CN113087249B - System and method for treating wastewater in H acid production - Google Patents
System and method for treating wastewater in H acid production Download PDFInfo
- Publication number
- CN113087249B CN113087249B CN201911333993.3A CN201911333993A CN113087249B CN 113087249 B CN113087249 B CN 113087249B CN 201911333993 A CN201911333993 A CN 201911333993A CN 113087249 B CN113087249 B CN 113087249B
- Authority
- CN
- China
- Prior art keywords
- tank
- waste water
- oxidation
- wastewater
- oxidation reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 105
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 32
- APRRQJCCBSJQOQ-UHFFFAOYSA-N 4-amino-5-hydroxynaphthalene-2,7-disulfonic acid Chemical compound OS(=O)(=O)C1=CC(O)=C2C(N)=CC(S(O)(=O)=O)=CC2=C1 APRRQJCCBSJQOQ-UHFFFAOYSA-N 0.000 title claims abstract 5
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 100
- 230000003647 oxidation Effects 0.000 claims abstract description 71
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 26
- 238000001914 filtration Methods 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 12
- 238000004062 sedimentation Methods 0.000 claims description 11
- 239000002699 waste material Substances 0.000 claims description 9
- 238000006386 neutralization reaction Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 6
- 238000004042 decolorization Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 18
- 238000006243 chemical reaction Methods 0.000 abstract description 16
- 238000004065 wastewater treatment Methods 0.000 abstract description 8
- 230000005501 phase interface Effects 0.000 abstract description 7
- QPILZZVXGUNELN-UHFFFAOYSA-M sodium;4-amino-5-hydroxynaphthalene-2,7-disulfonate;hydron Chemical compound [Na+].OS(=O)(=O)C1=CC(O)=C2C(N)=CC(S([O-])(=O)=O)=CC2=C1 QPILZZVXGUNELN-UHFFFAOYSA-M 0.000 description 32
- 239000012071 phase Substances 0.000 description 16
- 238000009279 wet oxidation reaction Methods 0.000 description 11
- 239000007791 liquid phase Substances 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 7
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 239000000839 emulsion Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000012429 reaction media Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000013049 sediment Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 238000002848 electrochemical method Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 231100000086 high toxicity Toxicity 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 230000001699 photocatalysis Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- SGHZXLIDFTYFHQ-UHFFFAOYSA-L Brilliant Blue Chemical compound [Na+].[Na+].C=1C=C(C(=C2C=CC(C=C2)=[N+](CC)CC=2C=C(C=CC=2)S([O-])(=O)=O)C=2C(=CC=CC=2)S([O-])(=O)=O)C=CC=1N(CC)CC1=CC=CC(S([O-])(=O)=O)=C1 SGHZXLIDFTYFHQ-UHFFFAOYSA-L 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 241000282414 Homo sapiens Species 0.000 description 1
- 239000000980 acid dye Substances 0.000 description 1
- RZUBARUFLYGOGC-MTHOTQAESA-L acid fuchsin Chemical compound [Na+].[Na+].[O-]S(=O)(=O)C1=C(N)C(C)=CC(C(=C\2C=C(C(=[NH2+])C=C/2)S([O-])(=O)=O)\C=2C=C(C(N)=CC=2)S([O-])(=O)=O)=C1 RZUBARUFLYGOGC-MTHOTQAESA-L 0.000 description 1
- YJVBLROMQZEFPA-UHFFFAOYSA-L acid red 26 Chemical compound [Na+].[Na+].CC1=CC(C)=CC=C1N=NC1=C(O)C(S([O-])(=O)=O)=CC2=CC(S([O-])(=O)=O)=CC=C12 YJVBLROMQZEFPA-UHFFFAOYSA-L 0.000 description 1
- POJOORKDYOPQLS-UHFFFAOYSA-L barium(2+) 5-chloro-2-[(2-hydroxynaphthalen-1-yl)diazenyl]-4-methylbenzenesulfonate Chemical compound [Ba+2].C1=C(Cl)C(C)=CC(N=NC=2C3=CC=CC=C3C=CC=2O)=C1S([O-])(=O)=O.C1=C(Cl)C(C)=CC(N=NC=2C3=CC=CC=C3C=CC=2O)=C1S([O-])(=O)=O POJOORKDYOPQLS-UHFFFAOYSA-L 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000003712 decolorant Substances 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000000982 direct dye Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- AOMZHDJXSYHPKS-UHFFFAOYSA-L disodium 4-amino-5-hydroxy-3-[(4-nitrophenyl)diazenyl]-6-phenyldiazenylnaphthalene-2,7-disulfonate Chemical compound [Na+].[Na+].[O-]S(=O)(=O)C1=CC2=CC(S([O-])(=O)=O)=C(N=NC=3C=CC=CC=3)C(O)=C2C(N)=C1N=NC1=CC=C([N+]([O-])=O)C=C1 AOMZHDJXSYHPKS-UHFFFAOYSA-L 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- MCJGNVYPOGVAJF-UHFFFAOYSA-N quinolin-8-ol Chemical compound C1=CN=C2C(O)=CC=CC2=C1 MCJGNVYPOGVAJF-UHFFFAOYSA-N 0.000 description 1
- 239000000985 reactive dye Substances 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 210000002268 wool Anatomy 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
- 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
- C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
-
- 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
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- 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
-
- 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
- C02F1/5281—Installations for water purification using chemical agents
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- 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
- C02F2101/38—Organic compounds containing nitrogen
-
- 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
- C02F2101/40—Organic compounds containing sulfur
-
- 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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention provides a system and a method for treating wastewater in H acid production. The processing system comprises: the system comprises a raw water tank, a waste water heat exchanger, a waste water heater and an oxidation reaction device which are connected in sequence, wherein the waste water heat exchanger is provided with a material inlet, a material outlet, a heat source inlet and a heat source outlet; the oxidized water from the oxidation reaction device enters the wastewater heat exchanger from the heat source inlet, the heat source outlet is connected with a finished product tank, the material inlet is connected with the raw water tank, and the material outlet is connected with the wastewater heater; the oxidation reaction device comprises a primary oxidation reactor and a secondary oxidation reactor which are sequentially connected, and oxidation water after oxidation treatment of the primary oxidation reactor continuously enters the secondary oxidation reactor for oxidation treatment. The treatment system improves the contact of the reaction phase interface by arranging the micro-interface generation system, and can ensure good wastewater treatment effect under the condition of mild operation conditions.
Description
Technical Field
The invention relates to the field of wastewater treatment in H acid production, in particular to a system and a method for treating wastewater in H acid production.
Background
H acid is a chemical substance and is mainly used for producing acid, direct and reactive dyes, such as more than 90 types of acid fuchsin 6B, acid scarlet G, acid black 10B, direct black, reactive brilliant red K-2BP, reactive purple K-3R, reactive brilliant blue K-R and the like, and the dyes are used for dyeing wool fabrics and cotton fabrics. Can also be used for producing drugs, which can generate a large amount of waste water and waste liquid in the synthetic preparation process, and the waste water is characterized in that: high concentration, high color, high salt content, high suspended matter content and high toxicity. The pH value of the generated waste water and waste liquid is generally between 7 and 9, the COD is about 10 ten thousand mg/L, the content of organic matters is higher, the waste water and waste liquid is typical industrial waste water containing organic compounds which are difficult to degrade, and if the waste water and waste liquid are not well treated subsequently, the waste water and waste liquid have great harm to the environment and human beings and pollute the environment.
In the prior art, the treatment method for the waste liquid mainly depends on an adsorption method, a coagulation method, an extraction method, a photocatalytic oxidation method, a catalytic wet oxidation method, an ultrasonic degradation method, a stripping method, a membrane separation method, an electrochemical method and various comprehensive treatment processes, but the treatment processes are relatively complex in operation, most of the waste water treated by the treatment processes does not reach the standard, and the waste water treated by the treatment processes can reach the emission standard after further deep treatment, so that the operation cost is increased invisibly, the operation period is prolonged, and the cost of matched manpower and material resources is increased.
The wet oxidation technology is adopted, under the conditions of high temperature and high pressure, the temperature can reach 150-.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The first purpose of the invention is to provide a treatment system for wastewater in H acid production, which improves the mass transfer effect between two phases by arranging a micro-interface generator, the micro-interface generator can break bubbles into micron-level bubbles, so as to increase the phase interface area between a gas phase and a liquid phase, so that oxygen can be better fused with the wastewater in H acid production to form gas-liquid emulsion, the oxidation reaction efficiency is improved, the retention time of the oxygen in the wastewater in H acid production is longer, the reaction efficiency is further improved, the mass transfer effect of a reaction phase interface is increased, the operation temperature and pressure can be properly reduced, a series of potential safety hazards caused by high temperature and high pressure are avoided, and the treatment system has the advantages of low energy consumption, low cost, excellent treatment effect and the like.
The second purpose of the invention is to provide a method for treating wastewater in H acid production by using the treatment system, the treatment method is simple and convenient to operate, the operation condition is milder, the energy consumption is low, and the removal rate of harmful substances in the treated wastewater in H acid production can reach 99%.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
the invention provides a wastewater treatment system for treating wastewater in H acid production, which comprises: the system comprises a raw water tank, a waste water heat exchanger, a waste water heater and an oxidation reaction device which are connected in sequence, wherein the waste water heat exchanger is provided with a material inlet, a material outlet, a heat source inlet and a heat source outlet;
the oxidized water from the oxidation reaction device enters the wastewater heat exchanger from the heat source inlet, the heat source outlet is connected with a finished product tank, the material inlet is connected with the raw water tank, and the material outlet is connected with the wastewater heater;
the oxidation reaction device comprises a primary oxidation reactor and a secondary oxidation reactor which are sequentially connected, and oxidation water after oxidation treatment of the primary oxidation reactor continuously enters the secondary oxidation reactor for oxidation treatment;
the outer side of the secondary oxidation reactor is provided with a micro-interface generator for dispersing broken gas into bubbles, the micro-interface generator is provided with an air inlet and a waste water inlet, waste water which enters from the waste water inlet is recycled from the oxidation reaction device, fresh supplementary air or oxygen enters from the air inlet, and the structure of the primary oxidation reactor is consistent with that of the secondary oxidation reactor.
The wastewater in the H acid production required to be treated by the invention is characterized in that: high concentration, high chroma, high salt content, high suspended matter, high toxicity, high COD value, high salt content and poor biodegradability, and the prior art mainly adopts an adsorption method, a coagulation method, an extraction method, a photocatalytic oxidation method, a catalytic wet oxidation method, an ultrasonic degradation method, a stripping method, a membrane separation method, an electrochemical method and various comprehensive treatment processes, wherein the wet oxidation method is commonly used, the temperature can reach 150-, this reduces the reaction efficiency and also increases the processing cost.
The invention aims to solve the technical problems and provides a treatment system specially for treating wastewater in H acid production, wherein a micro-interface generator is arranged on the outer side of an oxidation reaction device, air or oxygen entering the oxidation reaction device is broken and dispersed into bubbles, so that the bubbles and the wastewater form gas-liquid emulsion, the phase interface area between the gas and the wastewater is increased, the reaction efficiency is further improved, and the oxygen is fused into the wastewater as much as possible after the mass transfer effect of a reaction phase interface is increased, so that the operation and control conditions of temperature and pressure can be fully reduced after the mass transfer effect is improved, the pressure is between 1.8 and 2.4MPa, and the temperature is between 130 and 135 ℃, and the wastewater can be treated under mild operation conditions.
In addition, the micro-interface generator is preferably a pneumatic micro-interface generator, compressed air or oxygen is introduced into the micro-interface generator, and then the compressed air or oxygen is contacted with wastewater and then is crushed into a micro-bubble form, so that the mass transfer effect is improved.
The invention adopts two-stage oxidation reactors, and aims to improve the effect of wet oxidation, and each oxidation reactor adopts an external mode to arrange a micro-interface generator, and the external mode is adopted because the mode is convenient to maintain, easy to disassemble and convenient to operate.
Because the micro-interface generator adopts an external mode, a liquid phase and a gas phase need to be simultaneously connected into the micro-interface generator, waste liquid circulating pipelines are arranged on the side walls of the primary oxidation reactor and the secondary oxidation reactor and are used for introducing the circulated waste water into the micro-interface generator from a waste water inlet, fresh supplemented air or oxygen enters the micro-interface generator from an air inlet, and the gas phase and the liquid phase are contacted in the micro-interface generator and are crushed into micro-bubbles.
It is understood by those skilled in the art that a Micro Interfacial Generator (MIG) can break up a gas phase and/or a liquid phase in a multi-phase reaction medium into Micro bubbles and/or Micro droplets with a diameter of micron level in a Micro Interfacial Generator through a mechanical microstructure and/or a turbulent microstructure in a preset action mode before the multi-phase reaction medium enters a reactor, so as to increase a phase boundary mass transfer area between the gas phase and/or the liquid phase and/or the solid phase during a reaction process, improve mass transfer efficiency between reaction phases, and strengthen a multi-phase reaction within a preset temperature and/or a preset pressure range.
The preset action mode can be selected from one or more of a micro-channel action mode, a field force action mode and a mechanical energy action mode;
the micro-channel has the action mode that a micro-structure of a flow channel is constructed, so that a gas phase and/or a liquid phase passing through the micro-channel are/is broken into micro-bubbles and/or micro-droplets; the field force action mode is that the external field force is used for acting in a non-contact mode to input energy to the fluid, so that the fluid is broken into the micro-bubbles or micro-droplets; the mechanical energy action mode is to convert the mechanical energy of the fluid into the surface energy of the bubbles or the liquid drops so as to break the bubbles or the liquid drops into the micro-bubbles or the micro-liquid drops.
The micro-interface generator can be used for reactions of gas-liquid, liquid-solid, gas-liquid, gas-liquid-solid, liquid-solid and other multi-phase reaction media, the specific structure of the micro-interface generator can be freely selected according to different flowing media, and corresponding records are also provided in patents and documents before the specific structure and specific functional action of the micro-interface generator, and additional details are not provided herein. Meanwhile, the number and the position of the air inlets can be adjusted according to the actual engineering requirements and the factors such as the height, the length, the diameter, the waste water flow rate and the like of the oxidation reaction device in the system, so that the better air supply effect is achieved, and the degradation rate of wet oxidation on waste water treatment is improved.
In addition, in the scheme of the invention, in order to recover the resources in the wastewater in the H acid production, reduce the difficulty of wet oxidation of the wastewater in the H acid production and improve the COD removal rate of the wastewater, the wastewater in the H acid production is preferably pretreated before the wet oxidation, the pretreatment method comprises pretreatment means such as neutralization, precipitation, decoloration and the like, and other pretreatment modes can be correspondingly adopted according to actual working conditions.
Therefore, the system for treating the wastewater in the H acid production also comprises a neutralization tank, a sedimentation tank, a first filtering tank, a decoloring tank and a second filtering tank. The raw water tank is sequentially connected with the neutralization tank, the sedimentation tank, the first filtering tank, the decoloring tank and the second filtering tank.
The wastewater in the hydroxyquinoline production is high in chroma, so that the decolorization is also important, the treatment system firstly carries out a filtration link, then an oxidation decolorizing agent and a flocculating agent are added into a decolorizing tank for decolorization, and the wastewater after the decolorization treatment is filtered in a second filtering tank and then can enter a subsequent wet oxidation section for further organic matter removal operation.
Preferably, the treatment system further comprises a dryer, and the bottoms of the sedimentation tank and the second filtering tank are connected with the dryer through pipelines so as to be used for drying sedimentation and filtering residues. The bottom of sedimentation tank and second filtering ponds has partly sediment and residue, with this part waste material for the convenience of subsequent innocent treatment after discharging from the bottom, increased the drying apparatus drying process, sediment and residue after the drying process can realize taking out rapidly, have improved work efficiency.
Preferably, a delivery pump is arranged between the second filtering tank and the wastewater heat exchanger.
Preferably, the side upper part of the secondary oxidation reactor is provided with an oxidized water outlet, and the oxidized water outlet is connected with the heat source inlet through a pipeline.
Preferably, the processing system further comprises an air compression device, the air compression device is communicated with the air inlet, and air or compressed oxygen compressed by the air compression device enters the micro-interface generator through the air inlet to be dispersed and smashed. Preferably, the compressed air or oxygen from the air compressor is heated in a gas heating device, preferably a heat exchanger, before entering the micro-interface generator, and therefore a gas heating device is also provided in the conduit connecting between the air compressor and the inlet of the micro-interface generator.
Preferably, the treatment system further comprises a gas-liquid separation tank, and the oxidized water from the oxidized water outlet enters the gas-liquid separation tank to realize gas-liquid separation, and then enters the wastewater heat exchanger from the heat source inlet.
The treatment system can be provided with the pump body on the corresponding connecting pipeline according to actual requirements.
The treatment system for the wastewater in the H acid production has high treatment capacity, and after the treatment by the treatment system, the treatment system can ensure that the wastewater has a higher treatment effect under the condition of lower energy consumption, and the removal rate of harmful substances can reach 99%.
In addition, the invention also provides a method for treating the wastewater in the H acid production, which comprises the following steps:
heating the wastewater in the H acid production, then feeding the heated wastewater into an oxidation reaction device, and simultaneously introducing compressed air or compressed oxygen into the oxidation reaction device to perform oxidation reaction;
the compressed air or the compressed oxygen entering the oxidation reaction device is firstly dispersed and crushed by the micro-interface generating system.
The reaction temperature of the oxidation reaction is between 130 ℃ and 135 ℃ and the reaction pressure is between 1.8 and 2.4MPa, and the operation temperature and pressure are fully reduced by adopting a micro-interface generation system, so that the whole operation process is milder, and the operation safety is also improved.
The method for treating the wastewater in the H acid production has the advantages of simple and convenient operation, milder operation condition and low energy consumption, the removal rate of harmful substances and COD of the treated wastewater in the H acid production can reach 99 percent, the discharge of industrial wastes is reduced, the method is more environment-friendly, and the method is worthy of wide popularization and application.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the treatment system for the wastewater in the H acid production, the mass transfer effect between two phases is improved by arranging the micro-interface generator, the micro-interface generator can break bubbles into micron-level bubbles, so that the phase interface area between a gas phase and a liquid phase is increased, oxygen can be better fused with the wastewater in the H acid production to form a gas-liquid emulsion, and the oxidation reaction efficiency is improved;
(2) according to the wastewater treatment system, the two-stage oxidation reactors are connected in series for wet oxidation, so that the wastewater treatment effect is improved, and the positions of the micro-interface generators are reasonably arranged, so that the overhaul and the disassembly are more convenient;
(3) the treatment system of the invention fully reduces the operation temperature and the operation pressure, the operation temperature is basically between 130 ℃ and 135 ℃, the reaction pressure is maintained between 1.8 MPa and 2.4MPa, and the effects of low energy consumption and low operation cost are realized.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of a wastewater treatment system in H acid production according to an embodiment of the present invention.
Description of the drawings:
10-a raw water tank; 20-a neutralization tank;
30-a sedimentation tank; 40-a first filtration tank;
50-a decoloring tank; 60-a second filtering tank;
70-a primary oxidation reactor; 80-wastewater heat exchanger;
81-material inlet; 82-a material outlet;
83-inlet of heat source; 84-outlet of heat source;
90-a waste water heater; 100-a secondary oxidation reactor;
101-an oxidized water outlet; 102-a micro-interface generator;
1021-an air intake; 1022-a wastewater inlet;
103-gas heating means; 104-air compression means;
105-a vent; 110-a gas-liquid separation tank;
120-a delivery pump; 130-finished product tank.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to more clearly illustrate the technical solution of the present invention, the following description is made in the form of specific embodiments.
Examples
Referring to fig. 1, a system for treating wastewater in H acid production according to an embodiment of the present invention includes a raw water tank 10, a wastewater heat exchanger 80, a wastewater heater 90, a primary oxidation reactor 70, a secondary oxidation reactor 100, and an air compressor 104, which are connected in sequence.
The waste water heat exchanger 80 is respectively provided with a material inlet 81, a material outlet 82, a heat source inlet 83 and a heat source outlet 84, oxidation water which sequentially passes through the primary oxidation reactor 70 and the secondary oxidation reactor 100 enters the waste water heat exchanger 80 from the heat source inlet 83, the heat source outlet 84 is connected with the finished product tank 130, the material inlet 81 is connected with the raw water tank 10, the material outlet 82 is connected with the waste water heater 90, and in the waste water heat exchanger 50, the oxidation water after the reaction of the primary oxidation reactor 70 and the secondary oxidation reactor 100 exchanges heat with waste water in H acid production to be treated, so that the effect of fully utilizing energy is achieved.
The micro-interface generator 102 is arranged on the outer sides of the primary oxidation reactor 70 and the secondary oxidation reactor 100, the micro-interface generator 102 is used for dispersing broken gas into bubbles, the micro-interface generator 102 is respectively provided with a gas inlet 1021 and a waste water inlet 1022, the air compression device 104 is communicated with the gas inlet 1021, and air or oxygen compressed by the air compression device 104 enters the micro-interface generator 102 through the gas inlet 1021, so that the crushing and dispersion of the gas are realized, and the mass transfer effect between the two phases is enhanced. The air compressor 104 is preferably an air compressor. Air or oxygen compressed by the air compressor is preheated by the gas heating device 103 and then enters the micro-interface generator 102, so that the reaction efficiency is improved. The type of air compressor can be selected as a centrifugal air compressor, and the type of compressor is low in cost and convenient to use. The liquid phase from the waste water inlet 1022 is waste water recycled from the oxidation reaction apparatus 100.
The micro-interface generator 102 is of a pneumatic type, and the micro-interface generator 102 may be implemented by way of pipe reinforcement.
The side upper parts of the primary oxidation reactor 70 and the secondary oxidation reactor 100 are provided with an oxidized water outlet 101, oxidized water from the oxidized water outlet 101 is subjected to gas-liquid separation in a gas-liquid separation tank 110, and then is discharged from the bottom of the gas-liquid separation tank 110 and is connected with a heat source inlet 83 through a pipeline, so that the oxidized water is conveyed to a waste water heat exchanger 80 for heat exchange, and is cooled down after the heat exchange and conveyed to a finished product tank 130 for storage. The water from the product tank 130 may continue to undergo subsequent desalination, which may be accomplished by conventional means known in the art. The top of the primary oxidation reactor 70 and the secondary oxidation reactor 100 are provided with a vent 105. The structure of the primary oxidation reactor 70 is identical to that of the secondary oxidation reactor 100.
The treatment system also comprises a pretreatment system comprising a neutralization tank 20, a sedimentation tank 30, a first filtering tank 40, a decoloring tank 50 and a second filtering tank 60, and the wastewater after impurities are separated by the pretreatment system enters a wastewater heat exchanger 80 through a delivery pump 120.
In the above embodiment, the number of the micro-interface generators is not limited, and in order to increase the dispersion and mass transfer effects, additional micro-interface generators may be additionally provided, especially, the installation position of the micro-interface generator is not limited, and the micro-interface generator may be external or internal, and when the micro-interface generator is internal, the micro-interface generator may be installed on the side wall in the kettle in a manner of being oppositely arranged, so as to realize the opposite flushing of micro-bubbles coming out from the outlet of the micro-interface generator.
In the two embodiments, the number of the pump bodies is not specifically required, and the pump bodies can be arranged at corresponding positions according to requirements.
The working process and principle of the wastewater treatment system in H acid production according to the present invention are briefly described as follows:
firstly, after nitrogen gas purges pipelines of a raw water tank 10, a waste water heat exchanger 80, a waste water heater 90, a primary oxidation reactor 70 and a secondary oxidation reactor 100 and the inside of the oxidation reactor, waste water in H acid production in the raw water tank 10 is sent to a neutralization tank 20, sulfuric acid is added to neutralize, the neutralized waste water enters a sedimentation tank 30, and the coagulant is added to precipitate, and then the next link of treatment is continued.
Subsequently, after the wastewater is filtered in the first filtering tank 40, an oxidation decolorant and a flocculant are added to the decoloring tank 50 to perform decoloring treatment, and then the wastewater is filtered in the second filtering tank 60. The bottoms of the sedimentation tank 30 and the second filtering tank 60 are connected with a dryer through pipelines for drying sediment and filtering residues.
Then, the wastewater in the H acid production is sent into a wastewater heat exchanger 80 through a delivery pump 120 for heat exchange, and then is further heated through a wastewater heater 90, the heated wastewater in the H acid production sequentially passes through a primary oxidation reactor 70 and a secondary oxidation reactor 100 for oxidation treatment, compressed air or compressed oxygen enters from a micro-interface generator 102 on the side of the oxidation reactor, and is dispersed and crushed into micro-bubbles through the micro-interface generator 102, so that the effect of strengthening the oxidation reaction is achieved, the mass transfer efficiency of a phase interface is improved, and in order to improve the safety, vent holes 105 are formed in the tops of the primary oxidation reactor 70 and the secondary oxidation reactor 100.
Finally, the oxidation water after oxidation reaction in the first-stage oxidation reactor 70 and the second-stage oxidation reactor 100 returns to the waste water heat exchanger 80 from the top of the oxidation reaction device for heat exchange and cooling treatment, and then is conveyed to the finished product tank 130 for storage.
The above steps are repeated circularly to make the whole treatment system run smoothly.
The treatment system ensures that wet oxidation is carried out under the conditions of mild pressure and temperature by laying the micro-interface generation system. Compared with the treatment system of the wastewater in the H acid production in the prior art, the treatment system has the advantages of few equipment components, small occupied area, low energy consumption, low cost, high safety, controllable reaction and wide popularization and application value. In a word, the treatment system for the wastewater in the H acid production has high treatment capacity, and after the treatment by the treatment system, the treatment system can ensure that the treatment system has a high treatment effect under the condition of low energy consumption, and the removal rate of harmful substances and COD can reach 99%.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (8)
1. A processing system of waste water in H acid production, characterized by comprising: the system comprises a raw water tank, a waste water heat exchanger, a waste water heater and an oxidation reaction device which are connected in sequence, wherein the waste water heat exchanger is provided with a material inlet, a material outlet, a heat source inlet and a heat source outlet;
the oxidized water from the oxidation reaction device enters the wastewater heat exchanger from the heat source inlet, the heat source outlet is connected with a finished product tank, the material inlet is connected with the raw water tank, and the material outlet is connected with the wastewater heater;
the oxidation reaction device comprises a primary oxidation reactor and a secondary oxidation reactor which are sequentially connected, and oxidation water after oxidation treatment of the primary oxidation reactor continuously enters the secondary oxidation reactor for oxidation treatment;
a micro-interface generator for dispersing broken gas into bubbles is arranged on the outer side of the secondary oxidation reactor, an air inlet and a waste water inlet are arranged on the micro-interface generator, waste water which is circulated back from the oxidation reactor enters from the waste water inlet, fresh supplementary air or oxygen enters from the air inlet, and the structure of the primary oxidation reactor is consistent with that of the secondary oxidation reactor;
the micro-interface generator is a pneumatic micro-interface generator;
the treatment method of the wastewater in the H acid production of the treatment system comprises the following steps:
heating the wastewater in the H acid production, then feeding the wastewater into an oxidation reaction device, and simultaneously introducing compressed air or compressed oxygen into the oxidation reaction device to perform oxidation reaction;
the compressed air or the compressed oxygen entering the oxidation reaction device is firstly dispersed and crushed by a micro-interface generation system;
the temperature of the oxidation reaction is controlled between 130 ℃ and 135 ℃, and the pressure is controlled between 1.8 MPa and 2.4 MPa.
2. The treatment system according to claim 1, wherein the side walls of the primary oxidation reactor and the secondary oxidation reactor are provided with waste liquid circulation pipelines for introducing the waste water circulated back from the waste water inlet.
3. The treatment system of claim 2, further comprising a neutralization tank, a sedimentation tank, a first filtration tank, a decolorization tank, and a second filtration tank, wherein the raw water tank is connected to the neutralization tank, the sedimentation tank, the first filtration tank, the decolorization tank, and the second filtration tank in this order.
4. A treatment system according to claim 3, wherein a transfer pump is provided between the second filtration tank and the waste water heat exchanger.
5. The treatment system according to any one of claims 1 to 4, wherein an oxidized water outlet is provided at an upper side of the secondary oxidation reactor, and the oxidized water outlet is connected to the heat source inlet through a pipe.
6. The treatment system according to claim 5, further comprising a gas-liquid separation tank, wherein the oxidized water from the oxidized water outlet enters the waste water heat exchanger from the heat source inlet after entering the gas-liquid separation tank for gas-liquid separation.
7. The treatment system of any one of claims 1-4, further comprising a pneumatic device in communication with the air inlet.
8. The treatment system of claim 7, wherein a gas heating device is disposed on a conduit connecting the air compressing device and the air inlet.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911333993.3A CN113087249B (en) | 2019-12-23 | 2019-12-23 | System and method for treating wastewater in H acid production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911333993.3A CN113087249B (en) | 2019-12-23 | 2019-12-23 | System and method for treating wastewater in H acid production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113087249A CN113087249A (en) | 2021-07-09 |
| CN113087249B true CN113087249B (en) | 2022-04-22 |
Family
ID=76663824
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911333993.3A Active CN113087249B (en) | 2019-12-23 | 2019-12-23 | System and method for treating wastewater in H acid production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113087249B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117509953B (en) * | 2023-11-09 | 2025-04-01 | 江苏南大华兴环保科技股份公司 | System and method for treating vitamin B1 centrifugal mother liquor by enhanced wet oxidation |
| CN118062978A (en) * | 2024-01-31 | 2024-05-24 | 首建科技有限公司 | A pretreatment method for wastewater containing chloramines |
Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1177519A (en) * | 1996-08-27 | 1998-04-01 | 株式会社日本催化剂 | Gas-liquid dispersing device, gas-liquid contacting device and waste-water treating device |
| CN101041521A (en) * | 2007-03-07 | 2007-09-26 | 王国华 | H acid waste water by natrium chloratum addition process |
| CN101104533A (en) * | 2007-06-05 | 2008-01-16 | 南开大学 | A kind of treatment method of H-acid production wastewater |
| CN101870522A (en) * | 2009-04-24 | 2010-10-27 | 株式会社安来特 | Fine bubble generating apparatus |
| EP2443249A2 (en) * | 2009-06-15 | 2012-04-25 | 3M Innovative Properties Company | Detection of acid-producing bacteria |
| KR20120071622A (en) * | 2010-12-23 | 2012-07-03 | 한국건설기술연구원 | Micro bubble type gpv-wao reactor |
| ES2392598T3 (en) * | 2007-06-27 | 2012-12-12 | H R D Corporation | Process for water treatment using a high speed shear device |
| CN204185356U (en) * | 2014-10-22 | 2015-03-04 | 北京久顺科技有限公司 | A kind of Novel oxidation column |
| CN105152417A (en) * | 2015-08-28 | 2015-12-16 | 浙江奇彩环境科技有限公司 | Method for recycling salt in organic waste water |
| CN206203975U (en) * | 2016-10-11 | 2017-05-31 | 羿太环保科技（上海）有限公司 | The continuous wet-type oxidation technology equipment of degrading high concentration organic wastewater |
| CN106865851A (en) * | 2017-02-13 | 2017-06-20 | 内蒙古美力坚科技化工有限公司 | The method of dyestuff intermediate such as 2 naphthols production wastewater treatments and recycling |
| CN107572651A (en) * | 2017-09-14 | 2018-01-12 | 同济大学 | A kind of method and device of multistage wet oxidation processing industrial wastewater |
| CN108947069A (en) * | 2018-07-28 | 2018-12-07 | 大连微凯化学有限公司 | System and method based on micro passage reaction continuous processing organic wastewater |
| CN211733961U (en) * | 2019-12-23 | 2020-10-23 | 南京延长反应技术研究院有限公司 | Processing system of waste water in sour production of H |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7547388B2 (en) * | 2004-07-20 | 2009-06-16 | Think Village-Kerfoot, Llc | Superoxidant poiser for groundwater and soil treatment with in-situ oxidation-reduction and acidity-basicity adjustment |
-
2019
- 2019-12-23 CN CN201911333993.3A patent/CN113087249B/en active Active
Patent Citations (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1177519A (en) * | 1996-08-27 | 1998-04-01 | 株式会社日本催化剂 | Gas-liquid dispersing device, gas-liquid contacting device and waste-water treating device |
| CN101041521A (en) * | 2007-03-07 | 2007-09-26 | 王国华 | H acid waste water by natrium chloratum addition process |
| CN101104533A (en) * | 2007-06-05 | 2008-01-16 | 南开大学 | A kind of treatment method of H-acid production wastewater |
| ES2392598T3 (en) * | 2007-06-27 | 2012-12-12 | H R D Corporation | Process for water treatment using a high speed shear device |
| CN101870522A (en) * | 2009-04-24 | 2010-10-27 | 株式会社安来特 | Fine bubble generating apparatus |
| EP2443249A2 (en) * | 2009-06-15 | 2012-04-25 | 3M Innovative Properties Company | Detection of acid-producing bacteria |
| KR20120071622A (en) * | 2010-12-23 | 2012-07-03 | 한국건설기술연구원 | Micro bubble type gpv-wao reactor |
| CN204185356U (en) * | 2014-10-22 | 2015-03-04 | 北京久顺科技有限公司 | A kind of Novel oxidation column |
| CN105152417A (en) * | 2015-08-28 | 2015-12-16 | 浙江奇彩环境科技有限公司 | Method for recycling salt in organic waste water |
| CN206203975U (en) * | 2016-10-11 | 2017-05-31 | 羿太环保科技（上海）有限公司 | The continuous wet-type oxidation technology equipment of degrading high concentration organic wastewater |
| CN106865851A (en) * | 2017-02-13 | 2017-06-20 | 内蒙古美力坚科技化工有限公司 | The method of dyestuff intermediate such as 2 naphthols production wastewater treatments and recycling |
| CN107572651A (en) * | 2017-09-14 | 2018-01-12 | 同济大学 | A kind of method and device of multistage wet oxidation processing industrial wastewater |
| CN108947069A (en) * | 2018-07-28 | 2018-12-07 | 大连微凯化学有限公司 | System and method based on micro passage reaction continuous processing organic wastewater |
| CN211733961U (en) * | 2019-12-23 | 2020-10-23 | 南京延长反应技术研究院有限公司 | Processing system of waste water in sour production of H |
Non-Patent Citations (5)
| Title |
|---|
| "Foamability in high viscous non-Newtonian aqueous two-phase systems composed of surfactant and polymer";Ding Ping et al.;《COLLOIDS AND SURFACES A-PHYSICOCHEMICAL AND ENGINEERING ASPECTS》;20190820;第582卷;文献号：123817 * |
| "Microbubbles intensification and mechanism of wet air oxidation process of MDEA-containing wastewater";zhao jun et al.;《ENVIRONMENTAL TECTNOLOGY》;20210628;第1-10页 * |
| "多相反应体系的微界面强化简述";张志炳等;《化工学报》;20180131;第69卷(第1期);第44-49页 * |
| "湿式空气氧化处理高浓度H酸废水的研究";陈拥军等;《化学工业与工程》;20020831(第4期);第292-296页 * |
| "超微气泡对铜酞青污水处理的实验研究";周清童等;《能源研究与信息》;20091230;第25卷(第4期);第208-211页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113087249A (en) | 2021-07-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113087254B (en) | Treatment system and method for acrylic acid and acrylic ester wastewater | |
| CN113087249B (en) | System and method for treating wastewater in H acid production | |
| CN113087192B (en) | Treatment system and method for cephalosporin wastewater | |
| WO2021047044A1 (en) | System and process for preparing hydrogen peroxide based on anthraquinone process | |
| CN106904806A (en) | The integrated treatment reactor and processing method of a kind of sludge wet oxidation | |
| CN113087252B (en) | Treatment system and method for caprolactam production wastewater | |
| CN111573962B (en) | External micro-interface papermaking sewage treatment system and treatment method | |
| CN211733961U (en) | Processing system of waste water in sour production of H | |
| CN212127668U (en) | Processing system of cephalo class waste water | |
| CN116282621A (en) | A high-salt and low-COD wastewater treatment system and method | |
| CN113087248B (en) | System and method for treating wastewater in hydroxyquinoline production | |
| WO2023138073A1 (en) | Ultrasonic wastewater treatment device and method | |
| CN207845373U (en) | A kind of emulsified waste liquid processing unit | |
| CN211733964U (en) | Treatment system for acrylic acid and ester wastewater thereof | |
| CN211813635U (en) | Processing system of waste water in hydroxyquinoline production | |
| CN113087253B (en) | Treatment system and method for landfill leachate | |
| CN113087256A (en) | Treatment system and method for ethylene desulfurization wastewater | |
| CN211733962U (en) | Caprolactam waste water's processing system | |
| CN215102210U (en) | Catalytic wet oxidation reactor | |
| CN211734109U (en) | Intelligent processing system of cephalo class waste water | |
| CN115403235A (en) | Continuous sludge pyrohydrolysis system | |
| CN213506147U (en) | Landfill leachate's processing system | |
| CN2892837Y (en) | High-concentration industrial waste water processing system | |
| CN113045106A (en) | Intelligent treatment system and method for cephalosporin wastewater | |
| CN213085651U (en) | External micro-interface papermaking 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 | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: No. 88, Tanqu South Road, Jiangbei New District, Nanjing City, Jiangsu Province Patentee after: Nanjing Anlige Co.,Ltd. Country or region after: China Address before: No. 88, Tanqu South Road, Jiangbei New District, Nanjing City, Jiangsu Province Patentee before: Nanjing Yanchang Reaction Technology Research Institute Co.,Ltd. Country or region before: China |