CN104925911A - Dynamic electrocatalytic oxidation experiment system for sewage - Google Patents
Dynamic electrocatalytic oxidation experiment system for sewage Download PDFInfo
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- CN104925911A CN104925911A CN201510211258.0A CN201510211258A CN104925911A CN 104925911 A CN104925911 A CN 104925911A CN 201510211258 A CN201510211258 A CN 201510211258A CN 104925911 A CN104925911 A CN 104925911A
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Abstract
The invention discloses a dynamic electrocatalytic oxidation experiment system for sewage. The dynamic electrocatalytic oxidation experiment system comprises a peristaltic pump, an electrocatalytic oxidation vessel and a stirring vessel, wherein a water inlet of the peristaltic pump is communicated with a water outlet of the stirring vessel, a water outlet of the peristaltic pump is communicated with a water inlet of the electrocatalytic oxidation vessel, a water outlet of the electrocatalytic oxidation vessel is communicated with a water inlet of the stirring vessel, a plurality of electrode plates are arranged in the electrocatalytic oxidation vessel, a gap exists between every two adjacent electrode plates, meanwhile, all electrode plates are in a suspended state, gaps exist between the electrode plates and the bottom face and side faces of electrocatalytic oxidation vessel, and the electrode plates are located below a liquid surface of the electrocatalytic oxidation vessel; and the electrode plates comprise anode plates and cathode plates, and the anode plates and the cathode plates are placed in a spaced manner.
Description
Technical field
The present invention relates to environmental technology field, specifically sewage dynamic electric catalytic system.
Background technology
Coked waste water is the waste water produced in the high temperature carbonization of coal, gas purification and Chemicals treating process.Current employing biochemical process can remove the organic pollutant such as phenols and ammonia nitrogen in this kind of waste water substantially, but still do not reach discharging standards or enterprise's reuse requirement containing the heterocycle of some difficult degradations or many lopps organic pollutant in the water outlet after process, need advanced treatment be carried out.
By Electrocatalytic Oxidation is cleaning method, and without the need to adding oxygenant, non-secondary pollution in addition, floor space is little, clearance is high, selectivity is strong, can advanced treatment on coking wastewater.A lot of to the research of By Electrocatalytic Oxidation process waste water both at home and abroad, but mostly concentrate in the research to influence factor, as the impact on water treatment effect such as electrode materials, current density, polar plate spacing, bath voltage, but seldom study energy consumption problem.Although By Electrocatalytic Oxidation can Treatment of Wastewater in Coking effectively, improve the biodegradability of waste water, high energy consumption constrains its application in the treatment of waste water.Therefore need to be studied the energy consumption problem in catalytic oxidation Treatment of Wastewater in Coking.
Summary of the invention
The object of the present invention is to provide a kind of sewage dynamic electric catalytic system, this system is designed to a set of independently dynamic electric catalytic system, may be used for the relation studying energy consumption and By Electrocatalytic Oxidation.
Object of the present invention is achieved through the following technical solutions: sewage dynamic electric catalytic system, comprise peristaltic pump, catalytic oxidation container, stirred vessel, wherein, the water-in of peristaltic pump is communicated with the water outlet of stirred vessel, the water outlet of peristaltic pump is communicated with the water-in of catalytic oxidation container, the water outlet of catalytic oxidation container is communicated with the water-in of stirred vessel, some battery lead plates are provided with in catalytic oxidation container, gap is there is between adjacent electrode plates, all battery lead plates are in vacant state simultaneously, the bottom surface of battery lead plate and catalytic oxidation container, all there is gap in side, and battery lead plate is in below the liquid level in catalytic oxidation container, battery lead plate comprises positive pole electroplax and negative pole electroplax, and positive pole electroplax and negative pole electroplax interval are placed.
The operational process of said apparatus is: sewage is full of in peristaltic pump, catalytic oxidation container, stirred vessel and the communication path between them; Under the pushing effect of peristaltic pump, peristaltic pump is entered into after sewage is stirred in stirred vessel, finally be pushed into catalytic oxidation container, in catalytic oxidation container, every 2 of battery lead plate is that positive and negative direct supply is connected in one group of formation, and sewage obtains catalytic oxidation in catalytic oxidation container; Battery lead plate is erected at reactor center position and has certain distance with catalytic oxidation container bottoms, side, the water surface, facilitates current to pass through, and eliminates current dead angle when stirring.In experimentation, we can change the electric current of battery lead plate, quantity, peristaltic pump the parameter such as flow velocity as unique variable parameter, make the result run according to it measure the relation drawing energy waste and By Electrocatalytic Oxidation, and find best implementation method.
When flow velocity is 400 mL/min, the treatment effect of COD is the poorest, and after processing 360 min, COD is only down to 92.1 mg/L from 123.6 mg/L, and after processing 360 min equally, flow velocity is that the treatment effect in 20,50,200 mL/min situations is more or less the same.When flow velocity is 50 mL/min, COD removes speed is the fastest, processes 120 min COD and can be reduced to 72.6 mg/L, close to Schwellenwert.Known flow velocity is that the EC under 50 mL/min conditions remains minimum, is only 78.6 Wh/g during 120 min, so flow velocity 50 mL/min is optimum value.Therefore, under plug-flow is circulating fluidized, excessive or too small flow velocity is all unfavorable for the carrying out reacted.Because sewage is circular treatment, so under different in flow rate the actual treatment time of sewage all the same, if now flow velocity is too fast, sewage cannot fully contact with pole plate thus cause efficiency to reduce, if water flow velocity is spent slowly, although the high overall COD removal speed of Local C OD clearance is lower between pole plate.So only have suitable flow velocity could ensure that the mass transfer velocity of oxygenant on the one hand, also ensure that organism is combined with oxygenant and the time of oxidizing reaction occurs on the other hand, finally reach and not only improve COD degradation rate and efficiency, also make electric energy obtain efficiency utilization.
Preferably, described positive pole electroplax is ruthenium titanium net, and negative pole electroplax is titanium net.
Preferably, the water-in of catalytic oxidation container comprises the water inlet be communicated with peristaltic pump water outlet to be responsible for, the part that water inlet supervisor extends to catalytic oxidation internal tank is provided with the quantity exit branch equal with battery lead plate, and what exit branch was corresponding is arranged on immediately below battery lead plate; Said structure can make to shunt from the water of exit branch ejection respectively through the guide functions of battery lead plate, further reaches the current dead angle of eliminating when stirring, and reduces short flow phenomenon.
Preferably, be provided with magnetic stirring apparatus below described stirred vessel, stirred vessel inside is provided with magnetic rotor.
The quantity of battery lead plate mostly is 8 most.
The invention has the advantages that: structure is simple, and cost is low, simple and quick.
Accompanying drawing explanation
Fig. 1 is the schematic side view of embodiment 1.
Reference numeral in figure is expressed as: 1, peristaltic pump; 2, catalytic oxidation container; 21, water inlet supervisor; 22, exit branch; 23, battery lead plate; 3, stirred vessel; 4, magnetic rotor; 5, magnetic stirring apparatus.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited thereto.
Embodiment 1:
As shown in Figure 1,
Sewage dynamic electric catalytic system, comprise peristaltic pump 1, catalytic oxidation container 2, stirred vessel 3, wherein, the water-in of peristaltic pump 1 is communicated with the water outlet of stirred vessel 3, the water outlet of peristaltic pump 1 is communicated with the water-in of catalytic oxidation container 2, the water outlet of catalytic oxidation container 2 is communicated with the water-in of stirred vessel 3, some battery lead plates 23 are provided with in catalytic oxidation container 2, gap is there is between adjacent electrode plates, all battery lead plates are in vacant state simultaneously, the bottom surface of battery lead plate and catalytic oxidation container 2, all there is gap in side, and battery lead plate is in below the liquid level in catalytic oxidation container 2, battery lead plate comprises positive pole electroplax and negative pole electroplax, and positive pole electroplax and negative pole electroplax interval are placed.
The operational process of said apparatus is: sewage is full of in peristaltic pump 1, catalytic oxidation container 2, stirred vessel 3 and the communication path between them; Under the pushing effect of peristaltic pump 1, sewage enters into peristaltic pump 1 after being stirred in stirred vessel 3, finally be pushed into catalytic oxidation container 2, in catalytic oxidation container 2, every 2 of battery lead plate is that positive and negative direct supply is connected in one group of formation, and sewage obtains catalytic oxidation in catalytic oxidation container 2; Battery lead plate is erected at reactor center position and has certain distance with catalytic oxidation container 2 bottom surface, side, the water surface, facilitates current to pass through, and eliminates current dead angle when stirring.In experimentation, we can change the electric current of battery lead plate, quantity, peristaltic pump 1 the parameter such as flow velocity as unique variable parameter, make the result run according to it measure the relation drawing energy waste and By Electrocatalytic Oxidation, and find best implementation method.
When flow velocity is 400 mL/min, the treatment effect of COD is the poorest, and after processing 360 min, COD is only down to 92.1 mg/L from 123.6 mg/L, and after processing 360 min equally, flow velocity is that the treatment effect in 20,50,200 mL/min situations is more or less the same.When flow velocity is 50 mL/min, COD removes speed is the fastest, processes 120 min COD and can be reduced to 72.6 mg/L, close to Schwellenwert.Known flow velocity is that the EC under 50 mL/min conditions remains minimum, is only 78.6 Wh/g during 120 min, so flow velocity 50 mL/min is optimum value.Therefore, under plug-flow is circulating fluidized, excessive or too small flow velocity is all unfavorable for the carrying out reacted.Because sewage is circular treatment, so under different in flow rate the actual treatment time of sewage all the same, if now flow velocity is too fast, sewage cannot fully contact with pole plate thus cause efficiency to reduce, if water flow velocity is spent slowly, although the high overall COD removal speed of Local C OD clearance is lower between pole plate.So only have suitable flow velocity could ensure that the mass transfer velocity of oxygenant on the one hand, also ensure that organism is combined with oxygenant and the time of oxidizing reaction occurs on the other hand, finally reach and not only improve COD degradation rate and efficiency, also make electric energy obtain efficiency utilization.
Preferably, described positive pole electroplax is ruthenium titanium net, and negative pole electroplax is titanium net.
Preferably, the water-in of catalytic oxidation container 2 comprises the water inlet be communicated with peristaltic pump 1 water outlet and is responsible for 21, the part that water inlet supervisor 21 extends to catalytic oxidation container 2 inside is provided with the quantity exit branch equal with battery lead plate 22, exit branch 22 correspondence be arranged on immediately below battery lead plate; Said structure can make the water sprayed from exit branch 22 shunt respectively through the guide functions of battery lead plate, further reaches the current dead angle of eliminating when stirring, and reduces short flow phenomenon.
Preferably, be provided with magnetic stirring apparatus 5 below described stirred vessel, stirred vessel inside is provided with magnetic rotor 4.
The quantity of battery lead plate mostly is 8 most.
Experimentation of the present invention is as follows: experimental water parameter:
Experimental water is from the coking chemical waste water after A2/O art breading, and COD is 110 ~ 125 mg/L, and pH is about 6.45, and ammonia nitrogen mass concentration is about 32.2 mg/L.For meeting the requirement of follow-up reuse technology to water quality, the water outlet COD after catalytic oxidation process requires to be less than 75 mg/L.
The mensuration of COD: use CTL-12 type COD Quick testing instrument, adopts rapid-digestion method wastewater measurement COD.
Experimental implementation: add in said system by 2 L waste water, be respectively 20,50,200,400 mL/min by changing peristaltic pump speed adjustment flow, current density is adjusted to 100 A/m2, and magnetic stirring apparatus rotating speed is 1 800 r/min.Respectively at 0,40,80,120,160,240,360 min timing node places, sampling and measuring COD from stirred vessel.
The calculating of waste water energy consumption: calculate the energy consumption that catalytic oxidation removes unit mass COD by formula (1).
ＥＣ＝（U*I*t/V*△COD）*1000（1）。
In formula: EC is the energy consumption removing unit mass COD, Wh/g; U is bath voltage, V; I is electric current, A; T is the treatment time, h; V is the process water yield, L; Δ COD is the difference of COD before and after reaction, mg/L.
When current density is increased to 100 A/m2 from 50 A/m2, COD treatment effect significantly improves, but when current density is increased to 200 A/m2, COD removal effect declines on the contrary.This is because when low current, electric current is larger, the transfer rate of electronics in electrode and waste water is faster, and the activated intermediate product of tool is more, and COD removal effect is better.But because direct oxidation needs pollutent mass transfer to the surface of electrode, and indirect oxidation needs the strong oxidizer height of pollutent and generation to mix, namely electrochemical speed of reaction is subject to the restriction of the mass transfer effect in reactor, is to a certain degree difficult to afterwards improve treatment effect again so current density is increased to.And current density is too high that side reaction (as liberation of hydrogen, oxygen evolution reaction) can be impelled on the contrary to occur, reduce current efficiency.Consider above experimental result, in subsequent experimental, current density is chosen as 100 A/m2.
During actual treatment coking chemical waste water, because the process water yield increases, need corresponding increase electrocatalysis oxidation apparatus volume and battery lead plate reaction area, this is by increasing quantity of polar plate or increasing battery lead plate area and corresponding increase battery lead plate spacing realizes.But in actually operating, rear a kind of mode will cause bath voltage to raise, the not only easy passivation of pole plate, work-ing life decline, and when voltage exceeded analyse oxygen overvoltage time, also can cause analysing the side reactions such as oxygen sharply increases, thus causes current efficiency to reduce.Therefore the front a kind of mode of many employings in practical application.
Ideally, namely quantity of polar plate increase increases pole plate reaction area, and treatment effect can corresponding lifting, and utilization rate of electrical remains unchanged.If current cannot walk around pole plate, can only pass through from the little mesh pole plate, too much pole plate serves the effect of dividing plate to a certain extent, thus hinder fully mixing of water oxygen agent and organic pollutant, make the short flow phenomenon of inside reactor serious, oxygenant mass transfer velocity declines, and causes treatment effect to decline.By contrast, battery lead plate method to set up effect of the present invention is excellent, more can improve efficiency and make full use of the advantage of 4 pairs of electrodes after structure is improved.From above-mentioned experimental result, in electrocatalysis oxidation reaction, if when in solution, the mass transfer velocity of oxygenant is the limiting factor of COD removal efficiency, raising electrical energy fed and effective affecting acreage significantly cannot improve processing efficiency, and could will realize by improving mass transfer velocity, can also efficiency be improved while doing like this, reduce energy consumption.
Dynamichandling part is the circulating fluidised form of plug-flow, the different fluidised forms studying waste water in reactor with this are on the impact of electrocatalysis oxidation reaction, result shows: when flow velocity is 400 mL/min, the treatment effect of COD is the poorest, after processing 360 min, COD is only down to 92.1 mg/L from 123.6 mg/L, and after processing 360 min equally, flow velocity is that the treatment effect in 20,50,200 mL/min situations is more or less the same.When flow velocity is 50 mL/min, COD removes speed is the fastest, processes 120 min COD and can be reduced to 72.6 mg/L, close to Schwellenwert.Known flow velocity is that the EC under 50 mL/min conditions remains minimum, is only 78.6 Wh/g during 120 min, so flow velocity 50 mL/min is optimum value.
Result illustrates, under plug-flow is circulating fluidized, excessive or too small flow velocity is all unfavorable for the carrying out reacted.Because sewage is circular treatment, so under different in flow rate the actual treatment time of sewage all the same, if now flow velocity is too fast, sewage cannot fully contact with pole plate thus cause efficiency to reduce, if water flow velocity is spent slowly, although the high overall COD removal speed of Local C OD clearance is lower between pole plate.So only have suitable flow velocity could ensure that the mass transfer velocity of oxygenant on the one hand, also ensure that organism is combined with oxygenant and the time of oxidizing reaction occurs on the other hand, finally reach and not only improve COD degradation rate and efficiency, also make electric energy obtain efficiency utilization.
As mentioned above, then well the present invention can be realized.
Claims (5)
1. sewage dynamic electric catalytic system, it is characterized in that: comprise peristaltic pump (1), catalytic oxidation container (2), stirred vessel (3), wherein, the water-in of peristaltic pump (1) is communicated with the water outlet of stirred vessel (3), the water outlet of peristaltic pump (1) is communicated with the water-in of catalytic oxidation container (2), the water outlet of catalytic oxidation container (2) is communicated with the water-in of stirred vessel (3), some battery lead plates (23) are provided with in catalytic oxidation container (2), gap is there is between adjacent electrode plates, all battery lead plates are in vacant state simultaneously, the bottom surface of battery lead plate and catalytic oxidation container (2), all there is gap in side, and battery lead plate is in below the liquid level in catalytic oxidation container (2), battery lead plate comprises positive pole electroplax and negative pole electroplax, and positive pole electroplax and negative pole electroplax interval are placed.
2. sewage dynamic electric catalytic system according to claim 1, is characterized in that: described positive pole electroplax is ruthenium titanium net, and negative pole electroplax is titanium net.
3. sewage dynamic electric catalytic system according to claim 1, it is characterized in that: the water-in of catalytic oxidation container (2) comprises the water inlet be communicated with peristaltic pump (1) water outlet to be responsible for (21), the part that water inlet supervisor (21) extends to catalytic oxidation container (2) inner is provided with the quantity exit branch equal with battery lead plate (22), corresponding being arranged on immediately below battery lead plate of exit branch (22).
4. sewage dynamic electric catalytic system according to claim 1, it is characterized in that: be provided with magnetic stirring apparatus (5) below described stirred vessel, stirred vessel inside is provided with magnetic rotor (4).
5. sewage dynamic electric catalytic system according to claim 1, is characterized in that: the quantity of battery lead plate mostly is 8 most.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108069491A (en) * | 2016-11-18 | 2018-05-25 | 北京化工大学 | For the electrocatalytic oxidation method and reaction unit of used water difficult to degradate |
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| JP3922639B2 (en) * | 2002-12-10 | 2007-05-30 | 澤田 欽二 | Electrolyzed water generator and multi-electrolyzed water supply system using the same |
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