CN113023836B - Preparation method of composite metal ion water - Google Patents
Preparation method of composite metal ion water Download PDFInfo
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- CN113023836B CN113023836B CN202110289027.7A CN202110289027A CN113023836B CN 113023836 B CN113023836 B CN 113023836B CN 202110289027 A CN202110289027 A CN 202110289027A CN 113023836 B CN113023836 B CN 113023836B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 324
- 229910021645 metal ion Inorganic materials 0.000 title claims abstract description 124
- 239000002131 composite material Substances 0.000 title claims abstract description 58
- 238000002360 preparation method Methods 0.000 title claims abstract description 21
- 239000008367 deionised water Substances 0.000 claims abstract description 100
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 100
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 60
- 229910052709 silver Inorganic materials 0.000 claims description 57
- 239000004332 silver Substances 0.000 claims description 57
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 54
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 47
- 229910052802 copper Inorganic materials 0.000 claims description 47
- 239000010949 copper Substances 0.000 claims description 47
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 40
- 230000005684 electric field Effects 0.000 claims description 40
- 229910052742 iron Inorganic materials 0.000 claims description 34
- 229910017052 cobalt Inorganic materials 0.000 claims description 28
- 239000010941 cobalt Substances 0.000 claims description 28
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 28
- 229910052750 molybdenum Inorganic materials 0.000 claims description 28
- 239000011733 molybdenum Substances 0.000 claims description 28
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 26
- 239000010936 titanium Substances 0.000 claims description 26
- 229910052719 titanium Inorganic materials 0.000 claims description 26
- 229910052725 zinc Inorganic materials 0.000 claims description 26
- 239000011701 zinc Substances 0.000 claims description 26
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 25
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 24
- 229910052782 aluminium Inorganic materials 0.000 claims description 24
- 229910052749 magnesium Inorganic materials 0.000 claims description 24
- 239000011777 magnesium Substances 0.000 claims description 24
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 22
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 19
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 18
- 229910052759 nickel Inorganic materials 0.000 claims description 18
- YGSDEFSMJLZEOE-UHFFFAOYSA-N salicylic acid Chemical compound OC(=O)C1=CC=CC=C1O YGSDEFSMJLZEOE-UHFFFAOYSA-N 0.000 claims description 18
- 229910052804 chromium Inorganic materials 0.000 claims description 17
- 239000011651 chromium Substances 0.000 claims description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 14
- FJKROLUGYXJWQN-UHFFFAOYSA-N papa-hydroxy-benzoic acid Natural products OC(=O)C1=CC=C(O)C=C1 FJKROLUGYXJWQN-UHFFFAOYSA-N 0.000 claims description 9
- 229960004889 salicylic acid Drugs 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 8
- 239000008399 tap water Substances 0.000 claims description 8
- 235000020679 tap water Nutrition 0.000 claims description 8
- 229920000742 Cotton Polymers 0.000 claims description 7
- 239000000654 additive Substances 0.000 claims description 7
- 230000000996 additive effect Effects 0.000 claims description 7
- 239000012528 membrane Substances 0.000 claims description 7
- 238000001223 reverse osmosis Methods 0.000 claims description 7
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 6
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical group [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 229910045601 alloy Inorganic materials 0.000 claims description 4
- 239000000956 alloy Substances 0.000 claims description 4
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 claims description 2
- 239000004021 humic acid Substances 0.000 claims description 2
- 230000004913 activation Effects 0.000 claims 1
- 150000002500 ions Chemical class 0.000 abstract description 12
- 238000005868 electrolysis reaction Methods 0.000 description 307
- -1 silver ions Chemical class 0.000 description 40
- 238000005265 energy consumption Methods 0.000 description 30
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 27
- 229910052748 manganese Inorganic materials 0.000 description 25
- 239000011572 manganese Substances 0.000 description 25
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 description 13
- 229910001431 copper ion Inorganic materials 0.000 description 13
- FOIXSVOLVBLSDH-UHFFFAOYSA-N Silver ion Chemical compound [Ag+] FOIXSVOLVBLSDH-UHFFFAOYSA-N 0.000 description 11
- YJVLWFXZVBOFRZ-UHFFFAOYSA-N titanium zinc Chemical compound [Ti].[Zn] YJVLWFXZVBOFRZ-UHFFFAOYSA-N 0.000 description 10
- 229910001437 manganese ion Inorganic materials 0.000 description 9
- ZAUUZASCMSWKGX-UHFFFAOYSA-N manganese nickel Chemical compound [Mn].[Ni] ZAUUZASCMSWKGX-UHFFFAOYSA-N 0.000 description 8
- VNTLIPZTSJSULJ-UHFFFAOYSA-N chromium molybdenum Chemical compound [Cr].[Mo] VNTLIPZTSJSULJ-UHFFFAOYSA-N 0.000 description 7
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 6
- WAEMQWOKJMHJLA-UHFFFAOYSA-N Manganese(2+) Chemical compound [Mn+2] WAEMQWOKJMHJLA-UHFFFAOYSA-N 0.000 description 6
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 6
- 229910001430 chromium ion Inorganic materials 0.000 description 6
- 229910001429 cobalt ion Inorganic materials 0.000 description 6
- XLJKHNWPARRRJB-UHFFFAOYSA-N cobalt(2+) Chemical compound [Co+2] XLJKHNWPARRRJB-UHFFFAOYSA-N 0.000 description 6
- 238000009713 electroplating Methods 0.000 description 6
- 229910001425 magnesium ion Inorganic materials 0.000 description 6
- 229910001453 nickel ion Inorganic materials 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- PUKLDDOGISCFCP-JSQCKWNTSA-N 21-Deoxycortisone Chemical compound C1CC2=CC(=O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@@](C(=O)C)(O)[C@@]1(C)CC2=O PUKLDDOGISCFCP-JSQCKWNTSA-N 0.000 description 4
- FCYKAQOGGFGCMD-UHFFFAOYSA-N Fulvic acid Natural products O1C2=CC(O)=C(O)C(C(O)=O)=C2C(=O)C2=C1CC(C)(O)OC2 FCYKAQOGGFGCMD-UHFFFAOYSA-N 0.000 description 4
- LCKIEQZJEYYRIY-UHFFFAOYSA-N Titanium ion Chemical compound [Ti+4] LCKIEQZJEYYRIY-UHFFFAOYSA-N 0.000 description 4
- 229940095100 fulvic acid Drugs 0.000 description 4
- 239000002509 fulvic acid Substances 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000004659 sterilization and disinfection Methods 0.000 description 3
- 229910000838 Al alloy Inorganic materials 0.000 description 2
- 229910001182 Mo alloy Inorganic materials 0.000 description 2
- 229910000990 Ni alloy Inorganic materials 0.000 description 2
- VEQPNABPJHWNSG-UHFFFAOYSA-N Nickel(2+) Chemical compound [Ni+2] VEQPNABPJHWNSG-UHFFFAOYSA-N 0.000 description 2
- 229910001297 Zn alloy Inorganic materials 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000003242 anti bacterial agent Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011002 quantification Methods 0.000 description 1
- 230000027756 respiratory electron transport chain Effects 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 229940100890 silver compound Drugs 0.000 description 1
- 150000003379 silver compounds Chemical class 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000012360 testing method Methods 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
- 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
- C02F1/46104—Devices therefor; Their operating or servicing
-
- 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
-
- 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
- C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4612—Controlling or monitoring
- C02F2201/46125—Electrical variables
- C02F2201/46135—Voltage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4612—Controlling or monitoring
- C02F2201/46125—Electrical variables
- C02F2201/4614—Current
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Medicinal Chemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The invention discloses a preparation method of composite metal ion water, which comprises the following steps: step one, two electrolytic polar plates are put into each water tank; 2. injecting deionized water into each water tank; 3. carrying out electrolytic treatment; 4. and mixing deionized water containing metal ions to obtain the composite metal ion water. According to the invention, two electrolytic polar plates are placed in each water tank, direct-current voltage is applied to the two electrolytic polar plates, metal ions on the two electrolytic polar plates are electrolyzed into deionized water by switching positive and negative poles of the direct-current voltage and controlling the switching time, and the ion quantity of the two electrolytic polar plates respectively entering the deionized water is accurately controlled, so that the concentration of the metal ions in the obtained composite metal ion water is controlled, and the composite metal ion water is obtained by mixing all the deionized water containing the metal ions in the water tanks, so that the obtained composite metal ion water can be applied to various environments.
Description
Technical Field
The invention belongs to the technical field of deionized water preparation, and particularly relates to a preparation method of composite metal ion water.
Background
In some special cases, complex water containing various metal ions is required, for example: silver and copper ion water can be used for disinfection and sterilization, and iron, zinc, manganese, aluminum and other composite ion water can be used for agriculture. Since the application field of the composite metal ion water is not widely known, a method specially applied to the preparation of the metal ion water is rarely used in the market.
The metal ions are positive charge-carrying cations, are formed by electron transfer through chemical reaction, usually exist in the form of aqueous solution, and the solution is colorless and transparent and has no solid particles. Taking silver ion water as an example: the industrial production of electrolytic silver ion antibacterial agents has been a dream of many researchers. The silver ions of the electrolytic method which are popular at one time are finally limited by the current technical history conditions and are not realized. The reason for the large difficulty of industrial production is that: silver ion is an extremely reactive ion that oxidizes extremely easily to metallic silver or combines easily with other components to form a stable silver compound. The high-concentration and high-purity silver ions are difficult to decompose, purify and concentrate, and the production environment is demanding.
Accordingly, there is a need to provide a method of preparing complex metal ion water.
Disclosure of Invention
The invention aims to solve the technical problem of providing a preparation method of composite metal ion water aiming at the defects in the prior art. According to the invention, two electrolytic polar plates are placed in each water tank, direct-current voltage is applied to the two electrolytic polar plates, metal ions on the two electrolytic polar plates are electrolyzed into deionized water by switching positive and negative poles of the direct-current voltage and controlling the switching time, and the ion quantity of the two electrolytic polar plates respectively entering the deionized water is accurately controlled, so that the concentration of the metal ions in the obtained composite metal ion water is controlled, and the composite metal ion water is obtained by mixing all the deionized water containing the metal ions in the water tanks, so that the obtained composite metal ion water can be applied to various environments.
In order to solve the technical problems, the technical scheme provided by the invention is as follows: the preparation method of the composite metal ion water is characterized by comprising the following steps of:
step one, regarding a water tank as 1 water tank or dividing the water tank into a plurality of water tanks, and then putting two parallel electrolytic polar plates into each water tank to obtain an electrolytic device;
injecting deionized water into each water tank of the electrolytic device obtained in the first step;
Step three, carrying out electrolytic treatment on the electrolytic device injected with the deionized water in the step two, and obtaining deionized water containing metal ions in each water tank; the electrolytic treatment process comprises the following steps: applying direct current voltage to two electrolytic polar plates in each water tank, reversing the direct current voltage after a certain time, keeping a certain time after reversing, and repeating for a plurality of times;
and step four, mixing the deionized water containing metal ions obtained in the step three in each water tank to obtain the composite metal ion water.
When composite water containing two metal ions is needed, the water tank is regarded as 1 water tank, two mutually parallel electrolytic polar plates are placed in the water tank, the two electrolytic polar plates are guaranteed to contain two metals altogether, direct current is conducted on the two electrolytic polar plates after deionized water is added to form an electrolytic tank, the metal ions of the electrolytic polar plates are electrolyzed into the deionized water to form composite water containing metal ions, when the composite water containing more than two metal ions is needed, the water tank is divided into a plurality of water tanks, two mutually parallel electrolytic polar plates are placed in each water tank, all the electrolytic polar plates used contain more than two metals altogether, direct current is conducted on the two electrolytic polar plates after the deionized water is added to form an electrolytic tank, the metal ions of the electrolytic polar plates are electrolyzed into the composite water containing the metal ions, and the composite water containing different metal ions formed in the plurality of water tanks is mixed to obtain composite metal ion water; in the invention, during electrolysis, oxidation reaction occurs at the positive electrode, ions of the electrolytic polar plate connected with the positive electrode of the power supply enter water, and the two electrolytic polar plates respectively become the positive electrodes by reversing the direct-current voltage, namely, switching the positive electrode and the negative electrode, so that metal ions generated by electrolysis of the two electrolytic polar plates can enter deionized water.
The preparation method of the composite metal ion water is characterized in that in the first step, the division is performed through the movable partition plate, and the number of the water tanks is 2-6. According to the invention, the water tank is divided into a plurality of water tanks through the movable partition plates, and after the electrolysis is finished, the composite water containing different metal ions in the water tanks can be mixed only by extracting the movable partition plates, so that the operation is simple, the preparation of the composite metal ion water containing a plurality of metal ions is realized by controlling the number of the water tanks, and the actual use requirement is met.
The preparation method of the composite metal ion water is characterized in that the material of the electrolytic polar plate in the first step is as follows: silver, copper, iron, manganese, zinc, aluminum, titanium, magnesium, molybdenum, chromium, cobalt and nickel. According to the invention, the material of the electrolytic polar plate is controlled, so that the electrolytic polar plate used in the electrolytic device is made of more than two materials in actual use, the preparation of the composite metal ion water is realized, and the components of metal ions in the obtained composite metal ion water are controlled by controlling the specific material of the electrolytic polar plate, so that the obtained composite metal ion water can be applied to various environments.
The preparation method of the composite metal ion water is characterized in that deionized water is obtained by sequentially filtering tap water through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter; the deionized water is added with an additive, wherein the additive is sodium hypochlorite, humic acid or salicylic acid. According to the invention, municipal tap water passes through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter to remove rust, sediment, residual chlorine, colloid, bacteria, heavy metals, scale, heterochromatic and peculiar smell in the tap water, so that deionized water required by the preparation of the composite metal ion water is obtained, and various metal ion components and quantity of the composite metal ion water can be effectively controlled by using the deionized water, so that the electrolytic polar plate is prevented from being poisoned; the additive is added into deionized water according to a certain proportion, the additive is added to meet the purpose of the final composite metal ion water, the additive can increase the electrolysis efficiency of raw water and play a favorable synergistic effect in the final finished product, the composite metal ion water for disinfection can be prepared by adding sodium hypochlorite, and the composite metal ion water for agriculture can be prepared by adding fulvic acid or salicylic acid.
The preparation method of the composite metal ion water is characterized in that the direct-current voltage in the third step is 3-900V, two electric field polar plates are respectively arranged on two sides, perpendicular to an electrolysis polar plate, of the outside of a water tank in the electrolysis device, and ultrahigh voltage of 30-600 kV is applied to the two electric field polar plates. In the invention, in the electrolytic process, oxidation reaction occurs at the positive electrode, ions in the electrolytic polar plate enter water, reduction reaction occurs at the negative plate, the ions are electroplated on the negative plate, when the ion concentration reaches a certain value in the water, oxidation and reduction reach balance, the ion concentration in the water can not be increased any more, by arranging two electric field polar plates, an ultrahigh voltage is applied to the electric field polar plates positioned outside the electrolytic water tank to form an electric field, the electric field pushes metal ions generated by the electrolytic polar plates to the negative electric field polar plates side and form an ion enrichment area, the metal ions are prevented from undergoing electroplating reaction, namely reduction reaction, so as to improve the ion concentration, and ensure the smooth progress of the electrolytic reaction, and the invention sets the electrifying parameters of each pair of electrolytic polar plates by calculation, and comprises: the reverse time of the electrolytic electrode plate, namely the reverse period, the duty ratio of the energizing time of the two electrolytic electrode plates, the voltage of the two electrolytic electrode plates and the power consumption of the two electrolytic electrode plates, energizing the electrolytic electrode plates according to the calculated parameters, reversing the voltage according to the parameters, and repeating for a plurality of times, so that the concentration of each metal ion in the composite metal ion water is accurately controlled, and the obtained composite metal ion water meets the use requirement.
The preparation method of the composite metal ion water is characterized in that the direct current voltage is reversely forward, the positive electrode and the negative electrode of the direct current voltage are subjected to flash for 5 times to 100 times, and the flash process comprises the following steps: when the direct current voltage is in the forward direction, the direct current voltage is switched to the reverse holding time T, then the direct current voltage is switched to the forward holding time T, and when the direct current voltage is in the reverse direction, the direct current voltage is switched to the forward holding time T, then the direct current voltage is switched to the reverse holding time T, wherein the T is 50 ms-1000 ms. The invention rapidly switches the positive electrode and the negative electrode of the direct current voltage by flashing the positive electrode and the negative electrode of the direct current voltage before the direct current voltage is reversely switched, namely, the positive electrode and the negative electrode are rapidly switched, which is equivalent to a shaking process, metal ions generated on an electrolytic polar plate are shaken off into deionized water, and because the principle of electrolysis is the same as that of electroplating, when the metal ions in the deionized water reach a certain concentration, electroplating can occur.
The preparation method of the composite metal ion water is characterized in that the concentration of each metal ion in the deionized water containing two metal ions is as follows: power consumption of the electrolytic electrode plate = metal ion concentration x total volume of water in all water tanks x power consumption constant of the electrolytic electrode plate; the power consumption constant is: the electrolytic electrode plate increases the power consumption required by 1ppm of solute in every 1g of deionized water under the direct current voltage of 38V and the electric field of 60kV/m in the deionized water with the total solid content of 10 ppm. According to the invention, the power consumption constant of the electrolytic polar plates is obtained through testing under specific conditions, so that the power consumption of the electrolytic polar plates is calculated, and the time for respectively taking the two electrolytic polar plates in each water tank as the positive electrode and the total power-on time can be obtained, thereby controlling the content of each metal ion in the composite metal ion water.
The preparation method of the composite metal ion water is characterized in that when the sum of the power consumption of the two electrolytic polar plates in each water tank is smaller than the starting threshold value of the electric field polar plate, the electric field polar plate is not started. When the sum of the power consumption of the two electrolytic polar plates is smaller than the starting threshold value of the electric field polar plate, the generated metal ions are less and insufficient for generating electroplating reaction, the electric field polar plate is not required to be opened, and the resource is saved.
Compared with the prior art, the invention has the following advantages:
1. according to the invention, two electrolytic polar plates are placed in each water tank, direct-current voltage is applied to the two electrolytic polar plates, metal ions on the two electrolytic polar plates are electrolyzed into deionized water by switching positive and negative poles of the direct-current voltage and controlling the switching time, and the ion quantity of the two electrolytic polar plates respectively entering the deionized water is accurately controlled, so that the concentration of the metal ions in the obtained composite metal ion water is controlled, and the composite metal ion water is obtained by mixing all the deionized water containing the metal ions in the water tanks, so that the obtained composite metal ion water can be applied to various environments.
2. The invention shakes the metal ions generated on the electrolytic polar plate into deionized water by carrying out flash on the positive and negative poles of the direct voltage before the direct voltage is reversed, thus blocking the electroplating process, preventing the electrolytic polar plate from being damaged and prolonging the service life of the electrolytic polar plate.
3. According to the invention, the high-voltage electric field generated by the two electric field polar plates enables metal ions generated by the electrolytic polar plates to be far away from the positive electrode of the electrolytic polar plates, and a metal ion enrichment area is formed around the negative electrode of the electric field polar plates, so that the metal ions are prevented from generating electroplating reaction, namely reduction reaction, and the concentration of the metal ions in the composite metal ion water is improved.
4. The preparation method of the composite metal ion water can flexibly prepare and produce various composite metal ion water, solves the problems of poor preparation efficiency, difficult quantification, low concentration and the like of the specific composite metal ion water, and has the advantages of high automation degree, accurate concentration control, low production cost, wide application scene and the like.
The technical scheme of the invention is further described in detail through the drawings and the embodiments.
Drawings
FIG. 1 is a schematic view of the structure of the electrolytic device of the present invention.
Reference numerals illustrate:
1-a water tank; 2-a separator; 3-a water tank;
4-an electrolytic polar plate; 5-electric field polar plate.
Detailed Description
As shown in fig. 1, the electrolytic device of the invention comprises a water tank 1 and a partition plate 2 for dividing the water tank 1 into a water tank 3, wherein two mutually parallel electrolytic pole plates 4 are arranged in the water tank 3, and two electric field pole plates 5 are respectively arranged on two sides of the outside of the water tank 1, which are perpendicular to the electrolytic pole plates 4.
The present invention is described in detail with reference to examples 1 to 4.
Example 1
This example is to prepare 10kg of complex metal ion water containing 0.1ppm silver ion, 0.1ppm copper ion and 3ppm sodium hypochlorite.
The embodiment comprises the following steps:
step one, regarding a water tank as 1 water tank, and then putting two parallel silver electrolysis polar plates and copper electrolysis polar plates into the water tank;
step two, respectively installing two electric field polar plates on two sides, which are perpendicular to the electrolytic polar plates, of the outside of the water tank after the electrolytic polar plates are placed in the step one, so as to obtain an electrolytic device;
step three, 10kg of deionized water is injected into a water tank in the electrolytic device obtained in the step two; the deionized water is obtained by filtering tap water sequentially through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter; 0.12g of sodium hypochlorite solution with the mass concentration of 25% is added into the deionized water;
step four, carrying out electrolytic treatment on the electrolytic device injected with the deionized water in the step three, and obtaining deionized water containing metal ions in each water tank;
the electrolytic constant of the silver electrolytic plate is 0.01 (Wh/kg.ppm); the electrolytic constant of the copper electrolytic plate is 0.02 (Wh/kg.ppm); the starting threshold value of the electric field polar plate is set to be 5Wh; the reverse phase period of the electrolytic polar plate is 60s; applying 3V direct current voltage to the electrolytic polar plates in the electrolytic treatment, and measuring the current value flowing through each pair of electrolytic polar plates;
Power consumption of silver electrolysis plate = electrolysis constant of silver electrolysis plate x deionized water mass x silver ion concentration = 0.01 (Wh/kg.ppm) ×10 (kg) ×0.1 (ppm) = 0.01Wh;
power consumption of copper electrolysis plate = electrolysis constant of copper electrolysis plate x deionized water mass x copper ion concentration = 0.02 (Wh/kg.ppm) ×10 (kg) ×0.1 (ppm) = 0.02Wh;
the electrolysis plate energy consumption ratio=the power consumption of the silver electrolysis plate/(the power consumption of the silver electrolysis plate+the power consumption of the copper electrolysis plate) =0.01 Wh/(0.01 wh+0.02 Wh) =1/3;
positive pulse width of silver electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 60s x 1/3 = 20s;
positive pulse width of copper electrolysis plate = electrolysis plate inversion period-positive pulse width of silver electrolysis plate = 60s-20s = 40s;
after 3V direct current voltage is connected, measuring that the passing current of the silver electrolysis polar plate and the copper electrolysis polar plate is 0.05A;
number of pulses=int (3600× (power consumption of silver electrolysis plate/(voltage×current))/positive pulse width of silver electrolysis plate) +1=int (3600× (0.01/(3×0.05)/20) =12, wherein INT is a rounded function, and is an integer value of the value;
electrolysis time = number of pulses x electrolysis plate inversion period = 12 x 60s = 720s;
total electrode plate energy consumption = silver electrode plate power consumption + copper electrode plate power consumption = 0.03Wh < electric field plate start threshold 5Wh, electric field plate is not started;
The electrolytic treatment process comprises the following steps: applying 3V direct current voltage to the two electrolytic polar plates, and keeping the silver electrolytic polar plates connected with the positive electrode and the copper electrolytic polar plates connected with the negative electrode; reversing the direct current voltage after 20 seconds, keeping for 40 seconds after reversing, and repeating for 12 times to obtain water containing copper and silver metal ions in a water tank;
the direct-current voltage is reversely forward, the positive electrode and the negative electrode of the direct-current voltage are subjected to flash for 5 times, and the flash process comprises the following steps: when the direct current voltage is in the forward direction, switching the direct current voltage into a reverse holding time T, and then switching the direct current voltage into a forward holding time T; when the direct current voltage is reverse, switching the direct current voltage into a forward holding time T, and then switching the direct current voltage into a reverse holding time T, wherein T is 1000ms;
and fifthly, mixing the deionized water containing the metal ions obtained in the step four in each water tank to obtain the composite metal ion water containing 0.1ppm of silver ions, 0.1ppm of copper ions and 3ppm of sodium hypochlorite.
Example 2
This example is 1000kg of complex metal ion water containing 0.5ppm silver ion, 1ppm copper ion, 0.3ppm iron ion, 0.2ppm manganese ion and 10ppm fulvic acid.
The embodiment comprises the following steps:
Dividing a water tank into 2 water tanks which are respectively marked as a water tank A and a water tank B through a movable partition plate, then putting two parallel silver electrolysis polar plates and copper electrolysis polar plates into the water tank A, and then putting two parallel iron electrolysis polar plates and manganese electrolysis polar plates into the water tank B;
step two, respectively installing two electric field polar plates on two sides, which are perpendicular to the electrolytic polar plates, of the outside of the water tank after the electrolytic polar plates are placed in the step one, so as to obtain an electrolytic device;
step three, injecting 500kg of deionized water into the water tank A in the electrolytic device obtained in the step two, and injecting 500kg of deionized water into the water tank B; the deionized water is obtained by filtering tap water sequentially through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter; 20g of fulvic acid solution with the mass concentration of 50% is added into the deionized water;
step four, carrying out electrolytic treatment on the electrolytic device injected with the deionized water in the step three, and obtaining deionized water containing metal ions in each water tank;
the electrolytic constant of the silver electrolytic plate is 0.01 (Wh/kg.ppm); the electrolytic constant of the copper electrolytic plate is 0.02 (Wh/kg.ppm); the electrolytic constant of the iron electrolytic plate is 0.015 (Wh/kg.ppm); the electrolytic constant of the manganese electrolytic plate is 0.035 (Wh/kg. Ppm); the starting threshold value of the electric field polar plate is 10Wh; the reverse phase period of the electrolytic polar plate is 60s; applying 220V direct current voltage to the electrolytic polar plates in the electrolytic treatment, and measuring the current value flowing through each pair of electrolytic polar plates;
Power consumption of silver electrolysis plate = electrolysis constant of silver electrolysis plate x deionized water mass x silver ion concentration = 0.01 (Wh/kg.ppm) ×1000 (kg) ×0.5 (ppm) = 5Wh;
power consumption of copper electrolysis plate = electrolysis constant of copper electrolysis plate x deionized water mass x copper ion concentration = 0.02 (Wh/kg.ppm) ×1000 (kg) ×1 (ppm) = 20Wh;
power consumption of iron electrolysis plate = electrolysis constant of iron electrolysis plate x deionized water mass x iron ion concentration = 0.015 (Wh/kg.ppm) ×1000 (kg) ×0.3 (ppm) = 4.5Wh
Power consumption of manganese electrolysis plate = electrolysis constant of manganese electrolysis plate x deionized water mass x manganese ion concentration = 0.035 (Wh/kg) ×1000 (kg) ×0.2 (ppm) = 7Wh
Total energy consumption of the electrode plate = power consumption of the silver electrolytic electrode plate + power consumption of the copper electrolytic electrode plate + power consumption of the ferroelectric electrode plate + power consumption of the manganese electrolytic electrode plate = 36.5Wh > electric field electrode plate starting threshold 10Wh, electric field electrode plate starting;
in the water tank A:
electrolytic plate energy consumption ratio = power consumption of silver electrolytic plate/(power consumption of silver electrolytic plate + power consumption of copper electrolytic plate) =5wh/(5wh+20wh) =0.2;
positive pulse width of silver electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 60s x 0.2 = 12s;
positive pulse width of copper electrolysis plate = electrolysis plate inversion period-positive pulse width of silver electrolysis plate = 60s-12s = 48s;
After 220V direct current voltage is switched on, measuring that the passing current of the silver electrolysis polar plate and the copper electrolysis polar plate is 0.55A;
number of pulses=int (3600× (power consumption of silver electrolysis plate/(voltage×current))/positive pulse width of silver electrolysis plate) +1=int (3600× (5/(220×0.55))/12) +1=13;
electrolysis time = number of pulses x electrolysis plate inversion period = 13 x 60s = 780s;
in the water tank B:
the electrolysis plate energy consumption ratio=the power consumption of the electrolysis plate/(the power consumption of the electrolysis plate+the power consumption of the manganese electrolysis plate) =4.5 Wh/(4.5 wh+7wh) =0.39;
positive pulse width of the ferroelectric plate=reverse period of the electrolytic plate×energy consumption ratio of the electrolytic plate=60 s×0.39=23 s;
positive pulse width of manganese electrolytic plate=electrolytic plate inversion period-positive pulse width of iron electrolytic plate=60 s-23 s=37 s;
after 220V direct current voltage is switched on, the passing current of the ferroelectric electrolytic pole plate and the manganese electrolytic pole plate is measured to be 0.35A;
number of pulses=int (3600× (power consumption of the ferroelectric plate/(voltage×current))/positive pulse width of the ferroelectric plate) +1=int (3600× (4.5/(220×0.35)/23) +1=9;
electrolysis time = number of pulses x electrolysis plate inversion period = 9 x 60s = 540s;
the electrolytic treatment process comprises the following steps: applying 30kV ultrahigh voltage on the two electric field polar plates;
In the water tank A: applying 220V direct current voltage on the silver electrolysis polar plate and the copper electrolysis polar plate, and keeping the silver electrolysis polar plate connected with the positive electrode and the copper electrolysis polar plate connected with the negative electrode; the direct current voltage is reversed after 12 seconds, the direct current voltage is kept for 48 seconds after the reversing and is repeated for 13 times, and water containing copper and silver metal ions is obtained in a water tank A;
in the water tank B: applying 220V direct current voltage on the iron electrolysis polar plate and the manganese electrolysis polar plate, and keeping the iron electrolysis polar plate connected with the anode and the manganese electrolysis polar plate connected with the cathode; the direct current voltage is reversed after 23 seconds, the direct current voltage is maintained for 37 seconds after the reversing, and the direct current voltage is repeated for 9 times, so that water containing iron and manganese metal ions is obtained in a water tank B;
the direct-current voltage is reversely forward, the positive electrode and the negative electrode of the direct-current voltage are subjected to 100 times of flash, and the flash process comprises the following steps: when the direct current voltage is in the forward direction, switching the direct current voltage into a reverse holding time T, and then switching the direct current voltage into a forward holding time T; when the direct current voltage is reverse, switching the direct current voltage into a forward holding time T, and then switching the direct current voltage into a reverse holding time T, wherein T is 50ms;
and step five, mixing the water containing the metal ions obtained in the water tank A and the water tank B in the step four to obtain 1000kg of composite metal ion water containing 0.5ppm of silver ions, 1ppm of copper ions, 0.3ppm of iron ions, 0.2ppm of manganese ions and 10ppm of fulvic acid.
Example 3
This example is to prepare 3000kg of complex metal ion water containing 0.5ppm silver ion, 1ppm copper ion, 0.3ppm iron ion, 0.2ppm manganese ion, 0.1ppm zinc ion, 0.2ppm aluminum ion, 0.1ppm titanium ion, 0.5ppm magnesium ion, 0.1ppm molybdenum ion, 0.05ppm chromium ion, 0.01ppm cobalt ion, 0.3ppm nickel ion and 10ppm salicylic acid.
The embodiment comprises the following steps:
dividing a water tank into 6 water tanks through a movable partition board, namely a water tank A, a water tank B, a water tank C, a water tank D, a water tank E and a water tank F in sequence, then putting two parallel silver electrolysis polar plates and copper electrolysis polar plates into the water tank A, and putting two parallel iron electrolysis polar plates and manganese electrolysis polar plates into the water tank B; two zinc electrolysis polar plates and aluminum electrolysis polar plates which are parallel to each other are put into the water tank C; two titanium electrolytic polar plates and magnesium electrolytic polar plates which are parallel to each other are put into the water tank D; two molybdenum electrolysis polar plates and chromium electrolysis polar plates which are parallel to each other are put into the water tank E; two cobalt electrolysis polar plates and nickel electrolysis polar plates which are parallel to each other are put into the water tank F;
step two, respectively installing two electric field polar plates on two sides, which are perpendicular to the electrolytic polar plates, of the outside of the water tank after the electrolytic polar plates are placed in the step one, so as to obtain an electrolytic device;
Step three, injecting 500kg of deionized water into the water tanks A-F in the electrolytic device obtained in the step two; the deionized water is obtained by filtering tap water sequentially through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter; 60g of salicylic acid with the mass concentration of 50% is added into the deionized water;
step four, carrying out electrolytic treatment on the electrolytic device injected with the deionized water in the step three, and obtaining deionized water containing metal ions in each water tank;
the electrolytic constant of the silver electrolytic plate is 0.01 (Wh/kg.ppm); the electrolytic constant of the copper electrolytic plate is 0.02 (Wh/kg.ppm); the electrolytic constant of the iron electrolytic plate is 0.015 (Wh/kg.ppm); the electrolytic constant of the manganese electrolytic plate is 0.035 (Wh/kg. Ppm); the electrolytic constant of the zinc electrolytic plate is 0.011 (Wh/kg.ppm); the electrolytic constant of the aluminum electrolytic plate is 0.025 (Wh/kg.ppm); the electrolytic constant of the titanium electrolytic plate is 0.005 (Wh/kg.ppm); the electrolysis constant of the magnesium electrolysis polar plate is 0.025 (Wh/kg.ppm); the electrolytic constant of the molybdenum electrolytic plate is 0.013 (Wh/kg.ppm); the electrolytic constant of the chromium electrolytic plate is 0.029 (Wh/kg.ppm); the electrolytic constant of the cobalt electrolytic plate is 0.015 (Wh/kg.ppm); the electrolytic constant of the nickel electrolytic polar plate is 0.035 (Wh/kg. Ppm); the starting threshold value of the electric field polar plate is 10Wh; the reverse phase period of the electrolytic polar plate is 60s; applying 90V direct current voltage to the electrolytic polar plates in the electrolytic treatment, and measuring the current value flowing through each pair of electrolytic polar plates;
Power consumption of silver electrolysis plate = electrolysis constant of silver electrolysis plate x deionized water mass x silver ion concentration = 0.01 (Wh/kg.ppm) ×3000 (kg) ×0.5 (ppm) = 15Wh;
power consumption of copper electrolysis plate = electrolysis constant of copper electrolysis plate x deionized water mass x copper ion concentration = 0.02 (Wh/kg.ppm) ×3000 (kg) ×1 (ppm) = 60Wh;
power consumption of iron electrolysis plate = electrolysis constant of iron electrolysis plate x deionized water mass x iron ion concentration = 0.015 (Wh/kg.ppm) ×3000 (kg) ×0.3 (ppm) = 13.5Wh
Power consumption of manganese electrolysis plate = electrolysis constant of manganese electrolysis plate x deionized water mass x manganese ion concentration = 0.035 (Wh/kg) ×3000 (kg) ×0.2 (ppm) = 21Wh
Power consumption of zinc electrolysis plate = electrolysis constant of zinc electrolysis plate x deionized water mass x zinc ion concentration = 0.011 (Wh/kg.ppm) ×3000 (kg) ×0.1 (ppm) =3.3 Wh)
Power consumption of aluminum electrolysis plate = electrolysis constant of aluminum electrolysis plate x deionized water mass x aluminum ion concentration = 0.0025 (Wh/kg) x 3000 (kg) x 0.2 (ppm) = 15Wh
Power consumption of titanium electrolytic plate = electrolysis constant of titanium electrolytic plate x deionized water mass x titanium ion concentration = 0.0025 (Wh/kg.ppm) ×3000 (kg) ×0.1 (ppm) = 7.5 Wh)
Power consumption of magnesium electrolysis plate = electrolysis constant of magnesium electrolysis plate x deionized water mass x magnesium ion concentration = 0.025 (Wh/kg.ppm) ×3000 (kg) ×0.5 (ppm) = 37.5 Wh)
Power consumption of molybdenum electrolysis plate = electrolysis constant of molybdenum electrolysis plate x deionized water mass x molybdenum ion concentration = 0.0013 (Wh/kg.ppm) ×3000 (kg) ×0.1 (ppm) = 3.9 Wh)
Power consumption of chromium electrolysis plate = electrolysis constant of chromium electrolysis plate x deionized water mass x chromium ion concentration = 0.0025 (Wh/kg.ppm) ×3000 (kg) ×0.05 (ppm) = 4.35Wh
Power consumption of cobalt electrolysis plate = electrolysis constant of cobalt electrolysis plate x deionized water mass x cobalt ion concentration = 0.001 (Wh/kg.ppm) ×3000 (kg) ×0.01 (ppm) = 0.45Wh
Power consumption of nickel electrolysis plate = electrolysis constant of nickel electrolysis plate x deionized water mass x nickel ion concentration = 0.035 (Wh/kg.ppm) ×3000 (kg) ×0.3 (ppm) = 31.5Wh
Total energy consumption of the electrode plate = power consumption of the silver electrolytic electrode plate + power consumption of the copper electrolytic electrode plate + power consumption of the manganese electrolytic electrode plate + power consumption of the zinc electrolytic electrode plate + power consumption of the aluminum electrolytic electrode plate + power consumption of the titanium electrolytic electrode plate + power consumption of the magnesium electrolytic electrode plate + power consumption of the molybdenum electrolytic electrode plate + power consumption of the chromium electrolytic electrode plate + power consumption of the cobalt electrolytic electrode plate + power consumption of the nickel electrolytic electrode plate = 213Wh > electric field electrode plate start threshold 10Wh, electric field electrode plate start;
in the water tank A:
electrolytic plate energy consumption ratio = power consumption of silver electrolytic plate/(power consumption of silver electrolytic plate + power consumption of copper electrolytic plate) =15 Wh/(15 wh+60 Wh) =0.2;
Positive pulse width of silver electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 60s x 0.2 = 12s;
positive pulse width of copper electrolysis plate = electrolysis plate inversion period-positive pulse width of silver electrolysis plate = 60s-12s = 48s;
after the direct-current voltage of 90V is switched on, the passing current of the silver electrolysis polar plate and the copper electrolysis polar plate is measured to be 0.55A;
number of pulses=int (3600× (power consumption of silver electrolysis plate/(voltage×current))/positive pulse width of silver electrolysis plate) +1=int (3600× (15/(220×0.55)/12) +1=38;
electrolysis time = number of pulses x electrolysis plate inversion period = 38 x 60s = 2280s;
in the water tank B:
the electrolysis plate energy consumption ratio=the power consumption of the electrolysis plate/(the power consumption of the electrolysis plate+the power consumption of the manganese electrolysis plate) =0.39;
positive pulse width of the ferroelectric plate=reverse period of the electrolytic plate×energy consumption ratio of the electrolytic plate=60 s×0.39=23 s;
positive pulse width of manganese electrolytic plate=electrolytic plate inversion period-positive pulse width of iron electrolytic plate=60 s-23 s=37 s;
after the direct-current voltage of 90V is switched on, the passing current of the ferroelectric electrolytic plate and the manganese electrolytic plate is measured to be 0.35A;
number of pulses=int (3600× (power consumption of ferroelectric plate/(voltage×current))/positive pulse width of ferroelectric plate) +1=27
Electrolysis time = number of pulses x electrolysis plate inversion period = 27 x 60s = 1620s;
in the water tank C:
the electrolysis plate energy consumption ratio=the power consumption of the zinc electrolysis plate/(the power consumption of the zinc electrolysis plate+the power consumption of the aluminum electrolysis plate) =0.18;
positive pulse width of zinc electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 11s;
positive pulse width of aluminum electrolysis plate=electrolysis plate inversion period-positive pulse width of zinc electrolysis plate=60 s-11 s=49 s;
after the direct-current voltage of 90V is switched on, the passing current of the zinc electrolysis polar plate and the aluminum electrolysis polar plate is measured to be 0.35A;
number of pulses=int (3600× (power consumption of zinc electrolysis plate/(voltage×current))/positive pulse width of zinc electrolysis plate) +1=15;
electrolysis time = number of pulses x electrolysis plate inversion period = 15 x 60s = 900s;
in the water tank D:
the electrolysis plate energy consumption ratio=the power consumption of the titanium electrolysis plate/(the power consumption of the titanium electrolysis plate+the power consumption of the magnesium electrolysis plate) =0.17;
positive pulse width of titanium electrolytic plate=electrolytic plate reverse phase period×electrolytic plate energy consumption ratio=60 s×0.17=10 s;
positive pulse width of magnesium electrolysis plate = electrolysis plate inversion period-positive pulse width of titanium electrolysis plate = 60s-10s = 50s;
after the direct-current voltage of 90V is switched on, the passing current of the titanium electrolysis polar plate and the magnesium electrolysis polar plate is measured to be 0.33A;
Number of pulses=int (3600× (power consumption of titanium electrolysis plate/(voltage×current))/positive pulse width of titanium electrolysis plate) +1=38;
electrolysis time = number of pulses x electrolysis plate inversion period = 38 x 60s = 2280s;
in the water tank E:
the electrolysis plate energy consumption ratio=the power consumption of the molybdenum electrolysis plate/(the power consumption of the molybdenum electrolysis plate+the power consumption of the chromium electrolysis plate) =0.47;
positive pulse width of molybdenum electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 60s x 0.47 = 28s;
positive pulse width of chromium electrolysis plate = electrolysis plate inversion period-positive pulse width of molybdenum electrolysis plate = 60s-28s = 32s;
after the direct-current voltage of 90V is switched on, the passing current of the molybdenum electrolysis polar plate and the chromium electrolysis polar plate is measured to be 0.45A;
number of pulses=int (3600× (power consumption of molybdenum electrolysis plate/(voltage×current))/positive pulse width of molybdenum electrolysis plate) +1=6;
electrolysis time = number of pulses x electrolysis plate inversion period = 6 x 60s = 360s;
in the water tank F:
the electrolysis plate energy consumption ratio=the power consumption of the cobalt electrolysis plate/(the power consumption of the cobalt electrolysis plate+the power consumption of the nickel electrolysis plate) =0.014;
positive pulse width of cobalt electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 60s x 0.014 = 1s;
Positive pulse width of nickel electrolysis plate = electrolysis plate inversion period-positive pulse width of cobalt electrolysis plate = 60s-1s = 59s;
after the direct-current voltage of 90V is switched on, the passing current of the cobalt electrolysis polar plate and the nickel electrolysis polar plate is measured to be 0.41A;
number of pulses=int (3600× (power consumption of cobalt electrolysis plate/(voltage×current))/positive pulse width of cobalt electrolysis plate) +1=22;
electrolysis time = number of pulses x electrolysis plate inversion period = 22 x 60s = 1320s;
the electrolytic treatment process comprises the following steps: applying 600kV ultra-high voltage on the two electric field polar plates;
in the water tank A: applying 220V direct current voltage on the silver electrolysis polar plate and the copper electrolysis polar plate, and keeping the silver electrolysis polar plate connected with the positive electrode and the copper electrolysis polar plate connected with the negative electrode; the direct current voltage is reversed after 12 seconds, the direct current voltage is kept for 48 seconds after the reversing, and the direct current voltage is repeated for 38 times, so that deionized water containing copper and silver metal ions is obtained in a water tank A;
in the water tank B: applying 220V direct current voltage on the iron electrolysis polar plate and the manganese electrolysis polar plate, and keeping the iron electrolysis polar plate connected with the anode and the manganese electrolysis polar plate connected with the cathode; the direct current voltage is reversed after 23 seconds, the direct current voltage is maintained for 37 seconds after the reversing, and the direct current voltage is repeated for 27 times, so that deionized water containing iron and manganese metal ions is obtained in a water tank B;
In the water tank C: applying 220V direct current voltage on the zinc electrolysis polar plate and the aluminum electrolysis polar plate, and keeping the zinc electrolysis polar plate connected with the positive electrode and the aluminum electrolysis polar plate connected with the negative electrode; reversing the direct current voltage after 11 seconds, keeping 49 seconds after reversing, and repeating for 15 times to obtain deionized water containing zinc and aluminum metal ions in a water tank C;
in the water tank D: applying 220V direct current voltage on the titanium electrolysis polar plate and the magnesium electrolysis polar plate, and keeping the titanium electrolysis polar plate connected with the positive electrode and the magnesium electrolysis polar plate connected with the negative electrode; the direct current voltage is reversed after 10 seconds, the direct current voltage is maintained for 50 seconds after the reversing and is repeated for 38 times, and deionized water containing titanium and magnesium metal ions is obtained in a water tank D;
in the water tank E: applying 220V direct current voltage on the molybdenum electrolysis polar plate and the chromium electrolysis polar plate, and keeping the molybdenum electrolysis polar plate connected with the positive electrode and the chromium electrolysis polar plate connected with the negative electrode; reversing the direct current voltage after 28 seconds, keeping for 32 seconds after reversing, and repeating for 6 times to obtain deionized water containing molybdenum and chromium metal ions in a water tank E;
in the water tank F: applying 220V direct current voltage on the cobalt electrolysis polar plate and the nickel electrolysis polar plate, and keeping the cobalt electrolysis polar plate connected with the anode and the nickel electrolysis polar plate connected with the cathode; the direct current voltage is reversed after 1 second, the direct current voltage is kept for 59 seconds after the direct current voltage is reversed, and the direct current voltage is repeated for 22 times, so that deionized water containing cobalt and nickel metal ions is obtained in a water tank F;
The direct current voltage is reversely forward, the positive electrode and the negative electrode of the direct current voltage are subjected to flash for 50 times, and the flash process comprises the following steps: when the direct current voltage is in the forward direction, switching the direct current voltage into a reverse holding time T, and then switching the direct current voltage into a forward holding time T; when the direct current voltage is reverse, switching the direct current voltage into a forward holding time T, and then switching the direct current voltage into a reverse holding time T, wherein T is 400ms;
mixing the deionized water containing the metal ions obtained in the water tank A, B, C, D, E, F in the step four to obtain 3000kg of composite metal ion water containing 0.5ppm of silver ions, 1ppm of copper ions, 0.3ppm of iron ions, 0.2ppm of manganese ions, 0.1ppm of zinc ions, 0.2ppm of aluminum ions, 0.1ppm of titanium ions, 0.5ppm of magnesium ions, 0.1ppm of molybdenum ions, 0.05ppm of chromium ions, 0.01ppm of cobalt ions, 0.3ppm of nickel ions and 10ppm of salicylic acid.
Example 4
This example is to prepare 4000kg of complex metal ion water containing 0.5ppm of silver ion, 1ppm of copper ion, 0.3ppm of iron ion, 0.2ppm of manganese ion, 0.1ppm of zinc ion, 0.2ppm of aluminum ion, 0.22ppm of titanium ion, 0.5ppm of magnesium ion, 0.11ppm of molybdenum ion, 0.05ppm of chromium ion, 0.01ppm of cobalt ion, 0.2ppm of nickel ion and 10ppm of salicylic acid.
The embodiment comprises the following steps:
step one, manufacturing an electrolytic plate with the same power consumption into an alloy electrolytic plate according to the power consumption required by the electrolytic plate; the alloy electrolytic polar plate comprises the following elements in proportion: the percentage content of element a=the required concentration of element a/(the required concentration of element a+the required concentration of element B) ×100; the percentage content of the B element=the required concentration of the a element/(the required concentration of the a element+the required concentration of the B element) ×100;
the electrolytic constant of the silver electrolytic plate is 0.01 (Wh/kg.ppm); the electrolytic constant of the copper electrolytic plate is 0.02 (Wh/kg.ppm); the electrolytic constant of the iron electrolytic plate is 0.015 (Wh/kg.ppm); the electrolytic constant of the manganese electrolytic plate is 0.035 (Wh/kg. Ppm); the electrolytic constant of the zinc electrolytic plate is 0.011 (Wh/kg.ppm); the electrolytic constant of the aluminum electrolytic plate is 0.025 (Wh/kg.ppm); the electrolytic constant of the titanium electrolytic plate is 0.005 (Wh/kg.ppm); the electrolysis constant of the magnesium electrolysis polar plate is 0.025 (Wh/kg.ppm); the electrolytic constant of the molybdenum electrolytic plate is 0.013 (Wh/kg.ppm); the electrolytic constant of the chromium electrolytic plate is 0.029 (Wh/kg.ppm); the electrolytic constant of the cobalt electrolytic plate is 0.015 (Wh/kg.ppm); the electrolytic constant of the nickel electrolytic polar plate is 0.035 (Wh/kg. Ppm); the starting threshold value of the electric field polar plate is 100Wh; the reverse phase period of the electrolytic polar plate is 60s; applying 900V direct current voltage to the electrolytic polar plates in the electrolytic treatment, and measuring the current value flowing through each pair of electrolytic polar plates;
Power consumption of silver electrolysis plate = electrolysis constant of silver electrolysis plate x deionized water mass x silver ion concentration = 0.01 (Wh/kg.ppm) ×4000 (kg) ×0.5 (ppm) = 20Wh;
power consumption of copper electrolysis plate = electrolysis constant of copper electrolysis plate x deionized water mass x copper ion concentration = 0.02 (Wh/kg.ppm) x 4000 (kg) x 1 (ppm) = 80Wh;
power consumption of iron electrolysis plate = electrolysis constant of iron electrolysis plate x deionized water mass x iron ion concentration = 0.015 (Wh/kg.ppm) ×4000 (kg) ×0.3 (ppm) = 18Wh
Power consumption of manganese electrolysis plate = electrolysis constant of manganese electrolysis plate x deionized water mass x manganese ion concentration = 0.035 (Wh/kg) ×4000 (kg) ×0.2 (ppm) = 28Wh
Power consumption of zinc electrolysis plate = electrolysis constant of zinc electrolysis plate x deionized water mass x zinc ion concentration = 0.011 (Wh/kg.ppm) ×4000 (kg) ×0.1 (ppm) = 4.4Wh
Power consumption of aluminum electrolysis plate = electrolysis constant of aluminum electrolysis plate x deionized water mass x aluminum ion concentration = 0.0025 (Wh/kg) x 4000 (kg) x 0.2 (ppm) = 20Wh
Power consumption of titanium electrolytic plate = electrolysis constant of titanium electrolytic plate x deionized water mass x titanium ion concentration = 0.005 (Wh/kg.ppm) ×4000 (kg) ×0.22 (ppm) = 4.4Wh
Power consumption of magnesium electrolysis plate = electrolysis constant of magnesium electrolysis plate x deionized water mass x magnesium ion concentration = 0.025 (Wh/kg.ppm) ×4000 (kg) ×0.5 (ppm) = 50Wh
Power consumption of molybdenum electrolysis plate = electrolysis constant of molybdenum electrolysis plate x deionized water mass x molybdenum ion concentration = 0.0013 (Wh/kg.ppm) ×4000 (kg) ×0.11 (ppm) = 5.72 Wh)
Power consumption of chromium electrolysis plate = electrolysis constant of chromium electrolysis plate x deionized water mass x chromium ion concentration = 0.0025 (Wh/kg.ppm) x 4000 (kg) x 0.05 (ppm) = 5.8Wh
Power consumption of cobalt electrolysis plate = electrolysis constant of cobalt electrolysis plate x deionized water mass x cobalt ion concentration = 0.015 (Wh/kg.ppm) ×4000 (kg) ×0.01 (ppm) = 0.6Wh
Power consumption of nickel electrolysis plate = electrolysis constant of nickel electrolysis plate x deionized water mass x nickel ion concentration = 0.035 (Wh/kg.ppm) ×4000 (kg) ×0.2 (ppm) = 28Wh
Making the electrode plates with the same power consumption into alloy electrode plates, and making the electrode plates into silver-aluminum alloy electrolytic electrode plates with uniform textures according to 71.4% of silver and 28.6% of aluminum; preparing a chromium-molybdenum alloy electrolytic plate with uniform texture according to 31.2% of chromium and 68.8% of molybdenum; preparing a titanium-zinc alloy electrolytic plate with uniform texture according to 68.8% of titanium and 31.2% of zinc; preparing manganese-nickel alloy electrolytic plates with uniform textures according to 50% of manganese and 50% of nickel;
dividing a water tank into 4 water tanks through a movable partition plate, namely a water tank A, a water tank B, a water tank C and a water tank D in sequence, then putting two parallel silver-aluminum alloy electrolytic pole plates and chromium-molybdenum alloy electrolytic pole plates into the water tank A, and putting two parallel copper electrolytic pole plates and cobalt electrolytic pole plates into the water tank B; placing two parallel magnesium electrolytic polar plates and an iron electrolytic polar plate into the water tank C; two titanium-zinc alloy electrolytic polar plates and manganese-nickel alloy electrolytic polar plates which are parallel to each other are put into the water tank D;
Step three, respectively installing two electric field polar plates on two sides, which are perpendicular to the electrolytic polar plates, of the outside of the water tank after the electrolytic polar plates are placed in the step two, so as to obtain an electrolytic device;
step four, injecting 1000kg of deionized water into the water tanks A-D in the electrolytic device obtained in the step three; the deionized water is obtained by filtering tap water sequentially through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter; 80g of salicylic acid with the mass concentration of 50% is added into the deionized water;
step five, carrying out electrolytic treatment on the electrolytic device injected with the deionized water in the step four, and obtaining deionized water containing metal ions in each water tank;
total energy consumption of the electrode plate = power consumption of the silver electrolytic electrode plate + power consumption of the copper electrolytic electrode plate + power consumption of the manganese electrolytic electrode plate + power consumption of the zinc electrolytic electrode plate + power consumption of the aluminum electrolytic electrode plate + power consumption of the titanium electrolytic electrode plate + power consumption of the magnesium electrolytic electrode plate + power consumption of the molybdenum electrolytic electrode plate + power consumption of the chromium electrolytic electrode plate + power consumption of the cobalt electrolytic electrode plate + power consumption of the nickel electrolytic electrode plate = 198.7Wh > electric field electrode plate start threshold 100Wh, electric field electrode plate start;
in the water tank A:
The energy consumption ratio of the electrolysis electrode plate=the power consumption of the silver-aluminum electrolysis electrode plate/(the power consumption of the silver-aluminum electrolysis electrode plate+the power consumption of the chromium-molybdenum electrolysis electrode plate) =40 Wh/(40wh+11.5wh) =0.776;
positive pulse width of silver-aluminum electrolytic plate=electrolytic plate reverse phase period×electrolytic plate energy consumption ratio=60 s×0.776=47 s;
positive pulse width of chromium molybdenum electrolysis plate = electrolysis plate reverse phase period-positive pulse width of silver aluminum electrolysis plate = 60s-47s = 13s;
after the 900V direct current voltage is connected, measuring that the passing current of the silver aluminum electrolysis pole plate and the chromium molybdenum electrolysis pole plate is 0.9A;
pulse number=int (3600× (power consumption of silver-aluminum electrolysis plate/(voltage×current))/positive pulse width of silver-aluminum electrolysis plate) =3600× (40/(900×0.9)/47=3.8;
electrolysis time = number of pulses x electrolysis plate inversion period = 3.8 x 60s = 229s;
in the water tank B:
electrolytic plate energy consumption ratio=power consumption of copper electrolytic plate/(power consumption of copper electrolytic plate+power consumption of cobalt electrolytic plate) =0.993;
positive pulse width of copper electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 60s x 0.993 = 59.6s;
positive pulse width of cobalt electrolysis plate = electrolysis plate inversion period-positive pulse width of iron electrolysis plate = 60s-59.6s = 0.4s;
after the direct-current voltage of 900V is connected, the passing current of the copper electrolysis polar plate and the cobalt electrolysis polar plate is 1.2A;
Pulse number=3600× (power consumption of ferroelectric plate/(voltage×current))/positive pulse width of ferroelectric plate=4.5
Electrolysis time = number of pulses x electrolysis plate inversion period = 4.5 x 60s = 269s;
in the water tank C:
the electrolysis plate energy consumption ratio=the power consumption of the magnesium electrolysis plate/(the power consumption of the magnesium electrolysis plate+the power consumption of the ferroelectric plate) =0.735;
positive pulse width of magnesium electrolysis plate = electrolysis plate inversion period x electrolysis plate energy consumption ratio = 44.1s;
positive pulse width of the ferroelectric plate=negative period of the electrolytic plate-positive pulse width of the zinc electrolytic plate=60 s-44.1s=15.9 s;
after 990V direct current voltage is switched on, the passing current of the magnesium electrolysis pole plate and the iron electrolysis pole plate is 1.1A;
pulse number=3600× (power consumption of zinc electrolysis plate/(voltage×current))/positive pulse width of zinc electrolysis plate=4.1;
electrolysis time = number of pulses x electrolysis plate inversion period = 4.1 x 60s = 247s;
in the water tank D:
the electrolysis plate energy consumption ratio=the power consumption of the titanium-zinc electrolysis plate/(the power consumption of the titanium electrolysis plate+the power consumption of the manganese-nickel electrolysis plate) =0.136;
positive pulse width of titanium zinc electrolytic plate=reverse phase period of electrolytic plate×energy consumption ratio of electrolytic plate=60 s×0.136=8 s;
Positive pulse width of manganese nickel electrolytic plate = negative phase period of electrolytic plate-positive pulse width of titanium electrolytic plate = 60s-8s = 52s;
after 900V direct current voltage is connected, the passing current of the titanium zinc electrolytic pole plate and the manganese nickel electrolytic pole plate is 1.0A;
pulse number=3600× (power consumption of titanium zinc electrolytic plate/(voltage×current))/positive pulse width of titanium zinc electrolytic plate=4.3;
electrolysis time = number of pulses x electrolysis plate inversion period = 4.3 x 60s = 259s;
the electrolytic treatment process comprises the following steps: applying ultra-high voltage of 400kV to the two electric field polar plates;
in the water tank A: applying 900V direct current voltage on the silver-aluminum electrolytic pole plate and the chromium-molybdenum electrolytic pole plate, and keeping the silver electrolytic pole plate connected with the positive pole and the copper electrolytic pole plate connected with the negative pole; the direct current voltage is reversed after 47 seconds, the direct current voltage is kept for 13 seconds after the reversing and is repeated for 3.8 times, and water containing silver aluminum and chromium molybdenum metal ions is obtained in a water tank A;
in the water tank B: applying 900V direct current voltage on the copper electrolysis polar plate and the cobalt electrolysis polar plate, and keeping the copper electrolysis polar plate connected with the anode and the cobalt electrolysis polar plate connected with the cathode; the direct current voltage is reversed after 59.6 seconds, the direct current voltage is kept for 0.4 seconds after the direct current voltage is reversed, and the direct current voltage is repeated for 4.5 times, so that water containing copper and cobalt metal ions is obtained in the water tank B;
In the water tank C: applying 900V direct current voltage on the magnesium electrolysis polar plate and the ferroelectric electrolysis polar plate, and keeping the magnesium electrolysis polar plate connected with the anode and the ferroelectric electrolysis polar plate connected with the cathode; the direct current voltage is reversed after 44.1 seconds, and is kept for 15.9 seconds after the reversal, and is repeated for 4.1 times, so that water containing magnesium and iron metal ions is obtained in the water tank C;
in the water tank D: applying 900V direct current voltage on the titanium-zinc electrolytic pole plate and the manganese-nickel electrolytic pole plate, and keeping the titanium-zinc electrolytic pole plate connected with the positive pole and the manganese-nickel electrolytic pole plate connected with the negative pole; the direct current voltage is reversed after 8 seconds, the direct current voltage is kept for 52 seconds after the reversing and is repeated for 4.3 times, and water containing titanium zinc and manganese nickel metal ions is obtained in a water tank D;
the direct current voltage is reversely forward, the positive electrode and the negative electrode of the direct current voltage are subjected to flash for 50 times, and the flash process comprises the following steps: when the direct current voltage is in the forward direction, switching the direct current voltage into a reverse holding time T, and then switching the direct current voltage into a forward holding time T; when the direct current voltage is reverse, switching the direct current voltage into a forward holding time T, and then switching the direct current voltage into a reverse holding time T, wherein T is 100ms;
step six, mixing the deionized water containing metal ions obtained in the water tank A, B, C, D in step five to obtain 4000kg of composite metal ion water containing 0.5ppm of silver ions, 0.2ppm of aluminum ions, 0.05ppm of chromium ions, 0.11ppm of molybdenum ions, 1ppm of copper ions, 0.01ppm of cobalt ions, 0.5ppm of magnesium ions, 0.3ppm of iron ions, 0.22ppm of titanium ions, 0.1ppm of zinc ions, 0.2ppm of manganese ions, 0.2ppm of nickel ions and 10ppm of salicylic acid.
The above description is only of the preferred embodiments of the present invention, and is not intended to limit the present invention. Any simple modification, variation and equivalent variation of the above embodiments according to the technical substance of the invention still fall within the scope of the technical solution of the invention.
Claims (5)
1. The preparation method of the composite metal ion water is characterized by comprising the following steps of:
step one, regarding a water tank as 1 water tank or dividing the water tank into a plurality of water tanks, and then putting two parallel electrolytic polar plates into each water tank to obtain an electrolytic device; the electrolytic polar plate is made of the following materials: an alloy composed of one or more of silver, copper, iron, manganese, zinc, aluminum, titanium, magnesium, molybdenum, chromium, cobalt and nickel;
injecting deionized water into each water tank of the electrolytic device obtained in the first step;
step three, carrying out electrolytic treatment on the electrolytic device injected with the deionized water in the step two, and obtaining deionized water containing metal ions in each water tank; the electrolytic treatment process comprises the following steps: applying direct current voltage to two electrolytic polar plates in each water tank, reversing the direct current voltage after a certain time, keeping a certain time after reversing, and repeating for a plurality of times; the direct-current voltage is 3-900V, two electric field polar plates are respectively arranged on two sides of the outside of the water tank and perpendicular to the electrolytic polar plates in the electrolytic device, and ultrahigh voltage of 30-600 kV is applied to the two electric field polar plates; the direct-current voltage is reversely forward, the positive electrode and the negative electrode of the direct-current voltage are subjected to flash for 5 times to 100 times, and the flash process comprises the following steps: when the direct current voltage is in the forward direction, switching the direct current voltage into a reverse holding time T, switching the direct current voltage into a forward holding time T, and when the direct current voltage is in the reverse direction, switching the direct current voltage into a forward holding time T, and switching the direct current voltage into a reverse holding time T, wherein T is 50 ms-1000 ms;
And step four, mixing the deionized water containing metal ions obtained in the step three in each water tank to obtain the composite metal ion water.
2. The method for preparing composite metal ion water according to claim 1, wherein in the first step, the division is performed by a movable partition plate, and the number of the plurality of water tanks is 2-6.
3. The method for preparing composite metal ion water according to claim 1, wherein in the second step, deionized water is obtained by filtering tap water sequentially through a PP cotton filter, an activated carbon filter and an RO reverse osmosis membrane filter; the deionized water is added with an additive, wherein the additive is sodium hypochlorite, humic acid or salicylic acid.
4. The method for preparing composite metal ion water according to claim 1, wherein the concentration of each metal ion in deionized water containing two metal ions satisfies: power consumption of the electrolytic electrode plate = metal ion concentration x total volume of water in all water tanks x power consumption constant of the electrolytic electrode plate; the power consumption constant is: the electrolytic plate increased the power consumption required for 1ppm solute per 1g deionized water in deionized water with a total dissolved solids content of 10ppm at 38V dc voltage, 60kV/m electric field.
5. The method of claim 4, wherein the electric field plates are not activated when the sum of the power consumption of the two electrolytic plates in each water tank is less than the activation threshold of the electric field plates.
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