CN115259429A - Processing device for flowback liquid - Google Patents
Processing device for flowback liquid Download PDFInfo
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- CN115259429A CN115259429A CN202110482804.XA CN202110482804A CN115259429A CN 115259429 A CN115259429 A CN 115259429A CN 202110482804 A CN202110482804 A CN 202110482804A CN 115259429 A CN115259429 A CN 115259429A
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- 238000005345 coagulation Methods 0.000 claims abstract description 40
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- 238000005188 flotation Methods 0.000 claims abstract description 33
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 26
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- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims description 5
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- 238000004891 communication Methods 0.000 claims description 4
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- 239000011574 phosphorus Substances 0.000 description 7
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
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- 235000019982 sodium hexametaphosphate Nutrition 0.000 description 1
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 description 1
- 235000019832 sodium triphosphate Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910001427 strontium ion Inorganic materials 0.000 description 1
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- 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
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
-
- 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
-
- 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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- 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
- C02F2209/05—Conductivity or salinity
- C02F2209/055—Hardness
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- 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
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- 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
- C02F2209/11—Turbidity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The application provides a processing apparatus of flowing back liquid belongs to sewage treatment technical field. The processing device includes: the device comprises an air flotation unit, a softening unit, a coagulation sedimentation unit, a first filtering unit, a second filtering unit and a reverse osmosis unit; the device comprises an air flotation unit, a softening unit, a coagulation sedimentation unit, a first filtering unit, a second filtering unit and a reverse osmosis unit, wherein the air flotation unit is used for reducing the concentration of organic matters and the concentration of microorganisms in the flowback liquid to be treated, the softening unit is used for reducing scale forming ions in the flowback liquid by adding a descaling agent, the coagulation sedimentation unit is used for reducing the turbidity of the flowback liquid by adding a turbidity reducing agent, the first filtering unit is used for filtering impurities in the flowback liquid, the second filtering unit is used for filtering the scale forming ions in the flowback liquid, and the reverse osmosis unit is used for reducing the mineralization degree in the flowback liquid to obtain a liquid preparation of the fracturing liquid. Because the treatment device can reduce the concentration of organic matters, the concentration, the turbidity, the impurities, the scaling ions and the mineralization degree in the flowback fluid, the quality of the prepared fracturing fluid is improved.
Description
Technical Field
The application relates to the technical field of sewage treatment, in particular to a treatment device for backflow liquid.
Background
At present, hydraulic fracturing is an important technology for improving the shale gas exploitation amount of a reservoir. In the process of hydraulic fracturing of a reservoir, a large amount of impurities such as sludge, suspended matters, organic matters and the like are contained in a flowback fluid discharged from the reservoir, and the flowback fluid needs to be treated by a flowback fluid treatment device in order to be reused.
In the related art, a treatment device for flowback liquid comprises a coagulation sedimentation unit; and reducing the turbidity of the return fluid through a coagulation and sedimentation unit to obtain a prepared fluid of the fracturing fluid. However, the treatment apparatus in the related art described above can only reduce the turbidity of the flowback fluid, and the water quality requirement of the prepared fracturing fluid includes not only the turbidity requirement but also other requirements such as resistance reduction, and the reduction of the turbidity of the flowback fluid cannot satisfy the water quality requirement of the prepared fracturing fluid, so that the water quality of the prepared fracturing fluid obtained by the treatment apparatus for the flowback fluid is poor.
Disclosure of Invention
The embodiment of the application provides a processing apparatus of flowing back liquid, can improve the quality of water of joining in marriage the liquid of the fracturing fluid that obtains after flowing back liquid is handled. The technical scheme is as follows:
the application provides a processing apparatus of flowing back liquid, processing apparatus includes: the device comprises an air flotation unit, a softening unit, a coagulation sedimentation unit, a first filtering unit, a second filtering unit and a reverse osmosis unit;
the air flotation unit, the softening unit, the coagulation sedimentation unit, the first filtering unit, the second filtering unit and the reverse osmosis unit are communicated in sequence;
the air flotation unit is used for reducing the concentration of organic matters and the concentration of microorganisms in the flowback liquid to be treated, the softening unit is used for reducing scale forming ions in the flowback liquid by adding a descaling agent, the coagulation sedimentation unit is used for reducing the turbidity of the flowback liquid by adding a turbidity reducing agent, the first filtering unit is used for filtering impurities in the flowback liquid, the second filtering unit is used for filtering the scale forming ions in the flowback liquid, and the reverse osmosis unit is used for reducing the mineralization degree in the flowback liquid to obtain the liquid preparation of the fracturing liquid.
In one possible implementation, the air flotation unit includes a lift pump, an air flotation machine, and a first container;
the lifting pump and the air floatation machine are respectively communicated with a water inlet of the first container, and a water outlet of the first container is communicated with a water inlet of the softening unit;
the lifting pump is used for lifting the flow-back liquid to the first container, and the air flotation machine is used for filling first gas into the first container and reducing the concentration of organic matters in the flow-back liquid through the first gas.
In another possible implementation manner, the air flotation unit further comprises a sterilization tank;
the sterilizing tank is communicated with the water inlet of the first container and is used for introducing sterilizing agent into the first container, and the concentration of microorganisms in the flowback liquid is reduced through the sterilizing agent.
In another possible implementation, the air flotation machine comprises an air compressor and a dissolved air tank;
the air compressor is communicated with the water inlet of the first container through the dissolved air tank;
the air compressor is used for compressing air into water in the air dissolving tank to form air dissolving water, the air dissolving tank is used for inputting the air dissolving water into the first container, and ferrous ions in the backflow liquid are oxidized into ferric ions through the air in the air dissolving water to form precipitates.
In another possible implementation manner, the softening unit comprises a second container, a third container, a pH value detector, a hardness detector, an alkaline adjusting tank and a descaling tank;
the water inlet of the second container is communicated with the water outlet of the air floatation unit, the water outlet of the upper part of the second container is communicated with the water inlet of the upper part of the third container, the water outlet of the lower part of the third container is communicated with the water inlet of the lower part of the coagulation sedimentation unit, the pH value detector is arranged in the second container, the hardness detector is arranged in the third container, the alkaline adjusting tank is communicated with the second container, and the descaling tank is communicated with the third container;
the backflow liquid treated by the air floatation unit enters the second container through a water outlet of the air floatation unit and a water inlet of the second container, the pH value detector is used for detecting the pH value of the backflow liquid in the second container, the hardness detector is used for detecting the hardness of the backflow liquid in the third container, the alkalinity adjusting tank is used for introducing an acid-base adjusting agent into the second container to adjust the pH value of the backflow liquid, and the descaling tank is used for introducing a descaling agent into the third container to reduce scale forming ions in the backflow liquid.
In another possible implementation, the softening unit further comprises a first controller;
the first controller is used for determining a first volume of the acid-base regulator and a second volume of the descaling agent which are added into the second container according to the pH value and the hardness of the return liquid, controlling the alkaline regulating tank to feed the acid-base regulator with the first volume into the second container, and controlling the descaling tank to feed the descaling agent with the second volume into the third container.
In another possible implementation, the coagulation sedimentation unit comprises a fourth container, a fifth container, a sixth container and a turbidity regulation tank;
a water inlet at the lower part of the fourth container is communicated with a water outlet of the softening unit, a water outlet at the upper part of the fourth container is communicated with a water inlet at the upper part of the fifth container, a water outlet at the middle part of the fifth container is communicated with a water inlet at the middle part of the sixth container, a water outlet at the upper part of the sixth container is communicated with the first filtering unit, and the turbidity adjusting tank is respectively communicated with the fifth container and the sixth container;
the returned liquid treated by the softening unit enters the fourth container through a water outlet of the softening unit and a water inlet of the fourth container, the turbidity regulating tank is used for introducing a turbidity reducing agent into the fourth container and the fifth container to reduce the turbidity of the returned liquid, and the sixth container is used for collecting precipitates in the returned liquid.
In another possible implementation, the turbidity adjusting tanks include a first turbidity adjusting tank and a second turbidity adjusting tank, the turbidity reducing agent includes a coagulant and a flocculant, the first turbidity adjusting tank is in communication with the fourth container, and the second turbidity adjusting tank is in communication with the fifth container;
the first turbidity adjusting tank is used for introducing a coagulant into the fourth container to enable small particulate matters in the return liquid to form large particulate matters; and the second turbidity adjusting tank is used for introducing a flocculating agent into the fifth container to enable large granular substances to form large flocs, so that the turbidity of the return liquid is reduced.
In another possible implementation manner, the coagulation sedimentation unit further comprises a second controller, a first turbidity detector and a second turbidity detector;
the first turbidity detector is arranged in the fourth container, the second turbidity detector is arranged in the fifth container, and the second controller is respectively and electrically connected with the first turbidity detector, the second turbidity detector, the first turbidity adjusting tank and the second turbidity adjusting tank;
the first turbidity detector is used for detecting a first turbidity of the return liquid in the fourth container, the second turbidity detector is used for detecting a second turbidity of the return liquid in the fifth container, the second controller is used for determining a third volume of the coagulant added into the fourth container according to the first turbidity, determining a fourth volume of the flocculant added into the fifth container according to the second turbidity, controlling the first turbidity adjusting tank to feed the coagulant of the third volume into the fourth container, and controlling the second turbidity adjusting tank to feed the flocculant of the fourth volume into the fifth container.
In another possible implementation, the first filtration unit comprises an ultrafiltration membrane, an acidity regulation tank, an oxidation-reduction potential ORP regulation tank, and a seventh vessel;
the water outlet of the coagulation sedimentation unit is communicated with the water inlet of the seventh container, the water outlet of the seventh container is communicated with the water inlet of the ultrafiltration membrane, the water outlet of the ultrafiltration membrane is communicated with the second filtering unit, and the acidity regulation tank and the ORP regulation tank are respectively communicated with the seventh container;
the acidity adjusting tank is used for introducing a third solution into the seventh container to adjust the pH value of the return liquid, the ORP adjusting tank is used for introducing a fourth solution into the seventh container to adjust the ORP value of the return liquid, and the ultrafiltration membrane is used for filtering impurities in the return liquid.
The technical scheme provided by the embodiment of the application has the beneficial effects that at least:
the application provides a processing apparatus who returns flowing back, because this processing apparatus includes the air supporting unit, softening unit, the unit is subsided to the coagulation, first filter unit, second filter unit and reverse osmosis unit, and the air supporting unit can reduce the concentration of organic matter and the concentration of microorganism in the flowing back, softening unit can reduce the scale formation ion in the flowing back through adding the detergent, the unit is subsided to the coagulation can reduce the turbidity of flowing back, first filter unit, can filter the impurity in the flowing back, second filter unit, be arranged in further filtering the scale formation ion in the flowing back, reverse osmosis unit, can reduce the degree of mineralization in the flowing back, therefore can know, this processing apparatus can reduce the concentration of organic matter in the flowing back, the concentration of microorganism, turbidity, impurity, scale formation ion and degree of mineralization, so the quality of water of the joining in marriage liquid of the fracturing fluid that obtains has been improved.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a device for processing a flow-back fluid according to an embodiment of the present application;
fig. 2 is a flowchart of a processing apparatus for a flowback liquid, according to an embodiment of the present disclosure, for processing the flowback liquid.
Reference numerals:
11. air flotation unit
12. Softening unit
13. Coagulation sedimentation unit
14. A first filter unit
15. Second filter unit
16. Reverse osmosis unit
Detailed Description
To make the objects, technical solutions and advantages of the present application more clear, embodiments of the present application will be described in further detail below with reference to the accompanying drawings.
Fig. 1 is a schematic structural diagram of a treatment apparatus for a flowback liquid according to an embodiment of the present disclosure. Referring to fig. 1, the processing apparatus includes: the device comprises an air flotation unit 11, a softening unit 12, a coagulation sedimentation unit 13, a first filtering unit 14, a second filtering unit 15 and a reverse osmosis unit 16;
the air flotation unit 11, the softening unit 12, the coagulation sedimentation unit 13, the first filtering unit 14, the second filtering unit 15 and the reverse osmosis unit 16 are communicated in sequence;
the gas floating unit 11 is used for reducing the concentration of organic matters and the concentration of microorganisms in the return liquid to be treated, the softening unit 12 is used for reducing scale forming ions in the return liquid by adding a descaling agent, the coagulating sedimentation unit 13 is used for reducing the turbidity of the return liquid by adding a turbidity reducing agent, the first filtering unit 14 is used for filtering impurities in the return liquid, the second filtering unit 15 is used for filtering the scale forming ions in the return liquid, and the reverse osmosis unit 16 is used for reducing the mineralization degree in the return liquid to obtain the liquid preparation of the fracturing liquid.
The application provides a processing apparatus who returns flowing back, because this processing apparatus includes air supporting unit 11, softening unit 12, coagulation sedimentation unit 13, first filter unit 14, second filter unit 15 and reverse osmosis unit 16, and air supporting unit 11 can reduce the concentration of organic matter and the concentration of microorganism in the flowing back, softening unit 12 can reduce the scale forming ion in the flowing back through adding the detergent, coagulation sedimentation unit 13 can reduce the turbidity of flowing back, first filter unit 14, can filter the impurity in the flowing back, second filter unit 15, be used for further filtering the scale forming ion in the flowing back, reverse osmosis unit 16, can reduce the degree of mineralization in the flowing back, therefore can know, this processing apparatus can reduce the concentration of organic matter in the flowing back, the concentration of microorganism, turbidity, impurity, scale forming ion and degree of mineralization, so the quality of water of the joining in marriage liquid of the fracturing fluid that obtains has been improved.
Introduction of the air flotation unit 11: and the air flotation unit 11 is connected with the softening unit 12 and is used for reducing the concentration of organic matters and the concentration of microorganisms in the flowback liquid to be treated.
In a possible implementation, the air floating unit 11 includes a lift pump, an air floating machine and a first container; the lift pump and the air floatation machine are respectively communicated with a water inlet of the first container, and a water outlet of the first container is communicated with a water inlet of the softening unit 12; the lifting pump is used for lifting the return liquid to the first container, and the air floatation machine is used for filling the first container with first gas and reducing the concentration of organic matters in the return liquid through the first gas; the flow-back liquid treated by the air floatation unit enters the softening unit 12 from the water outlet of the first container.
The density of the organic matter is lower than that of the flowback liquid, separation of the organic matter from the flowback liquid can be accelerated by the first gas, and the organic matter rises to the liquid surface of the flowback liquid by buoyancy, thereby reducing the concentration of the organic matter in the flowback liquid. Wherein the organic matter may be crude oil.
In a possible implementation, the air floating unit 11 further comprises a sterilization tank; the sterilizing tank is communicated with the water inlet of the first container, is used for introducing a sterilizing agent into the first container, and is used for reducing the concentration of microorganisms in the return liquid through the sterilizing agent.
Wherein, the bactericide can be an oxidant; for example, sodium hypochlorite; the sodium hypochlorite can remove Bacteria, such as SRB (Sulfate-Reducing Bacteria), TGB (Saprophytic Bacteria), FB (FB Bacteria, siderobia), etc., in the fracturing fluid, thereby Reducing the concentration of microorganisms in the flowback fluid. The concentration of the germicide may be any value between 2mg/L and 8mg/L, for example, 2mg/L, 5mg/L, 8mg/L, etc.; in the embodiment of the present application, the concentration of the bactericide is not particularly limited, and may be set and modified as needed.
The flowback liquid contains divalent iron ions, and the first gas is an oxidizing gas. The air flotation unit 11 can oxidize ferrous ions into ferric ions through oxidizing gas to form precipitates, so as to reduce the content of ferrous ions in the return liquid. Optionally, the first gas is air; and the air flotation machine is used for charging air into the first container, and oxidizing ferrous ions in the return liquid into ferric ions through the air to form precipitates.
In one possible implementation, the air flotation machine comprises an air compressor and a dissolved air tank; the air compressor is communicated with a water inlet of the first container through a dissolved air tank; the air compressor is used for compressing air into water in the air dissolving tank to form air dissolving water, the air dissolving tank is used for inputting the air dissolving water into the first container, the air in the air dissolving water is separated out in the return liquid to form air bubbles, and then ferrous ions in the return liquid are oxidized into ferric ions through the air bubbles to form precipitates, and the precipitates are carried to the surface of the return liquid. Wherein the volume of air in the dissolved air water input to the first container is related to the volume of the flowback liquid input to the first container. Optionally, the volume of the input air is any value between 2% and 5% of the volume of the input flow-back liquid; e.g., 2%, 3%, 4%, etc.
In a possible implementation manner, the air flotation unit 11 further includes a mud scraper, the mud scraper is horizontally disposed in the first container, and the height of the mud scraper matches with the liquid level of the flow-back fluid in the first container; and scraping the ferric iron ion precipitate on the surface of the flow-back liquid by a mud scraper.
Introduction of the softening unit 12: the water inlet of the softening unit 12 is communicated with the water outlet of the air flotation unit 11, and the water outlet of the softening unit 12 is communicated with the water inlet of the coagulation sedimentation unit 13. And a softening unit 12 for reducing the hardness of the flowback fluid.
In one possible implementation, the softening unit 12 includes a second vessel, a third vessel, a ph detector, a hardness detector, an alkalinity adjusting tank, and a descaling tank;
the water inlet of the second container is communicated with the water outlet of the air flotation unit 11, the water outlet of the upper portion of the second container is communicated with the water inlet of the upper portion of the third container, the water outlet of the lower portion of the third container is communicated with the water inlet of the lower portion of the coagulation sedimentation unit 13, the pH value detector is arranged in the second container, the hardness detector is arranged in the third container, the alkaline adjusting tank is communicated with the second container, and the descaling tank is communicated with the third container. The water inlet of the softening unit 12 is the same as the water inlet of the second container.
The return liquid treated by the air flotation unit 11 enters the second container through a water outlet of the air flotation unit 11 and a water inlet of the second container, and the device comprises a pH value detector for detecting the pH value of the return liquid in the second container, a hardness detector for detecting the hardness of the return liquid in the third container, an alkalinity adjusting tank for introducing a pH regulator into the second container to adjust the pH value of the return liquid, and a descaling tank for introducing a descaling agent into the third container to reduce scale forming ions in the return liquid.
Optionally, the PH detector is a PH (hydrogen ion concentration index) probe, and the hardness detector is a hardness probe. The pH regulator is sodium hydroxide (NaOH) solution, and the scale remover is sodium carbonate (Na)2CO3) And (3) solution. The concentration of the NaOH solution is related to the pH of the flowback fluid, and Na is2CO3The concentration of the solution correlates to the hardness value of the flowback fluid.
In one possible implementation, the softening unit 12 further comprises a first controller; the first controller is used for determining a first volume of an acid-base regulator and a second volume of a descaling agent which are added into the second container according to the pH value and the hardness of the return liquid, controlling the alkaline regulating tank to feed the acid-base regulator with the first volume into the second container, and controlling the descaling tank to feed the descaling agent with the second volume into the second container.
In a possible implementation, the softening unit 12 further comprises a first stirrer; and the first stirrer is arranged in the second container and is used for uniformly mixing the acid-base regulator, the descaling agent and the flowback liquid. The rotating speed of the first stirrer can be any value between 30r/min and 60 r/min; for example, 30r/min, 40r/min, 60r/min, etc.; in the embodiment of the present application, the size of the filtration pore size of the ultrafiltration membrane is not particularly limited, and may be set and modified as needed.
Optionally, the first Controller is a PLC (Programmable logic Controller) central control system. Firstly, setting the pH value of the return fluid to be a first preset value and setting the hardness of the return fluid to be a second preset value by a PLC central control system; wherein the first preset value is any value between 10 and 11.5, such as 11, and the second preset value is any value between 500mg/l and 1000mg/l, such as 800mg/l.
Then, the PLC central control system detects the pH value and the hardness in the return fluid in real time through a pH probe and a hardness probe; when the detected pH value reaches a first preset value of 11, controlling the alkaline adjusting tank to stop introducing the NaOH solution into the second container, and when the detected hardness value reaches a second preset value of 800mg/l, controlling the descaling tank to stop introducing Na into the second container2CO3And (3) solution.
The point to be noted is that after the alkaline adjusting tank is controlled by the PLC central control system to introduce the NaOH solution into the second container, the first stirrer rotates at a preset rotating speed for a first preset time period to uniformly mix the NaOH solution with the flowback liquid, so that magnesium ions in the flowback liquid form Mg (OH)2And (4) precipitating. In thatThe PLC central control system controls the hardness joint tank to feed Na into the second container2CO3After the solution, the first stirrer rotates at a preset rotation speed for a second preset time period for enabling Na2CO3The solution and the flowback liquid are mixed evenly, so that calcium ions in the flowback liquid form CaCO3And (4) precipitating.
The first preset time period and the second preset time period may be any value between 10min and 15min, for example, 10min, 12min, 15min, and the like; in the embodiment of the present application, the values of the first preset time period and the second preset time period are not specifically limited, and may be set and modified as needed.
In one possible implementation, na2CO3The concentration of the solution being CaCO in the flowback liquid30.9 to 1.1 times the concentration of (b). For example, caCO in flowback fluids3The concentration of (A) is 5mg/L; then Na is present2CO3The concentration of the solution was 5mg/L.
Introduction of the coagulation sedimentation unit 13: the water inlet of the coagulation sedimentation unit 13 is communicated with the water outlet of the softening unit 12, and the water outlet of the coagulation sedimentation unit 13 is communicated with the first filtering unit 14. And the coagulation sedimentation unit 13 is used for reducing the turbidity of the return liquid.
In one possible implementation, the coagulation sedimentation unit 13 comprises a fourth container, a fifth container, a sixth container and a turbidity regulating tank;
a water inlet at the lower part of the fourth container is communicated with a water outlet of the softening unit 12, a water outlet at the upper part of the fourth container is communicated with a water inlet at the upper part of the fifth container, a water outlet at the middle part of the fifth container is communicated with a water inlet at the middle part of the sixth container, a water outlet at the upper part of the sixth container is communicated with the first filtering unit 14, and the turbidity adjusting tank is respectively communicated with the fifth container and the sixth container;
the back flowing back after softening unit 12 handles gets into the fourth container through the delivery port of softening unit 12 and the water inlet of fourth container, and the turbidity adjusts the jar for let in the turbidity reducing agent and reduce the turbidity of back flowing back liquid in to fourth container and the fifth container, the sixth container is arranged in collecting the sediment that returns in the flowing back liquid.
In one possible implementation mode, the turbidity regulating tank comprises a first turbidity regulating tank and a second turbidity regulating tank, the turbidity reducing agent comprises a coagulant and a flocculant, and the first turbidity regulating tank and the second turbidity regulating tank are respectively communicated with the third container; the first turbidity adjusting tank is used for introducing a coagulant into the fourth container to enable small particulate matters in the return liquid to form large particulate matters; and the second turbidity adjusting tank is used for introducing a flocculating agent into the fifth container to enable large granular substances to form large flocs, so that the turbidity of the return liquid is reduced.
Optionally, the coagulant is PAC (Poly aluminum Chloride). Optionally, the flocculant is PAM (Polyacrylic amide); wherein the molecular weight of the flocculant is any value between 800 and 1500 ten thousand.
In a possible implementation manner, the coagulation sedimentation unit 13 further includes a second controller, a first turbidity detector, and a second turbidity detector; the first turbidity detector is arranged in the fourth container, and the second turbidity detector is arranged in the fifth container; the second controller is electrically connected with the first turbidity detector, the second turbidity detector, the first turbidity adjusting tank and the second turbidity adjusting tank respectively; the first turbidity detector is used for detecting the first turbidity of the return liquid in the fourth container, and the second turbidity detector is used for detecting the second turbidity of the return liquid in the fifth container; and the second controller is used for determining a third volume of coagulant to be added into the fourth container according to the first turbidity of the return liquid, determining a fourth volume of flocculant to be added into the fifth container according to the second turbidity, controlling the first turbidity adjusting tank to introduce the coagulant in the third volume into the fourth container, and controlling the second turbidity adjusting tank to introduce the flocculant in the fourth volume into the fifth container.
The concentration of the coagulant fed into the fourth vessel is related to the turbidity of the flowback liquid output by the softening unit 12; the concentration of the flocculant introduced into the fifth vessel is related to the turbidity of the flowback liquid after the coagulant is added.
It should be noted that the volume of the flow-back liquid in the fourth vessel is increased by the product of the flow rate of the flow-back liquid into the fourth vessel and the flow-in time, and the third volume of the coagulant added to the fourth vessel is the product of the flow rate of the coagulant into the fourth vessel and the flow-in time. When the increased volume of the flow-back liquid in the fourth vessel and the third volume of coagulant added are fixed, the greater the first turbidity of the flow-back liquid, the greater the concentration of coagulant needed to be added.
In one possible implementation, the second controller is configured to determine, according to the first turbidity of the return liquid, a concentration of coagulant to be added to the fourth vessel by the following formula one;
the formula I is as follows: y =0.58X +94.7; wherein Y represents the coagulant concentration and X represents the first turbidity of the flowback fluid.
It should be noted that the volume of the flow-back liquid in the fifth vessel is increased by the product of the flow rate of the flow-back liquid into the fifth vessel and the flow-in time, and the fourth volume of the flocculant added into the fifth vessel is the product of the flow rate of the coagulant into the fifth vessel and the flow-in time. When the increased volume of the flowback liquid in the fifth container and the fourth volume of the flocculant added are fixed, the greater the second turbidity of the flowback liquid, the greater the concentration of the flocculant needs to be added.
In one possible implementation, the second controller is used for determining the concentration of coagulant added into the third container according to the second turbidity of the return liquid by the following formula two;
the formula II is as follows: z =0.034X-0.017; wherein Z represents the second concentration and X represents the second turbidity of the flowback fluid.
In a possible implementation, the coagulation sedimentation unit 13 further comprises a second stirrer; the quantity of second agitator is two, and a setting is in the fourth container for make coagulant and return the flowing back homogeneous mixing, improve the speed that the small particle matter in the flowing back formed large granule material, another setting is in the fifth container, is used for making flocculating agent and return flowing back homogeneous mixing, improves the speed that the large granule material in the flowing back formed the big floc and deposits.
In one possible implementation mode, the coagulant is PAC, the flocculant is PAM, and the second controller is a PLC central control system. The PLC central control system can determine the volume of the coagulant to be added and the volume of the flocculant to be added according to the turbidity of the return liquid. The method comprises the following specific steps: firstly, a PLC central control system detects first turbidity in the return liquid through a first turbidity detector, determines a first concentration of added PAC through a formula Y =0.58X +94.7 according to the first turbidity of the return liquid, and determines a third volume of added PAC according to the first concentration of PAC and the volume of the return liquid; wherein Y represents a first concentration and X represents a first turbidity of the flowback fluid; and the PLC central control system controls the first turbidity adjusting tank to introduce PAC with a third volume into the fourth container. Then, the PLC central control system detects a second turbidity in the return liquid in the fifth container through a second turbidity detector, determines a second concentration of PAM to be added according to the second turbidity of the return liquid and a formula Z =0.034X-0.017, and determines a fourth volume of PAM to be added according to the second concentration of PAM and the volume of the return liquid; wherein Z represents a second concentration and X represents a second turbidity of the flowback fluid; and the PLC central control system controls the second turbidity adjusting tank to introduce PAM with a fourth volume into the fifth container.
The third volume of PAC is introduced into the fourth container by the first turbidity adjusting tank under the control of the PLC central control system, and the second stirrer rotates at a preset rotating speed for a third preset time period to enable small particles in the backflow liquid to form large particles through bridging and electrical neutralization. And after the PLC central control system controls the second turbidity adjusting tank to introduce PAM with a fourth volume into the fifth container, the second stirrer rotates at a preset rotating speed for a fourth preset time period to enable large-particle substances in the return liquid to form large-floc precipitates through bridging and electric neutralization. The third preset time period and the fourth preset time period may be any value between 10min and 15min, for example, 10min, 12min, 15min, and the like; in the embodiment of the present application, the values of the third preset time period and the fourth preset time period are not specifically limited, and may be set and modified as needed.
The sixth container can be an inclined plate sedimentation tank, and the return liquid in the fifth container enters the inclined plate sedimentation tank through a water inlet in the middle of the inclined plate sedimentation tank; then, standing the drainage liquid in the inclined plate sedimentation tank; the standing time is any value between 20min and 30min, such as 20min, 25min, 30min, etc. In a possible implementation mode, the bottom end of the inclined plate sedimentation tank is provided with a funnel-shaped sewage draining outlet, return liquid in the inclined plate sedimentation tank is stood, and sediment formed in the return liquid is settled to the bottom of the inclined plate sedimentation tank and is discharged through the sewage draining outlet.
Introduction to the first filter unit 14: the first filtering unit 14 is communicated with a water outlet of the coagulation sedimentation unit 13 and is used for filtering impurities in the return liquid.
In one possible implementation, the first filtration unit 14 includes an ultrafiltration membrane, an acidity-regulation tank, an ORP (oxidation-reduction potential) regulation tank, and a seventh vessel;
a water outlet of the coagulation sedimentation unit 13 is communicated with a water inlet of a seventh container, a water outlet of the seventh container is communicated with a water inlet of an ultrafiltration membrane, a water outlet of the ultrafiltration membrane is communicated with a second filtering unit, and an acidity regulation tank and an ORP regulation tank are respectively communicated with the seventh container; the acidity adjusting tank is used for introducing a third solution into the seventh container to adjust the pH value of the return liquid, the ORP adjusting tank is used for introducing a fourth solution into the seventh container to adjust the ORP value of the return liquid, and the ultrafiltration membrane is used for filtering impurities in the return liquid.
In one possible implementation, the third solution is a hydrochloric acid (HCl) solution; the fourth solution is sodium bisulfite (NaHSO)3) And (3) solution. The ultrafiltration membrane is hollow fiber type dead-end filtration, and the filtration pore diameter of the ultrafiltration membrane is any value between 0.01 μm and 0.03 μm, such as 0.01 μm, 0.015 μm, 0.02 μm and the like; in the embodiment of the present application, the size of the filtration pore size of the ultrafiltration membrane is not particularly limited, and may be set and modified as needed.
One point to be noted is that, HCl is added into a seventh container until the PH value of the return liquid is adjusted to a third preset value; adding sodium bisulfite into a seventh container until the ORP of the return liquid is adjusted to a fourth preset value; wherein the third preset value is any value between 6.5 and 7.5, such as 7, and the fourth preset value is any value between-100 mv and +100mv, such as 0mv.
In a possible implementation manner, the first filtering unit 14 further includes a scale inhibition tank, the scale inhibition tank is communicated with the seventh container, a scale inhibitor is disposed in the scale inhibition tank, and the scale forming ions in the backflow liquid are reduced by adding the scale inhibitor into the seventh container. It should be noted that the scale inhibitor may be added after the flowback liquid is treated by the ultrafiltration membrane. Correspondingly, the treatment device further comprises an eighth container, a water outlet of the ultrafiltration membrane is connected with a water inlet of the eighth container, a water outlet of the eighth container is connected with a water inlet of the second filtering unit, and the scale inhibition tank is communicated with the eighth container.
In a possible implementation manner, the scale inhibitor is a phosphorus-containing scale inhibitor, and the concentration of the phosphorus-containing scale inhibitor is any value between 20mg/L and 40 mg/L. Wherein, the phosphorus-containing scale inhibitor can be inorganic phosphorus-containing scale inhibitor, such as sodium tripolyphosphate, sodium hexametaphosphate, etc.; the phosphorus-containing scale inhibitor may also be an organic phosphorus-containing scale inhibitor, including hydroxyethylidene diphosphonic acid, polyamino polyether methylene phosphonate, etc. In the embodiment of the present application, the type of the scale inhibitor is not particularly limited, and may be set and modified as needed.
Introduction of the second filtering unit 15: and the second filtering unit 15 is used for filtering the scaling ions in the return liquid. Wherein, the scaling ions comprise at least one of calcium ions, magnesium ions, barium ions, strontium ions and carbonate ions.
In a possible implementation, the water inlet of the second filtering unit 15 is directly communicated with the water outlet of the first filtering unit 14, and the water outlet of the second filtering unit 15 is connected with the water inlet of the reverse osmosis unit 16.
In one possible implementation, the second filtering unit 15 is a rolled nanofiltration membrane. Wherein the operating pressure of the rolled nanofiltration membrane is any value between 0.1MPa and 1 MPa; for example, 0.1MPa, 0.5MPa, 0.9MPa, etc.; the water yield of the rolled nanofiltration membrane is 40-80%.
Introduction of reverse osmosis unit 16: and a water inlet of the reverse osmosis unit 16 is connected with a water outlet of the second filtering unit 15 and is used for reducing the mineralization degree in the return liquid to obtain the preparation liquid of the fracturing liquid. The degree of mineralization can be determined, among other things, by the concentration of TDS (total dissolved solids).
In one possible implementation, the reverse osmosis unit 16 is a disk-tube reverse osmosis membrane. Wherein the operating pressure of the disc-tube type reverse osmosis membrane is any value between 8MPa and 11 MPa; for example, 8MPa, 9MPa, 10MPa, etc.; the water yield of the disc-tube reverse osmosis membrane is 40-70%.
The processing flow of the apparatus for processing the flow-back liquid will be described below. Fig. 2 is a flow chart of a treatment device for the flowback liquid, which is provided according to an embodiment of the present application, for treating the flowback liquid; referring to fig. 2, the step of processing the flow-back liquid by the processing device includes:
And 202, adding a sodium hydroxide solution to adjust the pH value of the flow-back fluid to 11, and adding a sodium carbonate solution to reduce the concentration of calcium ions in the flow-back fluid.
And step 203, detecting the turbidity of the return liquid, adding a coagulant in a third volume and a flocculant in a fourth volume according to the turbidity of the return liquid, and standing for precipitation.
And 204, filtering impurities in the flow-back liquid through the first filtering unit, adding a hydrochloric acid solution to adjust the pH value of the flow-back liquid to 7, and adding a phosphorus-containing scale inhibitor.
And step 206, reducing the mineralization degree in the return liquid through a reverse osmosis unit to obtain a preparation liquid of the fracturing liquid.
The quality of the effluent water of the treatment device for the flowback fluid in the prior art is compared with the quality of the effluent water of the treatment device for the flowback fluid in the application, and the quality of the prepared fracturing fluid obtained after treatment can be improved by the treatment device in the application.
The treatment process of the treatment device for the backflow liquid in the prior art comprises the following steps: adding 300ppm of sodium hydroxide into the flow-back liquid, and adding 1500ppm of sodium carbonate into the flow-back liquid. The processing procedure of the treatment device for the backflow liquid in the application is as follows: sodium hydroxide is added to the flowback liquid in an amount to raise the pH of the flowback liquid to 10. And adding sodium carbonate into the flowback fluid, wherein the addition amount of the sodium carbonate is 1.06 times of the hardness of calcium in the flowback fluid.
Comparing the hardness of effluent quality with the PH value:
6 groups of samples are selected for comparative analysis, the 6 groups of samples are respectively treated by the treatment device in the prior art and the treatment device, the hardness and the pH value of the fracturing fluid obtained after treatment are tested, and the test results are shown in the following table 1.
TABLE 1 hardness of effluent water versus pH
The water quality analysis results in Table 1 show that the hardness of the effluent is lower than 260mg/L, while the hardness fluctuation of the effluent in the prior art is larger and is between 50 and 580 mg/L. The alkalinity of the effluent of the application is stable and ranges from 470 mg/L to 600mg/L, while the alkalinity of the effluent of the prior art is generally high and reaches up to 2000mg/L, which indicates that the sodium carbonate is added excessively. The pH value of the effluent of the application is always stable at about 10, and the pH value of the effluent in the prior art fluctuates between 8.7 and 11.65, which indicates that the addition of the sodium hydroxide is inaccurate. Therefore, the effluent quality is better and stable, and the hardness, the pH value and the alkalinity of the flowback liquid can be stably controlled.
(II) comparing the turbidity of the effluent water quality:
the 6 groups of samples were tested after being treated by the treatment device in the prior art and the coagulation sedimentation unit in the treatment device in the present application, and the test results are shown in the following table 2.
TABLE 2 turbidity comparison of effluent quality
The water quality analysis results in table 2 show that the effluent turbidity after the treatment of the present application is lower than 4NTU and can reach 1.1NTU at least, while the effluent turbidity of the prior art is greater than 10NTU and can reach more than 20NTU at most, and the effluent turbidity fluctuation is large. Therefore, the water quality of the effluent of the application is better and stable.
And (III) comparing the turbidity, the hardness and the alkalinity of the effluent quality:
in the embodiment of the present application, after passing through the coagulation sedimentation unit, the flowback liquid continues to pass through the first filtering unit and the second filtering unit for treatment, and the results are shown in table 3 below compared with the effluent quality of the prior art and the effluent quality of the present application.
TABLE 3 quality of effluent of the prior art and effluent quality comparative analysis of the present application
The water quality analysis results in Table 3 show that the turbidity of the flowback liquid after being treated by the coagulation sedimentation unit, the first filtering unit and the second filtering unit is basically 0.2NTU or less, the hardness is within 100mg/l, and the alkalinity is within 250 mg/l. From this, it can be seen that the water quality of the prepared fracturing fluid obtained by the treatment apparatus of the present application is good and stable because the small particulate matter, colloid, and scale-forming ions in the flowback fluid are further removed.
The quality of raw water of the flowback fluid and the quality of the prepared fracturing fluid obtained after the treatment of the treatment device are compared and analyzed with the fracturing fluid quality standard (NB/T14002.3-2015), so that the quality of the prepared fracturing fluid obtained after the treatment of the treatment device can meet the fracturing fluid quality standard. The comparative analysis results are shown in table 4 below.
TABLE 4 analysis of quality of flow-back raw water and reverse osmosis membrane effluent
The water quality analysis result in table 4 shows that the quality of water of the joining in marriage liquid of the fracturing fluid that obtains after the processing apparatus of this application handles can satisfy fracturing fluid water quality standard.
The above description is only exemplary of the present application and should not be taken as limiting, as any modification, equivalent replacement, or improvement made within the spirit and principle of the present application should be included in the protection scope of the present application.
Claims (10)
1. A treatment device for flowback liquid, comprising: the device comprises an air flotation unit (11), a softening unit (12), a coagulation sedimentation unit (13), a first filtering unit (14), a second filtering unit (15) and a reverse osmosis unit (16);
the air flotation unit (11), the softening unit (12), the coagulation sedimentation unit (13), the first filtering unit (14), the second filtering unit (15) and the reverse osmosis unit (16) are communicated in sequence;
the device comprises an air flotation unit (11) used for reducing the concentration of organic matters and the concentration of microorganisms in the return liquid to be treated, a softening unit (12) used for reducing scale forming ions in the return liquid by adding a descaling agent, a coagulation sedimentation unit (13) used for reducing the turbidity of the return liquid by adding a turbidity reducing agent, a first filtering unit (14) used for filtering impurities in the return liquid, a second filtering unit (15) used for filtering the scale forming ions in the return liquid, and a reverse osmosis unit (16) used for reducing the mineralization degree in the return liquid to obtain the liquid preparation of the fracturing liquid.
2. The processing apparatus according to claim 1, wherein the air flotation unit (11) comprises a lift pump, an air flotation machine and a first container;
the lifting pump and the air floatation machine are respectively communicated with a water inlet of the first container, and a water outlet of the first container is communicated with a water inlet of the softening unit (12);
the lift pump is used for lifting the flowback liquid to the first container, and the air floatation machine is used for filling first gas into the first container and reducing the concentration of organic matters in the flowback liquid through the first gas.
3. The processing apparatus of claim 2, wherein the air flotation machine comprises an air compressor and a dissolved air tank;
the air compressor is communicated with the water inlet of the first container through the dissolved air tank;
the air compressor is used for compressing air into water in the air dissolving tank to form air dissolving water, the air dissolving tank is used for inputting the air dissolving water into the first container, and ferrous ions in the backflow liquid are oxidized into ferric ions through the air in the air dissolving water to form precipitates.
4. The processing device according to claim 2, characterized in that said air-flotation unit (11) further comprises a sterilization tank;
the sterilizing tank is communicated with the water inlet of the first container and is used for introducing sterilizing agent into the first container, and the concentration of microorganisms in the flowback liquid is reduced through the sterilizing agent.
5. The processing apparatus according to claim 1, wherein the softening unit (12) comprises a second vessel, a third vessel, a pH value detector, a hardness detector, an alkaline adjusting tank, and a descaling tank;
the water inlet of the second container is communicated with the water outlet of the air flotation unit (11), the water outlet of the upper part of the second container is communicated with the water inlet of the upper part of the third container, the water outlet of the lower part of the third container is communicated with the water inlet of the lower part of the coagulation sedimentation unit (13), the pH value detector is arranged in the second container, the hardness detector is arranged in the third container, the alkaline adjusting tank is communicated with the second container, and the descaling tank is communicated with the third container;
the backflow liquid treated by the air floatation unit (11) enters the second container through a water outlet of the air floatation unit (11) and a water inlet of the second container, the pH value detector is used for detecting the pH value of the backflow liquid in the second container, the hardness detector is used for detecting the hardness of the backflow liquid in the third container, the alkalinity adjusting tank is used for introducing an acid-base adjusting agent into the second container to adjust the pH value of the backflow liquid, and the descaling tank is used for introducing a descaling agent into the third container to reduce scale forming ions in the backflow liquid.
6. The processing apparatus according to claim 5, wherein the softening unit (12) further comprises a first controller;
the first controller is used for determining a first volume of the acid-base regulator and a second volume of the descaling agent which are added into the second container according to the pH value and the hardness of the return liquid, controlling the alkaline regulating tank to feed the acid-base regulator with the first volume into the second container, and controlling the descaling tank to feed the descaling agent with the second volume into the third container.
7. The processing plant according to claim 1, characterized in that the coagulation sedimentation unit (13) comprises a fourth vessel, a fifth vessel, a sixth vessel and a turbidity regulating tank;
a water inlet at the lower part of the fourth container is communicated with a water outlet of the softening unit (12), a water outlet at the upper part of the fourth container is communicated with a water inlet at the upper part of the fifth container, a water outlet at the middle part of the fifth container is communicated with a water inlet at the middle part of the sixth container, a water outlet at the upper part of the sixth container is communicated with the first filtering unit (14), and the turbidity adjusting tank is respectively communicated with the fifth container and the sixth container;
the returned liquid treated by the softening unit (12) enters the fourth container through a water outlet of the softening unit (12) and a water inlet of the fourth container, the turbidity adjusting tank is used for introducing a turbidity reducing agent into the fourth container and the fifth container to reduce the turbidity of the returned liquid, and the sixth container is used for collecting precipitates in the returned liquid.
8. The processing apparatus according to claim 7, wherein the turbidity adjusting tanks include a first turbidity adjusting tank and a second turbidity adjusting tank, the turbidity reducing agent includes a coagulant and a flocculant, the first turbidity adjusting tank is in communication with the fourth vessel, and the second turbidity adjusting tank is in communication with the fifth vessel;
the first turbidity adjusting tank is used for introducing a coagulant into the fourth container to enable small particulate matters in the return liquid to form large particulate matters; and the second turbidity adjusting tank is used for introducing a flocculating agent into the fifth container to enable large granular substances to form large flocs, so that the turbidity of the return liquid is reduced.
9. The processing apparatus according to claim 8, wherein the coagulation sedimentation unit (13) further comprises a second controller, a first turbidity detector and a second turbidity detector;
the first turbidity detector is arranged in the fourth container, the second turbidity detector is arranged in the fifth container, and the second controller is respectively and electrically connected with the first turbidity detector, the second turbidity detector, the first turbidity adjusting tank and the second turbidity adjusting tank;
the first turbidity detector is used for detecting a first turbidity of the return liquid in the fourth container, the second turbidity detector is used for detecting a second turbidity of the return liquid in the fifth container, the second controller is used for determining a third volume of the coagulant added into the fourth container according to the first turbidity, determining a fourth volume of the flocculant added into the fifth container according to the second turbidity, controlling the first turbidity adjusting tank to feed the coagulant of the third volume into the fourth container, and controlling the second turbidity adjusting tank to feed the flocculant of the fourth volume into the fifth container.
10. The treatment plant according to claim 1, wherein the first filtration unit (14) comprises an ultrafiltration membrane, an acidity regulation tank, an oxidation-reduction potential ORP regulation tank, and a seventh vessel;
a water outlet of the coagulation sedimentation unit (13) is communicated with a water inlet of the seventh container, a water outlet of the seventh container is communicated with a water inlet of the ultrafiltration membrane, a water outlet of the ultrafiltration membrane is communicated with the second filtering unit (15), and the acidity regulation tank and the ORP regulation tank are respectively communicated with the seventh container;
the acidity adjusting tank is used for introducing a third solution into the seventh container to adjust the pH value of the return liquid, the ORP adjusting tank is used for introducing a fourth solution into the seventh container to adjust the ORP value of the return liquid, and the ultrafiltration membrane is used for filtering impurities in the return liquid.
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