CN211733961U - Processing system of waste water in sour production of H - Google Patents
Processing system of waste water in sour production of H Download PDFInfo
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- CN211733961U CN211733961U CN201922334611.0U CN201922334611U CN211733961U CN 211733961 U CN211733961 U CN 211733961U CN 201922334611 U CN201922334611 U CN 201922334611U CN 211733961 U CN211733961 U CN 211733961U
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Images
Abstract
The utility model provides a processing system of waste water in sour production of H. 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 utility model discloses a processing system improves the contact at reaction phase interface after having laid little interface emergence system, under operating condition milder condition, also can guarantee good waste water treatment effect.
Description
Technical Field
The utility model relates to a waste water treatment field in the sour production of H particularly, relates to a processing system of waste water in sour production of H.
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 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 waste water in sour production of H, this processing system is through laying behind the micro-interface generator, 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 phase interface area between gaseous phase and the liquid phase, make oxygen can form the gas-liquid emulsion with the better integration of waste water in sour production of H, improve oxidation reaction efficiency, make the time that oxygen dwells in the waste water in sour production of H longer, further improve reaction efficiency, the mass transfer effect at reaction phase interface has been increased, thereby operating temperature and pressure can be appropriate reduction, the emergence of a series of potential safety hazards that high temperature high pressure brought has been avoided, and the energy consumption is low, and is low in cost, the treatment effect is excellent, etc.
A second object of the utility model is to provide an adopt above-mentioned processing system to carry out the processing method of waste water in the sour production of H, this processing method is easy and simple to handle, operating condition is gentler, and the energy consumption is low, and in the sour production waste water of H after the processing, harmful removal rate can reach 99%.
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 waste water in sour production of H, include: 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 utility model discloses waste water in the sour production of required H of handling, the characteristics of this waste water are: 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 utility model provides a solve above-mentioned technical problem, a special processing system to waste water treatment in the sour production of H is provided, this processing system sets up the micro-interface generator through the outside at oxidation reaction device, smash the air or the oxygen that get into oxidation reaction device and disperse into the bubble, make bubble and waste water form the gas-liquid emulsion, thereby increased the interfacial area between gas and the waste water, further improved reaction efficiency, increased after the mass transfer effect at reaction interfacial, make oxygen melt into waste water as much as possible, like this through having promoted the mass transfer effect after, the condition of controlling of fully reduced temperature and pressure, between pressure 1.8-2.4MPa, temperature 130 adds between 135 ℃, can guarantee to handle waste water under mild operating condition.
In addition, the utility model discloses a preferred pneumatic micro-interface generator of micro-interface generator, through let in the micro-interface generator with air or oxygen after the compression after, with the broken form that forms the microbubble in waste water contact back, improve the mass transfer effect.
The utility model discloses an so adopt the oxidation reactor of two-stage, also be for improving wet oxidation's effect, every oxidation reactor all adopts external mode to set up the micro-interface generator moreover, so adopt external mode, because this kind of mode easy maintenance, easy dismounting, convenient operation.
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 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 enhance 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 utility model, in order to retrieve the resource in the waste water in the sour production of H, reduce the wet-type oxidation degree of difficulty of waste water in the sour production of H, improve the COD clearance of waste water, carry out the preliminary treatment to waste water in the sour production of H before wet-type oxidation earlier preferably, the method of preliminary treatment includes pretreatment means such as neutralization, sediment, decoloration, of course according to actual operating mode, also can corresponding adoption to some other preliminary treatment modes.
Therefore, the utility model discloses in the processing system of waste water in the sour production of H, neutralization pond, sedimentation tank, first filtering ponds, decoloration pond and second filtering ponds have still been included. 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 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 throughput of waste water is high in the sour production of H, handles the back through this processing system, can guarantee under the energy consumption condition that is lower than, possess higher treatment, and harmful removal rate can reach 99%.
In addition, the utility model also provides a processing method of waste water in H sour production, including following step:
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 utility model discloses a processing method of waste water in the sour production of H is easy and simple to handle, operating condition is gentler, and the energy consumption is low, and waste water in the sour production of H after handling, harmful substance, COD clearance can reach 99%, have reduced the emission of industrial waste, and is 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 the processing system of waste water in the sour production of H has improved the mass transfer effect between the double-phase through laying the micro-interface generator after, this micro-interface 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 the fusion of waste water in the sour production of H, thereby improve oxidation reaction efficiency;
(2) the wastewater treatment system of the utility model adopts the two-stage oxidation reactor to carry out wet oxidation in series, thereby improving the treatment effect of wastewater, and the maintenance and the disassembly are more convenient by reasonably arranging the position of the micro-interface generator;
(3) the treatment system of the utility model 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 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 provided by 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 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, the 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 the principle of the wastewater treatment system in the H acid production 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 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 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. Compare with the processing system of waste water in the sour production of prior art H, the utility model discloses a processing 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 processing system throughput of waste water is high in the sour production of H, handles the back through this processing system, can guarantee under the energy consumption condition that compares lowly, 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 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;
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.
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 processing system according to any of claims 1 to 4, wherein the micro-interface generator is a pneumatic micro-interface generator.
6. 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.
7. The treatment system of claim 6, 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.
8. The treatment system of any one of claims 1-4, further comprising a pneumatic device in communication with the air inlet.
9. The treatment system of claim 8, wherein a gas heating device is disposed on a conduit of the air compressing device in communication with the air inlet.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113087249A (en) * | 2019-12-23 | 2021-07-09 | 南京延长反应技术研究院有限公司 | System and method for treating wastewater in H acid production |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113087249A (en) * | 2019-12-23 | 2021-07-09 | 南京延长反应技术研究院有限公司 | System and method for treating wastewater in H acid production |
| CN113087249B (en) * | 2019-12-23 | 2022-04-22 | 南京延长反应技术研究院有限公司 | System and method for treating wastewater in H acid production |
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