CN103351088B - Treatment and regenerative cyclic utilization device for tobacco sheet production wastewater - Google Patents
Treatment and regenerative cyclic utilization device for tobacco sheet production wastewater Download PDFInfo
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Abstract
The invention relates to a treatment and regenerative cyclic utilization device for tobacco sheet production wastewater. The treatment and regenerative cyclic utilization device comprises a mechanical coarse-grille water collecting basin, a rotary fine-grille machine, a regulation pool, a primary decalcification reaction pool, a secondary decalcification reaction pool, a primary sedimentation tank, a filtering device, a coagulation tank, an air flotation tank, a UASB (Upflow Anaerobic Sludge Blanket) anaerobic tank, an electrolyzer a, an anaerobic pool, an aerobic pool, a secondary sedimentation tank, an electrolyzer b, a membrane treatment device or biological aerated filter, an electrolyzer c, a water supply pump, a desalting device, a reclaimed water storage tank, a sludge tank, a sludge dewatering device, an accident pool, a gas collection device and a marsh gas storage tank. The treatment and regenerative cyclic utilization device has the advantages that on the basis that chemical decalcification techniques, biochemical techniques, electrochemical techniques, BAF (Biological Aerated Filter) techniques and membrane technologies are combined, the cost is lower, and the efficiency is higher; after the tobacco sheet production wastewater is treated, 75-85% of the tobacco sheet production wastewater can be utilized in a regenerative and cyclic manner, so that the discharge of the wastewater is reduced, the environmental pollution caused by the wastewater is avoided, and the waste of water resources is reduced; and the cost of reclaimed recycled water can be lower than the price of tap water, so that the reclaimed recycled water is economical and reasonable, and a better economic benefit is generated.
Description
Technical field
The present invention relates to a kind of processing and recycling utilization device 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 device 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 unit of the tobacco factory effluent of recycling utilization.
The processing of tobacco sheet factory effluent and recycling utilization device, comprise mechanical coarse rack water collecting basin, rotation fine grid machine, equalizing tank, one-level decalcification reaction tank, secondary decalcification reaction tank, preliminary sedimentation tank, filtration unit, coagulation basin, air flotation pool, UASB anaerobic pond, electrolysis machine a, anoxic pond, Aerobic Pond, second pond, electrolysis machine b, membrane treatment appts or BAF (BAF), electrolysis machine c, working shaft, desalting plant, reuse water basin, sludge sump, sludge dehydration device, accident pool, gas collector and biogas storage tank;
The import of described mechanical coarse rack water collecting basin connects with the outlet of tobacco wastewater, machinery coarse rack water collecting basin water outlet connects with rotation fine grid machine water-in, rotation fine grid machine water outlet connects with equalizing tank water-in, equalizing tank water outlet connects with one-level decalcification reaction tank water-in, one-level decalcification reaction tank water outlet connects with secondary decalcification reaction tank water-in, secondary decalcification reaction tank water outlet connects with preliminary sedimentation tank water-in, preliminary sedimentation tank water outlet connects with the import of filtration unit, the outlet of filtration unit connects with coagulation basin water-in, coagulation basin water outlet connects with air flotation pool water-in, air flotation pool water outlet with connect with UASB anaerobic pond water-in, UASB anaerobic pond water outlet connects with electrolysis machine a water-in, electrolysis machine a water outlet connects with anoxic pond water-in, anoxic pond water outlet connects with Aerobic Pond water-in, Aerobic Pond water outlet connects with second pond water-in, second pond water outlet connects with electrolysis machine b water-in, electrolysis machine b water outlet connects with water-in or the BAF water-in of membrane treatment appts, the water outlet of membrane treatment appts or BAF water outlet connect with electrolysis machine c water-in, electrolysis machine c water outlet connects with desalting plant water-in through working shaft, the water-dialyzing outlet of desalting plant connects the import of reuse water basin, the condensed water of desalting plant exports a road and flow to equalizing tank through back of pipeline, another road connects with discharge channel, the water-in of accident pool connects with the outlet of tobacco sheet factory effluent, and accident pool water outlet connects with mechanical coarse rack water collecting basin water-in, UASB anaerobic pond pneumatic outlet connects with gas collector import, and gas collector outlet connects with secondary decalcification reaction tank water-in, and the pneumatic outlet of secondary decalcification reaction tank connects with biogas storage tank import, throw out in preliminary sedimentation tank, UASB anaerobic pond, anoxic pond, Aerobic Pond, second pond, membrane treatment appts/BAF and the outlet of the scum silica frost of air flotation pool all connect with sludge sump import, and sludge sump outlet connects with sludge dehydration device import,
Described filtration unit is the one of centrifugal filter, vacuum filter or pressure filter; Described membrane treatment appts is the one of MBR device or ultra-filtration equipment; Described desalting plant is the one of reverse osmosis system, nanofiltration system, electrodialysis or capacitive adsorption deionizing system.
Described coagulation basin is with dispensing system and medicine system.
Described electrolysis machine a, electrolysis machine b and electrolysis machine c are equipped with power supply and electrolyzer; 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 hollow fiber film assembly of described MBR device or the one of 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 described reverse osmosis system 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.
Treatment process of the present invention is: tobacco sheet factory effluent → slagging-off → chemical decalcification → air supporting → anaerobic treatment → electrolysis → A/O processing → re-electrolysis → film processing/BAF biochemistry → tri-time electrolysis → desalination → reuse water.
Waste water is as shown in table 1 through the above effect of processing:
The effect of the each treatment process of table 1 tobacco sheet factory effluent
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 the biochemical treatment of aeration biochemical filter tank, 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 the processing of tobacco sheet factory effluent of the present invention and the block diagram of recycling utilization device.
Embodiment
1 explanation the specific embodiment of the present invention with reference to the accompanying drawings.
With reference to Fig. 1, the processing of tobacco sheet factory effluent and recycling utilization device, , comprise: mechanical coarse rack water collecting basin 1, rotation fine grid machine 2, equalizing tank 3, one-level decalcification reaction tank 4, secondary decalcification reaction tank 5, preliminary sedimentation tank 6, filtration unit 7, coagulation basin 8, air flotation pool 9, UASB anaerobic pond 10, electrolysis machine a11, anoxic pond 12, Aerobic Pond 13, second pond 14, electrolysis machine b15, membrane treatment appts/BAF16, electrolysis machine c17, discharge canal 18, accident pool 19, sludge sump 20, sludge dehydration device 21, lift pump 22, lift pump 23, lift pump 24, lift pump 25, lift pump 26, gas collector 27, biogas storage tank 28, working shaft 29, desalting plant 30 and reuse water basin 31.
The import of machinery coarse rack water collecting basin 1 connects with the outlet of tobacco sheet factory effluent, machinery coarse rack water collecting basin 1 water outlet connects with rotation fine grid machine 2 water-ins through lift pump 20, rotation fine grid machine 2 water outlets connect with equalizing tank 3 water-ins, equalizing tank 3 water outlets connect with one-level decalcification reaction tank 4 water-ins, one-level decalcification reaction tank 4 water outlets connect with secondary decalcification reaction tank 5 water-ins, secondary decalcification reaction tank 5 water outlets connect with preliminary sedimentation tank 6 water-ins, preliminary sedimentation tank 6 water outlets connect with filtration unit 7 water-ins through lift pump 23, filtration unit 7 water outlets connect with coagulation basin 8 water-ins, coagulation basin 8 water outlets connect with air flotation pool 9 water-ins, air flotation pool 9 water outlets connect with UASB anaerobic pond 10 water-ins through lift pump 24, UASB anaerobic pond 10 water outlets connect with electrolysis machine a11 water-in, electrolysis machine a11 water outlet connects with anoxic pond 12 water-ins, anoxic pond 12 water outlets connect with Aerobic Pond 13 water-ins, Aerobic Pond 13 water outlets connect with second pond 14 water-ins, second pond 14 water outlets connect with electrolysis machine b15 water-in, electrolysis machine b water outlet connects with water-in or the BAF16 water-in of membrane treatment appts, the water outlet of membrane treatment appts and BAF16 water outlet connect with electrolysis machine c17 water-in through lift pump 25, electrolysis machine c17 water outlet connects with desalting plant 30 water-ins through working shaft 29, the water-dialyzing outlet of desalting plant 30 connects the import of reuse water basin 31, the condensed water of desalting plant 30 exports a road and is back to equalizing tank 3 through stopping valve, another road connects with discharge channel 18, and throw out (being mud) in preliminary sedimentation tank 6, UASB anaerobic pond 10, anoxic pond 12, Aerobic Pond 13, second pond 14, membrane treatment appts/BAF16 and scum silica frost (the being mud) outlet of air flotation pool 9 connect with sludge sump 20 imports, sludge sump 20 outlets connect with sludge dehydration device 21 imports, the water-in of accident pool 19 connects with the outlet of tobacco sheet factory effluent, and accident pool 19 water outlets connect with mechanical coarse rack water collecting basin 1 water-in by pump 26, UASB anaerobic pond 10 pneumatic outlets connect with gas collector 27 imports, and gas collector 27 outlets connect with secondary decalcification reaction tank 5 water-ins, and the pneumatic outlet of secondary decalcification reaction tank 5 connects with biogas storage tank 28 imports.
As can be seen from Figure 1, mechanical coarse rack water collecting basin 1 and transporting outward by packing every slag that rotation fine grid machine 2 produces.
The present invention is the design to tobacco sheet production wastewater treatment and recycling utilization device 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 uses by the combination of the methods such as chemical decalcification, biochemistry, electrolysis, BAF, film processing, thereby forms a kind of processing and recycling utilization device that is particularly suitable for tobacco sheet factory effluent.
Provide the embodiment of tobacco sheet production wastewater treatment and recycling utilization device below in conjunction with Fig. 1.
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.
The water-quality guideline of table 2 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | Measured value |
| 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 | PH value | —— | 5.5 |
(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 rotation 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 again enter electrolysis machine b15 and carry out electrolysis, 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) aeration biochemical filter tank 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
The each treatment process of table 3 tobacco sheet factory effluent effect after treatment
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 standard |
| 1 | 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/L | 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 |
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.
The water-quality guideline of table 5 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | Measured value |
| 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 | PH value | —— | 6.2 |
(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 rotation 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 again enter electrolysis machine b15 and carry out electrolysis, 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
The each treatment process of table 6 tobacco sheet factory effluent effect after treatment
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 standard |
| 1 | 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 |
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.
The water-quality guideline of table 8 tobacco sheet factory effluent
| Sequence number | Project | Unit | Measured value | Sequence number | Project | Unit | Measured value |
| 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 | PH value | —— | 6.5 |
(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 rotation 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 again enter electrolysis machine b15 and carry out electrolysis, 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
The each treatment process of table 9 tobacco sheet factory effluent effect after treatment
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 standard |
| 1 | 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 | Measured value |
| 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 | PH value | —— | 6.0 |
(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 rotation 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 again enter electrolysis machine b15 and carry out electrolysis, 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
The each treatment process of table 12 tobacco sheet factory effluent effect after treatment
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 standard |
| 1 | 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 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 (9)
1. the processing of tobacco sheet factory effluent and recycling utilization device, is characterized in that: comprise mechanical coarse rack water collecting basin, rotation fine grid machine, equalizing tank, one-level decalcification reaction tank, secondary decalcification reaction tank, preliminary sedimentation tank, filtration unit, coagulation basin, air flotation pool, UASB anaerobic pond, electrolysis machine a, anoxic pond, Aerobic Pond, second pond, electrolysis machine b, membrane treatment appts or BAF, electrolysis machine c, working shaft, desalting plant, reuse water basin, sludge sump, sludge dehydration device, accident pool, gas collector and biogas storage tank;
The import of described mechanical coarse rack water collecting basin connects with the outlet of tobacco sheet factory effluent, machinery coarse rack water collecting basin water outlet connects with rotation fine grid machine water-in, rotation fine grid machine water outlet connects with equalizing tank water-in, equalizing tank water outlet connects with one-level decalcification reaction tank water-in, one-level decalcification reaction tank water outlet connects with secondary decalcification reaction tank water-in, secondary decalcification reaction tank water outlet connects with preliminary sedimentation tank water-in, preliminary sedimentation tank water outlet connects with the import of filtration unit, the outlet of filtration unit connects with coagulation basin water-in, coagulation basin water outlet connects with air flotation pool water-in, air flotation pool water outlet connects with UASB anaerobic pond water-in, UASB anaerobic pond water outlet connects with electrolysis machine a water-in, electrolysis machine a water outlet connects with anoxic pond water-in, anoxic pond water outlet connects with Aerobic Pond water-in, Aerobic Pond water outlet connects with second pond water-in, second pond water outlet connects with electrolysis machine b water-in, electrolysis machine b water outlet connects with water-in or the BAF water-in of membrane treatment appts, the water outlet of membrane treatment appts or effluent of aeration biological filter mouth connect with electrolysis machine c water-in, electrolysis machine c water outlet connects with desalting plant water-in through working shaft, the water-dialyzing outlet of desalting plant connects the import of reuse water basin, the condensed water of desalting plant exports a road and flow to equalizing tank through back of pipeline, another road connects with discharge channel, the water-in of accident pool connects with the outlet of tobacco sheet factory effluent, and accident pool water outlet connects with mechanical coarse rack water collecting basin water-in, UASB anaerobic pond pneumatic outlet connects with gas collector import, and gas collector outlet connects with secondary decalcification reaction tank water-in, and the pneumatic outlet of secondary decalcification reaction tank connects with biogas storage tank import, throw out in preliminary sedimentation tank, UASB anaerobic pond, anoxic pond, Aerobic Pond, second pond, membrane treatment appts/BAF and the outlet of the scum silica frost of air flotation pool all connect with sludge sump import, and sludge sump outlet connects with sludge dehydration device import,
Described filtration unit is the one of centrifugal filter, vacuum filter or pressure filter; Described membrane treatment appts is the one of MBR device or ultra-filtration equipment; Described desalting plant is the one of reverse osmosis system, nanofiltration system, electrodialysis or capacitive adsorption deionizing system.
2. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, is characterized in that: described coagulation basin is with dispensing system and medicine system.
3. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, is characterized in that: described electrolysis machine a, electrolysis machine b and electrolysis machine c are equipped with power supply and electrolyzer; 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 1 and recycling utilization device, is characterized in that: the membrane module of described MBR device 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.
5. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, it is characterized in that: 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.
6. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, it is characterized in that: the reverse osmosis membrane assembly in described reverse osmosis system 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.
7. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, it is characterized in that: the nanofiltration membrane component in described nanofiltration system 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.
8. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, is characterized in that: the working conditions of described electrodialysis system is operating voltage pressure 0.5～3.0 kg/cm
2, operating voltage 50～250V, strength of current 1～3A.
9. the processing of tobacco sheet factory effluent as claimed in claim 1 and recycling utilization device, is characterized in that: 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.
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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 |
| CN103524002B (en) * | 2013-10-28 | 2015-08-26 | 波鹰(厦门)科技有限公司 | A kind of high fatty foods processing waste water treatment unit |
| CN103549641B (en) * | 2013-11-14 | 2016-01-06 | 红塔烟草(集团)有限责任公司 | The purifying treatment method that stalk water circulation uses is washed in a kind of papermaking-method reconstituted tobaccos production process |
| CN106007272A (en) * | 2016-08-11 | 2016-10-12 | 桂琪 | Biochemical treatment method and apparatus for high calcium and high magnesium waste water |
| CN107581963A (en) * | 2017-10-24 | 2018-01-16 | 焦宁磊 | A kind of fecaluria processing system, method and asexuality lavatory |
| CN111196648B (en) * | 2020-01-19 | 2022-08-12 | 湖南中金岭南康盟环保科技有限公司 | Treatment method of calcium-containing wastewater |
| CN111807613A (en) * | 2020-06-28 | 2020-10-23 | 四川盛玖源环境工程有限公司 | Tobacco plant slice wastewater treatment process |
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| JP2002355692A (en) * | 2001-05-29 | 2002-12-10 | Natl Inst For Environmental Studies | Method for removing 2,2-bis(4-hydroxyphenyl) propane |
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| CN101007693A (en) * | 2007-01-12 | 2007-08-01 | 华南理工大学 | Method for anerobic aerobic granular sludge treating high concentration waste water from paper-making method tobacco slice production |
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