CN112624490B - System and process for treating wastewater generated by oxidizing tert-butyl alcohol into methacrylic acid in chemical plant - Google Patents
System and process for treating wastewater generated by oxidizing tert-butyl alcohol into methacrylic acid in chemical plant Download PDFInfo
- Publication number
- CN112624490B CN112624490B CN202011233022.4A CN202011233022A CN112624490B CN 112624490 B CN112624490 B CN 112624490B CN 202011233022 A CN202011233022 A CN 202011233022A CN 112624490 B CN112624490 B CN 112624490B
- Authority
- CN
- China
- Prior art keywords
- adsorption
- net
- tank
- water
- wastewater
- 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
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 239000002351 wastewater Substances 0.000 title claims abstract description 61
- 239000000126 substance Substances 0.000 title claims abstract description 53
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 33
- 230000001590 oxidative effect Effects 0.000 title claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000012528 membrane Substances 0.000 claims abstract description 91
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 50
- 238000001035 drying Methods 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 244000005700 microbiome Species 0.000 claims abstract description 37
- 238000001704 evaporation Methods 0.000 claims abstract description 25
- 230000008020 evaporation Effects 0.000 claims abstract description 23
- 239000012153 distilled water Substances 0.000 claims abstract description 20
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 16
- 238000001556 precipitation Methods 0.000 claims abstract description 14
- 239000000945 filler Substances 0.000 claims abstract description 13
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 13
- 239000007787 solid Chemical group 0.000 claims abstract description 9
- 238000005374 membrane filtration Methods 0.000 claims abstract description 7
- 230000018044 dehydration Effects 0.000 claims abstract description 3
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 3
- 238000001179 sorption measurement Methods 0.000 claims description 139
- 239000007788 liquid Substances 0.000 claims description 56
- 239000000843 powder Substances 0.000 claims description 48
- 238000004062 sedimentation Methods 0.000 claims description 46
- 241000196324 Embryophyta Species 0.000 claims description 36
- 238000002347 injection Methods 0.000 claims description 28
- 239000007924 injection Substances 0.000 claims description 28
- 241000894006 Bacteria Species 0.000 claims description 26
- 238000012856 packing Methods 0.000 claims description 25
- 239000010802 sludge Substances 0.000 claims description 25
- 238000005192 partition Methods 0.000 claims description 24
- 238000004821 distillation Methods 0.000 claims description 20
- 238000011049 filling Methods 0.000 claims description 20
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 18
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 18
- 239000000084 colloidal system Substances 0.000 claims description 18
- 239000000243 solution Substances 0.000 claims description 18
- 238000011010 flushing procedure Methods 0.000 claims description 17
- 239000002245 particle Substances 0.000 claims description 16
- 229910002651 NO3 Inorganic materials 0.000 claims description 14
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 10
- 229910052760 oxygen Inorganic materials 0.000 claims description 10
- 239000002893 slag Substances 0.000 claims description 10
- 230000003647 oxidation Effects 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 8
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 7
- 229930195729 fatty acid Natural products 0.000 claims description 7
- 239000000194 fatty acid Substances 0.000 claims description 7
- 150000004665 fatty acids Chemical class 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 7
- 239000002184 metal Substances 0.000 claims description 7
- 238000007789 sealing Methods 0.000 claims description 7
- 150000001413 amino acids Chemical class 0.000 claims description 6
- 238000007664 blowing Methods 0.000 claims description 6
- 150000004676 glycans Chemical class 0.000 claims description 6
- 150000002772 monosaccharides Chemical class 0.000 claims description 6
- 238000006396 nitration reaction Methods 0.000 claims description 6
- 150000007524 organic acids Chemical class 0.000 claims description 6
- 229920001282 polysaccharide Polymers 0.000 claims description 6
- 239000005017 polysaccharide Substances 0.000 claims description 6
- 102000004169 proteins and genes Human genes 0.000 claims description 6
- 108090000623 proteins and genes Proteins 0.000 claims description 6
- 239000013049 sediment Substances 0.000 claims description 6
- 230000001112 coagulating effect Effects 0.000 claims description 4
- 238000003756 stirring Methods 0.000 claims description 4
- 210000002268 wool Anatomy 0.000 claims description 4
- 239000003818 cinder Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 230000001568 sexual effect Effects 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 239000003245 coal Substances 0.000 claims description 2
- 239000008213 purified water Substances 0.000 claims description 2
- 235000005985 organic acids Nutrition 0.000 claims 1
- 239000012141 concentrate Substances 0.000 abstract 3
- 230000015556 catabolic process Effects 0.000 abstract 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 9
- 230000001546 nitrifying effect Effects 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 239000002699 waste material Substances 0.000 description 6
- 239000002912 waste gas Substances 0.000 description 5
- 238000005273 aeration Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N Hydroquinone Chemical compound OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 2
- 241001148470 aerobic bacillus Species 0.000 description 2
- 150000001720 carbohydrates Chemical class 0.000 description 2
- 235000014633 carbohydrates Nutrition 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- PTPLXVHPKMTVIW-FPLPWBNLSA-N (Z)-hydroxyimino-oxido-phenylazanium Chemical compound O\N=[N+](/[O-])c1ccccc1 PTPLXVHPKMTVIW-FPLPWBNLSA-N 0.000 description 1
- PQJUJGAVDBINPI-UHFFFAOYSA-N 9H-thioxanthene Chemical compound C1=CC=C2CC3=CC=CC=C3SC2=C1 PQJUJGAVDBINPI-UHFFFAOYSA-N 0.000 description 1
- 241000193830 Bacillus <bacterium> Species 0.000 description 1
- 241001478240 Coccus Species 0.000 description 1
- 241000589989 Helicobacter Species 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 1
- 241000612652 Spirobacillus Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 230000004099 anaerobic respiration Effects 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000003851 biochemical process Effects 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 230000000802 nitrating effect Effects 0.000 description 1
- 150000002826 nitrites Chemical class 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000009935 nitrosation Effects 0.000 description 1
- 238000007034 nitrosation reaction Methods 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 230000000644 propagated effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 238000007738 vacuum evaporation Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
Abstract
The invention relates to the technical field of wastewater treatment, in particular to a system and a process for oxidizing tertiary butanol into methacrylic acid wastewater in a chemical plant, wherein the system comprises a precipitation system, an A/O water treatment system, a membrane filtration system, an evaporation system and an evaporation drying system, wherein the A/O water treatment system is provided with a reaction tank, a filler which is a microorganism is arranged in the reaction tank, the membrane filtration system comprises an ultrafiltration membrane device and a reverse osmosis membrane device, the evaporation system is provided with a separator, a heat exchanger and a circulating pump, membrane concentrate is sucked from the lower part of the separator by the circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrate, and the membrane concentrate flows in the heat exchanger from bottom to top; and (3) carrying out circulating dehydration, concentration and drying on the concentrated solution by an evaporation and drying system to obtain distilled water and solid residues. The invention is not easy to cause the phenomenon that the breakdown failure of the treatment system can not reach the emission standard, and the treated effluent meets the emission requirement.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a system and a process for treating wastewater from oxidizing tert-butanol into methacrylic acid in a chemical plant.
Background
The high concentration waste water produced in the process of oxidizing tert-butanol into methacrylic acid in chemical plant contains molybdenum, arsenic, ammonia nitrogen, methanol, toluene, diethanolamine, thioxanthene, hydroquinone, p-azodiphenylamine, 4-dimethyl-6-tert-butylphenol, polyalkylsiloxane, nitrosophenylhydroxylamine, etc. and has COD concentration as high as 10000-100000 mg/L, pungent smell, conductivity as high as 6000-50000 mu S/cm, and great amount of suspended particles or floccules dispersed in different liquid depths, long settling time and high treatment difficulty.
In the prior art, a second generation anaerobic technology is generally used for treatment, percolate enters an up-flow anaerobic sludge bed reactor firstly after pretreatment, and anaerobic effluent enters an A/O system after treatment by the up-flow anaerobic sludge bed reactor. The aerobic technology of the A/O system is widely used for treating high ammonia nitrogen wastewater at present, and is also a core treatment unit, after the treatment of the A/O system, the aerobic effluent enters an external tubular ultrafiltration system to be used as a pretreatment measure of an advanced treatment system. After the treatment of the external tubular ultrafiltration system, the ultrafiltration effluent enters an advanced treatment system, namely a reverse osmosis filtration system. However, the typical biological process (anaerobic + aerobic) +membrane process (ultrafiltration + reverse osmosis) percolate treatment chemical plant tertiary butanol oxidation to high concentration wastewater generated during methacrylic acid production process still has the following disadvantages:
1. the sedimentation time in the sedimentation tank is long, the treatment efficiency is low, and only a sedimentation tank with larger volume can be used for storing water, but waste gas with the concentration exceeding the environmental protection standard is easily generated by long-time sedimentation, and the waste gas needs to be treated;
2. the front settlement is incomplete, so that a membrane system is easy to block and lose efficacy and difficult to clean, and the membrane system needs to be cleaned and replaced by frequent shutdown;
based on the defects, the existing wastewater treatment technology is used for treating high-concentration wastewater generated in the process of oxidizing tert-butanol in a chemical plant into methacrylic acid production process, so that a treatment system is easy to collapse and lose effectiveness, the emission standard cannot be met, and the treated residual toxic and harmful substances cause serious environmental pollution.
Disclosure of Invention
The invention aims to provide a system and a process for treating wastewater from oxidizing tert-butanol into methacrylic acid in a chemical plant, aiming at overcoming the defects in the prior art.
In order to achieve the above object, the chemical plant tert-butanol oxidation to methacrylic acid wastewater treatment system of the present invention comprises: the sedimentation system is provided with a sedimentation tank, a powder injector and a circulating adsorption device, wastewater entering the sedimentation tank is subjected to coagulating sedimentation reaction, slag removal, CODcr, BOD and colloid are carried out on the wastewater, and liquid and sediment muddy water after sedimentation treatment are obtained; the sedimentation tank is provided with a net inlet tank, an adsorption tank, a net outlet tank and a liquid inlet; the net inlet pool and the net outlet pool are positioned at two ends of the adsorption pool, the net inlet pool and the net outlet pool are respectively communicated with two ends of the bottom of the adsorption pool, and the liquid inlet is used for conveying wastewater to the net inlet pool; the powder injector is used for spraying magnetic adsorption powder above the liquid level of the wastewater in the adsorption tank; the powder injector is provided with a plastic box filled with magnetic adsorption powder; the circulating adsorption device is provided with a flexible adsorption net capable of adsorbing magnetic adsorption powder, a circulating power device for driving the flexible adsorption net to move, a drying device for drying sludge on the flexible adsorption net and a vibrating mesh screen for removing the sludge from the flexible adsorption net; the flexible adsorption net is annular, and sequentially passes through the net inlet pool, the adsorption pool, the net outlet pool, the drying device and the vibration mesh screen along the moving direction of the flexible adsorption net;
the A/O water treatment system is provided with a reaction tank, a filler containing microorganisms is arranged in the reaction tank, polysaccharide substances in the liquid after precipitation treatment are decomposed into monosaccharide or organic acid by utilizing the microorganisms, protein is decomposed into amino acid, fat substances are decomposed into fatty acid and glycerol, and simultaneously, nitration reaction is carried out to obtain film-entering liquid; the organic matters which are difficult to biodegrade are degraded into biochemical organic matters, so that the biodegradability of the wastewater is improved, and the organic load of the subsequent aerobic section is reduced.
The membrane filtration system comprises an ultrafiltration membrane device and a reverse osmosis membrane device; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water; separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device;
the evaporation system is provided with a separator, a heat exchanger and a circulating pump, wherein the membrane concentrated water is sucked from the lower part of the separator by the circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrated solution, and the membrane concentrated water flows in the heat exchanger from bottom to top at a flow rate of 2.5-3.5 m/s;
and the evaporation drying system is used for circularly dehydrating, concentrating and drying the concentrated solution to obtain distilled water and solid residues.
Further, the sedimentation tank is internally provided with an inclined pipeline, the pipeline is internally provided with a filler, and the surface hydraulic load of the pipeline is 1.0-1.2 m 3 /(m 2 ·h)。
Further, a dynamic filling device is arranged in the reaction tank, the dynamic filling device is provided with a contact cabin, a feed inlet, a discharge outlet and a pressure device, the filling is pushed into the contact cabin by the pressure device through the feed inlet, and the filling at the discharge outlet is pushed out of the contact cabin; a packing cavity is arranged in the contact cabin, a contact window is arranged on the wall of the contact cabin, and packing in the packing cavity is contacted with liquid in the reaction tank through the contact window; the contact chamber is suspended in the reaction tank.
Further, the contact cabin is provided with a cabin door for closing the contact window; the dynamic filling devices are arranged in parallel, and the filling directions of two adjacent dynamic filling devices are reversely arranged.
Further, the ultrafiltration membrane device comprises a flushing cabin, an ultrafiltration membrane component and two openable and closable sealing doors, wherein the ultrafiltration membrane component is provided with an ultrafiltration membrane, the ultrafiltration membrane component is replaceable and inserted into the flushing cabin, the two sealing doors are arranged on two sides of the ultrafiltration membrane component, the upper end part and the lower end part of the flushing cabin are respectively provided with a high-pressure injection nozzle, and the high-pressure injection nozzles are used for injecting purified water containing oxygen into the ultrafiltration membrane component to flush the ultrafiltration membrane.
Further, the evaporation drying system is provided with a distillation kettle, a stirrer, a condenser, a vacuum pump and a buffer water tank, wherein the stirrer is used for stirring concentrated solution in the distillation kettle, and the distillation kettle, the condenser and the vacuum pump are sequentially connected in a conducting way; distilled water reacted in the distillation kettle is condensed by the condenser and then pumped into the buffer water tank by the vacuum pump, and the distillation kettle is in a negative pressure state.
Further, the powder injector further comprises an injection pipe, an electromagnetic valve and an air compressor, wherein a horn-shaped injection nozzle with an upward opening is arranged at one end of the injection pipe, an inverted conical diffuser is arranged in the middle of the injection nozzle, the distance between the diffuser and the horn-shaped injection nozzle is sequentially increased from top to bottom, the other end of the injection pipe is communicated with the air compressor through the electromagnetic valve, a plastic box is arranged above the injection pipe and is communicated with the middle of the injection pipe, and the air compressor is used for pressurizing the injection pipe.
Further, a plurality of alternately arranged upper through partition plates and lower through partition plates are arranged in the adsorption tank, a through hole is formed in the upper end portion of each upper through partition plate, a through hole is formed between the lower end portion of each lower through partition plate and the tank bottom of the adsorption tank, and rotatable plastic corner rollers are arranged at the upper end portion of each upper through partition plate and the included angle between each upper through partition plate and the adsorption tank, so that the flexible adsorption net is attached to the upper through partition plates and the tank bottom of the adsorption tank.
Further, the upper through partition plate is provided with a through hole, the flexible adsorption net is formed by sequentially sleeving and buckling a plurality of metal rings, and each metal ring is bound with adsorption Mao Sheng; the diameter of the passing hole is 1.5-2 times of the diameter of the mesh of the flexible adsorption net; the diameter of the mesh of the flexible adsorption net is a millimeter, the conductivity of the wastewater entering the sedimentation tank is b mu S/cm, the particle size of the magnetic adsorption powder is c millimeter, the length and the diameter of the adsorption wool rope are d millimeter and e millimeter respectively, and the following mathematical relationship exists between a, b, c, d, e: a=c=b=e, where c is 1 to 3,e and 0.5 to 2.
Another object of the present invention is to provide a process for treating wastewater from the oxidation of t-butanol to methacrylic acid in a chemical plant, using the wastewater treatment system of the present invention, comprising the steps of: the circulating power device drives the flexible adsorption net to sequentially pass through the net inlet pool, the adsorption pool, the net outlet pool, the drying device and the vibration mesh screen, and then the flexible adsorption net is recycled into the net inlet pool; the waste water firstly enters the net inlet tank through the liquid inlet, and enters the adsorption tank through the bottom of the net inlet tank, the powder injector sprays sand to the upper part of the waste water liquid level in the adsorption tank at regular time to adsorb powder, and the adsorption powder can be magnetic adsorption powder or a mixture of the magnetic adsorption powder and coal cinder powder; slag removal, CODcr, BOD and colloid are carried out in an adsorption tank, and liquid after precipitation treatment is obtained; the adsorption powder adsorbs colloid, floccules and slag, then sinks to be adsorbed by the flexible adsorption net and moves along with the adsorption net; the adsorption net brings the sludge out of the sedimentation tank and then enters a drying device, the sludge is dried in the drying device and then adhered to the sexual adsorption net, and the dried sludge in the vibration mesh screen is separated from the adsorption net; the device also comprises a blowing device for blowing away the sludge on the adsorption net before entering the net pond;
the reaction tank is internally provided with a filler for retaining microorganisms, the microorganisms are utilized to decompose polysaccharide substances in the liquid after the precipitation treatment into monosaccharide or organic acid, protein is decomposed into amino acid, fat substances are decomposed into fatty acid and glycerol, and simultaneously, nitration reaction is carried out to obtain film-entering liquid, and the utilized microorganisms comprise nitrite bacteria and nitrate bacteria; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water; the dynamic filling device pushes fresh filling with microorganisms into the contact cabin according to a certain flow, so that the content of the microorganisms in the reaction tank is kept stable;
separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device; the membrane concentrated water is sucked from the lower part of the separator by a circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrated solution, the membrane concentrated water flows from bottom to top in the heat exchanger, and the flow speed is 2.5-3.5 m/s; and a precipitated mud water outlet of the precipitation system is communicated with the evaporation drying system, and the precipitated mud water and the concentrated solution are mixed and then enter the evaporation drying system to be circularly dehydrated, concentrated and dried, so that distilled water and solid residues are obtained.
Advantageous effects
The treatment system and the process for oxidizing the tert-butanol into the methacrylic acid wastewater in the chemical plant have the advantages of short time consumption in the sedimentation process in the sedimentation tank, high treatment efficiency, short placement time of the waste liquid in the sedimentation tank and low concentration of the generated waste gas; the method can treat high-concentration wastewater generated in the process of oxidizing tertiary butanol into methacrylic acid, has high-efficiency treatment effect on suspended particles or floccules dispersed in different depths of liquid, ensures thorough front settlement, protects a rear membrane system, prolongs the service life of the membrane system, is not easy to block and lose efficacy, does not need to be frequently stopped to clean and replace the membrane system, and improves the quality of tail water.
Drawings
FIG. 1 is a schematic diagram of the connection structure of the wastewater treatment system of the present invention.
Fig. 2 is a schematic structural diagram of the precipitation system of the present invention.
FIG. 3 is a schematic structural view of a dynamic packing device according to the present invention
Fig. 4 is a schematic structural view of an ultrafiltration membrane apparatus of the present invention.
Fig. 5 is a schematic partial structure of the flexible adsorption net of the present invention.
The reference numerals include:
1-sedimentation system 11-sedimentation tank
111-net inlet tank 112-adsorption tank 113-net outlet tank 114-liquid inlet
115-up-pass spacing plate 116-down-pass spacing plate
12-powder injector 121-injection tube 122-solenoid valve
123-spray nozzle 124-diffuser
13-cycle adsorption device
131-flexible adsorption net 132-circulating power device 133-drying device
134-vibrating screen
2-A/O water treatment system 21-reaction tank 22-dynamic filling device
221-contact chamber 222-feed inlet 223-discharge outlet
224-pressure device
3-membrane filtration system
31-flushing cabin 32-ultrafiltration membrane component 33-sealing door
34-high pressure spray nozzle
4-evaporation system
5-an evaporation drying system.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings.
As shown in fig. 1, 2 and 5, the chemical plant tertiary butanol oxidation to methacrylic acid wastewater treatment system of the present invention comprises: the sedimentation system 1, the sedimentation system 1 is provided with a sedimentation tank 11, a powder injector 12 and a circulating adsorption device 13, wastewater entering the sedimentation tank 11 undergoes coagulating sedimentation reaction, slag removal, CODcr, BOD and colloid are carried out on the wastewater, and liquid and sediment muddy water after sedimentation treatment are obtained; the sedimentation tank 11 is provided with a net inlet tank 111, an adsorption tank 112, a net outlet tank 113 and a liquid inlet 114; the net inlet pool 111 and the net outlet pool 113 are positioned at two ends of the adsorption pool 112, the net inlet pool 111 and the net outlet pool 113 are respectively communicated with two ends of the bottom of the adsorption pool 112, and the liquid inlet 114 is used for conveying wastewater to the net inlet pool 111; the powder injector 12 is used for spraying magnetic adsorption powder above the wastewater level in the adsorption tank 112; the powder injector 12 is provided with a plastic tank containing magnetically adsorbed powder; the circulation adsorbing device 13 is provided with a flexible adsorbing net 131 capable of adsorbing magnetic adsorbing powder, a circulation power device 132 for driving the flexible adsorbing net 131 to move, a drying device 133 for drying sludge on the flexible adsorbing net 131 and a vibrating mesh screen 134 for removing the sludge from the flexible adsorbing net 131; the flexible adsorption net 131 is in a ring shape, and the flexible adsorption net 131 sequentially passes through the inlet net pond 111, the adsorption pond 112, the outlet net pond 113, the drying device 133 and the vibration screen 134 along the moving direction of the flexible adsorption net 131.
The drying device 133 may be a drying device or an air drying device, and may be heated by generating steam using a heat source of a chemical plant. The vibrating screen 134 includes a screen plate and a motor for driving the screen plate. The flexible adsorption net 131 can be gathered and piled for a certain length on a screen disc, and the screen disc collides and rubs the metal rings of the flexible adsorption net 131 with each other, so that the dried sludge is crushed and falls off.
The A/O water treatment system 2 is provided with a reaction tank 21, a filler which is used for maintaining microorganisms is arranged in the reaction tank 21, polysaccharide substances in the liquid after precipitation treatment are decomposed into monosaccharide or organic acid by utilizing the microorganisms, protein is decomposed into amino acid, fat substances are decomposed into fatty acid and glycerol, and simultaneously, nitration reaction is carried out to obtain film-entering liquid;
the membrane filtration system 3, the membrane filtration system 3 comprises an ultrafiltration membrane device and a reverse osmosis membrane device; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water; separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device;
the evaporation system 4 is provided with a separator, a heat exchanger and a circulating pump, wherein the membrane concentrated water is sucked from the lower part of the separator by the circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrated solution, and the membrane concentrated water flows in the heat exchanger from bottom to top at a flow rate of 2.5-3.5 m/s;
and the evaporation drying system 5 is used for circularly dehydrating, concentrating and drying the concentrated solution to obtain distilled water and solid residues.
The treatment system and the process for oxidizing the tert-butanol into the methacrylic acid wastewater in the chemical plant have the advantages of short time consumption in the sedimentation process in the sedimentation tank, high treatment efficiency, short placement time of the waste liquid in the sedimentation tank and low concentration of the generated waste gas; the method can treat high-concentration wastewater generated in the process of oxidizing tertiary butanol into methacrylic acid, has high-efficiency treatment effect on suspended particles or floccules dispersed in different depths of liquid, ensures thorough front settlement, protects a rear membrane system, prolongs the service life of the membrane system, is not easy to block and lose efficacy, does not need to be frequently stopped to clean and replace the membrane system, and improves the quality of tail water.
Specifically, the invention relates to a treatment system for oxidizing tert-butanol into methacrylic acid wastewater in a chemical plant, wherein an inclined pipeline is arranged in a sedimentation tank 11, a filler is arranged in the pipeline, and the surface hydraulic load of the pipeline is 1.0-1.2 m 3 /(m 2 ·h)。
As shown in fig. 3, in the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in a chemical plant, a dynamic packing device 22 is arranged in the reaction tank 21, the dynamic packing device 22 is provided with a contact cabin 221, a feed inlet 222, a discharge outlet 223 and a pressure device 224, the packing is pushed into the contact cabin 221 by the pressure device 224 through the feed inlet 222, and the packing at the discharge outlet 223 is pushed out of the contact cabin 221; a packing cavity is arranged in the contact cabin 221, a contact window is arranged on the wall of the contact cabin 221, and packing in the packing cavity is contacted with liquid in the reaction tank 21 through the contact window; the contact chamber 221 is suspended in the reaction tank 21. According to the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in the chemical plant, the pressure device 224 can slowly introduce fresh filler containing nitrifying bacteria into the contact cabin 221, so that microorganisms in the wastewater can maintain a certain concentration, and the microorganism treatment effect is improved. Further, in the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in a chemical plant, the contact cabin 221 is provided with a cabin door for closing a contact window; the dynamic filling devices 22 are arranged in parallel, and the filling directions of two adjacent dynamic filling devices 22 are reversed, so that the effect of supplementing microorganisms into the waste liquid is further improved.
Referring to fig. 4, the ultrafiltration membrane device of the treatment system for oxidizing tertiary butanol into methacrylic acid wastewater in a chemical plant of the present invention comprises a flushing cabin 31, an ultrafiltration membrane assembly 32 and two openable and closable closing doors 33, wherein the ultrafiltration membrane assembly 32 is provided with an ultrafiltration membrane, the ultrafiltration membrane assembly 32 is replaceably inserted into the flushing cabin 31, the two closing doors 33 are arranged at both sides of the ultrafiltration membrane assembly 32, the upper end and the lower end of the flushing cabin 31 are respectively provided with a high pressure injection nozzle 34, and the high pressure injection nozzles 34 inject pure water containing oxygen to the ultrafiltration membrane assembly 32 for flushing the ultrafiltration membrane. The high-pressure flushing of the wastewater treatment system for oxidizing tert-butanol into methacrylic acid in the chemical plant can be completed without pumping the ultrafiltration membrane component 32 from the reaction tank 21. Specifically, a drain pipe may be provided in the flushing tank 31.
Furthermore, the chemical plant tertiary butanol is oxidized into methacrylic acid wastewater treatment system, the evaporation drying system 5 is provided with a distillation still, a stirrer, a condenser, a vacuum pump and a buffer water tank, the stirrer is used for stirring concentrated solution in the distillation still, and the distillation still, the condenser and the vacuum pump are sequentially connected in a conducting way; distilled water reacted in the distillation kettle is condensed by the condenser and then pumped into the buffer water tank by the vacuum pump, and the distillation kettle is in a negative pressure state. The evaporation drying system 5 can be an existing vacuum evaporation drying system 5.
As shown in fig. 1, further, the system for treating waste water from oxidizing t-butanol into methacrylic acid in chemical plant according to the present invention, the powder injector 12 further comprises an injection pipe 121, an electromagnetic valve 122 and an air compressor, wherein a horn-shaped injection nozzle 123 with an upward opening is installed at one end of the injection pipe 121, an inverted conical diffuser 124 is provided at the middle of the injection nozzle 123, the distance between the diffuser 124 and the horn-shaped injection nozzle 123 is sequentially increased from top to bottom, the other end of the injection pipe 121 is communicated with the air compressor through the electromagnetic valve 122, a plastic tank is installed above the injection pipe 121 and is communicated with the middle of the injection pipe 121, and the air compressor is used for pressurizing the injection pipe 121. The chemical plant tertiary butanol oxidation methacrylic acid wastewater treatment system can be provided with a PLC (programmable logic controller) specifically, after an electromagnetic valve 122 is electrified, an air compressor is used for introducing high-pressure gas into an injection pipe 121, powder entering the injection pipe 121 is pushed into an injection nozzle 123 and uniformly dispersed and sprinkled above the liquid level in an adsorption tank 112 after being diffused by a diffuser 124, and the magnetic adsorption powder is uniformly dispersed during sprinkling.
Further, in the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in a chemical plant, a plurality of upper through partition plates 115 and lower through partition plates 116 which are alternately arranged are arranged in the adsorption tank 112, a through hole is formed at the upper end part of the upper through partition plates 115, a through hole is formed between the lower end part of the lower through partition plates 116 and the tank bottom of the adsorption tank 112, and rotatable plastic corner rollers are arranged at the upper end part of the upper through partition plates 115 and at the included angles between the upper through partition plates 115 and the adsorption tank 112, so that the flexible adsorption net 131 is attached to the upper through partition plates 115 and the tank bottom of the adsorption tank 112. According to the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in the chemical plant, the flowing time of the waste liquid in the adsorption tank 112 is long, the contact time of the waste liquid with the flexible adsorption net 131 is long, and the adsorption effect of particles, floccules and colloid by the flexible adsorption net 131 is good. To reduce the possibility of flocs falling off the flexible adsorption net 131, the speed of advancing the flexible adsorption net 131 is controlled to be 1m/h or less.
According to the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in the chemical plant, the upper through partition plate 115 is provided with through holes, the flexible adsorption net 131 is a net formed by sequentially sleeving and buckling a plurality of metal rings, and each metal ring is bound with adsorption Mao Sheng; the diameter of the passing holes is 1.5-2 times of the diameter of the meshes of the flexible adsorption net 131; the diameter of the mesh of the flexible adsorption net 131 is a mm, the conductivity of the wastewater entering the sedimentation tank 11 is b mu S/cm, the particle size of the magnetic adsorption powder is c mm, the length and the diameter of the adsorption wool rope are d mm and e mm respectively, and the following mathematical relationship exists between the length and the diameter of the adsorption wool rope and a, b, c, d, e: a=c=b=e, where c is 1 to 3,e and 0.5 to 2. In the system for treating wastewater from oxidizing tert-butanol into methacrylic acid in a chemical plant, a is preferably 20, d is 18, and e is preferably 2. According to the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in the chemical plant, disclosed by the invention, the specification of the particle size of magnetic adsorption powder to be selected can be determined according to the conductivity of wastewater to be treated, so that the system has a better effect.
The invention relates to a process for treating wastewater from oxidizing tert-butanol into methacrylic acid in a chemical plant, which uses the wastewater treatment system of the invention, and comprises the following steps: the circulation power device 132 drives the flexible adsorption net 131 to sequentially pass through the net inlet pool 111, the adsorption pool 112, the net outlet pool 113, the drying device 133 and the vibration mesh screen 134, and then to be recycled into the net inlet pool 111; the waste water firstly enters the net inlet pool 111 through the liquid inlet 114, then enters the adsorption pool 112 through the bottom of the net inlet pool 111, the powder injector 12 sprays sand to the upper part of the waste water liquid surface in the adsorption pool 112 at regular time to adsorb powder, and the adsorption powder can be magnetic adsorption powder or the mixture of the magnetic adsorption powder and cinder powder; slag removal, CODcr, BOD and colloid are carried out in an adsorption tank 112, and liquid after precipitation treatment is obtained; the adsorption powder adsorbs colloid, floccules and slag, then sinks, is adsorbed by the flexible adsorption net 131 and moves along with the adsorption net; the adsorption net brings the sludge out of the sedimentation tank 11 and then enters the drying device 133, the sludge is dried in the drying device 133 and then is adhered to the sexual adsorption net, and the dried sludge in the vibration mesh screen 134 is separated from the adsorption net; and also comprises a blowing device for blowing away the sludge on the adsorption net before entering the net entering pool 111;
the reaction tank 21 is internally provided with a filler for retaining microorganisms, the microorganisms are utilized to decompose polysaccharide substances in the liquid after the precipitation treatment into monosaccharide or organic acid, protein is decomposed into amino acid, fat substances are decomposed into fatty acid and glycerol, and simultaneously, nitration reaction is carried out to obtain film-entering liquid, and the utilized microorganisms comprise nitrite bacteria and nitrate bacteria; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water; the dynamic packing device 22 pushes fresh packing with microorganisms into the contact cabin 221 according to a certain flow rate, so that the content of the microorganisms in the reaction tank 21 is kept stable;
separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device; the membrane concentrated water is sucked from the lower part of the separator by a circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrated solution, the membrane concentrated water flows from bottom to top in the heat exchanger, and the flow speed is 2.5-3.5 m/s; the sediment mud water outlet of the sediment system 1 is communicated with the evaporation drying system 5, and the sediment mud water and the concentrated solution are mixed and then enter the evaporation drying system 5 to be circularly dehydrated, concentrated and dried, so that distilled water and solid residues are obtained.
The reaction tank 21 is internally provided with a filler for maintaining microorganisms, and the primary function of the anaerobic tank is denitrification; and secondly, releasing phosphorus by the sludge. Ammonia nitrogen is converted into nitrate by nitrifying bacteria loaded on the filler. The nitrification is a two-step process, which utilizes two types of microorganisms, namely nitrite bacteria and nitrate bacteria, respectively. The first step is to convert ammonia nitrogen into nitrite, the ammonia nitrogen is first converted into nitrite by nitrite bacteria, and the second step is to convert nitrite into nitrate. Nitrite bacteria include nitrite unicellular bacteria, nitrite helicobacter bacteria and nitrite coccus bacteria. The conversion of nitrite to nitrate is accomplished by nitrate bacteria, which also consist of bacillus, spirobacillus and coccum. Nitrite bacteria and nitrate bacteria are collectively referred to as nitrifying bacteria. Nitrifying bacteria are obligate autotrophic gram-negative aerobic bacteria that utilize the energy released during ammonia nitrogen conversion as an energy source for their own metabolism.
The reaction process of the first step is as follows:
the second step of reaction is:
the hydrolysis zone operates under the anoxic condition, the concentration of dissolved oxygen is controlled below 0.5mg/L, an anoxic activated sludge layer mainly containing hydrolytic acidification bacteria is formed, water flows in from a calandria distributed at the bottom of the tank and flows upwards through the sludge layer, and the sludge layer intercepts suspended matters in the water and decomposes macromolecular organic matters in the water into small molecular organic matters which are easy to biodegrade, so that the requirement of aerobic treatment on the dissolved oxygen is reduced by about 30 percent.
Under proper anoxic conditions, nitrate in sewage is reduced into molecular nitrogen by utilizing facultative microorganisms and is escaped into the atmosphere to play a role in denitrification, and the anaerobic tank plays a role in acidic fermentation to degrade carbohydrate into fatty acid and degrade macromolecular substances and solid substances into soluble substances, so that the biochemical performance of the biological contact oxidation tank is improved. The hydraulic retention time was 1 hour.
The reaction of the aerobic section adopts multistage biological oxidation to digest and remove residual organic carbide, the aeration time is controlled to realize different requirements of BOD removal, digestion, phosphorus absorption and the like, and the intensity of aeration or a stirrer is controlled to maintain an anaerobic or anoxic state in the reactor, so that the digestion and denitrification processes are realized. The whole system forms an internal circulation, and jet aeration is carried out, so that high-efficiency aerobic bacteria in sewage fully contact with oxygen, microorganisms are rapidly propagated under the condition of sufficient oxygen, and organic matters in the water are efficiently degraded. At the moment, the aerobic nitrifying bacteria in the water oxidize ammonia nitrogen in the water into nitrate or nitrite through nitrifying reaction, and convert the nitrate or nitrite into nitrate nitrogen.
The biological denitrification process consists of two biochemical processes of aerobic biological nitrification and anaerobic or anoxic denitrification. The nitrifying process is to convert ammonia nitrogen into nitrite nitrogen by nitrifying bacteria under aerobic condition, and then to oxidize nitrite by nitrifying bacteria. Nitrosations and nitrites are autotrophs, and the nitritation process requires higher mass concentrations of dissolved oxygen and lower mass concentrations of organics. In the later stage of the aeration reaction, the mass concentration of dissolved oxygen in the reactor is higher, the mass concentration of matrix is greatly reduced, and the ammonia nitrogen in the wastewater completes the nitrification process on the basis of removing organic matters. The denitrification process is completed by facultative bacteria or anaerobic bacteria, nitrate is used as an electron acceptor, various carbohydrates are used as electron donors for anaerobic respiration, and nitrate nitrogen is reduced into nitrogen to escape on the basis of oxidative decomposition of organic matters.
Further, the sedimentation tank 11 is internally provided with a pipeline which is obliquely arranged, the pipeline is internally provided with a filler, and the surface hydraulic load of the pipeline is 1.0-1.2 m 3 /(m 2 H). The treatment system for oxidizing tert-butanol into methacrylic acid wastewater in chemical plants provided by the invention can degrade organic matters which are difficult to biodegrade into biochemically degradable organic matters, so that the biodegradability of wastewater is improved, and the subsequent aerobic section is lightenedAn organic load.
Further, in the treatment system for oxidizing tert-butanol into methacrylic acid wastewater in a chemical plant, a dynamic packing device 22 is arranged in the reaction tank 21, the dynamic packing device 22 is provided with a contact cabin 221, a feed inlet 222, a discharge outlet 223 and a pressure device 224, the packing is pushed into the contact cabin 221 by the pressure device 224 through the feed inlet 222, and the packing positioned at the discharge outlet 223 is pushed out of the contact cabin 221; a packing cavity is arranged in the contact chamber 221, a contact window is arranged on the wall of the contact chamber 221, and packing in the packing cavity is contacted with liquid in the reaction tank 21 through the contact window. The pressure device 224 may be a screw feeder.
Further, in the chemical plant tertiary butanol oxidation to methacrylic acid wastewater treatment system of the present invention, the contact chamber 221 is provided with a chamber door for closing a contact window.
Furthermore, the ultrafiltration membrane device comprises a flushing cabin 31, an ultrafiltration membrane component 32 and two openable and closable sealing doors 33, wherein the ultrafiltration membrane component 32 is provided with an ultrafiltration membrane, the ultrafiltration membrane component 32 is replaceably inserted in the flushing cabin 31, the two sealing doors 33 are arranged on two sides of the ultrafiltration membrane component 32, the upper end part and the lower end part of the flushing cabin 31 are respectively provided with a high-pressure spray nozzle 34, and the high-pressure spray nozzles 34 spray pure water containing oxygen to the ultrafiltration membrane component 32 for flushing the ultrafiltration membrane.
Furthermore, the chemical plant tertiary butanol is oxidized into methacrylic acid wastewater treatment system, the evaporation drying system 5 is provided with a distillation still, a stirrer, a condenser, a vacuum pump and a buffer water tank, the stirrer is used for stirring concentrated solution in the distillation still, and the distillation still, the condenser and the vacuum pump are sequentially connected in a conducting way; distilled water reacted in the distillation kettle is condensed by the condenser and then pumped into the buffer water tank by the vacuum pump, and the distillation kettle is in a negative pressure state.
The process for treating wastewater from oxidizing tert-butanol into methacrylic acid in chemical plants, which is disclosed by the invention, comprises the following steps of: the wastewater entering the sedimentation tank 11 undergoes coagulating sedimentation reaction, slag removal, CODcr, BOD and colloid are carried out, and liquid after sedimentation treatment is obtained; the reaction tank 21 is internally provided with a filler for retaining microorganisms, the microorganisms are utilized to decompose polysaccharide substances in the liquid after the precipitation treatment into monosaccharide or organic acid, protein is decomposed into amino acid, fat substances are decomposed into fatty acid and glycerol, and simultaneously, nitration reaction is carried out to obtain film-entering liquid, and the utilized microorganisms comprise nitrite bacteria and nitrate bacteria; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water; separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device; the membrane concentrated water is sucked from the lower part of the separator by a circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrated solution, the membrane concentrated water flows from bottom to top in the heat exchanger, and the flow speed is 2.5-3.5 m/s; the evaporation drying system 5 carries out circulation dehydration, concentration and drying on the concentrated solution to obtain distilled water and solid residues. The treatment system and the process for oxidizing the tert-butanol into the methacrylic acid wastewater in the chemical plant have the advantages of short time consumption in the sedimentation process in the sedimentation tank, high treatment efficiency, short placement time of the waste liquid in the sedimentation tank and low concentration of the generated waste gas; the method can treat high-concentration wastewater generated in the process of oxidizing tertiary butanol into methacrylic acid, has high-efficiency treatment effect on suspended particles or floccules dispersed in different depths of liquid, ensures thorough front settlement, protects a rear membrane system, prolongs the service life of the membrane system, is not easy to block and lose efficacy, does not need to be frequently stopped to clean and replace the membrane system, and improves the quality of tail water.
In view of the above, the present invention has the above-mentioned excellent characteristics, so that it can be used to improve the performance and practicality of the prior art, and is a product with great practical value.
The foregoing is merely exemplary of the present invention, and those skilled in the art should not be considered as limiting the invention, since modifications may be made in the specific embodiments and application scope of the invention in light of the teachings of the present invention.
Claims (2)
1. A process for the treatment of wastewater from the oxidation of t-butanol to methacrylic acid in a chemical plant, wherein a wastewater treatment system is used, said wastewater treatment system comprising:
the sedimentation system is provided with a sedimentation tank, a powder injector, a muddy water outlet and a circulating adsorption device, wastewater entering the sedimentation tank is subjected to coagulating sedimentation reaction, slag removal, CODcr, BOD and colloid are carried out on the wastewater, and liquid and sediment muddy water after sedimentation treatment are obtained; the sedimentation tank is provided with a net inlet tank, an adsorption tank, a net outlet tank and a liquid inlet; the net inlet pool and the net outlet pool are positioned at two ends of the adsorption pool, the net inlet pool and the net outlet pool are respectively communicated with two ends of the bottom of the adsorption pool, and the liquid inlet is used for conveying wastewater to the net inlet pool; the powder injector is used for spraying magnetic adsorption powder above the liquid level of the wastewater in the adsorption tank; the powder injector is provided with a plastic box filled with magnetic adsorption powder; the circulating adsorption device is provided with a flexible adsorption net capable of adsorbing magnetic adsorption powder, a circulating power device for driving the flexible adsorption net to move, a drying device for drying sludge on the flexible adsorption net and a vibrating mesh screen for removing the sludge from the flexible adsorption net; the flexible adsorption net is annular, and sequentially passes through the net inlet pool, the adsorption pool, the net outlet pool, the drying device and the vibration mesh screen along the moving direction of the flexible adsorption net;
the A/O water treatment system is provided with a reaction tank, and a filler for maintaining microorganisms is arranged in the reaction tank; the reaction tank is internally provided with a dynamic filling device, the dynamic filling device is provided with a contact cabin, a feed inlet, a discharge outlet and a pressure device, the filling is pushed into the contact cabin by the pressure device through the feed inlet, and the filling at the discharge outlet is pushed out of the contact cabin; a packing cavity is arranged in the contact cabin, a contact window is arranged on the wall of the contact cabin, packing in the packing cavity is contacted with liquid in the reaction tank through the contact window, and the pressure device is a spiral feeder; the contact cabin is provided with cabin doors for closing the contact windows, a plurality of dynamic filling devices are arranged in parallel, and filling directions of two adjacent dynamic filling devices are reversely arranged;
the membrane filtration system comprises an ultrafiltration membrane device and a reverse osmosis membrane device; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water; separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device;
the evaporation system is provided with a separator, a heat exchanger and a circulating pump, wherein the membrane concentrated water is sucked from the lower part of the separator by the circulating pump and then pushed into the heat exchanger to obtain distilled water and concentrated solution, and the membrane concentrated water flows in the heat exchanger from bottom to top at a flow rate of 2.5-3.5 m/s;
the evaporation drying system is used for carrying out circulation dehydration, concentration and drying on the concentrated solution to obtain distilled water and solid residues, and is provided with a distillation still, a stirrer, a condenser, a vacuum pump and a buffer water tank, wherein the stirrer is used for stirring the concentrated solution in the distillation still, and the distillation still, the condenser and the vacuum pump are sequentially connected in a conducting manner; distilled water reacted in the distillation kettle is condensed by a condenser and then pumped to a buffer water tank by a vacuum pump, and the distillation kettle is in a negative pressure state;
the wastewater treatment system also comprises a blowing device which is used for blowing away sludge on the adsorption net before entering the net entering pool;
a plurality of upper through partition plates and lower through partition plates which are alternately arranged are arranged in the adsorption tank, a through hole is formed in the upper end part of each upper through partition plate, a through hole is formed between the lower end part of each lower through partition plate and the tank bottom of the adsorption tank, and rotatable plastic corner rollers are arranged at the upper end part of each upper through partition plate and at the included angle between each upper through partition plate and the adsorption tank, so that a flexible adsorption net is attached to the upper through partition plates and the tank bottom of the adsorption tank;
the upper through partition plate is provided with a through hole, the flexible adsorption net is formed by sequentially sleeving and buckling a plurality of metal rings, and each metal ring is bound with adsorption Mao Sheng; the diameter of the passing hole is 1.5-2 times of the diameter of the mesh of the flexible adsorption net; the diameter of the mesh of the flexible adsorption net is a millimeter, the conductivity of the wastewater entering the sedimentation tank is b mu S/cm, the particle size of the magnetic adsorption powder is c millimeter, the length and the diameter of the adsorption wool rope are d millimeter and e millimeter respectively, and the following mathematical relationship exists between a, b, c, d, e: a-c d=b-e, wherein c is 1-3 and e is 0.5-2;
the treatment process for oxidizing tert-butanol into methacrylic acid wastewater in the chemical plant comprises the following steps:
the circulating power device drives the flexible adsorption net to sequentially pass through the net inlet pool, the adsorption pool, the net outlet pool, the drying device and the vibration mesh screen, and then the flexible adsorption net is recycled into the net inlet pool; the waste water firstly enters a net inlet tank through a liquid inlet, then enters an adsorption tank through the bottom of the net inlet tank, and a powder injector sprays adsorption powder to the upper part of the waste water liquid level in the adsorption tank at regular time, wherein the adsorption powder is magnetic adsorption powder or a mixture of the magnetic adsorption powder and coal cinder powder; slag removal, CODcr, BOD and colloid are carried out in an adsorption tank, and liquid after precipitation treatment is obtained; the adsorption powder adsorbs colloid, floccules and slag, then sinks to be adsorbed by the flexible adsorption net and moves along with the adsorption net; the adsorption net brings the sludge out of the sedimentation tank and then enters a drying device, the sludge is dried in the drying device and then adhered to the sexual adsorption net, and the dried sludge in the vibration mesh screen is separated from the adsorption net;
the effluent of the precipitation system enters an A/O water treatment system, a dynamic packing device pushes fresh packing with microorganisms into a contact cabin according to a certain flow, the content of the microorganisms in a reaction tank is kept stable, the microorganisms are utilized to decompose polysaccharide substances in the liquid after precipitation treatment into monosaccharides or organic acids, proteins are decomposed into amino acids, fat substances are decomposed into fatty acids and glycerol, and simultaneously, nitration reaction is carried out to obtain film-entering liquid, wherein the utilized microorganisms comprise nitrite bacteria and nitrate bacteria; introducing the obtained membrane-entering liquid into an ultrafiltration membrane device to filter microorganisms, suspended particles, macromolecular organic matters and colloid, so as to obtain pretreated produced water;
separating the pretreated product water into product water and membrane concentrated water by using a reverse osmosis membrane device, and evaporating the membrane concentrated water by using an evaporation system to obtain distilled water and concentrated solution; and a precipitated mud water outlet of the precipitation system is communicated with the evaporation drying system, and the precipitated mud water and the concentrated solution are mixed and then enter the evaporation drying system to be circularly dehydrated, concentrated and dried, so that distilled water and solid residues are obtained.
2. The process for treating wastewater from oxidizing t-butanol to methacrylic acid in chemical plant according to claim 1, wherein: the ultrafiltration membrane device comprises a flushing cabin, an ultrafiltration membrane component and two openable and closable sealing doors, wherein the ultrafiltration membrane component is provided with an ultrafiltration membrane, the ultrafiltration membrane component is replaceable and inserted into the flushing cabin, the two sealing doors are arranged on two sides of the ultrafiltration membrane component, the upper end part and the lower end part of the flushing cabin are respectively provided with a high-pressure injection nozzle, and the high-pressure injection nozzles are used for injecting purified water containing oxygen into the ultrafiltration membrane component to flush the ultrafiltration membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011233022.4A CN112624490B (en) | 2020-11-06 | 2020-11-06 | System and process for treating wastewater generated by oxidizing tert-butyl alcohol into methacrylic acid in chemical plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011233022.4A CN112624490B (en) | 2020-11-06 | 2020-11-06 | System and process for treating wastewater generated by oxidizing tert-butyl alcohol into methacrylic acid in chemical plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112624490A CN112624490A (en) | 2021-04-09 |
| CN112624490B true CN112624490B (en) | 2024-04-16 |
Family
ID=75303031
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011233022.4A Active CN112624490B (en) | 2020-11-06 | 2020-11-06 | System and process for treating wastewater generated by oxidizing tert-butyl alcohol into methacrylic acid in chemical plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112624490B (en) |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857304A (en) * | 2010-07-06 | 2010-10-13 | 深圳清华大学研究院 | Dynamic filtering-membrane bioreactor for sewage treatment and filtering method thereof |
| CN104876324A (en) * | 2015-05-27 | 2015-09-02 | 重庆大学 | Wastewater treatment microbial reaction pot easy for cleaning |
| CN204625440U (en) * | 2015-05-08 | 2015-09-09 | 中国城市建设研究院有限公司 | Domestic waste Leachate site zero-discharge treatment system |
| CN105565570A (en) * | 2016-02-03 | 2016-05-11 | 丁西军 | Multifunctional sewage treatment device |
| CN107384792A (en) * | 2017-08-30 | 2017-11-24 | 宁波佗鹊堂生物科技有限公司 | Microorganism species mother liquor cultural method |
| CN107879414A (en) * | 2017-12-04 | 2018-04-06 | 宿州冬宇环保科技有限公司 | A kind of grease oil residue separating apparatus |
| CN207608426U (en) * | 2017-10-26 | 2018-07-13 | 天津碧水源膜材料有限公司 | A kind of sewage disposal device |
| CN208161376U (en) * | 2018-03-06 | 2018-11-30 | 天津德鑫石化设备有限公司 | A kind of washing unit with reverse osmosis membrane |
| CN110550787A (en) * | 2019-08-20 | 2019-12-10 | 生态环境部华南环境科学研究所 | Desalting treatment equipment and method for fertilizer utilization of cow breeding wastewater |
-
2020
- 2020-11-06 CN CN202011233022.4A patent/CN112624490B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857304A (en) * | 2010-07-06 | 2010-10-13 | 深圳清华大学研究院 | Dynamic filtering-membrane bioreactor for sewage treatment and filtering method thereof |
| CN204625440U (en) * | 2015-05-08 | 2015-09-09 | 中国城市建设研究院有限公司 | Domestic waste Leachate site zero-discharge treatment system |
| CN104876324A (en) * | 2015-05-27 | 2015-09-02 | 重庆大学 | Wastewater treatment microbial reaction pot easy for cleaning |
| CN105565570A (en) * | 2016-02-03 | 2016-05-11 | 丁西军 | Multifunctional sewage treatment device |
| CN107384792A (en) * | 2017-08-30 | 2017-11-24 | 宁波佗鹊堂生物科技有限公司 | Microorganism species mother liquor cultural method |
| CN207608426U (en) * | 2017-10-26 | 2018-07-13 | 天津碧水源膜材料有限公司 | A kind of sewage disposal device |
| CN107879414A (en) * | 2017-12-04 | 2018-04-06 | 宿州冬宇环保科技有限公司 | A kind of grease oil residue separating apparatus |
| CN208161376U (en) * | 2018-03-06 | 2018-11-30 | 天津德鑫石化设备有限公司 | A kind of washing unit with reverse osmosis membrane |
| CN110550787A (en) * | 2019-08-20 | 2019-12-10 | 生态环境部华南环境科学研究所 | Desalting treatment equipment and method for fertilizer utilization of cow breeding wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112624490A (en) | 2021-04-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106242163B (en) | A kind of processing method of percolate embrane method concentrate | |
| CN106277669B (en) | Ecological dredging recycling method | |
| CN101624253A (en) | High efficient complex enzyme sewage treatment process and high efficient complex enzyme sewage treatment device | |
| KR101964759B1 (en) | A treatment apparatus of high concentration organic wastewater using odor removal microorganism | |
| CN110862182A (en) | Landfill leachate treatment device and method | |
| CN108751581B (en) | Treatment process of biochemical effluent of landfill leachate | |
| CN1225417C (en) | Saponin waste water handling method | |
| CN201648186U (en) | Composite membrane bioreactor | |
| CN112624490B (en) | System and process for treating wastewater generated by oxidizing tert-butyl alcohol into methacrylic acid in chemical plant | |
| CN205974184U (en) | Processing system of landfill leachate embrane method concentrate | |
| CN102050547A (en) | Pretreatment method of organic wastewater difficult to biochemically degrade | |
| CN105060412A (en) | Apparatus for adsorption-electrolysis-aeration synergistic integrated treatment of eutrophic water body | |
| KR100537572B1 (en) | Advanced treatment of sewage method and apparatus for eliminating chemical component such as nitrogen and phosphorus and fog reducing sludge | |
| CN101665305B (en) | Method for processing straw-pulp-papermaking wastewater by using combined UASB plus A/O technique | |
| CN105836974B (en) | A kind of garbage leachate treatment device and method | |
| CN115572017A (en) | Internal circulation method and system for aquaculture tail water | |
| CN209957611U (en) | Advanced treatment device for biodegradable wastewater | |
| CN109824217B (en) | Fenton's reagent of pesticide waste water and hydrodynamic cavitation combined treatment system | |
| CN110642364B (en) | Device for catalytic oxidation of coal chemical wastewater by using suspension catalyst | |
| CN112811732A (en) | System for efficiently treating acrylonitrile wastewater and combined process thereof | |
| RU2472719C2 (en) | Method of increasing efficiency of aerobic waste water treatment | |
| CN1072613C (en) | Anaerobic reation pool and method for treating waste water | |
| CN101113066A (en) | Sewage treatment system of plant pharmaceutical factory and its method | |
| CN1440941A (en) | Anaerobic moleculer decomposing method of refuse percolate | |
| CN203382616U (en) | Sewage treatment system |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |