CN106517425B - A kind of processing method of oily waste water - Google Patents
A kind of processing method of oily waste water Download PDFInfo
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Abstract
The invention discloses a kind of processing methods of oily waste water, this method comprises: being electrolysed oily waste water in the presence of pink salt, the oily waste water after the electrolysis is settled, wherein the anode plate used that is electrolysed is investigation of titanium anode coated with metal oxide.Oily wastewater treatment method of the present invention can be electrolysed in the case where not consumable anode, obtain the triple role of electrolytic flocculation, electrofloatation and free-radical oxidation, to reach the treatment effect of preferable oily waste water, treated, and waste water can be with direct emission or reuse.
Description
Technical field
The present invention relates to a kind of processing methods of oily waste water.
Background technique
Oily waste water is a kind of common industrial wastewater, its source is very extensive, mainly includes oil exploitation and refining
Industry, petrochemical industry and food and drink and food-processing industry.According to statistics, at least 500~10,000,000 tons annual in the world
Oils waste water enters water body by all means, while causing water resource pollution and the oily wasting of resources, oil pollutant pair
Environmental ecology and human health also have extreme influence.Therefore, all the time domestic and international research institution all to the processing of oily waste water
Method is paid much attention to.
The country mostly uses " old three sets " (oil removal-flocculation-air floating-biochemistry) process oily waste water, with production technology
The raising and national sewage comprehensive emission standard that development, effluent quality require are increasingly strict, and " old three sets " treatment process is badly in need of
It improves.Wherein, chemical flocculation and air bearing processing technique all need to add flocculant, and higher cost, pollution are larger, and these means institutes
It needs equipment volume big, takes up an area more, subsequent processing complexity, it is difficult to which by, small enterprise receives；Biologic treating technique, which can only be handled, to be contained
The substance of bio-degradable in oily waste water, thus the pollutant in waste water can only be limitedly removed, and oily waste water ingredient is multiple
Miscellaneous, treatment effeciency is simultaneously bad, and water outlet oil content is high；However the adaptation of electrolytic flocculation air flotation technology is wide, can handle oily waste water simultaneously
Multiple pollutant in water, and take up an area less, convenient and flexible operation, easily realize that automatic control, sludge quantity are few, post-processing is extremely simple
It is single, normally referred to as cleaning treatment technology, therefore it is practicable for replacing with it flocculation-air floating technique, and is had very much competing
Strive power.
Electrolytic flocculation is to make sacrificial electrode, passing through using soluble anode such as metallic aluminium or iron under external voltage effect
Reaction is learned, bubble required for dissolved air flotation had both been generated, also generating makes the flocculated flocculant of suspended matter.Utilize electrolytic flocculation method
Oily waste water is administered, there is a large amount of report both at home and abroad.But the water quality come out through electrolytic flocculation method is due to containing Fe2+And Fe3 +Deng most of water has color, generally brown or green, is unable to direct emission.
CN104291415A discloses a kind of method of Treatment of Oil/Water Emulsion by Electrolytic Flocculation, and this method is by using aluminium sheet
For anode plate, flocculated effect is realized by Aluminum, although this method can reach preferable COD removal effect,
Its aluminium sheet used still can have electrode corrosion as anode.
There can be apparent uneven dissolution phenomenon using soluble anode plate, the thinning speed of pole plate is inconsistent, electrolysis
After a period of time, it will lead to pole plate bulk and fall off.The corrosion of metal electrode can make to generate foreign ion in water, and there are anodes
The disadvantages of metal wastage is big, power consumption is high and operating cost is higher.
Summary of the invention
The purpose of the present invention is be to overcome the processing method of existing oily waste water need using soluble anode plate into
The defect of row electrolytic flocculation provides a kind of processing of oily waste water that electrolytic flocculation can also be carried out using non-solubility anode plate
Method.
To achieve the goals above, the present invention provides a kind of processing method of oily waste water, wherein this method comprises:
In the presence of pink salt, oily waste water is electrolysed, the oily waste water after the electrolysis is settled, wherein the electrolysis is adopted
Anode plate is investigation of titanium anode coated with metal oxide.
The processing method of the oily waste water provided through the invention, can using investigation of titanium anode coated with metal oxide this
In the case where kind non-solubility anode plate, so that it can be electrolysed in the case where not consumable anode, electrolysis wadding can be obtained
Solidifying, electrofloatation and free-radical oxidation triple role, to reach the treatment effect of preferable oily waste water, it is useless that treated
Water can be with direct emission or reuse.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The present invention provides a kind of processing method of oily waste water, wherein this method comprises: in the presence of pink salt, by oil-containing
Waste water is electrolysed, and the oily waste water after the electrolysis is settled, wherein the anode plate used that is electrolysed is titanium-based gold
Belong to oxide coating electrode.
According to the present invention, the oily waste water is not particularly limited, can be the oily waste water in various sources, such as stone
One of oily exploitation, petroleum refining, petrochemical industry, storage and shipping of oil products, vehicle cleaning, machine-building and food processing or a variety of productions
Raw oily waste water.And method of the invention can be used for the processing of the oily waste water of any oil content in above-mentioned various sources,
Such as it can be used for the oily waste water that oil content is 5-900mg/L and (be preferably applied to the oily waste water to the oil content of 10-50mg/L
The processing of water) processing.
In a preferred embodiment of the invention, method of the invention is suitable for being 10-100mg/ to oil content
L, COD value 100-600mg/L, BOD5Value is 30-200mg/L, and SS value is the processing of the oily waste water of 20-200mg/L.It is more excellent
Selection of land, the oil content of the oily waste water are 10-40mg/L, COD value 300-500mg/L, BOD5Value is 70-120mg/L, SS
Value is 70-120mg/L.
According to the present invention, in the presence of pink salt, the oily waste water is electrolysed, can be obtained under not consumable anode
The triple role of electrolytic flocculation, electrofloatation and free-radical oxidation is obtained, in order to preferably utilize this triple role degradation institute
State the greasy dirt in oily waste water, it is preferable that relative to the volume of the oily waste water, the dosage of the pink salt in terms of tin ion
For 0.005-0.1mg/L, preferably 0.01-0.05mg/L.Here dosage is referred to relative to oily waste water to be processed
Volume for, the concentration of pink salt bring tin ion.
Wherein, water-soluble pink salt that the pink salt can be common for this field, it is preferable that the pink salt is chlorination
One of tin, stannous chloride, STANNOUS SULPHATE CRYSTALLINE and nitric acid tin are a variety of.
According to the present invention, the anode plate that the electrolysis uses is the titanium-based metal oxide coating that will not be lost by electrolysis
Electrode.Wherein, the investigation of titanium anode coated with metal oxide refers to by coating on one or two surface of titanium mesh
The electrode plate that metal oxide is formed.It is normal that metal oxide used in the investigation of titanium anode coated with metal oxide can be this field
Rule for being coated with the metal oxides of the metal electrode boards such as titanium plate, under preferable case, which is SnO2、IrO2、
TiO2、PbO2And RuO2One of or it is a variety of.
In order to preferably reach the treatment effect to oily waste water, investigation of titanium anode coated with metal oxide in the present invention
The thickness of coating of metal oxides is preferably 5-20 μm, and the crystallite dimension of metal oxide is preferably 4-30nm, more preferably 5-
15nm。
In a preferred embodiment of the invention, the anode plate is Ti/SnO2Electrode plate, Ti/IrO2Electrode
Plate, Ti/PbO2Electrode plate or Ti/RuO2Electrode plate.
In addition, the cathode plate used that is electrolysed can be the electrode as cathode of this field routine, it is preferable that described
The cathode plate of electrolysis is titanium mesh, nickel metal plate, graphite plate or Ti-Ni alloy plate.
According to the present invention, in order to reaching handled the oily waste water above-mentioned three better by electrolysis
Recast is used, it is preferable that the condition of the electrolysis includes: that pole plate spacing is 1-3cm, current density 10-50mA/cm2(more preferably
For 20-40mA/cm2), reaction temperature is 25-40 DEG C, and electrolysis time is 2-20min (more preferably 5-10min), pH 5-9.
Wherein, in order to guarantee that oily waste water has certain conductive capability, conductivity needs>=1mS/cm, and work as conductivity<1mS/cm
When, sodium chloride or sodium sulphate can be added into the oily waste water.
According to the present invention, above-mentioned electrolysis can carry out in the reaction vessel of this field routine, as long as can reach above-mentioned
Electrolysis effectiveness, it is preferable that the electrolysis carries out in electrolysis reactor, and such electrolysis reactor can be cement material
The container of matter, the container of steel plate material, the container of plastic material, container of glass material etc., in addition, the reaction vessel selected
Volume can be arbitrary size, can be selected according to the amount of oily waste water to be processed, details are not described herein again.
According to the present invention, when the cathode plate and anode plate are located among reaction vessel, under preferable case, the cathode
Plate, anode plate are parallel with the two sides of the chamber wall of reaction vessel, and the cathode plate and anode plate have same or similar face
The size of product, the area can be selected according to the amount of oily waste water to be processed and the volume of reaction vessel used, such as this
The area of electrode plate is 380-420cm in the preferred embodiment of invention2。
According to the present invention, this method further includes settling the oily waste water after the electrolysis, and the sedimentation can be
It is carried out in the sedimentation basin of this field routine, the present invention is not particularly limited this.Preferably, the surface loading of the sedimentation basin is
0.2-1.3m3/(m2 .h)。
According to the present invention, the sedimentation can settle down the impurity such as suspended particulate in the oily waste water after electrolysis,
To obtain the opposite waste water purified, in order to enable oily waste water reaches better treatment effect in sedimentation link, it is preferable that
The residence time of the sedimentation is 1-6h.The residence time refers to that entering sedimentation basin from oily waste water leaves needed for sedimentation basin to it
Time.
According to the present invention, method provided by the invention either batch process oily waste water method, but for work
Industryization is using consideration, and method of the invention is preferably the method for continuous processing oily waste water, i.e., oily waste water is with certain flow
It is continually injected into the container at electrolysis place, the reservoir where container and sedimentation where being electrolysed, so that after being electrolysed
Oily waste water is also constantly passed into the container of sedimentation.Using continuation method, stop in electrolysis reactor
Staying the time is electrolysis time.
Wherein, it will be apparent to a skilled person that the pink salt can also using continuous method
Continuously to put into, and the pink salt that can be converted according to above-mentioned dosage adds flow.
The processing method of the oily waste water provided through the invention can use titanium-based metal oxide in the presence of pink salt
This non-solubility anode plate of coated electrode is electrolysed, and three recasts of electrolytic flocculation, electrofloatation and free-radical oxidation are obtained
With to reach the treatment effect of preferable oily waste water.
The present invention will be described in detail by way of examples below.
In following embodiment and comparative example, the processing method of used oily waste water is continuous processing method, that is, is contained
Oily waste water is continually added from the water inlet of electrolysis reactor and is electrolysed into reactor, and the waste water after electrolysis is constantly arranged again
Enter and settled into sedimentation basin, the waste water after sedimentation is constantly discharged from the water outlet of sedimentation basin.
In following embodiment and comparative example, daily into embodiment and comparative example electrolysis reactor oily waste water into
Water water quality is defaulted as likewise, being all influent quality shown in table 1.
The measurement of oil content is using the infrared spectrophotometry in GB/T12152-2007；
The measurement of COD (COD) uses the dichromate titration of GB11914-89；
Five-day BOD (BOD5) measurement use GB7488-87 measuring method；
The measurement of suspended matter (SS) uses the measuring method of GB/T11901-1989.
Embodiment 1
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
Oily waste water is sent in electrolysis reactor with the volume flow of 48L/h and is electrolysed, and with 1.42mg/h's
Adding speed addition Tin tetrachloride pentahydrate, (dosage of tin tetrachloride is 0.01mg/L), containing after electrolysis i.e. in terms of tin ion
Oily waste water is sent in sedimentation basin with the volume flow of 48L/h and is settled, in which:
Electrolysis reactor: anode Ti/SnO2Electrode, cathode are titanium plate, pole plate spacing 1cm；Current density is 20mA/
cm2, electrolysis time 5min, 25 DEG C of inflow temperature, pH 6；
Sedimentation basin: surface loading 0.8m3/(m2H), residence time 3.5h；
After the water outlet water quality in pond to be precipitated is basicly stable, continuous 30 days, daily respectively from the water inlet of electrolysis reactor
Respectively taken with the water outlet of sedimentation basin oil content in a water determination water sample, oil content removal rate, COD, COD removal rate,
BOD5、BOD5/ COD and SS, testing result is as shown in Tables 1 and 2.
Embodiment 2
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
Oily waste water is sent in electrolysis reactor with the volume flow of 24L/h and is electrolysed, and with the throwing of 1.3mg/h
STANNOUS SULPHATE CRYSTALLINE (dosage of STANNOUS SULPHATE CRYSTALLINE is 0.03mg/L i.e. in terms of tin ion) is added in acceleration, and the oily waste water after electrolysis is with 24L/
The volume flow of h, which is sent in sedimentation basin, to be settled, in which:
Electrolysis reactor: anode Ti/IrO2Electrode, cathode are graphite plate, pole plate spacing 2cm；Current density is 30mA/
cm2, electrolysis time 10min, 30 DEG C of inflow temperature, pH 5；
Sedimentation basin: surface loading 0.80m3/(m2H), residence time 3.5h；
After the water outlet water quality in pond to be precipitated is basicly stable, continuous 30 days, daily respectively from the water inlet of electrolysis reactor
Respectively taken with the water outlet of sedimentation basin oil content in a water determination water sample, oil content removal rate, COD, COD removal rate,
BOD5、BOD5/ COD and SS, testing result is as shown in Tables 1 and 2.
Embodiment 3
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
Oily waste water is sent in electrolysis reactor with the volume flow of 30L/h and is electrolysed, and with 3.07mg/h's
Add speed be added nitric acid tin (dosage of nitric acid tin is 0.05mg/L) i.e. in terms of tin ion, the oily waste water after electrolysis with
The volume flow of 30L/h, which is sent in sedimentation basin, to be settled, in which:
Electrolysis reactor: anode Ti/PbO2Electrode, cathode are nickel metal plate, pole plate spacing 3cm；Current density is
40mA/cm2, electrolysis time 8min, 40 DEG C of inflow temperature, pH 9；
Sedimentation basin: surface loading 1m3/(m2H), residence time 2.8h；
After the water outlet water quality in pond to be precipitated is basicly stable, continuous 30 days, daily respectively from the water inlet of electrolysis reactor
Respectively taken with the water outlet of sedimentation basin oil content in a water determination water sample, oil content removal rate, COD, COD removal rate,
BOD5、BOD5/ COD and SS, testing result is as shown in Tables 1 and 2.
Embodiment 4
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
Oily waste water is sent in electrolysis reactor with the volume flow of 40L/h and is electrolysed, and with 4.09mg/h's
Add speed be added nitric acid tin (dosage of nitric acid tin is 0.05mg/L) i.e. in terms of tin ion, the oily waste water after electrolysis with
The volume flow of 40L/h, which is sent in sedimentation basin, to be settled, in which:
Electrolysis reactor: anode Ti/RuO2Electrode, cathode are Ti-Ni alloy plate, pole plate spacing 1.5cm；Current density
For 25mA/cm2, electrolysis time 6min, 35 DEG C of inflow temperature, pH 7；
Sedimentation basin: surface loading 1.2m3/(m2H), residence time 2.3h；
After the water outlet water quality in pond to be precipitated is basicly stable, continuous 30 days, daily respectively from the water inlet of electrolysis reactor
Respectively taken with the water outlet of sedimentation basin oil content in a water determination water sample, oil content removal rate, COD, COD removal rate,
BOD5、BOD5/ COD and SS, testing result is as shown in Tables 1 and 2.
Embodiment 5
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
According to method described in embodiment 1, the difference is that the current density of electrolysis reactor is 10mA/cm2, to heavy
After the water outlet water quality in shallow lake pond is basicly stable, continuous 30 days, going out from the water inlet of electrolysis reactor and sedimentation basin respectively daily
The mouth of a river respectively takes oil content in a water determination water sample, oil content removal rate, COD, COD removal rate, BOD5、BOD5/ COD and
SS, testing result is as shown in Tables 1 and 2.
Embodiment 6
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
According to method described in embodiment 1, the difference is that the electrolysis time of electrolysis reactor is 2min, pond to be precipitated
Water outlet water quality it is basicly stable after, continuous 30 days, daily respectively from the water outlet of the water inlet of electrolysis reactor and sedimentation basin
Respectively take oil content in a water determination water sample, oil content removal rate, COD, COD removal rate, BOD5、BOD5/ COD and SS, inspection
Survey the results are shown in Table shown in 1 and table 2.
Embodiment 7
The present embodiment is used to illustrate the processing method of oily waste water of the invention.
According to method described in embodiment 1, the difference is that the dosage of stannic chloride is 0.005mg/L, pond to be precipitated
It is continuous 30 days, each from the water outlet of the water inlet of electrolysis reactor and sedimentation basin respectively daily after water outlet water quality is basicly stable
Take oil content in a water determination water sample, oil content removal rate, COD, COD removal rate, BOD5、BOD5/ COD and SS, detection
It the results are shown in Table shown in 1 and table 2.
Comparative example 1
According to method described in embodiment 1, the difference is that pink salt is not added in electrolytic process, the water outlet in pond to be precipitated
After saliva matter is basicly stable, continuous 30 days, one is respectively taken from the water outlet of the water inlet of electrolysis reactor and sedimentation basin respectively daily
Oil content, oil content removal rate, COD, COD removal rate, BOD in part water determination water sample5、BOD5/ COD and SS, testing result
As shown in Tables 1 and 2.
Comparative example 2
According to method described in embodiment 1, the difference is that anode plate, using graphite electrode, pond to be precipitated goes out
After mouth of a river water quality is basicly stable, continuous 30 days, respectively taken from the water outlet of the water inlet of electrolysis reactor and sedimentation basin respectively daily
Oil content, oil content removal rate in a water determination water sample, COD, COD removal rate, BOD5、BOD5/ COD and SS, detection knot
Fruit is as shown in Tables 1 and 2.
Comparative example 3
According to method described in embodiment 1, the difference is that anode plate is using metal iron electrode, pond to be precipitated
It is continuous 30 days, each from the water outlet of the water inlet of electrolysis reactor and sedimentation basin respectively daily after water outlet water quality is basicly stable
Take oil content in a water determination water sample, oil content removal rate, COD, COD removal rate, BOD5、BOD5/ COD and SS, detection
It the results are shown in Table shown in 1 and table 2, the water color of outlet is brown, and iron electrode has passivation and corrosion phenomenon.
Comparative example 4
According to method described in embodiment 1, the difference is that the iron chloride (in terms of iron ion) for adding 0.01mg/L replaces
Stannic chloride, after the water outlet water quality in pond to be precipitated is basicly stable, continuous 30 days, daily respectively from the water inlet of electrolysis reactor and
The water outlet of sedimentation basin respectively takes oil content in a water determination water sample, oil content removal rate, COD, COD removal rate, BOD5、
BOD5/ COD and SS, for testing result as shown in Tables 1 and 2, the water color of outlet is brown.
Comparative example 5
According to method described in embodiment 1, the difference is that the aluminium chloride (in terms of aluminium ion) for adding 0.01mg/L replaces
Stannic chloride, after the water outlet water quality in pond to be precipitated is basicly stable, continuous 30 days, daily respectively from the water inlet of electrolysis reactor and
The water outlet of sedimentation basin respectively takes oil content in a water determination water sample, oil content removal rate, COD, COD removal rate, BOD5、
BOD5/ COD and SS, testing result is as shown in Tables 1 and 2.
The fluctuation range of the testing result of water sample in table 1:30 days
| Oil content/mg/L | COD/mg/L | BOD5/mg/L | SS/mg/L | |
| Water inlet 1 | 11.9-32.5 | 320.6-431.4 | 72.6-97.8 | 76.1-102.2 |
| Embodiment 1 | 0.5-0.9 | 34.6-50.7 | 13.8-21.9 | 1.6-7.7 |
| Embodiment 2 | 0.4-0.8 | 33.7-50.1 | 13.6-21.8 | 1.4-6.9 |
| Embodiment 3 | 0.4-0.7 | 33.2-48.9 | 13.5-21.2 | 1.4-6.5 |
| Embodiment 4 | 0.5-0.8 | 34.1-49.3 | 13.6-21.6 | 1.5-7.1 |
| Embodiment 5 | 1.2-1.8 | 47.3-63.2 | 16.9-28.6 | 5.2-9.9 |
| Embodiment 6 | 1.5-1.9 | 49.6-67.5 | 18.8-29.3 | 5.3-10.4 |
| Embodiment 7 | 1.8-2.2 | 51.2-69.4 | 19.4-30.1 | 5.6-11.0 |
| Comparative example 1 | 8.3-26.6 | 201.7-306.4 | 59.7-76.1 | 27.7-52.8 |
| Comparative example 2 | 5.5-10.9 | 102.1-176.2 | 37.3-53.1 | 18.5-33.8 |
| Comparative example 3 | 5.2-10 | 98.5-165.3 | 36.9-50.7 | 10.2-21.6 |
| Comparative example 4 | 7.6-21.2 | 188.7-286.9 | 55.2-73 | 20.8-43.2 |
| Comparative example 5 | 7.8-22.6 | 190.2-292 | 55.7-74.1 | 21.1-45 |
The testing result average value of water sample in table 2:30 days
Note: oil content removal rate refer to embodiment and comparative example water inlet oil content and water outlet oil content difference with into
The percentage of water oil content；COD removal rate refers to the influent COD and water outlet COD difference and influent COD of embodiment and comparative example
Percentage.
It can be seen that from the data in Tables 1 and 2 by processing method of the invention treated oily waste water, it can
Higher oil content removal rate is obtained, reaches 91% or more, it might even be possible to reach 97% or so；And it can obtain higher
COD removal rate can reach 84% or more, it might even be possible to reach 88% or more；BOD5The numerical value of/COD can be improved by 0.23
To 0.41 or more, bio-degradable is significantly increased, and SS is also declined, and therefore, handles by method of the invention useless
Water can be with direct emission or reuse.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should also be regarded as the disclosure of the present invention.
Claims (9)
1. a kind of processing method of oily waste water, which is characterized in that this method comprises: in the presence of pink salt, by oily waste water into
Row electrolysis, the oily waste water after the electrolysis is settled, wherein the anode plate used that is electrolysed is titanium-based metal oxidation
Object coated electrode；The pink salt is one of stannic chloride, stannous chloride, STANNOUS SULPHATE CRYSTALLINE and nitric acid tin or a variety of.
2. according to the method described in claim 1, wherein, relative to the volume of the oily waste water, the tin in terms of tin ion
The dosage of salt is 0.005-0.1mg/L.
3. according to the method described in claim 2, wherein, relative to the volume of the oily waste water, the tin in terms of tin ion
The dosage of salt is 0.01-0.05mg/L.
4. method described in any one of -3 according to claim 1, wherein in the investigation of titanium anode coated with metal oxide
Metal oxide is SnO2、IrO2、TiO2、PbO2And RuO2One of or it is a variety of.
5. according to the method described in claim 4, wherein, the anode plate is Ti/SnO2Electrode plate, Ti/IrO2Electrode plate, Ti/
PbO2Electrode plate or Ti/RuO2Electrode plate.
6. method described in any one of -3 and 5 according to claim 1, wherein the cathode plate of the electrolysis be titanium mesh,
Nickel metal plate, graphite plate or Ti-Ni alloy plate.
7. according to the method described in claim 6, wherein, the condition of the electrolysis includes: that pole plate spacing is 1-3cm, and electric current is close
Degree is 10-50mA/cm2, reaction temperature is 25-40 DEG C, electrolysis time 2-20min, pH 5-9.
8. according to the method described in claim 7, wherein, the condition of the electrolysis includes: that pole plate spacing is 1-3cm, and electric current is close
Degree is 20-40mA/cm2, reaction temperature is 25-40 DEG C, electrolysis time 5-10min, pH 5-9.
9. method described in any one of -3,5 and 7-8 according to claim 1, wherein the oil content of the oily waste water is
10-100mg/L, COD value 100-600mg/L, BOD5Value is 30-200mg/L, and SS value is 20-200mg/L.
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| CN103288254A (en) * | 2012-02-29 | 2013-09-11 | 张太亮 | Process and device for electric cracking catalytic oxidation for petroleum drilling wastewater |
| CN104628216A (en) * | 2013-11-12 | 2015-05-20 | 中国石油化工股份有限公司 | Treatment method for oily wastewater |
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| CN103288254A (en) * | 2012-02-29 | 2013-09-11 | 张太亮 | Process and device for electric cracking catalytic oxidation for petroleum drilling wastewater |
| CN104628216A (en) * | 2013-11-12 | 2015-05-20 | 中国石油化工股份有限公司 | Treatment method for oily wastewater |
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