Spiral internal circulation type electrochemical wastewater treatment device and operation method thereof

Abstract

The application provides a spiral internal circulation type electrochemical wastewater treatment device and a running method thereof, wherein the device comprises a tank body, a water distribution chamber, a reaction chamber and a drainage chamber arranged in the tank body; the water distribution chamber and the drainage chamber are located at two ends in the tank body; the reaction chamber is connected between the water distribution chamber and the drainage chamber; a first partition plate with a first water flow opening is arranged between the reaction chamber and the water distribution chamber; a second partition plate with a second water flow opening is arranged between the drainage chamber and the reaction chamber; the reaction chamber is divided into a first upflow zone, an intermediate downflow zone and a second upflow zone; BDD electrolysis modules are contained in the first upflow zone and the second upflow zone; a first wastewater circulation is formed between the first upflow zone and the intermediate downflow zone, and a second wastewater circulation is formed between the second upflow zone and the intermediate downflow zone. The device integrates two side BDD electrolysis modules in the reaction chamber, wastewater spirally travels, the structure is compact, and electrolysis is more sufficient.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of electrochemical wastewater treatment, and particularly relates to a spiral internal circulation type electrochemical wastewater treatment equipment and a running method thereof. BACKGROUND

[0002] BDD (boron-doped diamond) electrolytic wastewater treatment, as an electrochemical oxidation method, is a highly potential high-concentration / difficultly biodegradable organic wastewater treatment technology, and is particularly suitable for places where conventional biochemical means are difficult to handle. The suitable range includes: pretreatment of difficultly biodegradable organic wastewater, high-salt organic wastewater (+ recovery of salt), high-toxicity organic wastewater, high-concentration wastewater, high-ammonia-nitrogen wastewater, and strong-acid and strong-base organic wastewater (+ recovery of acid and base).

[0003] At present, in the application of BDD, the BDD material is usually packaged in a standard module, and a plurality of standard electrolytic modules are connected in series to form a BDD treatment device. A wastewater storage tank is arranged, and wastewater in the wastewater storage tank is pumped to the BDD treatment device for electrolysis, and then returned to the wastewater storage tank, and the cycle is repeated until the wastewater in the wastewater storage tank meets the standard. This method has the following disadvantages: 1. The system is relatively complex, and a pump is required to form a wastewater circulation system to achieve wastewater treatment effect, which occupies a large area, is troublesome to install, and has high energy consumption; 2. Since gas is generated during the operation of BDD, the presence of the gas reduces the actual contact area between the wastewater and the BDD electrode plate, thereby reducing the degradation efficiency compared with a single standard electrolytic module. The more standard electrolytic modules connected in series, the lower the degradation efficiency of the standard electrolytic module close to the end due to gas accumulation, and finally the overall degradation efficiency is reduced. 3. Each reaction batch is a sequencing batch reaction, and after each batch reaction is completed, the wastewater meeting the standard is discharged, and then water is added. When treating large water volume and low concentration COD wastewater, due to the short reaction time of each batch, the number of batches per day is large, which leads to a long idle time of the BDD electro-catalytic module and low utilization rate.

[0004] Therefore, the prior art still needs to be improved and developed. SUMMARY

[0005] The present application provides a spiral internal circulation type electrochemical wastewater treatment equipment and a running method thereof, and aims to solve the technical problems mentioned in the background part of the prior art electrochemical wastewater treatment equipment.

[0006] The content of the present application is as follows:

[0007] The first aspect of the present application provides a spiral internal circulation type electrochemical wastewater treatment device, comprising a tank body and a water distribution chamber, a reaction chamber and a drainage chamber arranged in the tank body; the water distribution chamber and the drainage chamber are arranged at two ends of the tank body in the length direction; the reaction chamber is connected between the water distribution chamber and the drainage chamber; a first partition plate is arranged between the reaction chamber and the water distribution chamber, and a first water flow opening is arranged at the top of the first partition plate; a second partition plate is arranged between the reaction chamber and the drainage chamber, and a second water flow opening is arranged at the top of the second partition plate; a waste gas discharge port is arranged on the tank body at the top of the reaction chamber;

[0008] The reaction chamber is divided into a first upflow zone, an intermediate downflow zone and a second upflow zone in the width direction by two parallel and spaced flow guide plates; the first upflow zone and the second upflow zone each contain a BDD electrolysis module; a first wastewater circulation is formed between the first upflow zone and the intermediate downflow zone, and a second wastewater circulation is formed between the second upflow zone and the intermediate downflow zone.

[0009] In an optional embodiment of the first aspect of the present application, each of the first upflow zone and the second upflow zone is divided into a plurality of upflow channels by a vertical partition plate, and each upflow channel contains one BDD electrolysis module.

[0010] In an optional embodiment of the first aspect of the present application, the BDD electrolysis modules in adjacent upflow channels in the first upflow zone and the second upflow zone are arranged in a staggered manner.

[0011] In an optional embodiment of the first aspect of the present application, each of the upflow channels in the first upflow zone and each of the upflow channels in the second upflow zone are arranged symmetrically; the BDD electrolysis modules in the symmetric upflow channels of the first upflow zone and the second upflow zone are also arranged symmetrically.

[0012] In an optional embodiment of the first aspect of the present application, in the upflow channel, the BDD electrolysis module is arranged close to the top end of the upflow channel or the BDD electrolysis module is arranged close to the bottom end of the upflow channel.

[0013] In an optional embodiment of the first aspect of the present application, the BDD electrolysis module comprises a flange base plate and cathode and anode plates vertically and spacedly arranged on the flange base plate; a flange interface is formed in the tank wall of the tank body at the position of each upflow channel, and a module support plate is arranged inside the corresponding upflow channel; the flange base plate is mounted on the flange interface, and the cathode and anode plates extend into the upflow channel and are supported and fixed on the module support plate.

[0014] In an optional embodiment of the first aspect of the present invention, the surfaces of the anode and cathode plates are both vertically arranged within the current-boosting channel.

[0015] In an optional embodiment of the first aspect of the present invention, an inlet flange and an inlet drain flange are provided on the bottom wall of the water distribution chamber, and a perforated transverse water distribution plate is provided in the height direction of the water distribution chamber; a drain flange and a drain drain flange are provided on the bottom wall of the drainage chamber.

[0016] In an optional embodiment of the first aspect of the present invention, the first water flow opening and the second water flow opening are both directly opposite the intermediate settling zone on both sides of the intermediate settling zone.

[0017] A second aspect of the present invention provides an operating method for a spiral internal circulation electrochemical wastewater treatment device, comprising:

[0018] Wastewater is continuously injected into the water distribution chamber, and flows into the reaction chamber after the wastewater level in the water distribution chamber exceeds the first water flow opening on the first partition.

[0019] When the liquid level in the reaction chamber submerges the BDD electrolysis module, electrolysis is started. The gas and heat generated by electrolysis cause the wastewater in the first and second upflow zones of the reaction chamber to flow upward.

[0020] Wastewater in the first and second upflow zones flows upward. After the wastewater exceeds the guide plate, it flows into the middle settling zone of the reaction chamber and flows downward to form an internal wastewater circulation within the reaction chamber.

[0021] As wastewater continues to flow into the first water inlet, the wastewater circulation in the reaction chamber gradually flows towards the drainage chamber and gradually meets the standard under the continuous electrolysis of the BDD electrolysis module.

[0022] When the wastewater level on the drainage chamber side of the reaction chamber exceeds the second water flow opening on the second partition, the wastewater that meets the electrolysis standards flows into the drainage chamber and is discharged after passing the test.

[0023] Beneficial effects: the present application provides a spiral internal circulation type electrochemical wastewater treatment equipment and its operation method, wherein the equipment comprises a tank body and a water distribution chamber, a reaction chamber and a drainage chamber arranged in the tank body; the water distribution chamber and the drainage chamber are located at both ends in the tank body; the reaction chamber is connected between the water distribution chamber and the drainage chamber; a first partition plate with a first water flow opening is arranged between the reaction chamber and the water distribution chamber; a second partition plate with a second water flow opening is arranged between the drainage chamber and the reaction chamber; the reaction chamber is divided into a first upflow zone, an intermediate downflow zone and a second upflow zone; a BDD electrolysis module is contained in each of the first upflow zone and the second upflow zone; a first wastewater circulation is formed between the first upflow zone and the intermediate downflow zone, and a second wastewater circulation is formed between the second upflow zone and the intermediate downflow zone. The equipment of the present application integrates 2-side BDD electrolysis modules in the reaction chamber, the wastewater spirally travels, the structure is compact, and the electrolysis is more sufficient. BRIEF DESCRIPTION OF DRAWINGS

[0024] Figure 1 It is a cut structure schematic view of the length direction of a spiral internal circulation type electrochemical wastewater treatment equipment from the front perspective of the present application.

[0025] Figure 2 It is a cut structure schematic view of the width direction of a spiral internal circulation type electrochemical wastewater treatment equipment from the present application.

[0026] Figure 3 It is a cut structure schematic view of a spiral internal circulation type electrochemical wastewater treatment equipment from the perspective of the present application.

[0027] Figure 4 It is a cut view of the installation mode of a BDD electrolysis module from the present application.

[0028] Figure 5 It is a schematic view of the three-dimensional structure of a spiral internal circulation type electrochemical wastewater treatment equipment from the present application.

[0029] The drawings are as follows:

[0030] 10-water distribution chamber; 20-reaction chamber; 30-drainage chamber; 40-first partition plate; 50-first water flow opening; 60-second partition plate; 70-waste gas discharge port; 80-flow guide plate; 90-first upflow zone; 100-intermediate downflow zone; 110-second upflow zone; 120-BDD electrolysis module; 130-first wastewater circulation; 140-second wastewater circulation; 150-vertical partition plate; 160-upflow channel; 170-flange base plate; 180-cathode and anode plate; 190-flange interface; 200-module support plate; 210-water inlet flange opening; 220-water inlet chamber emptying flange opening; 230-horizontal water distribution plate; 240-drainage flange opening; 250-drainage chamber emptying flange opening; 260-tank body; 270-second water flow opening. DETAILED DESCRIPTION

[0031] In order to make the objects, technical solutions and effects of the present application clearer and more explicit, the present application is further described in detail below. It should be understood that the specific embodiments described herein are only used to explain the present application and not used to limit the present application.

[0032] Referring to Figure 1 , the first aspect of the present application provides a spiral internal circulation type electrochemical wastewater treatment equipment, comprising a tank body 260 (which is a cuboid as a whole) and a water distribution chamber 10, a reaction chamber 20 and a drainage chamber 30 arranged in the tank body 260; the water distribution chamber 10 and the drainage chamber 30 are arranged at the two ends of the length direction of the tank body 260 respectively; the reaction chamber 20 is connected between the water distribution chamber 10 and the drainage chamber 30; a first partition plate 40 is arranged between the reaction chamber 20 and the water distribution chamber 10, the upper and lower ends of the first partition plate 40 are closedly connected with the top and bottom plates of the tank body 260, the two side edges of the first partition plate 40 are closedly connected with the two side plates of the tank body 260, the first partition plate 40 and the three side plates and the top and bottom of the tank body 260 form a compartment (i.e. the water distribution chamber 10), and a first water flow opening 50 is arranged on the top of the first partition plate 40, which is used for water flow circulation between the water distribution chamber 10 and the reaction chamber 20.

[0033] Similarly, referring to Figure 1 , a second partition plate 60 is arranged between the drainage chamber 30 and the reaction chamber 20, the second partition plate 60 and the three side plates and the top and bottom of the other side of the tank body 260 form another compartment (i.e. the drainage chamber 30), a second water flow opening 270 is arranged on the top of the second partition plate 60, which is used for water flow circulation between the reaction chamber 20 and the drainage chamber 30; a waste gas exhaust port 70 is arranged on the tank body 260 at the top of the reaction chamber 20, and an exhaust pipe and a fan are connected to the waste gas exhaust port 70.

[0034] In the first aspect of the present application, referring to Figure 2 and Figure 3 , the reaction chamber 20 is divided into a first upflow zone 90, an intermediate downflow zone 100 (on both sides of the intermediate downflow zone 100, the first water flow opening 50 and the second water flow opening 270 are opposite to the intermediate downflow zone 100) and a second upflow zone 110 in the width direction by two parallel and spaced flow guide plates 80 in the reaction chamber 20; if the length direction of the tank body 260 is regarded as the front-rear direction, the reaction chamber 20 is divided in the left-right direction in the tank body 260, the two ends of each flow guide plate 80 are connected with the first partition plate 40 and the second partition plate 60 respectively, and the upper and lower ends of the first partition plate 40 and the second partition plate 60 are not closed to allow water flow.

[0035] In the first aspect of the present application, Figure 4 The first rising flow area 90 and the second rising flow area 110 each contain a BDD electrolysis module 120, and the BDD electrolysis module 120 in the first rising flow area 90 and the BDD electrolysis module 120 in the second rising flow area 110 are each provided with a plurality of BDD electrolysis modules in the length direction of the tank body 260. The first rising flow area 90 and the intermediate sinking flow area 100 form a first wastewater circulating flow 130, and the second rising flow area 110 and the intermediate sinking flow area 100 form a second wastewater circulating flow 140.

[0036] In the first aspect of the present application, Figure 3 The first rising flow area 90 and the second rising flow area 110 are each divided into a plurality of rising flow channels 160 by a vertical partition plate 150, and each of the rising flow channels 160 contains one BDD electrolysis module. In the present application, the BDD electrolysis modules in the first rising flow area 90 and the second rising flow area 110 are separated by the vertical partition plate 150, and the first rising flow area 90 and the second rising flow area 110 do not have dead water and invalid water flow areas in the length direction of the tank body 260, and the bubbles generated by each BDD electrolysis module do not interfere with each other, thereby avoiding affecting the electrolysis efficiency of the BDD electrolysis module.

[0037] In the present application, Figure 4 And Figure 5 The BDD electrolysis module includes a flange base plate 170 and cathode and anode plates 180 vertically spaced on the flange base plate 170 (the anode plate is a BDD electrode plate, and the cathode plate is a titanium plate or a stainless steel plate), and the flange base plate 170 is provided with a terminal post on the side opposite to the cathode and anode plates 180. In the present application, a flange interface 190 is formed on the tank wall of the tank body 260 at the position of each rising flow channel 160, and a module support plate 200 is provided inside the corresponding rising flow channel 160. The flange base plate 170 is installed on the flange interface 190, the cathode and anode plates 180 extend into the rising flow channel 160 and are supported and fixed on the module support plate 200, and the plate surfaces of the cathode and anode plates 180 are vertically arranged in the rising flow channel 160. In the present application, the plate surfaces of the cathode and anode plates 180 are vertically arranged, and the gaps between adjacent electrode plates are also vertically arranged, which facilitates the smooth upward movement of the bubbles generated by electrolysis.

[0038] In an alternative embodiment of the present application, the anode plate of the BDD electrolysis module is a boron-doped diamond and metal matrix composite, which is composed of a metal matrix and diamond reinforcement dispersed in the metal matrix, including but not limited to diamond composite film layer material; the diamond reinforcement is composed of diamond particles and a diamond surface modification layer, which is composed of a diamond film layer and a diamond transition layer formed during the growth of the diamond film layer, and the main component is a carbon-metal bond formed by diamond and metal matrix, which can enhance the bonding force between the diamond film layer and the metal matrix.

[0039] Specifically, the electrode plate containing the diamond reinforcement has the following gain effects on the electrode module: it takes diamond particles as the core, sets a polycrystalline diamond transition layer on the surface, and then sets a doped diamond shell layer, wherein the high-purity polycrystalline diamond transition layer is in-situ grown on the single-crystal diamond particles, maintaining the original properties of single-crystal diamond, such as high thermal conductivity, high hardness, and high wear resistance. The doped diamond shell layer is in-situ grown on the polycrystalline diamond transition layer, and this structure containing the transition layer can improve the wettability and bonding force of diamond and metal. The electrode module with this structure has a long service life and can work stably under strong water flow impact without BDD film layer peeling. In addition, the diamond surface modification layer set on the outer surface of the single-crystal diamond particles can also play an isolation and protection role for the diamond particles, which can protect the diamond from graphitization, oxidation reaction and other chemical reactions under high temperature conditions; at the same time, it can improve the adhesion of the diamond, the modification layer acts as a bonding bridge between the two, and it can also improve the wettability of the diamond and the matrix metal; and it can also improve the strength of the diamond particles, the plating layer plays a reinforcing and toughening role, and the diamond surface defects, micro-cracks and small pores can be compensated by the modification layer to improve the strength. In addition, the addition of a small amount of rare earth elements (rare earth elements are one or a combination of lanthanum, cerium, neodymium, europium, gadolinium, dysprosium, holmium, ytterbium, lutetium, yttrium, and scandium) in the metal matrix can refine the matrix grains, purify the interface between the diamond and the matrix, promote the reaction between the carbide in the matrix and the diamond, and improve the adhesion between the metal matrix and the diamond, thereby improving the interface bonding state of the matrix and the diamond. The finished structure of the diamond / metal matrix composite used is not limited, i.e., it can be a regular structure or made into a multi-size or special-shaped structure to meet the module requirements.

[0040] In the first aspect of the present application, the BDD electrolysis modules 120 in the first up-flow zone 90 and the second up-flow zone 110 are staggered. Specifically, in the up-flow channel 160, the BDD electrolysis modules 120 are arranged near the top end of the up-flow channel 160 or near the bottom end of the up-flow channel 160. Staggered means that if the BDD electrolysis modules 120 in the left up-flow channel 160 are arranged at the bottom end of the up-flow channel 160, the BDD electrolysis modules 120 in the right up-flow channel 160 are arranged at the top end of the up-flow channel 160. Further, in the present application, all the BDD electrolysis modules 120 arranged at the bottom end of the up-flow channel 160 form a straight line, and all the BDD electrolysis modules 120 arranged at the top end of the up-flow channel 160 form a straight line.

[0041] In the first aspect of the present application, the up-flow channels 160 in the first up-flow zone 90 and the second up-flow zone 110 are symmetrically arranged, that is, the up-flow channels 160 on both sides of the middle down-flow zone 100 are symmetrically arranged. The BDD electrolysis modules in the symmetrically arranged up-flow channels 160 of the first up-flow zone 90 and the second up-flow zone 110 are also symmetrically arranged, that is, the heights of the BDD electrolysis modules in the two up-flow channels 160 on the same straight line on both sides of the middle down-flow zone 100 are equal (that is, symmetric). The up-flow channels 160 and the BDD electrolysis modules on both sides of the middle down-flow zone 100 are symmetrically arranged, which can ensure the synchronization of electrolysis on both sides of the middle down-flow zone 100 and avoid the non-uniformity of the electrolysis wastewater concentration at the same progress position, thereby ensuring the qualification of the electrolyzed wastewater.

[0042] Referring to Figure 1 and Figure 5 In the first aspect of the present application, the water inlet flange 210 and the water inlet chamber emptying flange 220 are arranged on the groove wall at the bottom of the water distribution chamber 10 (more close to the bottom), and the perforated transverse water distribution plate 230 is arranged in the height direction of the water distribution chamber 10. The transverse water distribution plate 230 can ensure the water level of the water distribution chamber 10 to be flat, thereby stabilizing the water inlet flow and avoiding the change of water inlet load. The transverse water distribution plate 230 can also play a role in filtering large impurities. The drain flange 240 and the drain chamber emptying flange 250 are arranged on the groove wall at the bottom of the drain chamber 30 (more close to the bottom), and the reaction chamber emptying flange is also arranged on the groove wall at the bottom of the reaction chamber 20.

[0043] The second aspect of the present application provides a running method of the spiral internal circulation type electrochemical wastewater treatment equipment, comprising:

[0044] continuously injecting wastewater into the water distribution chamber, when the wastewater level in the water distribution chamber exceeds the first water flow opening on the first partition, the wastewater flows into the reaction chamber;

[0045] when the liquid level in the reaction chamber submerges the BDD electrolysis module, electrolysis is started (which can be monitored by a liquid level meter), the gas and heat generated by electrolysis make the wastewater in the first upflow zone and the second upflow zone of the reaction chamber flow upwards, and the gas is discharged through the exhaust gas outlet after reaching the top of the reaction chamber;

[0046] The wastewater in the first upflow zone and the second upflow zone flows upwards, and when the wastewater exceeds the flow guide plate, the wastewater flows into the middle downflow zone of the reaction chamber and flows downwards, forming an internal circulation of wastewater in the reaction chamber;

[0047] As the wastewater continues to flow through the first water flow opening, the wastewater circulation in the reaction chamber gradually flows to the drainage chamber side and gradually meets the standard under the continuous electrolysis of the BDD electrolysis module;

[0048] When the wastewater level on the drainage chamber side of the reaction chamber exceeds the second water flow opening on the second partition, the wastewater that meets the standard under electrolysis flows into the drainage chamber and is discharged externally after being detected to meet the standard.

[0049] In the second aspect of the present application, when electrolysis is started, the BDD electrolysis module can be started in pairs from the drainage chamber side to the water distribution chamber side (two BDD electrolysis modules at symmetrical positions on the left and right sides of the reaction chamber are called a pair), the time interval for starting each pair of BDD electrolysis modules is, for example, 30 seconds to 1 minute, and the electrolysis power of each pair of BDD electrolysis modules increases in equal differences from the water distribution chamber side to the drainage chamber side (the electrolysis power of the BDD electrolysis module with a higher height is greater than that of the BDD electrolysis module with a lower height), so that the water on the drainage chamber side flows faster and has lower pressure, and the water on the water distribution chamber side flows slower and has higher pressure, under the action of the pressure, the wastewater will spontaneously flow to the drainage chamber side, through the starting mode of the BDD electrolysis module of the present application, the electrolysis workload of the BDD electrolysis module is more uniform, and the problem of electrode plate blockage of the BDD electrolysis module on the drainage chamber side can be better prevented.

[0050] In an alternative embodiment of the second aspect of the application, the spiral internal circulation type electrochemical wastewater treatment device is configured with an autonomous learning control system, which comprises a central computing module, an exponential current output module, a COD online detector and a flow rate monitoring device. The central computing module is used to analyze the collected data of COD concentration, current, flow rate, etc. and send control instructions: the central computing module is built-in with a calculation model of the relationship between COD degradation and current and flow rate changes, and the energy consumption of each batch of wastewater treatment is calculated after the treatment is completed. The lowest energy consumption when the same COD initial concentration is treated to the standard in the database is compared, and the current and flow rate parameters are continuously corrected autonomously according to the calculation model to find the corresponding parameters for running at the lowest energy consumption. The exponential current output module is used to convert the current parameter correction instructions of the central computing module into corresponding current output to the BDD. The COD online detection device is used to detect the COD change of wastewater from the influent to the effluent in real time. First, the initial COD concentration is sent to the central computing module, and the central computing module sends the optimal operating parameters of the COD to the exponential current output module for operation according to the database. The flow rate monitoring device is used to monitor the speed of organic wastewater through the BDD material and send the flow rate signal to the central computing module, so as to calculate the influence of different flow rates on the degradation efficiency of the BDD and obtain the best economic flow rate.

[0051] At the first use, for each batch of wastewater, there is no available electrolysis current and flow rate data for the COD concentration of the batch of wastewater. At this time, the initial parameters need to be determined according to the actual wastewater pilot test, including the exponential current parameter, the flow rate, the allowable temperature, etc. Specifically, since each wastewater composition and concentration is different, the required parameters for degradation are different, and the wastewater concentration will fluctuate during actual operation. Therefore, the operating parameters need to be determined according to the inflow COD concentration during actual operation. However, it is impossible to do all cases at the beginning of the project, so the wastewater concentration of a representative stage is taken to the laboratory for testing. After sampling, the COD concentration is measured first, and the limiting current density is calculated to the corresponding current. Then, the current is used as a constant current to be added to the BDD for electrolysis until the wastewater reaches the standard. The flow rate is a fixed reference flow rate of the BDD material through a large number of tests of other devices before. The reference flow rate is directly used for small test. In this way, the COD degradation curve of wastewater can be obtained by sampling water at different stages to measure COD. The initial exponential current parameter is determined by the degradation curve, and the energy consumption corresponding to the exponential current parameter can be calculated. The actual introduced flow rate is the aforementioned reference flow rate.

[0052] After starting to run, each time the running data is stored, the total energy consumption from the start to the wastewater standard is calculated, and the increase and decrease of the energy consumption are compared to correct the parameters in the next run, and the adjustment method is as follows: Since the variable parameters are current and flow rate, each optimization adjustment will fix one variable, and the flow rate is fixed first. Then increase the exponential current parameter, electrolyze to the standard after comparison with the initial value, if the energy consumption increases, decrease the exponential current parameter in the next time, and so on to find the best exponential current parameter under a certain COD concentration. Then take the flow rate as a variable, and the method is the same as before, and the best flow rate is found. Through continuous data accumulation and comparison, the best running parameters corresponding to COD (i.e. the historical best exponential current parameter and the historical best flow rate corresponding to a certain COD concentration described above) can be obtained. The longer the running time is, the more accurate it is, and compared with the original control mode, the running energy consumption can be greatly reduced, and the running safety can be improved.

[0053] In summary, the present application provides a spiral internal circulation type electrochemical wastewater treatment equipment and its operation method, wherein the equipment comprises a tank body and a water distribution chamber, a reaction chamber and a drainage chamber arranged in the tank body; the water distribution chamber and the drainage chamber are located at both ends in the tank body; the reaction chamber is connected between the water distribution chamber and the drainage chamber; a first partition plate with a first water flow opening is arranged between the reaction chamber and the water distribution chamber; a second partition plate with a second water flow opening is arranged between the drainage chamber and the reaction chamber; the reaction chamber is divided into a first upflow zone, an intermediate downflow zone and a second upflow zone; BDD electrolysis modules are contained in the first upflow zone and the second upflow zone; a first wastewater circulation is formed between the first upflow zone and the intermediate downflow zone, and a second wastewater circulation is formed between the second upflow zone and the intermediate downflow zone. The equipment integrates 2-side BDD electrolysis modules in the reaction chamber, the wastewater spirally travels, the structure is compact, and the electrolysis is more sufficient.

[0054] The above-described embodiments are only used to illustrate the technical solutions of the present application, rather than limit them; although the foregoing embodiments of the present application have been described in detail, those skilled in the art should understand that they can modify the technical solutions recorded in the foregoing embodiments, or make equivalent replacement for some technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the present application.

Claims

1. A spiral internal circulation electrochemical wastewater treatment device, characterized in that, The system includes a tank and a water distribution chamber, a reaction chamber, and a drainage chamber disposed within the tank. The water distribution chamber and the drainage chamber are respectively located at opposite ends of the tank along its length. The reaction chamber is connected between the water distribution chamber and the drainage chamber. A first partition is provided between the reaction chamber and the water distribution chamber, and a first water flow opening is provided at the top of the first partition. A second partition is provided between the drainage chamber and the reaction chamber, and a second water flow opening is provided at the top of the second partition. An exhaust gas outlet is provided on the tank at the top of the reaction chamber. The reaction chamber is divided into a first upflow zone, an intermediate settling zone, and a second upflow zone in the width direction by two parallel and spaced guide plates. Both the first and second upflow zones contain BDD electrolysis modules. A first wastewater circulation is formed between the first upflow zone and the intermediate settling zone, and a second wastewater circulation is formed between the second upflow zone and the intermediate settling zone. Both the first and second upflow zones are divided into several upflow channels by vertical partitions, and each upflow channel contains one BDD electrolysis module. In the first and second current-boosting regions, the BDD electrolysis modules in adjacent current-boosting channels are staggered. The current-boosting channels in the first and second current-boosting regions are symmetrically arranged. The BDD electrolysis modules in the corresponding current-boosting channels in the first and second current-boosting regions are also symmetrically arranged. In the current-boosting channels, the BDD electrolysis modules are positioned near the top of the current-boosting channel or near the bottom of the current-boosting channel.

2. The spiral internal circulation electrochemical wastewater treatment equipment according to claim 1, characterized in that, The BDD electrolysis module includes a flange base plate and anode and cathode plates vertically spaced on the flange base plate; a flange interface is provided on the tank wall of the tank at the location of each current riser channel, and a module support plate is provided inside the current riser channel corresponding to the flange interface; the flange base plate is installed on the flange interface, and the anode and cathode plates extend into the current riser channel and are supported and fixed on the module support plate.

3. The spiral internal circulation electrochemical wastewater treatment equipment according to claim 2, characterized in that, Within the current-boosting channel, the surfaces of both the anode and cathode plates are vertically oriented.

4. The spiral internal circulation electrochemical wastewater treatment equipment according to claim 1, characterized in that, The bottom wall of the water distribution chamber is provided with a water inlet flange and a water inlet chamber drain flange, and a perforated horizontal water distribution plate is provided in the height direction of the water distribution chamber; the bottom wall of the drainage chamber is provided with a drainage flange and a drainage chamber drain flange.

5. The spiral internal circulation electrochemical wastewater treatment equipment according to claim 1, characterized in that, On both sides of the intermediate settling zone, the first water flow opening and the second water flow opening are directly opposite the intermediate settling zone.

6. A method for operating a spiral internal circulation electrochemical wastewater treatment device, characterized in that, The internal circulation electrochemical wastewater treatment equipment according to any one of claims 1-5 includes: Wastewater is continuously injected into the water distribution chamber, and flows into the reaction chamber after the wastewater level in the water distribution chamber exceeds the first water flow opening on the first partition. When the liquid level in the reaction chamber submerges the BDD electrolysis module, electrolysis is started. The gas and heat generated by electrolysis cause the wastewater in the first and second upflow zones of the reaction chamber to flow upward. Wastewater in the first and second upflow zones flows upward. After the wastewater exceeds the guide plate, it flows into the middle settling zone of the reaction chamber and flows downward to form an internal wastewater circulation within the reaction chamber. As wastewater continues to flow into the first water inlet, the wastewater circulation in the reaction chamber gradually flows towards the drainage chamber and gradually reaches the standard under the continuous electrolysis of the BDD electrolysis module. When the wastewater level on the drainage chamber side of the reaction chamber exceeds the second water flow opening on the second partition, the wastewater that meets the electrolysis standards flows into the drainage chamber and is discharged after passing the test.

Images