CN115259429B - Treatment device for flowback fluid - Google Patents
Treatment device for flowback fluid Download PDFInfo
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- CN115259429B CN115259429B CN202110482804.XA CN202110482804A CN115259429B CN 115259429 B CN115259429 B CN 115259429B CN 202110482804 A CN202110482804 A CN 202110482804A CN 115259429 B CN115259429 B CN 115259429B
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- 239000012530 fluid Substances 0.000 title claims abstract description 191
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 140
- 238000001914 filtration Methods 0.000 claims abstract description 71
- 239000007788 liquid Substances 0.000 claims abstract description 54
- 238000004062 sedimentation Methods 0.000 claims abstract description 51
- 238000005345 coagulation Methods 0.000 claims abstract description 33
- 230000015271 coagulation Effects 0.000 claims abstract description 33
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 28
- 150000002500 ions Chemical class 0.000 claims abstract description 23
- 239000012535 impurity Substances 0.000 claims abstract description 15
- 244000005700 microbiome Species 0.000 claims abstract description 15
- 230000033558 biomineral tissue development Effects 0.000 claims abstract description 12
- 230000001112 coagulating effect Effects 0.000 claims abstract description 11
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 10
- 239000000701 coagulant Substances 0.000 claims description 27
- 239000012528 membrane Substances 0.000 claims description 25
- 230000001105 regulatory effect Effects 0.000 claims description 24
- 238000000108 ultra-filtration Methods 0.000 claims description 18
- 230000001276 controlling effect Effects 0.000 claims description 14
- 239000013049 sediment Substances 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 7
- 229910001448 ferrous ion Inorganic materials 0.000 claims description 7
- 239000003206 sterilizing agent Substances 0.000 claims description 7
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 6
- 229910001447 ferric ion Inorganic materials 0.000 claims description 6
- 230000001954 sterilising effect Effects 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 5
- 238000001556 precipitation Methods 0.000 claims description 5
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 4
- 238000011049 filling Methods 0.000 claims description 4
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 239000008394 flocculating agent Substances 0.000 claims description 3
- 230000033116 oxidation-reduction process Effects 0.000 claims description 3
- 238000012545 processing Methods 0.000 abstract description 12
- 238000005188 flotation Methods 0.000 abstract description 11
- 239000010865 sewage Substances 0.000 abstract description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 30
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 12
- 239000002455 scale inhibitor Substances 0.000 description 11
- 239000007789 gas Substances 0.000 description 10
- 239000005416 organic matter Substances 0.000 description 9
- 229920002401 polyacrylamide Polymers 0.000 description 8
- 241000894006 Bacteria Species 0.000 description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical group [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 6
- 239000011574 phosphorus Substances 0.000 description 6
- 229910052698 phosphorus Inorganic materials 0.000 description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000000523 sample Substances 0.000 description 4
- 238000007790 scraping Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- 238000010835 comparative analysis Methods 0.000 description 3
- 238000009472 formulation Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 230000000844 anti-bacterial effect Effects 0.000 description 2
- 239000003899 bactericide agent Substances 0.000 description 2
- 230000003750 conditioning effect Effects 0.000 description 2
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 2
- 239000004289 sodium hydrogen sulphite Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- BAERPNBPLZWCES-UHFFFAOYSA-N (2-hydroxy-1-phosphonoethyl)phosphonic acid Chemical compound OCC(P(O)(O)=O)P(O)(O)=O BAERPNBPLZWCES-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 241000295146 Gallionellaceae Species 0.000 description 1
- TTZMPOZCBFTTPR-UHFFFAOYSA-N O=P1OCO1 Chemical compound O=P1OCO1 TTZMPOZCBFTTPR-UHFFFAOYSA-N 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 150000001408 amides Chemical class 0.000 description 1
- 229910001422 barium ion Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 230000002070 germicidal effect Effects 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 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
- 229910001427 strontium ion Inorganic materials 0.000 description 1
- 239000001577 tetrasodium phosphonato phosphate Substances 0.000 description 1
Classifications
-
- 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
-
- 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]
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/11—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
Abstract
The application provides a flow-back liquid treatment device, belongs to sewage treatment technical field. The processing device comprises: 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 floatation unit, a softening unit, a coagulating sedimentation unit, a first filtering unit, a second filtering unit and a reverse osmosis unit, wherein the air floatation unit is used for reducing the concentration of organic matters and the concentration of microorganisms in a flowback fluid to be treated, the softening unit is used for reducing scale forming ions in the flowback fluid by adding a scale remover, the coagulating sedimentation unit is used for reducing the turbidity of the flowback fluid by adding a turbidity reducing agent, the first filtering unit is used for filtering impurities in the flowback fluid, the second filtering unit is used for filtering scale forming ions in the flowback fluid, and the reverse osmosis unit is used for reducing the mineralization degree in the flowback fluid to obtain the fracturing fluid. The treatment device can reduce the concentration of organic matters, the concentration of microorganisms, turbidity, impurities, scale forming ions and mineralization degree in the flowback fluid, so that the water 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 flowback liquid.
Background
Hydraulic fracturing is currently an important technique to enhance shale gas recovery from reservoirs. In the hydraulic fracturing of a reservoir, a large amount of impurities such as sludge, suspended solids, and organic matter 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 reuse the flowback fluid.
In the related art, the treatment device of the flowback fluid comprises a coagulation sedimentation unit; and reducing the turbidity of the flowback fluid through a coagulation sedimentation unit to obtain the preparation liquid of the fracturing fluid. However, the treatment apparatus in the above-mentioned related art can only reduce the turbidity of the flowback fluid, but the water quality requirement of the fracturing fluid formulation includes not only the turbidity requirement but also other requirements such as resistance reduction, and the reduction of the turbidity of the flowback fluid alone cannot satisfy the water quality requirement of the fracturing fluid formulation, so the water quality of the fracturing fluid formulation obtained by the flowback fluid treatment apparatus is poor.
Disclosure of Invention
The embodiment of the application provides a treatment device for flowback fluid, which can improve the quality of the prepared liquid of fracturing fluid obtained after flowback fluid treatment. The technical scheme is as follows:
the application provides a processing apparatus of flowing back returns, 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 floatation unit, the softening unit, the coagulation sedimentation unit, the first filtering unit, the second filtering unit and the reverse osmosis unit are sequentially communicated;
the device comprises an air floatation unit, a softening unit, a coagulation sedimentation unit, a first filtering unit, a second filtering unit and a reverse osmosis unit, wherein the air floatation unit is used for reducing the concentration of organic matters and the concentration of microorganisms in a flowback fluid to be treated, the softening unit is used for reducing scale forming ions in the flowback fluid through adding a scale remover, the coagulation sedimentation unit is used for reducing the turbidity of the flowback fluid through adding a turbidity reducing agent, the first filtering unit is used for filtering impurities in the flowback fluid, the second filtering unit is used for filtering the scale forming ions in the flowback fluid, and the reverse osmosis unit is used for reducing the mineralization degree in the flowback fluid to obtain the distribution liquid of the fracturing fluid.
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 the water inlet of the first container, and the water outlet of the first container is communicated with the water inlet of the softening unit;
the lifting pump is used for lifting the flowback liquid to the first container, the air floatation machine is used for filling first gas into the first container, and the concentration of organic matters in the flowback liquid is reduced through the first gas.
In another possible implementation, 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 fluid is reduced through the sterilizing agent.
In another possible implementation, the air floatation machine includes 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 dissolved air tank to form dissolved air water, the dissolved air tank is used for inputting the dissolved air water into the first container, and ferrous ions in the flowback fluid are oxidized into ferric ions through the air in the dissolved air water to form precipitation.
In another possible implementation, the softening unit includes a second container, a third container, a ph detector, a hardness detector, an alkaline conditioning 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 regulating tank is communicated with the second container, and the descaling tank is communicated with the third container;
The device comprises an air flotation unit, a second container, a pH value detector, a hardness detector, an alkaline adjusting tank, a descaling tank and a scale remover, wherein the flowback liquid treated by the air flotation unit enters the second container through a water outlet of the air flotation unit and a water inlet of the second container, the pH value detector is used for detecting the pH value of the flowback liquid in the second container, the hardness detector is used for detecting the hardness of the flowback liquid in the third container, the alkaline adjusting tank is used for introducing an acid-base regulator into the second container to adjust the pH value of the flowback liquid, and the scale remover is used for introducing a scale remover into the third container to reduce scale-forming ions in the flowback 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 added into the second container according to the pH value and the hardness of the flowback fluid, controlling the alkaline regulating tank to introduce the acid-base regulator of the first volume into the second container, and controlling the descaling tank to introduce the descaling agent of the second volume into the third container.
In another possible implementation, the coagulation sedimentation unit includes a fourth vessel, a fifth vessel, a sixth vessel, and a turbidity adjustment tank;
The water inlet at the lower part of the fourth container is communicated with the water outlet of the softening unit, the water outlet at the upper part of the fourth container is communicated with the water inlet at the upper part of the fifth container, the water outlet at the middle part of the fifth container is communicated with the water inlet at the middle part of the sixth container, the 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 flowback liquid treated by the softening unit enters the fourth container through the water outlet of the softening unit and the water inlet of the fourth container, the turbidity adjusting tank is used for introducing turbidity reducing agent into the fourth container and the fifth container to reduce the turbidity of the flowback liquid, and the sixth container is used for collecting sediment in the flowback liquid.
In another possible implementation, the turbidity adjustment tank includes a first turbidity adjustment tank and a second turbidity adjustment tank, the turbidity reducing agent includes a coagulant and a flocculant, the first turbidity adjustment tank is in communication with the fourth container, and the second turbidity adjustment 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 flowback fluid to form large particulate matters; and the second turbidity adjusting tank is used for introducing a flocculating agent into the fifth container to enable the large granular substances to form large flocs so as to reduce the turbidity of the flowback fluid.
In another possible implementation, 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 the first turbidity of the flowback liquid in the fourth container, the second turbidity detector is used for detecting the second turbidity of the flowback liquid in the fifth container, the second controller is used for determining the third volume of the coagulant added into the fourth container according to the first turbidity, determining the fourth volume of the flocculant added into the fifth container according to the second turbidity, and controlling the first turbidity adjusting tank to introduce the third volume of the coagulant into the fourth container and controlling the second turbidity adjusting tank to introduce the fourth volume of the flocculant into the fifth container.
In another possible implementation, the first filtration unit comprises an ultrafiltration membrane, an acidity adjustment tank, an oxidation-reduction potential ORP adjustment 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 filtration unit, and the acid regulating tank and the ORP regulating tank are respectively communicated with the seventh container;
the acid regulating tank is used for introducing a third solution into the seventh container to regulate the pH value of the flowback fluid, the ORP regulating tank is used for introducing a fourth solution into the seventh container to regulate the ORP value of the flowback fluid, and the ultrafiltration membrane is used for filtering impurities in the flowback fluid.
The beneficial effects of the technical scheme provided by the embodiment of the application at least comprise:
the application provides a processing apparatus of flowing back, because this processing apparatus includes air supporting unit, softening unit, coagulating sedimentation unit, 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, the softening unit can reduce the scale ion that becomes in the flowing back through adding the detergent, coagulating sedimentation unit can reduce the turbidity of flowing back, first filter unit, can filter the impurity in the flowing back, the second filter unit for further filter the scale ion in the flowing back, reverse osmosis unit can reduce the mineralization degree in the flowing back, from this, this processing apparatus can reduce the concentration of organic matter in the flowing back, the concentration of microorganism, turbidity, impurity, scale ion and mineralization degree, so improved the quality of water of the joining in marriage liquid of the fracturing fluid that obtains.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic view of a flow-back fluid treatment apparatus according to an embodiment of the present application;
fig. 2 is a flowchart of a flow-back fluid treatment device for treating a flow-back fluid according to an embodiment of the present application.
Reference numerals:
11. air floatation unit
12. Softening unit
13. Coagulation sedimentation unit
14. First filter unit
15. Second filter unit
16. Reverse osmosis unit
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present application more apparent, the 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 flow-back fluid treatment device according to an embodiment of the present application. Referring to fig. 1, the processing apparatus includes: an air floatation 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 floatation 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 sequentially communicated;
the device comprises an air floatation unit 11, a softening unit 12, a coagulating sedimentation unit 13, a first filtering unit 14, a second filtering unit 15, a reverse osmosis unit 16 and a fracturing fluid, wherein the air floatation unit is used for reducing the concentration of organic matters and the concentration of microorganisms in a flowback fluid to be treated, the softening unit 12 is used for reducing scale forming ions in the flowback fluid by adding a scale remover, the coagulating sedimentation unit 13 is used for reducing the turbidity of the flowback fluid by adding a turbidity reducer, the first filtering unit 14 is used for filtering impurities in the flowback fluid, the second filtering unit 15 is used for filtering the scale forming ions in the flowback fluid, and the reverse osmosis unit 16 is used for reducing the mineralization degree in the flowback fluid to obtain the fracturing fluid.
The application provides a treatment device of flow-back fluid, because the treatment device includes air supporting unit 11, softening unit 12, coagulating 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 flow-back fluid, softening unit 12 can reduce the scale ion in the flow-back fluid through adding the scale remover, coagulating sedimentation unit 13 can reduce the turbidity of the flow-back fluid, first filter unit 14 can filter the impurity in the flow-back fluid, second filter unit 15, be used for further filtering the scale ion in the flow-back fluid, reverse osmosis unit 16 can reduce the mineralization degree in the flow-back fluid, from this, this treatment device can reduce the concentration of organic matter in the flow-back fluid, the concentration of microorganism, turbidity, impurity, scale ion and mineralization degree, so the quality of the liquid of the fracturing fluid that has improved.
Introduction of the air-floatation unit 11: an air floatation unit 11 connected with the softening unit 12 for reducing the concentration of organic matters and microorganisms in the flowback fluid to be treated.
In one possible implementation, 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 the water inlet of the first container, and the water outlet of the first container is communicated with the water inlet of the softening unit 12; the lifting 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; the flowback fluid treated by the air floatation unit enters the softening unit 12 from the water outlet of the first container.
The concentration of the organic matter in the flowback fluid is reduced by the fact that the first gas accelerates the separation of the organic matter from the flowback fluid and the organic matter is raised to the liquid surface of the flowback fluid by buoyancy. Wherein the organic matter may be crude oil.
In one possible implementation, the air-bearing unit 11 further comprises a sterilizing tank; the sterilization tank is communicated with the water inlet of the first container, is used for introducing the sterilizing agent into the first container, and is used for reducing the concentration of microorganisms in the flowback fluid through the sterilizing agent.
Wherein the bactericide may be an oxidizing agent; for example, sodium hypochlorite; sodium hypochlorite can remove Bacteria in the fracturing fluid, such as SRB (Sulfate-Reducing Bacteria, sulfate reducing Bacteria), TGB (Saprophytic Bacteria, saprophytes), FB (FB Bacteria, iron Bacteria), etc., 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 ferrous ions, and the first gas is an oxidizing gas. The air flotation unit 11 can oxidize ferrous ions to ferric ions by an oxidizing gas to form a precipitate, thereby reducing the content of ferrous ions in the flowback fluid. Optionally, the first gas is air; and the air floatation machine is used for filling air into the first container, and oxidizing ferrous ions in the flowback fluid into ferric ions through the air to form a precipitate.
In one possible implementation, the air floatation machine includes 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 dissolved air tank to form dissolved air water, the dissolved air tank is used for inputting the dissolved air water into the first container, the air in the dissolved air water is separated out in the flowback fluid to form air bubbles, and ferrous ions in the flowback fluid are oxidized into ferric ions through the air bubbles to form sediment, and the sediment is carried to the surface of the flowback fluid. Wherein the volume of air in the dissolved air water input to the first container is related to the volume of the flowback fluid 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 flowback fluid; for example, 2%, 3%, 4%, etc.
In a possible implementation manner, the air-floating unit 11 further comprises a mud scraping plate, wherein the mud scraping plate is horizontally arranged in the first container, and the height of the mud scraping plate is matched with the liquid level of the flowback fluid in the first container; and scraping ferric ion sediment on the surface of the flowback fluid through a scraper.
Introduction of softening unit 12: the water inlet of the softening unit 12 is communicated with the water outlet of the air floatation unit 11, and the water outlet of the softening unit 12 is communicated with the water inlet of the coagulation sedimentation unit 13. Softening unit 12 for reducing the hardness of the flowback fluid.
In one possible implementation, softening unit 12 comprises a second vessel, a third vessel, a ph detector, a hardness detector, an alkaline conditioning tank, and a descaling tank;
the water inlet of the second container is communicated with the water outlet of the air floatation 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 water inlet of the softening unit 12 is the same as the water inlet of the second container.
The flow-back liquid treated by the air floatation unit 11 enters the second container through the water outlet of the air floatation unit 11 and the water inlet of the second container, and the pH value detector is used for detecting the pH value of the flow-back liquid in the second container, the hardness detector is used for detecting the hardness of the flow-back liquid in the third container, the alkaline regulating tank is used for introducing an acid-base regulator into the second container to regulate the pH value of the flow-back liquid, and the descaling tank is used for introducing a descaling agent into the third container to reduce scale-forming ions in the flow-back liquid.
Optionally, the pH detector is a pH (hydrogen ion concentration, hydrogen ion concentration index) probe, and the hardness detector is a hardness probe. The acid-base regulator is sodium hydroxide (NaOH) solution, and the scale remover is sodium carbonate (Na) 2 CO 3 ) A solution. Note that, the concentration of NaOH solution was related to the pH of the flowback fluid, na 2 CO 3 The concentration of the solution is related to the hardness value of the flowback fluid.
In one possible implementation, softening unit 12 further comprises a first controller; and the first controller is used for determining the first volume of the acid-base regulator and the second volume of the descaling agent added into the second container according to the pH value and the hardness of the flowback fluid, controlling the alkaline regulating tank to introduce the first volume of the acid-base regulator into the second container, and controlling the descaling tank to introduce the second volume of the descaling agent into the second container.
In one possible implementation, softening unit 12 further comprises a first stirrer; the first stirrer is arranged in the second container and is used for uniformly mixing the acid-base regulator, the scale remover and the flowback liquid. The rotational speed of the first stirrer may 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 diameter 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, programmable controller) central control system. Firstly, setting the pH value of the flowback fluid as a first preset value and setting the hardness of the flowback fluid as a second preset value by a PLC central control system; wherein the first preset value is any value between 10 and 11.5, e.g. 11, and the second preset value is any value between 500mg/l and 1000mg/l, e.g. 800mg/l.
Then, the PLC central control system detects the pH value and the hardness in the flowback fluid in real time through a pH probe and a hardness probe; when the detected pH value reaches a first preset value 11, controlling the alkaline regulating tank to stop introducing NaOH solution into the second container, and when the detected hardness value reaches a second preset value 800mg/l, controlling the descaling tank to stop introducing Na into the second container 2 CO 3 A solution.
It is to be noted that after the PLC central control system controls the alkaline regulating tank to introduce NaOH solution into the second container, the first stirrer rotates for a first preset time period at a preset rotation speed for uniformly mixing the NaOH solution and the flowback fluid, so that magnesium ions in the flowback fluid form Mg (OH) 2 And (5) precipitation. The PLC central control system controls the hardness section tank to introduce Na into the second container 2 CO 3 After the solution, the first stirrer rotates at a preset rotation speed for a second preset period of time for Na 2 CO 3 The solution is uniformly mixed with the flowback fluid, so that calcium ions in the flowback fluid form CaCO 3 And (5) precipitation.
Wherein, the first preset time period and the second preset time period can be any value between 10min and 15min, for example, 10min, 12min, 15min and the like; in this embodiment of the present application, the values of the first preset duration and the second preset duration are not specifically limited, and may be set and modified as needed.
In one possible implementation, na 2 CO 3 The concentration of the solution is CaCO in the flowback fluid 3 From 0.9 to 1.1 times the concentration of (c). For example CaCO in flowback fluid 3 Is 5mg/L; na is then 2 CO 3 The concentration of the solution was 5mg/L.
Introduction of 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 a coagulation sedimentation unit 13 for reducing turbidity of the flowback fluid.
In one possible implementation, the coagulation sedimentation unit 13 comprises a fourth vessel, a fifth vessel, a sixth vessel and a turbidity adjustment tank;
the water inlet at the lower part of the fourth container is communicated with the water outlet of the softening unit 12, the water outlet at the upper part of the fourth container is communicated with the water inlet at the upper part of the fifth container, the water outlet at the middle part of the fifth container is communicated with the water inlet at the middle part of the sixth container, the 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 flowback liquid treated by the softening unit 12 enters the fourth container through the water outlet of the softening unit 12 and the water inlet of the fourth container, the turbidity adjusting tank is used for introducing turbidity reducing agent into the fourth container and the fifth container to reduce the turbidity of the flowback liquid, and the sixth container is used for collecting sediment in the flowback liquid.
In one possible implementation, the turbidity adjustment tank comprises a first turbidity adjustment tank and a second turbidity adjustment tank, the turbidity reducing agent comprises a coagulant and a flocculant, and the first turbidity adjustment tank and the second turbidity adjustment tank are respectively communicated with the third container; the first turbidity adjusting tank is used for introducing coagulant into the fourth container to enable small particulate matters in the flowback fluid to form large particulate matters; and the second turbidity adjusting tank is used for introducing flocculating agent into the fifth container to enable the large-particle substances to form large flocs so as to reduce the turbidity of the flowback fluid.
Optionally, the coagulant is PAC (Poly Aluminium Chloride, polyaluminum oxide). Optionally, the flocculant is PAM (Polyacrylic amide, cationic polyacrylamide); wherein the molecular weight of the flocculant is any value between 800 ten thousand and 1500 ten thousand.
In one possible implementation, 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, and the second turbidity detector is arranged in the fifth container; 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; a first turbidity detector for detecting a first turbidity of the flowback fluid in the fourth container, and a second turbidity detector for detecting a second turbidity of the flowback fluid in the fifth container; and the second controller is used for determining a third volume of coagulant added into the fourth container according to the first turbidity of the flowback liquid, determining a fourth volume of flocculant added into the fifth container according to the second turbidity, controlling the first turbidity adjusting tank to introduce the third volume of coagulant into the fourth container, and controlling the second turbidity adjusting tank to introduce the fourth volume of flocculant into the fifth container.
Note that the concentration of the coagulant introduced into the fourth container is related to the turbidity of the flowback fluid output from the softening unit 12; the concentration of the flocculant introduced into the fifth container is related to the turbidity of the flowback fluid after the coagulant is added.
In another point, the volume of the flow-back liquid in the fourth container is the product of the flow rate of the flow-back liquid into the fourth container and the inflow time, and the third volume of the coagulant added to the fourth container is the product of the flow rate of the coagulant into the fourth container and the inflow time. When the volume of the flowback liquid in the fourth container is increased and the third volume of the coagulant is added is fixed, the higher the first turbidity of the flowback liquid is, the higher the concentration of the coagulant to be added is.
In one possible implementation, the second controller is configured to determine, according to the first turbidity of the flowback fluid, a concentration of the coagulant added to the fourth container by the following formula one;
equation one: y=0.58x+94.7; wherein Y represents the concentration of the coagulant, and X represents the first turbidity of the flowback fluid.
In another point, the volume of the flow-back liquid in the fifth container is the product of the flow rate of the flow-back liquid into the fifth container and the inflow time, and the fourth volume of the flocculant added to the fifth container is the product of the flow rate of the coagulant into the fifth container and the inflow time. When the volume of the flowback fluid in the fifth container is increased and the fourth volume of the flocculant is added is fixed, the greater the second turbidity of the flowback fluid, the greater the concentration of the flocculant to be added is required.
In one possible implementation, the second controller is configured to determine, according to the second turbidity of the flowback fluid, a concentration of the coagulant added to the third container by the following formula two;
formula II: z=0.034x-0.017; wherein Z represents the second concentration and X represents the second turbidity of the flowback fluid.
In one possible implementation, the coagulation sedimentation unit 13 further comprises a second stirrer; the number of the second agitators is two, one agitators is arranged in the fourth container and used for uniformly mixing the coagulant with the flowback fluid, so that the speed of forming large granular matters by small granular matters in the flowback fluid is improved, and the other agitators is arranged in the fifth container and used for uniformly mixing the flocculant with the flowback fluid, so that the speed of forming large floc sediment by the large granular matters in the flowback fluid is improved.
In one possible implementation, 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 flowback fluid. The method comprises the following specific steps: firstly, detecting first turbidity in a flowback fluid by a PLC central control system through a first turbidity detector, determining first concentration of added PAC according to the first turbidity of the flowback fluid through a formula Y=0.58X+94.7, and determining third volume of added PAC according to the first concentration of PAC and the volume of the flowback fluid; wherein Y represents a first concentration, and X represents a first turbidity of the flowback fluid; the PLC central control system controls the first turbidity adjusting tank to be filled with PAC with a third volume into the fourth container. Then, the PLC central control system detects the second turbidity in the flowback fluid in the fifth container through a second turbidity detector, determines the second concentration of the added PAM according to the second turbidity of the flowback fluid through a formula Z=0.034X-0.017, and determines the fourth volume of the added PAM according to the second concentration of the PAM and the volume of the flowback fluid; 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 regulating tank to introduce the fourth volume of PAM into the fifth container.
The point is that after the PLC central control system controls the first turbidity adjusting tank to introduce the PAC with the third volume into the fourth container, the second stirrer rotates for a third preset time period according to a preset rotating speed, so that small particulate matters in the flowback fluid are formed into large particulate matters through bridging and electric neutralization. After the PLC central control system controls the second turbidity adjusting tank to introduce a fourth volume of PAM into the fifth container, the second stirrer rotates for a fourth preset time period according to a preset rotating speed, and the second stirrer is used for forming large floc sediment by bridging and electric neutralization of large granular substances in the flowback fluid. Wherein the third preset time period and the fourth preset time period may be any value between 10min and 15min, for example, 10min, 12min, 15min, etc.; in this embodiment of the present application, the values of the third preset duration and the fourth preset duration are not specifically limited, and may be set and modified as needed.
The sixth container can be an inclined plate sedimentation tank, and the flowback fluid 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 flowback liquid in the inclined plate sedimentation tank; the rest time is any value between 20min and 30min, such as 20min, 25min, 30min, etc. In one possible implementation manner, a funnel-shaped sewage drain is arranged at the bottom end of the inclined plate sedimentation tank, the flowback liquid in the inclined plate sedimentation tank is kept stand, and sediment formed in the flowback liquid is settled to the bottom of the inclined plate sedimentation tank and is discharged through the sewage drain.
Introduction of the first filter unit 14: the first filtering unit 14 is communicated with the water outlet of the coagulating sedimentation unit 13 and is used for filtering impurities in the flowback fluid.
In one possible implementation, the first filtration unit 14 includes an ultrafiltration membrane, an acidity adjustment tank, an ORP (oxidation-reduction potential) adjustment tank, and a seventh vessel;
the water outlet of the coagulation sedimentation unit 13 is communicated with the water inlet of a seventh container, the water outlet of the seventh container is communicated with the water inlet of an ultrafiltration membrane, the water outlet of the ultrafiltration membrane is communicated with a second filtration unit, and the acid regulating tank and the ORP regulating tank are respectively communicated with the seventh container; the acid regulating tank is used for introducing a third solution into the seventh container to regulate the pH value of the flowback fluid, the ORP regulating tank is used for introducing a fourth solution into the seventh container to regulate the ORP value of the flowback fluid, and the ultrafiltration membrane is used for filtering impurities in the flowback fluid.
In one possible implementation, the third solution is a hydrochloric acid (HCl) solution; the fourth solution is sodium bisulphite (NaHSO) 3 ) A 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, for example, 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 diameter of the ultrafiltration membrane is not particularly limited, and may be set and modified as needed.
The point is that HCl is added into the seventh container until the pH value of the flowback fluid is regulated to a third preset value; adding sodium bisulphite into the seventh container until the ORP of the flowback fluid is regulated to a fourth preset value; wherein the third preset value is any value between 6.5 and 7.5, for example, 7, and the fourth preset value is any value between-100 mv and +100mv, for example, 0mv.
In one possible implementation, the first filtering unit 14 further includes a scale inhibition tank, which is in communication with the seventh container, in which a scale inhibitor is disposed, and scale-forming ions in the flowback fluid are reduced by adding the scale inhibitor to the seventh container. Alternatively, the scale inhibitor may be added after the flowback fluid is treated with the ultrafiltration membrane. Correspondingly, the treatment device also comprises an eighth container, the water outlet of the ultrafiltration membrane is connected with the water inlet of the eighth container, the water outlet of the eighth container is connected with the water inlet of the second filtering unit, and the scale inhibition tank is communicated with the eighth container.
In one possible implementation, the scale inhibitor is a phosphorus-containing scale inhibitor having a concentration of any value between 20mg/L and 40 mg/L. Wherein, the phosphorus scale inhibitor can be inorganic phosphorus scale inhibitor, such as sodium tripolyphosphate, sodium hexametaphosphate, etc.; the phosphorus-containing scale inhibitor may also be an organic phosphorus-containing scale inhibitor, such as hydroxyethylidene diphosphonic acid, polyamino polyether methylene phosphonate, and the like. 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 filter unit 15: and a second filtering unit 15 for filtering scale-forming ions in the flowback fluid. Wherein the scale forming ions comprise at least one of calcium ions, magnesium ions, barium ions, strontium ions and carbonate ions.
In one possible implementation, the water inlet of the second filter unit 15 is directly connected to the water outlet of the first filter unit 14, and the water outlet of the second filter unit 15 is connected to the water inlet of the reverse osmosis unit 16.
In one possible implementation, the second filter unit 15 is a roll nanofiltration membrane. Wherein, the operating pressure of the coiled 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 coiled nanofiltration membrane is 40-80%.
Introduction of reverse osmosis unit 16: the water inlet of the reverse osmosis unit 16 is connected with the water outlet of the second filtering unit 15, and is used for reducing the mineralization degree in the flowback fluid, so as to obtain the fracturing fluid. The degree of mineralization can be determined by the concentration of TDS (total dissolved solids ), among others.
In one possible implementation, the reverse osmosis unit 16 is a dished tubular reverse osmosis membrane. Wherein the operation pressure of the disc-tube reverse osmosis membrane is any value between 8MPa and 11 MPa; for example, 8MPa, 9MPa, 10MPa, etc.; the water yield of the disc-tube type reverse osmosis membrane is 40-70%.
The flow of the treatment device for the flowback fluid will be described below. FIG. 2 is a flow chart of a flow-back fluid treatment device for treating a flow-back fluid according to an embodiment of the present application; referring to fig. 2, the step of processing the flowback fluid by the processing apparatus includes:
in step 201, the concentration of organic matters and the concentration of microorganisms in the flowback fluid to be treated are reduced through an air floatation unit, and the bacteria in the flowback fluid are reduced by adding sodium hypochlorite solution.
And 202, adding sodium hydroxide solution to adjust the pH value of the flowback fluid to 11, and adding sodium carbonate solution to reduce the concentration of calcium ions in the flowback fluid.
Step 203, detecting turbidity of the flowback fluid, adding a third volume of coagulant and a fourth volume of flocculant according to the turbidity of the flowback fluid, and standing for precipitation.
Step 204, filtering impurities in the flowback fluid through a first filtering unit, adding a hydrochloric acid solution to adjust the pH value of the flowback fluid to 7, and adding a phosphorus-containing scale inhibitor.
Step 205, filtering scale-forming ions in the flowback fluid by a second filtering unit.
And 206, reducing the mineralization degree in the flowback fluid through a reverse osmosis unit to obtain the preparation liquid of the fracturing fluid.
The water quality of the fracturing fluid obtained after treatment can be improved by comparing the water quality of the water discharged by the treatment device of the flowback fluid in the prior art with the water quality of the water discharged by the treatment device of the flowback fluid in the application.
The treatment process of the treatment device of the flowback fluid in the prior art comprises the following steps: sodium hydroxide was added to the flowback fluid in an amount of 300ppm, and sodium carbonate was added to the flowback fluid in an amount of 1500ppm. The treatment process of the treatment device for the flowback fluid in the application is as follows: sodium hydroxide was added to the flowback fluid in an amount to raise the pH of the flowback fluid to 10. Sodium carbonate is added into the flowback fluid, and the addition amount of the sodium carbonate is 1.06 times of the hardness of the calcium in the flowback fluid.
(one) hardness of effluent water quality is compared with pH value:
and 6 groups of samples are selected for comparative analysis, the 6 groups of samples are respectively processed by a processing device in the prior art and the processing device in the application, and the hardness and the PH value of the fracturing fluid obtained after the processing are tested, and the test results are shown in the following table 1.
TABLE 1 hardness versus pH of effluent quality
The water quality analysis results in Table 1 show that the hardness of the effluent of the present application is lower than 260mg/L, while the hardness fluctuation of the effluent quality in the prior art is larger, and is between 50 and 580 mg/L. The alkalinity of the effluent is stable and is 470-600 mg/L, while the alkalinity of the effluent in the prior art is generally higher and reaches 2000mg/L at most, which indicates that the sodium carbonate is excessively added. The pH value of the effluent of the application is always stabilized 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 sodium hydroxide is added inaccurately. Therefore, the water quality of the effluent is good and stable, and the hardness, the pH value and the alkalinity of the flowback fluid can be stably controlled.
(II) turbidity contrast of effluent quality:
the 6 groups of samples were treated by the treatment apparatus of the prior art and tested after being treated by the coagulation sedimentation unit in the treatment apparatus of the present application, respectively, and the test results are shown in table 2 below.
TABLE 2 turbidity contrast of effluent quality
The water quality analysis results in table 2 show that the turbidity of the treated effluent is lower than 4NTU, the lowest turbidity can reach 1.1NTU, the turbidity of the effluent in the prior art is higher than 10NTU, the highest turbidity reaches more than 20NTU, and the fluctuation of the turbidity of the effluent is larger. Therefore, the effluent quality of the water treatment device is good and stable.
(III) turbidity, hardness and alkalinity comparison of effluent quality:
in this embodiment of the present application, after passing through the coagulation sedimentation unit, the flowback fluid continues to pass through the first filtering unit and the second filtering unit for treatment, and the results are shown in the following table 3, comparing the effluent quality of the prior art with the effluent quality of the present application.
TABLE 3 comparative analysis of the quality of the prior art effluent and the quality of the effluent of the present application
The results of water quality analysis in Table 3 show that the turbidity of the flowback fluid after being treated by the coagulation sedimentation unit, the first filtration unit and the second filtration unit is substantially 0.2NTU or less, the hardness is within 100mg/l, and the alkalinity is within 250 mg/l. From this, it was found that the small particulate matter, colloid and scale-forming ions in the flowback fluid were further removed, and therefore the water quality of the fracturing fluid obtained by the treatment apparatus of the present application was good and stable.
The quality of raw water of the flowback fluid and the quality of the prepared fracturing fluid after being treated by the treatment device in the application are respectively compared with the fracturing fluid quality standard (NB/T14002.3-2015), and the quality of the prepared fracturing fluid after being treated by the treatment device in the application can be determined to meet the fracturing fluid quality standard. The comparative analysis results are shown in table 4 below.
TABLE 4 analysis of the quality of flowback raw water and reverse osmosis membrane effluent
The water quality analysis results in table 4 show that the water quality of the fracturing fluid prepared by the treatment device can meet the water quality standard of the fracturing fluid.
The foregoing description of the preferred embodiments is merely exemplary in nature and is in no way intended to limit the invention, since it is intended that all modifications, equivalents, improvements, etc. that fall within the spirit and scope of the invention.
Claims (6)
1. A treatment device for flowback fluid, the treatment device comprising: an air floatation 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 floatation 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 sequentially communicated;
The device comprises an air floatation unit (11), a softening unit (12), a coagulating sedimentation unit (13), a first filtering unit (14) and a second filtering unit (15), wherein the air floatation unit is used for reducing the concentration of organic matters and the concentration of microorganisms in a flowback fluid to be treated, the softening unit (12) is used for reducing scale forming ions in the flowback fluid through adding a scale remover, the coagulating sedimentation unit (13) is used for reducing the turbidity of the flowback fluid through adding a turbidity reducer, the first filtering unit (14) is used for filtering impurities in the flowback fluid, the second filtering unit (15) is used for filtering the scale forming ions in the flowback fluid, and the reverse osmosis unit (16) is used for reducing the mineralization degree in the flowback fluid to obtain a fracturing fluid;
the air floatation unit (11) comprises a lift pump, an air floatation machine and a first container;
the lifting pump and the air floatation machine are respectively communicated with the water inlet of the first container, and the water outlet of the first container is communicated with the water inlet of the softening unit (12);
the lifting pump is used for lifting the flowback fluid to the first container, the air floatation machine is used for filling first gas into the first container, and the concentration of organic matters in the flowback fluid is reduced through the first gas;
the air floatation unit (11) further comprises a sterilizing tank, wherein the sterilizing tank is communicated with the water inlet of the first container and is used for introducing a sterilizing agent into the first container, and the concentration of microorganisms in the flowback fluid is reduced through the sterilizing agent, and the sterilizing agent comprises sodium hypochlorite;
The softening unit (12) 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 (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 regulating tank is communicated with the second container, and the descaling tank is communicated with the third container;
the flow-back liquid treated by the air floatation unit (11) enters the second container through the water outlet of the air floatation unit (11) and the water inlet of the second container, the pH value detector is used for detecting the pH value of the flow-back liquid in the second container, the hardness detector is used for detecting the hardness of the flow-back liquid in the third container, the alkaline regulating tank is used for introducing an acid-base regulator into the second container to regulate the pH value of the flow-back liquid, and the descaling tank is used for introducing a descaling agent into the third container to reduce scale-forming ions in the flow-back liquid;
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 added into the second container according to the pH value and the hardness of the flowback fluid, controlling the alkaline regulating tank to introduce the acid-base regulator of the first volume into the second container, and controlling the descaling tank to introduce the descaling agent of the second volume into the third container.
2. The treatment device of claim 1, wherein the air floatation 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 dissolved air tank to form dissolved air water, the dissolved air tank is used for inputting the dissolved air water into the first container, and ferrous ions in the flowback fluid are oxidized into ferric ions through the air in the dissolved air water to form precipitation.
3. The treatment device according to claim 1, characterized in that the coagulation sedimentation unit (13) comprises a fourth container, a fifth container, a sixth container and a turbidity adjustment tank;
The water inlet at the lower part of the fourth container is communicated with the water outlet of the softening unit (12), the water outlet at the upper part of the fourth container is communicated with the water inlet at the upper part of the fifth container, the water outlet at the middle part of the fifth container is communicated with the water inlet at the middle part of the sixth container, the 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 flowback liquid treated by the softening unit (12) enters the fourth container through the water outlet of the softening unit (12) and the water inlet of the fourth container, the turbidity adjusting tank is used for introducing turbidity reducing agent into the fourth container and the fifth container to reduce the turbidity of the flowback liquid, and the sixth container is used for collecting sediment in the flowback liquid.
4. A treatment device according to claim 3, wherein the turbidity adjustment tank comprises a first turbidity adjustment tank and a second turbidity adjustment tank, the turbidity reducing agent comprising a coagulant and a flocculant, the first turbidity adjustment tank being in communication with the fourth vessel, the second turbidity adjustment tank being 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 flowback fluid to form large particulate matters; and the second turbidity adjusting tank is used for introducing a flocculating agent into the fifth container to enable the large granular substances to form large flocs so as to reduce the turbidity of the flowback fluid.
5. The treatment device according to claim 4, characterized in that 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 the first turbidity of the flowback liquid in the fourth container, the second turbidity detector is used for detecting the second turbidity of the flowback liquid in the fifth container, the second controller is used for determining the third volume of the coagulant added into the fourth container according to the first turbidity, determining the fourth volume of the flocculant added into the fifth container according to the second turbidity, and controlling the first turbidity adjusting tank to introduce the third volume of the coagulant into the fourth container and controlling the second turbidity adjusting tank to introduce the fourth volume of the flocculant into the fifth container.
6. The treatment device according to claim 1, characterized in that the first filtration unit (14) comprises an ultrafiltration membrane, an acidity adjustment tank, an oxidation-reduction potential ORP adjustment tank and a seventh vessel;
the water outlet of the coagulation sedimentation unit (13) 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 (15), and the acid regulating tank and the ORP regulating tank are respectively communicated with the seventh container;
the acid regulating tank is used for introducing a third solution into the seventh container to regulate the pH value of the flowback fluid, the ORP regulating tank is used for introducing a fourth solution into the seventh container to regulate the ORP value of the flowback fluid, and the ultrafiltration membrane is used for filtering impurities in the flowback fluid.
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