CN102190412B - Method for recycling textile dyeing and finishing wastewater - Google Patents
Method for recycling textile dyeing and finishing wastewater Download PDFInfo
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Abstract
The invention discloses a method for recycling textile dyeing and finishing wastewater, which comprises the following steps of: regulating the pH of the textile dyeing and finishing wastewater in a regulating tank to be 7.0 by using acidic solution, performing coagulative precipitation in a coagulative precipitation tank by using an inorganic flocculating agent, and performing anaerobic treatment in a high-efficiency anaerobic reactor; performing anaerobic/anoxic and aerobic circulation treatment in a multi-stage circulation aerobic treatment system, wherein the multi-stage circulation aerobic treatment system consists of anaerobic/anoxic reaction tanks A and aerobic reaction tanks O in an A-O-A-O-A-O-A staggered series connection mode; performing coagulative precipitation in a high-efficiency air floatation coagulative precipitation tank; and performing ozone oxidation and disinfection in an ozone oxidation tank to obtain recycled water. Compared with the conventional physical-chemical method, the technology has the advantages that: operating cost is obviously reduced, and over 30 percent of economic benefit is achieved. The quality of the treated water is high, and 70 percent of recycling rate can be achieved.
Description
(1) technical field;
The present invention relates to a kind of textile dyeing and finishing waste water reclamation treatment process, belong to the Study on Water Pollution Control field.
(2) background technology:
Water is that human survival and fundamental conditions are irreplaceable most important basic substances in the human society activity in production process.China belongs to the heavy lack of water of moderate country, and lack of water makes annual national industrial or agricultural lose 3,500 hundred million yuan, about 2,000 hundred million Renminbi of the loss of annual gross industrial output value.Water resources supply and demand deficiency more and more becomes " bottleneck " that influences socio-economic development, causing a major reason of water resources critical shortage is exactly that pollution tendencies increases the weight of day by day, wherein trade effluent especially the below standard discharging of textile printing and dyeing wastewater be one of major reason that causes water resource pollution.Along with dyeing and printing process and shift in product mix; variation has also taken place in the composition of dyeing waste water; dyeing waste water organic pollutant content height, dark, alkaline big, the complicated component of colourity; the intractability of waste water increases, and therefore strengthens the processing research of the organic dyeing waste water of difficult degradation is had great importance to the protection environment.
The country of many serious water shortages comprises Israel, Japan, the U.S., Russia, Britain etc. all in active development sewage recycling technology in the world at present.The sewage recycling cause of China has also entered comprehensive the unloading phase, national standardization management committee has newly released " urban sewage reutilization classification " (GB/T 18919-2002), " urban sewage reutilization city miscellaneous water water quality " (GB/T 18920-2002) and " urban sewage reutilization water for scenic environment use water quality " (GB/T 18921-2002), filled up the blank of China's urban sewage reutilization standard, for realizing that sewage recycling provides technical basis.Sound along with the progress of society and standard specifications, the regeneration effluent technology requirement has also been mentioned a new height, and development and application novel sewage recycling technology has safely and efficiently become research focus and the development trend of 21 century water-treatment technology field.
The most scabrous in the dyeing waste water advanced treatment process is the removal of colourity and hardly degraded organic substance, handles fundamental method and mainly contains physics, chemistry, bioremediation (table 1).Simple physics, chemistry, biological treatment are difficult to make waste water to reach water quality and then realization qualified discharge and middle water reuse preferably.Coupling technique but can make physics, chemistry, biological cleaning action organically combine, and has complementary advantages, and gives full play to the strong point of various treatment processs, and pollutent is farthest removed.
The quality analysis of the different dyeing and finishing wastewater treatment processs of table 1
(3) summary of the invention
The objective of the invention is to by using anaerobic-aerobic+ozone oxidation sterilizing decoloration process,, colourity height poor at the dyeing waste water biochemical and the high problem of ionic strength are carried out orientation and are removed, and enhanced biological is degraded, decolorization.Utilize the high sludge activity of the efficient anaerobic+aerobic combination process that refluxes and the characteristics of high volumetric loading more, realize waste water advanced processing, adopt ozone oxidation decolouring disinfection technology further to decolour at last and sterilize, finish organically blending of wastewater treatment and resource utilization, guarantee that reuse water can be back to use in the middle of the dyeing process.
The technical solution used in the present invention is:
A kind of textile dyeing and finishing waste water reclamation treatment process said method comprising the steps of:
(1) textile dyeing and finishing waste water is regulated pH to 7.0 with acidic solution in equalizing tank,
(2) waste water of handling through step (1) enters coagulative precipitation tank and uses inorganic flocculating agent to carry out coagulating sedimentation to handle, and the dosage of described inorganic flocculating agent is: 3-5mg/L waste water;
(3) waste water after step (2) precipitation process enters high efficiency anaerobic reactor and carries out anaerobic treatment;
(4) waste water of handling through step (3) enters multi-stage circulating aerobic treatment system and carries out anaerobic/anoxic, aerobic circular treatment, and described multi-stage circulating aerobic treatment system is composed in series (aerobic reaction pond O can by aeration and water inlet adjusting) by the staggered mode according to A-O-A-O-A-O-A of anaerobic/anoxic reaction tank A and aerobic reaction pond O;
(5) waste water after step (4) is handled enters the efficient air-floating coagulative precipitation tank, in coagulative precipitation tank, feed microbubble, add flocculation agent PAC and coagulant aids PAM carries out coagulating sedimentation, flocculation agent PAC dosage in the described efficient air-floating coagulative precipitation tank is 2-5mg/L waste water, and the dosage of described coagulant aids PAM is 0.1-0.5mg/L waste water;
(6) waste water after step (5) is handled enters the ozone oxidation pond, carries out ozone oxidation sterilizing and handles, and the ozone dosage is 1.1-5mg/L waste water in the described ozone oxidation pond, obtains handling the water of recovery.
Acidic solution in the described step (1) is used for adjust pH, because dyeing and finishing wastewater all is alkalescence, so regulate with acidic solution.For cost saving, preferably transfer (such as common laboratory has acid experiment waste water) with acid waste water, can certainly use common acid reagent such as sulfuric acid, hydrochloric acid.
Inorganic flocculating agent in the described step (2) can be polymerize aluminum chloride, aluminium iron polychloride, ferrous sulfate or bodied ferric sulfate, and wherein the ferrous sulfate effect is best, but the polymerize aluminum chloride price comparison is low, industrial advantageous applications polymerize aluminum chloride.
High efficiency anaerobic reactor in the described step (3) is for obtaining the IC reactor of high reactivity anaerobic bacteria flora by debugging in early stage, domestication, under pH value neutrallty condition, in the anaerobic environment, under the 20-40 ℃ of temperature, handle 18-36h, preferably make anaerobism water outlet COD below 800mg/L.
Further, described debugging in early stage is carried out by the following method: inoculate anaerobic grain sludge in the IC reactor, feed debugging waste water again, under pH value neutrallty condition, in the anaerobic environment, acclimation sludge under the 20-40 ℃ of temperature, the COD concentration of debugging waste water begins to increase every day concentration from 200mg/L, increasing velocity with 100mg/L every day, enter up to Yuan Shui, adopt the microbial ecological in the PCR-DGGE method detection waste water, and follow the tracks of the water outlet of IC reactor and produce the biogas situation, when IC reactor water outlet COD can be stabilized between the 500-900mg/L, biogas yield reaches 0.25m
3/ kg.COD represents that namely system debug is stable, and domestication obtains the high anaerobic bacteria flora of living.
The waste water that obtains through step (3) in the described step (4) enters multi-stage circulating aerobic treatment system and carries out anaerobic/anoxic, aerobic circular treatment, anaerobic/anoxic reaction tank A is 2: 1 with the useful volume ratio of aerobic reaction pond O in the described multi-stage circulating aerobic treatment system, obtain staged denitrogenation flora by debugging domestication in early stage among the anaerobic/anoxic reaction tank A of described multi-stage circulating aerobic treatment system and the aerobic reaction pond O, handle under the normal temperature and reach following standard until water outlet: below the BOD 10mg/L, below the COD 50mg/L, below the TP 0.5mg/L, NH
3Below-N the 5mg/L, below the TN 15mg/L.
Further, the anaerobic/anoxic reaction tank A of described multi-stage circulating aerobic treatment system and the early stage among the O of aerobic reaction pond, debugging was carried out by the following method:
Inoculate aerobic activated sludge among the anaerobic/anoxic reaction tank A, concentration is 3-5g/L, inoculate aerobic activated sludge among the O of aerobic reaction pond, concentration is 3-5g/L, feed debugging waste water, acclimation sludge, the COD concentration of debugging waste water begins to increase every day concentration from 50mg/L, the gradient that increase every day is 10-20mg/L, up to default IC reactor effluent COD concentration, the debugging waste strength arrives namely that step (3) is about to obtain when going out water concentration, adopts the PCR-DGGE method to detect microbial ecological in the waste water, and follows the tracks of the water outlet of multi-stage circulating aerobic treatment system, when water outlet can be stablized the following standard that reaches: below the BOD 10mg/L, below the COD 50mg/L, below the TP 0.5mg/L, NH
3Below-N the 5mg/L, below the TN 15mg/L, the expression system debug is stable.
Preferred, preceding 2 aerobic reaction pond O carry out multipoint water feeding in the described multi-stage circulating aerobic treatment system, and making C/N (carbon-nitrogen ratio) is 2.8～3.2.
Waste water in the described step (5) after step (4) is handled enters the efficient air-floating coagulative precipitation tank and handles common first coagulation 15min at normal temperatures; Precipitate 30min then.
It is to adopt the micro-pore aeration mode that ozone oxidation sterilizing described in the described step (6) is handled, feed ozone at the waste water of handling through step (5) and carry out the ozone oxidation sterilizing processing, handle 12min-20min, water outlet COD is reached below the 25mg/L, obtain handling the water of recovery.
Under multistage backflow aerobic treatment system in the step (4) be used for the efficient COD of removal and TN; The highly effective coagulation precipitation of step (5) is for reducing SS, colourity and COD; Use the ozonation aerated system of micropore in the step (6), further decolouring, sterilization guarantee the effluent reuse standard.
The advantage of the technology of the present invention:
1) the technology main body adopts biodegradation technique (anaerobic-aerobic), can reclaim certain quantity of energy---biogas in wastewater treatment process, has energy-saving and emission-reduction effect preferably.
2) the efficient anaerobic degradation technique of technology application adopts directed microbiological deterioration technology, COD degraded and the decolorizing effect pointed and good to textile dyeing and finishing waste water.
3) many backflows aerobic treatment technology reinforced phosphor-removing denitrifying of technology application makes outputted aerobic water can reach " the main water pollutant emission limit of TAI HU AREA urban wastewater treatment firm and priority industry industry " standard.
4) technology is in the mode of biological-chemical method coupling, obviously reduces than the physical-chemical method running cost of routine, has the economic benefit more than 30%.
5) the water quality treatment quality is higher, and water outlet can reach " urban sewage reutilization city miscellaneous water water quality " (GB/T 18920-2002), can reach 70% regeneration rate.
6) present method has higher industrial applications prospect, is fit to the exploitation of series product.
The present invention adopts efficient anaerobic-many backflows aerobic treatment technology to estimate to make that the clearance of COD reaches 95% in the waste water, and water outlet COD is down to 50mg/L, NH
3-N is less than 5.0mg/L, and TP is less than 0.5mg/L, and TN is less than 15mg/L, reach one-level A emission standard, satisfy the processing requirement that washes cloth, wastewater recycle rate surpasses more than 70%, can reach advanced treatment and regeneration requirement, this process system is stable, capacity of resisting impact load is strong; The follow-up operation cost of investment of employing again and low coagulating sedimentation and the ozone oxidation of running cost are main degree of depth recycling processing technique, guarantee that water outlet can be back to use in the dyeing and Finishing, the gained water outlet is applied to dyeing and finishing (washing cloth) technology, can not cause dyeing and finishing aberration and cloth spot problem.
The present technique main body adopts the biologic treating technique of anaerobic-aerobic, has good input-output ratio.Ton wastewater treatment expense is lower than 5.2 yuan, and processing costs is handled low more than 30% than conventional materialization.Can partially recycled biogas be used for the heating of processing unit in addition in the anaerobic technique section, the advanced treatment water outlet can direct reuse in dyeing and finishing technology, when reducing discharging, also saved enterprise water use greatly.
In the inventive method, the main process of the advanced treatment of textile dyeing and finishing waste water and reuse technology mainly by efficient anaerobic-reflux more aerobic and system, coupled ozone oxidation finish.Strengthen the lifting of clearing up and reacting load of decolouring, hardly degraded organic substance by the regulation and control of the microorganism in the anaerobic reaction process; The aerobic employing multiple spot reflux techniques that reflux are determined the multistage microorganism gradient of reaction process more, form have the different process requirement along journey, strengthen nitrogen removal performance and advanced treatment effect in the reaction process; Ozone oxidation adopts micro-pore aeration system, further removes colourity and the sterilization of bio-chemical effluent, guarantees the reuse requirement of water outlet.
The inventive method is sought suitable operational conditions ratio by the regulation and control to anaerobic technique pH, nutritive salt and characteristic microorganism species in reactive system, improve reactor load and decolorizing efficiency, the feedback regulation of multi-stage circulating aerobic system reflux ratio, aeration rate and microorganism carries out condition optimizing, seeks optimum reaction conditions; The ozone oxidation system determines the dosage of economical rationality by the condition research to whole coupling reaction system temperature, water inlet DOC, ionic strength, free radical scavenger.On this basis, set up textile dyeing and finishing waste water recycling coupled system, accomplish the processing efficiency height, operating automation degree height, the reactive system of the little and economic and reliable of labour intensity.
(4) description of drawings
Fig. 1 process flow sheet
Fig. 2 high efficiency anaerobic reactor Inlet and outlet water COD concentration and removal efficiency diagram
Fig. 3 multi-stage circulating aerobic treatment Inlet and outlet water COD of system concentration and removal efficiency diagram
Fig. 4 multi-stage circulating aerobic treatment system Inlet and outlet water ammonia nitrogen concentration and removal efficiency diagram
Fig. 5 multi-stage circulating aerobic treatment system Inlet and outlet water total nitrogen concentration and removal efficiency diagram
Fig. 6 efficient air-floating coagulative precipitation tank Inlet and outlet water ionic strength and removal efficiency diagram
Fig. 7 efficient air-floating coagulative precipitation tank Inlet and outlet water total nitrogen concentration and removal efficiency diagram
(5) embodiment
The present invention will be further described with specific embodiment below, but protection scope of the present invention is not limited thereto.
The multi-stage circulating aerobic treatment system that uses in the embodiment of the invention is composed in series according to the mode of A-O-A-O-A-O-A by anaerobic/anoxic reaction tank A and aerobic reaction pond O, anaerobic/anoxic reaction tank A (useful volume 10L) is 2: 1 with the useful volume ratio of aerobic reaction pond O (useful volume 5L)
Inoculation anaerobic grain sludge in the IC reactor (useful volume 50L), feed debugging waste water again, under pH value neutrallty condition, in the anaerobic environment, acclimation sludge under the 20-40 ℃ of temperature, the COD concentration of debugging waste water from 200mg/L begin to increase every day concentration (every day 100mg/L increasing velocity,) enter up to Yuan Shui, adopt the microbial ecological in the PCR-DGGE method detection waste water, and follow the tracks of the water outlet of IC reactor and produce the biogas situation, when IC reactor water outlet COD can be stabilized between the 500-900mg/L, biogas yield reaches 0.25m
3/ kg.COD represents that namely system debug is stable, and domestication obtains the high anaerobic bacteria flora of living.
Inoculate aerobic activated sludge among the anaerobic/anoxic reaction tank A, concentration is 4g/L, inoculate aerobic activated sludge among the O of aerobic reaction pond, concentration is 4g/L, feed debugging waste water, acclimation sludge, the COD concentration of debugging waste water begins to increase every day concentration (gradient of increase is 10-20mg/L) up to default IC reactor effluent COD concentration from 50mg/L, adopt the microbial ecological in the PCR-DGGE method detection waste water, and follow the tracks of the water outlet of multi-stage circulating aerobic treatment system, when water outlet can be stablized the following standard that reaches: below the BOD 10mg/L, below the COD 50mg/L, below the TP 0.5mg/L, NH
3Below-N the 5mg/L, below the TN 15mg/L, the expression system debug is stable.
After system debug is stable, feeds waste water and handle, waste water is continuous feeding, and system moves continuously, adjusts flow velocity, guarantees treatment time in each pond with hydraulic detention time HRT.Hydraulic detention time refers to that treatment sewage is in the reactor
Mean residence time, the average reaction time of microbial process in sewage and the bio-reactor just.Therefore, if the useful volume of reactor is V (cubic meter), then: HRT=V/Q (h).If height for reactor is H (rice), then:
Since Q=uA, V=HA
So HRT also can be expressed as: HRT=H/u (h)
It is the ratio that hydraulic detention time equals height for reactor and upper reaches speed.
This is to well known to a person skilled in the art knowledge, under the situation that the useful volume of each reaction tank is determined, can control HRT by regulating flooding velocity or upper reaches flow velocity, and the treatment time of indication is HRT in the embodiment of the invention.
(technical process waste water mixes to adopt common textile dyeing and finishing industry waste water, COD 3500mg/L), after entering equalizing tank (useful volume 60L), adopt acid experiment waste water to regulate pH to 7.0, enter coagulative precipitation tank then, add 4.5mg/L PAC (polymerize aluminum chloride) and carry out coagulating sedimentation, handle 50min, water outlet this moment COD 2200mg/L enters high efficiency anaerobic reactor IC reactor (Paques, Holland then, useful volume 50L), under pH value neutrallty condition, in the anaerobic environment, under the normal temperature, handle 24h, water outlet COD is average out to 600mg/L, enters multi-stage circulating aerobic treatment system again and carries out anaerobic/anoxic, handle 8h under the aerobic circular treatment, normal temperature, the BOD 10mg/L of water outlet, COD 45mg/L, TP 0.45mg/L, NH
3-N 4.2mg/L, TN 15mg/L.Water outlet enters efficient air-floating coagulative precipitation tank (useful volume 15L), and with highly effective coagulation air supporting method, the feeding microbubble adds 3mg/L flocculation agent PAC and 0.4mg/L coagulant aids PAM carries out coagulating sedimentation, first coagulation 15min; Precipitate 30min then, water outlet is better than country-level A standard, enters ozone oxidation pond (useful volume 5L) at last, carry out ozone oxidation sterilizing and handle, the ozone dosage is 2.5mg/L, adopts the micro-pore aeration mode, handle 15min, water outlet COD 20mg/L obtains handling the water of recovery.
According to the method described above, system moves many days continuously, record the IC reactor water inlet COD of every day, on average at 1980mg/L, water outlet COD, can be down to about 500mg/L, calculate its volumetric loading rate and COD clearance, see Fig. 1 for details, as can see from Figure 1, anaerobic biological reactor the volumetric loading rate can be increased to 15kg COD/ (d m
3) more than, the COD decreasing ratio can reach more than 70%.
Upflow velocity in the change IC reactor, the water outlet of respective reaction device and operating parameter outcome record such as following table 2.
Upflow velocity and reactor operating parameter in the table 2 anaerobic reactor operational process
Record the water inlet COD of every day of multi-stage circulating aerobic treatment system, on average at 350mg/L, water outlet COD, can be lower than 50mg/L, calculate its COD clearance, see Fig. 3 for details, as can see from Figure 3, the COD clearance is more than 50%.
Record the multi-stage circulating aerobic treatment system influent ammonia nitrogen value of every day, average out to 40mg/L, water outlet ammonia nitrogen value on average about 5mg/L, are calculated its ammonia nitrogen removal frank, see Fig. 4 for details, and as can see from Figure 4, ammonia nitrogen removal frank can reach 100%.
Record the multi-stage circulating aerobic treatment system water inlet total nitrogen value of every day, average out to 50mg/L, water outlet total nitrogen value about 15mg/L, are calculated its nitrogen removal rate, see Fig. 5 for details, and as can see from Figure 5, the TN clearance can reach 70%.
Record the efficient air-floating coagulative precipitation tank water inlet ionic strength of every day, average out to 2.8 * 10
3Mol/L, water outlet ionic strength are approximately 500mol/L, calculate its ionic strength clearance, see Fig. 6 for details, and as can see from Figure 6, the ionic strength clearance can reach more than 85%.
The water inlet total nitrogen value of record efficient air-floating coagulative precipitation tank every day about average out to 15mg/L, water outlet total nitrogen value, is lower than 12mg/L, calculates its nitrogen removal rate, sees Fig. 7 for details, and as can see from Figure 7, nitrogen removal rate can reach more than 10%.
Claims (8)
1. textile dyeing and finishing waste water reclamation treatment process is characterized in that said method comprising the steps of:
(1) textile dyeing and finishing waste water is regulated pH to 7.0 with acidic solution in equalizing tank,
(2) waste water of handling through step (1) enters coagulative precipitation tank and uses inorganic flocculating agent to carry out coagulating sedimentation to handle, and the dosage of described inorganic flocculating agent is 3-5mg/L waste water;
(3) waste water after step (2) precipitation process enters high efficiency anaerobic reactor and carries out anaerobic treatment; Described high efficiency anaerobic reactor is for obtaining the IC reactor of high reactivity anaerobic bacteria flora by debugging in early stage, domestication;
(4) waste water of handling through step (3) enters multi-stage circulating aerobic treatment system and carries out anaerobic/anoxic, aerobic circular treatment, and described multi-stage circulating aerobic treatment system is composed in series by the mode that anaerobic/anoxic reaction tank A and aerobic reaction pond O interlock according to A-O-A-O-A-O-A; Anaerobic/anoxic reaction tank A and the useful volume of aerobic reaction pond O are than being 2:1 in the described multi-stage circulating aerobic treatment system, obtain staged denitrogenation flora by debugging domestication in early stage among the anaerobic/anoxic reaction tank A of described multi-stage circulating aerobic treatment system and the aerobic reaction pond O, handle under the normal temperature and reach following standard until water outlet: below the BOD10mg/L, below the COD50mg/L, below the TP0.5mg/L, NH
3Below-the N5mg/L, below the TN15mg/L;
The anaerobic/anoxic reaction tank A of described multi-stage circulating aerobic treatment system and debugging domestication in the early stage among the O of aerobic reaction pond are carried out by the following method:
Inoculate aerobic activated sludge among the anaerobic/anoxic reaction tank A, concentration is 3-5g/L, inoculate aerobic activated sludge among the O of aerobic reaction pond, concentration is 3-5g/L, feed debugging waste water, acclimation sludge, debugging begins to increase every day concentration with the COD concentration of waste water from 50mg/L, the gradient that increases every day is 10-20mg/L, up to the default effluent COD concentration of IC reactor, adopts the PCR-DGGE method to follow the tracks of and detect the water outlet of described multi-stage circulating aerobic treatment system, can stablize when water outlet and to reach following: below the BOD10mg/L, below the COD50mg/L, below the TP0.5mg/L, NH
3Below-the N5mg/L, below the TN15mg/L, the expression system debug is stable;
(5) waste water after step (4) is handled enters the efficient air-floating coagulative precipitation tank, with highly effective coagulation air supporting method, feed microbubble, add flocculation agent PAC and coagulant aids PAM carries out coagulating sedimentation, flocculation agent PAC dosage in the described efficient air-floating coagulative precipitation tank is 2-5mg/L waste water, and the dosage of described coagulant aids PAM is 0.1-0.5mg/L waste water;
(6) waste water after step (5) is handled enters the ozone oxidation pond, carries out ozone oxidation sterilizing and handles, and the ozone dosage is 1.1-5mg/L waste water in the described ozone oxidation pond, obtains handling the water of recovery.
2. textile dyeing and finishing waste water reclamation treatment process as claimed in claim 1, it is characterized in that the high efficiency anaerobic reactor in the described step (3) obtains the IC reactor of high reactivity anaerobic bacteria flora for process debugging in early stage, domestication, under pH value neutrallty condition, in the anaerobic environment, under the 20-40 ℃ of temperature, handle 18-36h.
3. the method for claim 1 is characterized in that the waste water after step (4) is handled enters the efficient air-floating coagulative precipitation tank in the described step (5) to handle first coagulation 15min at normal temperatures; Precipitate 30min then.
4. the method for claim 1, it is characterized in that it is to adopt the micro-pore aeration mode that the ozone oxidation sterilizing described in the described step (6) is handled, feed ozone at the waste water of handling through step (5) and carry out the ozone oxidation sterilizing processing, handle 12min-20min, water outlet COD is reached below the 25mg/L, obtain handling the water of recovery.
5. the method for claim 1 is characterized in that the acidic solution in the described step (1) is acid waste water.
6. the method for claim 1 is characterized in that the inorganic flocculating agent in the described step (2) is polymerize aluminum chloride, aluminium iron polychloride, ferrous sulfate or bodied ferric sulfate.
7. method as claimed in claim 6 is characterized in that described inorganic flocculating agent is polymerize aluminum chloride.
8. method as claimed in claim 2, it is characterized in that described early stage, debugging was carried out by the following method: inoculate anaerobic grain sludge in the IC reactor, feed debugging waste water again, under pH value neutrallty condition, in the anaerobic environment, acclimation sludge under the 20-40 ℃ of temperature, the COD concentration of debugging waste water begins to increase every day concentration from 200mg/L, increasing velocity with 100mg/L every day, enter up to Yuan Shui, adopt the microbial ecological in the PCR-DGGE method detection waste water, and follow the tracks of the water outlet of IC reactor and produce the biogas situation, COD is stabilized between the 500-900mg/L when the water outlet of IC reactor, biogas yield reaches 0.25m
3/ kgCOD represents that namely system debug is stable, and domestication obtains the high anaerobic bacteria flora of living.
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|---|---|---|---|---|
| CN103508632A (en) * | 2013-09-24 | 2014-01-15 | 吴江唯奇布业有限公司 | Textile sewage treatment system |
| CN103523996B (en) * | 2013-10-18 | 2016-03-30 | 东华大学 | A kind for the treatment of unit of stamp destarch composite waste and method |
| CN103739064B (en) * | 2013-12-24 | 2016-03-23 | 广州中国科学院沈阳自动化研究所分所 | The application of a kind of aerobic activated sludge in treatment of dyeing wastewater process |
| CN104944693A (en) * | 2015-06-10 | 2015-09-30 | 上海化学工业区中法水务发展有限公司 | Method and device for purifying and treating chemical industrial wastewater |
| CN106630472A (en) * | 2016-12-30 | 2017-05-10 | 四川亿龙环保工程有限公司 | Printing and dyeing waste water treatment process |
| CN106915848A (en) * | 2017-04-20 | 2017-07-04 | 佛山市佳利达环保科技股份有限公司 | A kind of method using ozone tail gas treatment sewage is contained |
| CN109809647B (en) * | 2019-03-25 | 2024-01-09 | 福建省新宏港纺织科技有限公司 | Textile wastewater recycling process system |
| CN110255829A (en) * | 2019-07-12 | 2019-09-20 | 苏州苏沃特环境科技有限公司 | A kind of printing waste water Bio-DeN biological denitrification method and device |
| CN112010501B (en) * | 2020-08-19 | 2022-04-29 | 金润源环境科技（昆山）有限公司 | Comprehensive wastewater treatment device and comprehensive wastewater treatment method |
| CN115367874A (en) * | 2022-06-30 | 2022-11-22 | 华南理工大学 | Method for treating waste paper papermaking wastewater and recycling by using high-efficiency coagulation-biological strengthening combined process |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1800050A (en) * | 2005-12-15 | 2006-07-12 | 南京大学 | Waste water treatment method of anerobic- anoxia-aerobic-coagulated precipitation |
| CN1958477A (en) * | 2006-11-28 | 2007-05-09 | 厦门大学 | Integrative anaerobic - aerobic circulation biological method for treating organic wastewater |
| CN101293726A (en) * | 2008-06-06 | 2008-10-29 | 南京大学 | Method for processing and separate-recycling printing and dyeing wastewater |
-
2011
- 2011-05-23 CN CN 201110133330 patent/CN102190412B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1800050A (en) * | 2005-12-15 | 2006-07-12 | 南京大学 | Waste water treatment method of anerobic- anoxia-aerobic-coagulated precipitation |
| CN1958477A (en) * | 2006-11-28 | 2007-05-09 | 厦门大学 | Integrative anaerobic - aerobic circulation biological method for treating organic wastewater |
| CN101293726A (en) * | 2008-06-06 | 2008-10-29 | 南京大学 | Method for processing and separate-recycling printing and dyeing wastewater |
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| CN102190412A (en) | 2011-09-21 |
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Address after: 214100 Jiangsu city of Wuxi province Xishan economic and Technological Development Zone No. 2 Feng Wei Lu savera No. 1 107&108 Patentee after: Jiangsu Eic water Co., Ltd. Address before: 214100 Furong three road 99, Xishan Economic Development Zone, Xishan District, Wuxi, Jiangsu Patentee before: Jiangsu Shangda Water Affair Co., Ltd. |