CN113045048A - Shale gas fracturing flowback fluid treatment system - Google Patents
Shale gas fracturing flowback fluid treatment system Download PDFInfo
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- CN113045048A CN113045048A CN202110336773.7A CN202110336773A CN113045048A CN 113045048 A CN113045048 A CN 113045048A CN 202110336773 A CN202110336773 A CN 202110336773A CN 113045048 A CN113045048 A CN 113045048A
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 50
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 49
- 239000012528 membrane Substances 0.000 claims abstract description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 150000003839 salts Chemical class 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 35
- 229920005989 resin Polymers 0.000 claims abstract description 17
- 239000011347 resin Substances 0.000 claims abstract description 17
- 238000001914 filtration Methods 0.000 claims abstract description 14
- 238000004062 sedimentation Methods 0.000 claims abstract description 14
- 239000000126 substance Substances 0.000 claims abstract description 12
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000001179 sorption measurement Methods 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims description 37
- 230000001954 sterilising effect Effects 0.000 claims description 23
- 238000004659 sterilization and disinfection Methods 0.000 claims description 23
- 239000013505 freshwater Substances 0.000 claims description 20
- 239000004902 Softening Agent Substances 0.000 claims description 16
- 238000001728 nano-filtration Methods 0.000 claims description 16
- 239000002351 wastewater Substances 0.000 claims description 16
- 238000011084 recovery Methods 0.000 claims description 15
- 239000000701 coagulant Substances 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 8
- 230000008020 evaporation Effects 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 6
- 238000010907 mechanical stirring Methods 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 6
- 229910001385 heavy metal Inorganic materials 0.000 claims description 5
- 238000001556 precipitation Methods 0.000 claims description 5
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 4
- 238000005188 flotation Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 3
- 230000000844 anti-bacterial effect Effects 0.000 claims description 3
- 239000003899 bactericide agent Substances 0.000 claims description 3
- 229920001429 chelating resin Polymers 0.000 claims description 3
- 239000000571 coke Substances 0.000 claims description 3
- 238000002425 crystallisation Methods 0.000 claims description 3
- 230000008025 crystallization Effects 0.000 claims description 3
- 238000000909 electrodialysis Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 150000002500 ions Chemical class 0.000 claims description 3
- 238000005374 membrane filtration Methods 0.000 claims description 3
- 238000009287 sand filtration Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims 1
- 150000001768 cations Chemical class 0.000 claims 1
- 239000012141 concentrate Substances 0.000 claims 1
- 229920000620 organic polymer Polymers 0.000 claims 1
- 238000003912 environmental pollution Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 3
- 238000009825 accumulation Methods 0.000 abstract description 2
- 230000000630 rising effect Effects 0.000 abstract 1
- 238000009834 vaporization Methods 0.000 abstract 1
- 230000008016 vaporization Effects 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 19
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 239000011780 sodium chloride Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 4
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 4
- 239000000920 calcium hydroxide Substances 0.000 description 4
- 235000011116 calcium hydroxide Nutrition 0.000 description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 125000000129 anionic group Chemical group 0.000 description 3
- 230000003204 osmotic effect Effects 0.000 description 3
- 229920002401 polyacrylamide Polymers 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 125000002091 cationic group Chemical group 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 239000008394 flocculating agent Substances 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 229910001629 magnesium chloride Inorganic materials 0.000 description 2
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 2
- 235000019341 magnesium sulphate Nutrition 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000012267 brine Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000013522 chelant Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
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- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
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- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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Abstract
The invention belongs to the technical field of water treatment, and particularly relates to a treatment system for shale gas fracturing flowback fluid. The treatment system is through reasonable design reaction system, the sedimentation system, filtration system, deoiling system, the piece-rate system, the resin softens the system, receive the relation of connection and the processing relation between each systems such as filter membrane salt system, reverse osmosis membrane concentration system, vaporization system and ammonia nitrogen adsorption system, salt and other chemical composition in the flowing back are returned in the sufficient effective removal fracturing, product water can retrieval and utilization up to standard, salt in the waste liquid can be drawed out, sell as industrial salt, realize resource rationalization utilization, and environment friendly, and system equipment is simple, the maneuverability is strong, the running cost reduces, the problem of salt and other chemical composition accumulation production cost rising and environmental pollution that cause when shale atmospheric pressure splits flowing back and uses has good economic benefits and social.
Description
Technical Field
The invention belongs to the technical field of water treatment, and particularly relates to a treatment system for shale gas fracturing flowback fluid.
Background
Shale gas is a clean, low-carbon and unconventional natural gas resource which is in an adsorption, dissolution and free state and is contained in shale. Shale gas development has the advantages of long mining life, high yield and long production period, and becomes a new bright point for exploration and development of global oil and gas resources. However, as the most mature shale gas mining method, namely the hydraulic fracturing technology, the environmental problems of release of greenhouse gases such as methane, discharge of waste water, pollution of underground water and the like are brought about, the high attention of governments and people of all countries is attracted, and the problem of water pollution is the most worrisome. The shale gas fracturing flowback fluid has the characteristics of complex composition, high pollutant concentration, high viscosity, high emulsification degree and multiple points, can cause serious environmental pollution and water resource waste if directly discharged, and has high treatment difficulty. In fact, after the return water is basically filtered and mixed with fresh water at the early stage, the return water can be frequently used for many times under certain geological conditions after being added with a fracturing chemical agent, and then the oil-gas flow can be improved. However, the accumulated brine and other chemical components are still disposed of, and thus problems of high production costs and environmental pollution still remain.
Disclosure of Invention
The invention aims to solve the problems in the prior art and provides a treatment system for shale gas fracturing flow-back fluid, which can effectively remove salt and other chemical components in the fracturing flow-back fluid and realize resource utilization of water and salt in wastewater.
The technical scheme adopted by the invention for solving the technical problems is as follows:
a shale gas fracturing flowback fluid treatment system comprises the following steps:
1) after large-particle-size impurities in the shale gas fracturing flow-back fluid are removed through sedimentation in a wastewater collection tank, supernatant enters a reaction tank of a first reaction system, a coagulant and a flocculant are uniformly added into the reaction tank of the first reaction system through a coagulant and flocculant dosing device, the mixture is fully reacted through a mechanical stirring device and an aeration system, after 15min of reaction residence time, feed liquid in the reaction tank is conveyed into the sedimentation system, and suspended matters in the wastewater are removed through sedimentation;
2) supernatant of the precipitation system enters a filtration system again to further remove substances such as suspended particles or colloid and the like in the wastewater;
3) the effluent of the filtering system enters a sterilization system again to sterilize the wastewater, and the wastewater reaches the standard of recycling of fracturing flow-back fluid:
4) the effluent of the sterilization system enters an oil removal system for oil-water separation, and oil substances in the water are removed until the indexes of a subsequent film inlet system are reached;
5) the effluent of the oil removal system enters a reaction tank of a second reaction system, softening agents are uniformly added into the reaction tank of the second reaction system through a softening agent dosing device, the softening agents are fully reacted through a mechanical stirring device and an aeration system, and after 30min of reaction residence time, feed liquid in the reaction tank is conveyed to a separation system to separate solid from liquid;
6) the water discharged from the separation system enters a resin softening system to further remove the hardness in the water and the heavy metal ions which are not precipitated by reaction;
7) the effluent of the resin softening system enters a nanofiltration membrane salt separation system to carry out divalent salt separation, membrane fresh water is rich in monovalent salt, concentrated water is rich in divalent metal salt, the membrane fresh water enters a subsequent reverse osmosis membrane concentration system to be re-concentrated, the membrane concentrated water returns to a second reaction system, and heavy metals and concentrated organic matters in the concentrated water are removed in a mode of adding a softening agent;
8) the reverse osmosis membrane concentration system is used for concentrating and reducing the membrane fresh water of the nanofiltration membrane salt separation system to obtain a concentrated solution, the concentrated solution of the reverse osmosis membrane concentration system enters the auxiliary reverse osmosis system for further concentration and reduction, and finally the concentrated solution of the auxiliary reverse osmosis system is concentrated until the TDS is more than or equal to 140000mg/l and then enters the evaporation system for evaporation and crystallization;
9) the auxiliary reverse osmosis system is matched with a suction liquid recovery system, fresh water of the auxiliary reverse osmosis system enters the suction liquid recovery system, concentrated liquid of the suction liquid recovery system flows back to the auxiliary reverse osmosis system, the fresh water of the suction liquid recovery system and the fresh water of the reverse osmosis membrane concentration system enter the ammonia nitrogen adsorption system to remove ammonia nitrogen, and the fresh water is discharged or recycled after reaching the standard.
Preferably, the coagulant in the step 1) is one or a combination of more of polyaluminium sulfate, polyaluminium chloride and polyferric chloride, and the dosage is 30-50 mg/L; the flocculating agent is anionic polyacrylamide, and the dosage is 1-3 mg/L.
Preferably, the filtration system in step 2) is one or more of sand filtration and membrane filtration.
Preferably, the sterilization system in step 3) is one or more of ozone sterilization, ultraviolet sterilization and bactericide sterilization.
Preferably, the oil removing system in the step 4) is one or more of air flotation oil removing, active coke oil removing, active carbon oil removing and membrane method oil removing.
Preferably, the softening agent in the step 5) is any one or more of hydrated lime, sodium hydroxide or sodium carbonate; more preferably, the pH value of the reaction tank of the second system is controlled to be 11-11.4; more preferably, the dosage of the hydrated lime is 400-600mg/L, the dosage of the sodium hydroxide is 500-1000mg/L, and the dosage of the sodium carbonate is 2000-3300 mg/L.
Preferably, the separation system in the step 5) is one or more of a sedimentation tank and a tubular membrane.
Preferably, the resin softening system in step 6) is one or more of a chelating resin and a weakly acidic cationic resin.
Preferably, the nanofiltration membrane salt separation system in the step 7) is one or more of nanofiltration salt separation and electrodialysis salt separation; mainly used for realizing the separation of mono-divalent salt.
Preferably, the auxiliary reverse osmosis system in the step 8) is provided with four ports, namely a water inlet, a concentrated water port, a drawing liquid water inlet and a diluted drawing liquid outlet; the draw solution is used to reduce the osmotic pressure at two ends of the reverse osmosis membrane so as to improve the concentration ratio of the reverse osmosis system.
Preferably, the auxiliary reverse osmosis system in step 8) is operated at a pressure of 60 to 80 bar.
Preferably, the auxiliary reverse osmosis system in step 8) is provided with a draw solution, and the draw solution is one or a combination of salts and organic high molecules; more preferably, the draw solution is one or more combinations of sodium chloride, magnesium chloride, calcium chloride or magnesium sulfate.
Preferably, the draw solution recovery system in step 9) is used for concentrating the diluted draw solution in the auxiliary reverse osmosis system and returning the concentrated draw solution to the auxiliary reverse osmosis system.
The invention provides a treatment system for shale gas fracturing flowback fluid, which has the following advantages compared with the prior art:
(1) the system equipment is simple, and the operability is strong;
(2) by using the auxiliary reverse osmosis system, the osmotic pressure at two ends of the reverse osmosis membrane is effectively reduced, the concentration ratio is improved, and the investment and the operation cost of a subsequent evaporator are reduced;
(3) the salt and other chemical components in the shale gas fracturing flowback fluid can be effectively removed, the produced water can be recycled up to the standard, the salt in the waste liquid can be extracted and sold as industrial salt, the reasonable utilization of resources is realized, and the environment is friendly;
(4) the problems of production cost increase and environmental pollution caused by accumulation of salt and other chemical components when the shale gas fracturing flowback fluid is reused are solved, and the shale gas fracturing flowback fluid has good economic and social benefits.
Drawings
Fig. 1 is a schematic diagram of a shale gas frac flowback fluid treatment system of the present invention.
Detailed Description
The technical solution of the present invention is further specifically described below by way of specific examples in conjunction with the accompanying drawings.
Example (b):
in one embodiment, the initial values of the shale gas frac flowback fluid are as follows:
TABLE 1 initial values of the components of shale gas fracturing flowback fluid
A shale gas fracturing flowback fluid treatment system comprises the following steps:
1) after large-particle-size impurities in the shale gas fracturing flow-back fluid are removed through sedimentation in a wastewater collection tank, supernatant enters a reaction tank of a first reaction system, a coagulant and a flocculant are uniformly added into the reaction tank of the first reaction system through a coagulant and flocculant dosing device, the mixture is fully reacted through a mechanical stirring device and an aeration system, after 15min of reaction residence time, feed liquid in the reaction tank is conveyed into the sedimentation system, and suspended matters in the wastewater are removed through sedimentation;
2) supernatant of the precipitation system enters a filtration system again to further remove substances such as suspended particles or colloid and the like in the wastewater;
3) the effluent of the filtering system enters a sterilization system again to sterilize the wastewater, and the wastewater reaches the standard of recycling of fracturing flow-back fluid:
4) the effluent of the sterilization system enters an oil removal system for oil-water separation, and oil substances in the water are removed until the indexes of a subsequent film inlet system are reached;
5) the effluent of the oil removal system enters a reaction tank of a second reaction system, softening agents are uniformly added into the reaction tank of the second reaction system through a softening agent dosing device, the softening agents are fully reacted through a mechanical stirring device and an aeration system, and after 30min of reaction residence time, feed liquid in the reaction tank is conveyed to a separation system to separate solid from liquid;
6) the water discharged from the separation system enters a resin softening system to further remove the hardness in the water and the heavy metal ions which are not precipitated by reaction;
7) the effluent of the resin softening system enters a nanofiltration membrane salt separation system to carry out divalent salt separation, membrane fresh water is rich in monovalent salt, concentrated water is rich in divalent metal salt, the membrane fresh water enters a subsequent reverse osmosis membrane concentration system to be re-concentrated, the membrane concentrated water returns to a second reaction system, and heavy metals and concentrated organic matters in the concentrated water are removed in a mode of adding a softening agent;
8) the reverse osmosis membrane concentration system is used for concentrating and reducing the membrane fresh water of the nanofiltration membrane salt separation system to obtain a concentrated solution, the concentrated solution of the reverse osmosis membrane concentration system enters the auxiliary reverse osmosis system for further concentration and reduction, and finally the concentrated solution of the auxiliary reverse osmosis system is concentrated until the TDS is more than or equal to 140000mg/l and then enters the evaporation system for evaporation and crystallization;
9) the auxiliary reverse osmosis system is matched with a suction liquid recovery system, fresh water of the auxiliary reverse osmosis system enters the suction liquid recovery system, concentrated liquid of the suction liquid recovery system flows back to the auxiliary reverse osmosis system, the fresh water of the suction liquid recovery system and the fresh water of the reverse osmosis membrane concentration system enter the ammonia nitrogen adsorption system to remove ammonia nitrogen, and the fresh water is discharged or recycled after reaching the standard.
Wherein the coagulant in the step 1) is polyaluminium sulfate, and the addition amount is 40 mg/L; the flocculating agent is anionic polyacrylamide, and the dosage is 2 mg/L.
In the step 2), the filtering system is sand filtering, and after the shale gas fracturing flow-back fluid is treated by the first reaction system, the precipitation system and the filtering system, the data are shown in the following table:
TABLE 2 values of the components after treatment in the first reaction system and the precipitation filtration system
The sterilization system in the step 3) is used for ozone sterilization.
The oil removing system in the step 4) is air flotation oil removing, and after being treated by the sterilization system and the oil removing system, the data are shown in the following table:
TABLE 3 values of the ingredients after treatment with the sterilization system and the oil removal system
In the step 5), the softening agent is hydrated lime, the adding amount is 500mg/L, and the pH value of a reaction tank of the second reaction system is 11; the separation system is a sedimentation tank. After treatment in the second reaction system and the separation system, the data are shown in the following table:
TABLE 4 values of the components after treatment in the second reaction System and the separation System
The resin softening system in the step 6) is chelate resin, and after the resin softening system is used for processing, the data are shown in the following table:
TABLE 5 values of the ingredients after treatment in the resin softening System
The nanofiltration membrane salt separation system in the step 7) is used for nanofiltration salt separation, and after the nanofiltration membrane salt separation system is used for treatment, the data are shown in the following table:
TABLE 6 values of the components after treatment by the nanofiltration membrane salt separation system
After treatment in the reverse osmosis membrane concentration system in step 8), the data are shown in the following table:
TABLE 7 values of the components after treatment by the reverse osmosis membrane concentration system
The auxiliary reverse osmosis system in the step 8) is provided with four ports which are a water inlet, a concentrated water port, a drawing liquid water inlet and a diluted drawing liquid outlet respectively; the draw solution is used for reducing the osmotic pressure at two ends of the reverse osmosis membrane so as to improve the concentration ratio of the reverse osmosis system; wherein the draw solution is sodium chloride; the operating pressure of the auxiliary reverse osmosis system is 60-80bar, and after the auxiliary reverse osmosis system is used for treatment, the data are shown in the following table:
TABLE 8 values of the components after treatment with an auxiliary reverse osmosis system
After treatment in the evaporation system in step 8), the data are shown in the following table:
TABLE 9 values of the components after treatment in the Evaporation System
After treatment by the ammonia nitrogen adsorption system in the step 9), the data are shown in the following table:
TABLE 10 values of the components after treatment by the ammonia nitrogen adsorption system
In summary, after the shale gas fracturing flow-back fluid is processed by the processing system, the data are shown in the following table:
TABLE 11 shale gas fracturing flowback fluid after treatment by the treatment system
In one embodiment, the coagulant in step 1) is one or more of polyaluminium sulfate, polyaluminium chloride or polyferric chloride, the dosage is 30-50mg/L, the flocculant is anionic polyacrylamide, and the dosage is 1-3 mg/L.
In one embodiment, the filtration system in step 2) is one or more of sand filtration and membrane filtration.
In one embodiment, the sterilization system in step 3) is one or more of ozone sterilization, ultraviolet sterilization and bactericide sterilization.
In one embodiment, the oil removing system in step 4) is one or more of air flotation oil removal, active coke oil removal, active carbon oil removal and membrane method oil removal.
In one embodiment, the pH value of the second system reaction tank is controlled to be 11-11.4 in the step 5), the softening agent is hydrated lime, the adding amount is 400-600mg/L, or the softening agent is sodium hydroxide, the adding amount is 500-1000mg/L, or the softening agent is sodium carbonate, and the adding amount is 2000-3300 mg/L.
In one embodiment, the separation system in step 5) is one or more of a sedimentation tank and a tubular membrane.
In one embodiment, the resin softening system in step 6) is one or more combination of chelating resin, weakly acidic cationic resin.
In one embodiment, the nanofiltration membrane salt separation system in the step 7) is one or more of nanofiltration salt separation and electrodialysis salt separation.
In one embodiment, the draw solution in step 8) is one or more combinations of sodium chloride, magnesium chloride, calcium chloride or magnesium sulfate.
In one embodiment, the water inlet of the auxiliary reverse osmosis system in the step 8) is pumped into waste water with the concentration of TDS 70000mg/L by a high-pressure pump, the pressure is 66bar, meanwhile, NaCl solution with the concentration of 90000mg/L is pumped into the water inlet of the drawing liquid, then the outlet water of the concentrated water outlet is concentrated water with the concentration of TDS 140000mg/L, the outlet water concentration of the diluted drawing liquid is NaCl solution with the concentration of 52000mg/L, and the diluted drawing liquid is concentrated to the concentration of 90000mg/L by the drawing liquid recovery system and then returns to the water inlet of the drawing liquid of the auxiliary reverse osmosis system for circulation.
The above-described embodiments are merely preferred embodiments of the present invention, which is not intended to be limiting in any way, and other variations and modifications are possible without departing from the scope of the invention as set forth in the appended claims.
Claims (10)
1. The treatment system of the shale gas fracturing flowback fluid is characterized by comprising the following steps of:
1) after large-particle-size impurities in the shale gas fracturing flow-back fluid are removed through sedimentation in a wastewater collection tank, supernatant enters a reaction tank of a first reaction system, a coagulant and a flocculant are uniformly added into the reaction tank of the first reaction system through a coagulant and flocculant dosing device, the mixture is fully reacted through a mechanical stirring device and an aeration system, after 15min of reaction residence time, feed liquid in the reaction tank is conveyed into the sedimentation system, and suspended matters in the wastewater are removed through sedimentation;
2) and (3) the supernatant of the precipitation system enters a filtering system again, and suspended particulate matters or colloidal substances in the wastewater are further removed:
3) the effluent of the filtering system enters a sterilization system for sterilization treatment;
4) the effluent of the sterilization system enters an oil removal system for oil-water separation to remove oil substances in water;
5) the effluent of the oil removal system enters a reaction tank of a second reaction system, softening agents are uniformly added into the reaction tank of the second reaction system through a softening agent dosing device, the softening agents are fully reacted through a mechanical stirring device and an aeration system, and after 30min of reaction residence time, feed liquid in the reaction tank is conveyed to a separation system to separate solid from liquid;
6) the water discharged from the separation system enters a resin softening system to further remove the hardness in the water and the heavy metal ions which are not precipitated by reaction;
7) the effluent of the resin softening system enters a nanofiltration membrane salt separation system, and the membrane fresh water enters a subsequent reverse osmosis membrane concentration system for re-concentration;
8) the reverse osmosis membrane concentration system carries out concentration decrement on fresh water of a nanofiltration membrane salt separation system, concentrated solution of the reverse osmosis membrane concentration system enters the auxiliary reverse osmosis system for further concentration decrement, and finally concentrated solution of the auxiliary reverse osmosis system is concentrated until TDS is more than or equal to 140000mg/l and then enters the evaporation system for evaporation crystallization;
9) the auxiliary reverse osmosis system is matched with a suction liquid recovery system, fresh water of the auxiliary reverse osmosis system enters the suction liquid recovery system, concentrated liquid of the suction liquid recovery system flows back to the auxiliary reverse osmosis system, and fresh water of the suction liquid recovery system and fresh water of the reverse osmosis membrane concentration system enter the ammonia nitrogen adsorption system to be discharged or recycled after ammonia nitrogen is removed.
2. The system for treating shale gas fracturing flowback fluid of claim 1, wherein the filtration system in step 2) is one or more of sand filtration and membrane filtration.
3. The shale gas fracturing flowback fluid treatment system of claim 1, wherein the sterilization system in step 3) is one or more of ozone sterilization, ultraviolet sterilization and bactericide sterilization.
4. The system for treating shale gas fracturing flowback fluid according to claim 1, wherein the oil removal system in step 4) is one or more of air flotation oil removal, active coke oil removal, active carbon oil removal and membrane method oil removal.
5. The system for treating the shale gas fracturing flowback fluid of claim 1, wherein the separation system in the step 5) is one or more of a sedimentation tank and a tubular membrane.
6. The system for treating shale gas fracturing flowback fluid of claim 1, wherein in step 6), the resin softening system is one or more of chelating resin and weak acid cation resin.
7. The system for treating shale gas fracturing flowback fluid of claim 1, wherein the nanofiltration membrane salt separation system in step 7) is one or more of nanofiltration salt separation and electrodialysis salt separation.
8. The system for treating shale gas fracturing flowback fluid of claim 1, wherein the auxiliary reverse osmosis system in step 8) is provided with four ports, namely a water inlet, a concentrate port, a drawing fluid inlet and a diluted drawing fluid outlet.
9. The system for treating shale gas fracturing flowback fluid of claim 1, wherein the auxiliary reverse osmosis system in step 8) is operated at a pressure of 60-80 bar.
10. The system for treating shale gas fracturing flowback fluid of claim 1, wherein the draw solution recovery system in step 9) is one or more of salts and organic polymers.
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| CN113880305A (en) * | 2021-11-01 | 2022-01-04 | 重庆助农生物科技有限公司 | Modular integrated type flowback wastewater treatment system and method |
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