CN117326752A - High-efficient combination processing system of reuse of reclaimed water in high salt waste water - Google Patents
High-efficient combination processing system of reuse of reclaimed water in high salt waste water Download PDFInfo
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- CN117326752A CN117326752A CN202311499549.5A CN202311499549A CN117326752A CN 117326752 A CN117326752 A CN 117326752A CN 202311499549 A CN202311499549 A CN 202311499549A CN 117326752 A CN117326752 A CN 117326752A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 109
- 239000002351 wastewater Substances 0.000 title claims abstract description 66
- 150000003839 salts Chemical class 0.000 title claims description 11
- 238000012545 processing Methods 0.000 title claims description 4
- 239000012528 membrane Substances 0.000 claims abstract description 88
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 80
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 41
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000000034 method Methods 0.000 claims abstract description 26
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 24
- 238000004064 recycling Methods 0.000 claims abstract description 20
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 238000007254 oxidation reaction Methods 0.000 claims description 38
- 230000003647 oxidation Effects 0.000 claims description 34
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 20
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 14
- 239000010865 sewage Substances 0.000 claims description 12
- 239000000126 substance Substances 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 239000003814 drug Substances 0.000 claims description 7
- 239000003344 environmental pollutant Substances 0.000 claims description 7
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 7
- 239000011790 ferrous sulphate Substances 0.000 claims description 7
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 7
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 238000010979 pH adjustment Methods 0.000 claims description 7
- 231100000719 pollutant Toxicity 0.000 claims description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 230000033116 oxidation-reduction process Effects 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 3
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 229910001447 ferric ion Inorganic materials 0.000 claims description 3
- 229910001448 ferrous ion Inorganic materials 0.000 claims description 3
- 239000011259 mixed solution Substances 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 239000013618 particulate matter Substances 0.000 claims description 3
- 239000010802 sludge Substances 0.000 claims description 3
- 239000000243 solution Substances 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 claims description 2
- 230000006378 damage Effects 0.000 claims description 2
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 2
- 230000000717 retained effect Effects 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 25
- 238000005516 engineering process Methods 0.000 abstract description 11
- 238000004062 sedimentation Methods 0.000 abstract description 7
- 238000002203 pretreatment Methods 0.000 abstract 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 24
- 238000007726 management method Methods 0.000 description 13
- 229910052799 carbon Inorganic materials 0.000 description 8
- 239000007787 solid Substances 0.000 description 7
- 230000001590 oxidative effect Effects 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000003203 everyday effect Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 150000003254 radicals Chemical class 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000003373 anti-fouling effect Effects 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000004992 fission Effects 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000036284 oxygen consumption Effects 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- -1 hydroxyl free radical Chemical class 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000004792 oxidative damage Effects 0.000 description 1
- 239000002699 waste material 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
- C02F1/28—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
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F7/00—Aeration of stretches of water
Abstract
The invention provides a high-efficiency combined treatment system for recycling reclaimed water in high-salt wastewater, which comprises a pre-treatment system, a tubular ultrafiltration membrane system and a high-pressure anti-pollution membrane system, wherein the novel process technology of Fenton oxidation-neutralization adsorption-tubular ultrafiltration membrane system-high-pressure anti-pollution membrane component is used for replacing the traditional process technology of anaerobic-aerobic biological treatment-sedimentation tank-multi-medium filter-activated carbon filter-column ultrafiltration membrane component-reverse osmosis membrane component, so as to solve the pain points and problems of long process flow, low stability and reliability, low efficiency, complex operation management, low water yield recovery rate, large occupied area and the like of the conventional high-salt wastewater reclaimed water recycling treatment technology.
Description
Technical Field
The invention relates to the technical field of water environment treatment, in particular to a high-efficiency combined treatment system for recycling reclaimed water in high-salt wastewater.
Background
The conventional reclaimed water recycling treatment process technology for industrial enterprise production wastewater at present comprises the following steps: anaerobic/aerobic biological treatment, sedimentation tank, multi-medium filtration, active carbon filtration, column type ultrafiltration membrane component and reverse osmosis membrane component. The conventional treatment process technology has the problems of long process flow, poor stability and reliability, low treatment efficiency, complex operation management, low water yield recovery rate, large occupied area and the like.
For high-salinity wastewater, the wastewater has high salt content (TDS is more than 15000 mg/L), so that the growth and propagation of microorganisms can be seriously inhibited, the biological treatment-secondary sedimentation tank treatment effect is poor, and the efficiency is low.
The multi-medium, activated carbon filter and column type ultrafiltration membrane component adopted in the traditional treatment process are backwashed after the operation is stopped every day, so that a large amount of water sources are consumed, the recovery rate of the whole treatment system is reduced, and the operation and the management are complex; the filter materials of the multi-medium and active carbon filter are easy to harden and need to be replaced frequently, and the workload of system maintenance and management is increased.
Current patent publication No.: CN209468220U discloses a sewage treatment system, which reduces oil content, solid suspended matter content, chemical oxygen consumption in sewage through an air floatation integrated machine, reduces oil content, solid suspended matter content, iron content, alkalinity and hardness in sewage through a inclined tube sedimentation tank, reduces iron content, solid suspended matter content and oil content in sewage through a multimedia filter, an iron removal filter and an activated carbon filter, and is used for reducing the solid suspended matter content, chemical oxygen consumption and iron content in sewage through an ultrafiltration device, and is used for reducing the alkalinity, hardness and chlorine content in sewage through a reverse osmosis filter device, so that the recycling of sewage is realized.
However, the high-salt wastewater has higher salt content, the traditional low-pressure brackish water membrane component is used for recycling treatment, the operation pressure level is lower (1.55 MPa), the recovery rate of reverse osmosis produced water is very low, and the membrane component is limited by the flow channel design and the material process because pollutants such as COD (chemical oxygen demand) and the like of the pretreatment process wastewater are not thoroughly removed, so that the membrane is easy to be blocked, the membrane is frequently cleaned, the treatment efficiency is low, and the produced water is unstable.
In recent years, along with the development of various national and local policies, the environmental protection pressure of enterprises is gradually increased, the wastewater recycling requirement is higher and higher, and the process technology for seeking more conciseness, reliability, stability, high efficiency and high recovery rate is imperative. And because of the increasingly tense land resources of enterprises, the process technology with small occupied area becomes the priority choice.
Therefore, how to solve the problems of long process flow, low stability and reliability, low treatment efficiency, complex operation management, low water recovery rate, large occupied area and the like of the traditional reclaimed water reuse treatment technology.
Disclosure of Invention
In view of the above problems and difficulties, a set of high-efficiency combined treatment system for recycling water in high-salt wastewater is designed and developed, and the novel process technology of Fenton oxidation-neutralization adsorption-tubular ultrafiltration membrane system-high-pressure anti-pollution membrane component is used for replacing the traditional process technology of anaerobic-aerobic biological treatment-sedimentation tank-multi-medium filter-activated carbon filter-column ultrafiltration membrane component-reverse osmosis membrane component, so as to solve the pain and problems of long process flow, low stability and reliability, low efficiency, complex operation management, low water yield, large occupied area and the like in the conventional high-salt wastewater water recycling treatment technology.
The utility model provides a high-efficient combination processing system of reuse of reclaimed water in high salt waste water which characterized in that: comprising a pretreatment system, a tubular ultrafiltration membrane system 10 and a high-pressure anti-pollution membrane system 15, wherein the pretreatment system sequentially comprises the following components from front to back: PH adjustment tank 1, oxidation tank 3, neutralization tank 4 and concentration tank 5, PH adjustment tank 1, oxidation tank 3, neutralization tank 4 and concentration tank 5 are equipped with the delivery port intercommunication respectively on adjusting tank 1, oxidation tank 3, neutralization tank 4 and the concentration tank 5 respectively through PH, pretreatment system's input is connected with high salt waste pipe, pretreatment system's output connecting pipe formula milipore filter system 10's input, tubular milipore filter system 10's output is connected the input of high pressure antipollution membrane system 15, high pressure antipollution membrane system 15 output concentrate and produced water, produced water flows into follow-up retrieval and utilization pond, as enterprise retrieval and utilization water source.
Further, the water outlets respectively arranged on the PH adjusting tank 1, the oxidizing tank 3, the neutralizing tank 4 and the concentrating tank 5 are arranged in a vertically staggered way, which is beneficial to mixing materials in the oxidizing tank 3, the neutralizing tank 4 and the concentrating tank 5.
In some embodiments, the PH adjusting tank 1, the oxidation tank 3 and the neutralization tank 4 are respectively provided with a stirrer 2, and the materials flowing into the PH adjusting tank 1, the oxidation tank 3 and the neutralization tank 4 are uniformly mixed by the stirrer 2.
In some embodiments, dilute sulfuric acid and ferrous sulfate chemical are added into the PH adjusting tank 1, the high-salt wastewater firstly flows into the PH adjusting tank 1, dilute sulfuric acid and ferrous sulfate chemical are added into the PH adjusting tank 1, stirring and mixing are performed by the stirrer 2 in the PH adjusting tank 1, and the PH value of the wastewater is controlled by controlling the amounts of the dilute sulfuric acid and the ferrous sulfate chemical.
Further, the pH value in the pH adjusting tank 1 is in the range of 2.5-3.5.
In some embodiments, hydrogen peroxide agent is added into the oxidation tank 3; the wastewater in the PH adjusting tank 1 flows into the oxidation tank 3, the hydrogen peroxide agent is added into the oxidation tank 3 and is subjected to Fenton oxidation reaction with the wastewater in the PH adjusting tank 1, the wastewater is stirred and mixed by the stirrer 2 in the oxidation tank 3, and the oxidation-reduction potential of the wastewater is controlled by controlling the amount of the hydrogen peroxide agent in the oxidation tank 3.
Further, fenton catalytic oxidation reaction has the following action mechanism:
Fe 2+ +H 2 O 2 →Fe 3+ +·OH+OH -
2Fe 2+ +H 2 O 2 →2Fe 3+ +2OH -
Fe 3+ +H 2 O 2 →Fe 2+ +HO 2 ·H +
HO 2 ·+H 2 O 2 →O 2 +H 2 O+·OH
RH+OH→R+H 2 O
R·+O 2 →ROO+→…→CO 2 +H 2 O
specifically, fe 2+ And H is 2 O 2 The reaction is fast, and oxidation energy is generatedHydroxyl radical (OH) with very strong forces, followed by Fe 2+ Then is combined with H 2 O 2 Rapidly reacting to generate OH, reacting OH with organic matter RH in the wastewater to generate organic free radical R.R.further oxidizing to finally cause the organic matter structure to generate carbon chain fission and oxidation to CO 2 And H 2 O, thus greatly reducing COD of the wastewater, and the Fenton reaction can oxidize most organic matters indiscriminately.
At the same time Fe 2+ As catalyst, can finally be replaced by O 2 Oxidation to Fe 3+ During subsequent pH adjustment, fe (OH) is formed 3 Colloid with flocculation effect.
Further, the oxidation-reduction potential of the wastewater ranges from 300 mV to 500mV.
In some embodiments, caustic soda and powdered activated carbon agents are added into the neutralization tank 4, the wastewater after Fenton oxidation flows into the neutralization tank 4, and is stirred and mixed by the stirrer 2 in the neutralization tank 4, so that pollutants such as COD in the wastewater are further removed by utilizing the adsorption effect of activated carbon.
Further, the pH value of the wastewater in the neutralization tank 4 is 7.5-8.5.
In some embodiments, a concentrating tank aeration device 6 is arranged in the concentrating tank 5, the wastewater flowing into the concentrating tank 5 is aerated and oxygenated by the concentrating tank aeration device 6, and the ferrous ions which are not completely oxidized in the wastewater are completely oxidized into ferric ions to form Fe (OH) 3 floccules, so that residual pollutants in the water can be removed by adsorption bridging.
Further, the wastewater flowing into the concentration tank 5 is stopped and aerated for 2-3H, so that residual hydrogen peroxide in the water can be effectively digested and driven away, and the oxidation damage to the membrane component is avoided.
Further, the output end of the concentration tank 5 is also connected with a sewage treatment system, and the waste water which is not required to be treated by the tubular ultrafiltration membrane system 10 is discharged to the sewage treatment system.
In some embodiments, the concentration tank 5 and the tubular ultrafiltration membrane system 10 are sequentially provided with: the ultrafiltration feed pump 7, the pocket type filter 8, the ultrafiltration circulating pump 9, the input of ultrafiltration feed pump 7 is connected to the output of concentration tank 5, the input of pocket type filter 8 is connected to the output of ultrafiltration feed pump 7, the input of ultrafiltration circulating pump 9 is connected to the output of pocket type filter 8, the input of the output connecting pipe type milipore filter system 10 of ultrafiltration circulating pump 9 promotes concentration tank 5 mixed solution by ultrafiltration feed pump 7, filters big particle diameter particulate matter through pocket type filter 8, and the pressurization of again through ultrafiltration circulating pump 9 is carried to tubular milipore filter system 10 and is separated.
Further, the tubular ultrafiltration membrane system 10 is composed of a plurality of flow channels connected end to end, the solid content of the feed of the tubular ultrafiltration membrane system 10 is 2-5%, and the filtering precision is similar to that of the conventional column type ultrafiltration, but the unique structure and the flow channel design can enable the tubular ultrafiltration membrane system to bear high solid content of the feed.
In some embodiments, the output end of the tubular ultrafiltration membrane system 10 is further connected with the input end of the ultrafiltration circulation pump 9 and the concentration tank 5, most of the mud-water mixture intercepted by the tubular ultrafiltration membrane system 10 flows back to the front end of the ultrafiltration circulation pump 9, the ultrafiltration circulation pump 9 is utilized to circularly wash the membrane assembly in a large flow way, dirt blockage is avoided, the rest mud-water mixture returns to the front end concentration tank 5 to be mixed and concentrated with raw water, and the concentrated solution in the concentration tank 5 is periodically discharged to the sludge treatment system for treatment.
In some embodiments, an ultrafiltration water producing tank 11 is disposed between the tubular ultrafiltration membrane system 10 and the high-pressure anti-pollution membrane system 15, and the produced water of the tubular ultrafiltration membrane system 10 flows into the ultrafiltration water producing tank 11 as reverse osmosis raw water.
Further, a reverse osmosis water feeding pump 12, a cartridge filter 13 and a reverse osmosis high pressure pump 14 are further arranged between the tubular ultrafiltration membrane system 10 and the high pressure anti-pollution membrane system 15, the output end of the ultrafiltration water producing tank 11 is connected with the input end of the reverse osmosis water feeding pump 12, the output end of the reverse osmosis water feeding pump 12 is connected with the input end of the cartridge filter 13, the output end of the cartridge filter 13 is connected with the input end of the reverse osmosis high pressure pump 14, the output end of the reverse osmosis high pressure pump 14 is connected with the input end of the high pressure reverse osmosis membrane system, clean water in the ultrafiltration water producing tank 11 is lifted by the reverse osmosis water feeding pump 12, is trapped by the cartridge filter 13, no particulate matters in the water are guaranteed to remain, and is pressurized to the high pressure anti-pollution membrane system 15 by the reverse osmosis high pressure pump 14 for separation.
In some embodiments, the output end of the high-pressure anti-pollution membrane system 15 is also connected to the input end of the reverse osmosis high-pressure pump 14, a concentrated water pressure reducing valve 16 is arranged on a pipeline connected with the high-pressure anti-pollution membrane system 15 and the reverse osmosis high-pressure pump 14, the concentrated water of the high-pressure anti-pollution membrane system 15 is reduced in pressure by the concentrated water pressure reducing valve 16 and then partially flows back to the front end of the reverse osmosis high-pressure pump 14, so that the recovery rate of the reverse osmosis produced water is improved, and the residual concentrated water is discharged to a total sewage discharge port of a factory.
Further, the operating pressure of the high-pressure anti-pollution membrane system 15 is 5.5MPa, and the high-salt concentrated water can be concentrated to the salt content of 60000-80000mg/L.
Further, the reverse osmosis high-pressure pump 14 adopts an axial plunger pump, and the pressure of the reverse osmosis high-pressure pump 14 is 6.0-8.0MPa.
The beneficial effects of the invention are as follows: the invention replaces four process units of a sedimentation tank, a multi-medium filter, an active carbon filter and a column type ultrafiltration membrane component of the traditional process by combining the front-added powder active carbon with the tubular ultrafiltration membrane system 10 and the high-pressure anti-pollution membrane system 15, the traditional process has long flow, poor process stability, complex operation management and large occupied area, and the multi-medium, the active carbon filter and the column type ultrafiltration membrane component all need to be backwashed after the shutdown every day, a large amount of clean water is consumed, the recovery rate of the whole treatment system is reduced, and the operation and the management are complex; the multi-medium and activated carbon filter material is easy to harden and needs frequent replacement, and the workload of system maintenance and management is increased; the pipe type ultrafiltration membrane system 10 used in the invention has super-strong anti-fouling capability, can replace a plurality of process sections, does not need frequent backwashing, only needs periodic chemical cleaning (the chemical cleaning procedure is similar to the traditional ultrafiltration), greatly improves the treatment efficiency and stability, improves the water yield recovery rate of the system, reduces the operation and management strength, and greatly reduces the occupied area; the membrane component adopts ultra-wide flow channels and special flow channel structure design to increase the anti-pollution capability of the membrane, and simultaneously performs electric neutral modification on the surface of the membrane, thereby avoiding floating pollution of charged particles and further improving the pollution resistance thereof; thereby improving the treatment efficiency of the system and the stability of produced water.
Drawings
Fig. 1 is a system diagram of a high-efficiency combined treatment system for recycling reclaimed water in high-salt wastewater of the embodiment.
And (3) main component description:
the invention will be further described in the following detailed description in conjunction with the above-described figures.
Detailed Description
The following examples are described to aid in the understanding of the present application and are not, nor should they be construed in any way to limit the scope of the present application.
In the following description, those skilled in the art will recognize that components may be described as separate functional units (which may include sub-units) throughout this discussion, but those skilled in the art will recognize that various components or portions thereof may be divided into separate components or may be integrated together (including integration within a single system or component).
Meanwhile, the connection between components or systems is not intended to be limited to a direct connection. Rather, data between these components may be modified, reformatted, or otherwise changed by intermediate components. In addition, additional or fewer connections may be used. It should also be noted that the terms "coupled," "connected," or "input" are to be construed as including direct connection, indirect connection or fixation through one or more intermediaries.
In the description of the present application, it should be noted that, directions or positional relationships indicated by terms such as "center", "upper", "lower", "left", "right", "side", "vertical", "horizontal", "inner", "outer", etc., are directions or positional relationships based on those shown in the drawings, or directions or positional relationships as used or conventionally recognized in the product of the application, are merely for convenience of description of the present application and simplification of description, and are not indicative or implying that the apparatus or element to be referred to must have a specific direction, be configured and operated in a specific direction, and thus should not be construed as limiting the present application. Furthermore, the terms "first," "second," "third," and the like are used merely to distinguish between descriptions and should not be construed as indicating or implying relative importance. The terms "horizontal", "vertical" and the like do not denote that the component is required to be absolutely horizontal or overhanging, but may be slightly inclined. As "horizontal" merely means that its direction is more horizontal than "vertical", and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
As shown in FIG. 1, a system diagram of a high-efficiency combined treatment system for recycling reclaimed water in high-salt wastewater in the embodiment is shown.
The high-salt wastewater firstly flows into a PH adjusting tank 1, dilute sulfuric acid and ferrous sulfate medicament are added into the PH adjusting tank 1, and are stirred and mixed by a stirrer 2, and the PH value of the wastewater is controlled to be approximately equal to 3; the wastewater then flows into an oxidation tank 3, hydrogen peroxide agent is added into the oxidation tank 3, stirring and mixing are carried out through a stirrer 2, and the oxidation-reduction potential of the wastewater is controlled to be 300-500mV in the oxidation tank 3; fenton catalytic oxidation reaction occurs, and the action mechanism is as follows:
Fe 2+ +H 2 O 2 →Fe 3+ +·OH+OH -
2Fe 2+ +H 2 O 2 →2Fe 3+ +2OH -
Fe 3+ +H 2 O 2 →Fe 2+ +HO 2 ·+H +
HO 2 ·+H 2 O 2 →O 2 +H 2 O+·OH
RH+·OH→R·+H 2 O
R·+O 2 →ROO+→…→CO 2 +H 2 O
Fe 2+ and H is 2 O 2 The reaction is quick, and hydroxyl free radical (OH) with strong oxidizing ability is generated. Then Fe 2+ Then is combined with H 2 O 2 Rapidly reacting to generate OH, reacting OH with organic RH to generate organic free radical R, further oxidizing R to finally cause carbon chain fission of organic structure, oxidizing to CO 2 And H 2 O, thus greatly reducing COD of the wastewater, and the Fenton reaction can oxidize most organic matters indiscriminately.
At the same time Fe 2+ As catalyst, can finally be replaced by O 2 Oxidation to Fe 3+ During subsequent pH adjustment, fe (OH) is formed 3 Colloid with flocculation effect.
The wastewater after Fenton oxidation flows into a neutralization tank 4, alkali and powdered activated carbon medicaments are added into the neutralization tank 4, the mixture is stirred and mixed by a stirrer 2, pollutants such as COD (chemical oxygen demand) in the wastewater are further removed by utilizing the adsorption effect of activated carbon, the pH value of the wastewater is approximately equal to 8, the wastewater flows into a concentration tank 5, a concentration tank aeration device 6 is arranged in the concentration tank 5, the wastewater is aerated and oxygenated by the concentration tank aeration device 6, the ferrous ions which are not completely oxidized in the wastewater are completely oxidized into ferric ions, fe (OH) 3 flocs are formed, and residual pollutants in the water can be removed by adsorption bridging.
In addition, residual hydrogen peroxide in water can be effectively digested and driven away by long-time stay and aeration (about 2 hours), so that oxidative damage to the membrane component is avoided.
The mixed solution of the concentration tank 5 is lifted by an ultrafiltration feed pump 7, filtered by a bag filter 8 to remove particles with large particle size, pressurized by an ultrafiltration circulating pump 9 and conveyed to a tubular ultrafiltration membrane system 10 for separation.
The produced water of the tubular ultrafiltration membrane system 10 flows into an ultrafiltration production water tank 11 as reverse osmosis raw water. The filtration accuracy of the tubular ultrafiltration membrane system 10 is similar to conventional column ultrafiltration, but its unique construction and flow channel design allows it to withstand very high feed solids (up to 2-5%).
Most of the mud-water mixture intercepted by the tubular ultrafiltration membrane flows back to the front end of the ultrafiltration circulating pump 9, the ultrafiltration circulating pump 9 is utilized to circularly wash the membrane component in a large flow, the pollution and blockage are avoided, and the rest mud-water mixture returns to the front end concentration tank 5 to be mixed and concentrated with raw water. The concentrated solution in the concentrating tank 5 is periodically discharged to a sludge treatment system for treatment.
The clear water in the ultrafiltration water production tank 11 is lifted by the reverse osmosis water feeding pump 12, is intercepted by the cartridge filter 13, ensures no particulate matter residue in the water, and is pressurized by the reverse osmosis high-pressure pump 14 to the high-pressure anti-pollution membrane system 15 for separation.
The produced water of the high-pressure anti-pollution film system 15 flows into a subsequent reuse water tank to be used as an enterprise reuse water source. The high-pressure reverse osmosis concentrated water is reduced in pressure by the concentrated water reducing valve 16 and then partially flows back to the front end of the high-pressure pump, so that the recovery rate of the reverse osmosis produced water is improved, and the residual concentrated water is discharged to the total sewage discharge port of the factory.
The operating pressure of the high-pressure anti-pollution membrane system 15 reaches 5.5MPa, and the high-salt concentrated water can be concentrated to the salt content of 60000-80000mg/L; the pressure reverse osmosis high-pressure pump 14 adopts an axial plunger pump, and the highest pressure can reach 6.0-8.0MPa.
The beneficial effects of the invention are as follows: the invention replaces four process units of a sedimentation tank, a multi-medium filter, an active carbon filter and a column type ultrafiltration membrane component of the traditional process by combining the front-added powder active carbon with the tubular ultrafiltration membrane system 10 and the high-pressure anti-pollution membrane system 15, the traditional process has long flow, poor process stability, complex operation management and large occupied area, and the multi-medium, the active carbon filter and the column type ultrafiltration membrane component all need to be backwashed after the shutdown every day, a large amount of clean water is consumed, the recovery rate of the whole treatment system is reduced, and the operation and the management are complex; the multi-medium and activated carbon filter material is easy to harden and needs frequent replacement, and the workload of system maintenance and management is increased; the pipe type ultrafiltration membrane system 10 used in the invention has super-strong anti-fouling capability, can replace a plurality of process sections, does not need frequent backwashing, only needs periodic chemical cleaning (the chemical cleaning procedure is similar to the traditional ultrafiltration), greatly improves the treatment efficiency and stability, improves the water yield recovery rate of the system, reduces the operation and management strength, and greatly reduces the occupied area; the membrane component adopts ultra-wide flow channels and special flow channel structure design to increase the anti-pollution capability of the membrane, and simultaneously performs electric neutral modification on the surface of the membrane, thereby avoiding floating pollution of charged particles and further improving the pollution resistance thereof; thereby improving the treatment efficiency of the system and the stability of produced water.
The foregoing examples illustrate only a few embodiments of the invention and are described in detail herein without thereby limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the invention, which are all within the scope of the invention. Accordingly, the scope of protection of the present invention is to be determined by the appended claims.
Claims (10)
1. The utility model provides a high-efficient combination processing system of reuse of reclaimed water in high salt waste water which characterized in that: the device comprises a pretreatment system, a tubular ultrafiltration membrane system (10) and a high-pressure anti-pollution membrane system (15), wherein the pretreatment system sequentially comprises the following components from front to back: PH adjustment tank (1), oxidation tank (3), neutralization tank (4) and concentrated tank (5), PH adjustment tank (1), oxidation tank (3), neutralization tank (4) and concentrated tank (5) are respectively through PH adjustment tank (1), oxidation tank (3), neutralization tank (4) and concentrated tank (5) on be equipped with the delivery port intercommunication respectively, pretreatment system's input is connected with high salt wastewater pipe, pretreatment system's output connecting pipe formula milipore filter system (10)'s input, high pressure antipollution membrane system (15) input is connected to tubular milipore filter system (10's output, high pressure antipollution membrane system (15) output concentrate and produce water, produce water inflow follow-up retrieval and utilization pond, as enterprise's retrieval and utilization water source.
2. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 1, which is characterized in that:
the water outlets respectively arranged on the PH adjusting tank (1), the oxidation tank (3), the neutralization tank (4) and the concentration tank (5) are arranged in a vertically staggered mode, so that the mixing of materials in the oxidation tank (3), the neutralization tank (4) and the concentration tank (5) is facilitated, stirrers (2) are arranged in the PH adjusting tank (1), the oxidation tank (3) and the neutralization tank (4), and the materials flowing into the PH adjusting tank (1), the oxidation tank (3) and the neutralization tank (4) are uniformly mixed through the stirrers (2).
3. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 2, which is characterized in that: the method comprises the steps of adding dilute sulfuric acid and ferrous sulfate medicament into a PH adjusting tank (1), enabling high-salt wastewater to flow into the PH adjusting tank (1) at first, adding the dilute sulfuric acid and the ferrous sulfate medicament into the PH adjusting tank (1), stirring and mixing by a stirrer (2) in the PH adjusting tank (1), and controlling the PH value of the wastewater by controlling the amounts of the dilute sulfuric acid and the ferrous sulfate medicament, wherein the PH value in the PH adjusting tank (1) ranges from 2.5 to 3.5.
4. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 2, which is characterized in that: adding hydrogen peroxide medicament into the oxidation tank (3); the wastewater of the PH adjusting tank (1) flows into the oxidation tank (3), hydrogen peroxide agent is added into the oxidation tank (3) and is subjected to Fenton oxidation reaction with the wastewater of the PH adjusting tank (1), stirring and mixing are carried out through the stirrer (2) in the oxidation tank (3), the oxidation-reduction potential of the wastewater is controlled by controlling the amount of the added hydrogen peroxide agent in the oxidation tank (3), and the oxidation-reduction potential of the wastewater is 300-500mV.
5. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 1, which is characterized in that: adding caustic soda and powdered activated carbon medicament into the neutralization tank (4), enabling the wastewater subjected to Fenton oxidation to flow into the neutralization tank (4), stirring and mixing by using a stirrer (2) in the neutralization tank (4), and further removing pollutants such as COD (chemical oxygen demand) in the wastewater by utilizing the adsorption effect of activated carbon, wherein the pH value range of the wastewater in the neutralization tank (4) is 7.5-8.5.
6. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 1, which is characterized in that: the concentration tank (5) is internally provided with a concentration tank aeration device (6), the wastewater flowing into the concentration tank (5) is aerated and oxygenated by the concentration tank aeration device (6), ferrous ions which are not completely oxidized in the wastewater are completely oxidized into ferric ions to form Fe (OH) 3 floccules, residual pollutants in the water can be removed through adsorption bridging, the wastewater flowing into the concentration tank (5) stays and is aerated for 2-3H, residual hydrogen peroxide in the water can be effectively digested and driven away, and oxidation damage to a membrane component is avoided.
7. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 1, which is characterized in that: the concentration tank (5) and the tubular ultrafiltration membrane system (10) are sequentially provided with: ultrafiltration feed pump (7), bag filter (8), ultrafiltration circulating pump (9), the input of ultrafiltration feed pump (7) is connected to the output of concentrated groove (5), the input of bag filter (8) is connected to the output of ultrafiltration feed pump (7), the input of ultrafiltration circulating pump (9) is connected to the output of bag filter (8), the input of ultrafiltration circulating pump (9) output connecting pipe formula milipore filter system (10) promotes concentrated groove (5) mixed solution by ultrafiltration feed pump (7), filters large-particle diameter particulate matter through bag filter (8), pressurizes through ultrafiltration circulating pump (9) again, carries out the separation to tubular milipore filter system (10).
8. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 7, which is characterized in that: the output end of the tubular ultrafiltration membrane system (10) is also connected with the input end of the ultrafiltration circulating pump (9) and the concentration tank (5), most of the mud-water mixture intercepted by the tubular ultrafiltration membrane system (10) flows back to the front end of the ultrafiltration circulating pump (9), the ultrafiltration circulating pump (9) is utilized to circularly wash the membrane component in a large flow, the pollution and blockage are avoided, the residual mud-water mixture returns to the front end concentration tank (5) to be mixed and concentrated with raw water, and the concentrated solution in the concentration tank (5) is periodically discharged to the sludge treatment system for treatment.
9. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 1, which is characterized in that: the ultrafiltration membrane system comprises a tubular ultrafiltration membrane system (10) and a high-pressure anti-pollution membrane system (15), wherein an ultrafiltration water production tank (11) is arranged between the tubular ultrafiltration membrane system (10) and the high-pressure anti-pollution membrane system (15), produced water of the tubular ultrafiltration membrane system (10) flows into the ultrafiltration water production tank (11) and serves as reverse osmosis raw water, a reverse osmosis water feed pump (12), a security filter (13) and a reverse osmosis high-pressure pump (14) are also arranged between the tubular ultrafiltration membrane system (10) and the high-pressure anti-pollution membrane system (15), the output end of the ultrafiltration water production tank (11) is connected with the input end of the security filter (12), the output end of the security filter (13) is connected with the input end of the reverse osmosis high-pressure pump (14), the output end of the reverse osmosis high-pressure pump (14) is connected with the input end of the high-pressure reverse osmosis membrane system, the clear water in the ultrafiltration water production tank (11) is lifted by the reverse osmosis pump (12), no particulate matters in the water is retained by the security filter (13), and the water is pressurized to the high-pressure anti-pollution membrane system (15) through the reverse osmosis high-pressure pump (14) for separation.
10. The high-efficiency combined treatment system for recycling water in high-salt wastewater according to claim 9, which is characterized in that: the output end of the high-pressure anti-pollution membrane system (15) is also connected with the input end of the reverse osmosis high-pressure pump (14), a concentrated water pressure reducing valve (16) is arranged on a pipeline connected with the high-pressure anti-pollution membrane system (15) and the reverse osmosis high-pressure pump (14), the concentrated water of the high-pressure anti-pollution membrane system (15) is reduced in pressure through the concentrated water pressure reducing valve (16) and then partially flows back to the front end of the reverse osmosis high-pressure pump (14) so as to improve the recovery rate of reverse osmosis produced water, the residual concentrated water is discharged to the total sewage discharge port of a factory, the operating pressure of the high-pressure anti-pollution membrane system (15) is 5.5MPa, and the high-salt concentrated water can be concentrated to the salt content
60000-80000mg/L, the reverse osmosis high pressure pump (14) adopts an axial plunger pump, and the pressure of the reverse osmosis high pressure pump (14) is 6.0-8.0MPa.
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