CN115403116B - Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method - Google Patents

Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method Download PDF

Info

Publication number
CN115403116B
CN115403116B CN202211217089.8A CN202211217089A CN115403116B CN 115403116 B CN115403116 B CN 115403116B CN 202211217089 A CN202211217089 A CN 202211217089A CN 115403116 B CN115403116 B CN 115403116B
Authority
CN
China
Prior art keywords
wastewater
electrode
plate
thick oil
electrode reaction
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202211217089.8A
Other languages
Chinese (zh)
Other versions
CN115403116A (en
Inventor
户传龙
张文艺
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Changzhou University
Original Assignee
Changzhou University
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Changzhou University filed Critical Changzhou University
Priority to CN202211217089.8A priority Critical patent/CN115403116B/en
Publication of CN115403116A publication Critical patent/CN115403116A/en
Application granted granted Critical
Publication of CN115403116B publication Critical patent/CN115403116B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F1/46114—Electrodes in particulate form or with conductive and/or non conductive particles between them
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
    • C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/32—Hydrocarbons, e.g. oil
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4616—Power supply
    • C02F2201/4617—DC only
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4619—Supplying gas to the electrolyte
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]

Abstract

The invention discloses a method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by a three-dimensional electrode electro-Fenton oxidation method, which comprises the steps of adding the thick oil demulsification wastewater into a three-dimensional electrode reaction system, and reducing the content of the petroleum hydrocarbon; the three-dimensional electrode reaction system comprises a particle electrode, wherein the particle electrode is a compound formed by nano iron and foam nickel according to the mass ratio of 1-4:1. According to the invention, the filling particles are made of composite materials containing nano iron and foam nickel, and the degradation effect is improved through the composite synergistic effect of the nano iron and the foam nickel, and meanwhile, the ratio of the nano iron to the foam nickel is optimized, so that the better degradation effect is realized.

Description

Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method
Technical Field
The invention belongs to the field of industrial wastewater treatment, and particularly relates to a method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by a three-dimensional electrode electro-Fenton oxidation method.
Background
Currently, crude oil fields which are easy to exploit are gradually reduced, and thickened oil fields are attracting more attention due to the abundant reserves thereof. The thick oil contains a large amount of colloid, asphaltene and natural emulsifying agent, so the thick oil has high viscosity and high density and is easy to form emulsion. In the process of exploitation, complex components such as CO are injected 2 、N 2 As well as various chemical additives, lead to more complex liquid components being produced, which presents a significant challenge in breaking thick oil.
At present, the petroleum hydrocarbon content in the effluent after demulsification and oil-water separation of the thick oil by various methods still exceeds the standard, and the national emission standard is not met. The oily wastewater formed after demulsification and separation of the thickened oil mainly contains surfactant, oil substances and other organic matters, and petroleum hydrocarbon in the wastewater is in a mutual-soluble state in water and has certain toxicity, and the advanced treatment method is required to reach the national emission standard.
The current treatment methods for thick oil demulsification wastewater are mainly classified into biological, physical and chemical methods. Although the traditional biological method is widely researched due to low cost and no harm, the traditional biological method has strict requirements on the living environment of microorganisms and limited wastewater treatment effect with low biodegradability, and the thick oil in China is mostly exploited in a Bohai sea ocean drilling platform and is difficult to treat by adopting the biological method with large occupied area. In this case, physical and chemical methods are critical in treating oily wastewater.
In recent years, various water treatment technologies such as Fenton oxidation, three-dimensional electrode electrocatalytic oxidation, ozone oxidation, plasma oxidation and ultrasonic degradation technologies have been rapidly developed. However, such techniques have drawbacks of inconvenient operation, high cost, and poor treatment effect.
Disclosure of Invention
This section is intended to outline some aspects of embodiments of the invention and to briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section as well as in the description summary and in the title of the application, to avoid obscuring the purpose of this section, the description summary and the title of the invention, which should not be used to limit the scope of the invention.
The present invention has been made in view of the above and/or problems occurring in the prior art.
Therefore, the invention aims to overcome the defects in the prior art and provide a method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using a three-dimensional electrode electro-Fenton oxidation method.
In order to solve the technical problems, the invention provides the following technical scheme: a method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by a three-dimensional electrode electro-Fenton oxidation method comprises the following steps of,
adding the thick oil demulsification wastewater into a three-dimensional electrode reaction system, and reducing the content of petroleum hydrocarbon; wherein,
the three-dimensional electrode reaction system comprises a particle electrode which is a compound formed by nano iron and foam nickel according to the mass ratio of 1-4:1.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the three-dimensional electrode reaction system comprises,
the electrode reaction system comprises an electrode reaction container 100, an anode plate 101, a cathode plate 102, a particle electrode 103, a direct current power supply 104 and an electric stirrer 105, wherein the anode plate 101 is connected with the positive electrode of the direct current power supply 104 through a wire, the cathode plate 102 is connected with the negative electrode of the direct current power supply 104 through a wire, the anode plate 101 and the cathode plate 102 are oppositely arranged in the electrode reaction container 100, the particle electrode 103 is arranged between the anode plate 101 and the cathode plate 102, and the bottom of the electric stirrer 105 is arranged between the anode plate 101 and the cathode plate 102;
the feeding system comprises a waste liquid barrel 200 and a water inlet 201, wherein the water inlet 201 is arranged on the side wall of the electrode reaction container 100, and the waste liquid barrel 200 is connected with the water inlet 201 through a communication conduit;
the discharging system comprises a water outlet 300 and a clean water tank 301, wherein the water outlet 300 is arranged on the side wall of the electrode reaction container 100, and the water outlet 300 is connected with the clean water tank 301 through a communication conduit;
the aeration system comprises an aeration pump 400, a rotameter 401 and an air disc 402, wherein the air disc 402 is arranged at the bottom of the electrode reaction container 100, the air disc 402 is connected with the rotameter 401 through a communication conduit, the rotameter 401 is connected with the aeration pump 400 through the communication conduit, and the rotameter 401 is arranged between the aeration pump 400 and the air disc 402;
the pH online detection and adjustment system comprises a pH meter 500, a control panel 501 and an acid-base tank 502, wherein the acid-base tank 502 is connected with the electrode reaction container 100 through a conduit, and the pH meter 500 is arranged in the electrode reaction container 100.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the anode plate is one of a porous graphite plate, a stainless steel plate and a titanium plate; the cathode plate is one of foam nickel, a stainless steel plate, a graphite plate and an activated carbon fiber felt.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the electrode reaction container is made of organic glass, the specification is 20cm multiplied by 10cm multiplied by 15cm, and the specification of the anode and the cathode plates is 15cm multiplied by 6cm multiplied by 0.5cm.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the input amount of the particle electrode is 100-400 g/L.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the input amount of the particle electrode is 200g/L.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the mass ratio of the nano iron to the foam nickel in the particle electrode is 2:1.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the pH on-line detection and adjustment system is characterized in that when the pH indicating number is more than 4, acid is automatically added to adjust the pH within the range of 2-4.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: the distance between the anode plate and the cathode plate is 4-10 cm, the voltage of the stabilized DC power supply is 10-30V, and the aeration intensity of the aerator is 0.5-1.5L/min.
As a preferable scheme of the method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using the three-dimensional electrode electro-Fenton oxidation method, the invention comprises the following steps: na with the concentration of 5g/L is also added into the three-dimensional electrode reaction system 2 SO 4 An electrolyte.
The invention has the beneficial effects that:
the invention provides a method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using a three-dimensional electrode electro-Fenton oxidation method, which combines a three-dimensional electrode with Fenton oxidation, adopts a composite material containing nano iron and foam nickel as filling particles, and does not need to add Fe in the reaction 2+ H and H 2 O 2 The current efficiency and the removal rate are improved, the running cost is saved, and the technology has excellent degradation effect in the aspect of oil-containing wastewater treatment;
according to the invention, the filling particles are composite materials containing nano iron and foam nickel, and the degradation effect is improved through the composite synergistic effect of the nano iron and the foam nickel, and meanwhile, the ratio of the nano iron to the foam nickel is optimized, so that the better degradation effect is realized;
the method has the advantages of convenient operation, lower cost, better treatment effect, no secondary pollution and realization of economical and efficient treatment of the oily wastewater.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the description of the embodiments will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art. Wherein:
FIG. 1 is a schematic diagram of a three-dimensional electrode reaction system in an embodiment of the invention.
Detailed Description
In order that the above-recited objects, features and advantages of the present invention will become more apparent, a more particular description of the invention will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, but the present invention may be practiced in other ways other than those described herein, and persons skilled in the art will readily appreciate that the present invention is not limited to the specific embodiments disclosed below.
Further, reference herein to "one embodiment" or "an embodiment" means that a particular feature, structure, or characteristic can be included in at least one implementation of the invention. The appearances of the phrase "in one embodiment" in various places in the specification are not necessarily all referring to the same embodiment, nor are separate or alternative embodiments mutually exclusive of other embodiments.
The grain size of the nano iron is 300nm; foam nickel parameters in the present invention: pore size 0.2mm (100 ppi), porosity 98%, areal density 350g/m 2 The method comprises the steps of carrying out a first treatment on the surface of the Other principles are all common commercial products.
The reaction principle of the invention:
the particle electrode in the invention adopts iron goldThe method is characterized in that after the mixture of other particles is put into operation and the power is turned on, the filling particle electrodes are electrified, and each particle electrode forms a micro-electrolytic cell. When the iron metal is mixed with other particles to be used as a particle electrode of the three-dimensional electrode, active sites of the electrode are provided for electro-Fenton oxidation of the three-dimensional electrode, and Fe with a catalytic effect is generated 2+ 。H 2 O 2 The method is characterized in that the aliphatic hydrocarbon is firstly oxidized and decomposed into alcohol, the alcohol is gradually oxidized into aldehyde and acid through multistage chain reaction, and finally the aldehyde and acid are completely oxidized into carbon dioxide and water through repeated circulation to finish the degradation of petroleum hydrocarbon. The main reaction equation is as follows.
Fe 2+ +H 2 O 2 →Fe 3+ +OH - +·OH
RCH 2 CH 3 +·OH→RCH 2 CH 2 OH+……→RCH 2 CHO+……→RCH 2 COOH+……→RCH 3 +……→RCH 2 OH+……→RCHO+……→RCOOH+……→CO 2 +H 2 O
Example 1
This embodiment provides a system for decomposing petroleum hydrocarbons in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation, which, referring to FIG. 1, comprises,
the electrode reaction system comprises an electrode reaction container 100, an anode plate 101, a cathode plate 102, a particle electrode 103, a direct current power supply 104 and an electric stirrer 105, wherein the anode plate 101 is connected with the positive electrode of the direct current power supply 104 through a wire, the cathode plate 102 is connected with the negative electrode of the direct current power supply 104 through a wire, the anode plate 101 and the cathode plate 102 are oppositely arranged in the electrode reaction container 100, the particle electrode 103 is arranged between the anode plate 101 and the cathode plate 102, and the bottom of the electric stirrer 105 is arranged between the anode plate 101 and the cathode plate 102;
the feeding system comprises a waste liquid barrel 200 and a water inlet 201, wherein the water inlet 201 is arranged on the side wall of the electrode reaction container 100, and the waste liquid barrel 200 is connected with the water inlet 201 through a communication conduit;
the discharging system comprises a water outlet 300 and a clean water tank 301, wherein the water outlet 300 is arranged on the side wall of the electrode reaction container 100, and the water outlet 300 is connected with the clean water tank 301 through a communication conduit;
the aeration system comprises an aeration pump 400, a rotameter 401 and an air disc 402, wherein the air disc 402 is arranged at the bottom of the electrode reaction container 100, the air disc 402 is connected with the rotameter 401 through a communication conduit, the rotameter 401 is connected with the aeration pump 400 through the communication conduit, and the rotameter 401 is arranged between the aeration pump 400 and the air disc 402;
the pH online detection and adjustment system comprises a pH meter 500, a control panel 501 and an acid-base tank 502, wherein the acid-base tank 502 is connected with the electrode reaction container 100 through a conduit, and the pH meter 500 is arranged in the electrode reaction container 100.
Specifically, thick oil demulsification wastewater enters the electrode reaction container 100 through the water inlet 201, the positive electrode of the direct current power supply 104 is connected with the anode plate in the electrode reaction container 100, the negative electrode of the direct current power supply 104 is connected with the cathode plate in the electrode reaction container 100, a certain distance is reserved between the anode plate and the cathode plate, and the voltage of the direct current stabilized power supply is controlled to be unchanged;
placing the filling particle electrode between the cathode and anode plates to form a three-dimensional electrode reaction system, placing a stirring rod and stirring blades of an electric stirrer 105 into an electrode reaction container 100, and keeping the rotating speed at 150r/min; the pH meter 500 is placed in the reactor liquid for detecting and regulating the pH value of the solution during the reaction, the gas disk 402 communicated by the connecting hose is placed near the cathode plate, the aeration pump 400 is started, a certain flow rate is controlled by the rotameter 401, and a proper amount of Na is added during the reaction 2 SO 4 Enhancing the conductivity of the solution.
Further, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reactor through the water inlet.
The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled at 6cm, and the voltage of a stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter.
In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 40.00mg/L, the total oil content is 6.23mg/L, the COD removal rate reaches 91.89%, and the total oil removal rate is 91.28%.
Example 2
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the distance between the anode plate and the cathode plate is controlled to be 4cm, and the voltage of a stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1.
And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter.
In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 53.91mg/L, the total oil content is 6.95mg/L, the COD removal rate is 89.07%, and the total oil removal rate is 90.27%.
Example 3
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled at 8cm, and the voltage of a stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1.
And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter. In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 58.60mg/L, the total oil content is 7.77mg/L, the COD removal rate is 88.12%, and the total oil removal rate is 89.13%.
Example 4
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled at 6cm, and the voltage of a stabilized DC power supply is set to be 15V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter.
In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 61.75mg/L, the total oil content is 8.64mg/L, the COD removal rate is 87.48%, and the total oil removal rate is 87.91%.
Example 5
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled at 6cm, and the voltage of a stabilized DC power supply is set to 25V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter. In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction.
Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 42.12mg/L, the total oil content is 6.41mg/L, the COD removal rate reaches 91.46%, and the total oil removal rate is 91.03%.
Example 6
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled at 6cm, and the voltage of a stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 0.8L/min through a rotameter. In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 65.75mg/L, the total oil content is 10.02mg/L, the COD removal rate is 86.67%, and the total oil removal rate is 85.98%.
Example 7
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a porous graphite plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the distance between the anode plate and the cathode plate is controlled to be 4cm, and the voltage of a stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.4L/min through a rotameter. In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction.
Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity. After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 48.78mg/L, the total oil content is 6.89mg/L, the COD removal rate reaches 90.11%, and the total oil removal rate is 90.36%.
Example 8
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of a stainless steel plate anode and a stainless steel cathode plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled to be 4cm, and the voltage of a stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter. In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 50.11mg/L, the total oil content is 7.21mg/L, the COD removal rate reaches 89.84%, and the total oil removal rate is 89.91%.
Example 9
Referring to the system of example 1, the oily wastewater formed after demulsification of the thickened oil is used as a treatment object, and the wastewater comprises the following components: oil content 71.44mg/L, ph=7.09, cod= 493.23mg/L.
And (3) introducing the thick oil demulsification wastewater in the waste liquid barrel into the three-dimensional electrode reaction system through the water inlet. The three-dimensional electrode reactor is made of organic glass with the specification of 20cm multiplied by 10cm multiplied by 15cm, the specifications of the anode plate and the cathode plate of the porous graphite plate are 15cm multiplied by 6cm multiplied by 0.5cm, the spacing between the anode plate and the cathode plate is controlled at 4cm, and the voltage of the stabilized DC power supply is set to be 20V.
The filling particle electrode used in the reactor is mixed particles of nano iron and foam nickel, and 200g/L is added between the cathode and anode plates according to a mass ratio of 2:1. And placing an air disc communicated with the connecting hose near the cathode plate, and controlling the aeration intensity to be 1.1L/min through a rotameter. In order to promote Fenton reaction to be better carried out, the pH value of the solution is regulated to be in the range of 2-4 by the pH on-line detection and regulation device before the reaction. Starting an electric stirring device in the reaction process, and adding Na with the concentration of 5g/L 2 SO 4 The electrolyte increases the conductivity.
After the reaction treatment, the COD of the wastewater oil-containing wastewater is reduced to 56.52mg/L, the total oil content is 7.66mg/L, the COD removal rate is 88.54%, and the total oil removal rate is 89.28%.
Comparative example 1
The mass ratio of nano iron to foam nickel was controlled under the conditions of example 1, and the other conditions were the same as those of example 1, and the conditions and results are shown in table 1.
TABLE 1
Test 1 Test 2 Test 3 Test 4 Test 5 Test 6
Nanometer iron (g) 67 100 133 150 160 200
Foam nickel (g) 133 100 67 50 40 0
COD removal Rate (%) 81.01 84.38 91.89 90.97 88.43 79.04
Total oil removal (%) 80.24 85.19 91.28 90.35 87.96 79.21
As can be seen from table 1, there is a synergistic effect between the nano iron and the foam nickel, and the degradation efficiency is improved; meanwhile, the ratio of nano iron to foam nickel is preferably 2:1, and the synergistic degradation effect is better.
It should be noted that the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solution of the present invention may be modified or substituted without departing from the spirit and scope of the technical solution of the present invention, which is intended to be covered in the scope of the claims of the present invention.

Claims (6)

1. A method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using a three-dimensional electrode electro-Fenton oxidation method is characterized by comprising the following steps of: comprising the steps of (a) a step of,
adding the thick oil demulsification wastewater into a three-dimensional electrode reaction system, and reducing the content of petroleum hydrocarbon; wherein,
the three-dimensional electrode reaction system comprises particle electrodes, wherein the particle electrodes are a compound formed by nano iron and foam nickel according to the mass ratio of 2:1, and the input amount of the particle electrodes is 200g/L;
wherein, the grain size of the nano iron is 300nm; the pore diameter of the foam nickel is 0.2mm, the porosity is 98%, and the areal density is 350g/m 2 ；
The three-dimensional electrode reaction system comprises,
the electrode reaction system comprises an electrode reaction container (100), an anode plate (101), a cathode plate (102), a particle electrode (103), a direct current power supply (104) and an electric stirrer (105), wherein the anode plate (101) is connected with the positive electrode of the direct current power supply (104) through a lead, the cathode plate (102) is connected with the negative electrode of the direct current power supply (104) through a lead, the anode plate (101) and the cathode plate (102) are oppositely arranged in the electrode reaction container (100), the particle electrode (103) is arranged between the anode plate (101) and the cathode plate (102), and the bottom of the electric stirrer (105) is arranged between the anode plate (101) and the cathode plate (102);
the feeding system comprises a waste liquid barrel (200) and a water inlet (201), wherein the water inlet (201) is arranged on the side wall of the electrode reaction container (100), and the waste liquid barrel (200) is connected with the water inlet (201) through a communication conduit;
the discharging system comprises a water outlet (300) and a clean water tank (301), wherein the water outlet (300) is arranged on the side wall of the electrode reaction container (100), and the water outlet (300) is connected with the clean water tank (301) through a communication conduit;
the aeration system comprises an aeration pump (400), a rotameter (401) and an air disc (402), wherein the air disc (402) is arranged at the bottom of the electrode reaction container (100), the air disc (402) is connected with the rotameter (401) through a communication conduit, the rotameter (401) is connected with the aeration pump (400) through a communication conduit, and the rotameter (401) is arranged between the aeration pump (400) and the air disc (402);
the pH on-line detection and adjustment system comprises a pH meter (500), a control panel (501) and an acid-base tank (502), wherein the acid-base tank (502) is connected with an electrode reaction container (100) through a conduit, and the pH meter (500) is arranged in the electrode reaction container (100).
2. The method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using three-dimensional electrode electro-Fenton oxidation method as claimed in claim 1, which is characterized in that: the anode plate is one of a porous graphite plate, a stainless steel plate and a titanium plate; the cathode plate is one of foam nickel, a stainless steel plate, a graphite plate and an activated carbon fiber felt.
3. The method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using three-dimensional electrode electro-Fenton oxidation method as claimed in claim 2, which is characterized in that: the electrode reaction container is made of organic glass, the specification is 20cm multiplied by 10cm multiplied by 15cm, and the specification of the anode and the cathode plates is 15cm multiplied by 6cm multiplied by 0.5cm.
4. The method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using three-dimensional electrode electro-Fenton oxidation method as claimed in claim 1, which is characterized in that: the pH on-line detection and adjustment system is characterized in that when the pH indicating number is more than 4, acid is automatically added to adjust the pH within the range of 2-4.
5. The method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using three-dimensional electrode electro-Fenton oxidation method as claimed in claim 4, which is characterized in that: the distance between the anode plate and the cathode plate is 4-10 cm, the voltage of the stabilized DC power supply is 10-30V, and the aeration intensity of the aerator is 0.5-1.5L/min.
6. The method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by using three-dimensional electrode electro-Fenton oxidation method as claimed in claim 4, which is characterized in that: na with the concentration of 5g/L is also added into the three-dimensional electrode reaction system 2 SO 4 An electrolyte.
CN202211217089.8A 2022-09-30 2022-09-30 Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method Active CN115403116B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202211217089.8A CN115403116B (en) 2022-09-30 2022-09-30 Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202211217089.8A CN115403116B (en) 2022-09-30 2022-09-30 Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method

Publications (2)

Publication Number Publication Date
CN115403116A CN115403116A (en) 2022-11-29
CN115403116B true CN115403116B (en) 2024-01-05

Family

ID=84168130

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202211217089.8A Active CN115403116B (en) 2022-09-30 2022-09-30 Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method

Country Status (1)

Country Link
CN (1) CN115403116B (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116143252A (en) * 2023-03-23 2023-05-23 昆明理工大学 Device for treating coffee preliminary processing wastewater by three-dimensional electrode-electro-Fenton coupling

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104961199A (en) * 2015-06-23 2015-10-07 广西大学 Preparation method of Pd-Fe/foamed nickel three-dimensional particle electrodes
CN113716655A (en) * 2021-09-10 2021-11-30 吉林建筑大学 Ferronickel bimetal three-dimensional electrode particle filler and preparation method and application thereof

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104961199A (en) * 2015-06-23 2015-10-07 广西大学 Preparation method of Pd-Fe/foamed nickel three-dimensional particle electrodes
CN113716655A (en) * 2021-09-10 2021-11-30 吉林建筑大学 Ferronickel bimetal three-dimensional electrode particle filler and preparation method and application thereof

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
三维电极—电芬顿耦合法处理石油采出水的试验研究;刘济嘉;《中国优秀硕士学位论文数据库 工程科技I辑》(第第09期期);第15-16、29-30页 *

Also Published As

Publication number Publication date
CN115403116A (en) 2022-11-29

Similar Documents

Publication Publication Date Title
JP5752608B2 (en) Method and apparatus for cleaning waste liquid
CN105439258A (en) Wastewater treatment method through generating H2O2 with in situ electricity to cooperate with O3 to oxidize
CN106044960B (en) A method of liquid being concentrated using three-diemsnional electrode processing landfill leachate
CN208561948U (en) A kind of organic wastewater catalytic ozonation processing system
CN115403116B (en) Method for decomposing petroleum hydrocarbon in thick oil demulsification wastewater by three-dimensional electrode electro-Fenton oxidation method
CN105198131A (en) Method for treating waste water through double catalytic oxidation process and device for achieving method
CN205347057U (en) Oil field tertiary oil recovery effluent disposal system
CN206188547U (en) Four -phase catalytic oxidation device
CN106745675B (en) A kind of Bioelectrochemical device and working method handling antibiotic waste water
CN205528153U (en) Electrochemistry sewage treatment device
CN104944697B (en) Microbial electrolysis cell-Fenton combined treatment device and process for treating furniture production wastewater
CN107640850A (en) Product oil storage field oil-contaminated water processing method
CN106082559A (en) A kind of integrated waste-water treater of efficient energy-saving
CN2646130Y (en) Tank shaped multiphase and polynary catalysis, electrolysis and oxidation sewage treatment device
CN207361952U (en) A kind of iron carbon catalyst oxidation reactor
CN107522361A (en) A kind of advanced treatment system for removing waste water mineral oil in fluid
CN108423928A (en) A kind of processing system of purified industrial waste water
CN101591129A (en) The advanced treatment method for sewage water of adopting combined use of hydroxyl radical active oxygen-bioactive carbon
CN204079675U (en) The device of circular treatment oily(waste)water
CN2646129Y (en) Multiphase and polynary catalysis, electrolysis and oxidation sewage treatment device adopting concentric circles electrodes
CN105366836A (en) Process and device for circulating multi-dimensional catalyzing advanced oxidation treatment of oily wastewater
CN205472817U (en) COD equipment falls in electricity catalytic oxidation
CN203754535U (en) Efficient micro-electrolysis multiphase flow air flotation reactor
CN107311360A (en) The method that catalytic ozonation coupling three-diemsnional electrode handles product oil storage field oil-polluted water
CN115432782A (en) Method and system for treating emulsion wastewater by three-dimensional electrode electro-Fenton oxidation method

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant