CN107569902B - A kind of processing method and processing device of dyeing waste water - Google Patents
A kind of processing method and processing device of dyeing waste water Download PDFInfo
- Publication number
- CN107569902B CN107569902B CN201710925044.9A CN201710925044A CN107569902B CN 107569902 B CN107569902 B CN 107569902B CN 201710925044 A CN201710925044 A CN 201710925044A CN 107569902 B CN107569902 B CN 107569902B
- Authority
- CN
- China
- Prior art keywords
- filter
- ceramic membrane
- tubular ceramic
- waste water
- polyacrylate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 55
- 238000004043 dyeing Methods 0.000 title claims abstract description 24
- 238000003672 processing method Methods 0.000 title claims abstract description 18
- 238000012545 processing Methods 0.000 title claims abstract description 11
- 239000012528 membrane Substances 0.000 claims abstract description 118
- 239000000919 ceramic Substances 0.000 claims abstract description 95
- 229920000058 polyacrylate Polymers 0.000 claims abstract description 56
- 238000000034 method Methods 0.000 claims abstract description 50
- 238000004140 cleaning Methods 0.000 claims abstract description 42
- 230000008569 process Effects 0.000 claims abstract description 40
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000001914 filtration Methods 0.000 claims abstract description 24
- 239000002002 slurry Substances 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims description 21
- 239000007788 liquid Substances 0.000 claims description 20
- 239000012065 filter cake Substances 0.000 claims description 19
- 239000000706 filtrate Substances 0.000 claims description 16
- 238000011045 prefiltration Methods 0.000 claims description 16
- 239000002253 acid Substances 0.000 claims description 15
- 239000003513 alkali Substances 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 15
- 230000000670 limiting effect Effects 0.000 claims description 15
- 239000012141 concentrate Substances 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 14
- 238000009990 desizing Methods 0.000 claims description 13
- 230000000149 penetrating effect Effects 0.000 claims description 13
- 238000003825 pressing Methods 0.000 claims description 13
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 229910017604 nitric acid Inorganic materials 0.000 claims description 12
- 239000011148 porous material Substances 0.000 claims description 12
- 230000002000 scavenging effect Effects 0.000 claims description 10
- 239000012298 atmosphere Substances 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- 239000004744 fabric Substances 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims description 7
- -1 sodium alkyl benzene Chemical class 0.000 claims description 7
- 239000010453 quartz Substances 0.000 claims description 6
- DPXJVFZANSGRMM-UHFFFAOYSA-N acetic acid;2,3,4,5,6-pentahydroxyhexanal;sodium Chemical compound [Na].CC(O)=O.OCC(O)C(O)C(O)C(O)C=O DPXJVFZANSGRMM-UHFFFAOYSA-N 0.000 claims description 5
- 229940077388 benzenesulfonate Drugs 0.000 claims description 5
- 239000011734 sodium Substances 0.000 claims description 5
- 229910052708 sodium Inorganic materials 0.000 claims description 5
- 239000001768 carboxy methyl cellulose Substances 0.000 claims description 4
- 229910052573 porcelain Inorganic materials 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 4
- 235000019812 sodium carboxymethyl cellulose Nutrition 0.000 claims description 4
- 229920001027 sodium carboxymethylcellulose Polymers 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims 2
- 238000007906 compression Methods 0.000 claims 2
- 230000004907 flux Effects 0.000 abstract description 22
- 238000005516 engineering process Methods 0.000 abstract description 11
- 238000011084 recovery Methods 0.000 abstract description 11
- 230000000903 blocking effect Effects 0.000 abstract description 10
- 238000005374 membrane filtration Methods 0.000 abstract description 3
- 239000011241 protective layer Substances 0.000 abstract description 3
- 239000010410 layer Substances 0.000 description 16
- 239000003795 chemical substances by application Substances 0.000 description 11
- 239000012466 permeate Substances 0.000 description 8
- 238000007670 refining Methods 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000013618 particulate matter Substances 0.000 description 3
- 238000007639 printing Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000000502 dialysis Methods 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 239000010812 mixed waste Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 1
- 235000011613 Pinus brutia Nutrition 0.000 description 1
- 241000018646 Pinus brutia Species 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229920003123 carboxymethyl cellulose sodium Polymers 0.000 description 1
- 229940063834 carboxymethylcellulose sodium Drugs 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000001427 coherent effect Effects 0.000 description 1
- 238000009295 crossflow filtration Methods 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000013051 drainage agent Substances 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000013076 target substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 229920003169 water-soluble polymer Polymers 0.000 description 1
- 238000009941 weaving Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/16—Use of chemical agents
- B01D2321/168—Use of other chemical agents
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a kind of processing method and processing devices of dyeing waste water to belong to water-treatment technology field more particularly to the processing method of desized wastewater in dyeing process.The processing method that the present invention uses can solve the problem that ceramic membrane is kept film operating flux low by the pollution of polyacrylate slurry, while solve the problems, such as that flux recovery is low after caused Membrane cleaning after polyacrylate blocking fenestra.The technical concept that the present invention uses is: filter aid diatomite is added in polyacrylate slurry to be processed; in membrane filtration processes; the protective layer of film surface can be formed; on the one hand the generation of fouling membrane is prevented; on the other hand it can prevent polyacrylate from blocking membrane flux, flux after Membrane cleaning is preferably restored；And filter aid is not allowed to easily cause the channel blockage of tubular ceramic membrane in filtering.
Description
Technical field
The present invention relates to a kind of processing method and processing devices of dyeing waste water, more particularly to desized wastewater in dyeing process
Processing method belongs to water-treatment technology field.
Background technique
The processes such as drift refining, dyeing, stamp, arrangement in dyeing and printing process generate largely containing the waste water of organic pollutant, tool
Have the features such as water is big, organic pollutant content is high, color is deep, alkalinity is big, change of water quality is big, belong to intractable industrial wastewater it
One.Printing and dyeing engineering and generally requires one or many washings using water as medium, and water consumption is bigger, the waste water of discharge at
Point complexity, environmental pollution is serious, processing it is difficult.The general processing method of dyeing waste water has physico-chemical process (such as absorption, gas
Floating, coagulation, oxidation, electrolysis etc.) and biochemical method and their combination, it is single at present in view of the special circumstances of dyeing waste water water quality
(for example ceramic membrane filter technology and other technologies join the not satisfactory of wastewater processing technology treatment effect so the combination of more technologies
With) have become the development trend of techniques of Dyeing Wastewater Treatment；Simultaneously as the reclamation rate of printing and dyeing mill's water is only 7%, it is entire to weave
Industry reusing rate is the minimum industry of all industry Treated sewage reusing rates in the whole nation less than 10%, so related researcher gradually will
Attention is transferred on technology of middle water recycle, and inorganic ceramic membrane also plays important, new role in this respect.
Polyacrylate is a kind of water soluble polymer, have excellent serous coat, adhesiveness, wearability and easily
The feature compatible with other slurries is applied to the industries such as weaving, papermaking, chemical industry as slurry.According to statistics, China's only spinning sizing agent
Just in 120,000 t or more, the desized wastewater generated every year causes environment huge the polyacrylate amount of consumption up to more than 2,500 ten thousand t
Pressure substantially reduce the biodegradability of desized wastewater due to value < 0.1 BOD5/CODCr of polyacrylate, increase place
Manage difficulty.
Membrane separation technique is achieved the purpose that purify sewage by separation, concentration, the recycling to Pollutants in Wastewater, mainly be had
Micro-filtration, ultrafiltration, nanofiltration and reverse osmosis membrane separation process have many advantages, such as energy conservation, without phase-change, easy to operate, equipment is simple, and can return
Recycling substance is received, has been found to be practicable in terms for the treatment of of dyeing wastewater.Polyacrylate in desized wastewater
If slurry can recycle, resource and cost can be saved, creates economic benefit, moreover it is possible to mitigate difficulty and the row of reduction of wastewater treatment
High-volume micro-filtration and ultrafiltration are separated based on screening mechanism, can retain suspended particles and macromolecular in desized wastewater,
But the effect of separation is not had in ultra-filtration process to the ion in water, liquid flows through film surface under pressure promotion, is less than film
The small molecule solute and water in hole become scavenging solution through moisture film, and the substance that polyacrylate etc. is greater than fenestra is trapped, with concentration
The discharge of liquid form, can be reused for desizing after adjusting polyacrylate concentrate to suitable concentration, scavenging solution can also be back to
Desizing.
CN103755050A discloses a kind of desized wastewater membrane method treating process, and technique includes the following steps: step 1, incites somebody to action
Polyacrylate desized wastewater is sent into purpose ceramic-film filter and is filtered, and obtains the first concentrate and the first penetrating fluid, and first
Penetrating fluid is sent to desizing workshop as desizing liquid reuse；Resulting first concentrate of step 2, step 1 carries out plus water dialysis, obtains
Second penetrating fluid, when the pH of the second penetrating fluid be 7 ~~7.5 when, stop dialysis, start to be concentrated, obtain the second concentrate,
Second concentrate is recycled for slurry, and the first penetrating fluid is back to polyacrylate desized wastewater tank.
A problem in the presence of above-mentioned technology is: polymer concentration, viscosity are all larger in polyacrylate slurry,
When carrying out concentration and recovery in purpose ceramic-film filter, polyacrylate can produce serious influence to the filtration flux of ceramic membrane, make
Flux is lower；Also, polyacrylate can enter ceramic membrane duct in form blocking pollution so that the ceramics after filter process
Film is not easy to clean, and the recovery difficulty for resulting in membrane flux is big.
Summary of the invention
The purpose of the present invention is: solve pollution of the ceramic membrane in CN103755050A technology by polyacrylate slurry
And the problem for keeping film operating flux low, while solving after polyacrylate blocking fenestra that flux recovery is low after caused Membrane cleaning
Problem.The technical concept that the present invention uses is: filter aid diatomite is added in polyacrylate slurry to be processed, in film mistake
During filter, the protective layer of film surface can be formed, the generation of fouling membrane is on the one hand prevented, on the other hand can prevent polypropylene
Acid esters blocks membrane flux, and flux after Membrane cleaning is preferably restored.
Technical solution is:
A kind of processing method of dyeing waste water, includes the following steps:
Step 1 is sent into prefilter polyacrylate desized wastewater and is filtered；
Filter aid is added in the filtrate obtained in step 1 in step 2, after mixing, is sent into tubular ceramic membrane filter
In be filtered；
Step 3, the penetrating fluid of tubular ceramic membrane filter are sent into desizing workshop as desizing liquid reuse；
Step 4, the concentrate of tubular ceramic membrane filter are sent into plate and frame filter press and extrude filter aid, plate and frame filter press
Filtrate is the polyacrylate slurry of recycling.
In the step 1, prefilter is quartz filter.
In the step 2, filter aid is diatomite, and additional amount is 0.5~2wt% of waste water weight.
In the step 2, the ceramic membrane average pore size scope in tubular ceramic membrane filter is 50~200nm, filtering
The crossflow velocity of process is 1~5m/s, and feed liquid temperature is 20~45 DEG C in filter process, filter pressure range is 0.1~
0.5MPa。
In the step 4, the filter cake of plate and frame filter press is sent into burner to burn in air atmosphere or oxygen atmosphere
Processing, the diatomite recycled.
In the step 4, the average pore size of the filter cloth of plate and frame filter press is at 5~20 μm.
In the step 2, tubular ceramic membrane filter after filtering, needs successively to carry out alkali cleaning and acid
The step of cleaning, the alkali cleans, is: using by sodium hydroxide, sodium carboxymethylcellulose, sodium alkyl benzene sulfonate according to weight
Cleaned than the compound alkaline cleaner mixed of 4:0.3~0.5:1~1.5, compound alkaline cleaner in water dosage be 2~
4wt%, the temperature of cleaning process are 40~50 DEG C, 4~6m/s of crossflow velocity in cleaning process, 30~60min of scavenging period；Institute
The step of acid cleaning stated, is: cleaned using nitric acid, the purity of nitric acid is 40~65wt%, nitric acid in water dosage be 1~
3wt%, the temperature of cleaning process are 40~50 DEG C, 4~6m/s of crossflow velocity in cleaning process, 20~40min of scavenging period.
A kind of processing unit of dyeing waste water, comprising:
Prefilter, for carrying out pre-filtering to polyacrylate desized wastewater；
First delivery pump, is connected to prefilter, for polyacrylate desized wastewater to be pressed into prefilter；
Mixing channel, is connected to the material liquid outlet of prefilter, filter aid is connected on mixing channel, tank is added, be used for pre- mistake
Filter aid is added in the permeate of filter, mixing channel is used to for filter aid being uniformly mixed in waste water；
Second delivery pump, is connected to mixing channel, for mixed waste water to be pressed into tubular ceramic membrane filter；
Tubular ceramic membrane filter, for carrying out secondary filter to waste water obtained in mixing channel, by polyacrylate size
Material retention concentration；
Flow container is permeated, the per-meate side of tubular ceramic membrane filter is connected to, for storing obtained filtrate；
Plate and frame filter press is connected to the concentration side of tubular ceramic membrane filter, for point to the filter aid in concentrate
From；
Filters pressing liquid storage tank is connected to the per-meate side of plate and frame filter press, for storing the obtained filter containing polyacrylate
Liquid；
Combustion chamber carries out burning for the filter cake to plate and frame filter press and handles to obtain recycling filter aid；
High-pressure air source is connected to plate and frame filter press, provides pressure to the filtering of plate and frame filter press.
Further include: tank is added in alkaline cleaner, is connected to tubular ceramic membrane filter, for tubular ceramic membrane filter
Alkaline cleaner is added when cleaning.
Further include: tank is added in acid cleaner, is connected to tubular ceramic membrane filter, for tubular ceramic membrane filter
Acid cleaner is added when cleaning.
Include: assembly housing in the structure of tubular ceramic membrane filter, be respectively equipped with end socket at the both ends of assembly housing, seals
It is respectively equipped with material inlet and material outlet on head, tubular ceramic membrane is installed in assembly housing；Both ends inside assembly housing
Equipped with floral disc, pressing plate is equipped in end socket, the both ends of tubular ceramic membrane are respectively fitted in the aperture on floral disc and pressing plate, and pressing plate will
Floral disc realizes the sealing of tubular ceramic membrane after compressing, the pipeline in tubular ceramic membrane is connected to end socket；It is additionally provided in assembly housing
Penetrating fluid outlet；It is additionally provided with anti-blockage structure in the inside for the end socket for being equipped with material outlet, for preventing the pipe of tubular ceramic membrane
Road is blocked by filter cake；Anti-blockage structure includes:
First fixed plate, is fixed on inside end socket；
The side of first fixing piece towards the pipeline of tubular ceramic membrane is connected with spoiler, spoiler court by the first spring
It is equipped with the body of rod to the side of the pipeline of tubular ceramic membrane, the body of rod protrudes into the inside of the pipeline of tubular ceramic membrane；
Second fixed plate, is fixed on inside end socket, and the side of the second fixed plate towards the pipeline of tubular ceramic membrane passes through the
Two springs are connected to spoiler, and the side of spoiler towards the pipeline of tubular ceramic membrane is additionally provided with elastic piece, the side of elastic piece
Equipped with protrusion；Limiting card is additionally provided in end socket, limiting card is used to limit the movement of protrusion；When the first spring is in normal
When state, second spring is in impaction state；When elastic piece deformation, limiting card no longer has position-limiting action to protrusion.
Beneficial effect
The processing method that the present invention uses, which can solve ceramic membrane, runs film by the pollution of polyacrylate slurry
The low problem of flux, while solving the problems, such as that flux recovery is low after caused Membrane cleaning after polyacrylate blocking fenestra.This hair
The technical concept of bright use is: filter aid diatomite is added in polyacrylate slurry to be processed, in membrane filtration processes,
The protective layer of film surface can be formed, the generation of fouling membrane is on the one hand prevented, on the other hand can prevent polyacrylate from blocking
Membrane flux restores flux after Membrane cleaning preferably；And filter aid is not allowed to easily cause tubular ceramic in filtering
The channel blockage of film.
Detailed description of the invention
Fig. 1 is the device figure that the present invention uses；
Fig. 2 is flux vs' figure of purpose ceramic-film filter in filtering；
Fig. 3 is the cleaning flux recovery figure of ceramic membrane in filtering；
Fig. 4 is the mechanism figure that tubular ceramic membrane particle on operational process forms filter cake process；
Fig. 5 is the schematic diagram of the different filter cake thickness of the inlet end and an outlet end of tubular ceramic membrane；
Fig. 6 is the structure chart of tubular ceramic membrane filter；
Fig. 7 is the enlarged drawing that plug structure is deterred in Fig. 6；
Fig. 8 is the structure chart at next filtering moment of Fig. 7.
Wherein, the 1, first delivery pump；2, prefilter；3, mixing channel；4, tank is added in filter aid；5, the second delivery pump；6,
Tubular ceramic membrane filter；7, flow container is permeated；8, plate and frame filter press；9, filters pressing liquid storage tank；10, combustion chamber；11, high-pressure air source；
12, tank is added in alkaline cleaner；13, tank is added in acid cleaner；14, assembly housing；15, end socket；16, penetrating fluid exports；17, tubular type
Ceramic membrane；18, material inlet；19, material outlet；20, pressing plate；21, floral disc；22, flange；23, sealing ring；24, anti-clogging knot
Structure；25, the first fixed plate；26, spoiler；27, the first spring；28, second spring；29, the body of rod；30, hairbrush；31；Elastic piece；
32, protrusion；33, limiting card；34, the second fixed plate.
Specific embodiment
Below by specific embodiment, invention is further described in detail.But those skilled in the art will manage
Solution, the following example is merely to illustrate the present invention, and should not be taken as limiting the scope of the invention.Specific skill is not specified in embodiment
Art or condition person, the according to the literature in the art described technology or conditions (such as " inoranic membrane point write with reference to Xu Nan equality
From technology and application ", Chemical Industry Press, 2003) or carry out according to product description.Agents useful for same or instrument are not infused
Bright production firm person, being can be with conventional products that are commercially available.
Approximate language used herein can be used for modifying in entire disclosure and claims any quantity statement, can
Permit being changed under conditions of not causing its relevant basic function to change.Therefore, it is repaired by term such as " about "
The value of decorations is not limited to specified exact value.In at least some cases, approximate language can be with the instrument for measuring the value
Precision it is corresponding.Unless indicating otherwise in context or sentence, otherwise range limit can be combined and/or exchange, and
And this range is confirmed as and including all subranges contained herein.In addition in the operation embodiment or elsewhere
In indicate except, the number of the amount of all expression compositions, reaction condition etc. used in specification and claims or
Expression shall be construed as the modification by word " about " in all cases.
The value expressed using range format should be interpreted as not only including clearly enumerating as range in a flexible way
The numerical value of limit value, but also including covering all single numbers or subinterval in the range, like each numerical value and sub-district
Between be expressly recited out.For example, the concentration range of " about 0.1% to about 5% " should be understood as not only including clearly enumerating
4%) and subinterval (example the concentration of about 0.1% to about 5% further includes the single concentration in how (e.g., 1%, 2%, 3% and
Such as, 0.1% to 0.5%, 1% to 2.2%, 3.3% to 4.4%).
" removal " in this specification, not only includes the case where completely removing target substance, further includes that part removal (is reduced
The amount of the substance) the case where." purification " in this specification, including remove arbitrary or specific impurity.
Word "include", "comprise" used herein, " having " or its any other variant are intended to cover non-exclusionism
Including.E.g., including technique, method, article or the equipment for listing element are not necessarily limited by those elements, but may include it
He is not explicitly listed or belongs to this technique, method, article or the intrinsic element of equipment.It should be understood that when an element
When being mentioned with another element " connection ", it can be connected directly with other elements or be indirectly connected with other elements, and
Inserted with element between them.
The present invention the percentage refer to mass percent in the absence of special instructions.
Present invention waste water to be dealt with is dyeing waste water, can especially refer in desizing processes and contain polyacrylate
Desized wastewater.
The method of use is:
Step 1 is sent into prefilter polyacrylate desized wastewater and is filtered；Pre-filtered purpose is to get rid of
The impurity of bulky grain in waste water, protects subsequent purpose ceramic-film filter, and prefilter can be quartz filter；
Filter aid is added in the filtrate obtained in step 1 in step 2, after mixing, is sent into tubular ceramic membrane filter
In be filtered, filter aid is diatomite, and additional amount is 0.5~2wt% of waste water weight；The effect of filtrate agent in process is
Cake layer is formed on the surface of ceramic membrane, prevents polyacrylate from blocking ceramic membrane duct, fouling membrane is prevented, improves to filter and lead to
Amount；Flux recovery rate after can also be improved Membrane cleaning；After ceramic membrane filter, refining agent, alkali in waste water can penetrate film layer,
Into per-meate side, and polyacrylate is trapped within concentrate side, the ceramic membrane average pore size model in tubular ceramic membrane filter
Enclosing is 50~200nm, and the crossflow velocity of filter process is 1~5m/s, and feed liquid temperature is 20~45 DEG C in filter process, filtration pressure
Power range is 0.1~0.5MPa；
Step 3, the penetrating fluid of tubular ceramic membrane filter are sent into desizing workshop as desizing liquid reuse；
Step 4, the concentrate of tubular ceramic membrane filter are sent into plate and frame filter press and extrude filter aid, plate and frame filter press
Filtrate is the polyacrylate slurry of recycling.Since the filtering accuracy of flame filter press is smaller, can by polyacrylate with help
Filtering agent is separated, and the particle of diatomite is larger, is retained by filter cloth, and polyacrylate can be used for slurry through after filter cloth
The reuse in workshop, the average pore size of the filter cloth of plate and frame filter press are at 5~20 μm.
The filter cake of plate and frame filter press is sent into burner the burning processing in air atmosphere or oxygen atmosphere, can be by poly- third
After olefin(e) acid ester destroys burning, it is left diatomite, it can reuse again.
In the step 2, tubular ceramic membrane filter after filtering, needs successively to carry out alkali cleaning and acid
The step of cleaning, the alkali cleans, is: using by sodium hydroxide, sodium carboxymethylcellulose, sodium alkyl benzene sulfonate according to weight
Cleaned than the compound alkaline cleaner mixed of 4:0.3~0.5:1~1.5, compound alkaline cleaner in water dosage be 2~
4wt%, the temperature of cleaning process are 40~50 DEG C, 4~6m/s of crossflow velocity in cleaning process, 30~60min of scavenging period；Institute
The step of acid cleaning stated, is: cleaned using nitric acid, the purity of nitric acid is 40~65wt%, nitric acid in water dosage be 1~
3wt%, the temperature of cleaning process are 40~50 DEG C, 4~6m/s of crossflow velocity in cleaning process, 20~40min of scavenging period.Hydrogen
The effect of sodium oxide molybdena is removal organic polluter, and there is carboxymethyl cellulose sodium surface anion to be easily adsorbed at polyacrylate
On particle surface, its dispersion in cleaning solution is more utilized, the surfactant of sodium alkyl benzene sulfonate plays the role of dispersion.
Based on above-mentioned method, processing unit structure provided by the invention is as shown in Figure 1:
Prefilter 2, for carrying out pre-filtering to polyacrylate desized wastewater；
First delivery pump 1, is connected to prefilter 2, for polyacrylate desized wastewater to be pressed into prefilter 2；
Mixing channel 3 is connected to the material liquid outlet of prefilter 2, be connected on mixing channel 3 filter aid be added tank 4, for
Filter aid is added in the permeate of prefilter 2, mixing channel 3 is used to for filter aid being uniformly mixed in waste water；
Second delivery pump 5, is connected to mixing channel 3, for mixed waste water to be pressed into tubular ceramic membrane filter 6；
Tubular ceramic membrane filter 6, for carrying out secondary filter to waste water obtained in mixing channel 3, by polyacrylate
Slurry retention concentration；
Flow container 7 is permeated, the per-meate side of tubular ceramic membrane filter 6 is connected to, for storing obtained filtrate；
Plate and frame filter press 8 is connected to the concentration side of tubular ceramic membrane filter 6, for the filter aid in concentrate
Separation；
Filters pressing liquid storage tank 9 is connected to the per-meate side of plate and frame filter press 8, for store obtain containing polyacrylate
Filtrate；
Combustion chamber 10 carries out burning for the filter cake to plate and frame filter press 8 and handles to obtain recycling filter aid；
High-pressure air source 11 is connected to plate and frame filter press 8, provides pressure to the filtering of plate and frame filter press 8.
Further include: tank 12 is added in alkaline cleaner, is connected to tubular ceramic membrane filter 6, for tubular ceramic membrane mistake
Alkaline cleaner is added when cleaning in filter 6.
Further include: tank 13 is added in acid cleaner, is connected to tubular ceramic membrane filter 6, for tubular ceramic membrane mistake
Acid cleaner is added when cleaning in filter 6.
Using tubular ceramic membrane when being filtered, in the super-cell cake layer of the inlet end and an outlet end of membrane tube
Thickness is different, and the THICKNESS CALCULATION mode of cake layer is as the formula (1), referring to fig. 4 (by particle sedimentation model in cross-flow filtration
To analysis Yang Zezhi, Xi Danli, Mao Yanmei of filter cake thickness, Donghua University's journal (natural science edition) the 6th phase of volume 34):
(1)；
In formula, Δ L is cake layer thickness；F1 is the power caused by permeating perpendicular to film surface；F2 is by cross-flow velocity
The caused power for being parallel to film surface；F3 is the power caused by adhering to and rubbing backward；S is the specific surface area of particle；C is
Grain mass concentration；Δ t is filtration time.
During the filtration process, there can be biggish flow at material inlet end, therefore flow velocity f2 is larger, the diatomite of formation
Filter aid cake layer be easy by cross-flow act on remove, therefore, input end formed super-cell cake layer thickness will not
It is thicker；And with the progress of filtering, penetrating fluid constantly enters per-meate side from the surface of ceramic membrane, and the flow in membrane tube will phase
Reduce with answering, causes the K3F2 item in formula (1) to correspondingly reduce, have led to the increase of filter cake thickness Δ L, will lead to filter cake
Layer is in outlet end thicker structure easy to form, as shown in figure 5, the super-cell cake layer thickness of inlet end and an outlet end
It is different；Have it is some it is extreme in the case where, the cake layer of outlet end can occur diatomite sometimes by the adhesive attraction by greasy dirt and
Generate mutually bonding, increase, until the case where causing channel to be blocked by particulate matter, stickum etc., and particulate matter is in a steady stream not
Enter disconnectedly, will lead to obturator and constantly increase, whole membrane tube channel is made all to be blocked and scrap.Therefore, how height is avoided
The feed liquid of solid content is not in that channel blockage is urgent problem to be solved in engineering in tubular type membrane filtration processes.
The structure of purpose ceramic-film filter employed in the present invention is as shown in Figure 6, comprising: assembly housing 14, in component shell
The both ends of body 14 are respectively equipped with end socket 15, and material inlet 18 and material outlet 19 are respectively equipped on end socket 15, in assembly housing 14
Tubular ceramic membrane 17 is installed；Both ends inside assembly housing 14 are equipped with floral disc 21, and pressing plate 20, tubular type pottery are equipped in end socket 15
The both ends of porcelain film 17 are respectively fitted in the aperture on floral disc 21 and pressing plate 20, and pressing plate 20 realizes tubular ceramic after compressing floral disc 21
The sealing of film 17, the pipeline in tubular ceramic membrane 17 are connected to end socket 15；Penetrating fluid outlet 16 is additionally provided in assembly housing 14；
It is additionally provided with anti-blockage structure 24 in the inside for the end socket for being equipped with material outlet 19, for preventing tubular ceramic membrane 17
Pipeline is blocked by super-cell filter cake；
The enlarged drawing of anti-blockage structure 24 as shown in fig. 7, comprises:
First fixed plate 25, is fixed on inside end socket 15；
The side of first fixed plate 25 towards the pipeline of tubular ceramic membrane 17 is connected with spoiler 26 by the first spring 27,
The side of spoiler 26 towards the pipeline of tubular ceramic membrane 17 is equipped with the body of rod 29, and the body of rod 29 protrudes into the pipeline of tubular ceramic membrane 17
It is internal；
Second fixed plate 34, is fixed on inside end socket 15, the second fixed plate 34 towards tubular ceramic membrane 17 pipeline one
Side is connected to spoiler 26 by second spring 28, and the side of spoiler 26 towards the pipeline of tubular ceramic membrane 17 is additionally provided with elasticity
The side of piece 31, elastic piece 31 is equipped with protrusion 32；Limiting card 33 is additionally provided in end socket 15, limiting card 33 is for limiting protrusion
The movement in portion 32；
When the first spring 27 is in normal condition, second spring 28 is in impaction state.
During the filtration process, the operational process of above-mentioned anti-blockage structure 24 is as follows: when starting filtering, since tubular type is made pottery
The fluid of pipeline has biggish flow velocity and impact force in porcelain film 17, when under state as shown in Figure 7, can impact spoiler
26, it after 26 stress of spoiler, can move to the direction close to material outlet 19, consolidate so that second spring 28 is compressed in second
On fixed board 34, and since protrusion 32 is connected on elastic piece 31, protrusion 31 is located at the close former of limiting card 33
The side of material outlet 19；When the first spring 27 is under normal condition (being neither stretched, the state not also being compacted), the second bullet
Spring 28 is compacted and the side of the close material outlet 19 that makes protrusion 31 be located at limiting card 33.In filter process, tubular type pottery
When the aggregation of super-cell cake layer, blocking will occur for pipe outlet side in porcelain film 17, the flow in pipeline will lead to
Reduce, therefore, fluid can also reduce the impact force of spoiler 26, and second spring 28 has the trend for restoring deformation, with pipe
Trickle further decreases in road, and protrusion 32 is more and more tightly pressed on limiting card 33 by second spring 28, due to convex
Portion 32 is mounted on elastic piece 31 out, when the trend of the recovery deformation of second spring 28 is bigger, elastic piece 31 can be made upward
It bounces, limiting card 33 cannot stop elastic piece 31 again, and second spring 28 can be hit by a bullet to the pipeline of tubular ceramic membrane 17 suddenly at this time
Out, it protrudes into the body of rod 29 into pipeline suddenly, destroys the super-cell cake layer structure to be formed, filter cake is made to become thin
Pine, since hydraulic pressure acts on, has more feed liquids and flows out from aperture, improve after the siltation in cake layer is discharged
The clearance rate of diatomite siltation；Simultaneously because second spring 28 is to be ejected from impaction state, and second spring 28 is in pressure
The first spring 27 is in normal condition, then the first spring 27 is unexpected after spoiler 26 is to pipe motion when tight state
It stretches, therefore, the first spring 27 also has the process of a reply deformation after being stretched, so that the body of rod 29 can also produce one
Towards the vibration in 19 direction of material outlet, that is to say, that the mutual linkage of the first spring 28 and second spring 28 is produced in Fig. 7
In spoiler 26 " to the right "-" to the left " coherent motion, such a movement can further make diatomite drainage
Agent cake layer is more loose, is also easier to be washed away by water flow.After water flow washes filter cake open, inside 17 pipeline of tubular ceramic membrane
Water flow can increase suddenly again, so that backward 19 side of material outlet of 26 stress of spoiler moves, since water flow pressure is larger, make
It obtains second spring 28 to be compacted again, after elastic piece 31 pops up, protrusion 31 is made to return back to the court of limiting card 33 again
To the side of material outlet 19, so that the state of Fig. 8 returns back to state as shown in FIG. 6 again.It loops back and forth like this, so that
In filter process, the end of filter just recycles as Fig. 7-Fig. 8 " blocking ", " loosening ", " a small amount of discharge ", " washes silt open
Product " moves back and forth, and solves the problems, such as that filter cake blocks filtration channel.In one embodiment, it is additionally provided on the body of rod 29
Hairbrush 30, hairbrush 30 is for breaing up cake layer；It can be further improved the effect loosened to super-cell cake layer.
Embodiment 1
Desized wastewater from different workshops is after quartz filter filters, CODCrAbout 16400 mg/L, alkali
Concentration 0.8%, concentration of refining agent 0.4%, then in waste water be added 2wt% filter aid diatomite, be sent into as Figure 6-Figure 8
It is filtered in purpose ceramic-film filter, the average pore size 200nm of ceramic membrane, sets 0.2 MPa of filter pressure, crossflow velocity 4m/
S eliminates most polyacrylate, liquor C OD in filtrateCrValue is about 6700 mg/L, alkali concentration and refining agent in clear liquid
Concentration and water inlet are consistent.Contain super-cell and polyacrylate in the concentrate of ceramic membrane, is sent into average pore size in 10 μ
It is filtered in the flame filter press of the filter cloth of m, diatomite is trapped in filter cake, is mainly polyacrylate in filtrate, is sent
Enter the reuse of desizing workshop.Diatomite is handled in the combustion chamber of air atmosphere in 200~300 DEG C of burnings, removes polyacrylate,
Obtain recycling diatomite.
Embodiment 2
Desized wastewater from different workshops is after quartz filter filters, CODCrAbout 16400 mg/L, alkali
Concentration 0.8%, concentration of refining agent 0.4%, then in waste water be added 1wt% filter aid diatomite, be sent into as Figure 6-Figure 8
It is filtered in purpose ceramic-film filter, the average pore size 50nm of ceramic membrane, sets 0.4 MPa of filter pressure, crossflow velocity 3m/s,
Most polyacrylate, liquor C OD are eliminated in filtrateCrValue is about 4200 mg/L, and alkali concentration and refining agent are dense in clear liquid
Degree is consistent with water inlet.Contain super-cell and polyacrylate in the concentrate of ceramic membrane, is sent into average pore size at 6 μm
It is filtered in the flame filter press of filter cloth, it is mainly polyacrylate in filtrate that diatomite, which is trapped in filter cake, and feeding is moved back
Starch workshop reuse.Diatomite is handled in the combustion chamber of air atmosphere in 200~300 DEG C of burnings, is removed polyacrylate, is obtained
Recycle diatomite.
Embodiment 3
Desized wastewater from different workshops is after quartz filter filters, CODCrAbout 16400 mg/L, alkali
Concentration 0.8%, concentration of refining agent 0.4%, then the filter aid diatomite of 1.5wt% is added in waste water, it is sent into as Figure 6-Figure 8
Purpose ceramic-film filter in be filtered, the average pore size 50nm of ceramic membrane, set 0.5 MPa of filter pressure, crossflow velocity 5m/
S eliminates most polyacrylate, liquor C OD in filtrateCrValue is about 4100 mg/L, alkali concentration and refining agent in clear liquid
Concentration and water inlet are consistent.Contain super-cell and polyacrylate in the concentrate of ceramic membrane, is sent into average pore size in 10 μ
It is filtered in the flame filter press of the filter cloth of m, diatomite is trapped in filter cake, is mainly polyacrylate in filtrate, is sent
Enter the reuse of desizing workshop.Diatomite is handled in the combustion chamber of air atmosphere in 200~300 DEG C of burnings, removes polyacrylate,
Obtain recycling diatomite.
Embodiment 4
Difference with embodiment 3 is: not installing anti-blockage structure 24 in tubular ceramic membrane filter.
Reference examples 1
Difference with embodiment 3 is: filter aid diatomite is not added in waste water.
The operating flux of the above filter process ceramic membrane is as shown in Fig. 2, stabilized flux is as shown in the table:
As can be seen from the above table, embodiment 3 has preferable membrane flux relative to the processing method of reference examples 1, is added
Diatomite facilitates the blocking for preventing polyacrylate slurry in film surface, due to cannot be compared in membrane filter in embodiment 4
The mixture of removal diatomite and polyacrylate are collectively formed well polymer, particulate matter, is easy to appear duct obstruction, causes
Filter damage.
Membrane cleaning effect compares:
Successively carry out alkali cleaning and acid cleaning, alkali clean the step of be: using by sodium hydroxide, sodium carboxymethylcellulose,
Sodium alkyl benzene sulfonate is cleaned according to the compound alkaline cleaner that weight ratio 4:0.4:1 is mixed, and compound alkaline cleaner is in water
Middle dosage is 3wt%, and the temperature of cleaning process is 45 DEG C, crossflow velocity 6m/s in cleaning process, scavenging period 40min；Acid cleaning
The step of be: cleaned using nitric acid, the purity of nitric acid is 65wt%, and dosage is 2wt%, the temperature of cleaning process to nitric acid in water
Degree is 44 DEG C, crossflow velocity 5m/s in cleaning process, scavenging period 30min.After over cleaning, the recovery feelings of membrane flux are calculated
Condition, as shown in figure 3, the recovery rate in embodiment 3 can achieve 85% or more, recovery rate is 75% or so in reference examples 1.
Claims (7)
1. a kind of processing method of dyeing waste water, which comprises the steps of:
Step 1 is sent into prefilter polyacrylate desized wastewater and is filtered；
Filter aid is added in the filtrate obtained in step 1 in step 2, after mixing, be sent into tubular ceramic membrane filter into
Row filtering；
Step 3, the penetrating fluid of tubular ceramic membrane filter are sent into desizing workshop as desizing liquid reuse；
Step 4, the concentrate of tubular ceramic membrane filter are sent into plate and frame filter press and extrude filter aid, the filtrate of plate and frame filter press
It is the polyacrylate slurry of recycling；
It include: assembly housing (14) in the structure of the tubular ceramic membrane filter (6), at the both ends of assembly housing (14) point
Not She You end socket (15), material inlet (18) and material outlet (19) are respectively equipped on end socket (15), in assembly housing (14)
Tubular ceramic membrane (17) are installed；The internal both ends of assembly housing (14) are equipped with floral disc (21), and pressing plate is equipped in end socket (15)
(20), the both ends of tubular ceramic membrane (17) are respectively fitted in the aperture on floral disc (21) and pressing plate (20), and pressing plate (20) is by floral disc
(21) sealing of tubular ceramic membrane (17) is realized after compressing, the pipeline in tubular ceramic membrane (17) is connected to end socket (15)；In group
Part shell (14) is additionally provided with penetrating fluid outlet (16)；Anti-blockage structure is additionally provided in the inside for the end socket for being equipped with material outlet (19)
(24), for preventing the pipeline of tubular ceramic membrane (17) from being blocked by filter cake；Anti-blockage structure (24) includes:
It is internal to be fixed on end socket (15) for first fixed plate (25)；
The side of first fixed plate (25) towards the pipeline of tubular ceramic membrane (17) is connected with spoiler by the first spring (27)
(26), the side of spoiler (26) towards the pipeline of tubular ceramic membrane (17) is equipped with the body of rod (29), and the body of rod (29) protrudes into tubular type pottery
The inside of the pipeline of porcelain film (17)；
Second fixed plate (34) is fixed on end socket (15) inside, pipeline of the second fixed plate (34) towards tubular ceramic membrane (17)
Side be connected to spoiler (26) by second spring (28), spoiler (26) towards tubular ceramic membrane (17) pipeline one
Side is additionally provided with elastic piece (31), and the side of elastic piece (31) is equipped with protrusion (32)；Limiting card is additionally provided in end socket (15)
(33), limiting card (33) is used to limit the movement of protrusion (32)；When the first spring (27) is in normal condition, second spring
(28) it is in impaction state；It is additionally provided on the body of rod (29) hairbrush (30), hairbrush (30) is for breaing up cake layer.
2. the processing method of dyeing waste water according to claim 1, which is characterized in that in the step 1, prefilter
It is quartz filter.
3. the processing method of dyeing waste water according to claim 1, which is characterized in that in the step 2, filter aid is
Diatomite, additional amount are 0.5~2wt% of waste water weight；In the step 2, the ceramic membrane in tubular ceramic membrane filter is flat
Equal pore diameter range is 50~200nm, and the crossflow velocity of filter process is 1~5m/s, and feed liquid temperature is 20~45 in filter process
DEG C, filter pressure range is 0.1~0.5MPa.
4. the processing method of dyeing waste water according to claim 1, which is characterized in that in the step 4, plate compression
The filter cake of machine is sent into burner burning processing, the diatomite recycled in air atmosphere or oxygen atmosphere.
5. the processing method of dyeing waste water according to claim 1, which is characterized in that in the step 4, plate compression
The average pore size of the filter cloth of machine is at 5~20 μm.
6. the processing method of dyeing waste water according to claim 1, which is characterized in that in the step 2, tubular ceramic
Membrane filter after filtering, needs successively to carry out alkali cleaning and acid cleaning.
7. the processing method of dyeing waste water according to claim 6, which is characterized in that the step of alkali cleans is:
It is answered using by sodium hydroxide, sodium carboxymethylcellulose, sodium alkyl benzene sulfonate according to what weight ratio 4:0.3~0.5:1~1.5 was mixed
It closes alkaline cleaner to be cleaned, dosage is 2~4wt% to compound alkaline cleaner in water, and the temperature of cleaning process is 40~50
DEG C, 4~6m/s of crossflow velocity in cleaning process, 30~60min of scavenging period；The step of acid cleans is: using nitric acid
It is cleaned, the purity of nitric acid is 40~65wt%, and dosage is 1~3wt% to nitric acid in water, and the temperature of cleaning process is 40~50
DEG C, 4~6m/s of crossflow velocity in cleaning process, 20~40min of scavenging period.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910336762.1A CN110078174A (en) | 2017-10-02 | 2017-10-02 | A kind of tubular ceramic membrane filter for wastewater treatment |
| CN201710925044.9A CN107569902B (en) | 2017-10-02 | 2017-10-02 | A kind of processing method and processing device of dyeing waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710925044.9A CN107569902B (en) | 2017-10-02 | 2017-10-02 | A kind of processing method and processing device of dyeing waste water |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910336762.1A Division CN110078174A (en) | 2017-10-02 | 2017-10-02 | A kind of tubular ceramic membrane filter for wastewater treatment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107569902A CN107569902A (en) | 2018-01-12 |
| CN107569902B true CN107569902B (en) | 2019-10-08 |
Family
ID=61040385
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710925044.9A Active CN107569902B (en) | 2017-10-02 | 2017-10-02 | A kind of processing method and processing device of dyeing waste water |
| CN201910336762.1A Withdrawn CN110078174A (en) | 2017-10-02 | 2017-10-02 | A kind of tubular ceramic membrane filter for wastewater treatment |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910336762.1A Withdrawn CN110078174A (en) | 2017-10-02 | 2017-10-02 | A kind of tubular ceramic membrane filter for wastewater treatment |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN107569902B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111661983A (en) * | 2020-06-16 | 2020-09-15 | 南京霄祥工程技术有限公司 | Municipal wastewater treatment method and system |
| CN112044593A (en) * | 2020-07-31 | 2020-12-08 | 高维川 | Epoxy mixture separation filter equipment |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101514057A (en) * | 2008-11-26 | 2009-08-26 | 浙江美欣达印染集团股份有限公司 | Method for recycling textile, printing and dyeing wastewater |
| CN203563649U (en) * | 2013-07-29 | 2014-04-30 | 中国环境科学研究院 | Turbid fruit and vegetable juice processing equipment and fruit and vegetable juice preparation device with same |
-
2017
- 2017-10-02 CN CN201710925044.9A patent/CN107569902B/en active Active
- 2017-10-02 CN CN201910336762.1A patent/CN110078174A/en not_active Withdrawn
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101514057A (en) * | 2008-11-26 | 2009-08-26 | 浙江美欣达印染集团股份有限公司 | Method for recycling textile, printing and dyeing wastewater |
| CN203563649U (en) * | 2013-07-29 | 2014-04-30 | 中国环境科学研究院 | Turbid fruit and vegetable juice processing equipment and fruit and vegetable juice preparation device with same |
Non-Patent Citations (1)
| Title |
|---|
| "微粒子辅助过滤控制膜污染";苏雪梅等;《膜科学与技术》;20130831;第33卷(第4期);第68-72页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107569902A (en) | 2018-01-12 |
| CN110078174A (en) | 2019-08-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101422700A (en) | Chemical cleaning method of ultrafiltration membrane | |
| CN107569902B (en) | A kind of processing method and processing device of dyeing waste water | |
| CN103619451A (en) | Washing method for separation membrane module | |
| CN107311391B (en) | A kind of processing method and processing device of paper waste | |
| CN1335274A (en) | Treatment method of textile printing industry effluent | |
| CN109499378B (en) | Cleaning method for organic dirt blockage of hollow fiber ultrafiltration membrane | |
| CN210457682U (en) | Cleaning system of water treatment system based on reverse osmosis membrane | |
| CN111495025A (en) | Oil product purification membrane filtration system and application process thereof | |
| CN114797483A (en) | Cleaning method and device for filtering membrane of water purification process | |
| CN214004228U (en) | Reverse osmosis water purification system for electroplating wastewater treatment | |
| CN213141656U (en) | Recycling system of main shaft cooling water | |
| CN212770173U (en) | A preliminary treatment clarification plant for domestic sewage | |
| CN212982601U (en) | Multiple water quality fresh water preparing equipment | |
| CN204259638U (en) | A kind of fish pond purifier | |
| CN204147626U (en) | A kind of mixing wastewater with air automatic backwash fiber price fixing filter | |
| CN209451656U (en) | A kind of cross-current type feed liquid filtering device | |
| CN208055051U (en) | A kind of Multistage Membranes composite filter element that water purifier uses | |
| CN220317578U (en) | Large-scale industrial water treatment reverse osmosis equipment | |
| CN219991249U (en) | Wastewater treatment device based on reverse osmosis membrane | |
| CN212334912U (en) | Paint mist waste liquid recycling production line | |
| CN204910948U (en) | Compound basket filter filter core | |
| CN217490440U (en) | Cleaning device for filtering membrane of water purification process | |
| CN217392064U (en) | Oily wastewater treatment device | |
| CN203602423U (en) | Circular ultrafiltration device capable of decontaminating deeply | |
| CN217939569U (en) | Shallow sand air filter |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20190123 Address after: 210046 18 -Q1916, Yin Chun Road, R & D base, Maigaoqiao Pioneer Park, Qixia District, Nanjing, Jiangsu Applicant after: NANJING XIAOXIANG ENGINEERING TECHNOLOGY Co.,Ltd. Address before: 210009 Dingjiaqiao Campus,Nanjing Tech University, No. 9 Xin Model Road, Gulou District, Nanjing City, Jiangsu Province Applicant before: Mao Qiangping |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20190902 Address after: Room A12-49, 4A Floor, 2300 Yangshupu Road, Yangpu District, Shanghai 200090 Applicant after: Hanyun Huafeng (Shanghai) Environmental Protection Technology Co.,Ltd. Address before: 210046 Science and Technology Research and Development Base of Maigaoqiao Pioneer Park, Qixia District, Nanjing City, Jiangsu Province, 18 Yinchun Road-Q1916 Applicant before: NANJING XIAOXIANG ENGINEERING TECHNOLOGY Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |