CN117735791A - Multistage treatment device for industrial high-salinity water desalination - Google Patents
Multistage treatment device for industrial high-salinity water desalination Download PDFInfo
- Publication number
- CN117735791A CN117735791A CN202410175442.3A CN202410175442A CN117735791A CN 117735791 A CN117735791 A CN 117735791A CN 202410175442 A CN202410175442 A CN 202410175442A CN 117735791 A CN117735791 A CN 117735791A
- Authority
- CN
- China
- Prior art keywords
- water
- desalination
- reactor
- filtered
- desalted
- 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.)
- Pending
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 197
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 48
- 239000012528 membrane Substances 0.000 claims abstract description 85
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 30
- 150000003839 salts Chemical class 0.000 claims abstract description 29
- 239000012267 brine Substances 0.000 claims abstract description 26
- 239000002002 slurry Substances 0.000 claims abstract description 21
- 150000001450 anions Chemical class 0.000 claims abstract description 19
- 150000001768 cations Chemical class 0.000 claims abstract description 18
- 238000011033 desalting Methods 0.000 claims abstract description 18
- 150000002500 ions Chemical class 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 238000002242 deionisation method Methods 0.000 claims abstract description 10
- 238000001223 reverse osmosis Methods 0.000 claims description 21
- 238000001728 nano-filtration Methods 0.000 claims description 19
- 239000011347 resin Substances 0.000 claims description 17
- 229920005989 resin Polymers 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 10
- 238000005342 ion exchange Methods 0.000 claims description 9
- 230000009471 action Effects 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 239000000853 adhesive Substances 0.000 claims description 5
- 230000001070 adhesive effect Effects 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 238000001556 precipitation Methods 0.000 claims description 5
- 238000003795 desorption Methods 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 28
- 230000008569 process Effects 0.000 abstract description 14
- 239000000126 substance Substances 0.000 abstract description 10
- 230000033558 biomineral tissue development Effects 0.000 abstract description 5
- 238000005868 electrolysis reaction Methods 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 description 30
- 238000001704 evaporation Methods 0.000 description 6
- 239000004745 nonwoven fabric Substances 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 5
- 239000010410 layer Substances 0.000 description 5
- 239000013078 crystal Substances 0.000 description 4
- 238000000909 electrodialysis Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- -1 hydroxide ions Chemical class 0.000 description 4
- 238000000108 ultra-filtration Methods 0.000 description 4
- 239000004568 cement Substances 0.000 description 3
- 238000009388 chemical precipitation Methods 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- BSKHPKMHTQYZBB-UHFFFAOYSA-N 2-methylpyridine Chemical compound CC1=CC=CC=N1 BSKHPKMHTQYZBB-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 2
- 239000004952 Polyamide Substances 0.000 description 2
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 2
- ULGYAEQHFNJYML-UHFFFAOYSA-N [AlH3].[Ca] Chemical compound [AlH3].[Ca] ULGYAEQHFNJYML-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000012459 cleaning agent Substances 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229920002647 polyamide Polymers 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- RGUKYNXWOWSRET-UHFFFAOYSA-N 4-pyrrolidin-1-ylpyridine Chemical compound C1CCCN1C1=CC=NC=C1 RGUKYNXWOWSRET-UHFFFAOYSA-N 0.000 description 1
- WRDWWAVNELMWAM-UHFFFAOYSA-N 4-tert-butylaniline Chemical compound CC(C)(C)C1=CC=C(N)C=C1 WRDWWAVNELMWAM-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- OJGMBLNIHDZDGS-UHFFFAOYSA-N N-ethyl-N-phenylamine Natural products CCNC1=CC=CC=C1 OJGMBLNIHDZDGS-UHFFFAOYSA-N 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000007900 aqueous suspension Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- UWCPYKQBIPYOLX-UHFFFAOYSA-N benzene-1,3,5-tricarbonyl chloride Chemical compound ClC(=O)C1=CC(C(Cl)=O)=CC(C(Cl)=O)=C1 UWCPYKQBIPYOLX-UHFFFAOYSA-N 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000004132 cross linking Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003864 humus Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 239000002346 layers by function Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000000941 radioactive substance Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000001488 sodium phosphate Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 1
- RYFMWSXOAZQYPI-UHFFFAOYSA-K trisodium phosphate Chemical compound [Na+].[Na+].[Na+].[O-]P([O-])([O-])=O RYFMWSXOAZQYPI-UHFFFAOYSA-K 0.000 description 1
- 229910000406 trisodium phosphate Inorganic materials 0.000 description 1
- 235000019801 trisodium phosphate Nutrition 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- 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
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to the field of desalination treatment, and provides a multistage treatment device for industrial high-salinity water desalination, which comprises the following components: a multi-media filter, a desalination reactor, a high pressure pump, a first pressure vessel, a first water jet, a reactor, a second water jet, a second pressure vessel, and a collection tank; the high-salt water firstly passes through a multi-medium filter to form filtered water, the filtered water enters a desalting reactor, and anions and cations in the filtered water are adsorbed in the electric slurry through a flowing electrode capacitance deionization reaction; after ions are removed from the water to be filtered, the water enters a high-pressure pump, then enters the membrane element of the first pressure container through a one-way valve of the high-pressure pump to be desalted, the water to be filtered is separated into strong brine and desalted water, the desalted water is collected, and the salt in the high-salinity water is reduced through an enrichment method, unlike the traditional method which adopts a chemical dosing or electrolysis mode, so that the process is more environment-friendly, and the mineralization degree of the water cannot be increased in the whole process.
Description
Technical Field
The invention belongs to the technical field of desalination treatment, and particularly relates to a multistage treatment device for industrial high-salinity water desalination.
Background
Various industrial waste water often contains very high concentration of soluble salts, such as sodium salt, potassium salt, calcium salt, magnesium salt and ammonium salt, and anions constituting the salts are usually chloride ion, sulfate ion, nitrate ion, carbonate ion and the like. The total concentration (TDS) of these soluble salts can often be as high as thousands or even tens of thousands of milligrams per liter, in individual cases even hundreds of thousands of milligrams per liter. The discharge of a large amount of salt into natural fresh water body can cause the salinity of surface water and underground water to be increased, thereby changing the physical and chemical properties of water environment and even affecting the stability and health of the ecological system to a certain extent.
Many cities have TDS limitation on discharged wastewater, especially when the treated wastewater is considered to be recycled, the TDS is often required to reach a concentration below a certain level, for example, the total dissolved solids of urban miscellaneous water must be lower than 1000-1500 mg/L; for the occasion with zero emission requirement, the wastewater is considered to enter a production device for recycling, and the soluble salt is also required to be removed; in addition, the too high salt concentration often causes difficulty in biochemical treatment of the wastewater, and in order to ensure effective biochemical treatment of the wastewater, desalination pretreatment of the wastewater with high salt content is also required; many conventional desalination processes, such as reverse osmosis, electrodialysis, ion exchange, etc., produce a certain amount of concentrated (brine) water, requiring additional desalination.
The common desalination processes in the current wastewater treatment include chemical precipitation, ion exchange, reverse osmosis, electrodialysis, evaporative crystallization and the like. Chemical precipitation is removed by changing the pH of the wastewater or adding another acid or salt such that an ion forms a precipitate that is insoluble or poorly soluble in water. Chemical precipitation methods tend to be ineffective in removing total salts due to the introduction of new ions; the ion exchange method adopts anion-cation resin to replace anions and cations in the wastewater, and simultaneously releases hydroxide ions and hydrogen ions into the water respectively to react to generate water. However, the ion exchange sites on the surface of the resin need to be regenerated after being saturated, and the anion and cation resin needs to be regenerated by replacing the adsorbed anions and cations with high-concentration alkali or acid respectively, so that a certain amount of strong brine is generated and needs to be treated separately; reverse osmosis and electrodialysis are used to effect separation of ions from water by moving water or ions across a membrane by reverse osmosis pressure or electric field. Such methods, while obtaining pure water, also produce a certain amount of concentrated (saline) water to be treated, and in addition the potential energy required for the transmembrane motion must be provided by high water pressure or high voltage electric fields, which all require a large amount of energy to be consumed; ion exchange, electrodialysis and reverse osmosis processes remove salts, and the volume of concentrated (brine) water produced typically accounts for more than 30% of the volume of water treated. The evaporating crystallization is to raise the temperature of waste water to over the boiling point of water to make water evaporate into steam and the salt concentration in water reach over the solubility, so that salt forms crystal to separate out from water and the salt is separated from water through centrifugal action. The steam is condensed and then becomes desalted water which can be recycled or discharged into wastewater for treatment. This process requires heating the water to the boiling point of water, with relatively high energy consumption, and with a ton of water evaporation of 30-40 kw. In addition, if the wastewater contains organic matters, the method of evaporation crystallization often cannot thoroughly remove salt; meanwhile, the evaporation tube is easy to scale, so that the service life of the evaporation tube is shortened, and long-term stable operation is difficult to realize.
Embedding toxic and harmful substances such as heavy metals and radioactive substances by the setting action of cement has been performed in europe early in the first half of the last century, and the united states has also begun to use this technology in large quantities in the last 70-80 th century to treat the toxic and harmful substances. Intensive studies have found that the solidification of cement is mainly due to the existence of calcium-aluminum crystals in cement, which are insoluble in water and have strong agglomeration, and have a complex structure formed by crosslinking 4 columnar bodies. The structure ensures that other ions mixed in water can diffuse into the inner cavity of the water to be embedded, and the surrounding hydrogen atoms and hydroxyl ions can be replaced by other ions, so that the ions are fixed in the calcium-aluminum crystal;
in the industrial production process of chemical plants and the like, a large amount of waste water and waste liquid are generated, industrial production data and the like are doped in the waste water, wherein the waste water with the total salt content of more than 1% and including 1% is called high-salt waste water, the waste water contains various substances such as salt, oil, organic heavy metals and the like, along with the continuous development of economy, the waste water quantity is increased year by year, if the waste water is directly discharged into nature, serious influence is caused on the environment, so the waste water needs to be purified, the existing waste water desalination mostly adopts distillation desalination, however, the existing industrial high-salinity water desalination treatment device has the following problems:
1. the existing treatment device for desalting industrial high-salinity water is inconvenient to pretreat the wastewater, so that a large amount of solid block substances in the wastewater are heated and evaporated along with the wastewater, the treatment device is affected to desalt the wastewater, and meanwhile, the wastewater is inconvenient to uniformly heat, so that the evaporation rate is reduced;
2. when the existing treatment device for desalting industrial high-salinity water is used for desalting high-salinity wastewater, salt crystals are adhered to the inner wall of a machine body, and under the condition of long-term accumulation, the device cannot be used, so that the service life of the treatment device is shortened.
Disclosure of Invention
In order to solve at least one technical problem in the background art described above, a first aspect of the present invention provides a multistage treatment apparatus for industrial high salinity water desalination, which reduces salt in high salinity water by an enrichment method, unlike the conventional method in which administration or electrolysis is performed, so that the process is more environment-friendly, and the entire process does not increase the mineralization degree of water.
In order to achieve the above purpose, the present invention adopts the following technical scheme: a multi-stage treatment apparatus for industrial high salinity water desalination, comprising: a multi-media filter, a desalination reactor, a high pressure pump, a first pressure vessel, a first water jet, a reactor, a second water jet, a second pressure vessel, and a collection tank;
the high-salt water firstly passes through a multi-medium filter to form filtered water, the filtered water enters a desalting reactor, and anions and cations in the filtered water are adsorbed in the electric slurry through a flowing electrode capacitance deionization reaction; the water to be filtered enters a high-pressure pump after ions are removed, then enters the membrane element of the first pressure container through a one-way valve of the high-pressure pump to be desalted, and the water to be filtered is separated into strong brine and desalted water; the desalted water is collected, the strong brine enters the first water ejector, the inlet end of the first water ejector is connected with the strong brine, the strong brine forms quick fluid under the action of the first water ejector, meanwhile, the reactor for loading the desalted resin forms negative pressure, the desalted resin reacts with the strong brine to form a mixture in the reactor, part of salt is separated out through precipitation to form low-salt water, the low-salt water is heated through the heater after passing through the second water ejector and the one-way valve of the second water ejector, then enters the inner membrane element of the second pressure container for desalting treatment to obtain the desalted water, and the desalted water is collected in the collecting tank.
Furthermore, the membrane element adopts reverse osmosis or nanofiltration membrane, and is assembled with the water inlet runner grid, the produced water runner material, the produced water central tube and the stress-resistant device by using adhesive.
Further, two types of membrane elements are arranged, namely a first membrane element and a second membrane element, wherein the first membrane element is arranged in a first pressure container, and the second membrane element is arranged in a second pressure container; the first membrane element adopts a nanofiltration membrane; the second membrane element adopts a reverse osmosis membrane.
Further, the desalination reactor is provided with an electric slurry, and anions and cations in the high-salinity water can be adsorbed in the electric slurry through a flow electrode capacitance deionization reaction; an electrode regeneration reactor connected with the desalting reactor, which can regenerate the electric slurry through the electrode regeneration reaction so as to desorb anions and cations into the eluting water; wherein, the electric slurry and the high salinity water, and the electric slurry and the washing and dehydrating water are separated by ion exchange structure, which can simultaneously carry out the adsorption and desorption operations of anions and cations.
Further, the multi-media filter adopts an MMF type multi-media filter.
Further, the high-pressure pump adopts a high-pressure plunger pump HP5V open pump.
The beneficial effects of the invention are as follows:
1. the method adopts high-salt water to firstly pass through a multi-medium filter to form filtered water, the filtered water enters a desalting reactor, and anions and cations in the filtered water are adsorbed in electric slurry through a flowing electrode capacitance deionization reaction; the water to be filtered enters a high-pressure pump after ions are removed, then enters the membrane element through a one-way valve of the high-pressure pump to be desalted, and the water to be filtered is separated into strong brine and desalted water; the desalinated water is collected, the concentrated brine enters a high-pressure pump, the inlet end of the high-pressure pump is connected with the concentrated brine, the concentrated brine forms quick fluid under the action of a water injector, meanwhile, a reactor for loading desalination resin forms negative pressure, the desalination resin reacts with the concentrated brine to form a mixture in the reactor, part of salt is separated out through precipitation to form low-salt water, the low-salt water enters a membrane element in a pressure container for desalination treatment, the desalinated water separated after the treatment is collected, and the salt in the high-salt water is reduced by an enrichment method instead of a chemical administration method, so that the process is more environment-friendly, and the mineralization degree of the water cannot be increased in the whole process.
2. The membrane elements are two types, namely the first membrane element adopting the nanofiltration membrane and the second membrane element adopting the reverse osmosis membrane, monovalent ions are partially removed by the first membrane element, after pretreatment by the nanofiltration membrane, the molecular weight of the trapped organic matters is about 200-400 Da, and then the dissolved salt and the organic matters with the molecular weight of more than 100Da can be filtered by the reverse osmosis membrane treatment of the second membrane element, so that the treatment efficiency can be improved by a multistage treatment mode, and the desalination treatment precision can be ensured.
Additional aspects of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention.
FIG. 1 is a schematic diagram of the structure of a multistage treatment apparatus for industrial high salinity water desalination of the present invention;
FIG. 2 is a schematic view of the structure of the membrane element of the present invention;
wherein: 1. a multi-media filter; 2. a desalination reactor; 3. a high pressure pump; 4. a first pressure vessel; 5. a first water jet; 6. a reactor; 7. a desalination resin storage tank; 8. a second water jet; 9. a heater; 10. a second pressure vessel; 11. a collecting tank; 12. reverse osmosis or nanofiltration membrane membranes; 13. a water inlet runner grid; 14. producing water channel material; 15. a water production central tube; 16. stress-resistant device.
Detailed Description
The invention will be further described with reference to the drawings and examples.
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present invention. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
In the present invention, terms such as "upper", "lower", "left", "right", "front", "rear", "vertical", "horizontal", "side", "bottom", etc. refer to an orientation or a positional relationship based on that shown in the drawings, and are merely relational terms, which are used for convenience in describing structural relationships of various components or elements of the present invention, and do not denote any one of the components or elements of the present invention, and are not to be construed as limiting the present invention.
In the present invention, terms such as "fixedly attached," "connected," "coupled," and the like are to be construed broadly and refer to either a fixed connection or an integral or removable connection; can be directly connected or indirectly connected through an intermediate medium. The specific meaning of the terms in the present invention can be determined according to circumstances by a person skilled in the relevant art or the art, and is not to be construed as limiting the present invention.
Example 1
As shown in fig. 1-2, the present embodiment provides a multistage treatment apparatus for industrial high salinity water desalination, comprising: the high-salt water firstly passes through a multi-medium filter 1, also called a mechanical impurity filter, so as to remove suspended matters, colloid, sediment, clay, humus, particulate matters and other impurities in the water body, the turbidity of the water is reduced to obtain filtered water, the filtered water enters a desalination reactor 2, and anions and cations in the filtered water are adsorbed in the electric slurry through a flowing electrode capacitance deionization reaction; the water to be filtered enters the high-pressure pump 3 after removing ions, then enters the membrane element of the first pressure container 4 through the high-pressure pump one-way valve to carry out desalination treatment, and the membrane element adopts reverse osmosis or nanofiltration membrane 12 to be assembled with the water inlet runner grid 13, the water producing runner material 14, the water producing central pipe 15 and the stress resisting device 16 through adhesives, so that the reverse osmosis or nanofiltration process can be realized, and the water inlet is separated into strong brine and desalted water; collecting desalted water, enabling the desalted water to enter a first water ejector 5, enabling the inlet end of the first water ejector 5 to be connected with the strong brine, enabling the strong brine to form quick fluid under the action of the first water ejector 5, enabling a reactor 6 loaded with desalting resin to form negative pressure, enabling the desalting resin to react with the strong brine in the reactor 6 to form a mixture, separating part of salt through precipitation to form low-salt water, enabling the low-salt water to enter an inner membrane element of a second pressure container 10 again after being heated through a heater 9 after passing through a second water ejector 8 and a one-way valve of the second water ejector 8, and conducting desalting treatment, wherein the desalting resin is stored in a desalting resin storage tank 7, and the desalting resin storage tank 7 is communicated with the reactor 6; when serious pollution or scaling occurs to the membrane element, replacing the new membrane element, and chemically cleaning the replaced membrane element through a cleaning agent; the desalted water generated after treatment is collected in the collecting tank 11, and the salt in the high-salinity water is reduced by an enrichment method, unlike the traditional method which adopts a chemical dosing or electrolysis mode, so that the process is more environment-friendly, and the mineralization degree of the water is not increased in the whole process.
The desalination reactor 2, which has an electric slurry, can absorb anions and cations in the high salinity water into the electric slurry through a flowing electrode capacitance deionization reaction; an electrode regeneration reactor 6 connected to the desalination reactor 2, which is capable of regenerating the slurry through an electrode regeneration reaction to desorb anions and cations into the eluting water; wherein, the electric slurry and the high salinity water, and the electric slurry and the washing and dehydrating water are separated by the ion exchange structure, can simultaneously carry out the adsorption and desorption operation of anions and cations, has high efficiency, and the electric slurry can circulate after desorption, thereby effectively reducing the cost. Fully embody the technical characteristics of safe, low energy consumption, continuous and stable flow electrode capacitance deionization technology.
The multi-medium filter 1 can adopt MMF type multi-medium filter, mainly be applicable to when former water suspension thing content is 30-50mg/L, as the preliminary treatment of industry feed water coarse filtration, ion exchange desalination system, reverse osmosis desalination system, including the jar body, set gradually coarse filtration net in the jar body, the water pump is installed at the top of the jar body, the bottom of water pump is connected with the drinking-water pipe, be equipped with transfer line and pivot in the jar body, the outside motor is connected to the transfer line, the transfer line drives the pivot and rotates, stirring vane is installed in the outside of pivot, stirring vane stirs high salinity water in the inside of inlet tube, high salinity water's filtration efficiency has been improved, can make things convenient for the spot evenly distributed in the high salinity water.
The high-pressure pump 3 adopts a high-pressure plunger pump HP5V open pump, and the volume of the working chamber is periodically changed by means of the reciprocating motion of a piston in the working chamber of a hydraulic cylinder (or by periodically elastically deforming a flexible element such as a diaphragm, a corrugated pipe and the like in the working chamber). Structurally, the working chamber of the reciprocating pump is isolated from the outside by a sealing device and communicated with or closed by a pump valve.
The high-salt water firstly passes through a multi-medium filter to form filtered water, the filtered water enters a desalting reactor, and anions and cations in the filtered water are adsorbed in the electric slurry through a flowing electrode capacitance deionization reaction; the water to be filtered enters a high-pressure pump after ions are removed, then enters the membrane element through a one-way valve of the high-pressure pump to be desalted, and the water to be filtered is separated into strong brine and desalted water; the desalinated water is collected, the concentrated brine enters a high-pressure pump, the inlet end of the high-pressure pump is connected with the concentrated brine, the concentrated brine forms quick fluid under the action of a water injector, meanwhile, a reactor for loading desalination resin forms negative pressure, the desalination resin reacts with the concentrated brine to form a mixture in the reactor, part of salt is separated out through precipitation to form low-salt water, the low-salt water enters a membrane element in a pressure container for desalination treatment, the desalinated water separated after the treatment is collected, and the salt in the high-salt water is reduced by an enrichment method instead of a chemical administration method, so that the process is more environment-friendly, and the mineralization degree of the water cannot be increased in the whole process.
Example 2
In this embodiment, compared with embodiment 1, two types of membrane elements are provided, namely a first membrane element and a second membrane element, wherein the first membrane element is disposed in a first pressure vessel, and the second membrane element is disposed in a second pressure vessel; the first membrane element is assembled by adopting a nanofiltration membrane, a water inlet runner grid, a water producing runner material, a water producing central tube and an adhesive for a stress resistance device, wherein the nanofiltration membrane is annular, the end face of the nanofiltration membrane is provided with the water inlet runner grid, the outer side face of the nanofiltration membrane is provided with the water producing runner material, a wastewater runner is formed between the nanofiltration membrane and the water producing runner material, the inner side face of the nanofiltration membrane is provided with the water producing central tube, a desalted water runner is formed in the water producing central tube, the inner side face of the water producing central tube is provided with stress resistance devices arranged at intervals, the surface of the water producing central tube is provided with a plurality of water through holes, the water producing runner material and the product central tube can be made of PVE material, the stress resistance device is a cylindrical structural member with through holes, after wastewater enters the end face of the nanofiltration membrane through the water inlet runner grid, desalted water and strong brine are separated by utilizing the selective permeability of two sides of the membrane, and the strong brine flows out through the wastewater runner, and the desalted water flows out through the desalted water runner.
The first membrane element partially removes monovalent ions, the osmotic pressure is low in the filtering process of the first membrane element, the operation pressure is lower, one side can remove residual monovalent ions of the desalination reactor, and the other side can utilize lower cost to carry out higher-precision treatment operation on large-capacity inflow water, if the reverse osmosis technology is directly utilized, the reverse osmosis membrane is aged too fast, frequent replacement is needed, a large amount of wastewater is generated, the subsequent desalination treatment is unfavorable, after the nanofiltration membrane is pretreated, the molecular weight of the trapped organic matters is about 200-400 Da, the reverse osmosis membrane is utilized for treatment, the soluble salts and the organic matters with the molecular weight larger than 100Da can be filtered, and the treatment efficiency can be improved by utilizing a multistage treatment mode, and the desalination treatment precision can also be ensured.
The nanofiltration membrane is soaked in a solution of 2.2 weight percent of piperazine and 1.5 weight percent of trisodium phosphate, the soaked ultrafiltration membrane is taken out and placed on a non-woven fabric for 10-15min, then the ultrafiltration membrane is put into a solution of 0.05 weight percent of trimesoyl chloride for soaking for 50s, the surface of the ultrafiltration membrane is taken out and quickly dried by an air heater, and the ultrafiltration membrane is washed with water to obtain the nanofiltration membrane.
The second membrane element is assembled with the water inlet runner grid, the water producing runner material, the water producing central pipe and the adhesive for the stress resisting device by adopting a reverse osmosis membrane, and the structure is consistent with that of the first membrane element, and detailed description is omitted. The reverse osmosis membrane comprises a non-woven fabric layer, a porous supporting layer and a polyamide layer which are sequentially arranged, wherein a solvent formed by 0.6wt% of tetrahydrofuran diacid chloride, 0.5wt% of 4-tertiary butyl aniline and 0.3wt% of 4-pyrrolidinyl pyridine is coated on the surface of the non-woven fabric, the non-woven fabric is solidified to form the porous supporting layer on the surface of the non-woven fabric, the non-woven fabric with the porous supporting layer sequentially contacts with a solution of 2-methylpyridine and an aqueous solution of an ethylaniline compound to form the polyamide functional layer, and the reverse osmosis membrane is obtained through post treatment.
The scale is removed by replacing the membrane element, a new membrane element is replaced, and the replaced membrane element is chemically cleaned by a cleaning agent, so that the pressure vessel cannot accumulate scale for a long time, the service life is effectively prolonged, the treatment efficiency can be improved, and the desalination treatment precision can be ensured by utilizing a multistage treatment mode.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A multi-stage treatment apparatus for the desalination of industrial high salinity water, comprising: a multi-medium filter (1), a desalination reactor (2), a high-pressure pump (3), a first pressure vessel (4), a first water jet (5), a reactor (6), a second water jet (8), a second pressure vessel (10) and a collection tank (11);
the high-salt water firstly passes through a multi-medium filter (1) to form filtered water, the filtered water enters a desalting reactor (2), and anions and cations in the filtered water are adsorbed in the electric slurry through a flowing electrode capacitance deionization reaction; the water to be filtered enters a high-pressure pump (3) after ions are removed, then enters the membrane element of a first pressure container (4) through a one-way valve of the high-pressure pump (3) to be desalted, and the water to be filtered is separated into strong brine and desalted water; the desalted water is collected, the strong brine enters the first water ejector (5), the inlet end of the first water ejector (5) is connected with the strong brine, the strong brine forms quick fluid under the action of the first water ejector (5), meanwhile, the reactor (6) loaded with desalting resin forms negative pressure, the desalting resin reacts with the strong brine to form a mixture in the reactor (6), part of the salt is separated through precipitation to form low-salt water, the low-salt water is heated through the heater (9) after passing through the second water ejector (8) and the second water ejector (8) one-way valve, then enters the inner membrane element of the second pressure container (10) to be desalted to obtain desalted water, and the desalted water is collected in the collecting tank (11).
2. The multistage processing device for industrial high salinity water desalination according to claim 1, wherein the membrane elements are assembled with the inlet runner grid, the produced water runner material, the produced water central tube and the stress-resistant adhesive by using reverse osmosis or nanofiltration membrane membranes.
3. The multistage treatment device for industrial high salinity water desalination according to claim 2, wherein the membrane elements are provided in two types, a first membrane element and a second membrane element, respectively, the first membrane element being provided in the first pressure vessel (4) and the second membrane element being provided in the second pressure vessel (10); the first membrane element adopts a nanofiltration membrane; the second membrane element adopts a reverse osmosis membrane.
4. The multistage treatment device for industrial high salinity water desalination according to claim 1, wherein the desalination reactor (2) has an electric slurry in which anions and cations in the high salinity water can be adsorbed by a flow electrode capacitive deionization reaction; an electrode regeneration reactor (6) connected to the desalination reactor (2) and capable of regenerating the slurry by an electrode regeneration reaction to desorb anions and cations into the eluting water; wherein, the electric slurry and the high salinity water, and the electric slurry and the washing and dehydrating water are separated by ion exchange structure, which can simultaneously carry out the adsorption and desorption operations of anions and cations.
5. The multistage treatment device for industrial high salinity water desalination according to claim 1, wherein the multi-media filter (1) employs an MMF-type multi-media filter.
6. The multistage treatment device for industrial high salinity water desalination according to claim 1, wherein the high pressure pump (3) is a high pressure plunger pump HP5V open pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410175442.3A CN117735791A (en) | 2024-02-08 | 2024-02-08 | Multistage treatment device for industrial high-salinity water desalination |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410175442.3A CN117735791A (en) | 2024-02-08 | 2024-02-08 | Multistage treatment device for industrial high-salinity water desalination |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN117735791A true CN117735791A (en) | 2024-03-22 |
Family
ID=90261174
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202410175442.3A Pending CN117735791A (en) | 2024-02-08 | 2024-02-08 | Multistage treatment device for industrial high-salinity water desalination |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117735791A (en) |
Citations (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20060078594A (en) * | 2006-06-09 | 2006-07-05 | 서희동 | The manufacture method of the mineral adjustment agent, drinking water, table salt and bittern from deep sea water |
| KR20080005682A (en) * | 2006-07-10 | 2008-01-15 | 서희동 | Treatment method of agriculture water from seawater or deep sea water |
| KR20110014745A (en) * | 2009-08-06 | 2011-02-14 | 박귀조 | Method to produce a drinking-water from the underground salty water of the seaside area, the island area or the sea bedrock |
| CN103172203A (en) * | 2013-03-28 | 2013-06-26 | 南京中电环保股份有限公司 | Pretreatment method of anti-osmosis strong brine |
| CN104326591A (en) * | 2014-09-12 | 2015-02-04 | 沈阳远大科技园有限公司 | Modular portable reverse osmosis seawater desalination integration apparatus and use method thereof |
| CN105236630A (en) * | 2015-11-06 | 2016-01-13 | 北京津工海水科技有限公司 | Treatment technology and system for strong brine discharged through reverse osmosis device |
| CN107640860A (en) * | 2017-10-09 | 2018-01-30 | 北京中科康仑环境科技研究院有限公司 | A kind of saliferous industrial wastewater desalination reuse technology of calcic magnesium ion, sulfate ion |
| CN107651794A (en) * | 2016-07-26 | 2018-02-02 | 中国科学院过程工程研究所 | A kind of processing system and processing method of industrial wastewater bio-chemical effluent |
| CN108314269A (en) * | 2018-04-04 | 2018-07-24 | 湖北君集水处理有限公司 | A kind of system and method for macropore denitrogenation acid-basic regenerated waste liquids in water processing and reuse |
| CN108636142A (en) * | 2018-05-07 | 2018-10-12 | 万华化学集团股份有限公司 | A kind of preparation method of composite nanometer filtering film |
| CN110818192A (en) * | 2019-11-20 | 2020-02-21 | 新疆天蓝水清环境服务有限公司 | Industrial park mixed wastewater desalination process |
| US20200180989A1 (en) * | 2018-12-10 | 2020-06-11 | ApHinity, Inc. | High salinity water purification processes and systems |
| CN112374705A (en) * | 2020-12-02 | 2021-02-19 | 邯郸钢铁集团有限责任公司 | High-salinity wastewater treatment process for iron and steel enterprises |
| CN113117527A (en) * | 2021-05-14 | 2021-07-16 | 万华化学集团股份有限公司 | Nanofiltration membrane and preparation method and application thereof |
| CN215712392U (en) * | 2021-08-06 | 2022-02-01 | 烟台金正环保科技有限公司 | High-efficient sea water comprehensive utilization system |
| CN114682102A (en) * | 2020-11-11 | 2022-07-01 | 沃顿科技股份有限公司 | Reverse osmosis membrane and preparation method thereof |
| CN114873816A (en) * | 2022-04-25 | 2022-08-09 | 厦门世达膜工程有限公司 | Phosphate waste water zero release processing system |
| CN114906989A (en) * | 2022-05-24 | 2022-08-16 | 天津高能时代水处理科技有限公司 | Coal chemical industry waste water salt-separation zero-emission process system and treatment method |
| CN217773798U (en) * | 2022-07-14 | 2022-11-11 | 陕西鼎澈膜科技有限公司 | High-pressure nanofiltration membrane element with high-power concentration |
| CN115888428A (en) * | 2022-11-15 | 2023-04-04 | 苏州富淼膜科技有限公司 | High-selectivity nanofiltration composite membrane and preparation method thereof |
| CN116573806A (en) * | 2023-06-07 | 2023-08-11 | 南京大学宜兴环保研究院 | Salt separation system combining reverse osmosis, electrodialysis and nanofiltration and application thereof |
-
2024
- 2024-02-08 CN CN202410175442.3A patent/CN117735791A/en active Pending
Patent Citations (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20060078594A (en) * | 2006-06-09 | 2006-07-05 | 서희동 | The manufacture method of the mineral adjustment agent, drinking water, table salt and bittern from deep sea water |
| KR20080005682A (en) * | 2006-07-10 | 2008-01-15 | 서희동 | Treatment method of agriculture water from seawater or deep sea water |
| KR20110014745A (en) * | 2009-08-06 | 2011-02-14 | 박귀조 | Method to produce a drinking-water from the underground salty water of the seaside area, the island area or the sea bedrock |
| CN103172203A (en) * | 2013-03-28 | 2013-06-26 | 南京中电环保股份有限公司 | Pretreatment method of anti-osmosis strong brine |
| CN104326591A (en) * | 2014-09-12 | 2015-02-04 | 沈阳远大科技园有限公司 | Modular portable reverse osmosis seawater desalination integration apparatus and use method thereof |
| CN105236630A (en) * | 2015-11-06 | 2016-01-13 | 北京津工海水科技有限公司 | Treatment technology and system for strong brine discharged through reverse osmosis device |
| CN107651794A (en) * | 2016-07-26 | 2018-02-02 | 中国科学院过程工程研究所 | A kind of processing system and processing method of industrial wastewater bio-chemical effluent |
| CN107640860A (en) * | 2017-10-09 | 2018-01-30 | 北京中科康仑环境科技研究院有限公司 | A kind of saliferous industrial wastewater desalination reuse technology of calcic magnesium ion, sulfate ion |
| CN108314269A (en) * | 2018-04-04 | 2018-07-24 | 湖北君集水处理有限公司 | A kind of system and method for macropore denitrogenation acid-basic regenerated waste liquids in water processing and reuse |
| CN108636142A (en) * | 2018-05-07 | 2018-10-12 | 万华化学集团股份有限公司 | A kind of preparation method of composite nanometer filtering film |
| US20200180989A1 (en) * | 2018-12-10 | 2020-06-11 | ApHinity, Inc. | High salinity water purification processes and systems |
| CN110818192A (en) * | 2019-11-20 | 2020-02-21 | 新疆天蓝水清环境服务有限公司 | Industrial park mixed wastewater desalination process |
| CN114682102A (en) * | 2020-11-11 | 2022-07-01 | 沃顿科技股份有限公司 | Reverse osmosis membrane and preparation method thereof |
| CN112374705A (en) * | 2020-12-02 | 2021-02-19 | 邯郸钢铁集团有限责任公司 | High-salinity wastewater treatment process for iron and steel enterprises |
| CN113117527A (en) * | 2021-05-14 | 2021-07-16 | 万华化学集团股份有限公司 | Nanofiltration membrane and preparation method and application thereof |
| CN215712392U (en) * | 2021-08-06 | 2022-02-01 | 烟台金正环保科技有限公司 | High-efficient sea water comprehensive utilization system |
| CN114873816A (en) * | 2022-04-25 | 2022-08-09 | 厦门世达膜工程有限公司 | Phosphate waste water zero release processing system |
| CN114906989A (en) * | 2022-05-24 | 2022-08-16 | 天津高能时代水处理科技有限公司 | Coal chemical industry waste water salt-separation zero-emission process system and treatment method |
| CN217773798U (en) * | 2022-07-14 | 2022-11-11 | 陕西鼎澈膜科技有限公司 | High-pressure nanofiltration membrane element with high-power concentration |
| CN115888428A (en) * | 2022-11-15 | 2023-04-04 | 苏州富淼膜科技有限公司 | High-selectivity nanofiltration composite membrane and preparation method thereof |
| CN116573806A (en) * | 2023-06-07 | 2023-08-11 | 南京大学宜兴环保研究院 | Salt separation system combining reverse osmosis, electrodialysis and nanofiltration and application thereof |
Non-Patent Citations (2)
| Title |
|---|
| 朱月海 等: "《工业给水处理》", 30 September 2016, 上海：同济大学出版社, pages: 307 - 309 * |
| 杨座国: "《膜科学技术过程与原理》", 31 August 2009, 上海：华东理工大学出版社, pages: 101 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104016529B (en) | Based on the Coal Chemical Industry salt-containing waste water treatment method of multi-stage countercurrent pole-reversing electroosmosis device | |
| CN108203197B (en) | Processing system who contains salt waste water | |
| CN101896251B (en) | Low energy system and method of desalinating seawater | |
| CN105000737B (en) | A kind of Industrial sewage treatment system and sewage water treatment method | |
| CN201817343U (en) | Zero-emission electroplating wastewater concentration treatment process equipment | |
| CN105000755A (en) | Wastewater zero-emission industrial sewage treatment system and treatment method | |
| CN105712560A (en) | Device and method for treating high-salinity wastewater with forward osmosis technique | |
| CA2976878C (en) | Storage and delivery for a water treatment system and method of using the same | |
| CN207596652U (en) | A kind of highly mineralized mine water near-zero release comprehensive resource PDCES processing systems | |
| CN102086072B (en) | Cyclic utilization method of dyeing and printing advanced treatment wastewater | |
| CN106966536A (en) | Strong brine zero-emission film concentration technology and equipment | |
| CN103787471A (en) | Device and method for processing sodium p-toluenesulfonate waste liquor | |
| CN102718351A (en) | Device and method for sewage desalting | |
| CN205710252U (en) | Positive infiltration technology processes the device of high slat-containing wastewater | |
| CN108328836B (en) | Water inlet control system based on high-salt-content wastewater reduction process | |
| CN202865053U (en) | Processing device for wastewater form circulating cooling water and reverse osmosis concentrated water | |
| CN110759570A (en) | Treatment method and treatment system for dye intermediate wastewater | |
| CN202164179U (en) | Zero-discharge concentration treatment equipment for nickel-containing wastewater | |
| CN105439347B (en) | A kind of mother liquor treatment process and system for the concentration of clopyralid feed separation | |
| CN202164190U (en) | Zero release concentrating treatment device for pyrophosphate copper waste water | |
| CN117735791A (en) | Multistage treatment device for industrial high-salinity water desalination | |
| Wenten et al. | Long-Term Performance of a Pilot Scale Combined Chemical Precipitation-Ultrafiltration Technique for Waste Brine Regeneration at Chevron Steam Flooding Plant. | |
| Bahuguna et al. | Physical method of Wastewater treatment-A review | |
| CN206915894U (en) | A kind of zero-emission equipment of high slat-containing wastewater processing | |
| CN206188546U (en) | Carbide acetylene chemical wastewater zero release processing system |
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 |