CN108483710B - Comprehensive seawater utilization method and system - Google Patents
Comprehensive seawater utilization method and system Download PDFInfo
- Publication number
- CN108483710B CN108483710B CN201810301118.6A CN201810301118A CN108483710B CN 108483710 B CN108483710 B CN 108483710B CN 201810301118 A CN201810301118 A CN 201810301118A CN 108483710 B CN108483710 B CN 108483710B
- Authority
- CN
- China
- Prior art keywords
- seawater
- tank
- reverse osmosis
- water
- absorption tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000013535 sea water Substances 0.000 title claims abstract description 107
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 48
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 claims abstract description 35
- 239000012528 membrane Substances 0.000 claims abstract description 35
- 239000003513 alkali Substances 0.000 claims abstract description 31
- 239000012267 brine Substances 0.000 claims abstract description 30
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 30
- 239000004576 sand Substances 0.000 claims abstract description 29
- 229910052567 struvite Inorganic materials 0.000 claims abstract description 29
- 239000000411 inducer Substances 0.000 claims abstract description 25
- 239000003085 diluting agent Substances 0.000 claims abstract description 22
- 239000011575 calcium Substances 0.000 claims abstract description 20
- 239000000126 substance Substances 0.000 claims abstract description 18
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000013505 freshwater Substances 0.000 claims abstract description 14
- 239000011777 magnesium Substances 0.000 claims abstract description 14
- 239000011159 matrix material Substances 0.000 claims abstract description 5
- 238000010521 absorption reaction Methods 0.000 claims description 39
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 28
- 238000006243 chemical reaction Methods 0.000 claims description 28
- 239000002253 acid Substances 0.000 claims description 23
- 238000010612 desalination reaction Methods 0.000 claims description 21
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 19
- 229910001425 magnesium ion Inorganic materials 0.000 claims description 19
- 238000001914 filtration Methods 0.000 claims description 18
- 229910021529 ammonia Inorganic materials 0.000 claims description 15
- 229910001424 calcium ion Inorganic materials 0.000 claims description 15
- 239000002351 wastewater Substances 0.000 claims description 15
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 14
- 238000004062 sedimentation Methods 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 10
- 239000004115 Sodium Silicate Substances 0.000 claims description 10
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 10
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052911 sodium silicate Inorganic materials 0.000 claims description 10
- 239000006228 supernatant Substances 0.000 claims description 10
- 229910019142 PO4 Inorganic materials 0.000 claims description 9
- 238000012824 chemical production Methods 0.000 claims description 9
- 239000011259 mixed solution Substances 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 claims description 7
- 239000004254 Ammonium phosphate Substances 0.000 claims description 6
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 6
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 claims description 6
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 claims description 6
- 229910000148 ammonium phosphate Inorganic materials 0.000 claims description 6
- 235000019289 ammonium phosphates Nutrition 0.000 claims description 6
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims description 6
- BNIILDVGGAEEIG-UHFFFAOYSA-L disodium hydrogen phosphate Chemical compound [Na+].[Na+].OP([O-])([O-])=O BNIILDVGGAEEIG-UHFFFAOYSA-L 0.000 claims description 6
- 235000019837 monoammonium phosphate Nutrition 0.000 claims description 6
- 238000009287 sand filtration Methods 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 5
- 239000004952 Polyamide Substances 0.000 claims description 4
- 125000004122 cyclic group Chemical group 0.000 claims description 4
- 238000011033 desalting Methods 0.000 claims description 4
- 239000003814 drug Substances 0.000 claims description 4
- 229920002647 polyamide Polymers 0.000 claims description 4
- 229910021536 Zeolite Inorganic materials 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 230000003068 static effect Effects 0.000 claims description 3
- 239000010457 zeolite Substances 0.000 claims description 3
- 238000011001 backwashing Methods 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 abstract description 12
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052791 calcium Inorganic materials 0.000 abstract description 7
- 229910052749 magnesium Inorganic materials 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 6
- 150000003839 salts Chemical class 0.000 abstract description 5
- 235000011121 sodium hydroxide Nutrition 0.000 abstract description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 abstract description 4
- 150000001768 cations Chemical class 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000002245 particle Substances 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract 1
- 229910000029 sodium carbonate Inorganic materials 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- DLYUQMMRRRQYAE-UHFFFAOYSA-N tetraphosphorus decaoxide Chemical compound O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 description 6
- 238000004064 recycling Methods 0.000 description 5
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 230000008092 positive effect Effects 0.000 description 4
- 239000011591 potassium Substances 0.000 description 4
- 229910052700 potassium Inorganic materials 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 238000012377 drug delivery Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 1
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 1
- 239000001099 ammonium carbonate Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a method and a system for comprehensively utilizing seawater, which are characterized in that struvite is generated by adding an inducer and a diluent together with calcium and magnesium plasma in seawater; removing the softened seawater with more than divalent cations in seawater, and treating by a sand filtration-security filtration-mixed matrix reverse osmosis combined membrane device to obtain fresh water; the separated softened strong brine basically removes calcium and magnesium particles, can replace industrial salt to enter the production of an alkali factory, simplifies the process flow of the traditional salt chemical industry, and greatly reduces the cost of salt chemical products such as sodium carbonate or caustic soda and the like. The invention is a new technology with environmental protection, energy saving and comprehensive utilization of seawater resources, and the energy consumption can be reduced and the fresh water production capacity can be improved by utilizing the technology to desalt the seawater.
Description
Technical Field
The invention relates to a seawater desalination technology, in particular to a method and a system for comprehensively utilizing seawater.
Background
The seawater desalination is one of the main methods for solving the crisis of fresh water, and is mainly divided into two main types, namely a distillation method (thermal method) and a reverse osmosis method (membrane method), and more than 20 specific seawater desalination technologies comprise multi-stage flash evaporation, low-temperature multi-effect, reverse osmosis, electrodialysis, vapor compression distillation, dew point evaporation, water and electricity cogeneration, hot membrane cogeneration, seawater desalination technologies utilizing nuclear energy, solar energy, wind energy and tidal energy and the like. Through the development of half a century, industrial technologies which take multistage flash evaporation, multi-effect distillation and reverse osmosis as main flows are formed.
Reverse Osmosis (RO) seawater desalination has been rapidly advanced in recent years, and the desalination installed capacity accounts for more than 65%. However, RO seawater desalination has the problems of high medicament and membrane cost, membrane surface scaling, large process energy consumption, high desalination cost, poor ecological effect of strong brine discharge and the like. In order to prevent the membrane from scaling, a nano-filtration-reverse osmosis combined seawater desalination process is adopted. For example, the nanofiltration-reverse osmosis (NF-RO) seawater desalination process proposed by Hassan A M, Al-Sofi M AK, Al-A moudi A and the like adopts the NF process to remove most of divalent ions and a part of monovalent ions in seawater, and then adopts the high-pressure RO process to further desalt to obtain the desalinated seawater. NF is adopted as the first stage desalination, the scale formation of the RO membrane surface can be effectively avoided, and the osmotic pressure of inlet water is reduced, thereby improving the recovery rate of water and the quality of produced water. However, the nanofiltration membrane also has the problem of membrane surface scaling; and the problem of strong brine after nanofiltration and reverse osmosis is still not solved; the energy-saving advantages of nanofiltration and reverse osmosis are not obvious enough, and the cost of desalinated water is still high. The research on RO seawater desalination at home and abroad mainly focuses on high-performance membranes and energy recovery devices, but the performance of polyamide membranes is nearly the limit, and the maturity of the energy recovery devices is high, so that the search for a new breakthrough point is the key for further improving the RO seawater desalination efficiency.
Disclosure of Invention
The invention aims to solve the technical problem of the prior art and provides a comprehensive seawater utilization method, which utilizes an inducer and a diluent to remove divalent ions in seawater to obtain struvite, desalts softened seawater, recycles strong brine generated in the desalinization process, and has the characteristics of no discharge, no pollution and good comprehensive utilization effect.
The invention also aims to provide a seawater comprehensive utilization system for realizing the method.
The technical problem to be solved by the invention is realized by the following technical scheme, and the invention provides a comprehensive seawater utilization method, which comprises the following steps: (1) sand filtering seawater, adding inducer phosphate and/or ammonium salt into sand filtered seawater, and adjusting Mg in mixed solution2+、NH4 +、PO4 3-To a molar ratio of 1: 0.9-1.2: 1.1-1.2, adding a combined alkali liquor diluent consisting of ammonia water and a sodium silicate aqueous solution, adjusting the pH value of the mixed solution to 7.5-8.0, stirring the mixed solution for reaction, and performing solid-liquid separation to obtain softened seawater and a first product, namely struvite; (2) carrying out air stripping absorption treatment on the softened seawater, absorbing ammonia gas dissolved in the softened seawater by using phosphoric acid, and recycling ammonium phosphate generated after absorption; (3) carrying out sand filtration, security filtration and reverse osmosis treatment on the softened seawater subjected to the stripping absorption treatment to obtain a second product fresh water, wherein the working pressure of the reverse osmosis is 4.0-5.0 MPa; (4) and recovering the strong brine obtained by reverse osmosis to be used as a third product, wherein the third product is used for replacing industrial salt to be used as a soda plant for producing soda or caustic soda chemical products.
As a further improvement of the invention, in the step (1), the inducer is one or more of ammonium dihydrogen phosphate, ammonium hydrogen carbonate and disodium hydrogen phosphate.
As a further improvement of the invention, the steps(1) Adding inducer phosphate and/or ammonium salt, and adjusting Mg in the mixed solution2+、NH4 +、PO4 3-To a molar ratio of 1: 0.9: 1.1.
as a further improvement of the invention, the combined alkali liquor diluent is added in the step (1), the pH value of the mixed solution is adjusted to 8.0, and the mixed solution is stirred for reaction and then subjected to solid-liquid separation to obtain softened seawater and a first product struvite.
As a further improvement of the invention, the combined alkali liquor diluent added in the step (1) consists of ammonia water, silica sol and sodium silicate aqueous solution with the mass concentration of 0.1-0.3%.
As a further improvement of the invention, the mass concentration of the ammonia water in the combined alkali liquor diluent is 1.5%, the mass concentration of the sodium silicate is 0.1%, and the mass concentration of the silica sol is 0.2%.
As a further improvement of the invention, the working pressure of the low-pressure reverse osmosis in the step (3) is 4.5 MPa.
The invention also provides a seawater comprehensive utilization system for realizing the method, which comprises a struvite generating device, a blow-off treatment device, a seawater desalination combined device and a strong brine collecting device.
The struvite generating device is used for reacting seawater with the inducer to obtain struvite, and comprises a first sand filter, a medicine adding tank, a reaction tank and a struvite collecting device.
The inlet tube and the former pond in first sand filter are connected, the outlet pipe and the back pond of straining in first sand filter are connected, add the medicinal cupping including inducer dosing tank and combination alkali lye diluent dosing tank, inducer dosing tank pass through the drug delivery pipe with the back pond of straining is connected, makes inducer and the sea water mixture after straining, combination alkali lye diluent dosing tank pass through the drug delivery pipe with the outlet pipe of back pond of straining is connected to the reaction tank behind the static mixer, makes combination alkali lye diluent and mixed solution misce bene take place the reaction, generates struvite.
The reaction tank is connected with a sedimentation tank, the upper end of the sedimentation tank is connected with a water storage tank, softened seawater supernatant obtained after reaction is stored, and the bottom end of the sedimentation tank is connected with a centrifugal machine; centrifuge passes through the conveying pipeline and is connected with guanite collection device, collects the guanite that the reaction produced, centrifuge passes through the raceway and is connected with the wastewater collection pond, the wastewater collection pond pass through the raceway with the former pond is connected, and the waste water cyclic utilization who obtains the centrifugation.
The stripping device removes gas dissolved in the supernatant after the reaction, and comprises: a stripping tower, an acid absorption tower and a post-treatment tank.
The bottom of the water storage tank is connected with the upper end of the stripping tower through a water delivery pipe by a pump, the bottom of the stripping tower is connected with an effluent collecting well through a water delivery pipe, the effluent collecting well is connected with the post-treatment tank, and softened seawater subjected to stripping treatment is collected.
Blow off the tower bottom and be connected with the air buffer tank through the circuit, blow off the tower top through circuit and acid absorption tower bottom entry linkage, the acid absorption tower top is connected with the air buffer tank after being connected through circuit and draught fan again, the bottom and the phosphoric acid storage tank of acid absorption tower one side are connected, the circuit of acid absorption tower offside bottom through the pump with the absorption tower top is connected, the waste water discharge port of acid absorption tower bottom through the raceway with waste water collecting tank connects, realizes cyclic utilization.
The seawater desalination combined device comprises: the second sand filter, the security filtration, the mixed matrix reverse osmosis combined membrane device and the fresh water collection device; the post-treatment tank is connected with the second sand filter, the cartridge filter and the reverse osmosis membrane module in series through water pipes, and the low-pressure side of the reverse osmosis membrane module is connected with the fresh water collecting device through a water pipe; the strong brine collection device is connected with the high-pressure side of the reverse osmosis membrane component through a strong brine transfer pipe.
As a further improvement of the invention, the reverse osmosis membrane module is a polyamide mixed matrix reverse osmosis membrane module filled with nano zeolite.
As a further improvement of the invention, the first sand filter, the second sand filter and the security filter are respectively connected with back washing.
Compared with the prior art, the invention has the following technical effects:
firstly, seawater is pretreated by adding an inducer and an ammonia water and sodium silicate aqueous solution combined alkali liquor diluent, so that cations with more than two valences in the seawater are removed, precipitate struvite is formed in the process, the ammonia water and sodium silicate aqueous solution combined alkali liquor diluent can be used for enhancing the crystallization precipitation of the struvite, and the content of silicon elements in the struvite is increased;
secondly, the pretreated softened seawater is treated by a reverse osmosis combined membrane device to obtain fresh water; because the pretreatment basically removes the cations with more than two valences in the seawater, the scaling and pollution are reduced, and the cost is saved;
thirdly, the strong brine separated by seawater desalination basically removes calcium and magnesium particles, can be recycled to replace industrial salt to enter an alkali factory for production, comprehensively utilizes seawater in the whole process, obtains various products, and has no emissions and no pollution.
Drawings
FIG. 1 is a schematic diagram of the system architecture of the present invention.
Detailed Description
The embodiments of the present invention will be further described with reference to the accompanying drawings so as to facilitate the further understanding of the present invention by those skilled in the art, and do not limit the right thereto.
Example 1
Collecting near-shore seawater in Hongyun harbor region, wherein Total Dissolved Solids (TDS) of seawater is 34700Mg/L, and Mg2+1080mg/L，Ca2 +395 mg/L，SO4 2-2120 mg/L. The method comprises the following specific steps: filtering seawater with sand, adding inducer ammonium dihydrogen phosphate and disodium hydrogen phosphate to obtain Mg in the mixed reaction solution2+:NH4 +:PO4 3-=1.0:0.9: 1.1. The pH value is adjusted to 8.0 by a combined alkali liquor diluent consisting of 1.5 mass percent of ammonia water, 0.1 mass percent of sodium silicate and 0.2 mass percent of silica sol, the reaction time is 50 minutes, and solid-liquid separation is carried out after the reaction is finished. Supernatant is softened seawater, and solid substance is struvite containing nitrogen 4.8%27.1 percent of phosphorus, 8.5 percent of magnesium, 2.06 percent of calcium, 0.12 percent of sulfur, 0.06 percent of potassium and the like. TDS is about 28500 mg/L. The removal rate of calcium and magnesium ions in the original seawater is 95.63 percent, wherein the removal rate of calcium ions is 91.44 percent, and the removal rate of magnesium ions is 97.17 percent. The supernatant water quality is shown in Table 1.
TABLE 1 Water quality composition comparison table
| Ion(s) | Ca2+ | K+ | Mg2+ | Na+ | SO4 2- |
| Raw seawater | 395 | 265 | 1080 | 9072 | 2120 |
| Treating water | 33.8 | 200 | 30.6 | 8920 | 1930 |
And (3) passing the treated supernatant softened seawater through a stripping tower and an absorption tower to remove ammonia dissolved in the softened seawater, reacting the ammonia with phosphoric acid in an acid absorption tower to generate ammonium phosphate, and recycling the ammonia dissolved in the softened seawater through phosphoric acid.
The softened seawater after the stripping absorption treatment is desalted, the turbidity of the effluent after sand filtration and security filtration is less than 0.3NTU, the SDI is less than 3, the reverse osmosis operating pressure is 4.5MPa, the TDS is less than 800mg/L, and the recovery rate reaches 65%.
Recovering strong brine on the high-pressure side of the reverse osmosis membrane; the recovered concentrated brine does not contain calcium and magnesium ions, can be used for alkali chemical production, and has positive effects of reducing the production cost of the alkali chemical production and simplifying the process flow.
Example 2
Collecting near-shore seawater in Hongyun harbor region, wherein Total Dissolved Solids (TDS) of seawater is 34700Mg/L, and Mg2+1080mg/L，Ca2 +395 mg/L，SO4 2-2120 mg/L. The method comprises the following specific steps: filtering seawater with sand, adding inducer ammonium dihydrogen phosphate and disodium hydrogen phosphate to obtain Mg in the mixed reaction solution2+:NH4 +:PO4 3-=1.0:1.0: 1.1. The pH value is adjusted to 8.0 by a combined alkali liquor diluent consisting of 3 mass percent ammonia water, 0.1 mass percent sodium silicate and 0.3 mass percent silica sol, the reaction time is 50 minutes, and solid-liquid separation is carried out after the reaction is finished. The solid matter is struvite, which contains over thirty elements, such as nitrogen 4.9%, phosphorus pentoxide 27.2%, magnesium 8.5%, calcium 2.05%, sulfur 0.12%, potassium 0.05%, etc. TDS is about 28500 mg/L. The removal rate of calcium and magnesium ions in the original seawater is 95.58 percent, wherein the removal rate of calcium ions is 91.39 percent, and the removal rate of magnesium ions is 97.11 percent.
And (3) passing the treated softened seawater through a stripping tower and an absorption tower to remove ammonia dissolved in the softened seawater, reacting the ammonia with phosphoric acid in an acid absorption tower to generate ammonium phosphate, and recycling the ammonia dissolved in the softened seawater through the phosphoric acid.
And desalting the softened seawater subjected to the stripping absorption treatment, and performing reverse osmosis treatment after sand filtration and security filtration to obtain fresh water.
Recovering strong brine on the high-pressure side of the reverse osmosis membrane; the recovered concentrated brine does not contain calcium and magnesium ions, can be used for alkali chemical production, and has positive effects of reducing the production cost of the alkali chemical production and simplifying the process flow.
Example 3
Collecting near-shore seawater in Hongyun harbor region, wherein Total Dissolved Solids (TDS) of seawater is 34700Mg/L, and Mg2+1080mg/L，Ca2 +395 mg/L，SO4 2-2120 mg/L. The method comprises the following specific steps: filtering seawater with sand, adding inducer ammonium dihydrogen phosphate and disodium hydrogen phosphate to obtain Mg in the mixed reaction solution2+:NH4 +:PO4 3-=1.0:1.1: 1.1. The pH value is adjusted to 8.0 by a combined alkali liquor diluent consisting of 1% ammonia water, 0.3% sodium silicate and 0.1% silica sol, the reaction time is 50 minutes, and solid-liquid separation is carried out after the reaction is finished. The solid matter is struvite, which contains over thirty elements, such as nitrogen 5.0%, phosphorus pentoxide 27.1%, magnesium 8.5%, calcium 2.05%, sulfur 0.12%, potassium 0.05%, etc. TDS is about 28500 mg/L. The removal rate of calcium and magnesium ions in the original seawater is 95.57%, wherein the removal rate of calcium ions is 91.34%, and the removal rate of magnesium ions is 97.11%.
And (3) passing the treated softened seawater through a stripping tower and an absorption tower to remove ammonia dissolved in the softened seawater, reacting the ammonia with phosphoric acid in an acid absorption tower to generate ammonium phosphate, and recycling the ammonia dissolved in the softened seawater through the phosphoric acid.
And desalting the softened seawater subjected to the stripping absorption treatment, and performing reverse osmosis treatment after sand filtration and security filtration to obtain fresh water.
Recovering strong brine on the high-pressure side of the reverse osmosis membrane; the recovered concentrated brine does not contain calcium and magnesium ions, can be used for alkali chemical production, and has positive effects of reducing the production cost of the alkali chemical production and simplifying the process flow.
Example 4
Connecting pipeNear-shore seawater in Harbour of cloud, Total Dissolved Solids (TDS) of seawater 34700Mg/L, wherein Mg2+1080mg/L，Ca2 +395 mg/L，SO4 2-2120 mg/L. The method comprises the following specific steps: filtering seawater with sand, adding inducer ammonium dihydrogen phosphate and disodium hydrogen phosphate to obtain Mg in the mixed reaction solution2+:NH4 +:PO4 3-=1.0:1.2: 1.1. The pH value is adjusted to 8.0 by a combined alkali liquor diluent consisting of 2% ammonia water, 0.2% sodium silicate and 0.2% silica sol, the reaction time is 50 minutes, and solid-liquid separation is carried out after the reaction is finished. The solid matter is struvite, which contains over thirty elements, such as nitrogen 5.1%, phosphorus pentoxide 27.1%, magnesium 8.5%, calcium 2.06%, sulfur 0.12%, potassium 0.05%, etc. TDS is about 28500 mg/L. The removal rate of calcium and magnesium ions in the original seawater is 95.57 percent, wherein the removal rate of calcium ions is 91.31 percent, and the removal rate of magnesium ions is 97.13 percent.
And (3) passing the treated softened seawater through a stripping tower and an absorption tower to remove ammonia dissolved in the softened seawater, reacting the ammonia with phosphoric acid in an acid absorption tower to generate ammonium phosphate, and recycling the ammonia dissolved in the softened seawater through the phosphoric acid.
And desalting the softened seawater subjected to the stripping absorption treatment, and performing reverse osmosis treatment after sand filtration and security filtration to obtain fresh water.
Recovering strong brine on the high-pressure side of the reverse osmosis membrane; the recovered concentrated brine does not contain calcium and magnesium ions, can be used for alkali chemical production, and has positive effects of reducing the production cost of the alkali chemical production and simplifying the process flow.
Referring to fig. 1, the seawater comprehensive utilization system for implementing the seawater comprehensive utilization method described in embodiments 1 to 4 includes a struvite generating device, a stripping treatment device, a seawater desalination combination device, and a concentrated brine collecting device. The system comprises a struvite generating device, a blow-off treatment device, a seawater desalination combined device and a strong brine collecting device; the struvite generating device is used for reacting seawater with the inducer to obtain struvite, and comprises a first sand filter 2, a medicine adding tank 3, a reaction tank 6 and a struvite collecting device 8; the water inlet pipe of the first sand filter 2 is connected with the raw water tank 1, the water outlet pipe of the first sand filter 2 is connected with the filtered water tank 4, the chemical feeding tank 3 comprises an inducer chemical feeding tank and a combined alkali liquor diluent chemical feeding tank, the inducer chemical feeding tank is connected with the filtered water tank 4 through a chemical conveying pipe, so that the inducer is mixed with filtered seawater, the lower part of the filtered water tank 4 is connected with an air blower, so that the inducer is uniformly mixed with the filtered seawater, the combined alkali liquor diluent chemical feeding tank is connected to the reaction tank 6 through a chemical conveying pipe and the water outlet pipe of the filtered water tank 4 after passing through a static mixer 5, so that the combined alkali liquor diluent is uniformly mixed with the mixed solution, and reacts to generate struvite; reaction tank 6 is connected with sedimentation tank 7, sedimentation tank 7 upper portion is connected with tank 11, deposits the softened seawater supernatant that obtains in the storage sedimentation tank 7, sedimentation tank 7 bottom is connected with centrifuge 9, centrifuge 9 is connected with struvite collection device 8, centrifuge 9 bottoms and waste water collecting tank 10 are connected, waste water collecting tank 10 through the pump with former pond 1 is connected, recycles the waste water of collecting.
The stripping device removes gas dissolved in the supernatant after the reaction, and comprises: a stripping tower 14, an acid absorption tower 16 and a post-treatment tank 18;
the bottom of the water storage tank 11 is connected with the upper end of a stripping tower 14 through a water delivery pipe by a pump, the bottom of the stripping tower 14 is connected with an effluent collecting well 15 through a water delivery pipe, and the effluent collecting well 15 is connected with a post-treatment tank 18 and used for collecting softened seawater subjected to stripping treatment;
blow and take off 14 bottoms in the tower and be connected with air buffer tank 17 through the circuit, blow and take off 14 tops in the tower and be connected through circuit and 16 bottoms entry in the acid absorption tower, 16 tops in the acid absorption tower are connected with air buffer tank 17 after circuit and draught fan are connected again, and phosphoric acid storage tank 12 is connected with the bottom of 16 one sides in the acid absorption tower, 16 offside bottoms in the acid absorption tower the circuit through the pump with 16 tops in the absorption tower are connected, the waste water of 16 bottoms in the acid absorption tower get rid of the mouth through with waste water collecting tank 10 connects, realizes cyclic utilization.
The seawater desalination combined device comprises: a second sand filter 19, a cartridge filter 20, a reverse osmosis membrane module 21 and a fresh water collecting device 23; the post-treatment tank 18 is connected with the second sand filter 19, the cartridge filter 20 and the reverse osmosis membrane module 21 in series, and the low-pressure side of the reverse osmosis membrane module 21 is connected with a fresh water collecting device 23; the reverse osmosis membrane is a polyamide mixed matrix reverse osmosis membrane filled with nano zeolite; the first sand filter 2, the second sand filter 19 and the security filter 20 are respectively connected with the back wash 13.
The strong brine collection device is connected with the high-pressure side of the reverse osmosis membrane module 21 through a strong brine storage tank 22 through a strong brine transfer pipe, and collects the filtered strong brine.
Claims (1)
1. A method for comprehensively utilizing seawater is characterized by comprising the following steps: the method comprises the following steps:
taking near-shore seawater in Hongyun harbor region, wherein the total dissolved solid TDS of the seawater is 34700Mg/L, and Mg2+ 1080mg/L，Ca2+ 395 mg/L，SO4 2-2120 mg/L; the method comprises the following specific steps: filtering seawater with sand, adding inducer ammonium dihydrogen phosphate and disodium hydrogen phosphate to obtain Mg in the mixed reaction solution2+:NH4 +:PO4 3-=1.0:0.9: 1.1; a combined alkali liquor diluent consisting of 1.5 mass percent of ammonia water, 0.1 mass percent of sodium silicate and 0.2 mass percent of silica sol is used for regulating the pH value to be 8.0, the reaction time is 50 minutes, and solid-liquid separation is carried out after the reaction is finished;
the treated supernatant softened seawater passes through a stripping tower and an absorption tower to remove ammonia dissolved in the softened seawater, the ammonia reacts with phosphoric acid in an acid absorption tower to generate ammonium phosphate, and the ammonia dissolved in the softened seawater is recycled through phosphoric acid;
desalting the softened seawater after the stripping absorption treatment, and performing reverse osmosis treatment after sand filtration and security filtration to obtain effluent with turbidity less than 0.3NTU, SDI less than 3 and reverse osmosis operating pressure of 4.5 MPa;
recovering strong brine on the high-pressure side of the reverse osmosis membrane; the recovered concentrated brine does not contain calcium and magnesium ions and is used for alkali chemical production;
the seawater comprehensive utilization system for realizing the seawater comprehensive utilization method comprises the following steps: a struvite generating device, a blowing-off treatment device, a seawater desalination combined device and a strong brine collecting device; the struvite generating device is used for reacting seawater with the inducer to obtain struvite, and comprises a first sand filter, a medicine adding tank, a reaction tank and a struvite collecting device; the water inlet pipe of the first sand filter is connected with a raw water tank, the water outlet pipe of the first sand filter is connected with a post-filtration water tank, the chemical adding tank comprises an inducer chemical adding tank and a combined alkali liquor diluent chemical adding tank, the inducer chemical adding tank is connected with the post-filtration water tank through a chemical conveying pipe, so that an inducer is mixed with filtered seawater, the lower part of the post-filtration water tank is connected with an air blower, so that the inducer is uniformly mixed with the filtered seawater, the combined alkali liquor diluent chemical adding tank is connected to the reaction tank through a chemical conveying pipe and the water outlet pipe of the post-filtration water tank after passing through a static mixer, so that the combined alkali liquor diluent is uniformly mixed with the mixed solution, and the reaction is carried out to generate struvite; the reaction tank is connected with a sedimentation tank, the upper part of the sedimentation tank is connected with a water storage tank, softened seawater supernatant obtained by sedimentation in the sedimentation tank is stored, the bottom of the sedimentation tank is connected with a centrifugal machine, the centrifugal machine is connected with a struvite collecting device, the bottom of the centrifugal machine is connected with a wastewater collecting tank, the wastewater collecting tank is connected with the raw water tank through a pump, and collected wastewater is recycled; the stripping device removes gas dissolved in the supernatant after the reaction, and comprises: a stripping tower, an acid absorption tower and a post-treatment tank;
the bottom of the water storage tank is connected with the upper end of the stripping tower through a water delivery pipe by a pump, the bottom of the stripping tower is connected with an effluent collecting well through a water delivery pipe, the effluent collecting well is connected with the post-treatment tank, and softened seawater subjected to stripping treatment is collected;
the bottom of the stripping tower is connected with an air buffer tank through a line, the top of the stripping tower is connected with an inlet at the bottom of the acid absorption tower through a line, the top of the acid absorption tower is connected with an induced draft fan through a line and then connected with the air buffer tank, a phosphoric acid storage tank is connected with the bottom end of one side of the acid absorption tower, the line at the bottom of the opposite side of the acid absorption tower is connected with the top end of the absorption tower through a pump, and a wastewater outlet at the bottom of the acid absorption tower is connected with the wastewater collection tank, so that cyclic utilization is realized;
the seawater desalination combined device comprises: the second sand filter, the cartridge filter, the reverse osmosis membrane module and the fresh water collecting device; the post-treatment tank is connected with the second sand filter tank, the security filter and the reverse osmosis membrane component in series, and the low-pressure side of the reverse osmosis membrane component is connected with a fresh water collecting device; the reverse osmosis membrane is a polyamide mixed matrix reverse osmosis membrane filled with nano zeolite; the first sand filter, the second sand filter and the security filter are respectively connected with back washing;
the strong brine collection device is connected with the high-pressure side of the reverse osmosis membrane module through a strong brine storage tank and a strong brine transfer pipe, and the strong brine after filtration is collected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810301118.6A CN108483710B (en) | 2018-04-04 | 2018-04-04 | Comprehensive seawater utilization method and system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810301118.6A CN108483710B (en) | 2018-04-04 | 2018-04-04 | Comprehensive seawater utilization method and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108483710A CN108483710A (en) | 2018-09-04 |
| CN108483710B true CN108483710B (en) | 2022-03-25 |
Family
ID=63314862
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810301118.6A Active CN108483710B (en) | 2018-04-04 | 2018-04-04 | Comprehensive seawater utilization method and system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108483710B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7305248B2 (en) | 2018-12-10 | 2023-07-10 | エルジー エナジー ソリューション リミテッド | Negative electrode active material, negative electrode containing the same, and lithium secondary battery |
| CN109368945A (en) * | 2018-12-18 | 2019-02-22 | 江苏科技大学 | Sewage from Ships processing and recovery of nitrogen and phosphorus integral system and method based on sea water magnesia source |
| CN110028215A (en) * | 2019-04-26 | 2019-07-19 | 广东益诺欧环保股份有限公司 | The purification device and application of synchronization process ammonium salt waste water and phosphate waste |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1413961A (en) * | 2002-10-21 | 2003-04-30 | 广饶县盐化工业集团总公司 | Method for preparing chemical fertilizer from salt-making mother liquor (bittern) or salt water |
| CN102001763A (en) * | 2010-10-15 | 2011-04-06 | 天津欧纳海洋科技发展有限公司 | Production method for desalting seawater by de-hardening preprocessing |
| CN102173526A (en) * | 2011-03-08 | 2011-09-07 | 天津欧纳海洋科技发展有限公司 | Method for using brine generated after seawater desalination as circulating cooling water for cooling tower of power plant |
-
2018
- 2018-04-04 CN CN201810301118.6A patent/CN108483710B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1413961A (en) * | 2002-10-21 | 2003-04-30 | 广饶县盐化工业集团总公司 | Method for preparing chemical fertilizer from salt-making mother liquor (bittern) or salt water |
| CN102001763A (en) * | 2010-10-15 | 2011-04-06 | 天津欧纳海洋科技发展有限公司 | Production method for desalting seawater by de-hardening preprocessing |
| CN102173526A (en) * | 2011-03-08 | 2011-09-07 | 天津欧纳海洋科技发展有限公司 | Method for using brine generated after seawater desalination as circulating cooling water for cooling tower of power plant |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108483710A (en) | 2018-09-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107265734B (en) | Reverse osmosis concentrated seawater treatment system and method | |
| CN105084587A (en) | Treatment method and equipment of high-salt waste water | |
| CN109231632A (en) | The processing method and system of a kind of highly mineralized mine water reuse and resource utilization | |
| CN208120896U (en) | Can resource recycling power plant desulfurization wastewater zero discharge treatment device | |
| CN108483710B (en) | Comprehensive seawater utilization method and system | |
| CN205603386U (en) | Strong brine zero release membrane concentrator | |
| CN102139983A (en) | Waste water treatment method and system | |
| CN112047553A (en) | PTA high-salinity wastewater treatment, reuse and zero-discharge system and method | |
| CN104909494A (en) | Process for impurity removal and purification of industrial high-concentration brine and special equipment of process | |
| CN105502791A (en) | Coal chemical industry wastewater salt extraction method and facility | |
| CN112919719A (en) | Treatment system and treatment method for shale gas fracturing flowback wastewater | |
| CN105036393A (en) | Treating method and apparatus for high-hardness high-salinity waste water | |
| CN214570785U (en) | System for extracting magnesium sulfate and sodium chloride from desulfurization wastewater | |
| CN212198888U (en) | Desulfurization waste water concentration decrement device based on film evaporation technique | |
| CN205347089U (en) | Desulfurization wastewater treatment system | |
| CN113173674A (en) | High-salinity concentrated water recycling treatment system and method | |
| CN204939142U (en) | Treatment facility of desulfurization waste water that flue gas desulfurization system discharged | |
| CN209411998U (en) | A kind of processing system of highly mineralized mine water reuse and resource utilization | |
| CN101503257B (en) | Method and apparatus for recovering and treating ammonium nitrate condensate liquid wastewater | |
| CN216918911U (en) | Treatment system for zero discharge and recycling of lithium iron phosphate production wastewater | |
| CN218146261U (en) | Zero release industrial water processing system of carbon neutralization | |
| CN105152405A (en) | Method and equipment for treating desulfurization wastewater discharged by flue gas desulfurization system | |
| CN215102628U (en) | Processing system of concentrated water resourceization of high salt | |
| CN112194298B (en) | System and method for recycling wastewater of whole power plant | |
| CN116395875A (en) | High-chlorine desulfurization wastewater zero-emission system and process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20240709 Address after: 230000 B-1015, wo Yuan Garden, 81 Ganquan Road, Shushan District, Hefei, Anhui. Patentee after: HEFEI MINGLONG ELECTRONIC TECHNOLOGY Co.,Ltd. Country or region after: China Address before: 222000 No. 2, Chenguang Road, Huaguoshan Avenue, Haizhou District, Lianyungang City, Jiangsu Province Patentee before: LIANYUNGANG TECHNICAL College Country or region before: China |
|
| TR01 | Transfer of patent right |