CN114477527A

CN114477527A - Workshop cleaning wastewater treatment method and system

Info

Publication number: CN114477527A
Application number: CN202210040810.4A
Authority: CN
Inventors: 叶伟炳; 王明富; 李琴
Original assignee: Guangdong Wenyang Environmental Technology Co ltd
Current assignee: Guangdong Wenyang Environmental Technology Co ltd
Priority date: 2022-01-14
Filing date: 2022-01-14
Publication date: 2022-05-13

Abstract

The invention relates to a workshop cleaning wastewater treatment method and a system. The method comprises the following steps: demulsifying the wastewater stock solution to obtain an oil-water mixture, and separating the oil-water mixture to obtain a first mixed solution; oxidizing the first mixed solution, layering the first mixed solution, and separating a turbid solution from the second mixed solution; and desalting the second mixed solution to obtain concentrated water and purified water. When the method is used for treating the wastewater stock solution, the wastewater stock solution is changed from an emulsified state to an oil-water mixed state through demulsification treatment, and oxidation treatment is carried out after separation so as to remove most organic matters in the first mixed solution. And finally, separating impurities from the purified water in the second mixed solution through desalting treatment. When the method is used for treating the workshop cleaning wastewater, the effluent quality of the purified water is higher.

Description

Workshop cleaning wastewater treatment method and system

Technical Field

The invention relates to the technical field of wastewater treatment, in particular to a workshop cleaning wastewater treatment method and a workshop cleaning wastewater treatment system.

Background

The types of the waste water generated in the life and production processes are various, and different types of waste water need to be treated in different modes, so that the waste water is better treated, and the pollution of the directly discharged waste water to the environment is reduced.

The workshop cleaning wastewater includes emulsion, degreasing wastewater, degreasing cleaning wastewater, cutting fluid cleaning wastewater, and the like, and the concentration of organic matters in the workshop cleaning wastewater is high. If the workshop cleaning wastewater is directly discharged, serious environmental pollution can be caused.

In the traditional technology, the quality of effluent is poor in the treatment process of workshop cleaning wastewater.

Disclosure of Invention

Therefore, it is necessary to provide a method and a system for treating workshop cleaning wastewater, aiming at the problem that the quality of effluent water in the treatment process of workshop cleaning wastewater is poor.

A workshop cleaning wastewater treatment method comprises the following steps:

demulsifying the wastewater stock solution to obtain an oil-water mixture, and separating the oil-water mixture to obtain a first mixed solution;

oxidizing the first mixed solution, layering the first mixed solution, and separating a turbid solution from the second mixed solution;

and desalting the second mixed solution to obtain concentrated water and purified water.

In one embodiment, the process of obtaining the second mixed solution from the first mixed solution specifically includes the following steps:

adjusting the pH value of the first mixed solution to 3-4;

sequentially adding ferrous sulfate and hydrogen peroxide into the acidic first mixed solution to perform oxidation reaction on the first mixed solution;

adjusting the first mixed solution after the oxidation reaction to be alkaline;

adding a flocculating agent into the first mixed solution adjusted to be alkaline for flocculation, so that the first mixed solution is layered;

and separating turbid liquid in the first mixed liquid to obtain a second mixed liquid.

In one embodiment, in the process of obtaining the first mixed liquid from the wastewater stock solution, the wastewater stock solution is adjusted to be alkaline, then the demulsifier is added into the wastewater stock solution to perform demulsification treatment, so that the wastewater is changed from an emulsified state to an oil-water layered state, then the flocculant is added to layer the wastewater stock solution, and after separating a lower layer of turbid liquid, the first mixed liquid is obtained.

In one embodiment, the step of desalting the second mixed solution to obtain concentrated water and purified water includes the following steps:

carrying out micro-flocculation filtration on the second mixed solution to obtain a first filtrate;

subjecting the first filtrate to ultrafiltration to obtain a second filtrate;

and performing reverse osmosis treatment on the second filtrate to obtain concentrated water and purified water.

A plant cleaning wastewater treatment system comprising:

the demulsification reaction device comprises a wastewater stock solution inlet end and a first mixed solution outlet end; the demulsification reaction device is used for performing demulsification treatment on the wastewater stock solution and separating to obtain a first mixed solution;

the oxidation treatment device comprises a first mixed liquid inlet end, a second mixed liquid outlet end and a sludge outlet end, wherein the first mixed liquid inlet end is communicated with the first mixed liquid outlet end; the oxidation treatment device is used for carrying out oxidation treatment on the first mixed liquor and separating sludge to obtain a second mixed liquor;

the desalting system comprises a second mixed liquid inlet end, a concentrated liquid outlet end and a purified water outlet end, and the second mixed liquid inlet end is communicated with the second mixed liquid outlet end; the desalting system is used for desalting the second mixed solution to obtain concentrated water and purified water.

In one embodiment, the demulsification reaction device comprises a pH value adjusting cavity, a demulsification adjusting cavity, a flocculating agent adjusting cavity and a first separation cavity which are communicated in sequence; the pH value adjusting cavity is provided with a wastewater stock solution feeding end, and the first separation cavity is provided with a first mixed solution discharging end.

In one embodiment, the first separation cavity is provided with a first separating part, the first separating part is arranged above the communication part of the first separation cavity and the flocculant adjusting cavity, and the first mixed liquid discharge end is arranged above the first separating part.

In one embodiment, the oxidation treatment device comprises a ferrous sulfate treatment cavity, a hydrogen peroxide treatment cavity, a neutralization flocculation cavity and a second separation cavity which are communicated in sequence; the ferrous sulfate treatment cavity is provided with the first mixed liquid inlet end; the second separation chamber is provided with a second mixed liquid discharge end.

In one embodiment, the desalination system comprises a filtration system, an ultrafiltration system and a reverse osmosis treatment system which are connected in sequence, wherein the filtration system is provided with the second mixed liquid inlet end, and the reverse osmosis treatment system is provided with a concentrated liquid outlet end and a purified water outlet end.

In one embodiment, the filtering system comprises a sand filter tank and a carbon filter tank which are sequentially communicated, the sand filter tank is provided with the second mixed liquid inlet end, and the carbon filter tank is communicated with the ultrafiltration system.

When the workshop cleaning wastewater treatment method is used for treating the wastewater stock solution, the wastewater stock solution is changed from an emulsified state to an oil-water mixed state through demulsification treatment, and oxidation treatment is carried out after separation so as to remove most organic matters in the first mixed solution. And finally, separating impurities from the purified water in the second mixed solution through desalting treatment. When the method is used for treating the workshop cleaning wastewater, the effluent quality of the purified water is higher.

Drawings

FIG. 1 is a flow chart of a method of a plant wastewater treatment process according to an embodiment of the present invention;

FIG. 2 is a flow chart of a method of a plant wastewater treatment process according to an embodiment of the present invention;

FIG. 3 is a schematic structural diagram of a plant wastewater treatment system according to an embodiment of the present invention.

Reference numerals are as follows:

100. a demulsification reaction device; 101. a stirring member; 110. a pH value adjusting cavity; 120. a demulsification adjusting cavity; 130. a PAC flocculant conditioning chamber; 140. a PAM flocculating agent adjusting cavity; 150. a first separation chamber; 151. a first separating member; 160. a first dosing system; 161. a first body; 162. a first conveyance member;

200. an oxidation treatment device; 201. a stirring paddle; 210. a ferrous sulfate treatment chamber; 220. a hydrogen peroxide treatment chamber; 230. PAC neutralization flocculation chamber; 240. PAM neutralizing flocculation cavity; 250. a second separation chamber; 251. a second separating member; 260. a second dosing system; 261. a second body; 262. a second conveyance member;

300. a desalination system; 310. a filtration system; 311. a sand filtration tank; 312. a carbon canister; 320. an ultrafiltration system; 321. ultrafiltration membranes; 322. an ultrafiltration water production tank; 330. a reverse osmosis treatment system; 331. a delivery pump body; 332. a cartridge filter; 333. a first high pressure pump; 334. a first-stage reverse osmosis device; 335. a secondary reverse osmosis device; 336. a third-stage reverse osmosis device; 337. an RO water producing tank; 338. a second high pressure pump;

400. a sludge treatment system; 410. a sludge pump; 420. a filter pressing device;

500. a temporary storage tank; 600. and (3) a filter.

Detailed Description

In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.

In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be considered limiting of the invention.

Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.

In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.

In the present invention, unless expressly stated or limited otherwise, the first feature "on" or "under" the second feature may be directly contacting the second feature or the first and second features may be indirectly contacting each other through intervening media. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.

It will be understood that when an element is referred to as being "secured to" or "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "upper," "lower," "left," "right," and the like as used herein are for illustrative purposes only and do not denote a unique embodiment.

Example 1

As shown in fig. 1, an embodiment of the present invention provides a method for treating plant cleaning wastewater, which includes the following steps:

s1, demulsifying the wastewater stock solution to obtain an oil-water mixture, and separating the oil-water mixture to obtain a first mixed solution;

s2, oxidizing the first mixed solution, layering the first mixed solution, and separating the turbid solution from the second mixed solution;

and S3, desalting the second mixed solution to obtain concentrated water and purified water.

In the above method, the wastewater stock solution is converted from an emulsified state to an oil-water layered state by demulsifying the wastewater stock solution, thereby facilitating oil-water separation to reduce COD (Chemical Oxygen Demand) in the wastewater stock solution. And separating the demulsified wastewater stock solution to obtain a first mixed solution with low COD content. The first mixed solution can be used for carrying out oxidation reaction on other organic matters contained in the wastewater through oxidation treatment so as to separate the organic matters in the wastewater to obtain a second mixed solution. The impurities contained in the second mixed solution can be concentrated and separated through desalination treatment to obtain purified water which can be discharged or recycled, and the residual concentrated water has high salt content and can be subjected to subsequent treatment through other treatment lines.

As shown in fig. 2, in some embodiments, the step S1 specifically includes the following steps:

s11; and adjusting the wastewater stock solution to be alkaline.

In the process of adjusting the wastewater stock solution, pH regulators such as sodium hydroxide and the like can be selected for adjusting the wastewater stock solution. The pH may be 7.5-9, for example 7.5, 8, 8.5 or 9.0. When the pH value of the wastewater stock solution is adjusted, the pH value of the wastewater stock solution can fluctuate within a certain range, and a certain specific pH value does not need to be maintained all the time.

S12; and adding a demulsifier into the wastewater stock solution for demulsification treatment.

And adding a demulsifier into the alkaline wastewater stock solution to change the wastewater stock solution from an emulsified state to an oil-water layered state. Wherein, the mass ratio range of the demulsifier to the wastewater stock solution can be (1-5): 1000. in the range, the demulsifier can demulsify the wastewater stock solution to a better degree, so that the oil-water separation degree of the wastewater stock solution is better.

In some of these embodiments, the mass ratio of the demulsifier to the wastewater dope can be 1:1000, 2:1000, 3:1000, 4:1000, or 5: 1000. For example, in a single wastewater treatment process, 2 kg of demulsifier is added to 1 ton of wastewater.

S13; and adding a flocculating agent after demulsification is finished.

And adding a flocculating agent into the demulsified wastewater stock solution, so that colloids and solid particles in the wastewater can be quickly adsorbed and bonded to form larger particles, and the larger particles are convenient to precipitate.

In some of these embodiments, the flocculating agent may include PAC (Poly aluminum Chloride) and PAM (Polyacrylamide). When the flocculating agent is added into the wastewater stock solution, PAC is added firstly, so that colloid in the wastewater stock solution reacts with PAC and is adsorbed and combined with PAC to form larger particles. And adding PAM into the wastewater stock solution, and bonding the particles into larger particles through the adsorption and bridging action of the PAM, so that the particles are easy to precipitate.

The PAC to wastewater liquor ratio during flocculant addition may range from (20 liters to 50 liters): 1 ton. When the PAC in the ratio range reacts with the colloid in the wastewater stock solution, the reaction is complete, and the waste of the PAC is less. For example, the ratio of PAC to the wastewater stock may be 20 liters: 1 ton, 30 l: 1 ton, 40 l: 1 ton or 50 l: 1 ton. Wherein, the mass concentration of PAC can be 3% -8%. The PAC with the mass concentration has better treatment effect when being treated. For example, the mass concentration of PAC may be 3%, 4%, 5%, 6%, 7% or 8%. For example, in a single wastewater treatment process, 30 liters of 5% PAC was added to 1 ton of wastewater.

The ratio of PAM to wastewater stock may range from (5 liters to 20 liters): 1 ton. The PAM in the ratio range has better effect when reacting with particles in the wastewater stock solution. For example, the ratio of PAM to wastewater stock may be 5 liters: 1 ton, 10 liters: 1 ton, 15 l: 1 ton or 20 l: 1 ton. Wherein, the mass concentration of the PAM can be 0.2-1.0%. When PAM with the mass concentration is treated, the adsorption and bonding effects are good. For example, the mass concentration of PAM may be 0.2%, 0.4%, 0.5%, 0.7%, 0.8%, or 1.0%. For example, in a single wastewater treatment process, 10 liters of PAM with a concentration of 0.5% is added to 1 ton of wastewater.

S14; separating to obtain a first mixed solution.

And separating the layered waste water stock solution after the flocculant is heated. The supernatant is the first mixed solution. The lower layer of turbid liquid can be subjected to mud-water separation, such as mud-water separation by a filter press device such as a plate filter press. Sludge and first filter pressing wastewater are obtained after mud-water separation. Wherein the first filter-pressing wastewater can be mixed with the wastewater stock solution for retreatment.

As shown in fig. 2, in some embodiments, the step S2 specifically includes the following steps:

s21, adjusting the pH value of the first mixed solution to 3-4.

And adjusting the first mixed solution to be acidic so that the pH value of the first mixed solution is 3-4, so as to form an acidic environment for subsequent reagents to react with the first mixed solution under appropriate conditions. For example, in some embodiments, the pH may be adjusted to 3.0, 3.2, 3.4, 3.6, 3.8, or 4.0. For example, in one embodiment, 11 kg of sodium hydroxide is added to 1 ton of wastewater to adjust the pH.

And S22, sequentially adding ferrous sulfate and hydrogen peroxide into the acidic first mixed solution to enable the first mixed solution to be subjected to oxidation reaction.

In the above step, the concentration of hydrogen peroxide by mass fraction may be 30%. The ratio of hydrogen peroxide to the first mixed liquor may be (3 liters to 8 liters): 1 ton. For example, the ratio of hydrogen peroxide to the first mixed solution may be 3 liters: 1 ton, 5 liters: 1 ton, 5.5 l: 1 ton or 8 l: 1 ton. For example, in one embodiment, 5.5 liters of 30% hydrogen peroxide is added to 1 ton of the first mixed solution.

The mass ratio of the ferrous sulfate to the first mixed solution can be (20-50): 1000. for example, the mass ratio of the ferrous sulfate to the first mixed solution may be 20:1000, 30:1000, 40:1000, or 50: 1000. For example, in one embodiment, 30 kg of ferrous sulfate is added to 1 ton of the first mixed solution.

And S23, adjusting the first mixed solution after the oxidation reaction to be alkaline.

And adjusting the first mixed solution after the oxidation reaction to be alkaline, so that solid matters in the first mixed solution are convenient to settle. In some embodiments, the pH may be adjusted to 8-10. For example, in some embodiments, the pH of the first mixed liquor is adjusted to 8, 8.5, 9, 9.5, or 10.

And S24, adding a flocculating agent into the first mixed solution adjusted to be alkaline for flocculation and separation to obtain a second mixed solution.

And adding a flocculating agent into the first mixed liquor which is adjusted to be alkaline so as to facilitate the solid matters in the first mixed liquor to agglomerate and precipitate.

In some of these embodiments, the flocculant may comprise PAC and PAM. When the flocculant is added to the first mixed solution, PAC is added first, and then PAM is added to the wastewater stock solution. Larger particles in the first mixed solution are agglomerated and precipitated through PAC and PAM, so that the separation is facilitated.

During the addition of the flocculant, the ratio of PAC to the first mixed liquor may range from (5 liters to 15 liters): 1 ton. For example, the ratio of PAC to first mixed liquor may be 5 liters: 1 ton, 8 liters: 1 ton, 10 liters: 1 ton or 15 l: 1 ton. Wherein, the mass concentration of PAC can be 3% -8%. For example, the mass concentration of PAC may be 3%, 4%, 5%, 6%, 7% or 8%. For example, in a single wastewater treatment process, 10 liters of 5% PAC is added to 1 ton of the first mixed liquor.

The ratio of PAM to first mixed liquor may range from (5 liters to 20 liters): 1 ton. For example, the ratio of PAM to wastewater stock may be 5 liters: 1 ton, 10 liters: 1 ton, 15 l: 1 ton or 20 l: 1 ton. Wherein, the mass concentration of the PAM can be 0.2-1.0%. For example, the mass concentration of PAM may be 0.2%, 0.4%, 0.5%, 0.7%, 0.8%, or 1.0%. For example, in a single wastewater treatment process, 10 liters of 0.5% PAM was added to 1 ton of the first mixed solution.

And when the flocculated first mixed solution is separated, the supernatant is the second mixed solution. The lower layer of turbid liquid can be introduced for sludge-water separation, for example, sludge-water separation by a filter press device such as a plate filter press. The filter press device may be the same as the filter press device in step S14, or may be another filter press device.

Sludge and second filter-pressing wastewater are obtained after mud-water separation. Wherein the second filter-pressing wastewater can be mixed with the wastewater stock solution for reprocessing.

As shown in fig. 2, in some embodiments, the step S3 specifically includes the following steps:

and S31, carrying out micro-flocculation filtration on the second mixed solution to obtain a first filtrate.

Suspended matter and non-soluble particles (such as oxides and particles) in the second mixed liquor are separated by micro-flocculation filtration. The turbidity and the pollution index in the second mixed solution can be effectively reduced, and trace heavy metal ions (such as mercury, chromium and the like) in the water can be removed.

Specifically, the second mixed solution may be subjected to sand filtration, and then the sand-filtered second mixed solution may be subjected to carbon filtration to obtain the first filtrate.

Through the mode of multi-media filtration, the water-insoluble impurities in the second mixed liquid are filtered, a certain protection effect can be achieved on a subsequent device, and the influence of the water-insoluble impurities in the second mixed liquid on the subsequent device can be prevented.

S32, carrying out ultrafiltration on the first filtrate to obtain a second filtrate;

and (3) carrying out ultrafiltration on the first filtrate to remove microorganisms, bacteria, colloid and fine suspended matters in the first filtrate. During ultrafiltration, the pressure difference between two sides of the ultrafiltration membrane is used as a driving force, and the ultrafiltration membrane is used as a filter medium. Under certain pressure, when the first filtrate flows across the surface of the ultrafiltration membrane, the dense fine micropores on the surface of the ultrafiltration membrane only allow water and small molecular substances to pass through to form the second filtrate, and substances with the volume larger than the micropore diameter on the surface of the membrane in the first filtrate are intercepted on the liquid inlet side of the ultrafiltration membrane to form the concentrated solution. Thereby realizing the purification, separation and concentration of the first filtrate. The concentrated solution may be mixed with the second mixed solution to facilitate the desalting treatment.

In some embodiments, the ultrafiltration membrane may be modified as appropriate. In the embodiment shown in FIG. 2, a membrane flux of 7.5m may be selected³A film of/d.

And S33, performing reverse osmosis treatment on the second filtrate to obtain concentrated water and purified water.

And performing reverse osmosis treatment on the second filtrate to remove soluble salt, colloid and organic matters in the second filtrate, thereby obtaining purified water. The quality of the outlet water of the purified water basically meets the water quality recycling standard or the discharge requirement.

The recovery rate of reverse osmosis treatment is more than 70%. The produced concentrated water can be subjected to outsourcing treatment.

In some embodiments, the reverse osmosis membrane can be modified according to the actual conditions. The membrane flux of the reverse osmosis membrane selected in the reverse osmosis treatment can be 10.6m³And d. Salt rejection: 97.5 percent, and selecting a 2-section reverse osmosis membrane.

In the workshop wastewater treatment process, the wastewater treatment effect is better, the yield of the obtained purified water is higher, and the quality of the effluent basically meets the water quality recycling standard or the discharge requirement. In addition, the workshop wastewater treatment process has low treatment cost and can reduce the pollution to the environment.

Example 2

As shown in fig. 3, an embodiment of the present invention provides a plant cleaning wastewater treatment system, which includes a demulsification reaction device 100, an oxidation treatment device 200, and a desalination system 300, which are sequentially disposed. The demulsification reaction device 100 is used for performing demulsification treatment on a wastewater stock solution and separating to obtain a first mixed solution. The oxidation treatment apparatus 200 is configured to perform oxidation treatment on the first mixed solution and separate sludge to obtain a second mixed solution. The desalination system 300 is configured to perform desalination on the second mixed solution to obtain concentrated water and purified water.

Through above-mentioned workshop cleaning wastewater treatment system, can handle workshop cleaning wastewater better, reduce the pollution to the environment.

In the embodiment shown in fig. 3, a is the point of entry of the raw wastewater. The B position is a sludge delivery position. The C position is a concentrated water discharge position. And D is a purified water discharge part. And E is a mixed wastewater inlet.

In some embodiments, the emulsion breaking reaction apparatus 100 includes a wastewater raw liquid inlet end and a first mixed liquid outlet end. The wastewater stock solution enters the emulsion breaking reaction device 100 from the wastewater stock solution inlet end, and then is subjected to emulsion breaking reaction and separation, and the first mixed solution is discharged from the first mixed solution end.

Specifically, in some embodiments, the emulsion breaking reaction device 100 includes a ph adjusting chamber 110, an emulsion breaking adjusting chamber 120, a flocculant adjusting chamber, and a first separation chamber 150, which are connected in sequence.

Wherein, the wastewater stock solution can sequentially pass through the pH value adjusting cavity 110, the demulsification adjusting cavity 120, the flocculating agent adjusting cavity and the first separating cavity 150. The liquid inlet end of the pH value adjusting cavity 110 is the inlet end of the wastewater stock solution. The first separation chamber 150 is provided with the aforementioned first mixed liquor end. The demulsification reaction device 100 is provided with a stirring piece 101 in each chamber except the first separation chamber 150. The stirring members 101 may be rotated with respect to the corresponding chambers so that the wastewater dope is sufficiently reacted with the chemical in the corresponding chambers.

In some embodiments, the flocculant comprises only one agent or two or more agents in no order, and only one flocculant-regulating chamber is provided. In other embodiments, where the flocculating agent requires multiple sequential doses of the agent, multiple sequentially connected flocculating agent conditioning chambers may be provided. For example, in one embodiment, the flocculant may be PAM + PAC, and thus, the flocculant adjustment chamber may include a PAC flocculant adjustment chamber 130 and a PAM flocculant adjustment chamber 140 in series.

In some embodiments, the first separation chamber 150 may be provided with a first separating member 151. The first separating member 151 may be a screen or other filtering elements may be used. The first separating member 151 may be disposed above where the first separating chamber 150 communicates with the flocculant adjustment chamber. The first mixed liquid discharge end is disposed above the first separator 151. The above arrangement enables the supernatant, that is, the first mixed solution to be discharged after the raw wastewater entering the first separation chamber 150 is separated by the first separating member 151. While the lower layer of turbid liquid can be discharged through the first separation chamber 150.

In some embodiments, the chambers are arranged in parallel. The horizontal positions of the communicated parts of the two adjacent chambers are different. For example, as shown in FIG. 3, in some embodiments, one of the junctions between two adjacent chambers is located at the top of the corresponding chamber wall, and the other of the junctions between two adjacent chambers is located at the bottom of the chamber wall. The arrangement can enable the cavity wall between the two chambers to have a choked flow effect when the wastewater stock solution moves from one chamber to the other chamber, so that the wastewater stock solution is mixed with the medicament more uniformly in the moving process.

In some embodiments, the first dosing system 160 may be used to add the chemical to each chamber of the emulsion breaking reaction device 100 other than the first separation chamber 150. First medicated system 160 may include a first body 161 and a first delivery member 162. The first transfer member 162 may supply the agent within the first body 161 to a corresponding chamber in the emulsion breaking reaction device 100.

In some embodiments, the number of the first bodies 161 and the first conveying members 162 is the same, and each set of the first bodies 161 and the first conveying members 162 corresponds to the ph adjusting chamber 110 and the emulsion breaking adjusting chamber 120 in the emulsion breaking reaction device 100 and corresponds to the flocculant adjusting chamber. Each first body 161 is rotatably provided therein with a stirrer blade. In other embodiments, the first body 161 has a plurality of independent chambers, and each chamber corresponds to the ph adjusting chamber 110, the emulsion breaking adjusting chamber 120 and the flocculant adjusting chamber in the emulsion breaking reaction device 100. Stirring blades are rotatably arranged in each cavity. One first conveying member 162 corresponds to each chamber, and the first conveying member 162 can convey the liquid in the chamber to the corresponding chamber of the emulsion breaking reaction device 100.

For example, in the embodiment shown in FIG. 3, the emulsion breaking reaction device 100 comprises a pH value adjusting chamber 110, an emulsion breaking adjusting chamber 120, a PAC flocculant adjusting chamber 130, a PAM flocculant adjusting chamber 140 and a first separation chamber 150 which are communicated in sequence. First medicating system 160 includes a first body 161 and four first delivery members 162. Four cavities are independently arranged in the first main body 161, and the four cavities are respectively connected with the corresponding first conveying members 162. The four cavities are respectively filled with an acid-base regulator (such as sodium hydroxide), a demulsifier, PAM and PAC.

The cavity containing the ph adjusting agent is communicated with the ph adjusting cavity 110 through the corresponding first conveying member 162. The chamber containing the emulsion breaker is in communication with the emulsion breaking conditioning chamber 120 via a corresponding first conveyance 162. Wherein the PAC containing cavity is in communication with PAC flocculant conditioning cavity 130 via a corresponding first transport member 162. Wherein the chamber containing PAM is in communication with PAM flocculant adjustment chamber 140 via a corresponding first conveyance member 162.

When the wastewater stock solution sequentially passes through the pH value adjusting cavity 110, the demulsification adjusting cavity 120, the PAC flocculant adjusting cavity 130 and the PAM flocculant adjusting cavity 140, the wastewater stock solution is subjected to demulsification and flocculation, and the emulsified wastewater stock solution is subjected to oil-water layering and flocculation. So that most of impurities in the waste water stock solution are agglomerated and settled. After the wastewater stock solution enters the first separation chamber 150, the supernatant is used as a first mixed solution and is input into the oxidation treatment device 200 for oxidation treatment. The lower layer of turbid liquid can be subjected to sludge separation, so that sludge is obtained.

In some embodiments, the oxidation treatment unit 200 includes a first mixed liquor inlet end, a second mixed liquor outlet end, and a sludge outlet end. The first mixed liquid enters the oxidation treatment device 200 from the first mixed liquid inlet end and is subjected to oxidation treatment. The second mixed liquid obtained after the treatment is discharged from the second mixed liquid discharge end. And discharging the sludge obtained after treatment from a sludge discharge end.

In some embodiments, the oxidation treatment apparatus 200 includes a ferrous sulfate treatment chamber 210, a hydrogen peroxide treatment chamber 220, a neutralization flocculation chamber, and a second separation chamber 250, which are in communication in sequence.

The first mixed liquid may sequentially pass through the ferrous sulfate treatment chamber 210, the hydrogen peroxide treatment chamber 220, the neutralization flocculation chamber, and the second separation chamber 250. The liquid inlet end of the ferrous sulfate treatment cavity 210 is the first mixed liquid inlet end of the oxidation treatment device 200. The second separation chamber 250 is provided with the aforementioned second mixed liquid discharge end and sludge discharge end. The stirring members 201 are provided in each chamber except the second separation chamber 250 of the oxidation treatment apparatus 200. The stirring members 201 may be rotated with respect to the corresponding chambers so that the first mixed solution is sufficiently reacted with the medicine in the corresponding chambers.

In some embodiments, the agent administered in the neutralization flocculation chamber may comprise only one agent or two or more agents without any sequence, and only one neutralization flocculation chamber is provided. In other embodiments, the agents to be added into the neutralization flocculation cavity are multiple agents to be added in sequence, and then multiple neutralization flocculation cavities which are communicated in sequence can be arranged. For example, in one embodiment, the agent for neutralizing the flocculation in the cavity can be PAM + PAC. Thus, the neutralization flocculation chamber may include a PAC neutralization flocculation chamber 230 and a PAM neutralization flocculation chamber 240 in serial communication.

The second separating chamber 250 may be provided with a second separating member 251. The second separating member 251 may be a screen, or other filtering elements may be used. The second separating member 251 may be disposed above where the second separating chamber 250 communicates with the neutralization and flocculation chamber. The second mixed liquid discharge end is disposed above the second separator 251. The above arrangement enables the supernatant, that is, the second mixed solution to be discharged after the first mixed solution entering the second separation chamber 250 is separated by the second separating member 251. And the lower layer turbid liquid can be discharged through the second separation chamber 250, and can be separated to obtain sludge after being discharged.

In some embodiments, the chambers are arranged in parallel. The horizontal positions of the communicated parts of the two adjacent chambers are different. For example, as shown in FIG. 3, in some embodiments, one of the junctions between two adjacent chambers is located at the top of the corresponding chamber wall, and the other of the junctions between two adjacent chambers is located at the bottom of the chamber wall. By the arrangement, when the first mixed liquid moves from one chamber to the other chamber, the chamber wall between the two chambers has a choked flow effect, so that the first mixed liquid is more uniformly mixed with the medicament in the moving process, and the oxidation reaction is more sufficient.

In some embodiments, the additional agent in each chamber may be delivered into the chamber by a second medicating system 260. Second medicated system 260 may include a second body 261 and a second delivery member 262. The second transfer member 262 may supply the agent within the second body 261 to a corresponding chamber in the emulsion breaking reaction device 100.

The second medicine adding system 260 may be used for adding the medicine to each chamber of the oxidation treatment apparatus 200 except the second separation chamber 250. Second medicated system 260 may include a second body 261 and a second delivery member 262. The second transfer member 262 may supply the agent in the second body 261 to a corresponding chamber in the oxidation treatment device 200.

In some embodiments, the number of the second bodies 261 and the number of the second conveying members 262 are the same, and each set of the second bodies 261 and the second conveying members 262 corresponds to the ferrous sulfate treatment chamber 210 and the hydrogen peroxide treatment chamber 220 in the oxidation treatment device 200 and the neutralization flocculation chamber. Stirring blades are rotatably arranged in each second main body 261. In other embodiments, the second body 261 has a plurality of independent cavities, and each of the cavities corresponds to the ferrous sulfate treatment cavity 210 and the hydrogen peroxide treatment cavity 220 in the oxidation treatment device 200, and the neutralization flocculation cavity. Stirring blades are rotatably arranged in each cavity. One second conveying member 262 corresponds to each chamber, and the second conveying member 262 can convey the liquid in the chamber to the corresponding chamber of the emulsion breaking reaction device 100.

For example, as shown in fig. 3, the oxidation treatment apparatus 200 includes a ferrous sulfate treatment chamber 210, a hydrogen peroxide treatment chamber 220, a neutralization and flocculation chamber, and a second separation chamber 250, which are connected in sequence. Second medicated system 260 includes a second body 261 and four second delivery members 262. Four cavities are independently arranged in the second main body 261 and are respectively connected with the corresponding second conveying pieces 262. Ferrous sulfate, hydrogen peroxide, PAM and PAC are respectively contained in the four cavities.

The cavity containing ferrous sulfate is communicated with the ferrous sulfate treatment cavity 210 through the corresponding second conveying element 262. The chamber containing hydrogen peroxide is in communication with the hydrogen peroxide treatment chamber 220 via a corresponding second delivery member 262. Wherein the chamber containing the PAC communicates with the PAC neutralization and flocculation chamber 230 through a corresponding second conveyance member 262. The cavity containing the PAM is communicated with the PAM neutralization flocculation chamber 240 through a corresponding second conveying member 262.

In some embodiments, the feed to the oxidation treatment apparatus 200 may also be fed with mixed wastewater. The mixed wastewater may be other wastewater that has been subjected to oil-water filtration, may be wastewater having a high concentration obtained after the treatment by the oxidation treatment apparatus 200, may be wastewater having a high concentration obtained after the treatment by the subsequent desalination system 300, or may be a mixed liquid of the above-described at least two types of wastewater.

In the oxidation treatment apparatus 200, the first mixed solution passes through the ferrous sulfate treatment chamber 210, the hydrogen peroxide treatment chamber 220, the PAC neutralization and flocculation chamber 230, and the PAM neutralization and flocculation chamber 240 in this order. The first mixed solution is subjected to Fenton oxidation and flocculation, and most of organic matters in the first mixed solution are subjected to oxidation reaction. Before the first mixed liquid enters the PAC neutralization flocculation chamber 230, the pH of the first mixed liquid may be adjusted to 8-10, and then flocculation may be performed. The arrangement mode can lead the sludge to be rapidly agglomerated and precipitated. After the first mixed solution enters the second separation chamber 250, the supernatant is input to the desalination system 300 as a second mixed solution for desalination. The lower layer of turbid liquid can be subjected to sludge separation, so that sludge is obtained.

In some embodiments, the plant cleaning wastewater treatment system further includes a sludge treatment system 400. The sludge treatment system 400 includes a sludge pump 410 and a filter press device 420. The sludge pump 410 can deliver the liquid with the more solid objects to the filter press device 420. The filter press device 420 can separate the liquid from the solid sludge. The filter press device 420 can be a plate filter press or other filter press devices.

In some of these embodiments, the sludge pump 410 may be in communication with a lower, turbid liquid discharge provided at the bottom of the first separation chamber 150. The sludge pump 410 can convey the lower layer of turbid liquid obtained from the first separation chamber 150 to the filter pressing device 420, so that the filter pressing device 420 can filter-press the turbid liquid to separate the solid sludge from the liquid.

In other embodiments, the sludge pump 410 may be in communication with a lower slurry discharge provided at the bottom of the second separation chamber 250. The sludge pump 410 can convey the lower layer of turbid liquid obtained by the second separation chamber 250 to the filter pressing device 420, so that the filter pressing device 420 can filter-press the turbid liquid to separate the solid sludge from the liquid.

In other embodiments, the number of the sludge pumps 410 may be two, wherein one of the sludge pumps 410 may be in communication with the lower turbid liquid outlet provided at the bottom of the first separation chamber 150, and the other sludge pump 410 may be in communication with the lower turbid liquid outlet provided at the bottom of the second separation chamber 250. The conduits of the two sludge pumps 410 can be communicated so as to convey the turbid liquid obtained from the first separation chamber 150 and the second separation chamber 250 together to the filter pressing device 420. Such an arrangement can reduce the number of filter press devices 420 and thus reduce costs.

The sludge obtained by the filter pressing device 420 can be transported out for subsequent treatment. The clear liquid obtained by the filter pressing device 420 may be mixed with the raw wastewater liquid and then input to the raw wastewater liquid inlet end of the emulsion breaking reaction device 100, or may be mixed with the first mixed liquid and then input to the first mixed liquid inlet end of the oxidation treatment device 200.

In some embodiments, the desalination system 300 can subject the second mixed liquor to a desalination process to obtain concentrated water and purified water. Specifically, in some embodiments, desalination system 300 includes a filtration system 310, an ultrafiltration system 320, and a reverse osmosis treatment system 330 connected in series. The filtering system 310 is provided with a second mixed liquid inlet end, and the filtering system 310 can perform micro-flocculation filtering on the second mixed liquid to obtain a first filtered liquid. The ultrafiltration system 320 can perform ultrafiltration on the first filtrate to obtain a second filtrate. The reverse osmosis treatment system 330 may perform a reverse osmosis treatment on the second filtrate to obtain concentrated water and purified water. Wherein the concentrated water can be subjected to outsourcing treatment. The quality of the outlet water of the purified water is good, and the purified water can be directly discharged or reused.

In some embodiments, the filtration system 310 includes a sand canister 311 and a carbon canister 312 in serial communication. The sand filter tank 311 is provided with the aforementioned second mixed liquid inlet end, and the carbon filter tank 312 is communicated with the ultrafiltration system 320. The second mixed solution passes through the sand filtration tank 311 and the carbon filtration tank 312 in this order. Impurities which are not dissolved in water are filtered through various media, so that the damage of the insoluble impurities to the reverse osmosis treatment system 330 is reduced when the subsequent reverse osmosis treatment system 330 is used for treatment.

Turbidity, contamination index, etc. in the second filtrate may be reduced by the aforementioned filtration system 310. In addition, the filtering system 310 may deodorize the second filtered liquid, and may also remove trace heavy metal ions (such as mercury, chromium, and the like), synthetic detergents, radioactive substances, and the like from the second filtered liquid.

In some embodiments, a temporary storage tank 500 may be further disposed between the sand filter tank 311 and the oxidation treatment device 200. The temporary storage tank 500 may temporarily store the second mixed liquid obtained by the oxidation treatment apparatus 200, so that the flow rate change of the second mixed liquid is reduced when the second mixed liquid is delivered to the filtering system 310. In some embodiments, a transfer pump may also be provided between the staging tank 500 and the sand filter tank 311. The transfer pump may be provided to facilitate the passage of the second mixed liquor from the holding tank 500 into the sand filtration tank 311.

In some embodiments, the ultrafiltration system 320 is provided with an ultrafiltration membrane 321. One side of the ultrafiltration membrane 321 is an inlet end of the first filtrate, and the other side of the ultrafiltration membrane 321 is an outlet end of the second filtrate. When the first filtrate moves from one side of the ultrafiltration membrane 321 to the other side under the action of pressure, the dense micropores on the surface of the ultrafiltration membrane 321 only allow water and small molecular substances to pass through to form a second filtrate, and substances with a volume larger than the micropore diameter on the surface of the membrane in the first filtrate are trapped on the liquid inlet side of the membrane to form a concentrated solution.

In some embodiments, the concentrate may be fed directly into the sand filter tank 311. In other embodiments, the concentrate may be transferred to the holding tank 500 and then pumped into the sand filter tank 311 for filtration.

In some embodiments, the first filtrate may be filtered by a filter 600 before entering the ultrafiltration system 320, thereby reducing large particulate matter.

The ultrafiltration system 320 can remove colloids and fine suspended matters in the first filtrate, has a certain removing effect on microorganisms, bacteria and the like in the first filtrate, and improves the running stability of the subsequent reverse osmosis treatment system 330.

In some embodiments, the ultrafiltration system 320 can be adjusted to suit the application. Ultrafiltration system 320 can be of the type: VNF 2-4040. The ultrafiltration membrane 321 may have a membrane flux of 7.5m³/d。

In some embodiments, the ultrafiltration device further comprises an ultrafiltration water production tank 322. The ultrafiltration water generating tank 322 can temporarily store the second filtrate so that the flow rate of the second mixed liquid delivered to the reverse osmosis treatment system 330 is stable.

In some embodiments, the reverse osmosis treatment system 330 includes a security device, a reverse osmosis device, and a RO product water tank 337. Wherein, the safety device is arranged between the reverse osmosis device and the ultrafiltration device. The safety device can pre-filter large-particle substances in the second filtrate, so that damage of the large-particle substances to the reverse osmosis device is reduced. The reverse osmosis device can carry out reverse osmosis on the second filtrate, so that concentrated water in the second filtrate is separated from purified water. The purified water may be stored through the RO product water tank 337.

In some embodiments, the safety device may include a delivery pump body 331, a safety filter 332, and a first high-pressure pump 333, which are sequentially disposed. The second filtrate may be fed to the cartridge filter 332 via feed pump 331 for pre-filtration to reduce damage to the reverse osmosis system 330 from large particles. The first high-pressure pump 333 supplies the second filtrate with a pressure so that the second filtrate can be subjected to reverse osmosis normally.

In some embodiments, the reverse osmosis apparatus may include a primary reverse osmosis apparatus 334, a secondary reverse osmosis apparatus 335, and a tertiary reverse osmosis apparatus 336. The first-stage reverse osmosis device 334, the second-stage reverse osmosis device 335 and the third-stage reverse osmosis device 336 are all provided with reverse osmosis membranes. Wherein the first stage reverse osmosis unit 334 is in communication with the first high pressure pump 333. The primary reverse osmosis device 334 may separate the first purified water from the second filtrate. The separated first purified water may be directly introduced into the RO product tank 337. The higher concentration liquid produced in the primary reverse osmosis unit 334 may enter the secondary reverse osmosis unit 335. The secondary reverse osmosis unit 335 further reverse osmosis the higher concentration liquid produced in the primary reverse osmosis unit 334 to separate the second purified water from the concentrate. The separated second purified water may be directly introduced into the RO product tank 337. The concentrate can then exit the reverse osmosis unit from the concentrate discharge.

The water outlet end of the RO product tank 337 may be connected to a second high pressure pump 338. The output of the second high pressure pump 338 may be connected to a tertiary reverse osmosis unit 336. The three-stage reverse osmosis device 336 may further subject the mixed liquid of the first purified water and the second purified water to a reverse osmosis process. Thereby obtaining purified water with high quality of outlet water. The liquid with slightly higher ion concentration obtained by the third-stage reverse osmosis device 336 can be input into the ultrafiltration water production tank 322 so as to continue the desalination treatment.

In some embodiments, the number of the first reverse osmosis device 334, the second reverse osmosis device 335 and the third reverse osmosis device 336 may be one, or two or more. For example, in the embodiment shown in FIG. 3, the number of primary, secondary and tertiary

reverse osmosis units

334, 335 and 336 is two. The two first-stage reverse osmosis devices 334 are arranged in parallel, that is, the liquid inlets of the two first-stage reverse osmosis devices 334 are communicated, and the liquid outlets of the two first-stage reverse osmosis devices 334 are communicated. Similarly, two secondary reverse osmosis units 335 are arranged in parallel. The tertiary reverse osmosis units 336 are arranged in parallel. The number of the first-stage reverse osmosis device 334, the second-stage reverse osmosis device 335 and the third-stage reverse osmosis device 336 can be adjusted according to actual conditions, and the number of the first-stage reverse osmosis device, the second-stage reverse osmosis device and the third-stage reverse osmosis device can be partially the same, different or completely the same.

The reverse osmosis membrane can be adjusted according to actual conditions. For example, in some embodiments, the reverse osmosis membrane may have a membrane flux of 10.6m³And d. The reverse osmosis device can be selected from ULP31-4040 the salt rejection may be 97.5%.

In some embodiments, the feed side of the primary, secondary and tertiary

reverse osmosis units

334, 335, 336 may be provided with a safety valve (not shown). The safety valve can ensure that the equipment operates under the safety pressure. The outlet ends of the first reverse osmosis unit 334, the second reverse osmosis unit 335 and the third reverse osmosis unit 336 can be provided with sampling valves (not shown in the figure), and the sampling valves can be arranged to facilitate the detection of the operation condition of the system.

In some embodiments, a cleaning system (not shown) is also provided. The cleaning system has a cleaning conduit. The cleaning pipeline can be communicated with the liquid inlet end and the liquid outlet end of the first-stage reverse osmosis device 334, the second-stage reverse osmosis device 335 and the third-stage reverse osmosis device 336. Such an arrangement may facilitate cleaning of the reverse osmosis unit, thereby improving the service life of the reverse osmosis unit.

Through the reverse osmosis system, soluble salt, colloid and organic matters in the second mixed solution can be removed, so that the quality of the outlet water of the purified water reaches the recycling standard or the discharge requirement.

The technical features of the embodiments described above may be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the embodiments described above are not described, but should be considered as being within the scope of the present specification as long as there is no contradiction between the combinations of the technical features.

The above-mentioned embodiments only express several embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the invention. It should be noted that, for a person skilled in the art, several variations and modifications can be made without departing from the inventive concept, which falls within the scope of the present invention. Therefore, the protection scope of the present patent shall be subject to the appended claims.

Claims

1. The method for treating the workshop cleaning wastewater is characterized by comprising the following steps of:

2. The method for treating plant cleaning wastewater according to claim 1, wherein the step of obtaining the second mixed liquor from the first mixed liquor comprises the following steps:

adjusting the pH value of the first mixed solution to 3-4;

adjusting the first mixed solution after the oxidation reaction to be alkaline;

3. The method for treating the workshop cleaning wastewater according to claim 1, wherein in the process of obtaining the first mixed solution from the wastewater stock solution, the wastewater stock solution is adjusted to be alkaline, then the demulsifier is added into the wastewater stock solution to perform demulsification treatment, so that the wastewater is changed from an emulsified state to an oil-water layered state, then the flocculant is added to layer the wastewater stock solution, and the first mixed solution is obtained after separating a lower layer of turbid solution.

4. The method for treating the plant cleaning wastewater according to any one of claims 1 to 3, wherein the step of subjecting the second mixed solution to desalination treatment to obtain concentrated water and purified water comprises the steps of:

subjecting the first filtrate to ultrafiltration to obtain a second filtrate;

and carrying out reverse osmosis treatment on the second filtrate to obtain concentrated water and purified water.

5. A plant cleaning wastewater treatment system, comprising:

the demulsification reaction device comprises a wastewater stock solution inlet end and a first mixed solution outlet end; the demulsification reaction device is used for performing demulsification treatment on the wastewater stock solution and separating the wastewater stock solution to obtain a first mixed solution;

the oxidation treatment device comprises a first mixed liquid inlet end, a second mixed liquid outlet end and a sludge outlet end, wherein the first mixed liquid inlet end is communicated with the first mixed liquid outlet end; the oxidation treatment device is used for carrying out oxidation treatment on the first mixed liquor and separating sludge to obtain second mixed liquor;

6. The workshop cleaning wastewater treatment system of claim 5, wherein the demulsification reaction device comprises a pH value adjusting cavity, a demulsification adjusting cavity, a flocculating agent adjusting cavity and a first separation cavity which are communicated in sequence; the pH value adjusting cavity is provided with a wastewater stock solution feeding end, and the first separation cavity is provided with a first mixed solution discharging end.

7. The plant cleaning wastewater treatment system according to claim 6, wherein the first separation chamber is provided with a first separator, the first separator is arranged above a position where the first separation chamber is communicated with the flocculant adjusting chamber, and the first mixed liquid discharge end is arranged above the first separator.

8. The workshop cleaning wastewater treatment system of claim 5, wherein the oxidation treatment device comprises a ferrous sulfate treatment chamber, a hydrogen peroxide treatment chamber, a neutralization flocculation chamber and a second separation chamber which are communicated in sequence; the ferrous sulfate treatment cavity is provided with the first mixed liquid inlet end; the second separation chamber is provided with a second mixed liquid discharge end.

9. The plant cleaning wastewater treatment system according to claim 5, wherein the desalination system comprises a filtration system, an ultrafiltration system and a reverse osmosis treatment system which are connected in sequence, the filtration system is provided with the second mixed liquid inlet end, and the reverse osmosis treatment system is provided with a concentrated liquid outlet end and a purified water outlet end.

10. The plant cleaning wastewater treatment system according to any one of claims 5 to 9, wherein the filtration system comprises a sand filtration tank and a carbon filtration tank which are communicated in sequence, the sand filtration tank is provided with the second mixed liquid inlet end, and the carbon filtration tank is communicated with the ultrafiltration system.