WO2014190876A1

WO2014190876A1 - Device and method for processing waste water from production of tobacco sheet

Info

Publication number: WO2014190876A1
Application number: PCT/CN2014/078262
Authority: WO
Inventors: 张世文
Original assignee: 波鹰(厦门)科技有限公司
Priority date: 2013-05-31
Filing date: 2014-05-23
Publication date: 2014-12-04

Abstract

A device for processing waste water from the production of a tobacco sheet, comprising a mechanical coarse-material grating collection tank, a rotary grating machine, a flotation tank, a first stage decalcification reaction tank, a second stage decalcification reaction tank, a coagulation tank, a primary settling tank, a regulation tank, a hydrolytic acidification tank, a UASB anaerobic tank, an electrolytic machine a, an anoxic tank, an aerobic tank, a middle settling tank, an electrolysis machine b, an MBR system, an electrolytic disinfection tank, a sludge tank, a sludge dehydration device, an accident tank, a gas collection device and a methane gas tank. A method for processing waste water from the production of a tobacco sheet, comprising the following steps: waste water from the production of a tobacco sheet→deslagging→chemically decalcifying→anaerobic treatment→electrolysis→A/O processing→secondary electrolysis→MBR→electrolyic disinfection→emission which meets standards. On the basis of the combination of a chemical decalcification technology, a biochemical technology, an electrochemical technology and an MBR technology, the present invention effectively treats the waste water from the production of a tobacco sheet, is low in cost and high in efficiency, and leads to a waste water emission which meets standards.

Description

Processing device and method for tobacco sheet production wastewater

Technical field

The present invention relates to a tobacco sheet production wastewater treatment device and method, and particularly to a tobacco flake production wastewater and tobacco production wastewater treatment device and method based on chemical decalcification technology, biochemical technology, electrochemical technology and MBR technology It belongs to the field of water pollution control in environmental engineering.

Background technique

When the tobacco leaves are produced, the raw materials cannot be fully utilized. During the production process of tobacco from the initial processing to the manufacture of cigarettes, the raw materials will produce about 1/3 of the total amount of the original tobacco materials. These tobacco scraps cannot be directly used as raw materials. The raw materials are again made into cigarette products. In order to reduce waste generation and realize the comprehensive utilization of scrap materials, tobacco sheet technology came into being. Tobacco flakes, also known as Reconstituted Tobacco, are made from flakes, stems, shredded tobacco and other tobacco materials as flakes or filaments. They are used as cigarette fillers to reduce tar content in cigarettes. To reduce the health hazards caused by smoking. The use of tobacco sheets has many advantages such as improving the quality of cut tobacco, reducing the cost of cigarettes, saving raw material consumption, and recycling resources. The roll pressing method, the thick pulp method and the paper making method are the main production methods of current tobacco sheets. Compared with the rolling method and the thick-slurry sheet, the paper-making sheet has obvious advantages: reducing the production cost of the cigarette, stabilizing the product quality, high filling value and yarn forming rate, good mechanical processing resistance, and improving the burning speed of the cigarette. It reduces the release of tar, has high plasticity and is easy to process, and is an effective process for producing 'healthy' cigarettes. It is precisely because papermaking sheets have the advantages that the rolling method and the thick slurry method cannot match, so they have been widely promoted at home and abroad.

The waste water produced in the production process of papermaking tobacco sheet has the commonality of papermaking wastewater, such as containing a large amount of fiber, and at the same time, the tobacco has high chroma and biodegradability, and the nicotine and calcium and magnesium content in the wastewater are unfavorable to the growth of microorganisms. The characteristics of high 150 ~ 500mg / L, the main pollution indicators are as follows:

序号Serial number	项目project	指标index
11	五日生化需氧量（BOD₅）Five-day biochemical oxygen demand (BOD ₅ )	600~10000mg/L600~10000mg/L
22	化学需氧量（COD_cr）Chemical oxygen demand (COD _cr )	1500~25000mg/L1500~25000mg/L
33	悬浮物（SS）Suspended matter (SS)	700~15000mg/L700~15000mg/L
44	pHpH	5.5~6.55.5~6.5
55	色度/倍Chroma/time	10000~2500010000~25000
66	水温Water temperature	45~65℃45~65°C
77	Ca²⁺ Ca ²⁺	200~500mg/L200~500mg/L

At the same time, the concentration of wastewater is fluctuating greatly, COD _{cr is} from 1500 to 25000 mg/L, SS is from 1000 to 15000 mg/L, nicotine and tar inhibit microbial growth, and high calcium and magnesium content can cause reactor fouling to fail to operate normally. Organic waste water.

Chinese patent CN1683261A discloses a method for treating wastewater from papermaking tobacco sheet production, that is, a method for treating coagulation air flotation + aerobic oxidation + mechanical filtration of tobacco sheet production wastewater.

Chinese patent CN102276093A discloses a method for treating wastewater from papermaking tobacco sheet production, the process comprising the steps of: passing the production wastewater through a coarse filter of a grid to flow into a wastewater regulating tank; and lifting the wastewater in the wastewater regulating tank to a mixed state by a lifting pump The Ca-diatomite complex coagulant is added to the condenser for 5-10 minutes, and then the ferric sulfate and polyacrylamide separating agent are added to the static reaction tank for reaction time of 50-60 min; the low concentration of organic wastewater is The pH is adjusted to be acidic and pumped into the ultrasonic micro-electrolysis reactor. The ultrasonic reaction and micro-electrolysis are combined to rapidly dissolve the chemical oxygen demand in the wastewater, and the reaction time is 30-60 min. The wastewater is then adsorbed by activated carbon and quartz. Sand filtration; the sludge produced in the conditioning tank and the static reaction tank section is used as a solid fuel after being dewatered by the snail sludge.

Chinese patent CN10133045A discloses that the papermaking tobacco sheet production wastewater is filtered back to the pulping section after one to three stages of filtration, and the recycled water is periodically discharged to the sewage treatment station, but the production wastewater is recycled back to the production. The effect of sheet quality.

Chinese patent CN1683261A discloses a method for removing waste water from a paper-making tobacco sheet production process by coagulation treatment, air floatation, and then feeding it to an aeration tank to remove most of the COD substance by aerobic microorganisms.

The above methods have certain effects on the treatment of tobacco sheet production wastewater, but there are defects such as long process flow, large equipment investment, large floor space, high operating cost, and more serious, because the wastewater contains a large amount of calcium, which directly leads to biochemistry. The treatment system and the membrane separation system have a large amount of scale, and the system cannot operate normally. The discharged wastewater after the treatment of the existing wastewater treatment technology cannot meet the discharge standard.

technical problem

The object of the present invention is to provide a long process flow, a large investment, a large floor space, a high operating cost, and a biochemical treatment system and a membrane treatment system that cannot be operated normally due to scaling in the existing tobacco production wastewater treatment method. After the treatment, the discharged wastewater does not meet the standards and defects, and provides a treatment based on chemical decalcification technology, biochemical technology, electrochemical technology and MBR technology, which has lower cost and higher efficiency, and makes it meet the standard discharge of tobacco production wastewater. Apparatus and method.

Technical solution

A processing device for producing tobacco sheet waste water, comprising mechanical coarse grid collecting basin, rotating grid machine, air floating pool, primary decalcification reaction tank, secondary decalcification reaction tank, coagulation tank, primary sedimentation tank, and adjustment tank , hydrolysis acidification tank, UASB anaerobic tank, electrolysis machine a, anoxic tank, aerobic tank, intermediate sedimentation tank, electrolysis machine b, MBR system, electrolytic disinfection tank, sludge tank, sludge dewatering device, accident pool, gas a collecting device and a biogas storage tank;

The inlet of the mechanical coarse grid collecting pool is connected with the outlet of the tobacco waste water, the water outlet of the mechanical coarse grid collecting pool is connected with the water inlet of the rotating grille machine, and the water outlet of the rotating grille machine is connected with the water inlet of the air floating pool, and the air floating pool is out. The nozzle is connected with the inlet of the first-stage decalcification reaction tank, the outlet of the primary decalcification reaction tank is connected with the inlet of the secondary decalcification reaction tank, and the outlet of the secondary decalcification reaction tank is connected with the inlet of the concrete pool, and the concrete pool is connected. The water outlet is connected with the inlet of the primary settling tank, the outlet of the primary settling tank is connected with the inlet of the regulating tank, the outlet of the regulating tank is connected with the inlet of the hydrolysis acidification tank, and the outlet of the hydrolysis acidification tank is connected with the inlet of the UASB anaerobic tank, UASB is boring The oxygen pool outlet is connected with the inlet of the electrolysis machine a, the outlet of the electrolysis machine a is connected with the inlet of the anoxic tank, the outlet of the anoxic tank is connected with the inlet of the aerobic tank, and the outlet of the aerobic tank is connected with the inlet of the sinking tank. The outlet of the intermediate sinking tank is connected with the inlet of the electrolysis machine b, the outlet of the electrolysis machine b is connected with the inlet of the MBR system, the outlet of the MBR system is connected with the inlet of the electrolytic disinfection tank, and the outlet of the electrolytic disinfection tank is connected with the drain; the accident pool The water inlet is connected with the outlet of the tobacco sheet production wastewater, and the accident pool outlet is connected with the mechanical coarse grid collecting water inlet; the UASB anaerobic gas outlet is connected with the gas collecting device inlet, the gas collecting device outlet and the secondary decalcification reaction tank The water inlet is connected, the gas outlet of the secondary decalcification reaction tank is connected with the inlet of the biogas storage tank; the sediment in the primary sedimentation tank, the UASB anaerobic tank, the anoxic tank, the aerobic tank, the intermediate sedimentation tank and the MBR system (ie The sludge) outlets are all connected to the sludge tank inlet, and the sludge tank outlet is connected to the sludge dewatering device inlet.

The air floating pool is a kind of air flotation method, electric float method, biological and chemical air floatation method or dissolved air flotation method.

The coagulation tank is provided with a dispensing system and a dosing system.

The electrolysis machine a and the electrolysis machine b are respectively provided with a power source and an electrolytic cell; the electrode materials in the electrolysis cell are graphite, titanium, iron, aluminum, zinc, copper, lead, nickel, molybdenum, chromium, alloy and nanocatalysis. One of the inert materials.

The surface layer of the nano catalytic inert electrode is coated with a metal oxide inert catalytic coating having a crystal grain of 10 to 35 nm, and the substrate of the nano catalytic inert electrode is a titanium plate or a plastic plate.

The membrane module of the MBR system is selected from the group consisting of a polyvinylidene fluoride hollow fiber membrane, a polypropylene hollow fiber membrane, a polysulfone hollow fiber membrane, a polyethersulfone hollow fiber membrane, a polyacrylonitrile hollow fiber membrane, and a polyvinyl chloride hollow fiber membrane. One kind.

The membrane module of the MBR system has a membrane pore size of 0.10 to 0.2 μm, a working pressure of -1 to -50 kPa, and an operating temperature of 5 to 45 °C.

The method for treating tobacco sheet production wastewater according to the present invention comprises the following steps:

(1) Deslagging

The tobacco flake production waste water is collected by pipelines and discharged into a mechanical coarse grid collecting tank. A coarse grille is arranged in the tank to isolate and remove the coarse floating floats in the sewage to prevent the subsequent processing equipment from being clogged, and then the tobacco is lifted by the lifting pump. The flake production waste water is lifted into the rotary mechanical grating machine, and most of the insoluble suspended solids in the water are further removed by the filtration of the filter screen, and the generated slag is packaged and transported, and the waste water is floated through the air floating pool for the air flotation. Separation of large particle fibers and other suspended materials greatly reduces the processing load of subsequent processes.

(2) Chemical decalcification

The effluent from the floatation tank flows into the first-stage decalcification reaction tank through the pipeline. After the stirring device, the appropriate amount of lime saturated solution is added to adjust the pH value to 8.5-9.5, and the pseudo-hardness (bicarbonate) is removed. In the decalcification reaction tank, the gas generated in the UASB anaerobic tank in the anaerobic treatment is introduced into the step (3), and the CO ₂ and the calcium and magnesium ions in the gas are reacted to form a carbonate precipitate, or 100 to 400 mg/L of Na ₂ CO is added. _{3. The} carbonate is reacted with calcium and magnesium ions to form a carbonate precipitate. After the effluent flows into the coagulation tank, 5~10 mg/L of FeSO _{4 is} added under stirring conditions, and then the pH value is adjusted to 8-9 by adding Na ₂ CO _{3 .} Finally, 2~3mg/L of polyphenylene amide (PAM) is added. After the reaction is completed, it enters the primary sedimentation tank for precipitation separation, thereby removing calcium and magnesium ions from the tobacco treatment wastewater, and the removal rate is 50-90%, reducing water. The hardness is such that Ca ^{2+ is} lower than 50mg/L, which prevents the subsequent equipment and facilities from being excessively Ca ²⁺ scaled; the sediment in the primary sedimentation tank (ie sludge) is sent to the sludge tank through the pump and pipeline. Finally, the filter is separated in the sludge dewatering device, and the calcium carbonate is recovered, and the water in the primary sedimentation tank is adjusted. Pool.

(3) Anaerobic treatment

The effluent from the regulating tank is lifted to the hydrolysis acidification tank by the lift pump, and stays in the hydrolysis acidification tank for a certain period of time. The acid-producing bacteria are used to hydrolyze and acidify the macromolecular organic matter in the wastewater into small molecular organic acid under the action of acid-producing bacteria, and then pass through the lift pump. Entering the UASB anaerobic tank, the organic acid is decomposed into methane and carbon dioxide through the adsorption, fermentation and methanogenesis of the anaerobic and facultative bacteria in the UASB anaerobic tank, and the B/C value of the wastewater is increased by anaerobic treatment. Improve the biodegradability of the wastewater; the methane and carbon dioxide produced are collected by the gas collection device and then introduced into the secondary decalcification reaction tank in the chemical decalcification step (2) to remove carbon dioxide, hydrogen sulfide, thiol compound impurities in the biogas, and purify After the biogas is recovered in the gas storage tank; the wastewater enters step (4).

(4) Electrolysis

The UASB anaerobic tank effluent enters the electrolysis machine a for electrolysis to remove the chromaticity and odor, and at the same time, the hard-to-biochemical macromolecular compound in the wastewater is opened and broken, becomes a biochemical small molecule, and further increases the B/C value. The conditions for subsequent biochemical treatment are improved; the voltage between adjacent electrodes of the electrolysis machine is 2 to 12 V, and the current density is 10 to 320 mA/cm ² .

(5) A/O processing

The electrolyzed effluent enters the anoxic tank, the aerobic tank and the intermediate settling tank in turn, and part of the sludge in the intermediate settling tank is returned to the anoxic tank through the reflux pump, and the nitrogen and phosphorus removal can be carried out by the alternating action of anoxic and aerobic microorganisms. And further oxidize and decompose the organic matter in the wastewater by aerobic treatment to deeply remove COD and BOD; the aerobic pool is uniformly filled with a large amount of biological suspended filler, providing a habitat for aerobic microorganisms to grow and reproduce, so that microorganisms form on the surface of the filler. Biofilm. An aerated oxygenation and agitation system is arranged at the bottom of the aerobic tank to oxygenate the sewage to maintain the dissolved oxygen in the water at 2 to 4 mg/L, and at the same time, the gas is used to increase the suspended matter and water in the pool. Contact, in addition to the agitation of gas and water backwashing, can effectively scouring the aged biofilm grown on the surface of the filler, promoting the replacement of the biofilm, so that the biofilm maintains high activity.

(6) Secondary electrolysis

The effluent from the sinking tank enters the electrolysis machine b again for electrolysis, so that the hard-to-biochemical macromolecular organic matter in the wastewater undergoes the open-loop chain scission through electrolysis, and is converted into a small-molecule organic matter that is easy to biochemical, and improves B/C; adjacent two electrodes during electrolysis The voltage between them is 2 to 6 V, and the current density is 20 to 200 mA/cm ² .

(7) MBR processing

The secondary electrolysis effluent enters the MBR system, biochemical and membrane separation of the wastewater, degradation of residual organic pollutants and removal of suspended solids.

(8) Disinfection

After the wastewater is treated by MBR, the effluent is treated by the electrolytic disinfection tank to further remove the color, and the wastewater is sterilized and disinfected, and finally discharged to the standard.

(9) Sludge treatment

Step (3) UASB anaerobic treatment in anaerobic treatment, step (5) A/O treatment, anoxic tank, aerobic tank and intermediate settling tank, and step (7) sludge produced by MBR treatment enter the sludge through the pipeline The pool is then dewatered by the sludge filter press to reduce the volume of the sludge. After dewatering, the mud cake is incinerated, and the filtrate is returned to the conditioning tank in step (2) chemical decalcification.

Step (1) The air flotation in the slag removal is a kind of air flotation method, electric float method, biological and chemical air float method, and dissolved air flotation method.

Step (2) The second step of chemical decalcification is to transfer the biogas generated by the UASB anaerobic tank (containing methane, carbon dioxide, hydrogen sulfide, mercaptan, ammonia, etc.) to the secondary decalcification tank to make CO in the gas. _{2 While} reacting with calcium and magnesium ions to form carbonate precipitates, hydrogen sulfide, thiol compounds, ammonia gas, etc. in the biogas react with calcium and magnesium ions to purify the biogas, and the purified biogas can be collected in the gas tank. Further use.

The electrolysis machine of step (4) and step (6) is provided with a power source and an electrolysis cell; the electrode material in the electrolysis cell is graphite, titanium, iron, aluminum, zinc, copper, lead, nickel, molybdenum, chromium, alloy And one of the nano catalytic inert materials; the surface layer of the nano catalytic inert electrode is coated with a metal oxide inert catalytic coating having a crystal grain of 10 to 35 nm, and the substrate of the nano catalytic inert electrode is a titanium plate or a plastic plate .

Step (7) The membrane component of the MBR system in the MBR treatment is selected from the group consisting of a polyvinylidene fluoride hollow fiber membrane, a polypropylene hollow fiber membrane, a polysulfone hollow fiber membrane, a polyethersulfone hollow fiber membrane, and a polyacrylonitrile.

One of a hollow fiber membrane and a polyvinyl chloride hollow fiber membrane;

Beneficial effect

Compared with the prior art, the present invention has the following outstanding advantages:

(1) After removing the pseudo hardness (bicarbonate) by the primary decalcification reaction of the chemical decalcification system, the carbonate is precipitated by reacting the carbonate with the calcium and magnesium ions through a secondary decalcification reaction tank, and then The carbonate precipitate in the coagulation tank is destabilized, coagulates with the coagulant such as FeSO ₄ and polyphenylene amide (PAM), aggregates into coarse squid granules, settles in the primary sedimentation tank, and finally effectively removes the tobacco. High-concentration calcium and magnesium ions in flake production wastewater, the removal rate is 50-90%, reducing the hardness of water, making Ca ²⁺ less than 50mg/L, preventing equipment fouling, ensuring smooth and stable subsequent biochemical treatment and electrolysis process run.

(2) After treatment by the UASB anaerobic treatment system, the COD and BOD in the wastewater are greatly reduced, and the generated gas is collected by the gas collection device and then introduced into the secondary decalcification reaction tank in the chemical decalcification to make the CO in the gas. ₂ reacting with calcium and magnesium ions to form carbonate precipitates, on the one hand, recovering CO ₂ in the gas, so that the gas can be effectively utilized; on the other hand, the H ₂ S in the gas is removed through the secondary decalcification reaction tank, the gas is purified, and the biogas is passed through The gas tank is collected or used at high altitude.

(3) After the slag removal and chemical decalcification system treatment, the SS removal rate in the wastewater is over 95%, the SS in the adjustment tank is greatly reduced, the deposition of sludge in the adjustment tank is avoided, and the daily mud running workload is reduced.

(4) The strong oxidizing free radical generated by nano-catalytic electrolysis causes the hard-to-biochemical macromolecular compound in the wastewater to be opened and broken, becomes a biochemical small molecule, further increases the B/C value, and improves the conditions of subsequent biochemical treatment. And remove the chromaticity and odor in the wastewater, and reduce indicators such as ammonia nitrogen and COD.

(5) After the A/O biochemical pool, the sewage can be denitrified and dephosphorized by the alternating action of anaerobic and aerobic.

(6) After being treated by the MBR system, the oxidative decomposition of microorganisms will further decompose the pollutants in the water, and at the same time, the effective interception effect of the membrane will be used to effectively remove the indexes such as SS, chromaticity and pollutants, and the effluent water quality is stable and reaches the standard discharge. .

DRAWINGS

1 is a schematic view showing the structure of an embodiment of a treatment apparatus for producing tobacco sheet waste water according to the present invention.

Figure 1 is a process flow diagram of the present invention.

BEST MODE FOR CARRYING OUT THE INVENTION

Referring to Fig. 1, a processing device for producing tobacco sheet waste water comprises: a mechanical coarse grid collecting tank 1, a rotating grid machine 2, an air floating pool 3, a primary decalcification reaction tank 4, and a secondary decalcification reaction tank 5 , coagulation tank 6, primary sedimentation tank 7, conditioning tank 8, hydrolysis acidification tank 9, UASB anaerobic tank 10, electrolysis machine a11, anoxic tank 12, aerobic tank 13, intermediate sedimentation tank 14, electrolysis machine b15, MBR System 16, electrolytic disinfection tank 17, drain channel 18, accident tank 19, sludge tank 20, sludge filter press 21, lift pump 22, lift pump 23, lift pump 24, lift pump 25, pump 26, gas collection device 27 and biogas storage tank 28. The inlet of the mechanical coarse grid collecting tank 1 is connected with the outlet of the tobacco sheet production wastewater, and the mechanical coarse grid collecting pool 1 outlet is connected with the water inlet of the rotary grill machine 2 by the lift pump 20, and the water outlet and the gas of the rotary grill machine 2 are rotated. The inlet of the floating pool 3 is connected, the outlet of the floating tank 3 is connected with the inlet of the first decalcification reaction tank 4, the outlet of the first decalcification reaction tank 4 is connected with the inlet of the secondary decalcification reaction tank 5, and the secondary decalcification reaction tank 5 The water outlet is connected with the water inlet of the coagulation tank 6, the water outlet of the concrete pool 6 is connected with the water inlet of the primary sedimentation tank 7, the water outlet of the primary sedimentation tank 7 is connected with the water inlet of the adjustment tank 8, and the water outlet of the adjustment tank 8 is passed through the lift pump 23 It is connected with the water inlet of the hydrolysis acidification tank 9, and the water outlet of the hydrolysis acidification tank 9 is connected with the water inlet of the UASB anaerobic tank 10 through the lift pump 24, and the water outlet of the UASB anaerobic tank 10 is connected with the water inlet of the electrolysis machine a11, and the water outlet of the electrolysis machine a11 is The anoxic tank 12 is connected with the water inlet, the outlet of the anoxic tank 12 is connected with the inlet of the aerobic tank 13, the outlet of the aerobic tank 13 is connected with the inlet of the intermediate settling tank 14, the outlet of the intermediate settling tank 14 and the inlet of the electrolysis machine b15 Connection, the water outlet of the electrolysis machine b15 is connected with the water inlet of the MBR system 16, and the water of the MBR system 16 is discharged. The mouth is connected to the water inlet of the electrolytic disinfection tank 17 through the lift pump 25, and the water outlet of the electrolytic disinfection tank 17 is connected with the drain 18, and the primary settling tank 7, the UASB anaerobic tank 9, the anoxic tank 12, the aerobic tank 13, and the sinking The sludge outlets of the pool 14 and the MBR system 16 are connected to the inlet of the sludge tank 20, and the outlet of the sludge tank 20 is connected to the inlet of the sludge filter press 21, and the water inlet of the accident pool 19 is connected with the outlet of the tobacco sheet production wastewater, the accident pool The water outlet of the 19 is connected to the inlet of the mechanical coarse grid collecting tank 1 by the pump 26; the gas outlet of the UASB anaerobic tank 10 is connected with the inlet of the gas collecting device 27, and the outlet of the gas collecting device 27 is connected with the inlet of the secondary decalcification reaction tank 5; The gas outlet of the secondary decalcification reaction tank 5 is connected with the inlet of the biogas storage tank 28; the primary settling tank 7, the UASB anaerobic tank 10, the anoxic tank 12, the aerobic tank 13, the intermediate settling tank 14 and the MBR system 16 The outlet of the sediment (i.e., sludge) is connected to the inlet of the sludge tank 20, and the outlet of the sludge tank 20 is connected to the inlet of the sludge dewatering device 21.

As can be seen from Fig. 1, the slag generated by the mechanical coarse grid collecting tank 1 and the rotary grill machine 2 is shipped out by packing.

The invention relates to the design of a waste water treatment device for tobacco sheet production after an in-depth systematic comparative study on the composition, properties and existing treatment schemes of the existing tobacco sheet production wastewater, which is through chemical decalcification, biochemistry, electrolysis, MBR. A combination of methods, etc., to form a treatment device that is particularly suitable for the production of wastewater from tobacco sheets.

Embodiments of the invention

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, embodiments of the present invention will be described with reference to FIG.

Example 1

Treatment method for 2000 tons/day tobacco sheet production wastewater.

The tobacco sheet production wastewater quality index is determined as shown in Table 1.

Table 1 Water quality indicators of tobacco sheet production wastewater

序号Serial number	项目project	单位unit	测定值measured value	序号Serial number	项目project	单位unit	测定值measured value
11	BOD₅ BOD ₅	mg/LMg/L	58005800	55	色度Chroma	倍Times	1500015000
22	COD_Cr COD _Cr	mg/LMg/L	2500025000	66	Ca²⁺ Ca ²⁺	mg/LMg/L	200200
33	SSSS	mg/LMg/L	1500015000	77	水温Water temperature	℃°C	5050
44	pH值pH value		6.26.2

(1) Deslagging

The tobacco sheet production waste water is collected into the mechanical coarse grid collecting tank 1 after being collected by the pipeline, and a coarse grid is arranged in the tank to isolate and remove the coarse floating floats in the sewage to prevent the subsequent processing equipment from being clogged, and then pass the lift pump 22, The waste water of the tobacco sheet production is raised into the rotary grill machine 2, and most of the insoluble suspended matter in the water is further removed by the filtration of the filter screen, and the generated slag is packed and transported, and the waste water passes through the air floating tank 3, in the waste water. Separation of large particle fibers and other suspended materials greatly reduces the processing load of subsequent processes.

(2) Chemical decalcification

The effluent of the air floatation tank 3 flows into the first-stage decalcification reaction tank 4 through the pipeline, and the pH is increased to 8.5 by adding a proper amount of lime saturated clarification solution under stirring by the dosing device, and the pseudo-hardness (bicarbonate) is removed, and then flows into the second stage. The decalcification reaction tank 5 is introduced into the gas generated by the UASB anaerobic tank 10 in the anaerobic treatment in the step (3), so that the CO _{2 in} the gas reacts with the calcium and magnesium ions to form a carbonate precipitate, and the effluent flows into the coagulation tank after stirring. Add 6mg/L FeSO _{4 first} , then add Na ₂ CO _{3 to} adjust the pH to 8 and finally add 2mg/L polyphenylene amide (PAM). After the reaction is completed, enter the primary sedimentation tank 7 for precipitation separation. In addition to the calcium and magnesium ions in the tobacco treatment wastewater, the removal rate is up to 75%, and the water hardness is reduced, so that the Ca ²⁺ concentration is 50 mg/L, preventing the excessive equipment and facilities from being excessively Ca ²⁺ scaled; the primary sedimentation tank 7 The precipitate (i.e., sludge) is sent to the sludge tank 20 through a pump and a pipe, and finally filtered and separated in the sludge filter press 21, and calcium carbonate is recovered, and the water from the primary settling tank 7 enters the conditioning tank 8.

(3) Anaerobic treatment

The effluent of the adjustment tank 8 is lifted to the hydrolysis acidification tank 9 by the lift pump 23, and stays in the hydrolysis acidification tank 9 for a certain period of time, and the acid-producing bacteria are used to hydrolyze and acidify the macromolecular organic matter in the wastewater to the small molecule organic acid under the action of the acid-producing bacteria. Then, the UASB anaerobic tank 10 is introduced through the lift pump 24, and the organic acid is decomposed into methane and carbon dioxide through the adsorption, fermentation and methanogenesis of the anaerobic bacteria and facultative bacteria in the UASB anaerobic tank 10, and is improved by anaerobic treatment. The B/C value of the wastewater improves the biodegradability of the wastewater; the generated methane and carbon dioxide are collected by the gas collection device 27 and then introduced into the secondary decalcification reaction tank 5 in the chemical decalcification step to remove carbon dioxide from the biogas. Hydrogen sulfide, thiol compound impurities, after purification, the biogas is recovered in the biogas storage tank 28; the wastewater proceeds to step (4).

(4) Electrolysis

The UASB anaerobic tank 10 effluent enters the electrolysis machine a11 for electrolysis to remove the chromaticity and odor, and at the same time, the difficult biochemical macromolecular compound in the wastewater is opened and broken, and becomes a biochemical small molecule, further improving the B/C value. To improve the conditions of the subsequent biochemical treatment; the voltage between the adjacent electrodes of the electrolysis machine a11 is 3V, and the current density is 300 mA/cm ² .

(5) A/O processing

The electrolyzed effluent sequentially enters the anoxic tank 12, the aerobic tank 13 and the intermediate settling tank 14, and part of the sludge in the intermediate settling tank 14 is returned to the anoxic tank 12 through the reflux pump, and can be replaced by anoxic and aerobic microorganisms. Denitrification and dephosphorization, and further oxidative decomposition of organic matter in wastewater by aerobic treatment, deep removal of COD and BOD; aerobic pool 13 is evenly filled with a large amount of biological suspension filler, providing a habitat for aerobic microorganisms, breeding and breeding So that microorganisms form a biofilm on the surface of the filler. An aeration and oxygenation agitation system is arranged at the bottom of the aerobic tank 13 to oxygenate the sewage to maintain the dissolved oxygen in the water at 2 to 4 mg/L, and at the same time, the action of the gas rises to make the suspended matter and the water in the pool more Fully contact, and the agitation action of gas and water backwashing can effectively wash the aged biofilm grown on the surface of the filler, promote the replacement of the biofilm, and maintain the biofilm with high activity.

(6) Secondary electrolysis

The effluent of the intermediate sinking tank 14 enters the electrolysis machine b15 again for electrolysis, so that the hard-to-biochemical macromolecular organic matter in the wastewater undergoes the open-loop chain-breaking action of electrolysis, and is converted into a small-molecule organic matter which is easy to biochemical, and improves B/C; The voltage between the electrodes was 6 V, and the current density was 20 mA/cm ² .

(7) MBR processing

The secondary electrolyzed effluent enters the MBR system 16, biochemical and membrane separation of the wastewater, degradation of residual organic pollutants and removal of suspended solids.

(8) Disinfection

After the wastewater is treated by the MBR, the effluent is lifted by the lift pump 25 to the electrolytic disinfection tank 17, and the chromaticity can be further removed, and the wastewater can be sterilized and disinfected, and finally discharged by the discharge channel 18.

(9) Sludge treatment

Step (3) Anaerobic treatment in the UASB anaerobic tank 10, step (5) A/O treatment in the anoxic tank 12, the aerobic tank 13 and the intermediate settling tank 14 and the sludge produced in the step (7) MBR treatment are passed The pipeline enters the sludge tank 20, and then the sludge is reduced by the dehydration of the sludge filter press 21. After dewatering, the mud cake is incinerated, and the filtrate is returned to the conditioning tank 8 in the step (2) chemical decalcification.

The effluent water quality indicators are determined as shown in Table 2.

Table 2 Water quality indicators of effluent

序号Serial number	项目project	单位unit	测定值measured value	序号Serial number	项目project	单位unit	测定值measured value
11	BOD₅ BOD ₅	mg/LMg/L	2020	55	色度Chroma	倍Times	2020
22	COD_Cr COD _Cr	mg/LMg/L	6060	66	Ca²⁺ Ca ²⁺	mg/LMg/L	4040
33	SSSS	mg/LMg/L	6060	77	水温Water temperature	℃°C	23twenty three
44	pH值pH value		6.86.8

Example 2

A treatment method for 5000 tons/day tobacco sheet production wastewater.

The tobacco sheet production wastewater quality index is determined as shown in Table 3.

Table 3 Water quality indicators of tobacco sheet production wastewater

序号Serial number	项目project	单位unit	测定值measured value	序号Serial number	项目project	单位unit	测定值measured value
11	BOD₅ BOD ₅	mg/LMg/L	20002000	55	色度Chroma	倍Times	2500025000
22	COD_Cr COD _Cr	mg/LMg/L	80008000	66	Ca²⁺ Ca ²⁺	mg/LMg/L	300300
33	SSSS	mg/LMg/L	62006200	77	水温Water temperature	℃°C	5555
44	pH值pH value		66

(1) Deslagging

(2) Chemical decalcification

The effluent of the air floatation tank 3 flows into the first-stage decalcification reaction tank 4 through the pipeline, and the pH is increased to 9.5 by adding a proper amount of lime saturated clarification solution under stirring by the dosing device, and the pseudo-hardness (bicarbonate) is removed, and then flows into the second stage. In the decalcification reaction tank 5, 400 mg/L of Na ₂ CO _{3 is added} to react the carbonate with the calcium and magnesium ions to form a carbonate precipitate, and the CO _{2 in} the gas reacts with the calcium and magnesium ions to form a carbonate precipitate, and the effluent flows into the coagulation. After the pool, 10 mg/L FeSO ₄ was added under stirring, then the pH value was adjusted to 8.5 by adding Na ₂ CO ₃ , and finally 2.5 mg/L polyphenylene amide (PAM) was added, and the reaction was completed and then entered the primary settling tank 7 Separation and sedimentation to remove calcium and magnesium ions from tobacco treatment wastewater, the removal rate is up to 84%, and the water hardness is reduced, so that the Ca ²⁺ concentration is 48 mg/L, preventing the subsequent equipment and facilities from being too high in Ca ²⁺ junction. The scale (the sludge) in the primary sedimentation tank 7 is sent to the sludge tank 20 through the pump and the pipeline, and finally filtered and separated in the sludge dewatering device, and the calcium carbonate is recovered, and the effluent of the primary sedimentation tank 7 enters. Adjust the pool 8.

(3) Anaerobic treatment

(4) Electrolysis

The UASB anaerobic tank 10 effluent enters the electrolysis machine a11 for electrolysis to remove the chromaticity and odor, and at the same time, the difficult biochemical macromolecular compound in the wastewater is opened and broken, and becomes a biochemical small molecule, further improving the B/C value. To improve the conditions of the subsequent biochemical treatment; the voltage between the adjacent electrodes of the electrolysis machine a11 is 8V, and the current density is 150 mA/cm ² .

(5) A/O processing

(6) Secondary electrolysis

The effluent of the intermediate sinking tank 14 enters the electrolysis machine b15 again for electrolysis, so that the hard-to-biochemical macromolecular organic matter in the wastewater undergoes the open-loop chain-breaking action of electrolysis, and is converted into a small-molecule organic matter which is easy to biochemical, and improves B/C; The voltage between the electrodes was 4 V, and the current density was 100 mA/cm ² .

(7) MBR processing

(8) Disinfection

(9) Sludge treatment

The effluent water quality indicators were determined as shown in Table 4.

Table 4 Water quality indicators of treated effluent

序号Serial number	项目project	单位unit	测定值measured value	序号Serial number	项目project	单位unit	测定值measured value
11	BOD₅ BOD ₅	mg/LMg/L	1515	55	色度Chroma	倍Times	2020
22	COD_Cr COD _Cr	mg/LMg/L	6060	66	Ca²⁺ Ca ²⁺	mg/LMg/L	3535
33	SSSS	mg/LMg/L	4040	77	水温Water temperature	℃°C	2525
44	pH值pH value		6.56.5

Example 3

Recycling and recycling method for 8,000 tons/day tobacco sheet production wastewater.

The tobacco sheet production wastewater quality index is determined as shown in Table 5.

Table 5 Water quality indicators of tobacco sheet production wastewater

序号Serial number	项目project	单位unit	测定值measured value	序号Serial number	项目project	单位unit	测定值measured value
11	BOD₅ BOD ₅	mg/LMg/L	600600	55	色度Chroma	倍Times	2000020000
22	COD_Cr COD _Cr	mg/LMg/L	20002000	66	Ca²⁺ Ca ²⁺	mg/LMg/L	400400
33	SSSS	mg/LMg/L	10001000	77	水温Water temperature	℃°C	5050
44	pH值pH value		6.56.5

(1) Deslagging

(2) Chemical decalcification

The effluent of the air floatation tank 3 flows into the first-stage decalcification reaction tank 4 through the pipeline, and the pH is increased to 9.0 by adding a proper amount of lime saturated clarification solution under stirring by the dosing device, and the pseudo-hardness (bicarbonate) is removed, and then flows into the second stage. Decalcification reaction tank 5, adding 100 mg/L of Na ₂ CO ₃ , reacting carbonate with calcium and magnesium ions to form carbonate precipitate, reacting CO ₂ with calcium and magnesium ions in the gas to form carbonate precipitate, and effluent flowing into coagulation After the pool, 5 mg/L of FeSO ₄ was added under stirring, then the pH was adjusted to 9.0 by adding Na ₂ CO ₃ , and finally 3 mg/L of polyphenylene amide (PAM) was added. After the reaction was completed, the reaction was completed and then entered into the primary settling tank 7 . Precipitation separation, thus removing calcium and magnesium ions in tobacco treatment wastewater, the removal rate is 87.5%, reducing the hardness of water, making the concentration of Ca ²⁺ 50mg / L, preventing excessive Ca ²⁺ scaling of subsequent equipment and facilities The sediment (ie sludge) in the primary settling tank 7 is sent to the sludge tank 20 through the pump and the pipeline, and finally filtered and separated in the sludge dewatering device, and the calcium carbonate is recovered, and the effluent of the primary settling tank 7 is adjusted. Pool 8.

(3) Anaerobic treatment

(4) Electrolysis

The UASB anaerobic tank 10 effluent enters the electrolysis machine a11 for electrolysis to remove the chromaticity and odor, and at the same time, the difficult biochemical macromolecular compound in the wastewater is opened and broken, and becomes a biochemical small molecule, further improving the B/C value. To improve the conditions of subsequent biochemical treatment; the voltage between the adjacent electrodes of the electrolysis machine a11 is 12V, and the current density is 50 mA/cm ² .

(5) A/O processing

(6) Secondary electrolysis

The effluent of the intermediate sinking tank 14 enters the electrolysis machine b15 again for electrolysis, so that the hard-to-biochemical macromolecular organic matter in the wastewater undergoes the open-loop chain-breaking action of electrolysis, and is converted into a small-molecule organic matter which is easy to biochemical, and improves B/C; The voltage between the electrodes was 2 V, and the current density was 200 mA/cm ² .

(7) MBR processing

(8) Disinfection

After the wastewater is treated by MBR, the effluent is lifted by the lift pump 25 to the electrolytic disinfection tank 17 to further remove the chromaticity, sterilize the wastewater, and finally discharge the standard.

(9) Sludge treatment

The effluent water quality indicators are determined as shown in Table 6.

Table 6 Water quality indicators of effluent

序号Serial number	项目project	单位unit	测定值measured value	序号Serial number	项目project	单位unit	测定值measured value
11	BOD₅ BOD ₅	mg/LMg/L	1515	55	色度Chroma	倍Times	2020
22	COD_Cr COD _Cr	mg/LMg/L	6060	66	Ca²⁺ Ca ²⁺	mg/LMg/L	4040
33	SSSS	mg/LMg/L	5050	77	水温Water temperature	℃°C	2525
44	pH值pH value		66

Industrial applicability

The invention can effectively remove the high concentration of calcium and magnesium ions in the waste water of the tobacco sheet production, the removal rate is 50-90%, the hardness of the water is lowered, the Ca ^{2+ is} lower than 50 mg/L, the scale of the equipment is prevented, and the subsequent biochemistry is ensured. The treatment and electrolysis process runs smoothly and stably, and has good industrial applicability.

Claims

The invention relates to a processing device for wastewater production of tobacco sheets, which comprises: a mechanical coarse grid collecting basin, a rotating grid machine, an air floating pool, a first-stage decalcification reaction tank, a secondary decalcification reaction tank, a concrete pool, and a primary sedimentation Pool, regulating tank, hydrolysis acidification tank, UASB anaerobic tank, electrolysis machine a, anoxic tank, aerobic tank, intermediate sedimentation tank, electrolysis machine b, MBR system, electrolytic disinfection tank, sludge tank, sludge dewatering device, Accident pool, gas collection device and biogas storage tank;

The inlet of the mechanical coarse grid collecting pool is connected with the outlet of the tobacco waste water, the water outlet of the mechanical coarse grid collecting pool is connected with the water inlet of the rotating grille machine, and the water outlet of the rotating grille machine is connected with the water inlet of the air floating pool, and the air floating pool is out. The nozzle is connected with the inlet of the first-stage decalcification reaction tank, the outlet of the primary decalcification reaction tank is connected with the inlet of the secondary decalcification reaction tank, and the outlet of the secondary decalcification reaction tank is connected with the inlet of the concrete pool, and the concrete pool is connected. The water outlet is connected with the inlet of the primary settling tank, the outlet of the primary settling tank is connected with the inlet of the regulating tank, the outlet of the regulating tank is connected with the inlet of the hydrolysis acidification tank, and the outlet of the hydrolysis acidification tank is connected with the inlet of the UASB anaerobic tank, UASB is boring The oxygen pool outlet is connected with the inlet of the electrolysis machine a, the outlet of the electrolysis machine a is connected with the inlet of the anoxic tank, the outlet of the anoxic tank is connected with the inlet of the aerobic tank, and the outlet of the aerobic tank is connected with the inlet of the sinking tank. The outlet of the intermediate sinking tank is connected with the inlet of the electrolysis machine b, the outlet of the electrolysis machine b is connected with the inlet of the MBR system, the outlet of the MBR system is connected with the inlet of the electrolytic disinfection tank, and the outlet of the electrolytic disinfection tank is connected with the drain; the accident pool The water inlet is connected with the outlet of the tobacco sheet production wastewater, and the accident pool outlet is connected with the mechanical coarse grid collecting water inlet; the UASB anaerobic gas outlet is connected with the gas collecting device inlet, the gas collecting device outlet and the secondary decalcification reaction tank The water inlet is connected, the gas outlet of the secondary decalcification reaction tank is connected with the inlet of the biogas storage tank; the sediment in the primary sedimentation tank, the UASB anaerobic tank, the anoxic tank, the aerobic tank, the intermediate sedimentation tank and the MBR system (ie The sludge) outlets are all connected to the sludge tank inlet, and the sludge tank outlet is connected to the sludge dewatering device inlet.
The apparatus for treating tobacco sheet production wastewater according to claim 1, wherein the air floating pool is one of air flotation, electrical floatation, biological and chemical air floatation or dissolved air floatation.
A tobacco sheet production wastewater treating apparatus according to claim 1, wherein said coagulation tank is provided with a dispensing system and a dosing system.
The apparatus for treating tobacco sheet production wastewater according to claim 1, wherein the electrolysis machine a and the electrolysis machine b are each provided with a power source and an electrolysis cell; and the electrode material in the electrolysis cell is graphite or titanium. One of iron, aluminum, zinc, copper, lead, nickel, molybdenum, chromium, alloys and nanocatalytic inert materials.
The apparatus for treating wastewater of tobacco sheet production according to claim 1 or 4, wherein the surface layer of the nano catalytic inert electrode is coated with a metal oxide inert catalytic coating having a crystal grain size of 10 to 35 nm. The substrate of the nano catalytic inert electrode is a titanium plate or a plastic plate.
The apparatus for treating tobacco sheet production wastewater according to claim 1, wherein the membrane module of the MBR system is selected from the group consisting of a polyvinylidene fluoride hollow fiber membrane, a polypropylene hollow fiber membrane, a polysulfone hollow fiber membrane, One of a polyethersulfone hollow fiber membrane, a polyacrylonitrile hollow fiber membrane, and a polyvinyl chloride hollow fiber membrane.
The apparatus for treating tobacco sheet production wastewater according to claim 1 or 6, wherein the membrane module of the MBR system has a membrane pore diameter of 0.10 to 0.2 μm, a working pressure of -1 to -50 kPa, and an operating temperature. It is 5 to 45 °C.
A method for treating wastewater from tobacco sheet production, comprising the steps of:

(1) Deslagging

The tobacco sheet production wastewater is collected in a pipeline and discharged into a mechanical coarse grid collecting tank. A coarse grid is arranged in the tank to isolate and remove the coarse floating floats in the sewage, and then the waste water of the tobacco sheet production is lifted to the rotating machine by the lifting pump. In the grid machine, most of the insoluble suspended solids in the water are further removed by filtration through the filter screen, and the generated slag is packed and transported, and the waste water is floated through the air floating pool to carry out large particle fiber and other suspended matter in the waste water. Separate

(2) Chemical decalcification

The effluent from the floatation tank flows into the first-stage decalcification reaction tank through the pipeline. After the stirring device, the appropriate amount of lime saturated solution is added to adjust the pH value to 8.5-9.5, and the pseudo-hardness (bicarbonate) is removed. In the decalcification reaction tank, the gas generated in the UASB anaerobic tank in the anaerobic treatment is introduced into the step (3), and the CO 2 and the calcium and magnesium ions in the gas are reacted to form a carbonate precipitate, or 100 to 400 mg/L of Na 2 CO is added. 3 The carbonate is reacted with calcium and magnesium ions to form a carbonate precipitate. After the effluent flows into the coagulation tank, 5-10 mg/L of FeSO 4 is added under stirring, and then the pH value is adjusted to 8-9 by adding Na 2 CO 3 . Finally, 2~3mg/L of polyphenylene amide (PAM) is added. After the reaction is completed, it enters the primary sedimentation tank for sedimentation. The sediment in the primary sedimentation tank (ie sludge) is sent to the sludge tank through the pump and pipeline. Finally, the filter is separated in the sludge dewatering device, and the calcium carbonate is recovered, and the effluent from the primary settling tank enters the regulating tank;

(3) Anaerobic treatment

The effluent from the regulating tank is lifted to the hydrolysis acidification tank by the lift pump, and stays in the hydrolysis acidification tank for a certain period of time. The acid-producing bacteria are used to hydrolyze and acidify the macromolecular organic matter in the wastewater into small molecular organic acid under the action of acid-producing bacteria, and then pass through the lift pump. Entering the UASB anaerobic tank, the organic acid is decomposed into methane and carbon dioxide through the adsorption, fermentation and methanogenesis of the anaerobic and facultative bacteria in the UASB anaerobic tank. The methane and carbon dioxide produced are collected by the gas collection device and then introduced. Step (2) the secondary decalcification reaction tank in the chemical decalcification, after the second decalcification reaction tank is purified, the biogas is recovered in the gas storage tank; the wastewater enters the step (4);

(4) Electrolysis

The UASB anaerobic tank effluent enters the electrolysis machine a for electrolysis. The voltage between the adjacent electrodes of the electrolysis machine a is 2 to 12 V, and the current density is 10 to 320 mA/cm 2 ;

(5) A/O processing

The electrolyzed effluent enters the anoxic tank, the aerobic tank and the intermediate settling tank in turn, and part of the sludge in the intermediate settling tank is returned to the anoxic tank through the reflux pump, and the nitrogen and phosphorus removal can be carried out by the alternating action of anoxic and aerobic microorganisms. And further oxidize and decompose the organic matter in the wastewater by aerobic treatment to deeply remove COD and BOD; the aerobic pool is uniformly filled with a large amount of biological suspended filler, providing a habitat for aerobic microorganisms to grow and reproduce, so that microorganisms form on the surface of the filler. The biofilm is provided with an aeration and oxygenation agitation system at the bottom of the aerobic tank to oxygenate the sewage, so that the dissolved oxygen in the water is maintained at 2 to 4 mg/L, and the suspended solids in the pool are utilized by the action of gas rising. The water is more fully contacted, and the agitation action of the backwashing of the gas and the water can effectively wash the aged biofilm grown on the surface of the filler, promote the replacement of the biofilm, and maintain the high activity of the biofilm;

(6) Secondary electrolysis

The effluent from the sinking tank enters the electrolysis machine b again for electrolysis. When the electrolysis machine b, the voltage between the adjacent electrodes is 2-6V, and the current density is 20-200 mA/cm 2 ;

(7) MBR processing

The secondary electrolysis effluent enters the MBR system, biochemical and membrane separation of the wastewater, degradation of residual organic pollutants and removal of suspended solids;

(8) Disinfection

After the wastewater is treated by MBR, the effluent is treated by an electrolytic disinfection tank to further remove the color, and the wastewater is sterilized and disinfected, and finally discharged to the standard;

(9) Sludge treatment

Step (3) UASB anaerobic treatment in anaerobic treatment, step (5) A/O treatment, anoxic tank, aerobic tank and intermediate settling tank, and step (7) sludge produced by MBR treatment enter the sludge through the pipeline The pool is then dewatered by the sludge filter press to reduce the volume of the sludge. After dewatering, the mud cake is incinerated, and the filtrate is returned to the conditioning tank in step (2) chemical decalcification.
The method for treating wastewater from tobacco sheet production according to claim 8, wherein in the step (1), the air flotation is a gas floatation method, an electrical float method, a biological and chemical air floatation method, A kind of dissolved air flotation method.
A method for treating tobacco sheet production wastewater according to claim 8, wherein the electrolysis machine of the step (4) and the step (6) is provided with a power source and an electrolytic cell; and the electrode material in the electrolytic cell is One of graphite, titanium, iron, aluminum, zinc, copper, lead, nickel, molybdenum, chromium, alloys, and nanocatalytic inert materials.
The method for treating wastewater from tobacco sheet production according to claim 8 or 10, wherein the surface layer of the nano catalytic inert electrode is coated with a metal oxide inert catalytic coating having a crystal grain size of 10 to 35 nm. The substrate of the nano catalytic inert electrode is a titanium plate or a plastic plate.
The method for treating wastewater from tobacco sheet production according to claim 8, wherein in the step (7), the membrane module of the MBR system is selected from the group consisting of a polyvinylidene fluoride hollow fiber membrane and a polypropylene hollow fiber membrane. One of a polysulfone hollow fiber membrane, a polyethersulfone hollow fiber membrane, a polyacrylonitrile hollow fiber membrane, and a polyvinyl chloride hollow fiber membrane.
The method for treating tobacco sheet production wastewater according to claim 8 or 12, wherein the membrane module of the MBR system has a membrane pore diameter of 0.10 to 0.2 μm, a working pressure of -1 to -50 kPa, and an operating temperature. It is 5 to 45 °C.