CN113087252B - Treatment system and method for caprolactam production wastewater - Google Patents
Treatment system and method for caprolactam production wastewater Download PDFInfo
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- CN113087252B CN113087252B CN201911334007.6A CN201911334007A CN113087252B CN 113087252 B CN113087252 B CN 113087252B CN 201911334007 A CN201911334007 A CN 201911334007A CN 113087252 B CN113087252 B CN 113087252B
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- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 239000002351 wastewater Substances 0.000 title claims abstract description 82
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 62
- 230000003647 oxidation Effects 0.000 claims abstract description 54
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 20
- 239000001301 oxygen Substances 0.000 claims description 20
- 229910052760 oxygen Inorganic materials 0.000 claims description 20
- 239000007789 gas Substances 0.000 claims description 18
- 239000002699 waste material Substances 0.000 claims description 17
- 238000004062 sedimentation Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000003054 catalyst Substances 0.000 abstract description 20
- 230000000694 effects Effects 0.000 abstract description 18
- 238000006243 chemical reaction Methods 0.000 abstract description 17
- 238000004065 wastewater treatment Methods 0.000 abstract description 10
- 230000005501 phase interface Effects 0.000 abstract description 8
- 239000012071 phase Substances 0.000 description 14
- 238000009279 wet oxidation reaction Methods 0.000 description 11
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- 239000000126 substance Substances 0.000 description 9
- NZNMSOFKMUBTKW-UHFFFAOYSA-N cyclohexanecarboxylic acid Chemical compound OC(=O)C1CCCCC1 NZNMSOFKMUBTKW-UHFFFAOYSA-N 0.000 description 7
- 239000007791 liquid phase Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 239000012535 impurity Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 4
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000000839 emulsion Substances 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 239000012429 reaction media Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000005711 Benzoic acid Substances 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 235000010233 benzoic acid Nutrition 0.000 description 2
- VEZUQRBDRNJBJY-UHFFFAOYSA-N cyclohexanone oxime Chemical compound ON=C1CCCCC1 VEZUQRBDRNJBJY-UHFFFAOYSA-N 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 150000003839 salts Chemical class 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
- 238000006237 Beckmann rearrangement reaction Methods 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- VZFUCHSFHOYXIS-UHFFFAOYSA-N cycloheptane carboxylic acid Natural products OC(=O)C1CCCCCC1 VZFUCHSFHOYXIS-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 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
- 230000008030 elimination Effects 0.000 description 1
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- 239000000835 fiber Substances 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 238000001914 filtration Methods 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
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000004064 recycling Methods 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
Images
Classifications
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- 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
- 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
- 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
Abstract
The invention provides a treatment system and a treatment method for caprolactam production wastewater. The processing system comprises: the system comprises a raw water tank, a waste water heat exchanger, a waste water heater and an oxidation reactor 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 oxidation reactor is characterized in that oxidation water from the oxidation reactor 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, the material outlet is connected with the wastewater heater, and a micro-interface generating system is arranged in the oxidation reactor and used for dispersing broken gas into bubbles. The treatment system improves the contact of the reaction phase interface by arranging the micro-interface generator, and can obtain good wastewater treatment effect without using a catalyst or adding a little catalyst.
Description
Technical Field
The invention relates to the field of caprolactam production wastewater treatment, and particularly relates to a caprolactam production wastewater treatment system and method.
Background
Caprolactam is an important chemical material, and is mainly used for producing polyurethane through polymerization, and can be further processed into fibers, plastics, films and the like. The main production methods of caprolactam in China are a toluene method and a benzene method, but the caprolactam is finally obtained through a cyclohexanone-oxime liquid-phase Beckmann rearrangement reaction. The wastewater mainly contains caprolactam, ammonium sulfate, acetic acid, toluene, benzoic acid, cyclohexane carboxylic sulfonic acid, hexahydrobenzoic acid, cyclohexane and other components, and has various organic matters, high COD value, high salt content and poor biodegradability.
In the prior art, caprolactam industrial wastewater is generally treated by a chemical oxidation method, such as a Fenton method or a wet oxidation method. Because the COD of the caprolactam wastewater is 5000-30000mg/L, a large amount of H is consumed by the Fenton method2O2The treatment cost is high, and the wet oxidation method has the defects of high equipment requirement, long reaction time, low COD elimination rate and the like.
In the wet oxidation treatment process, after the catalyst is adopted, although the reaction time can be shortened to a certain extent, and the operation temperature and pressure are reduced, the cost is higher after the catalyst is adopted, the problems of subsequent recovery and treatment of the catalyst are also considered after the subsequent reaction is finished, the operation is very inconvenient, and a lot of subsequent work is increased invisibly.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The first purpose of the invention is to provide a caprolactam production wastewater treatment system, which improves the mass transfer effect between two phases by arranging a micro-interface generator, wherein 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 caprolactam production wastewater to form gas-liquid emulsion, thereby improving the oxidation reaction efficiency, and meanwhile, the gas volume is reduced after the oxygen in the caprolactam production wastewater is broken into small bubbles, thereby slowing the buoyancy of bubble floating, so that the retention time of the oxygen in the caprolactam production wastewater is longer, further improving the reaction efficiency, and increasing the mass transfer effect of a reaction phase interface.
Meanwhile, after the micro-interface generator is adopted, the whole treatment system can be operated without adopting a catalyst, the cost is saved without adopting the catalyst, the problem of secondary pollution caused by the fact that the catalyst needs to be subsequently recovered and treated is solved, the whole treatment method is simple, convenient and quick to operate, and the operation flow is correspondingly simplified.
The second purpose of the invention is to provide a method for treating caprolactam production wastewater by using the treatment system, the treatment method is simple and convenient to operate, the operation conditions are milder, the energy consumption is low, the removal rate of harmful substances in the treated caprolactam production wastewater can reach about 99%, and the method is worthy of wide popularization and application.
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 caprolactam production wastewater, which comprises: the system comprises a raw water tank, a waste water heat exchanger, a waste water heater and an oxidation reactor 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 reactor enters a waste water heat exchanger from a heat source inlet, a finished product tank is connected with a heat source outlet, a material inlet is connected with a raw water tank, and a material outlet is connected with a waste water heater;
be provided with the micro-interface generating system in the oxidation reactor, the micro-interface generating system is used for dispersing broken gas and becomes the bubble, the micro-interface generating system is including the first micro-interface generator and the second micro-interface generator of arranging from top to bottom, first micro-interface generator lets in the waste water that returns from the oxidation reactor inner loop, first micro-interface generator is connected with the air duct, the liquid level that oxidation reactor was stretched out to the top of air duct is used for retrieving air or oxygen, oxidation reactor's lateral wall is provided with the air inlet, the end of air inlet extends to in the second micro-interface generator.
The caprolactam production wastewater required to be treated by the invention mainly contains caprolactam, ammonium sulfate, acetic acid, toluene, benzoic acid, cyclohexane carboxylic acid sulfonic acid, hexahydrobenzoic acid, cyclohexane and other components, the organic matters are various, the COD value is high, the salt content is high, the biodegradability is poor, a chemical oxidation method and a wet oxidation method are mainly adopted in the prior art, but in the wet oxidation treatment process, after the catalyst is adopted, although the operation temperature and the pressure are not high, the cost is higher after the catalyst is adopted, and after the subsequent reaction is finished, the problems of subsequent recovery and treatment of the catalyst are also considered, so that the operation is very inconvenient, and a lot of subsequent work is increased invisibly.
The invention aims to solve the technical problems and provides a treatment system specially aiming at caprolactam production wastewater treatment, the treatment system is characterized in that a micro-interface generation system is arranged at the bottom of the oxidation reactor, air or oxygen entering the oxidation reactor is broken and dispersed into bubbles, so that the bubbles and wastewater form gas-liquid emulsion, thereby increasing the phase interface area between the gas and the wastewater, further improving the reaction efficiency, and melting oxygen into the wastewater as much as possible after increasing the mass transfer effect of the reaction phase interface, thus, the good treatment effect can be ensured under the conditions of lower pressure and temperature without adopting a catalyst, or in order to ensure better treatment effect, a few catalysts can be added, the amount of the catalyst adopted in the traditional process can be reduced sufficiently, and the catalyst can be added or not added freely according to the actual operation condition.
For the micro-interface generation system, in order to realize circulation of waste liquid and provide power for the first micro-interface generator, the side wall of the oxidation reactor is provided with a circulating waste liquid outlet, the top of the first micro-interface generator is provided with a circulating waste liquid inlet, the circulating waste liquid inlet is connected with the circulating waste liquid outlet through a circulating pipeline, and the circulating pipeline is provided with a circulating pump for providing power. In the wet oxidation reaction process, a part of oxygen runs to a space above the liquid level of the wastewater in the reactor, and in order to fully recycle the oxygen, the circulating wastewater is used as power to circulate, so that the oxygen entering the gas guide pipe is sucked, and turbulence is formed to increase the contact area of the phase interface of the oxygen and the wastewater.
Therefore, the first micro-interface generator is preferably a hydraulic micro-interface generator, in actual operation, the circulating waste liquid enters from the middle of the top of the first micro-interface generator, and the oxygen is sucked in by being entrained from the channels on the two sides of the first micro-interface generator, so that the gas-liquid phase is fully contacted in the micro-interface generator, and the mass transfer effect is improved.
The second 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.
In order to further improve the sufficient contact of the reaction feed liquid, the outlet of the first micro-interface generator is preferably arranged opposite to the outlet of the second micro-interface generator.
Because the two micro-interface generators are both positioned below the liquid level, in order to avoid instability caused by impact of liquid flow on the micro-interface generators, a connecting rod for mutual fixation is preferably arranged between the first micro-interface generator and the second micro-interface generator, the specific material, shape and number of the connecting rod are not limited as long as the fixing effect can be achieved, and the connecting rod is preferably in a long rod shape.
It is understood by those skilled in the art that the micro-interface generator used in the present invention can break up the gas phase and/or the liquid phase in the multi-phase reaction medium into micro-bubbles and/or micro-droplets with micron-sized diameter in a preset action mode in the micro-interface generator before the multi-phase reaction medium enters the reactor through the mechanical microstructure and/or the turbulent microstructure, so as to increase the mass transfer area of the phase boundary between the gas phase and/or the liquid phase and/or the solid phase during the reaction, improve the mass transfer efficiency between the reaction phases, and strengthen the multi-phase reaction within a preset temperature and/or a preset pressure range.
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 reactor in the system, so that the better air supply effect is achieved, and the oxidative degradation rate is improved.
In addition, in the scheme of the invention, in order to recover resources in the caprolactam production wastewater, reduce the difficulty of wet oxidation of the caprolactam production wastewater and improve the COD removal rate of the wastewater, the caprolactam production wastewater is preferably pretreated before the wet oxidation, the pretreatment comprises pretreatment means such as precipitation, dosing and the like, and other pretreatment modes can be adopted according to actual working conditions.
Therefore, the system for treating the caprolactam production wastewater also comprises a sedimentation tank, and the sedimentation tank is connected with the raw water tank. The preliminary sedimentation can be gone out heavier particulate matter, impurity preliminary filtration, discharges from the bottom of sedimentation tank.
Preferably, the treatment system further comprises a dosing tank and a separation tank, and the sedimentation tank is sequentially connected with the dosing tank and the separation tank. Adding sulfuric acid into the chemical adding pool, adjusting the pH value of the wastewater to be treated to 1-6, removing precipitate after the precipitate is fully separated out, introducing the upper liquid phase into the separation pool after the precipitate is precipitated in the chemical adding pool, further precipitating and removing impurities in the separation pool, and carrying out next wet oxidation treatment on the waste liquid after the impurities are removed in the separation pool.
Preferably, the lateral upper part of the oxidation reactor is provided with an oxidation water outlet, and the oxidation 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. The compressed air or oxygen from the air compressor is preferably heated in a gas heating device, preferably a heat exchanger, before entering the micro-interface generator.
The treatment system can be provided with the pump body on the corresponding connecting pipeline according to actual requirements.
The treatment system for caprolactam production wastewater has high treatment capacity, and after the treatment by the treatment system, the caprolactam production wastewater can have higher treatment effect under the condition of lower energy consumption, and the removal rate of harmful substances can reach about 99%.
In addition, the invention also provides a treatment method of caprolactam production wastewater, which comprises the following steps:
heating caprolactam production wastewater, then feeding the heated caprolactam production wastewater into an oxidation reactor, and simultaneously introducing compressed air or compressed oxygen into the oxidation reactor to perform oxidation reaction;
the compressed air or the compressed oxygen entering the oxidation reactor is firstly dispersed and crushed by a micro-interface generating system.
The reaction temperature of the oxidation reaction is between 120 and 200 ℃, the reaction pressure is between 1 and 1.5MPa, and a catalyst is not needed after a micro-interface generation system is adopted, so that the problems that in the prior art, the pipeline is easily blocked and the post-treatment load is increased due to the adoption of catalysts such as iron powder, copper powder and manganese oxide are solved.
The method for treating the caprolactam production wastewater has the advantages of simple and convenient operation, milder operation conditions and low energy consumption, the removal rate of harmful substances and COD in the treated caprolactam production wastewater 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 caprolactam production wastewater, the mass transfer effect between two phases is improved by arranging the micro-interface generator, and 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 caprolactam production wastewater to form gas-liquid emulsion, and the oxidation reaction efficiency is improved;
(2) the wastewater treatment system disclosed by the invention is simple in structure, less in three wastes, small in occupied area and capable of realizing full recycling of oxygen;
(3) the wastewater treatment system improves the mass transfer effect between two phases by arranging the micro-interface generation system, reduces energy consumption and production cost, and obviously improves the oxidation reaction efficiency;
(4) the treatment system can realize wet oxidation reaction at a lower temperature and under a pressure condition without adopting a catalyst, not only saves the cost, but also avoids the problem of secondary pollution caused by the need of subsequent recovery and treatment of the catalyst, the operation of the whole treatment method is simpler, more convenient and faster, and the operation flow is correspondingly simplified.
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 caprolactam production wastewater treatment system provided by an embodiment of the invention.
Description of the drawings:
10-a raw water tank; 20-a sedimentation tank;
30-a medicine adding pool; 40-a separation tank;
50-a waste water heat exchanger; 51-material inlet;
52-material outlet; 53-heat source inlet;
54-heat source outlet; 60-a waste water heater;
70-an oxidation reactor; 71-an oxidized water outlet;
72-a first micro-interface generator; 73-a second micro-interface generator;
74-air compression means; 75-a vent;
76-an air inlet; 77-gas-guide tube;
78-connecting rod; 79-gas heating means;
80-a delivery pump; 90-finished product tank;
100-buffer 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 caprolactam production wastewater according to an embodiment of the present invention includes a raw water tank 10, a wastewater heat exchanger 50, a wastewater heater 60, an oxidation reactor 70, and an air compressor 74, which are connected in sequence.
The waste water heat exchanger 50 is respectively provided with a material inlet 51, a material outlet 52, a heat source inlet 53 and a heat source outlet 54, oxidized water from the oxidation reactor 70 enters the waste water heat exchanger 50 from the heat source inlet 53, the heat source outlet 54 is connected with a finished product tank 90, the material inlet 51 is connected with the raw water tank 10, the material outlet 52 is connected with a waste water heater 60, and in the waste water heat exchanger 50, the oxidized water after the reaction of the oxidation reactor 70 exchanges heat with caprolactam production waste water to be treated, so that the effect of fully utilizing energy is achieved.
The oxidation reactor 70 is internally provided with a micro-interface generating system, the micro-interface generating system is used for dispersing the broken gas into bubbles, the micro-interface generating system comprises a first micro-interface generator 72 and a second micro-interface generator 73 which are arranged up and down, the first micro-interface generator 72 is introduced into the wastewater circulating back from the oxidation reactor, the first micro-interface generator 72 is connected with a gas guide tube 77, the top end of the gas guide tube 77 extends out of the liquid level of the oxidation reactor 70 for recovering air or oxygen, the side wall of the oxidation reactor 70 is provided with a gas inlet 76, and the tail end of the gas inlet 76 extends into the second micro-interface generator 73. The air inlet 76 is connected with the second micro-interface generator 73 through a pipeline, the air pressure device 74 is communicated with the air inlet 76, and air or oxygen compressed by the air pressure device 74 enters the second micro-interface generator 73 through the air inlet 76, so that the crushing and dispersion of the air are realized, and the mass transfer effect between the two phases is enhanced. The air compressor 74 is preferably an air compressor. The air or oxygen compressed by the air compressor is preheated by the gas heating device 79 and then enters the second micro-interface generator 73, so as to improve the reaction efficiency. 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 first micro-interface generator 72 is a hydraulic micro-interface generator, the second micro-interface generator 73 is a pneumatic micro-interface generator, and a connecting rod 78 for fixing the micro-interface generators is arranged between the first micro-interface generator 72 and the second micro-interface generator 73 to prevent the impact of waste liquid. And the outlet of the first micro-interfacial surface generator 72 is opposite to the outlet of the second micro-interfacial surface generator 73 to increase the impact between the two and accelerate the turbulent flow.
The first micro-interface generator 72 may be fixed inside the oxidation reactor by a grid, and the second micro-interface generator 73 may be reinforced by a pipe.
A circulating waste liquid outlet is formed in the side wall of the oxidation reactor 70, a circulating waste liquid inlet is formed in the top of the first micro-interface generator 72, the circulating waste liquid inlet is connected with the circulating waste liquid outlet through a circulating pipeline, and a circulating pump is arranged on the circulating pipeline.
The side upper part of the oxidation reactor 70 is provided with an oxidized water outlet 71, the oxidized water from the oxidized water outlet 71 is connected with the heat source inlet 53 through a pipeline, the oxidized water from the oxidation reactor 70 directly enters the waste water heat exchanger 50 for heat exchange, and is cooled down after heat exchange and then is conveyed to the finished product tank 90 for storage. The water from the product tank 90 may continue to undergo subsequent desalination by conventional means of the prior art.
The treatment system also comprises a pretreatment system of the sedimentation tank 20, the dosing tank 30 and the separation tank 40, and the wastewater after impurities are separated by the pretreatment system is temporarily stored in the buffer tank 100 and then enters the wastewater heat exchanger 50 from the buffer tank 100 through the delivery pump 80.
In the above embodiment, the number of the micro-interface generators in the micro-interface generating system 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-bubble generator may be installed on the side wall in the kettle in a manner of being oppositely arranged, so as to generate the opposite impact of the 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 caprolactam production wastewater treatment system of 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 50, a waste water heater 60, an oxidation reactor 70 and the inside of the oxidation reactor 70, caprolactam production waste water in the raw water tank 10 is sent to a sedimentation tank 20 to remove preliminary impurities, sulfuric acid is added into a medicine adding tank 30 to adjust the pH value, the precipitation is separated in a separation tank 40 after the precipitation, and the waste water is temporarily stored in a buffer tank 100.
Then, caprolactam waste water is sent into a waste water heat exchanger 50 through a delivery pump 80 for heat exchange, and then is further heated through a waste water heater 60, the heated caprolactam waste water enters an oxidation reactor 70 for oxidation treatment, compressed air or compressed oxygen is introduced from the bottom of the side of the oxidation reactor 70, and is dispersed and crushed into micro bubbles through a first micro-interface generator 72 and a second micro-interface generator 73, so as to achieve the effect of strengthening the oxidation reaction, improve the mass transfer efficiency of a phase interface, and in order to improve the safety, a vent 75 is arranged at the top of the oxidation reactor 70.
Finally, the oxidized water after the oxidation reaction in the oxidation reactor 70 is returned to the waste water heat exchanger 50 from the top of the oxidation reactor for heat exchange and cooling treatment, and then is transported to the finished product tank 90 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, and does not need to adopt a catalyst. Compared with the treatment system for caprolactam production wastewater in the prior art, the treatment system has the advantages of fewer 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 caprolactam production wastewater has high treatment capacity, and after the treatment by the treatment system, the caprolactam production wastewater can have higher treatment effect under the condition of lower 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 (6)
1. A caprolactam waste water's processing system, characterized by includes: the system comprises a raw water tank, a waste water heat exchanger, a waste water heater and an oxidation reactor 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 reactor 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 reactor is internally provided with a micro-interface generation system, the micro-interface generation system is used for dispersing broken gas into bubbles, the micro-interface generation system comprises a first micro-interface generator and a second micro-interface generator which are arranged up and down, the first micro-interface generator is introduced with wastewater circulating back from the oxidation reactor, the first micro-interface generator is connected with an air guide pipe, the top end of the air guide pipe extends out of the liquid level of the oxidation reactor for recovering air or oxygen, the side wall of the oxidation reactor is provided with an air inlet, and the tail end of the air inlet extends into the second micro-interface generator;
a connecting rod for fixing the first micro-interface generator and the second micro-interface generator mutually is arranged between the first micro-interface generator and the second micro-interface generator;
the first micro-interface generator is a hydraulic micro-interface generator, and the second micro-interface generator is a pneumatic micro-interface generator;
the outlet of the first micro-interface generator is opposite to the outlet of the second micro-interface generator;
a circulating waste liquid outlet is formed in the side wall of the oxidation reactor, a circulating waste liquid inlet is formed in the top of the first micro-interface generator, and the circulating waste liquid inlet is connected with the circulating waste liquid outlet through a circulating pipeline;
and the circulating pipeline is provided with a circulating pump.
2. The treatment system of claim 1, further comprising a sedimentation tank connected to the raw water tank.
3. The treatment system of claim 2, further comprising a dosing tank and a separation tank, wherein the sedimentation tank is connected to the dosing tank and the separation tank in sequence.
4. The treatment system according to claim 1, wherein the oxidation reactor is provided at an upper side thereof with an oxidized water outlet connected to the heat source inlet through a pipe.
5. The treatment system of claim 1, further comprising an air compressor in communication with the air inlet, the communication conduit having a gas heater disposed thereon.
6. A method for treating caprolactam production wastewater in the treatment system of any one of claims 1 to 5, comprising the steps of:
heating caprolactam production wastewater, then feeding the heated caprolactam production wastewater into an oxidation reactor, and simultaneously introducing compressed air or compressed oxygen into the oxidation reactor to perform oxidation reaction;
the compressed air or the compressed oxygen entering the oxidation reactor is firstly dispersed and crushed by a micro-interface generating system.
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