CN211733962U - Caprolactam waste water's processing system - Google Patents
Caprolactam waste water's processing system Download PDFInfo
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- CN211733962U CN211733962U CN201922335112.3U CN201922335112U CN211733962U CN 211733962 U CN211733962 U CN 211733962U CN 201922335112 U CN201922335112 U CN 201922335112U CN 211733962 U CN211733962 U CN 211733962U
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- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 239000002351 wastewater Substances 0.000 title claims abstract description 79
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 62
- 230000003647 oxidation Effects 0.000 claims abstract description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 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
- 239000002699 waste material Substances 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 15
- 238000004062 sedimentation Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 238000004378 air conditioning Methods 0.000 claims 1
- 239000003054 catalyst Substances 0.000 abstract description 21
- 230000000694 effects Effects 0.000 abstract description 18
- 238000006243 chemical reaction Methods 0.000 abstract description 17
- 230000005501 phase interface Effects 0.000 abstract description 7
- 238000004065 wastewater treatment Methods 0.000 abstract description 7
- 238000000034 method Methods 0.000 description 15
- 239000012071 phase Substances 0.000 description 12
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- 238000004519 manufacturing process Methods 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
- 238000009279 wet oxidation reaction Methods 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
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- 239000012535 impurity Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000003672 processing method Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 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
- 238000010438 heat treatment Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000000839 emulsion Substances 0.000 description 3
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- 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
- 230000008901 benefit Effects 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
- 230000004927 fusion Effects 0.000 description 2
- 239000007792 gaseous phase 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
- 230000008676 import Effects 0.000 description 2
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- 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
- -1 cyclohexane Chemical compound 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The utility model provides a processing system of caprolactam waste water. 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 utility model discloses a processing system improves the contact at reaction phase interface through laying behind the micro-interface generator, need not use the catalyst, or add the catalyst less and also can obtain good waste water treatment effect.
Description
Technical Field
The utility model relates to a caprolactam waste water treatment field particularly, relates to a caprolactam waste water's processing system.
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 artThe 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 this, the present invention is especially provided.
SUMMERY OF THE UTILITY MODEL
A first object of the utility model is to provide a processing system of caprolactam waste water, this processing system is through laying behind the micro-interface generator, the mass transfer effect between the double-phase has been improved, this micro-interface generator can smash the bubble into micron level's bubble, thereby increase the interfacial area between gaseous phase and the liquid phase, make oxygen can form the gas-liquid emulsion with the better fusion of caprolactam waste water, improve oxidation reaction efficiency, simultaneously because oxygen in the caprolactam waste water is smashed after the small bubble, gaseous volume diminishes, thereby the buoyancy of bubble come-up has been slowed down, make the time that oxygen dwells in caprolactam waste water longer, further improve reaction efficiency, the mass transfer effect at reaction phase interface has been increased.
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 objective of the utility model is to provide an adopt above-mentioned processing system to carry out caprolactam waste water's processing method, this processing method is easy and simple to handle, operating condition is gentler, and the energy consumption is low, and in the caprolactam waste water after the processing, harmful removal rate can reach about 99%, is worth extensively popularizing and applying.
In order to realize the above purpose of the utility model, the following technical scheme is adopted:
the utility model provides a effluent disposal system for handling caprolactam waste water, include: 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 utility model discloses caprolactam waste water of required processing, mainly contain caprolactam, ammonium sulfate, acetic acid, toluene, benzoic acid, cyclohexane carboxylic acid sulfonic acid, hexahydrobenzoic acid, compositions such as cyclohexane, the organic matter is of a great variety, the COD value is high, the salt content is high, the biodegradability is poor, what mainly adopted among the prior art is chemical oxidation method and wet-type oxidation method, but in wet-type oxidation treatment process, after having adopted the catalyst, although operating temperature and pressure are not high, but adopted behind the catalyst cost per se higher, after the follow-up reaction, still consider the follow-up recovery of catalyst, the problem of processing, the operation is very inconvenient, many follow-up work have been increased among the intangible.
The utility model provides a treatment system specially aiming at caprolactam production wastewater treatment in order to solve the technical problems, 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 utility model discloses a system takes place for the micro-interface, for making the waste liquid can realize the circulation, for first micro-interface generator provides power, oxidation reactor's lateral wall is provided with circulation waste liquid export, and first micro-interface generator's top is provided with circulation waste liquid import, and circulation waste liquid import passes through circulating line with circulation waste liquid export and is connected, the last circulating pump that provides power that is provided with of circulating line. 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 can be understood by those skilled in the art that the micro-interface generator of the present invention can break the gas phase and/or the liquid phase in the multi-phase reaction medium into micro-bubbles and/or micro-droplets with a diameter of micron level in a preset action mode through the mechanical micro-structure and/or turbulent micro-structure in the micro-interface generator before the multi-phase reaction medium enters the reactor, 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 in the reaction process, 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.
Additionally, be in the utility model discloses an in the scheme, in order to retrieve the resource in caprolactam waste water, reduce caprolactam waste water's the wet-type oxidation degree of difficulty, improve the COD clearance of waste water, carry out the preliminary treatment to caprolactam waste water before wet-type oxidation earlier at best, the preliminary treatment is including deposiing, adding pretreatment methods such as medicine, and certain pretreatment methods that can also adopt to other according to the operating mode of reality certainly.
Therefore, the utility model discloses among the processing system of caprolactam waste water, still included the sedimentation tank, the sedimentation tank with raw water tank connects. 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 utility model discloses a can set up the pump body according to actual need on corresponding connecting tube among the processing system.
The utility model discloses a processing system of caprolactam waste water is high in treatment capacity, handles the back through this processing system, can guarantee under the energy consumption condition that is lower than, possess higher treatment effect, and harmful removal rate can reach about 99%.
In addition, the utility model also provides a caprolactam waste water's processing method, including the following step:
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 utility model discloses a caprolactam waste water's processing method easy and simple to handle, operating condition are gentler, and the energy consumption is low, and among the caprolactam waste water after the processing, harmful, COD clearance can reach 99%, has reduced industrial waste's emission, and environmental protection more is worth extensively popularizing and applying.
Compared with the prior art, the beneficial effects of the utility model reside in that:
(1) the utility model discloses caprolactam waste water's processing system has improved the mass transfer effect between the double-phase through laying little interfacial generator, and this little interfacial generator can break the bubble into micron level's bubble to increase the phase interface area between gaseous phase and the liquid phase, make oxygen can form the gas-liquid emulsion with better fusion of caprolactam waste water, improve oxidation reaction efficiency;
(2) the wastewater treatment system of the utility model has simple structure, less three wastes, full recycling of oxygen and small occupied area;
(3) the wastewater treatment system of the utility model improves the mass transfer effect between two phases by arranging the micro-interface generation system, reduces the energy consumption and the production cost, and obviously improves the oxidation reaction efficiency;
(4) the utility model discloses a processing system need not adopt the catalyst, just can realize carrying out wet oxidation reaction than lower temperature, pressure condition under, does not adopt the catalyst not only to practice thrift the cost, has still removed the catalyst from and needs follow-up recovery, processing, causes the appearance of secondary pollution's problem, and whole processing method operation is more for simple and efficient, and operation flow is also corresponding simplifies a lot.
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 waste water treatment system provided by an embodiment of the present 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 described clearly and completely with reference to the accompanying drawings and 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. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to 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", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific 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 is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; 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 meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to clarify 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 the principle of the caprolactam production wastewater treatment system of the utility model are briefly explained 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 utility model discloses a processing system has guaranteed that wet oxidation goes on under more gentle pressure and temperature condition through laying little interface emergence system, and need not adopt the catalyst. Compared with the treatment system of caprolactam waste water of the prior art, the utility model discloses a treatment system equipment subassembly is few, area is little, the energy consumption is low, with low costs, the security is high, the reaction is controllable, is worth extensively popularizing and applying.
In a word, the utility model discloses a caprolactam waste water's processing system throughput is high, handles the back through this processing system, can guarantee under the energy consumption condition that is lower than, possess higher treatment effect, and harmful, COD clearance 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; although the present invention has been described in detail with reference to the foregoing embodiments, it should 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; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (9)
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 air-conditioning system is characterized in that a micro-interface generating system is arranged in the oxidation reactor and used for dispersing broken gas into bubbles, the micro-interface generating 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 filled with wastewater which returns from the internal circulation of 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 and is used for recovering air or oxygen, an air inlet is formed in the side wall of the oxidation reactor, and the tail end of the air inlet extends into the second micro-interface generator.
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 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, and the circulating waste liquid inlet is connected with the circulating waste liquid outlet through a circulating pipeline.
5. The processing system according to claim 1, wherein a connecting rod is provided between the first and second micro-interface generators for mutual fixation.
6. The processing system of any of claims 1 to 5, wherein the first micro-interface generator is a hydraulic micro-interface generator and the second micro-interface generator is a pneumatic micro-interface generator.
7. The processing system of claim 6, wherein the outlet of the first micro-interface generator is opposite the outlet of the second micro-interface generator.
8. The treatment system according to any one of claims 1 to 5, wherein an oxidized water outlet is provided at an upper side of the oxidation reactor, and the oxidized water outlet is connected to the heat source inlet through a pipe.
9. The treatment system according to any one of claims 1 to 5, further comprising an air compressor in communication with the air inlet, the communication conduit having a gas heater disposed thereon.
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| CN113087252A (en) * | 2019-12-23 | 2021-07-09 | 南京延长反应技术研究院有限公司 | Treatment system and method for caprolactam production wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113087252A (en) * | 2019-12-23 | 2021-07-09 | 南京延长反应技术研究院有限公司 | Treatment system and method for caprolactam production wastewater |
| CN113087252B (en) * | 2019-12-23 | 2022-04-01 | 南京延长反应技术研究院有限公司 | Treatment system and method for caprolactam production wastewater |
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