CN114772826A - Reclaimed water resource recycling method - Google Patents
Reclaimed water resource recycling method Download PDFInfo
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- CN114772826A CN114772826A CN202210385633.3A CN202210385633A CN114772826A CN 114772826 A CN114772826 A CN 114772826A CN 202210385633 A CN202210385633 A CN 202210385633A CN 114772826 A CN114772826 A CN 114772826A
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- water
- reverse osmosis
- reclaimed water
- concentrated
- recycling
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 254
- 238000004064 recycling Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000000243 solution Substances 0.000 claims abstract description 41
- 239000012266 salt solution Substances 0.000 claims abstract description 40
- 239000005708 Sodium hypochlorite Substances 0.000 claims abstract description 28
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000001728 nano-filtration Methods 0.000 claims abstract description 27
- 239000002253 acid Substances 0.000 claims abstract description 26
- 239000002131 composite material Substances 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 239000004902 Softening Agent Substances 0.000 claims abstract description 20
- 239000003513 alkali Substances 0.000 claims abstract description 20
- 239000007800 oxidant agent Substances 0.000 claims abstract description 20
- 230000001590 oxidative effect Effects 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 8
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000000460 chlorine Substances 0.000 claims abstract description 7
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 7
- 239000012528 membrane Substances 0.000 claims description 118
- 238000001223 reverse osmosis Methods 0.000 claims description 104
- 239000000919 ceramic Substances 0.000 claims description 36
- 238000001471 micro-filtration Methods 0.000 claims description 36
- 238000006243 chemical reaction Methods 0.000 claims description 27
- 239000013535 sea water Substances 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 20
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 18
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 239000003814 drug Substances 0.000 claims description 16
- 239000002101 nanobubble Substances 0.000 claims description 15
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 8
- 238000005868 electrolysis reaction Methods 0.000 claims description 6
- 230000003139 buffering effect Effects 0.000 claims description 5
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 150000002500 ions Chemical class 0.000 claims description 3
- 230000000717 retained effect Effects 0.000 claims description 3
- 238000005292 vacuum distillation Methods 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 8
- 239000002245 particle Substances 0.000 description 7
- 238000003756 stirring Methods 0.000 description 7
- 238000002425 crystallisation Methods 0.000 description 5
- 230000008025 crystallization Effects 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000010842 industrial wastewater Substances 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- 239000006004 Quartz sand Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 239000013618 particulate matter Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 208000028659 discharge Diseases 0.000 description 2
- 239000002384 drinking water standard Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- -1 wherein Chemical compound 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/14—Alkali metal compounds
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/24—Halogens or compounds thereof
- C25B1/26—Chlorine; Compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/50—Processes
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
Abstract
The invention relates to a reclaimed water recycling method, which belongs to the technical field of reclaimed water treatment, and comprises the steps of pretreating reclaimed water, adding a composite strong oxidant and a softening agent, adjusting the pH value of the reclaimed water to a first set value, concentrating and separating the treated reclaimed water, carrying out nanofiltration separation on the concentrated water to obtain a monovalent salt solution and a divalent salt solution, evaporating and concentrating the monovalent salt solution, electrolyzing the distilled concentrated solution to obtain sodium hypochlorite and chlorine, wherein the sodium hypochlorite can be recycled as the composite strong oxidant, the divalent salt solution can be electrolyzed to obtain an acid solution and an alkali solution, the acid solution can be recycled for concentration and separation, and the alkali solution can be recycled as the softening agent.
Description
Technical Field
The invention belongs to the technical field of reclaimed water treatment, and particularly relates to a reclaimed water resource recycling method.
Background
In China, energy industries represented by coal-fired power generation, modern coal chemical industry and the like support the development of national economy, and simultaneously consume a large amount of water resources and generate a large amount of industrial wastewater. In recent years, with the increasing of the environmental protection work, how to safely and efficiently treat industrial wastewater becomes a major issue related to the health development of the industry. Especially in regions with water resource shortage and relatively fragile ecological environment, such as inner Mongolia, Shaanxi, Ningxia and Xinjiang, zero emission treatment of industrial wastewater becomes an increasingly urgent requirement.
At present, industrial wastewater is treated by a sewage plant to form reclaimed water, namely so-called reclaimed water, most of reclaimed water zero-discharge treatment technologies adopt 'multi-stage reverse osmosis membrane + evaporative concentration crystallization' to produce high-purity salts, the salts are separated in a form of crystallized salt and temporarily stored in a warehouse for waiting treatment, evaporated condensate water is subjected to biochemical treatment and then is recycled or discharged up to the standard, and reclaimed water recycling and zero discharge are realized. The reasonable reuse of the reclaimed water can reduce the environmental pollution of water and relieve the contradiction of water resource shortage, and is an important measure for implementing sustainable development. However, the evaporative crystallization system is adopted, so that the occupied area is large, the equipment investment and operation cost is high, the process is complex, and meanwhile, the temporarily stored waste salt belongs to hazardous waste.
Disclosure of Invention
In order to solve the above problems, a method for recycling reclaimed water is proposed.
In order to achieve the purpose, the invention provides the following technical scheme:
a reclaimed water resource recycling method comprises the following steps:
s100, pretreating the reclaimed water, adding a composite strong oxidant and a softening medicament, and adjusting the pH value of the reclaimed water to a first set value to obtain the pretreated reclaimed water;
s200, concentrating and separating the pretreated reclaimed water, and enabling the concentrated produced water to enter a reclaimed water recycling pool for recycling for later use;
s300, carrying out nanofiltration separation on the concentrated water to obtain monovalent salt solution and divalent salt solution;
s400, evaporating and concentrating the monovalent salt solution, electrolyzing the distilled concentrated solution to obtain sodium hypochlorite and chlorine, wherein the sodium hypochlorite can be recycled as a composite strong oxidant, and the distilled distillate enters a reclaimed water recycling pool to be recycled for later use;
and S500, electrolyzing the divalent salt solution to obtain acid liquor and alkali liquor, wherein the acid liquor can be recycled for concentration and separation, and the alkali liquor can be recycled as a softening agent.
The invention is further configured to: the composite strong oxidant is added into the first reaction tank, the reclaimed water reacts with the composite strong oxidant and stays for a first set time, the softening agent is added into the second reaction tank, and the reclaimed water reacts with the softening agent and stays for a second set time.
By adopting the technical scheme, the reclaimed water firstly reacts with the composite reinforcer, part of COD is oxidized, and after the COD stays for the first set time, the COD value of the oxidized reclaimed water is reduced by 70-80%, bacteria and microorganisms in the reclaimed water can be removed, and the pollution and blockage probability of the subsequent concentration process is reduced.
Then, the reclaimed water reacts with the softening medicament and stays for a second set time, so that calcium ions and magnesium ions in the reclaimed water fully react with the softening medicament to form precipitated particles.
The invention is further configured to: the composite strong oxidant is sodium hypochlorite and ozone, and the softening agent is one or any combination of two or more of sodium hydroxide, calcium hydroxide and sodium carbonate.
The invention is further configured to: the return water mixed with ozone is sprayed through the release spray head at a high pressure to form micro-nano bubbles, namely, the ozone is added into the first reaction tank in a micro-nano bubble form.
Through adopting above-mentioned technical scheme, micro-nano bubble disperses to first reaction tank uniformly, and micro-nano bubble rising speed reduces, and is higher in aquatic solubility, and dwell time is longer, can fully contact with the pollutant, improves the utilization ratio of ozone.
The invention is further configured to: and (3) monitoring the hardness value and alkalinity content of the reclaimed water on line, adding a softening agent, and stirring until the pH value of the reclaimed water in the second reaction tank is adjusted to 10.8, so that the low hardness of the discharged water is effectively ensured.
The invention is further configured to: sodium hypochlorite and soften the medicament and add through the medicament adds the pump, the medicament adds the pump and uses with the converter is supporting to with the online detector linkage of pH in order to adjust pH.
The invention is further configured to: the second reaction tank adopts a connected three-grid structure and comprises a first grid, a second grid and a third grid, the softening medicament is added into the first grid and the second grid respectively, and the third grid is used as a buffer grid.
Through adopting above-mentioned technical scheme, first check with the second check internal mixer stirs, makes softening medicament and return water intensive mixing and reaction, the third check is furnished with the mixer and stirs, prevents that the sediment particulate matter that the reaction generated is at the deposit.
The invention is further configured to: and the reclaimed water in the second reaction tank flows through the microfiltration ceramic membrane through the booster pump to be filtered.
By adopting the technical scheme, the micro-filtration ceramic membrane filters and removes precipitated particles, the purpose of removing hardness in the return water is realized, the micro-filtration ceramic membrane is adopted for filtration, a precipitation zone and a quartz sand filter are not required to be arranged after pretreatment, the process route is shortened, the occupied area is saved, and the hardness of the outlet water is less than 10mg/L after the filtration by the micro-filtration ceramic membrane.
The invention is further configured to: the reclaimed water permeating the micro-filtration ceramic membrane flows to a clear water outlet to form filtered clear liquid, the reclaimed water intercepted by the micro-filtration ceramic membrane flows to a concentration outlet to form filtered concentrated liquid, the concentration outlet is communicated with the water inlet end of the micro-filtration ceramic membrane through a circulation loop, and the clear water outlet and the concentration outlet form a cross flow structure.
The invention is further configured to: and the circulating pump with the flow which is many times of the flow of the water inlet end of the microfiltration ceramic membrane is arranged on the circulating loop, so that the water flow speed on the surface of the microfiltration ceramic membrane is improved to more than 5 m/s.
Through adopting above-mentioned technical scheme, improve the water velocity on micro-filtration ceramic membrane surface through the circulating pump, carry out large-traffic, quick washing away to micro-filtration ceramic membrane surface, prevent to deposit the particulate matter and pile up on micro-filtration ceramic membrane surface.
The invention is further configured to: the circulating pipelines of the filtered clear liquid and the filtered concentrated liquid are respectively provided with an electromagnetic flowmeter and an adjusting valve for detecting instantaneous flow and accumulated flow, the circulating pump frequency is adjusted through flow feedback signals, the circulating pipelines of the filtered clear liquid are provided with an online hardness detector and a turbidity meter, and the circulating pump frequency is adjusted through the online hardness detector feedback signals.
By adopting the technical scheme, the hardness of the filtered clear liquid can reach below 10ppm, and the turbidity is less than 1 NTU.
The invention is further configured to: and buffering the filtered clear liquid, adding acid liquor to adjust the pH value to a second set value to obtain pretreated reclaimed water, and staying for a third set time.
Through adopting above-mentioned technical scheme, too high pH can influence the desalination performance of brackish water reverse osmosis membrane and sea water reverse osmosis membrane, adds the acidizing fluid and adjusts pH to 9.5, guarantees that the pH of reverse osmosis dense water is less than 11, neither influences the membrane performance, can make the silicon in the aquatic keep the dissolved state again, can not cause reverse osmosis membrane dirt because of the scale deposit and block up.
Meanwhile, the clear filtrate stays for a third set time to play a role in removing hardness, and the calcium and magnesium slightly-soluble salts are prevented from being precipitated after reaching the saturation solubility in the reverse osmosis process to block the reverse osmosis membrane.
The invention is further configured to: the pretreated reclaimed water sequentially flows through the brackish water reverse osmosis membrane and the seawater reverse osmosis membrane through the booster pump to carry out reverse osmosis treatment, so that concentration and separation are realized.
The invention is further configured to: the filtration clear solution after the buffering treatment gets into the filter through the booster pump and filters, and the bitter water reverse osmosis membrane of rethread high-pressure pump flow through, bitter water reverse osmosis membrane adopts multilevel structure, sets up the booster pump between the bitter water reverse osmosis membrane of adjacent two-stage, carries out the pressure boost to preceding stage bitter water reverse osmosis membrane's dense water, guarantees rear stage bitter water reverse osmosis membrane's operating performance and water yield.
The invention is further configured to: and concentrating the filtered clear liquid subjected to buffer treatment by a brackish water reverse osmosis membrane by 3.5-4 times to form primary reverse osmosis produced water and primary reverse osmosis concentrated water, and feeding the primary reverse osmosis produced water into a reclaimed water recycling pool.
The invention is further configured to: concentrated water of one-level reverse osmosis gets into the filter through the booster pump and filters, and the sea water reverse osmosis membrane of rethread high-pressure pump flow through, sea water reverse osmosis membrane adopts the multilevel structure, sets up the booster pump between the sea water reverse osmosis membrane of adjacent two-stage, carries out the pressure boost to the concentrated water of preceding stage sea water reverse osmosis membrane, guarantees back level sea water reverse osmosis membrane's running performance and water yield.
The invention is further configured to: the first-stage reverse osmosis concentrated water is concentrated by a seawater reverse osmosis membrane for 2 times to form second-stage reverse osmosis produced water and second-stage reverse osmosis concentrated water, and the second-stage reverse osmosis produced water enters a reclaimed water recycling pool.
The invention is further configured to: and recovering the high-pressure energy of the secondary reverse osmosis concentrated water, and using the high-pressure energy to improve the pressure of the water inlet end of the seawater reverse osmosis membrane, reduce the energy consumption of the high-pressure pump and reduce the operating cost.
The invention is further configured to: the circulation pipelines of the first-stage reverse osmosis water production, the first-stage reverse osmosis concentrated water, the second-stage reverse osmosis water production and the second-stage reverse osmosis concentrated water are all provided with electromagnetic flow meters to detect instantaneous flow and accumulated flow, the frequency of the high-pressure pump is adjusted through flow feedback signals, and the water yield is ensured when the performance of the reverse osmosis membrane changes.
The invention is further configured to: and the circulation pipelines for the first-stage reverse osmosis water production and the second-stage reverse osmosis water production are provided with conductivity meters to monitor the water quality in real time.
By adopting the technical scheme, the brackish water reverse osmosis membrane and the seawater reverse osmosis membrane are combined, more than 85% of filtered clear liquid is recycled to the reclaimed water recycling pool, and the water quality of the reclaimed water recycling pool is far better than the ionic index requirement in the domestic drinking water standard.
The invention is further configured to: the concentrated water of second grade reverse osmosis gets into the filter through the booster pump and filters, and rethread high-pressure pump flows through and receives the filter membrane, receive the filter membrane and adopt multistage structure, set up the booster pump between the filter membrane of adjacent two-stage, carry out the pressure boost to the concentrated water of preceding stage nanofiltration membrane, guarantee the operating performance and the water yield of back stage nanofiltration membrane.
The invention is further configured to: and (3) nanofiltration separation of the secondary reverse osmosis concentrated water by a nanofiltration membrane to obtain a monovalent salt solution and a divalent salt solution, wherein the monovalent salt solution is mainly a sodium chloride solution, and the divalent salt solution is mainly a sodium sulfate solution.
The invention is further configured to: and the circulation pipelines of the monovalent salt solution and the divalent salt solution are respectively provided with an electromagnetic flowmeter, instantaneous flow and accumulated flow are detected, the frequency of the high-pressure pump is adjusted through flow feedback signals, and the water yield is ensured when the performance of the nanofiltration membrane is changed.
The invention is further configured to: and the flow pipelines of the monovalent salt solution and the divalent salt solution are respectively provided with a conductivity meter to monitor the water quality in real time.
By adopting the technical scheme, the monovalent salt and the divalent salt are separated by the nanofiltration membrane, so that the recycling according to quality is realized.
The invention is further configured to: the monovalent salt solution is evaporated and concentrated in a low-temperature distillation mode, the distilled distillate enters a reclaimed water recycling pool to be reused in enterprises, the concentration of the distilled concentrated solution reaches over 26 percent, and the distilled concentrated solution is lifted to an ion membrane electrolytic cell through a booster pump to be electrolyzed to prepare sodium hypochlorite and chlorine.
Through adopting above-mentioned technical scheme, need not to evaporate the crystallization and handle, avoid the polluted environment, but sodium hypochlorite retrieval and utilization is as compound strong oxidizer, and simultaneously, remaining sodium hypochlorite can supply the disinfection oxidation of enterprise to use.
The invention is further configured to: the divalent salt solution is lifted to the bipolar membrane electrolytic cell by a booster pump to prepare acid solution and alkali solution.
By adopting the technical scheme, the acid liquor can be reused for buffer treatment, the alkali liquor can be reused as a softening agent, and the residual acid liquor and alkali liquor can be used for sale.
In summary, compared with the prior art, the invention has the following beneficial effects:
1. by combining the pretreatment, concentration and separation, nanofiltration separation, evaporation concentration and electrolysis processes, products in all links are reasonably treated and recycled on the basis of realizing zero emission, and the aim of recycling reclaimed water is fulfilled.
2. The reclaimed water reacts with the composite reinforcer firstly, the COD value of the oxidized reclaimed water is reduced by 70-80%, bacteria and microorganisms in the reclaimed water can be removed, the pollution and blockage probability of a subsequent concentration process is reduced, and then the reclaimed water reacts with the softening agent, so that calcium ions and magnesium ions in the water fully react with the softening agent to form precipitated particles.
3. Ozone is added into water in a micro-nano bubble form, the rising speed of the micro-nano bubbles is reduced, the ozone can be fully contacted with pollutants, and the utilization rate of the ozone is improved.
4. The reclaimed water firstly passes through the microfiltration ceramic membrane, a precipitation zone and a quartz sand filter are not required to be arranged after the chemical reaction, the reclaimed water treatment process is shortened, the reclaimed water treatment efficiency is improved, and meanwhile, the occupied area is saved.
5. The brackish water reverse osmosis membrane is combined with the seawater reverse osmosis membrane, so that more than 85% of reclaimed water is recycled and flows to the reclaimed water recycling tank, the water inflow of nanofiltration separation is reduced, the treatment capacity of nanofiltration separation, evaporative concentration and electrolysis processes is reduced, and the treatment efficiency is improved.
6. And a nanofiltration salt separating mechanism is adopted to separate monovalent salt and divalent salt, so that quality-based recycling is realized.
7. Evaporation crystallization treatment is not needed, environment pollution is avoided, operation is convenient, and system floor area is reduced.
Drawings
FIG. 1 is a block flow diagram of the present invention;
FIG. 2 is a schematic diagram of a pretreatment configuration;
FIG. 3 is a schematic structural diagram of a brackish water reverse osmosis membrane and a seawater reverse osmosis membrane;
FIG. 4 is a schematic diagram of the structure of nanofiltration salt separation, evaporative concentration and electrolytic treatment.
In the drawings: the system comprises a raw water tank 1, a raw water tank 2, an ozone generator 3, a first reaction tank 4, a second reaction tank 4, a sodium hypochlorite adding port 5, a sodium hydroxide adding port 6, a sodium carbonate adding port 7, a microfiltration ceramic membrane 8, a buffer tank 9, an acid liquor adding port 10, a brackish water reverse osmosis membrane 11, a concentrated water buffer tank 12, a seawater reverse osmosis membrane 13, a reclaimed water recycling tank 14, a concentrated water buffer tank 15, a nanofiltration membrane 16, an evaporation concentration mechanism 17, an ionic membrane electrolytic tank 18, a sodium hypochlorite storage tank 19, a bipolar membrane electrolytic tank 20, an acid liquor storage tank 21 and an alkali liquor storage tank 22.
Detailed Description
In order to make the technical solutions of the present invention better understood, the following description of the technical solutions of the present invention with reference to the accompanying drawings of the present invention is made clearly and completely, and other similar embodiments obtained by a person of ordinary skill in the art without any creative effort based on the embodiments in the present application shall fall within the protection scope of the present application. In addition, directional terms such as "upper", "lower", "left", "right", etc. mentioned in the following embodiments are directions with reference to the drawings only, and thus, the directional terms used are intended to illustrate rather than limit the inventive concept.
Examples
As shown in fig. 1 to 4, a method for recycling reclaimed water includes the following steps:
s100, pretreating reclaimed water, adding a composite strong oxidant and a softening agent, and adjusting the pH value of the reclaimed water to a first set value to obtain pretreated reclaimed water;
s200, concentrating and separating the pretreated reclaimed water, and enabling the concentrated produced water to enter a reclaimed water recycling pool for recycling for later use;
s300, carrying out nanofiltration separation on the concentrated water to obtain monovalent salt solution and divalent salt solution;
s400, evaporating and concentrating monovalent salt solution, electrolyzing the distilled concentrated solution to obtain sodium hypochlorite and chlorine, wherein the sodium hypochlorite can be recycled as a composite strong oxidant, and the distilled distillate enters a reclaimed water recycling pool to be recycled for later use;
and S500, electrolyzing the divalent salt solution to obtain acid liquor and alkali liquor, wherein the acid liquor can be recycled for concentration and separation, and the alkali liquor can be recycled as a softening agent.
Specifically, as shown in fig. 2, reclaimed water firstly enters a raw water tank 1 to be collected, the composite strong oxidant is added into a first reaction tank 3, the reclaimed water reacts with the composite strong oxidant and stays for a first set time, the softening agent is added into a second reaction tank 4, and the reclaimed water reacts with the softening agent and stays for a second set time.
The reclaimed water reacts with the composite reinforcer, part of COD is oxidized, and after the COD stays for 10-20min (namely the first set time), the COD value of the oxidized reclaimed water is reduced by 70% -80%, bacteria and microorganisms in the reclaimed water can be removed, and the pollution and blockage probability of the subsequent concentration process is reduced. Then, the reclaimed water reacts with the softening medicament and stays for a second set time, so that calcium ions and magnesium ions in the reclaimed water fully react with the softening medicament to form precipitated particles.
Specifically, the composite strong oxidant is sodium hypochlorite and ozone, and in this embodiment, the first reaction tank 3 is provided with a sodium hypochlorite addition port 5 and an ozone addition port. The softening agent is one or any combination of two or more of sodium hydroxide, calcium hydroxide and sodium carbonate, and in this embodiment, the second reaction tank 4 is provided with a sodium hydroxide adding port 6 and a sodium carbonate adding port 7.
The return water mixed with ozone is sprayed through the release nozzle at a high pressure to form micro-nano bubbles, that is, the ozone is added into the first reaction tank 3 in the form of the micro-nano bubbles. The micro-nano bubbles are uniformly dispersed into the first reaction tank 3, the rising speed of the micro-nano bubbles is reduced, the micro-nano bubbles are higher in solubility in water, the retention time is longer, the micro-nano bubbles can be fully contacted with pollutants, and the utilization rate of ozone is improved.
The releasing spray head comprises a first generating plate and a second generating plate, wherein the first generating plate and the second generating plate are provided with pressure releasing holes, the first generating plate and the second generating plate are arranged at intervals to form a pressure releasing space, the number of the pressure releasing holes in the first generating plate is less than that of the pressure releasing holes in the second generating plate, return water mixed with ozone sequentially passes through the first generating plate and the second generating plate, passes through the pressure releasing holes in the first generating plate and then passes through the pressure releasing holes in the second generating plate, and pressure is released to multiple holes from few holes so as to form micro-nano bubbles.
The releasing spray head further comprises a generating column, a plurality of spiral holes penetrating through the generating column are formed in the generating column, the number of the spiral holes is less than that of the pressure releasing holes in the first generating plate, so that the water pressure of return water mixed with ozone when the return water passes through the spiral holes in the generating column is less than that when the return water passes through the pressure releasing holes in the first generating plate, namely, a pressure releasing process is added, and therefore the ozone can more fully form micro-nano bubbles.
Specifically, the hardness value and the alkalinity content of the reclaimed water are monitored on line, a softening agent is added, and stirring is carried out until the pH value of the reclaimed water in the second reaction tank 4 is adjusted to 10.8 (a first preset value), so that the low hardness of the discharged water is effectively ensured. Sodium hypochlorite and soften the medicament and add through the medicament adds the pump, the medicament adds the pump and uses with the converter is supporting to with the online detector linkage of pH in order to adjust pH.
Specifically, the second reaction tank 4 adopts a connected three-grid structure, and comprises a first grid, a second grid and a third grid, wherein the softening agent is added into the first grid and the second grid respectively, and the third grid is used as a buffer grid. The first grid and the second grid are internally provided with a stirrer for stirring, the reaction lasts for 10-20min, the softening medicament and the backwater are fully mixed and react, the third grid is provided with a stirrer for stirring, and the stirring lasts for 20-30min, so that the deposition of the precipitated particles generated by the reaction is prevented.
The bottom of the first grid is communicated with the bottom of the second grid, and the top of the second grid is communicated with the third grid through an overflow port. The bottom of third check is equipped with the drain, the drain passes through pipeline and dredge pump intercommunication, and the dredge pump mainly is used for the clearance to fall sedimentary sediment particulate matter and remaining return water.
Specifically, as shown in fig. 2 and 3, the reclaimed water in the second reaction tank 4 passes through the microfiltration ceramic membrane 8 for filtration treatment by the booster pump, and then passes through the brackish water reverse osmosis membrane 11 and the seawater reverse osmosis membrane 13 for reverse osmosis treatment by the booster pump in sequence, thereby realizing concentration and separation.
The reclaimed water permeating through the microfiltration ceramic membrane 8 flows to a clear water outlet to form filtered clear liquid, the reclaimed water intercepted by the microfiltration ceramic membrane 8 flows to a concentration outlet to form filtered concentrated liquid, the concentration outlet is communicated with the water inlet end of the microfiltration ceramic membrane through a circulation loop, and the clear water outlet and the concentration outlet form a cross flow structure. The circulation loop is provided with a circulation pump with the flow which is multiplied by the flow of the water inlet end of the microfiltration ceramic membrane 8, the water inlet end of the microfiltration ceramic membrane 8 is positioned at the bottom of the circulation loop, the clear water outlet is positioned at the top of the microfiltration ceramic membrane 8, and the concentration outlet is positioned at the side part of the microfiltration ceramic membrane 8. Preferably, the flow rate of the circulating pump is 4-8 times of the flow rate of the water inlet end of the microfiltration ceramic membrane 8, and the water flow rate on the surface of the microfiltration ceramic membrane 8 is increased to more than 5 m/s.
The micro-filtration ceramic membrane 8 filters and removes the precipitated particles, so that the purpose of removing the hardness in the return water is realized, the micro-filtration ceramic membrane 8 is adopted for filtration, a precipitation zone and a quartz sand filter are not required to be arranged, the process route is shortened, the occupied area is saved, and the hardness of the outlet water is less than 10mg/L after the outlet water is filtered by the micro-filtration ceramic membrane 8. Meanwhile, the water flow rate on the surface of the microfiltration ceramic membrane 8 is improved through the circulating pump, the surface of the microfiltration ceramic membrane 8 is subjected to large-flow and quick washing, and the deposition of particles on the surface of the microfiltration ceramic membrane 8 is prevented.
Specifically, an electromagnetic flowmeter and an adjusting valve are arranged on the circulating pipelines for filtering the clear liquid and the concentrated liquid, instantaneous flow and accumulated flow are detected, the frequency of the circulating pump is adjusted through flow feedback signals, an online hardness detector and a turbidity meter are arranged on the circulating pipelines for filtering the clear liquid, and the frequency of the circulating pump is adjusted through the feedback signals of the online hardness detector. The hardness of the filtered clear liquid can reach below 10ppm, and the turbidity is less than 1 NTU.
Specifically, the filtered clear liquid enters the buffer tank 9 for buffering, acid liquor is added to adjust the pH to a second set value, and the pH stays for a third set time, in this embodiment, the buffer tank 9 is provided with an acid liquor adding port 10. Too high pH can influence the desalination performance of brackish water reverse osmosis membrane 11 and sea water reverse osmosis membrane 13, adds acidizing fluid and adjusts pH to 9.5 (be the second setting value), guarantees that the pH of reverse osmosis dense water is less than 11, neither influences the membrane performance, can make the silicon in the aquatic keep the dissolved state again, can not cause reverse osmosis membrane dirt to block up because of the scale deposit. Meanwhile, the clear filtrate is retained for 60-90min (namely the third set time), so that the effect of removing hardness is achieved, and calcium and magnesium slightly-soluble salts are prevented from being precipitated after reaching the saturation solubility in the reverse osmosis process to block the reverse osmosis membrane.
Specifically, the clear liquid that filters after the buffering treatment gets into the filter through the booster pump and filters, and rethread high-pressure pump flows through brackish water reverse osmosis membrane 11, brackish water reverse osmosis membrane 11 adopts multistage structure, sets up the booster pump between the brackish water reverse osmosis membrane 11 of adjacent two-stage, carries out the pressure boost to the dense water of preceding level brackish water reverse osmosis membrane 11, guarantees the running property and the water yield of the brackish water reverse osmosis membrane 11 of back level.
And concentrating the filtered clear liquid subjected to the buffer treatment by a brackish water reverse osmosis membrane 11 by 3.5-4 times to form primary reverse osmosis produced water and primary reverse osmosis concentrated water, and enabling the primary reverse osmosis produced water to enter a reclaimed water recycling pool 14.
Specifically, the concentrated water of one-level reverse osmosis gets into first concentrated water buffer pool 12 and gets into the filter through the booster pump and filters, and the sea water reverse osmosis membrane 13 of rethread high-pressure pump flow through, sea water reverse osmosis membrane 13 adopts multistage structure, sets up the booster pump between the sea water reverse osmosis membrane 13 of adjacent two-stage, carries out the pressure boost to the concentrated water of the sea water reverse osmosis membrane 13 of preceding stage, guarantees the operating property and the water yield of the sea water reverse osmosis membrane 13 of back stage.
The first-stage reverse osmosis concentrated water is concentrated by a seawater reverse osmosis membrane 13 by 2 times to form a second-stage reverse osmosis produced water and a second-stage reverse osmosis concentrated water, and the second-stage reverse osmosis produced water enters a reclaimed water recycling pool 14. Meanwhile, the high-pressure energy of the secondary reverse osmosis concentrated water is recycled and used for increasing the pressure of the water inlet end of the seawater reverse osmosis membrane, reducing the energy consumption of the high-pressure pump and reducing the operating cost.
Specifically, electromagnetic flowmeters are respectively arranged on circulation pipelines of the first-stage reverse osmosis water production, the first-stage reverse osmosis concentrated water, the second-stage reverse osmosis water production and the second-stage reverse osmosis concentrated water, instantaneous flow and accumulated flow are detected, the frequency of the high-pressure pump is adjusted through a flow feedback signal, and the water yield is ensured when the performance of the reverse osmosis membrane changes. Meanwhile, the circulation pipelines of the first-stage reverse osmosis water production and the second-stage reverse osmosis water production are respectively provided with a conductivity meter for monitoring the water quality in real time.
The bitter salt water reverse osmosis membrane 11 and the seawater reverse osmosis membrane 13 are combined, more than 85% of filtered clear liquid is recycled to the reclaimed water recycling pool, and the water quality of the reclaimed water recycling pool 14 is far better than the ion index requirement in the domestic drinking water standard.
Specifically, as shown in fig. 3 and 4, the concentrated water of second grade reverse osmosis gets into second concentrated water buffer pool 15 and gets into the filter through the booster pump and filters, and rethread high-pressure pump flows through nanofiltration membrane 16, nanofiltration membrane 16 adopts multi-stage structure, sets up the booster pump between the nanofiltration membrane 16 of adjacent two-stage, carries out the pressure boost to the concentrated water of preceding stage's nanofiltration membrane 16, guarantees the operating performance and the water yield of the nanofiltration membrane 16 of back level.
And the secondary reverse osmosis concentrated water is subjected to nanofiltration separation by a nanofiltration membrane 16 to obtain monovalent salt solution and divalent salt solution, so that quality-based recycling is realized. Wherein the monovalent salt solution is mainly sodium chloride solution, and the divalent salt solution is mainly sodium sulfate solution. And the circulation pipelines of the monovalent salt solution and the divalent salt solution are respectively provided with an electromagnetic flowmeter, instantaneous flow and accumulated flow are detected, the frequency of the high-pressure pump is adjusted through flow feedback signals, and the water yield is ensured when the performance of the nanofiltration membrane is changed. Meanwhile, the flow pipelines of the monovalent salt solution and the divalent salt solution are both provided with conductivity meters to monitor the water quality in real time.
Specifically, monovalent salt solution enters into evaporative concentration mechanism 17 and carries out evaporative concentration through the mode of cryogenic distillation, and distilled distillate gets into reuse of reclaimed water pond 14 and recycles in the enterprise, and the concentrate concentration after the distillation reaches more than 26%, and the concentrate after the distillation promotes to ionic membrane electrolysis cell 18 through the booster pump and carries out the electrolysis and make sodium hypochlorite and chlorine, wherein, sodium hypochlorite storage is to sodium hypochlorite storage tank 19 in, just sodium hypochlorite storage tank 19 can with sodium hypochlorite interpolation mouth 5 is connected. Need not to evaporate the crystallization and handle, avoid the polluted environment, but sodium hypochlorite retrieval and utilization is as compound strong oxidizer, and simultaneously, remaining sodium hypochlorite can supply the disinfection oxidation of enterprise to use.
Specifically, a divalent salt solution is lifted to the bipolar membrane electrolytic cell 20 through the booster pump to prepare an acid solution and an alkali solution, the acid solution is stored in the acid solution storage tank 21, the acid solution storage tank 21 can be connected with the acid solution adding port 10, the acid solution is reused for buffer treatment, the alkali solution is stored in the alkali solution storage tank 22, the alkali solution storage tank 22 can be connected with the sodium hydroxide adding port 6, the alkali solution is reused as a softening agent, and the remaining acid solution and the remaining alkali solution can be sold.
In conclusion, the pretreatment, concentration and separation, nanofiltration separation, evaporation and concentration are combined with the electrolysis process, so that products in all links are reasonably treated and recycled on the basis of realizing zero emission, and the aim of recycling reclaimed water is fulfilled.
While the invention has been described in detail in connection with what is presently considered to be the most practical and preferred embodiment, it is to be understood that the invention is not to be limited to the disclosed embodiment, but on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims.
Claims (10)
1. A reclaimed water resource recycling method is characterized by comprising the following steps:
s100, pretreating the reclaimed water, adding a composite strong oxidant and a softening medicament, and adjusting the pH value of the reclaimed water to a first set value to obtain the pretreated reclaimed water;
s200, concentrating and separating the pretreated reclaimed water, and enabling the concentrated produced water to enter a reclaimed water recycling pool for recycling for later use;
s300, carrying out nanofiltration separation on the concentrated water to obtain monovalent salt solution and divalent salt solution;
s400, evaporating and concentrating the monovalent salt solution, electrolyzing the distilled concentrated solution to obtain sodium hypochlorite and chlorine, wherein the sodium hypochlorite can be recycled as a composite strong oxidant, and the distilled distillate enters a reclaimed water recycling pool to be recycled for later use;
and S500, electrolyzing the divalent salt solution to obtain acid liquor and alkali liquor, wherein the acid liquor can be recycled for concentration and separation, and the alkali liquor can be recycled as a softening medicament.
2. The method for recycling reclaimed water as claimed in claim 1, wherein in step S100, the composite strong oxidant is added to a first reaction tank, reclaimed water reacts with the composite strong oxidant and stays there for a first set time, the softener is added to a second reaction tank, the pH of the reclaimed water is adjusted to a first set value, and the reclaimed water reacts with the softener and stays there for a second set time.
3. The method for recycling reclaimed water as claimed in claim 2, wherein the composite strong oxidant is sodium hypochlorite and ozone, the softening agent is one or a combination of two or more of sodium hydroxide, calcium hydroxide and sodium carbonate, and the ozone is added into the first reaction tank in the form of micro-nano bubbles.
4. The recycled water resource recycling method according to claim 3, wherein recycled water passes through the microfiltration ceramic membrane through the second reaction tank for filtration treatment, the recycled water permeating the microfiltration ceramic membrane flows to a clear water outlet to form a clear filtered liquid, the recycled water retained by the microfiltration ceramic membrane flows to a concentrated outlet to form a filtered concentrated solution, the concentrated outlet is communicated with the water inlet end of the microfiltration ceramic membrane through a circulation loop, the circulation loop is provided with a circulation pump with the flow rate being multiple times of the flow rate of the water inlet end of the microfiltration ceramic membrane, and the water flow rate on the surface of the microfiltration ceramic membrane is increased to more than 5 m/s.
5. The method for recycling reclaimed water as claimed in claim 4, wherein the filtered clear solution is buffered, and acid solution is added to adjust the pH value to a second set value to obtain the pretreated reclaimed water, and the pretreated reclaimed water is retained for a third set time.
6. The method for recycling the reclaimed water as claimed in any one of claims 1 to 5, wherein in the step S200, the pretreated reclaimed water sequentially flows through the brackish water reverse osmosis membrane and the seawater reverse osmosis membrane through the booster pump to perform reverse osmosis treatment, so as to realize concentration and separation.
7. The method for recycling the reclaimed water as claimed in claim 6, wherein the pretreated reclaimed water is concentrated by a brackish water reverse osmosis membrane by 3.5-4 times to form primary reverse osmosis produced water and primary reverse osmosis concentrated water, the primary reverse osmosis concentrated water is concentrated by a seawater reverse osmosis membrane by 2 times to form secondary reverse osmosis produced water and secondary reverse osmosis concentrated water, and the primary reverse osmosis produced water and the secondary reverse osmosis produced water both enter a reclaimed water recycling pool.
8. The method for recycling reclaimed water as claimed in claim 7, wherein in step S300, the secondary reverse osmosis concentrated water is subjected to nanofiltration separation by a nanofiltration membrane to obtain a monovalent salt solution and a divalent salt solution.
9. The method for recycling reclaimed water as claimed in claim 8, wherein in step S400, the monovalent salt solution is evaporated and concentrated by low-temperature distillation, the distilled distillate enters a reclaimed water recycling tank, the concentration of the distilled concentrated solution reaches more than 26%, the distilled concentrated solution is lifted to an ion membrane electrolytic cell by a booster pump for electrolysis to obtain sodium hypochlorite and chlorine, and part of the sodium hypochlorite is recycled as the composite strong oxidant.
10. The method of claim 8, wherein in step S500, the divalent salt solution is lifted to the bipolar membrane electrolyzer by a booster pump to produce an acid solution and an alkali solution, a portion of the acid solution is recycled for buffering, and a portion of the alkali solution is recycled as a softening agent.
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