CN112919726A - Wastewater treatment process for producing hydrogen peroxide - Google Patents
Wastewater treatment process for producing hydrogen peroxide Download PDFInfo
- Publication number
- CN112919726A CN112919726A CN201911242605.0A CN201911242605A CN112919726A CN 112919726 A CN112919726 A CN 112919726A CN 201911242605 A CN201911242605 A CN 201911242605A CN 112919726 A CN112919726 A CN 112919726A
- Authority
- CN
- China
- Prior art keywords
- tank
- wastewater
- sludge
- hydrogen peroxide
- cass
- 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.)
- Pending
Links
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 238000000034 method Methods 0.000 title claims abstract description 65
- 230000008569 process Effects 0.000 title claims abstract description 47
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 27
- 239000002351 wastewater Substances 0.000 claims abstract description 70
- 238000004062 sedimentation Methods 0.000 claims abstract description 55
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 51
- 230000003647 oxidation Effects 0.000 claims abstract description 49
- 230000020477 pH reduction Effects 0.000 claims abstract description 29
- 230000007062 hydrolysis Effects 0.000 claims abstract description 22
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 22
- QMQXDJATSGGYDR-UHFFFAOYSA-N methylidyneiron Chemical compound [C].[Fe] QMQXDJATSGGYDR-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 claims abstract description 7
- 208000014451 palmoplantar keratoderma and congenital alopecia 2 Diseases 0.000 claims abstract 12
- 239000010802 sludge Substances 0.000 claims description 71
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 27
- 238000005273 aeration Methods 0.000 claims description 25
- 238000006243 chemical reaction Methods 0.000 claims description 24
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 20
- 238000005345 coagulation Methods 0.000 claims description 16
- 230000015271 coagulation Effects 0.000 claims description 15
- 238000007599 discharging Methods 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 230000014759 maintenance of location Effects 0.000 claims description 10
- 238000010992 reflux Methods 0.000 claims description 10
- 230000001105 regulatory effect Effects 0.000 claims description 10
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 7
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 7
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 7
- 230000035484 reaction time Effects 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 239000011790 ferrous sulphate Substances 0.000 claims description 6
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 239000004566 building material Substances 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 5
- 239000000920 calcium hydroxide Substances 0.000 claims description 5
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 239000003337 fertilizer Substances 0.000 claims description 5
- 230000003472 neutralizing effect Effects 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 229920002401 polyacrylamide Polymers 0.000 claims description 4
- 239000002244 precipitate Substances 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 16
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 16
- 239000011574 phosphorus Substances 0.000 abstract description 16
- 229910019142 PO4 Inorganic materials 0.000 abstract description 13
- 239000010452 phosphate Substances 0.000 abstract description 13
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 abstract description 11
- 230000001112 coagulating effect Effects 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 9
- 239000010865 sewage Substances 0.000 abstract description 8
- 230000003301 hydrolyzing effect Effects 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 6
- 239000013049 sediment Substances 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 230000003197 catalytic effect Effects 0.000 description 5
- 238000005086 pumping Methods 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- -1 hydroxyl radicals Chemical class 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- IBIRZFNPWYRWOG-UHFFFAOYSA-N phosphane;phosphoric acid Chemical compound P.OP(O)(O)=O IBIRZFNPWYRWOG-UHFFFAOYSA-N 0.000 description 3
- AUHZEENZYGFFBQ-UHFFFAOYSA-N 1,3,5-trimethylbenzene Chemical compound CC1=CC(C)=CC(C)=C1 AUHZEENZYGFFBQ-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- YEVQZPWSVWZAOB-UHFFFAOYSA-N 2-(bromomethyl)-1-iodo-4-(trifluoromethyl)benzene Chemical compound FC(F)(F)C1=CC=C(I)C(CBr)=C1 YEVQZPWSVWZAOB-UHFFFAOYSA-N 0.000 description 1
- SJEBAWHUJDUKQK-UHFFFAOYSA-N 2-ethylanthraquinone Chemical compound C1=CC=C2C(=O)C3=CC(CC)=CC=C3C(=O)C2=C1 SJEBAWHUJDUKQK-UHFFFAOYSA-N 0.000 description 1
- 241000272814 Anser sp. Species 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 108700038250 PAM2-CSK4 Proteins 0.000 description 1
- 101100206155 Schizosaccharomyces pombe (strain 972 / ATCC 24843) tbp1 gene Proteins 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009297 electrocoagulation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000012224 working solution Substances 0.000 description 1
Images
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
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F7/00—Fertilisers from waste water, sewage sludge, sea slime, ooze or similar masses
- C05F7/005—Waste water from industrial processing material neither of agricultural nor of animal origin
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention discloses a wastewater treatment process for producing hydrogen peroxide, and relates to a wastewater treatment process. The invention mainly solves the problem of hydrogen peroxide production wastewater treatment through a combined process of 'iron-carbon micro-electrolysis + Fenton oxidation + coagulating sedimentation + hydrolytic acidification + CASS', firstly, an iron-carbon micro-electrolysis-Fenton oxidation pretreatment process is applied to open a ring, heavy aromatics in sewage are reduced, the wastewater is easily degraded, and the load of biochemical treatment is reduced; then carrying out coagulating sedimentation treatment to remove total phosphorus; finally, a hydrolysis acidification and CASS scheme is used for deeply removing CODcr and phosphate, so that the wastewater reaches the discharge standard; the combined process has the advantages of wide application, good treatment effect, simple operation and management and low cost.
Description
Technical Field
The invention relates to a wastewater treatment process, in particular to a wastewater treatment process for producing hydrogen peroxide.
Background
At present, the comprehensive sewage discharged in the domestic hydrogen peroxide production process mainly comprises working solution washing water, condensate generated in the clay bed regeneration process, condensate generated in the hydrogenation tower regeneration process, soaking water, flushing equipment, ground and other waste water. The waste water mainly contains 2-ethyl anthraquinone, 1, 3, 5-trimethyl benzene, trioctyl phosphate, phosphoric acid, potassium carbonate and other pollution factors. Therefore, the treatment of wastewater from hydrogen peroxide production is actually the reduction of CODcr (chemical oxygen consumption) and the removal of phosphate, and at present, there are many methods for reducing CODcr and removing phosphate, and with the progress of research, various treatment technologies are mutually permeated, so that the treatment effect is better. In general, the main treatment techniques are physicochemical treatment and biochemical methods.
The literature on the aspect of wastewater treatment for producing hydrogen peroxide at home and abroad is less, such as: the Jiangxi Jiangjiang ammonia chemical industry Limited company utilizes that the wastewater contains hydrogen peroxide and then ferrous sulfate, and finds that the indirect treatment has better effect than the continuous treatment mode, the CODcr is reduced to 98mg/L from 3380mg/L, and the removal rate is 97.1 percent; aiming at the characteristics that the CODcr concentration of wastewater produced by a hydrogen peroxide plant is up to 50000mg/L and the total phosphorus content is 18g/L, the wastewater is pretreated by an electrocoagulation method, and then is further adsorbed and filtered by active carbon, test results show that the CODcr concentration is reduced to 90.84mg/L and the phosphorus concentration is reduced to 2.9mg/L, the color of sewage is changed from yellow goose to colorless and transparent, and the effluent meets the national standard; the effect and the optimal condition of treating the sewage produced by the hydrogen peroxide by the Fenton oxidation method are explored by the incumbent and the like, and the test results show that the pH is 3-4, the molar ratio of the hydrogen peroxide to the FeSO4 is 5: at 1, CODcr removing efficiency is the highest, reaching more than 90%. However, the above treatment method mainly has the following problems:
1) the CODcr and the phosphate in the sewage are difficult to be well removed only by physical and chemical measures, and the organic matters in the sewage are essentially transferred into the sediment sludge;
2) the advanced oxidation method with high processing capacity has high requirements on facilities and equipment, consumes power and materials, and is high in cost and uneconomical;
3) the traditional activated sludge method has the defects that the concentration of pollutants in wastewater produced by hydrogen peroxide is high, heavy aromatic hydrocarbons which are difficult to react are contained, the water quality and the water quantity are unstable, and the treatment effect of the traditional activated sludge method cannot reach the latest pollution discharge standard.
Most hydrogen peroxide manufacturing enterprises at present use hydrogen peroxide catalysis and oxidation-coagulation precipitation schemes to treat wastewater. According to literature data, many experimental researches and applications are conducted on chemical wastewater at home and abroad aiming at different chemical wastewater, but few reports are made on the researches and applications aiming at the wastewater treatment in hydrogen peroxide production. However, as known from the found literature, the research on wastewater produced by hydrogen peroxide mainly adopts a plurality of physical and chemical methods, but with the increasingly strict environmental protection requirements of the country, the requirements are difficult to meet only by using the physical and chemical methods, and the wastewater can reach the standard and be discharged after being treated by a combined process by combining a biochemical treatment process.
The process designed by a common sewage treatment station is a Fenton oxidation-flocculation method, the CODcr of raw water is 7000mg/L, the CODcr of outlet water can only be reduced to 400mg/L of 300 and still can not reach the discharge standard, but the invention thoroughly solves the problem of wastewater for producing hydrogen peroxide by the combined process of 'iron-carbon micro-electrolysis + Fenton oxidation + coagulating sedimentation + hydrolytic acidification + CASS (cyclic activated sludge process').
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a wastewater treatment process for producing hydrogen peroxide, and the combined process of 'iron-carbon micro-electrolysis + Fenton oxidation + coagulating sedimentation + hydrolytic acidification + CASS' adopted by the treatment process has the advantages of wide application, good treatment effect, simple operation and management and low cost, wherein the content of CODcr and phosphate is greatly reduced, so that the wastewater and sludge in the wastewater reach the discharge standard.
In order to realize the purpose, the invention adopts the technical scheme that:
a wastewater treatment process for producing hydrogen peroxide comprises the following process steps:
step 1, oxidation pretreatment: treating the wastewater by an adjusting tank, an iron-carbon micro-electrolysis tank, a Fenton oxidation tank, a coagulation oxidation tank and a sedimentation tank 1 in sequence;
step 2, biochemical treatment: the wastewater effluent from the step 1 is treated by a hydrolysis acidification tank, a CASS tank and a sedimentation tank 2 in sequence and then discharged into a clean water tank;
the oxidative pretreatment comprises the following steps:
(a) firstly, adjusting the wastewater to be consistent in wastewater concentration through an adjusting tank;
(b) the regulated wastewater enters an iron-carbon micro-electrolysis cell, the adding amount of iron powder is 8.4-11.2g and the adding amount of carbon powder is 1.2-2.4g based on each liter of wastewater, the pH value is regulated to 2.5-3.5 by sulfuric acid for reaction, and the reaction time is 3-4 h;
(c) introducing the effluent of the iron-carbon micro-electrolysis cell into a Fenton oxidation cell, wherein the adding amount of hydrogen peroxide is 3.6-5.5mL and the adding amount of ferrous sulfate is 0.6-0.8g per liter of wastewater, and adding sulfuric acid to adjust the pH value to 3-4 for reaction, wherein the reaction time is 55-65 min;
(d) introducing the effluent of the Fenton oxidation tank into a coagulation oxidation tank, firstly adding calcium hydroxide as a neutralizing agent to adjust the pH value to 10.5-11.5, adding 1.5-3g of PAM (polyacrylamide) into each liter of wastewater, and then stirring for 10-20 min;
(e) and introducing the effluent of the coagulation oxidation tank into a sedimentation tank 1 for sedimentation for 70-90 min.
A wastewater treatment process for producing hydrogen peroxide comprises the following steps:
(1) introducing the effluent from the sedimentation tank 1 into a hydrolysis acidification tank, and keeping the effluent for more than 10 days;
(2) introducing the water from the hydrolysis acidification tank into a CASS tank, wherein the retention time is 24-36h, the pH value is 6-9, and the temperature is 20-30 ℃;
(3) introducing the effluent of the CASS tank into the sedimentation tank 2, wherein the retention time is 100-120min, and discharging the effluent of the sedimentation tank 2 into a clean water tank.
Further, the concentration of hydrogen peroxide in the step 1(c) is 26.5%.
Further, the sediment left after the water is discharged from the sedimentation tank 1 in the step 1 is discharged into a sludge concentration tank for concentration for 20-50min, and is pumped into a sludge dewatering machine by a sludge pump for dewatering to obtain dry sludge.
Further, the CASS tank in the step (2) is divided into a CASS tank 1 and a CASS tank 2, the bottoms of the two tanks are provided with tubular microporous aeration systems, wherein the CASS tank 1 is subjected to anoxic reaction by weak aeration, the residence time is 10-20h, the CASS tank 2 is subjected to aerobic reaction by strong aeration, and the residence time is 14-16 h.
Further, the CASS tank 1 returns the underflow after strong aeration reaction to the weak aeration section of the CASS tank 1 by using a mixed liquid reflux pump, so that the nitrified ammonia nitrogen in the aerobic stage returns to the anoxic stage to be further denitrified, and finally the nitrified ammonia nitrogen is discharged in a nitrogen mode, wherein the reflux ratio is 70-90%.
And (3) discharging the sludge remained after water is discharged from the sedimentation tank 2 in the step (3) into a sludge tank, then refluxing into the hydrolysis acidification tank, repeating the operation process of the step (2), finally discharging into a sludge concentration tank from the sludge tank for concentration for 20-50min, and pumping into a sludge dewatering machine by using a sludge pump for dewatering to obtain dry sludge.
Further, the obtained dry sludge is applied to the aspect of preparing fertilizers or building materials.
The invention has the beneficial effects that: (1) the invention mainly solves the problem of hydrogen peroxide production wastewater treatment through a combined process of 'iron-carbon micro-electrolysis + Fenton oxidation + coagulating sedimentation + hydrolytic acidification + CASS', firstly, an iron-carbon micro-electrolysis-Fenton oxidation pretreatment process is applied to open a ring, heavy aromatics in sewage are reduced, the wastewater is easily degraded, and the load of biochemical treatment is reduced; then carrying out coagulating sedimentation treatment to remove total phosphorus; finally, a hydrolysis acidification and CASS scheme is used for deeply removing CODcr and phosphate, so that the wastewater reaches the discharge standard; the combined process has the advantages of wide application, good treatment effect, simple operation and management and low cost;
(2) the iron-carbon + Fenton catalytic oxidation technology in the combined process adopted by the invention adopts an iron-carbon micro-battery + Fenton strong oxidation system containing other impurity metals, utilizes the catalytic oxidation action of transition metals and oxidants (Fenton systems) in various iron carbons to form the oxidation-reduction action generated by potential difference, then carries out catalytic oxidation pretreatment on the wastewater, rearranges water molecules in the wastewater in the iron-carbon system according to the direction of magnetic lines of force of the micro-battery, reduces the molecular reaction barrier of organic matter activity and oxidants or reducing agents, and oxidizes organic molecular hydroxyl radicals in the wastewater, the flocculation precipitation, adsorption and complex bridging effects of ferric salt in a double-oxidation (ferrous/oxidant) Fenton reaction system are combined, so that the catalytic oxidation reaction and the catalytic condensation reaction are carried out on organic pollutants in wastewater without selection, and the content of CODcr and phosphate is greatly reduced;
(3) the pH value is adjusted to be alkaline in the coagulating sedimentation process step, the purpose of the invention is to make phosphate radicals precipitate in an alkaline environment and remove most phosphate contained in the wastewater, so that the total phosphorus content in the wastewater reaches the discharge standard, and the precipitated sludge also reaches the discharge standard.
Drawings
FIG. 1 is a process flow diagram of wastewater treatment for producing hydrogen peroxide according to the present invention.
Detailed Description
For a better understanding of the present invention, embodiments of the present invention are described in detail below with reference to examples, but those skilled in the art will understand that the following examples are only for illustrating the present invention and should not be construed as limiting the scope of the present invention.
In the embodiment, the wastewater of a chemical plant for producing hydrogen peroxide is treated, and the treatment capacity is 500m3The CODcr in the raw water is 4080mg/L, the phosphate is 20.0mg/L and the pH value is 7.
Example 1:
a wastewater treatment process for producing hydrogen peroxide comprises the following process steps:
step 1, oxidation pretreatment: treating the wastewater by an adjusting tank, an iron-carbon micro-electrolysis tank, a Fenton oxidation tank, a coagulation oxidation tank and a sedimentation tank 1 in sequence;
step 2, biochemical treatment: the wastewater effluent from the step 1 is treated by a hydrolysis acidification tank, a CASS tank and a sedimentation tank 2 in sequence and then discharged into a clean water tank;
the oxidative pretreatment comprises the following steps:
(a) firstly, adjusting the wastewater to be consistent in wastewater concentration through an adjusting tank;
(b) the regulated wastewater enters an iron-carbon micro-electrolysis cell, the adding amount of iron powder is 9.5g and the adding amount of carbon powder is 2.0g based on each liter of wastewater, the pH value is regulated to 2.5 by sulfuric acid for reaction, the reaction time is 3.5h, the CODcr is reduced to 1125mg/L, and the removal rate is 72.43%;
(c) introducing the effluent of the iron-carbon micro-electrolysis cell into a Fenton oxidation cell, wherein the adding amount of hydrogen peroxide with the concentration of 26.5 percent is 4.2mL and the adding amount of ferrous sulfate is 0.65g based on each liter of wastewater, adding sulfuric acid to adjust the pH value to 3.5, reacting for 60min, reducing the CODcr to 503mg/L, and obtaining the removal rate of 55.3%;
(d) introducing the effluent of the Fenton oxidation tank into a coagulation oxidation tank, adding calcium hydroxide as a neutralizing agent to adjust the pH value to 11, adding PAM3g into each liter of wastewater, and stirring for 15 min;
(e) and (2) introducing the effluent of the coagulation oxidation tank into a sedimentation tank 1 for sedimentation, wherein the sedimentation time is 80min, the concentration of total phosphorus (phosphate) is reduced to 0.3mg/L, the removal rate of the total phosphorus reaches 98.5%, the pollution discharge requirement is met, the sediment left after the effluent of the sedimentation tank 1 is discharged into a sludge concentration tank for concentration, the concentration time is 30min, and then the sediment is pumped into a sludge dehydrator by a sludge pump for dehydration, so that dry sludge is obtained.
A wastewater treatment process for producing hydrogen peroxide comprises the following steps:
introducing the effluent from the sedimentation tank 1 into a hydrolysis acidification tank, wherein the retention time is more than 10 days, the CODcr is 300mg/L, and the CODcr removal rate is 40%;
introducing the effluent of the hydrolysis acidification tank into a CASS tank, wherein the effluent is divided into a CASS tank 1 and a CASS tank 2, the bottoms of the two tanks adopt tubular microporous aeration systems, the CASS tank 1 adopts weak aeration to carry out anoxic reaction, the residence time is 20 hours, the CASS tank 2 adopts strong aeration to carry out aerobic reaction, the residence time is 16 hours, the pH value is 7, the temperature is 30 ℃, the CASS tank 1 also utilizes a mixed liquid reflux pump to return the lower layer liquid after the strong aeration reaction to the weak aeration section of the CASS tank 1, so that the nitrified ammonia nitrogen in the aerobic stage returns to the anoxic stage to be further denitrified, and finally the nitrified ammonia nitrogen is discharged in a nitrogen mode;
introducing the effluent of the CASS tank into a sedimentation tank 2, wherein the retention time is 100min, the CODcr is 54mg/L, the CODcr removal rate is 82%, the total phosphorus concentration is reduced to 0.231mg/L, the total phosphorus removal rate is 23%, the water quality reaches the standard, discharging the effluent of the sedimentation tank 2 into a clean water tank, discharging the sludge remained after the effluent into a sludge tank, then refluxing the sludge tank to a hydrolysis acidification tank, repeating the operation process of the step 2, finally discharging the effluent into a sludge concentration tank from the sludge tank for concentration, wherein the concentration time is 30min, and pumping the effluent into a sludge dewatering machine by using a sludge pump for dewatering to obtain dry sludge.
The obtained dry sludge is transported outside and is applied to the aspects of fertilizers and building materials.
Example 2:
a wastewater treatment process for producing hydrogen peroxide comprises the following process steps:
step 1, oxidation pretreatment: treating the wastewater by an adjusting tank, an iron-carbon micro-electrolysis tank, a Fenton oxidation tank, a coagulation oxidation tank and a sedimentation tank 1 in sequence;
step 2, biochemical treatment: the wastewater effluent from the step 1 is treated by a hydrolysis acidification tank, a CASS tank and a sedimentation tank 2 in sequence and then discharged into a clean water tank;
the oxidative pretreatment comprises the following steps:
(a) firstly, adjusting the wastewater to be consistent in wastewater concentration through an adjusting tank;
(b) the regulated wastewater enters an iron-carbon micro-electrolysis cell, the adding amount of iron powder is 8.4g and the adding amount of carbon powder is 2.4g based on each liter of wastewater, the pH value is regulated to 3.5 by sulfuric acid for reaction, the reaction time is 3h, the CODcr is reduced to 1120mg/L, and the removal rate is 72.55%;
(c) introducing the effluent of the iron-carbon micro-electrolysis tank into a Fenton oxidation tank, wherein the adding amount of hydrogen peroxide with the concentration of 26.5 percent is 3.6mL and the adding amount of ferrous sulfate is 0.8g based on each liter of wastewater, adding sulfuric acid to adjust the pH value to 3, reacting for 65min, reducing the CODcr to 515mg/L, and obtaining the removal rate of 54%;
(d) introducing the effluent of the Fenton oxidation tank into a coagulation oxidation tank, adding calcium hydroxide serving as a neutralizing agent to adjust the pH value to 10.5, adding 1.5g of PAMto each liter of wastewater, and stirring for 10 min;
(e) and introducing the effluent of the coagulation oxidation tank into a sedimentation tank 1 for sedimentation, wherein the sedimentation time is 70min, the concentration of total phosphorus (phosphate) is reduced to 0.4mg/L, the removal rate of the total phosphorus reaches 98.0%, the pollution discharge requirement is met, the sediment left after the effluent of the sedimentation tank 1 is discharged into a sludge concentration tank for concentration, the concentration time is 50min, and then the sediment is pumped into a sludge dehydrator by a sludge pump for dehydration, so that dry sludge is obtained.
A wastewater treatment process for producing hydrogen peroxide comprises the following steps:
introducing the effluent from the sedimentation tank 1 into a hydrolysis acidification tank, wherein the retention time is more than 10 days, the CODcr is 280mg/L, and the CODcr removal rate is 45.6%;
introducing the effluent of the hydrolysis acidification tank into a CASS tank, wherein the effluent is divided into a CASS tank 1 and a CASS tank 2, the bottoms of the two tanks adopt tubular microporous aeration systems, the CASS tank 1 adopts weak aeration to carry out anoxic reaction, the residence time is 10 hours, the CASS tank 2 adopts strong aeration to carry out aerobic reaction, the residence time is 14 hours, the pH value is 6, the temperature is 20 ℃, the CASS tank 1 also utilizes a mixed liquid reflux pump to return the lower layer liquid after the strong aeration reaction to the weak aeration section of the CASS tank 1, so that the nitrified ammonia nitrogen in the aerobic stage returns to the anoxic stage to be further denitrified, and finally the nitrified ammonia nitrogen is discharged in a nitrogen mode;
introducing the effluent of the CASS tank into a sedimentation tank 2, wherein the retention time is 120min, the CODcr is 60mg/L, the CODcr removal rate is 78.6%, the total phosphorus concentration is reduced to 0.312mg/L, the total phosphorus removal rate is 22%, the water quality reaches the standard, discharging the effluent of the sedimentation tank 2 into a clean water tank, discharging the sludge remained after the effluent into a sludge tank, refluxing the sludge tank into a hydrolysis acidification tank, repeating the operation process of the step 2, finally discharging the effluent from the sludge tank into a sludge concentration tank for concentration, wherein the concentration time is 20min, and pumping the effluent into a sludge dewatering machine by using a sludge pump for dewatering to obtain dry sludge.
The obtained dry sludge is transported outside and is applied to the aspects of fertilizers and building materials.
Example 3:
a wastewater treatment process for producing hydrogen peroxide comprises the following process steps:
step 1, oxidation pretreatment: treating the wastewater by an adjusting tank, an iron-carbon micro-electrolysis tank, a Fenton oxidation tank, a coagulation oxidation tank and a sedimentation tank 1 in sequence;
step 2, biochemical treatment: the wastewater effluent from the step 1 is treated by a hydrolysis acidification tank, a CASS tank and a sedimentation tank 2 in sequence and then discharged into a clean water tank;
the oxidative pretreatment comprises the following steps:
(a) firstly, adjusting the wastewater to be consistent in wastewater concentration through an adjusting tank;
(b) the regulated wastewater enters an iron-carbon micro-electrolysis cell, the adding amount of iron powder is 11.2g and the adding amount of carbon powder is 1.2g based on each liter of wastewater, the pH value is regulated to 3.0 by sulfuric acid for reaction, the reaction time is 4h, the CODcr is reduced to 1108mg/L, and the removal rate is 72.84%;
(c) introducing the effluent of the iron-carbon micro-electrolysis tank into a Fenton oxidation tank, wherein the adding amount of hydrogen peroxide with the concentration of 26.5 percent is 5.5mL and the adding amount of ferrous sulfate is 0.6g based on each liter of wastewater, adding sulfuric acid to adjust the pH value to 4, reacting for 55min, reducing the CODcr to 496mg/L and obtaining the removal rate of 55.2 percent;
(d) introducing the effluent of the Fenton oxidation tank into a coagulation oxidation tank, adding calcium hydroxide serving as a neutralizing agent to adjust the pH value to 11.5, adding 2.5g of PAM2 per liter of wastewater, and stirring for 20 min;
(e) and introducing the effluent of the coagulation oxidation tank into a sedimentation tank 1 for sedimentation, wherein the sedimentation time is 90min, the concentration of total phosphorus (phosphate) is reduced to 0.25mg/L, the removal rate of the total phosphorus reaches 98.75%, the pollution discharge requirement is met, the sediment left after the effluent of the sedimentation tank 1 is discharged into a sludge concentration tank for concentration, the concentration time is 20min, and then the sediment is pumped into a sludge dehydrator by a sludge pump for dehydration, so that dry sludge is obtained.
A wastewater treatment process for producing hydrogen peroxide comprises the following steps:
introducing the effluent from the sedimentation tank 1 into a hydrolysis acidification tank, wherein the retention time is more than 10 days, the CODcr is 275mg/L, and the CODcr removal rate is 44.6%;
introducing the effluent of the hydrolysis acidification tank into a CASS tank, wherein the effluent is divided into a CASS tank 1 and a CASS tank 2, the bottoms of the two tanks adopt tubular microporous aeration systems, the CASS tank 1 adopts weak aeration to carry out anoxic reaction, the residence time is 15h, the CASS tank 2 adopts strong aeration to carry out aerobic reaction, the residence time is 15h, the pH value is 9, the temperature is 25 ℃, the CASS tank 1 also utilizes a mixed liquid reflux pump to return the lower layer liquid after the strong aeration reaction to the weak aeration section of the CASS tank 1, so that the nitrified ammonia nitrogen in the aerobic stage returns to the anoxic stage to be further denitrified, and finally the nitrified ammonia nitrogen is discharged in a nitrogen mode;
introducing the effluent of the CASS tank into a sedimentation tank 2, wherein the retention time is 110min, the CODcr is 59mg/L, the CODcr removal rate is 78.5%, the total phosphorus concentration is reduced to 0.2mg/L, the total phosphorus removal rate is 20%, the water quality reaches the standard, discharging the effluent of the sedimentation tank 2 into a clean water tank, discharging the sludge remained after the effluent into a sludge tank, refluxing the sludge tank into a hydrolysis acidification tank, repeating the operation process of the step 2, finally discharging the effluent from the sludge tank into a sludge concentration tank for concentration, wherein the concentration time is 50min, and pumping the effluent into a sludge dewatering machine by using a sludge pump for dewatering to obtain dry sludge.
The obtained dry sludge is transported outside and is applied to the aspects of fertilizers and building materials.
The CODcr content, CODcr removal rate, total phosphorus and total phosphorus removal rate obtained by iron-carbon microelectrolysis, Fenton oxidation, coagulating sedimentation, hydrolytic acidification and CASS process treatment in the above examples are summarized in the following table.
From the above table, it can be seen that the combined process of "iron-carbon microelectrolysis + fenton oxidation + coagulating sedimentation + hydrolytic acidification + CASS" adopted by the invention, wherein the CODcr occupies 1/8 of the original wastewater after the treatment of the iron-carbon-fenton system, thereby greatly reducing the CODcr, wherein the pH value is adjusted to be alkaline in the coagulating sedimentation process step, the purpose is to precipitate phosphate radicals in an alkaline environment, remove most of phosphate contained in the wastewater, and finally the CODcr and the phosphate are deeply removed by using the scheme of hydrolytic acidification + CASS, so that the wastewater reaches the discharge standard.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above-described embodiments. Those skilled in the art should appreciate that many modifications and variations are possible in light of the above teaching without departing from the scope of the invention.
Claims (8)
1. A wastewater treatment process for producing hydrogen peroxide is characterized by comprising the following process steps:
step 1, oxidation pretreatment: treating the wastewater by an adjusting tank, an iron-carbon micro-electrolysis tank, a Fenton oxidation tank, a coagulation oxidation tank and a sedimentation tank 1 in sequence;
step 2, biochemical treatment: the wastewater effluent from the step 1 is treated by a hydrolysis acidification tank, a CASS tank and a sedimentation tank 2 in sequence and then discharged into a clean water tank;
the oxidative pretreatment comprises the following steps:
(a) firstly, adjusting the wastewater to be consistent in wastewater concentration through an adjusting tank;
(b) the regulated wastewater enters an iron-carbon micro-electrolysis cell, the adding amount of iron powder is 8.4-11.2g and the adding amount of carbon powder is 1.2-2.4g based on each liter of wastewater, the pH value is regulated to 2.5-3.5 by sulfuric acid for reaction, and the reaction time is 3-4 h;
(c) introducing the effluent of the iron-carbon micro-electrolysis cell into a Fenton oxidation cell, wherein the adding amount of hydrogen peroxide is 3.6-5.5mL and the adding amount of ferrous sulfate is 0.6-0.8g per liter of wastewater, and adding sulfuric acid to adjust the pH value to 3-4 for reaction, wherein the reaction time is 55-65 min;
(d) introducing the effluent of the Fenton oxidation tank into a coagulation oxidation tank, adding calcium hydroxide as a neutralizing agent to adjust the pH value to 10.5-11.5, adding 1.5-3g of PAM (polyacrylamide) into each liter of wastewater, and stirring for 10-20 min;
(e) and introducing the effluent of the coagulation oxidation tank into a sedimentation tank 1 for sedimentation for 70-90 min.
2. The wastewater treatment process for producing hydrogen peroxide according to claim 1, wherein the biochemical treatment comprises the following steps:
(1) introducing the effluent from the sedimentation tank 1 into a hydrolysis acidification tank, and keeping the effluent for more than 10 days;
(2) introducing the water from the hydrolysis acidification tank into a CASS tank, wherein the retention time is 24-36h, the pH value is 6-9, and the temperature is 20-30 ℃;
(3) introducing the effluent of the CASS tank into the sedimentation tank 2, wherein the retention time is 100-120min, and discharging the effluent of the sedimentation tank 2 into a clean water tank.
3. The wastewater treatment process for producing hydrogen peroxide according to claim 1, wherein the concentration of hydrogen peroxide in the step 1(c) is 26.5%.
4. The wastewater treatment process for producing hydrogen peroxide according to claim 1, wherein in the step 1, the precipitate left after the water is discharged from the sedimentation tank 1 is discharged into a sludge concentration tank for concentration for 20-50min, and then is pumped into a sludge dewatering machine by a sludge pump for dewatering to obtain dry sludge.
5. The wastewater treatment process for producing hydrogen peroxide according to claim 2, wherein the CASS tank in the step (2) is divided into a CASS tank 1 and a CASS tank 2, and the bottoms of the two tanks are provided with tubular microporous aeration systems, wherein the CASS tank 1 is subjected to an anoxic reaction by weak aeration for a residence time of 10-20h, and the CASS tank 2 is subjected to an aerobic reaction by strong aeration for a residence time of 14-16 h.
6. The wastewater treatment process for producing hydrogen peroxide according to claim 5, wherein the CASS tank 1 returns the underflow after the strong aeration reaction to the weak aeration section of the CASS tank 1 by using a mixed liquor reflux pump, so that the ammonia nitrogen which has been nitrified in the aerobic stage returns to the anoxic stage, is further denitrified, and is finally discharged in a nitrogen manner.
7. The wastewater treatment process for producing hydrogen peroxide according to claim 2, characterized in that the sludge left after the water is discharged from the sedimentation tank 2 in the step (3) is discharged into a sludge tank, then flows back to the hydrolysis acidification tank, the operation process of the step 2 is repeated, finally the sludge is discharged into a sludge concentration tank from the sludge tank for concentration for 20-50min, and then the sludge is pumped into a sludge dewatering machine by a sludge pump for dewatering to obtain dry sludge.
8. A process for the treatment of wastewater in the production of hydrogen peroxide according to claim 4 or 7, characterized in that the obtained dry sludge is used in the preparation of fertilizers or building materials.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911242605.0A CN112919726A (en) | 2019-12-06 | 2019-12-06 | Wastewater treatment process for producing hydrogen peroxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911242605.0A CN112919726A (en) | 2019-12-06 | 2019-12-06 | Wastewater treatment process for producing hydrogen peroxide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112919726A true CN112919726A (en) | 2021-06-08 |
Family
ID=76161717
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911242605.0A Pending CN112919726A (en) | 2019-12-06 | 2019-12-06 | Wastewater treatment process for producing hydrogen peroxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112919726A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114368876A (en) * | 2022-01-10 | 2022-04-19 | 辽宁大学 | Process for treating printing and dyeing wastewater by using chemical-biofilm method |
| CN115304221A (en) * | 2022-08-24 | 2022-11-08 | 菏泽市巨丰新能源有限公司 | Wastewater treatment process for producing hydrogen peroxide |
| CN115490391A (en) * | 2022-08-09 | 2022-12-20 | 杭州鲲宸环境科技有限公司 | Benzene series wastewater treatment method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203938522U (en) * | 2014-05-28 | 2014-11-12 | 南京绿岛环境工程有限公司 | A kind of CASS device that promotes the high ammonia nitrogen high phosphorus of high salt high-COD waste water processing efficiency |
| CN106277589A (en) * | 2016-08-25 | 2017-01-04 | 南京大学盐城环保技术与工程研究院 | A kind of system and method utilizing ferrum carbon Fenton pretreatment UBF A/O to process waste water from dyestuff |
-
2019
- 2019-12-06 CN CN201911242605.0A patent/CN112919726A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203938522U (en) * | 2014-05-28 | 2014-11-12 | 南京绿岛环境工程有限公司 | A kind of CASS device that promotes the high ammonia nitrogen high phosphorus of high salt high-COD waste water processing efficiency |
| CN106277589A (en) * | 2016-08-25 | 2017-01-04 | 南京大学盐城环保技术与工程研究院 | A kind of system and method utilizing ferrum carbon Fenton pretreatment UBF A/O to process waste water from dyestuff |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114368876A (en) * | 2022-01-10 | 2022-04-19 | 辽宁大学 | Process for treating printing and dyeing wastewater by using chemical-biofilm method |
| CN115490391A (en) * | 2022-08-09 | 2022-12-20 | 杭州鲲宸环境科技有限公司 | Benzene series wastewater treatment method |
| CN115490391B (en) * | 2022-08-09 | 2023-10-17 | 杭州鲲宸环境科技有限公司 | Benzene series wastewater treatment method |
| CN115304221A (en) * | 2022-08-24 | 2022-11-08 | 菏泽市巨丰新能源有限公司 | Wastewater treatment process for producing hydrogen peroxide |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107555701B (en) | Low-cost coking wastewater treatment method | |
| CN106554126B (en) | Deep standard-reaching treatment method and system for reverse osmosis concentrated water | |
| CN102730862B (en) | Sewage treatment method in synthetic rubber production | |
| CN112919726A (en) | Wastewater treatment process for producing hydrogen peroxide | |
| CN104478157A (en) | Landfill leachate nanofiltration concentrate treatment method | |
| CN104961304A (en) | High-concentration fluorine chemical wastewater treatment technology | |
| CN111439894A (en) | Treatment process of landfill leachate | |
| CN109231715A (en) | Method for treating chemical ammonia distillation wastewater | |
| CN109626739A (en) | A kind of Denitrification of Coking Wastewater method | |
| CN113003882A (en) | Treatment process of high-ammonia nitrogen high-salt landfill leachate | |
| CN115180767A (en) | Treatment method for realizing zero discharge of high-concentration pesticide wastewater | |
| CN113185059A (en) | Advanced treatment method for printed circuit board wastewater | |
| CN112939352A (en) | Treatment method of comprehensive sewage of industrial park | |
| CN114105396A (en) | Process method for efficiently treating Lyocell short fiber wastewater | |
| CN111453923A (en) | Treatment equipment and process for landfill leachate membrane concentrated solution | |
| CN108623096B (en) | Treatment process of high-concentration degradation-resistant sewage | |
| CN116119888A (en) | Combined treatment system and treatment method for post-concentration liquid of landfill leachate membrane | |
| CN115536206B (en) | Advanced treatment combined process for chemical refractory sewage | |
| CN115259573A (en) | Treatment method of high-sulfate organic wastewater in petroleum refining industry | |
| CN113816561A (en) | Treatment method of quaternary ammonium salt production wastewater | |
| CN203960004U (en) | A kind of printing ink wastewater iron carbon treatment facility | |
| CN111470722A (en) | Treatment method of rubber processing wastewater difficult to biodegrade | |
| CN112759151A (en) | Movable integrated landfill leachate treatment system and purification method thereof | |
| CN113526778A (en) | Treatment process of high-concentration industrial wastewater | |
| CN220098801U (en) | Treatment system of refractory industrial wastewater |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210608 |
|
| RJ01 | Rejection of invention patent application after publication |