CN102936077A - Treatment method of polyacrylonitrile fiber production sewage - Google Patents
Treatment method of polyacrylonitrile fiber production sewage Download PDFInfo
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- CN102936077A CN102936077A CN2011102334380A CN201110233438A CN102936077A CN 102936077 A CN102936077 A CN 102936077A CN 2011102334380 A CN2011102334380 A CN 2011102334380A CN 201110233438 A CN201110233438 A CN 201110233438A CN 102936077 A CN102936077 A CN 102936077A
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- waste water
- polyacrylonitrile fibre
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- polyacrylonitrile
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- 238000000034 method Methods 0.000 title claims abstract description 120
- 229920002239 polyacrylonitrile Polymers 0.000 title claims abstract description 79
- 238000007380 fibre production Methods 0.000 title claims abstract description 26
- 239000010865 sewage Substances 0.000 title abstract description 13
- 239000002351 wastewater Substances 0.000 claims abstract description 70
- 238000006116 polymerization reaction Methods 0.000 claims abstract description 29
- 238000002156 mixing Methods 0.000 claims abstract description 18
- 239000006228 supernatant Substances 0.000 claims abstract description 14
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 230000007062 hydrolysis Effects 0.000 claims abstract description 5
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 5
- 239000000835 fiber Substances 0.000 claims description 40
- 238000004519 manufacturing process Methods 0.000 claims description 39
- 239000002699 waste material Substances 0.000 claims description 21
- 239000002904 solvent Substances 0.000 claims description 20
- 238000009987 spinning Methods 0.000 claims description 19
- 239000010802 sludge Substances 0.000 claims description 15
- 239000003795 chemical substances by application Substances 0.000 claims description 14
- 238000005189 flocculation Methods 0.000 claims description 13
- 230000016615 flocculation Effects 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 13
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 12
- 239000000413 hydrolysate Substances 0.000 claims description 11
- 230000003647 oxidation Effects 0.000 claims description 10
- 238000007254 oxidation reaction Methods 0.000 claims description 10
- 238000012163 sequencing technique Methods 0.000 claims description 7
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical group [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 5
- 229920002401 polyacrylamide Polymers 0.000 claims description 4
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 3
- 229940037003 alum Drugs 0.000 claims description 3
- KCZFLPPCFOHPNI-UHFFFAOYSA-N alumane;iron Chemical compound [AlH3].[Fe] KCZFLPPCFOHPNI-UHFFFAOYSA-N 0.000 claims description 2
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 2
- 239000011790 ferrous sulphate Substances 0.000 claims description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 2
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 2
- 229920001495 poly(sodium acrylate) polymer Polymers 0.000 claims description 2
- 229920002717 polyvinylpyridine Polymers 0.000 claims description 2
- NNMHYFLPFNGQFZ-UHFFFAOYSA-M sodium polyacrylate Chemical compound [Na+].[O-]C(=O)C=C NNMHYFLPFNGQFZ-UHFFFAOYSA-M 0.000 claims description 2
- 239000000047 product Substances 0.000 abstract description 2
- 230000003301 hydrolyzing effect Effects 0.000 abstract 1
- 238000000926 separation method Methods 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 27
- 230000000052 comparative effect Effects 0.000 description 16
- 239000000463 material Substances 0.000 description 15
- 239000010786 composite waste Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000007795 chemical reaction product Substances 0.000 description 8
- 239000008394 flocculating agent Substances 0.000 description 7
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 6
- 238000005273 aeration Methods 0.000 description 5
- 239000000945 filler Substances 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 229920000642 polymer Polymers 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 description 4
- 229920002972 Acrylic fiber Polymers 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 230000000813 microbial effect Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- -1 quaternary ammonium salt cation Chemical class 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 2
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- VGTPCRGMBIAPIM-UHFFFAOYSA-M sodium thiocyanate Chemical compound [Na+].[S-]C#N VGTPCRGMBIAPIM-UHFFFAOYSA-M 0.000 description 2
- MPDGHEJMBKOTSU-YKLVYJNSSA-N 18beta-glycyrrhetic acid Chemical compound C([C@H]1C2=CC(=O)[C@H]34)[C@@](C)(C(O)=O)CC[C@]1(C)CC[C@@]2(C)[C@]4(C)CC[C@@H]1[C@]3(C)CC[C@H](O)C1(C)C MPDGHEJMBKOTSU-YKLVYJNSSA-N 0.000 description 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 description 1
- 239000004952 Polyamide Substances 0.000 description 1
- 229920004933 Terylene® Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 150000007942 carboxylates Chemical class 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 239000013530 defoamer Substances 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 244000144992 flock Species 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000011081 inoculation Methods 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 239000005020 polyethylene terephthalate Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000002166 wet spinning Methods 0.000 description 1
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention relates to a treatment method of polyacrylonitrile fiber production sewage. The method comprises the steps of: under the conditions of a pH value of 8-12, a pressure of 0.5-3MPa, and a temperature of 100-260DEG C, hydrolyzing the wastewater A generated in a polymerization process during polyacrylonitrile fiber production, mixing the hydrolysis product with the wastewater B generated by at least one process among other processes except the polymerization process during polyacrylonitrile fiber production, subjecting the mixture to settling separation, and then conducting biochemical treatment on the separated supernatant. The method provided in the invention can treat the polyacrylonitrile fiber production sewage till meeting the discharge standards, and can significantly reduce the consumption of an additional flocculant in the treatment process.
Description
Technical field
The present invention relates to a kind for the treatment of process of polyacrylonitrile fibre production waste.
Background technology
Polyacrylonitrile fibre (commodity are called acrylic fibers) is one of principal item of synthon, and 1-10 month polyacrylonitrile fibre cumulative production in 2009 is 58.63 ten thousand tons according to statistics, accounts for 2.89% of the synthon ultimate production same period, is only second to terylene and polyamide fibre.
The polyacrylonitrile fibre production waste mainly produces the process procedures such as auto-polymerization, spinning and solvent recuperation, and the water quality complexity often contains organonitrogen and the vitriol of low-molecular(weight)polymer, high density, also has the material of quite a few difficult for biological degradation.Wherein low-molecular(weight)polymer, exist with the suspension colloidal form usually, is difficult to natural subsidence and removes, and these low-molecular(weight)polymers not only affect the normal operation of biochemical system after entering biochemical system, and have increased the load of organic matter degradation; These low-molecular(weight)polymers easily stop up filler simultaneously, reduce the specific surface area of filler, have increased the wastewater biochemical intractability.The common employing of prior art is first flocculated with except low-molecular(weight)polymer, then carries out the method for biochemical treatment and processes the polyacrylonitrile fibre production waste.For example, CN 1293159A discloses a kind of bioremediation of acrylic fibers waste water by dry process, and the method comprises: the composite flocculation agent that (1) adopts polymerize aluminum chloride and quaternary ammonium salt cation flocculation agent to form is removed the oligopolymer colloid; (2) tandem phase-splitting anaerobic digestion; (3) Anoxybiotic-aerobic biologic denitrogenation, add water-soluble carboxylate as co-substrate at aerobic section; (4) sand filtration; (5) charcoal absorption.CN1539766A discloses a kind of for the treatment of take the method for the two-step approach acrylic fibre wet spinning technique trade effluent that Sodium Thiocyanate 99 is solvent, the method comprises successively: the oligopolymer in micro-electrolysis method degraded polymerization workshop section waste water, then add flocculation agent alum, separated by coagulant precipitation; Polymerization workshop section waste water mixes homogeneous with the cyanide wastewater of spinning and solvent recuperation workshop section; Then be hydrolyzed successively that acidifying, carbonization are nitrated, denitrification, aeration separate with sludge settling.Yet the method for above-mentioned existing processing polyacrylonitrile fibre production waste all needs to use relatively large flocculation agent.
Summary of the invention
The purpose of this invention is to provide a kind for the treatment of process of new polyacrylonitrile fibre production waste, the method has higher processing efficiency, and can obviously reduce the amount of additional flocculating agents, even can be fully without additional flocculating agents.
The invention provides a kind for the treatment of process of polyacrylonitrile fibre production waste, the method comprises: be 8～12 in the pH value, pressure is under 0.5～3MPa, the temperature condition that is 100～260 ℃, the waste water A that polymerization process in the production process of polyacrylonitrile fibre is produced is hydrolyzed, the waste water B that at least one operation in other operation except polymerization process in the production process of the hydrolysate that obtains and polyacrylonitrile fibre is produced mixes, and the mixture obtained is carried out settlement separate, then isolated supernatant liquid is carried out to biochemical treatment.
Method according to the present invention, the waste water produced by the polymerization process in the production process by polyacrylonitrile fibre is hydrolyzed under given conditions, then the waste water at least one operation in other operation except polymerization process in the production process of the hydrolysate that obtains and polyacrylonitrile fibre produced mixes, carry out settlement separate, can reduce the amount of additional flocculating agents, even can be fully without additional flocculating agents; And the polyacrylonitrile fibre production waste can be processed to meeting emission standard by follow-up biochemical treatment process.
Embodiment
The treatment process of polyacrylonitrile fibre production waste according to the present invention comprises: in the pH value, be 8～12, pressure is 0.5～3MPa, under the condition that temperature is 100～260 ℃, the waste water A that polymerization process in the production process of polyacrylonitrile fibre is produced (being called for short " waste water A ") is hydrolyzed, the waste water B (being called for short " waste water B ") that at least one operation in other operation except polymerization process in the production process of the hydrolysate that obtains and polyacrylonitrile fibre is produced mixes, and undertaken settlement separate by the mixture obtained, then isolated supernatant liquid is carried out to biochemical treatment.
In the preferred case, the condition of described waste water A hydrolysis is comprised: the pH value is 10～11, and pressure is 1～2MPa, and temperature is 170～200 ℃, and the time is 1～10h.In the present invention, described pressure refers to absolute pressure.
According to described method provided by the invention, the principal pollutant in described waste water A are polyacrylonitrile, and the content of polyacrylonitrile can be 0.001～0.01 quality %.
According to described method provided by the invention, the production process of described polyacrylonitrile fibre mainly comprises polymerization process, spinning process and solvent recuperation operation usually.Therefore, in the present invention, other operation in the production process of described polyacrylonitrile fibre except polymerization process mainly comprises spinning process and solvent recuperation operation.
According to described method provided by the invention, the COD of described waste water B can be 500～1200mg/L, BOD
5Can be 100～400mg/L, NH
3-N can be 20～100mg/L.Usually, the pollutent in described waste water B is mainly to be selected from the solvent that uses in methyl acrylate (MA), methyl methacrylate (MMA), vinyl acetate (VA), spinning process (as NaSCN, dimethyl formamide (DMF), N,N-DIMETHYLACETAMIDE (DMA), acetone and HNO
3Deng) and additive (as adding blue agent, defoamer etc.) in one or more.
According to described method provided by the invention, described hydrolysate (being about to the product obtained after described waste water A hydrolysis) can be 1: 0.1～10 with the mixing quality ratio of described waste water B, be preferably 1: 0.2～and 5.
In the present invention, described method can also be included in the process that the hydrolysate by obtaining after described waste water A hydrolysis is mixed with described waste water B and add flocculation agent.In this case, with respect to the total mass of described hydrolysate and the described waste water B of 100 mass parts, the add-on of described flocculation agent can be 0.001～0.07 mass parts.
In the present invention, described flocculation agent can be the conventional various flocculation agents that use in this area, can be for example at least one in hydrate, polyaluminium sulfate, polymerize aluminum chloride, aluminium iron polychloride, polymeric aluminum sulfate silicate, polyacrylamide, sodium polyacrylate, polyvinyl pyridine and the polymine of the hydrate of Tai-Ace S 150, alum, iron trichloride, ferrous sulfate, be preferably polymerize aluminum chloride and/or polyacrylamide.
According to described method provided by the invention, the method of described biochemical treatment can, for the conventional biochemical processing method used in sewage treatment area, for example can comprise at least one in activated sludge process, biological contact oxidation process, Gas biological filter, sequencing batch reactor, anaerobic biofilter method, Anaerobic Contact method, anaerobic-anoxic-oxic method and anoxic-anaerobic-aerobic method.
In the present invention, described activated sludge process can be the conventional activated sludge process of using in this area, refer in the aeration tank of artificial oxygenation, utilize active sludge to remove the organism in sewage, then make mud and moisture from, most of mud is back to aeration tank again, and the method that remainder mud is discharged.Described active sludge be by multiple aerobic microbiological and amphimicrobe (can contain a small amount of anaerobion) and sewage organically and inorganic nitrogen solids coagulation and the flock that forms.The operational condition of described activated sludge process can comprise: temperature is 25～35 ℃, and mud age is 3～5d, and sludge loading is 0.2～0.4kg BOD
5/ (kg MLSSd), volume load is 0.3-0.6kg BOD
5/ (M
3D), suspended solids (MLSS) concentration is 1500～3000mg/L, and the treatment time is 4～8h, and reflux ratio is 0.25～0.5.In the present invention, BOD
5Refer to 5 days biochemical oxygen requirements.
In the present invention, described biological contact oxidation process can be the conventional biological contact oxidation process used in this area, to load filler in biological contact oxidation pond, utilization is adsorbed on microbial film on filler and the oxygen of ample supply, pass through biological oxidation, the pollutant oxidations such as organic amine in described filtrate are decomposed, thereby reach the method for the purpose of purification.The operational condition of described biological contact oxidation process can comprise: temperature is 25～35 ℃, and volume load is 1.0～1.8kgBOD
5/ (M
3D), the treatment time is 2～8h.
In the present invention, described Gas biological filter can be the conventional Gas biological filter used in this area, refer to the granule filter material in the in-built raising specific surface area of bio-reactor, so that the carrier of microbial film growth to be provided, and lower to stream or upward flow to being divided into according to the various flows of sewage, sewage flows through filter material layer from top to bottom or from bottom to top, in the blast aeration of filter material layer bottom, air is reverse with sewage or contact in the same way, makes organism in sewage by with the filling surface microbial film, carrying out the method that biochemical reaction is removed.The operational condition of described Gas biological filter can comprise: temperature is 25～35 ℃, and volume load is 3～6kgCOD/ (M
3D), the air water volume ratio is 1～5: 1, and the treatment time is 2～10h.In the present invention, COD refers to chemical oxygen demand (COD).
In the present invention, the sequencing batch reactor that described sequencing batch reactor can be used for this area is conventional, be a kind of active sludge water technology moved by the intermittent aeration mode, claims again sequencing batch active sludge.The operational condition of described sequencing batch reactor can comprise: temperature is 25～35 ℃, and mud age is 5～15d, and the concentration of suspended solids (MLSS) is 2000～5000mg/L, filling time is 1～4h, reaction times 2～8h, sedimentation and drawing time 2～4h, time of repose 1～3h.
In the present invention, described anaerobic biofilter method can, for the conventional anaerobic biofilter method of using in this area, be a kind of anaerobic biological treatment method, in the sealing pond of placing filler, sewage enters at the bottom of pond, discharges from Chi Ding, thereby removes organic process.The operational condition of described anaerobic biofilter method can comprise: temperature is 25～35 ℃, and volume load is 3～6kg COD/ (M
3D), treatment time 12～96h.
In the present invention, the Anaerobic Contact method that described Anaerobic Contact method can be used for this area is conventional, be also a kind of anaerobic biological treatment method, and form class is similar to activated sludge process, establishes settling tank after digester, and precipitating sludge is back to digester.The operational condition of described Anaerobic Contact method can comprise: temperature is 25～35 ℃, and volume load is 3～5kg COD/ (M
3D), treatment time 12～48h.
In the present invention, described anaerobic-anoxic-oxic method can be the conventional anaerobic-anoxic-oxic method of using in this area, refer to the technique that anaerobism, anoxic, aerobic method are combined, sewage passes through anaerobic pond, anoxic pond and Aerobic Pond successively, the technical process of being processed.The operational condition of described anaerobic-anoxic-oxic method can comprise: temperature is 25～35 ℃, and volume load is 3～8kg COD/ (M
3D), the anaerobic treatment time is 12～48h, and the anaerobic treatment time is 12～48h, and the aerobic treatment time is 4～16h.
In the present invention, described anoxic-anaerobic-aerobic method can be the conventional anoxic of using in this area-anaerobic-aerobic method, refer to the technique that anaerobism, anoxic, aerobic method are combined, sewage passes through anoxic pond, anaerobic pond and Aerobic Pond successively, the technical process of being processed.The operational condition of described anoxic-anaerobic-aerobic method can comprise: temperature is 25～35 ℃, and volume load is 3～8kg COD/ (M
3D), the anaerobic treatment time is 12～48h, and the anaerobic treatment time is 12～48h, and the aerobic treatment time is 4～16h.
With Comparative Examples, the invention will be further described by the following examples.
In the following Examples and Comparative Examples, the BOD in the reuse water obtained after treatment
5Adopt GB7488-87 dilution and inoculation method to measure; COD measures according to the catalysis Quick Oxidation method in " water and effluent monitoring analytical procedure guide (middle volume) "; Ammonia nitrogen (NH
3-N) refer in water with free state (NH
3) or ammonium salt (NH
4 +) nitrogenous compound that exists of form, NH
3-N content adopts GB7479-87 nessler reagent spectrphotometric method for measuring; The water quality of the reuse water obtained is after treatment evaluated according to integrated wastewater discharge standard GB8978-1996, wherein, in GB8978-1996, stipulates: BOD
5First discharge standard be 20mg/L, the primary standard of COD is 100mg/L, NH
3The first discharge standard of-N is 15mg/L.
Embodiment 1
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.009 quality %) passes in retort, pH regulator to 9 by the material in retort, it is 170 ℃ that temperature is controlled, pressure-controlling is 1MPa, and keeps the about 3h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 781mg/L, BOD
5For 280mg/L, NH
3-N is 60mg/L) take mass ratio and mixed as 1: 1, after evenly mixing, by the standing 1h of the mixture obtained.Adopt afterwards activated sludge process that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 35 ℃, and mud age is 3 days, and sludge loading is 0.3kg BOD
5/ (kg MLSSd), volume load is 0.4kg BOD
5/ (M
3D), suspended solids (MLSS) concentration is 1500mg/L, and the treatment time is 8h, and reflux ratio is 0.40.By mensuration, learn, the COD in the reuse water obtained after processing is 80mg/L, BOD
5For 20mg/L, NH
3-N is 12mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Comparative Examples 1
(COD is 781mg/L to the waste water that spinning process in the production process of the waste water directly polymerization process in the production process of polyacrylonitrile fibre produced (containing the polyacrylonitrile of 0.009 quality %) and polyacrylonitrile fibre and solvent recuperation operation produce, BOD
5For 280mg/L, NH
3-N is 60mg/L) take mass ratio and mixed as 1: 1, then according to the method for embodiment 1, the composite waste obtained is carried out to biochemical treatment.By mensuration, learn, the COD in the reuse water obtained after processing is 120mg/L, BOD
5For 30mg/L, NH
3-N is 20mg/L, does not meet the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Comparative Examples 2
(COD is 781mg/L to the waste water that spinning process in the production process of the waste water directly polymerization process in the production process of polyacrylonitrile fibre produced (containing the polyacrylonitrile of 0.009 quality %) and polyacrylonitrile fibre and solvent recuperation operation produce, BOD
5For 280mg/L, NH
3-N is 60mg/L) take mass ratio and mixed as 1: 1, afterwards with respect to the composite waste obtained of 100 mass parts, in described composite waste, add the polyacrylamide of 0.1 mass parts (purchased from Beijing Hengju Chemical Group Co., Ltd company, trade mark HENGFLOC 70008), and standing 1h, then according to the method for embodiment 1, the supernatant liquid obtained after standing is carried out to biochemical treatment.By mensuration, learn, the COD in the reuse water obtained after processing is 100mg/L, BOD
5For 20mg/L, NH
3-N is 15mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
By embodiment 1 is compared and can find out with Comparative Examples 1, biochemical treatment is carried out in the waste water mixing that spinning process in the waste water directly polymerization process in the production process of described polyacrylonitrile fibre produced and the production process of described polyacrylonitrile fibre and solvent recuperation operation produce, the reuse water obtained does not meet emission standard, and method according to the present invention, the waste water produced by the polymerization process in the production process by described polyacrylonitrile fibre first is hydrolyzed under certain conditions, then after mixing, the waste water produced with spinning process in the production process of described polyacrylonitrile fibre and solvent recuperation operation carries out biochemical treatment, can be by wastewater treatment to meeting emission standard.
By embodiment 1 is compared and can find out with Comparative Examples 2, although also composite waste can be processed to meeting emission standard in Comparative Examples 2, but need additionally to use flocculation agent in Comparative Examples 2, and be better than according to the water quality that the method for embodiment 1 obtains reuse water the reuse water that the method according to Comparative Examples 2 obtains.As can be seen here, the method for embodiment 1 has the effect of processing preferably the polyacrylonitrile fibre production waste, and has saved the cost of additional flocculating agents with respect to Comparative Examples 2.
Embodiment 2
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.001 quality %) passes in retort, pH regulator to 8 by the material in retort, it is 200 ℃ that temperature is controlled, pressure-controlling is 2MPa, and keeps the about 5h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 1030mg/L, BOD
5For 370mg/L, NH
3-N is 50mg/L) take mass ratio and mixed as 1: 2, and to the polymerize aluminum chloride (purchased from Gongyi City natural resources water-purifying material company limited) that adds 0.05 mass parts in the composite waste obtained after the described mixing of 100 mass parts, after evenly mixing, by the standing 0.5h of the mixture obtained.Adopt afterwards biological contact oxidation process that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 25 ℃, and volume load is 1.5kg BOD
5/ (M
3D), the treatment time is 5h.By mensuration, learn, the COD in the reuse water obtained after processing is 70mg/L, BOD
5For 15mg/L, NH
3-N is 10mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Comparative Examples 3
(COD is 1030mg/L to the waste water that spinning process in the production process of the waste water directly polymerization process in the production process of polyacrylonitrile fibre produced (containing the polyacrylonitrile of 0.001 quality %) and polyacrylonitrile fibre and solvent recuperation operation produce, BOD
5For 370mg/L, NH
3-N is 50mg/L) take mass ratio and mixed as 1: 2, afterwards with respect to the composite waste obtained of 100 weight parts, to the polymerize aluminum chloride (purchased from Gongyi City natural resources water-purifying material company limited) that adds 0.1 mass parts in described composite waste, and standing 0.5h, then according to the method for embodiment 2, the supernatant liquid obtained after standing is carried out to biochemical treatment.By mensuration, learn, the COD in the reuse water obtained after processing is 90mg/L, BOD
5For 20mg/L, NH
3-N is 14mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
By embodiment 2 is compared and can find out with Comparative Examples 3, although also composite waste can be processed to meeting emission standard in Comparative Examples 3, but in Comparative Examples 3, the amount of the extra flocculation agent used obviously is greater than embodiment 2, and be better than according to the water quality that the method for embodiment 2 obtains reuse water the reuse water that the method according to Comparative Examples 3 obtains.As can be seen here, the method for embodiment 2 has the effect of processing preferably the polyacrylonitrile fibre production waste, and has obviously reduced the consumption of additional flocculating agents with respect to Comparative Examples 3.
Embodiment 3
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.002 quality %) passes in retort, pH regulator to 10 by the material in retort, it is 190 ℃ that temperature is controlled, pressure-controlling is 0.5MPa, and keeps the about 8h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 568mg/L, BOD
5For 150mg/L, NH
3-N is 34mg/L) take mass ratio and mixed as 1: 5, and to the polyaluminium sulfate (purchased from Gongyi City flourishing age water-purifying material company limited) that adds 0.03 mass parts in the composite waste obtained after the described mixing of 100 mass parts, after evenly mixing, by the standing 2h of the mixture obtained.Adopt afterwards the anaerobic biofilter method that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 35 ℃, and volume load is 4kg COD/ (M
3D), the treatment time is 72h.By mensuration, learn, the COD in the reuse water obtained after processing is 90mg/L, BOD
5For 20mg/L, NH
3-N is 12mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Embodiment 4
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.01 quality %) passes in retort, pH regulator to 12 by the material in retort, it is 180 ℃ that temperature is controlled, pressure-controlling is 1.5MPa, and keeps the about 10h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 800mg/L, BOD
5For 320mg/L, NH
3-N is 60mg/L) take mass ratio and mixed as 1: 0.5, after evenly mixing, by the standing 1.5h of the mixture obtained.Adopt afterwards Gas biological filter that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 25 ℃, and volume load is 3kg COD/ (M
3D), the air water volume ratio is 3: 1, and the treatment time is 8h.By mensuration, learn, the COD in the reuse water obtained after processing is 70mg/L, BOD
5For 10mg/L, NH
3-N is 10mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Embodiment 5
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.002 quality %) passes in retort, pH regulator to 11 by the material in retort, it is 100 ℃ that temperature is controlled, pressure-controlling is 2.5MPa, and keeps the about 1h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 905mg/L, BOD
5For 380mg/L, NH
3-N is 80mg/L) take mass ratio and mixed as 1: 4, and to the polymine (purchased from the Shanghai safe chemical industry of gold trade company limited) that adds 0.07 mass parts in the composite waste obtained after the described mixing of 100 mass parts, after evenly mixing, by the standing 1h of the mixture obtained.Adopt afterwards the anaerobic-anoxic-oxic method that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 35 ℃, and volume load is 8kg COD/ (M
3D), the anaerobic treatment time is 36h, and the anaerobic treatment time is 24h, and the aerobic treatment time is 16h.By mensuration, learn, the COD in the reuse water obtained after processing is 75mg/L, BOD
5For 18mg/L, NH
3-N is 14mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Embodiment 6
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.007 quality %) passes in retort, pH regulator to 10 by the material in retort, it is 200 ℃ that temperature is controlled, pressure-controlling is 2MPa, and keeps the about 4h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 630mg/L, BOD
5For 260mg/L, NH
3-N is 50mg/L) take mass ratio and mixed as 1: 0.2, after evenly mixing, by the standing 2h of the mixture obtained.Adopt afterwards sequencing batch reactor that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 35 ℃, mud age is 10 days, suspended solids (MLSS) concentration is 3000mg/L, filling time 2h, reaction times is 6h, and the sedimentation and drawing time is 3h, and time of repose is 2h.By mensuration, learn, the COD in the reuse water obtained after processing is 95mg/L, BOD
5For 20mg/L, NH
3-N is 13mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Embodiment 7
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.005 quality %) passes in retort, pH regulator to 9 by the material in retort, it is 260 ℃ that temperature is controlled, pressure-controlling is 1MPa, and keeps the about 3h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 550mg/L, BOD
5For 170mg/L, NH
3-N is 30mg/L) take mass ratio and mixed as 1: 3, and to the polymeric aluminum sulfate silicate (purchased from Vad, Jintan City chemical company limited of dragon) that adds 0.01 mass parts in the composite waste obtained after the described mixing of 100 mass parts, after evenly mixing, by the standing 2h of the mixture obtained.Adopt afterwards anoxic-anaerobic-aerobic method that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 30 ℃, and volume load is 6kg COD/ (M
3D), the anaerobic treatment time is 40h, and the anaerobic treatment time is 32h, and the aerobic treatment time is 8h.By mensuration, learn, the COD in the reuse water obtained after processing is 60mg/L, BOD
5For 10mg/L, NH
3-N is 11mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
Embodiment 8
The present embodiment is for illustrating the treatment process of described polyacrylonitrile fibre production waste of the present invention.
The waste water that polymerization process in the production process of polyacrylonitrile fibre is produced (containing the polyacrylonitrile of 0.004 quality %) passes in retort, pH regulator to 11 by the material in retort, it is 140 ℃ that temperature is controlled, pressure-controlling is 3MPa, and keeps the about 5h of reaction under this temperature and pressure.Then, by the waste water of the spinning process in the production process of the reaction product in retort and polyacrylonitrile fibre and the generation of solvent recuperation operation, (COD is 720mg/L, BOD
5For 300mg/L, NH
3-N is 45mg/L) take mass ratio and mixed as 1: 0.7, after evenly mixing, by the standing 1.5h of the mixture obtained.Adopt afterwards the Anaerobic Contact method that the supernatant liquid obtained after standing is carried out to biochemical treatment, concrete operational condition comprises: temperature is 30 ℃, and volume load is 5kg COD/ (M
3D), the treatment time is 30h.By mensuration, learn, the COD in the reuse water obtained after processing is 70mg/L, BOD
5For 15mg/L, NH
3-N is 13mg/L, meets the first discharge standard of stipulating in integrated wastewater discharge standard GB8978-1996.
As can be seen here, the polyacrylonitrile fibre production waste can be processed to meeting emission standard according to described method provided by the invention, and can significantly be reduced the consumption of additional flocculating agents in treating processes.
Claims (11)
1. the treatment process of a polyacrylonitrile fibre production waste, the method comprises: be 8～12 in the pH value, pressure is under 0.5～3MPa, the temperature condition that is 100～260 ℃, the waste water A that polymerization process in the production process of polyacrylonitrile fibre is produced is hydrolyzed, the waste water B that at least one operation in other operation except polymerization process in the production process of the hydrolysate that obtains and polyacrylonitrile fibre is produced mixes, and the mixture obtained is carried out settlement separate, then isolated supernatant liquid is carried out to biochemical treatment.
2. method according to claim 1, wherein, the condition of described hydrolysis comprises: the pH value is 10～11, and pressure is 1～2MPa, and temperature is 170～200 ℃, and the time is 1～10h.
3. method according to claim 1, wherein, described hydrolysate is 1: 0.1～10 with the mixing quality ratio of described waste water B.
4. method according to claim 3, wherein, described hydrolysate is 1: 0.2～5 with the mixing quality ratio of described waste water B.
5. according to the described method of claim 3 or 4, wherein, described method also is included in the process that described hydrolysate is mixed with described waste water B and adds flocculation agent.
6. method according to claim 5, wherein, with respect to the total mass of described hydrolysate and the waste water B of 100 mass parts, the add-on of described flocculation agent is 0.001～0.07 mass parts.
7. method according to claim 5, wherein, at least one in the hydrate that described flocculation agent is Tai-Ace S 150, alum, iron trichloride, hydrate, polyaluminium sulfate, polymerize aluminum chloride, aluminium iron polychloride, polymeric aluminum sulfate silicate, polyacrylamide, sodium polyacrylate, polyvinyl pyridine and the polymine of ferrous sulfate.
8. method according to claim 1, wherein, the method for described biochemical treatment is at least one in activated sludge process, biological contact oxidation process, Gas biological filter, sequencing batch reactor, anaerobic biofilter method, Anaerobic Contact method, anaerobic-anoxic-oxic method and anoxic-anaerobic-aerobic method.
9. method according to claim 1, wherein, the polyacrylonitrile that described waste water A contains 0.001～0.1 quality %.
10. method according to claim 1, wherein, other operation in the production process of described polyacrylonitrile fibre except polymerization process comprises spinning process and solvent recuperation operation.
11., according to the described method of claim 1 or 10, wherein, the COD of described waste water B is 500～1200mg/L, BOD
5Be 100～400mg/L, NH
3-N is 20～100mg/L.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103641277A (en) * | 2013-12-12 | 2014-03-19 | 中石化上海工程有限公司 | Acrylonitrile waste water treatment method |
| CN105557582A (en) * | 2015-12-24 | 2016-05-11 | 常州王者青城生态观光有限公司 | Green aquaculture method |
| CN106188359A (en) * | 2016-07-08 | 2016-12-07 | 中国石油化工股份有限公司 | The Application way of organic resource in a kind of Wastewater from Acrylonitrile Production |
| CN110498562A (en) * | 2019-08-08 | 2019-11-26 | 苏州苏净环保工程有限公司 | Treatment method of high-concentration stripping liquid wastewater |
| CN113562894A (en) * | 2021-08-20 | 2021-10-29 | 桂林南药股份有限公司 | Treatment method and treatment system for DMF (dimethyl formamide) wastewater and DMSO (dimethyl sulfoxide) wastewater |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1385380A (en) * | 2001-05-11 | 2002-12-18 | 中国石油化工股份有限公司 | Method for treating acrylonitrile and acrylic waste water |
| CN1539766A (en) * | 2003-04-23 | 2004-10-27 | 中国石化上海石油化工股份有限公司 | Method for treating wastewater from industry of spinning acrylics thrugh two steps wet processes by using sodium thiocyanate as solvent |
| KR100541467B1 (en) * | 2004-04-27 | 2006-01-11 | 서희동 | Biological treatment of sewage and wastewater by small grouping of water molecules |
| CN101423312A (en) * | 2007-10-31 | 2009-05-06 | 中国石油化工股份有限公司 | Acrylon production waste water treatment method |
-
2011
- 2011-08-15 CN CN201110233438.0A patent/CN102936077B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1385380A (en) * | 2001-05-11 | 2002-12-18 | 中国石油化工股份有限公司 | Method for treating acrylonitrile and acrylic waste water |
| CN1539766A (en) * | 2003-04-23 | 2004-10-27 | 中国石化上海石油化工股份有限公司 | Method for treating wastewater from industry of spinning acrylics thrugh two steps wet processes by using sodium thiocyanate as solvent |
| KR100541467B1 (en) * | 2004-04-27 | 2006-01-11 | 서희동 | Biological treatment of sewage and wastewater by small grouping of water molecules |
| CN101423312A (en) * | 2007-10-31 | 2009-05-06 | 中国石油化工股份有限公司 | Acrylon production waste water treatment method |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103641277A (en) * | 2013-12-12 | 2014-03-19 | 中石化上海工程有限公司 | Acrylonitrile waste water treatment method |
| CN103641277B (en) * | 2013-12-12 | 2015-05-27 | 中石化上海工程有限公司 | Acrylonitrile waste water treatment method |
| CN105557582A (en) * | 2015-12-24 | 2016-05-11 | 常州王者青城生态观光有限公司 | Green aquaculture method |
| CN106188359A (en) * | 2016-07-08 | 2016-12-07 | 中国石油化工股份有限公司 | The Application way of organic resource in a kind of Wastewater from Acrylonitrile Production |
| CN110498562A (en) * | 2019-08-08 | 2019-11-26 | 苏州苏净环保工程有限公司 | Treatment method of high-concentration stripping liquid wastewater |
| CN110498562B (en) * | 2019-08-08 | 2022-05-13 | 苏州苏净环保工程有限公司 | Treatment method of high-concentration stripping liquid wastewater |
| CN113562894A (en) * | 2021-08-20 | 2021-10-29 | 桂林南药股份有限公司 | Treatment method and treatment system for DMF (dimethyl formamide) wastewater and DMSO (dimethyl sulfoxide) wastewater |
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