet factory effluent enters mechanical coarse rack water collecting basin after pipeline is collected, coarse rack is set in the pond, cursory thing thick in the sewage is isolated removal, then pass through lift pump, the tobacco sheet factory effluent is promoted in the rotating machinery fine grid machine, further remove the suspended substance of most of insolubility in the water by the filtration of filter screen, generation every slag packing outward transport, waste water is then processed through chemical decalcification;
(2) chemical decalcification
Water outlet after the slagging-off flows into first equalizing tank through pipeline, enter again one-level decalcification reaction tank, the sodium hydroxide solution or the saturated clear liquor of lime adjust pH to 8.5～9.5 that under agitation add first 300 ~ 900mg/L through chemicals dosing plant, after removing false hardness (supercarbonate), enter secondary decalcification reaction tank, pass into the gas that the UASB anaerobic pond produces in step (4) anaerobic treatment, make CO in the gas
2Generate carbonate deposition with the calcium ions and magnesium ions reaction, perhaps add the Na of 200 ~ 800mg/L
2CO
3Make pH value to 8～9, carbonate and calcium ions and magnesium ions reaction generate carbonate deposition, enter preliminary sedimentation tank precipitation 3～4 hours;
(3) air supporting
The supernatant liquor of preliminary sedimentation tank pumps into filtration unit, get filtrate and precipitation, filtrate flows into coagulation basin, the PAC that under agitation condition, adds first 5 ~ 10mg/L, add at last the negatively charged ion polyphenyl alkene acid amides (PAM) of 2 ~ 3mg/L, enter air flotation pool after reacting completely and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in the sludge sump through pump and pipeline, carry out at last filtering separation in sludge dehydration device, the air flotation pool water outlet enters anaerobic pond; Described filtration unit is a kind of of centrifugal filter, vacuum filter or pressure filter;
(4) anaerobic treatment
The air flotation pool water outlet promotes through lift pump and enters the 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 in the process UASB anaerobic pond, after collecting through gas collector, the methane and carbon dioxide that produces imports the secondary decalcification reaction tank in the chemical decalcification of step (2), reclaim biogas in gas holder after secondary decalcification reaction tank purifies, waste water then enters step (5); The time that anaerobic treatment is processed 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
The 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, can carry out denitrogenation dephosphorizing under the alternating action of aerobic microbiological, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD, evenly fill up a large amount of biological suspended packings in the Aerobic Pond, for providing, aerobic microbiological perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface, be provided with the aeration aerating stirring system in the Aerobic Pond bottom, sewage is carried out oxygenation, make the dissolved oxygen in the water maintain 2～4 mg/L, the effect that utilizes simultaneously gas to rise, suspended substance in the pond is contacted with water is more abundant, and by the agitaion of gas and clear water back flushing, the aging microbial film that can effectively grow to filling surface washes away in addition, impel biomembranous update, make microbial film keep higher activity;
(7) re-electrolysis
The second pond water outlet again enters electrolysis machine b and carries out electrolysis, and electrolysis machine b adjacent two interelectrode voltages are 2～6V, and current density is 20～200mA/cm
2
(8) film is processed or BAF biochemical (BAF is biochemical)
Waste water after the re-electrolysis enters membrane treatment appts or BAF, and filtering separation or oxidation degradation effect by membrane treatment appts purify waste water, further remove COD, SS and ammonia nitrogen, are purified waste water; Described membrane treatment appts is membrane bioreactor (MBR device) or ultra-filtration equipment is a kind of;
(9) three electrolysis
After the film processing of waste water process or the BAF biochemical treatment, water outlet is processed through electrolysis machine c again, can further remove colourity, and waste water is carried out sterilization and disinfection;
(10) desalination
Waste water after three electrolysis enters desalting plant, separates to get water-dialyzing and condensed water, and water-dialyzing enters the reuse water basin, and a condensed water then part flow to equalizing tank in the chemical decalcification of step (2) by back of pipeline, and remainder discharges through discharge channel; Described desalting plant is a kind of 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 and step (8) membrane treatment appts or the biochemical treatment of aeration biochemical filter tank produced during UASB anaerobic pond, step (6) A/O processed in filtration unit in preliminary sedimentation tank in the chemical decalcification of step (2), step (3) air supporting and air flotation pool, step (4) anaerobic treatment all enters sludge sump by pipeline, then pass through the dehydration of sludge filter press so that reducing sludge volume, mud cake carries out burning disposal after the dehydration, and filtrate then 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 the UASB anaerobic pond produces is led to secondary decalcification pond, makes CO in the gas
2When generating carbonate deposition with the calcium ions and magnesium ions reaction, the hydrogen sulfide in the biogas, sulfur alcohol compound, ammonia etc. and calcium ions and magnesium ions reaction make biogas also obtain to purify, and the biogas after the purification can be collected in the gas holder and further utilize.
Air supporting described in step (3) air supporting is a kind of 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 a kind of of centrifuging, vacuum filtration or press filtration; The whizzer working speed of centrifuging is 3000～5000 rev/mins; The filter cloth aperture of vacuum filtration and press filtration is less than 5um.
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 the described electrolyzer is a kind of in graphite, titanium, iron, aluminium, zinc, copper, lead, nickel, molybdenum, chromium, alloy and the 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 a kind of of hollow fiber film assembly or plate film assembly; Hollow fiber film assembly is a kind of in Pvdf Microporous Hollow Fiber Membrane assembly, polypropylene hollow fiber membrane assembly, ps hollow fiber uf membrane assembly, polyethersulfone assembly, polyacrylonitrile assembly and the PVC hollow fiber membrane assembly, membrane pore size is 0.10～0.2 μ m, operating pressure is-1～-50kPa, working temperature is 5～45 ℃; Described ultra-filtration equipment is a kind of 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 ℃, the operating pressure of immersion ultrafiltration is-1～-50kPa, 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 the 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 ℃, and optimum temps is 25～35 ℃; Nanofiltration membrane component in the described nanofiltration system is a kind of of tubular membrane component, rolled membrane module or plate film assembly, and operating pressure is 6～45bar, and working temperature is 20～45 ℃, and optimum temps is 25～35 ℃; 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 effect of above processing:
The effect of each treatment process of table 1 tobacco sheet factory effluent
The present invention has following outstanding advantages compared with the prior art:
(1) after the reaction of the one-level decalcification by chemical decalcification system removes false hardness (supercarbonate), make carbonate and calcium ions and magnesium ions reaction generate carbonate deposition through secondary decalcification reaction tank again, then carbonate deposition takes off surely, flocculates mutually with the coagulant aids such as negatively charged ion polyphenyl alkene acid amides (PAM) in coagulation basin, be gathered into thick alumina blossom particles, in preliminary sedimentation tank, settle down, high-concentration Ca, magnesium ion in the final effective elimination tobacco sheet factory effluent, clearance reaches 50 ~ 90%, reduce water hardness, so that Ca
2+Be lower than 80 mg/L, prevent reactor fouling, guarantee 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 the waste water is dropped to below the 7000mg/L.
(3) after the UASB system for anaerobic treatment is processed, after collecting through gas collector, the index decreases such as the COD in the waste water, BOD, the gas of generation import the secondary decalcification reaction tank in the chemical decalcification, make CO in the gas
2Generate carbonate deposition with the calcium ions and magnesium ions reaction, on the one hand CO in the gas recovery
2, so that gas is utilized effectively; On the other hand by the H in the secondary decalcification reaction tank removal gas
2S, Purge gas, biogas is collected by gas holder and is utilized or high altitude discharge.
(3) through after slagging-off and the processing of chemical decalcification system, the SS clearance in the waste water reaches more than 95%, and the SS in the 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 that produces by the nano-catalytic electrolysis makes the difficult biochemical macromolecular cpd open loop chain rupture in the waste water, become can be biochemical small molecules, further improve the B/C value, improve the condition of follow-up biochemical treatment, and remove colourity and stink in the waste water, reduce the indexs such as ammonia nitrogen, COD.
(5) through the A/O biochemistry pool, by the alternating action of anaerobic-aerobic, can carry out denitrogenation dephosphorizing to sewage.
(6) through after the aeration biochemical filter tank biochemical treatment, the oxygenolysis by aerobic microbiological thoroughly decomposes pollutant in water, so that stable effluent quality, qualified discharge.
(7) the tobacco sheet factory effluent is through processing, and 75%～85% can recycling utilization, has both reduced discharge of wastewater, avoid the waste water environmental pollution, reduce again water resource waste, can also make the recirculated water cost of regeneration be lower than the tap water price, economical rationality produces preferably economic benefit.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
The present invention is in the design to tobacco sheet production wastewater treatment method of composition, character and the existing processing scheme of existing tobacco sheet factory effluent being goed deep into finish after 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 the tobacco sheet factory effluent.
1 the specific embodiment of the present invention is described with reference to the accompanying drawings.
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.
The water-quality guideline of table 2 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | Measured |
| 1 | COD Cr | mg/L | 25000 | 5 | Colourity | Doubly | 25000 |
| 2 | BOD 5 | mg/L | 6000 | 6 | Ca 2+ | mg/L | 500 |
| 3 | SS | mg/L | 15000 | 7 | Water temperature | ℃ | 50 |
| 4 | The pH value | —— | 5.5 |
(1) slagging-off
The tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in the pond, cursory thing thick in the sewage is isolated removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, the tobacco sheet factory effluent is promoted in the rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in the water by the filtration of filter screen, what produce transports outward every the slag packing, and waste water is processed through chemical decalcification.
(2) chemical decalcification
Water outlet after the slagging-off flows into first equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, the sodium hydroxide solution adjust pH to 8.5 that under agitation adds first 600mg/L through chemicals dosing plant, after removing false hardness (supercarbonate), enter secondary decalcification reaction tank 5, pass into the gas that UASB anaerobic pond 10 produces in step (4) anaerobic treatment, make CO in the gas
2Generate carbonate deposition with the calcium ions and magnesium ions reaction, 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, thereby removes the calcium ions and magnesium ions in the tobacco processing waste water, and clearance reaches 84%, reduces water hardness, so that Ca
2+Concentration prevents that less than 80 mg/L follow-up equipment, facility are because of too high Ca
2+Fouling;
(3) air supporting
Supernatant liquor in the preliminary sedimentation tank 6 pumps in the filtration unit 7 through lift pump 23, present embodiment adopts whizzer, centrifugation under 4200 rev/mins rotating speed, get filtrate and precipitation, filtrate flows into coagulation basin 8, the PAC that under agitation condition, adds first 10mg/L, the negatively charged ion polyphenyl alkene acid amides (PAM) that adds at last 2mg/L, enter air flotation pool 9 after reacting completely and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in the sludge sump 20 through pump and pipeline, carry out at last filtering separation in sludge dehydration device 21, air flotation pool 9 water outlets then pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion;
(4) anaerobic treatment
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make simultaneously the difficult biochemical macromolecular cpd open loop chain rupture in the waste water, become can be biochemical small molecules, further improve the 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
The 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 to fill up a large amount of biological suspended packings, perches for aerobic microbiological provides, the place of growth and breeding, so that microorganism forms microbial film at filling surface.Be provided with the aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out oxygenation, make the dissolved oxygen in the water maintain 2～4 mg/L, the effect that utilizes simultaneously gas to rise, suspended substance in the pond is contacted with water is more abundant, and by the agitaion of gas and clear water back flushing, the aging microbial film that can effectively grow to filling surface washes away in addition, impel biomembranous update, make microbial film keep higher activity.
(7) re-electrolysis
(8) BAF biochemical (BAF is biochemical)
Waste water after the re-electrolysis enters BAF 16, by the oxidation degradation effect waste water is purified, and further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
After 16 biochemical treatments of waste water process BAF, 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 sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters desalting plant 30 through working shaft 29, present embodiment adopts reverse osmosis unit, separate to get water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, a condensed water then part flow to equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder is through discharge channel 18 dischargings;
(11) sludge treatment
The mud that anoxic pond 12, Aerobic Pond 13 and second pond 14 and 16 biochemical treatments of step (8) aeration biochemical filter tank produced during UASB anaerobic pond 10, step (6) A/O processed in air flotation pool in preliminary sedimentation tank in the chemical decalcification of step (2), step (3) air supporting, step (4) anaerobic treatment all enters sludge sump 20 by pipeline, then pass through the dehydration of sludge dehydration device 21 so that reducing sludge volume, mud cake carries out burning disposal after the dehydration, and filtrate then is back to the equalizing tank 3 in the chemical decalcification of step (2).
Through effect such as the table 3 after each operation processing
Effect after each treatment process of table 3 tobacco sheet factory effluent is processed
The reuse water water-quality guideline is as shown in table 4 after measured.
The water-quality guideline of table 4 reuse water
| Sequence number | Project | Unit | Measured value | GB 5749-2006 |
| 1 | The pH value | —— | 7.0 | 6.5~8.5 |
| 2 | Colourity | Doubly | 2 | ≤3 |
| 3 | Chemical oxygen demand COD Cr | mg/L | ≤5 | ≤5 |
| 4 | Total dissolved solid TDS | mg/ | 23 | 150 |
| 5 | Smell | —— | Do not detect | Must not detect |
| 6 | Turbidity | NTU | ≤1 | ≤1 |
| 7 | Ammonia nitrogen | mg/L | 0.31 | ≤0.5 |
| 8 | Redox potential | mV | ≤300 | 300 |
| 9 | SS | mg/L | Do not detect |
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.
The water-quality guideline of table 5 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | |
| 1 | COD Cr | mg/L | 9000 | 5 | Colourity | Doubly | 12000 |
| 2 | BOD 5 | mg/L | 3000 | 6 | Ca 2+ | mg/L | 300 |
| 3 | SS | mg/L | 5000 | 7 | Water temperature | ℃ | 65 |
| 4 | The pH value | —— | 6.2 |
(1) slagging-off
The tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in the pond, cursory thing thick in the sewage is isolated removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, the tobacco sheet factory effluent is promoted in the rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in the water by the filtration of filter screen, what produce transports outward every the slag packing, and waste water is processed through chemical decalcification.
(2) chemical decalcification
Water outlet after the slagging-off flows into first equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, after chemicals dosing plant under agitation adds first the saturated settled solution of 900mg/L lime adjust pH to 9.5, removes false hardness (supercarbonate), enter secondary decalcification reaction tank 5, add the Na of 400mg/L
2CO
3Adjust pH to 8.5 makes the reaction of carbonate and calcium ions and magnesium ions generate carbonate deposition, enters preliminary sedimentation tank 6 after reacting completely and carries out precipitate and separate, sedimentation time is 3 hours, thereby removes the calcium ions and magnesium ions in the tobacco processing waste water, and clearance reaches 83.3%, reduce water hardness, so that Ca
2+Concentration prevents that less than 50 mg/L follow-up equipment, facility are because of too high Ca
2+Fouling;
(3) air supporting
Supernatant liquor in the preliminary sedimentation tank 6 pumps into filtration unit 7 through lift pump 23, present embodiment adopts in the vacuum filter, filtering separation under-0.3MPa vacuum condition, the filter cloth aperture is less than 5um, get filtrate and precipitation, filtrate flows into coagulation basin 8, the PAC that under agitation condition, adds first 5mg/L, the negatively charged ion polyphenyl alkene acid amides (PAM) that adds at last 3mg/L, enter air flotation pool 9 after reacting completely and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in the sludge sump 20 through pump and pipeline, carry out at last filtering separation in sludge dehydration device 21, and air flotation pool 9 water outlets then pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion;
(4) anaerobic treatment
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make simultaneously the difficult biochemical macromolecular cpd open loop chain rupture in the waste water, become can be biochemical small molecules, further improve the 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
The 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 to fill up a large amount of biological suspended packings, perches for aerobic microbiological provides, the place of growth and breeding, so that microorganism forms microbial film at filling surface.Be provided with the aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out oxygenation, make the dissolved oxygen in the water maintain 2～4 mg/L, the effect that utilizes simultaneously gas to rise, suspended substance in the pond is contacted with water is more abundant, and by the agitaion of gas and clear water back flushing, the aging microbial film that can effectively grow to filling surface washes away in addition, impel biomembranous update, make microbial film keep higher activity.
(7) re-electrolysis
(8) MBR processes
Waste water after the re-electrolysis enters membrane treatment appts 16, and present embodiment adopts the MBR device, separates with membrane filtration that by the oxidation degradation effect waste water is purified, and further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
After the biochemical treatment of waste water process MBR device, 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 sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters nanofiltration device 30 through working shaft 29, separate to get water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, and a condensed water then part flow to equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder is through discharge channel 18 dischargings.
(11) sludge treatment
The mud that anoxic pond 12, Aerobic Pond 13 and second pond 14 and the biochemical treatment of step (8) MBR device produced during UASB anaerobic pond 10, step (6) A/O processed in air flotation pool 9 in preliminary sedimentation tank 6 in the chemical decalcification of step (2), step (3) air supporting, step (4) anaerobic treatment all enters sludge sump 20 by pipeline, then pass through the dehydration of sludge dehydration device 21 so that reducing sludge volume, mud cake carries out burning disposal after the dehydration, and filtrate then is back to the equalizing tank 3 in the chemical decalcification of step (2).
Through effect such as the table 6 after each operation processing
Effect after each treatment process of table 6 tobacco sheet factory effluent is processed
The reuse water water-quality guideline is as shown in table 7 after measured.
The water-quality guideline of table 7 reuse water
| Sequence number | Project | Unit | Measured value | GB 5749-2006 |
| 1 | The pH value | —— | 6.8 | 6.5~8.5 |
| 2 | Colourity | Doubly | 2 | ≤3 |
| 3 | Chemical oxygen demand COD Cr | mg/L | ≤5 | ≤5 |
| 4 | Total dissolved solid TDS | mg/L | 120 | 150 |
| 5 | Smell | —— | Do not detect | Must not detect |
| 6 | Turbidity | NTU | ≤1 | ≤1 |
| 7 | Ammonia nitrogen | mg/L | 0.4 | ≤0.5 |
| 8 | Redox potential | mV | ≤300 | 300 |
| 9 | SS | mg/L | Do not detect |
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.
The water-quality guideline of table 8 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | |
| 1 | COD C | mg/L | 4000 | 5 | Colourity | Doubly | 1300 |
| 2 | BOD 5r | mg/L | 1800 | 6 | Ca 2+ | mg/L | 400 |
| 3 | SS | mg/L | 1200 | 7 | Water temperature | ℃ | 50 |
| 4 | The pH value | —— | 6.5 |
(1) slagging-off
The tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in the pond, cursory thing thick in the sewage is isolated removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, the tobacco sheet factory effluent is promoted in the rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in the water by the filtration of filter screen, what produce transports outward every the slag packing, and waste water is processed through chemical decalcification.
(2) chemical decalcification
Water outlet after the slagging-off flows into first equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, after chemicals dosing plant under agitation adds first the saturated settled solution of 300mg/L lime adjust pH to 9.0, removes false hardness (supercarbonate), enter secondary decalcification reaction tank 5, add the Na of 200mg/L
2CO
3Adjust pH to 9.0 makes the reaction of carbonate and calcium ions and magnesium ions generate carbonate deposition, enters preliminary sedimentation tank 6 after reacting completely and carries out precipitate and separate, sedimentation time is 3.5 hours, thereby removes the calcium ions and magnesium ions in the tobacco processing waste water, and clearance reaches 87.5%, reduce water hardness, so that Ca
2+Concentration prevents that less than 50 mg/L follow-up equipment, facility are because of too high Ca
2+Fouling;
(3) air supporting
Supernatant liquor in the preliminary sedimentation tank 6 pumps in the filtration unit 7 through lift pump 23, present embodiment adopts pressure filter, filtering separation in pressure filter, the filter cloth aperture is less than 5um, get filtrate and precipitation, filtrate flows into coagulation basin 8, the PAC that under agitation condition, adds first 8mg/L, the negatively charged ion polyphenyl alkene acid amides (PAM) that adds at last 2.5mg/L, enter air flotation pool 9 after reacting completely and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in the sludge sump 20 through pump and pipeline, carry out at last filtering separation in sludge dehydration device 21, and air flotation pool 9 water outlets then pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion;
(4) anaerobic treatment
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make simultaneously the difficult biochemical macromolecular cpd open loop chain rupture in the waste water, become can be biochemical small molecules, further improve the 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
The 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 to fill up a large amount of biological suspended packings, perches for aerobic microbiological provides, the place of growth and breeding, so that microorganism forms microbial film at filling surface.Be provided with the aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out oxygenation, make the dissolved oxygen in the water maintain 2～4 mg/L, the effect that utilizes simultaneously gas to rise, suspended substance in the pond is contacted with water is more abundant, and by the agitaion of gas and clear water back flushing, the aging microbial film that can effectively grow to filling surface washes away in addition, impel biomembranous update, make microbial film keep higher activity.
(7) re-electrolysis
(8) uf processing
Waste water after the re-electrolysis enters membrane treatment appts 16, and present embodiment adopts ultra-filtration equipment, separates that by ultrafiltration membrance filter waste water is purified, and further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
After waste water was processed through ultra-filtration equipment, water outlet was promoted to electrolysis machine c17 by lift pump 25 and processes, and can further remove colourity, and waste water is carried out sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters desalting plant 30 through working shaft 29, present embodiment adopts the capacitive adsorption deionizing desalting plant, separate to get water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, a condensed water then part flow to equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder is through discharge channel 18 dischargings.
(11) sludge treatment
Through effect such as the table 9 after each operation processing
Effect after each treatment process of table 9 tobacco sheet factory effluent is processed
The reuse water water-quality guideline is as shown in table 10 after measured.
The water-quality guideline of table 10 reuse water
| Sequence number | Project | Unit | Measured value | GB 5749-2006 |
| 1 | The pH value | —— | 7.2 | 6.5~8.5 |
| 2 | Colourity | Doubly | 2 | ≤3 |
| 3 | Chemical oxygen demand COD Cr | mg/L | ≤5 | ≤5 |
| 4 | Total dissolved solid TDS | mg/L | 130 | 150 |
| 5 | Smell | —— | Do not detect | Must not detect |
| 6 | Turbidity | NTU | ≤1 | ≤1 |
| 7 | Ammonia nitrogen | mg/L | ≤0.5 | ≤0.5 |
| 8 | Redox potential | mV | ≤300 | 300 |
| 9 | SS | mg/L | Do not detect |
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.
The water-quality guideline of table 11 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | |
| 1 | COD C | mg/L | 1500 | 5 | Colourity | Doubly | 1000 |
| 2 | BOD 5r | mg/L | 600 | 6 | Ca 2+ | mg/L | 150 |
| 3 | SS | mg/L | 700 | 7 | Water temperature | ℃ | 45 |
| 4 | The pH value | —— | 6.0 |
(1) slagging-off
The tobacco sheet factory effluent enters mechanical coarse rack water collecting basin 1 after pipeline is collected, coarse rack is set in the pond, cursory thing thick in the sewage is isolated removal, to prevent that follow-up treatment facility from stopping up, then by lift pump 22, the tobacco sheet factory effluent is promoted in the rotating machinery fine grid machine 2, further removes the suspended substance of most of insolubility in the water by the filtration of filter screen, what produce transports outward every the slag packing, and waste water is processed through chemical decalcification.
(2) chemical decalcification
Water outlet after the slagging-off flows into first equalizing tank 3 through pipeline, enter again one-level decalcification reaction tank 4, under agitation add first 900mg/LNaOH solution adjust pH to 9.5 through chemicals dosing plant, remove false hardness (supercarbonate) after, enter secondary decalcification reaction tank 5, add the Na of 800mg/L
2CO
3Adjust pH to 9.0 makes the reaction of carbonate and calcium ions and magnesium ions generate carbonate deposition, enters preliminary sedimentation tank 6 after reacting completely and carries out precipitate and separate, sedimentation time is 3 hours, thereby removes the calcium ions and magnesium ions in the tobacco processing waste water, and clearance reaches 66.7%, reduce water hardness, so that Ca
2+Concentration prevents that less than 50 mg/L follow-up equipment, facility are because of too high Ca
2+Fouling;
(3) air supporting
Supernatant liquor in the preliminary sedimentation tank 6 pumps into filtration unit 7 through lift pump 23, present embodiment adopts in the whizzer, centrifugation under 5000 rev/mins rotating speed, get filtrate and precipitation, filtrate flows into coagulation basin 8, the PAC that under agitation condition, adds first 8mg/L, the negatively charged ion polyphenyl alkene acid amides (PAM) that adds at last 2.5mg/L, enter air flotation pool 9 after reacting completely and carry out dissolved air flotation, filtering-depositing and scum silica frost (being mud) are sent in the sludge sump 20 through pump and pipeline, carry out at last filtering separation in sludge dehydration device 21, air flotation pool 9 water outlets then pump into anaerobic pond 10 through lift pump 24 and carry out anaerobic digestion;
(4) anaerobic treatment
(5) electrolysis
10 water outlets of UASB anaerobic pond enter electrolysis machine a11 and carry out electrolysis, to remove colourity, smelly, make simultaneously the difficult biochemical macromolecular cpd open loop chain rupture in the waste water, become can be biochemical small molecules, further improve the 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
The 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 to fill up a large amount of biological suspended packings, perches for aerobic microbiological provides, the place of growth and breeding, so that microorganism forms microbial film at filling surface.Be provided with the aeration aerating stirring system in Aerobic Pond 13 bottoms, sewage is carried out oxygenation, make the dissolved oxygen in the water maintain 2～4 mg/L, the effect that utilizes simultaneously gas to rise, suspended substance in the pond is contacted with water is more abundant, and by the agitaion of gas and clear water back flushing, the aging microbial film that can effectively grow to filling surface washes away in addition, impel biomembranous update, make microbial film keep higher activity.
(7) re-electrolysis
(8) uf processing
Waste water after the re-electrolysis enters membrane treatment appts 16, and present embodiment adopts ultra-filtration equipment, separates that by ultrafiltration membrance filter waste water is purified, and further removes COD, SS and ammonia nitrogen, is purified waste water.
(9) three electrolysis
After waste water was processed through ultra-filtration equipment, water outlet was promoted to electrolysis machine c17 by lift pump 25 and processes, and can further remove colourity, and waste water is carried out sterilization and disinfection.
(10) desalination
Waste water after three electrolysis enters desalting plant 30 through working shaft 29, present embodiment adopts electrodialysis unit, separate to get water-dialyzing and condensed water, water-dialyzing enters reuse water basin 31, a condensed water then part flow to equalizing tank 3 in the chemical decalcification of step (2) by back of pipeline, and remainder is through discharge channel 18 dischargings.
(11) sludge treatment
Through effect such as the table 12 after each operation processing
Effect after each treatment process of table 12 tobacco sheet factory effluent is processed
The reuse water water-quality guideline is as shown in table 13 after measured.
The water-quality guideline of table 13 reuse water
| Sequence number | Project | Unit | Measured value | GB 5749-2006 |
| 1 | The pH value | —— | 7.2 | 6.5~8.5 |
| 2 | Colourity | Doubly | 2 | ≤3 |
| 3 | Chemical oxygen demand COD Cr | mg/L | ≤5 | ≤5 |
| 4 | Total dissolved solid TDS | mg/L | 130 | 150 |
| 5 | Smell | —— | Do not detect | Must not detect |
| 6 | Turbidity | NTU | ≤1 | ≤1 |
| 7 | Ammonia nitrogen | mg/L | ≤0.5 | ≤0.5 |
| 8 | Redox potential | mV | ≤300 | 300 |
| 9 | SS | mg/L | Do not detect |
Above-mentioned only is the specific embodiment of the present invention, but design concept of the present invention is not limited to this, allly utilizes this design that the present invention is carried out the change of unsubstantiality, 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 may further comprise the steps:
(1) slagging-off
The tobacco sheet factory effluent enters mechanical coarse rack water collecting basin after pipeline is collected, coarse rack is set in the pond, cursory thing thick in the sewage is isolated removal, then pass through lift pump, the tobacco sheet factory effluent is promoted in the rotating machinery fine grid machine, further remove the suspended substance of most of insolubility in the water by the filtration of filter screen, generation every slag packing outward transport, waste water is then processed through chemical decalcification;
(2) chemical decalcification
Water outlet after the slagging-off flows into first equalizing tank through pipeline, enter again one-level decalcification reaction tank, the sodium hydroxide solution or the saturated clear liquor of lime adjust pH to 8.5～9.5 that under agitation add first 300 ~ 900mg/L through chemicals dosing plant, after removing false hardness supercarbonate, enter secondary decalcification reaction tank, pass into the gas that the UASB anaerobic pond produces in step (4) anaerobic treatment, make CO in the gas
2Generate carbonate deposition with the calcium ions and magnesium ions reaction, perhaps add the Na of 200 ~ 800mg/L
2CO
3Make pH value to 8～9, carbonate and calcium ions and magnesium ions reaction generate carbonate deposition, enter 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, get filtrate and precipitation, filtrate flows into coagulation basin, the PAC that under agitation condition, adds first 5 ~ 10mg/L, the negatively charged ion polyphenyl alkene acid amides that adds at last 2 ~ 3mg/L, enter air flotation pool after reacting completely and carry out dissolved air flotation, filtering-depositing and scum silica frost are sent in the sludge sump through pump and pipeline, in sludge dehydration device, carry out at last filtering separation, the air flotation pool water outlet enters anaerobic pond, described filtration is centrifuging, vacuum filtration or press filtration a kind of, the whizzer working speed of centrifuging is 3000～5000 rev/mins, the filter cloth aperture of vacuum filtration and press filtration is less than 5um;
(4) anaerobic treatment
The air flotation pool water outlet promotes through lift pump and enters the 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 in the process UASB anaerobic pond, after collecting through gas collector, the methane and carbon dioxide that produces imports the secondary decalcification reaction tank in the chemical decalcification of step (2), after purifying, reclaims secondary decalcification reaction tank biogas in gas holder, waste water then 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
The 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, can carry out denitrogenation dephosphorizing under the alternating action of aerobic microbiological, and by the organism in the further oxygenolysis waste water of aerobic treatment, the degree of depth is removed COD and BOD, evenly fill up a large amount of biological suspended packings in the Aerobic Pond, for providing, aerobic microbiological perches, the place of growth and breeding, so that microorganism forms microbial film at filling surface, be provided with the aeration aerating stirring system in the Aerobic Pond bottom, sewage is carried out oxygenation, make the dissolved oxygen in the water maintain 2～4 mg/L, the effect that utilizes simultaneously gas to rise, suspended substance in the pond is contacted with water is more abundant, by the agitaion of gas and clear water back flushing, effectively the aging microbial film of filling surface growth washed away in addition, impel biomembranous update, make microbial film keep higher activity;
(7) re-electrolysis
The second pond water outlet again enters electrolysis machine b and carries out electrolysis, and electrolysis machine b adjacent two interelectrode voltages are 2～6V, and current density is 20～200mA/cm
2
(8) film is processed or BAF biochemistry
Waste water after the 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 a kind of of MBR device or ultra-filtration equipment;
(9) three electrolysis
After the film processing of waste water process or the BAF biochemical treatment, water outlet is processed through electrolysis machine c again, can further remove colourity, and waste water is carried out sterilization and disinfection;
(10) desalination
Waste water after three electrolysis enters desalting plant, separate to get water-dialyzing and condensed water, water-dialyzing enters the reuse water basin, a condensed water then part flow to equalizing tank in the chemical decalcification of step (2) by back of pipeline, remainder discharges through discharge channel, and described desalting plant is a kind of 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 in the chemical decalcification of step (2), step (3) air supporting, the UASB anaerobic pond in step (4) anaerobic treatment, step (6) A/O process and step (8) membrane treatment appts or the biochemical treatment of aeration biochemical filter tank produce all enters sludge sump by pipeline, then pass through the dehydration of sludge dehydration device so that reducing sludge volume, mud cake carries out burning disposal after the dehydration, and filtrate then 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: air supporting is a kind of of gas distribution By Bubble-floating Method, electric floating method, biology and chemical floatation treatment, dissolved air flotation described in step (3) slagging-off.
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, and the electrode in the described electrolyzer is a kind of in graphite, titanium, iron, aluminium, zinc, copper, lead, nickel, molybdenum, chromium, alloy and the 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, it is characterized in that: the membrane module of the described MBR device of step (8) is a kind of of hollow fiber film assembly or plate film assembly; Hollow fiber film assembly is a kind of in Pvdf Microporous Hollow Fiber Membrane assembly, polypropylene hollow fiber membrane assembly, ps hollow fiber uf membrane assembly, polyethersulfone assembly, polyacrylonitrile assembly and the PVC hollow fiber membrane assembly, membrane pore size is 0.10～0.2 μ m, operating pressure is-1～-50kPa, working temperature is 5～45 ℃.
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 a kind of 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 ℃, the operating pressure of immersion ultrafiltration is-1～-50kPa, 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 the 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 ℃.
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 a kind of of tubular membrane component, rolled membrane module or plate film assembly, operating pressure is 6～45bar, and working temperature is 20～45 ℃.
9. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization method, it 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, it is characterized in that: the working conditions of the described capacitive adsorption deionizing of step (10) system is that volts DS is 110V～2 * 10
6V, strength of current is less than or equal to 1A.
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