CN218665629U - Fracturing flow-back fluid advanced treatment unit - Google Patents
Fracturing flow-back fluid advanced treatment unit Download PDFInfo
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- CN218665629U CN218665629U CN202222601679.2U CN202222601679U CN218665629U CN 218665629 U CN218665629 U CN 218665629U CN 202222601679 U CN202222601679 U CN 202222601679U CN 218665629 U CN218665629 U CN 218665629U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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Abstract
The utility model discloses a flowing back degree of depth processing unit is returned to fracturing, it includes line mixer, ozone vapor floating device, ozone vapor floating water pool, buffer tank, filter, ultrafiltration device, surpass and filter out water pitcher, reverse osmosis unit, first dense water tank, superhigh pressure reverse osmosis unit, second dense water tank, ion exchange reaction equipment, MVR evaporation crystallization device and product pond. The advantages are that: the system further removes organic matters in the wastewater through an ozone air flotation device, then removes particle impurities in the wastewater through two-stage filtration of sand filtration and ultrafiltration, and then separates recyclable fresh water from a sewage body through two-stage membrane filtration of reverse osmosis and ultrahigh pressure reverse osmosis so as to reduce the treatment capacity of high-concentration brine; concentrated water produced by membrane filtration is evaporated and desalted by adopting an MVR technology, so that inorganic salt is removed from a water body in a crystal form; the final water production has low organic matter content, the high-concentration brine treatment capacity is effectively reduced, and the system operation cost is effectively reduced.
Description
The technical field is as follows:
the utility model relates to a flowing back processing system is returned in fracturing, and specifically speaking relates to a flowing back depth processing unit is returned to fracturing.
Background art:
the fracturing flow-back fluid treatment system mainly comprises three procedures of pretreatment, biochemical treatment and advanced treatment. The effluent of the fracturing flow-back fluid pretreatment is characterized by high COD content and high salinity, the COD content is 3500-4500mg/l, the salinity is 25000-35000mg/l, the COD is effectively reduced after biochemical treatment, then the effluent is directly sent to an evaporative crystallization device of an advanced treatment process for evaporative crystallization, and the condensate water discharged by the evaporative crystallization device is output as produced water; however, a small amount of organic matters and particle impurities still exist in biochemical production water, so that the amount of salt-containing wastewater reaching the evaporative crystallization equipment is large, the treatment capacity of the evaporative crystallization equipment is large, the operation load is high, and the cost is increased; and the evaporation crystallization equipment can not remove organic matters, so that the organic matter content of the final produced water is still higher.
The utility model has the following contents:
an object of the utility model is to provide a flowing back degree of depth processing unit is returned to fracturing that can reduce the handling capacity that reduces high enriched brine.
The utility model discloses by following technical scheme implement: the deep treatment unit of the fracturing flow-back fluid comprises a pipeline mixer, an ozone vapor floating device, an ozone vapor floating water outlet pool, a buffer tank, a filter, an ultrafiltration device, a super-filtration water tank, a reverse osmosis device, a first concentrated water tank, an ultrahigh pressure reverse osmosis device, a second concentrated water tank, ion exchange reaction equipment, an MVR evaporative crystallization device and a water production pool;
the outlet water of the biochemical water outlet tank is communicated with an inlet pipeline of the pipeline mixer, the outlet of the pipeline mixer is communicated with an inlet pipeline of the ozone vapor flotation device, the outlet of the ozone vapor flotation device is communicated with an inlet pipeline of the ozone vapor flotation water outlet tank, the outlet of the ozone vapor flotation water outlet tank is communicated with an inlet pipeline of the buffer tank, the outlet of the buffer tank is communicated with an inlet pipeline of the filter, the outlet of the filter is communicated with an inlet pipeline of the ultrafiltration device, the concentrated water outlet of the ultrafiltration device is communicated with an inlet pipeline of the buffer tank, the produced water of the ultrafiltration device is communicated with an inlet pipeline of the ultrafiltration water tank, the outlet of the ultrafiltration water tank is communicated with an inlet pipeline of the reverse osmosis device, the concentrated water outlet of the reverse osmosis device is communicated with the first concentrated water tank pipeline, the outlet of the first concentrated water tank is communicated with an inlet pipeline of the ultrahigh pressure reverse osmosis device, the outlet of the ultrahigh pressure reverse osmosis device is communicated with the second concentrated water tank pipeline, and the produced water outlet of the reverse osmosis device are communicated with an inlet pipeline of the produced water inlet pipeline of the reverse osmosis device; the outlet of the second concentrated water tank is communicated with the inlet pipeline of the ion exchange reaction equipment, the outlet of the ion exchange reaction equipment is communicated with the inlet pipeline of the MVR evaporative crystallization device, and the condensed water outlet of the MVR evaporative crystallization device is communicated with the inlet pipeline of the water production tank.
Furthermore, an overflow port of the buffer tank is communicated with an inlet pipeline of the ozone vapor floating water outlet pool.
Furthermore, the outlet of the water production tank is respectively communicated with the back flush inlet pipelines of the filter, the ultrafiltration device, the reverse osmosis device and the ultrahigh pressure reverse osmosis device, and the back flush outlets of the filter, the ultrafiltration device, the reverse osmosis device and the ultrahigh pressure reverse osmosis device are communicated with the inlet pipeline of the biochemical water outlet tank through pipelines.
Furthermore, the ion exchange reaction equipment comprises a first ion exchange reactor, a second ion exchange reactor and an ion exchange water outlet tank, wherein an inlet of the first ion exchange reactor is communicated with an outlet pipeline of the second concentrated water tank, an outlet of the first ion exchange reactor is communicated with an inlet pipeline of the second ion exchange reactor, an outlet of the second ion exchange reactor is communicated with an inlet pipeline of the ion exchange water outlet tank, and an outlet of the ion exchange water outlet tank is communicated with an inlet pipeline of the MVR evaporative crystallization device.
The utility model has the advantages that: the system further removes organic matters in the wastewater through an ozone air flotation device, then removes particle impurities in the wastewater through two-stage filtration of sand filtration and ultrafiltration, and then separates recyclable fresh water from a sewage body through two-stage membrane filtration of reverse osmosis and ultrahigh pressure reverse osmosis so as to reduce the treatment capacity of high-concentration brine; concentrated water produced by membrane filtration is evaporated and desalted by adopting an MVR technology, so that inorganic salt is removed from a water body in a crystal form; the final water production has low organic matter content and good water production quality, the treatment capacity of high-concentration brine is effectively reduced, and the system operation cost is effectively reduced.
Description of the drawings:
fig. 1 is a schematic view of the overall structure of the present invention.
The system comprises a pipeline mixer 1, an ozone vapor floating device 2, an ozone vapor floating water outlet tank 3, a buffer tank 4, a filter 5, an ultrafiltration device 6, an ultrafiltration water outlet tank 7, a reverse osmosis device 8, a first concentrated water tank 9, an ultrahigh pressure reverse osmosis device 10, a second concentrated water tank 11, ion exchange reaction equipment 12, an MVR evaporative crystallization device 13, a water production tank 14, a biochemical water outlet tank 15, a first ion exchange reactor 121, a second ion exchange reactor 122 and an ion exchange water outlet tank 123.
The specific implementation mode is as follows:
in the description of the present invention, it should be noted that, as the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. appear, the indicated orientation or positional relationship is based on the orientation or positional relationship shown in the drawings, and is only for convenience of description and simplification of description, but does not indicate or imply that the indicated device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" as appearing herein are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
As shown in fig. 1, the fracturing flow-back fluid advanced treatment unit includes a pipeline mixer 1, an ozone vapor flotation device 2, an ozone vapor flotation water outlet pool 3, a buffer tank 4, a filter 5, an ultrafiltration device 6, an ultrafiltration water outlet tank 7, a reverse osmosis device 8, a first concentrated water tank 9, an ultrahigh pressure reverse osmosis device 10, a second concentrated water tank 11, an ion exchange reaction device 12, an MVR evaporative crystallization device 13 and a water production pool 14;
the outlet of the biochemical water outlet tank 15 is communicated with an inlet pipeline of the pipeline mixer 1, the outlet of the pipeline mixer 1 is communicated with an inlet pipeline of the ozone vapor flotation device 2, the outlet of the ozone vapor flotation device 2 is communicated with an inlet pipeline of the ozone vapor flotation water outlet tank 3, the outlet of the ozone vapor flotation water outlet tank 3 is communicated with an inlet pipeline of the buffer tank 4, the outlet of the buffer tank 4 is communicated with an inlet pipeline of the filter 5, the filter 5 adopts a quartz sand filter, the outlet of the filter 5 is communicated with an inlet pipeline of the ultrafiltration device 6, the concentrated water outlet of the ultrafiltration device 6 is communicated with an inlet pipeline of the buffer tank 4, the produced water of the ultrafiltration device 6 is communicated with an inlet pipeline of the ultrafiltration water outlet tank 7, the outlet of the ultrafiltration water outlet tank 7 is communicated with an inlet pipeline of the reverse osmosis device 8, the concentrated water outlet of the reverse osmosis device 8 is communicated with a pipeline of the first concentrated water tank 9, the outlet of the first concentrated water tank 9 is communicated with an inlet pipeline of the ultrahigh pressure reverse osmosis device 10, the outlet of the reverse osmosis device 10 is communicated with a second concentrated water tank 11, and the produced water outlet of the reverse osmosis device 8 and the ultrahigh pressure water outlet of the ultrahigh pressure water tank 14 are communicated with an inlet pipeline of the produced water tank 14; the outlet of the second concentrated water tank 11 is communicated with the inlet pipeline of the ion exchange reaction device 12, the outlet of the ion exchange reaction device 12 is communicated with the inlet pipeline of the MVR evaporative crystallization device 13, and the condensed water outlet of the MVR evaporative crystallization device 13 is communicated with the inlet pipeline of the water production pool 14.
Although the content of organic matters in the biochemical effluent sent from the biochemical effluent pool 15 after being treated by the biochemical treatment unit is effectively reduced, a small amount of colloid or dissolved organic pollutants which are difficult to be biochemically degraded still remain in the water body; in order to remove the organic matters, an ozone advanced treatment process is added after biochemical treatment; the specific treatment process is as follows:
adding a coagulant in the process that biochemical effluent from the biochemical effluent pool 15 passes through the pipeline mixer 1, then entering the ozone air flotation device 2, catalyzing ozone by using the coagulant to generate hydroxyl radicals with strong oxidizing property, and further removing organic matters in wastewater; then two-stage filtration is realized through a filter 5 and an ultrafiltration device 6, then the wastewater is sent into an ultrafiltration water outlet tank 7 for caching, the wastewater in the ultrafiltration water outlet tank 7 is sent into a reverse osmosis device 8 for membrane filtration, the concentrated water discharged by the reverse osmosis device 8 is cached in a first concentrated water tank 9, then the concentrated water is filtered by an ultrahigh pressure reverse osmosis device 10 for ultrahigh pressure membrane filtration, the concentrated water is cached in a second concentrated water tank 11 and then sent to an ion exchange reaction device 12 for treatment, and then the concentrated water is sent to an MVR evaporative crystallization device 13 for evaporative crystallization to separate out crystal salt; the produced water of the reverse osmosis device 8 and the ultrahigh pressure reverse osmosis device 10 and the condensed water discharged by the MVR evaporative crystallization device 13 are stored in a water producing tank 14 as produced water and can be reused for production.
According to the system, organic matters in the wastewater are further removed through the ozone air flotation device 2, then, particle impurities in the wastewater are removed through two-stage filtration of sand filtration and ultrafiltration, and then, recyclable fresh water is separated from a sewage body through two-stage membrane filtration of reverse osmosis and ultrahigh pressure reverse osmosis so as to reduce the treatment capacity of high-concentration brine; concentrated water produced by membrane filtration is evaporated and desalted by adopting an MVR technology, so that inorganic salt is removed from a water body in a crystal form.
The overflow port of the buffer tank 4 is communicated with the inlet pipeline of the ozone vapor floating water outlet pool 3 to prevent the overflow caused by the over-high liquid level in the buffer tank 4.
The outlet of the water producing tank 14 is respectively communicated with the back flush inlet pipelines of the filter 5, the ultrafiltration device 6, the reverse osmosis device 8 and the ultrahigh pressure reverse osmosis device 10, and the back flush outlets of the filter 5, the ultrafiltration device 6, the reverse osmosis device 8 and the ultrahigh pressure reverse osmosis device 10 are all communicated with the inlet pipeline of the biochemical water outlet tank 15 through pipelines. The produced water in the water producing tank 14 can be used for backwashing the filter 5, the ultrafiltration device 6, the reverse osmosis device 8 and the ultrahigh-pressure reverse osmosis device 10, and then is sent back to the biochemical water outlet tank 15 for cyclic treatment; therefore, the fresh water source investment of the system is reduced, the system operation load is reduced, and the fresh water consumption is reduced.
The ion exchange reaction equipment 12 comprises a first ion exchange reactor 121, a second ion exchange reactor 122 and an ion exchange water outlet tank 123, wherein the inlet of the first ion exchange reactor 121 is communicated with the outlet pipeline of the second concentrated water tank 11, the outlet of the first ion exchange reactor 121 is communicated with the inlet pipeline of the second ion exchange reactor 122, the outlet of the second ion exchange reactor 122 is communicated with the inlet pipeline of the ion exchange water outlet tank 123, and the outlet of the ion exchange water outlet tank 123 is communicated with the inlet pipeline of the MVR evaporative crystallization device 13. That is, in this embodiment, the ion exchange device employs two-stage exchange, so as to further enhance the treatment effect.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications or substitutions do not depart from the scope of the invention in its corresponding aspects.
Claims (4)
1. The fracturing flow-back fluid advanced treatment unit is characterized by comprising a pipeline mixer, an ozone vapor floating device, an ozone vapor floating water outlet pool, a buffer tank, a filter, an ultrafiltration device, a super-filtration water tank, a reverse osmosis device, a first concentrated water tank, an ultrahigh pressure reverse osmosis device, a second concentrated water tank, ion exchange reaction equipment, an MVR evaporation crystallization device and a water production pool;
the outlet water of the biochemical water outlet tank is communicated with an inlet pipeline of the pipeline mixer, the outlet of the pipeline mixer is communicated with an inlet pipeline of the ozone vapor flotation device, the outlet of the ozone vapor flotation device is communicated with an inlet pipeline of the ozone vapor flotation water outlet tank, the outlet of the ozone vapor flotation water outlet tank is communicated with an inlet pipeline of the buffer tank, the outlet of the buffer tank is communicated with an inlet pipeline of the filter, the outlet of the filter is communicated with an inlet pipeline of the ultrafiltration device, the concentrated water outlet of the ultrafiltration device is communicated with an inlet pipeline of the buffer tank, the produced water of the ultrafiltration device is communicated with an inlet pipeline of the ultrafiltration water tank, the outlet of the ultrafiltration water tank is communicated with an inlet pipeline of the reverse osmosis device, the concentrated water outlet of the reverse osmosis device is communicated with the first concentrated water tank pipeline, the outlet of the first concentrated water tank is communicated with an inlet pipeline of the ultrahigh pressure reverse osmosis device, the outlet of the ultrahigh pressure reverse osmosis device is communicated with the second concentrated water tank pipeline, and the produced water outlet of the reverse osmosis device are communicated with an inlet pipeline of the produced water inlet pipeline of the reverse osmosis device; the outlet of the second concentrated water tank is communicated with the inlet pipeline of the ion exchange reaction equipment, the outlet of the ion exchange reaction equipment is communicated with the inlet pipeline of the MVR evaporative crystallization device, and the condensed water outlet of the MVR evaporative crystallization device is communicated with the inlet pipeline of the water production tank.
2. The advanced treatment unit for the fracturing flow-back fluid according to claim 1, wherein an overflow port of the buffer tank is communicated with an inlet pipeline of the ozone vapor floating water outlet pool.
3. The fracturing flow-back fluid advanced treatment unit according to claim 1 or 2, wherein the outlet of the water production tank is respectively communicated with the back flush inlet pipelines of the filter, the ultrafiltration device, the reverse osmosis device and the ultrahigh pressure reverse osmosis device, and the back flush outlets of the filter, the ultrafiltration device, the reverse osmosis device and the ultrahigh pressure reverse osmosis device are respectively communicated with the inlet pipeline of the biochemical water outlet tank through pipelines.
4. The deep treatment unit for the fracturing flow-back fluid according to claim 1 or 2, wherein the ion exchange reaction equipment comprises a first ion exchange reactor, a second ion exchange reactor and an ion exchange water outlet tank, wherein an inlet of the first ion exchange reactor is communicated with an outlet pipeline of a second concentrated water tank, an outlet of the first ion exchange reactor is communicated with an inlet pipeline of the second ion exchange reactor, an outlet of the second ion exchange reactor is communicated with an inlet pipeline of the ion exchange water outlet tank, and an outlet of the ion exchange water outlet tank is communicated with an inlet pipeline of the MVR evaporative crystallization device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222601679.2U CN218665629U (en) | 2022-09-28 | 2022-09-28 | Fracturing flow-back fluid advanced treatment unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222601679.2U CN218665629U (en) | 2022-09-28 | 2022-09-28 | Fracturing flow-back fluid advanced treatment unit |
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| Publication Number | Publication Date |
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| CN218665629U true CN218665629U (en) | 2023-03-21 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202222601679.2U Active CN218665629U (en) | 2022-09-28 | 2022-09-28 | Fracturing flow-back fluid advanced treatment unit |
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| CN (1) | CN218665629U (en) |
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