CN205151981U - System for sea water salt manufacturing - Google Patents
System for sea water salt manufacturing Download PDFInfo
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- CN205151981U CN205151981U CN201520882348.8U CN201520882348U CN205151981U CN 205151981 U CN205151981 U CN 205151981U CN 201520882348 U CN201520882348 U CN 201520882348U CN 205151981 U CN205151981 U CN 205151981U
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Abstract
The utility model provides a system for sea water salt manufacturing, including grit chamber, nanofiltration membrane filter, ionic membrane reactor and evaporated crystallizer, the grit chamber with the nanofiltration membrane filter intercommunication, nanofiltration membrane filter with ionic membrane reactor intercommunication, the ionic membrane reactor with the evaporated crystallizer intercommunication, the sea water gets into after the grit chamber water intaking receive the filter membrane reactor, the process it intakes to obtain ED after the filter membrane reactor of receiving is handled, ED intake through after handling, the ionic membrane reactor obtains ED strong brine and the light salt solution of ED, the ED strong brine gets into evaporated crystallizer handles can obtain salt. Adopt the utility model discloses an it is reducible 75% that the salt manufacturing system can make follow -up evaporated crystallizer handle the scale, can reduce the totality investment 20% or more, and evaporation area dwindles the back by a wide margin, and the system can save 60% steam consumption, reduction operating power consumption more than 40%.
Description
Technical field
The utility model relates to salt manufacturing field, particularly relates to a kind of system utilizing preparing salt by working up seawater.
Background technology
At present, have more than 100 countries and regions to produce salt in the world, ultimate production is about 2.4 hundred million tons.Main salt producing country is China, the U.S., Russia, Germany, Canada, Britain, India, France, Mexico, Australia.China and U.S.A is two maximum salt producing countries in the world, accounts for 36% of global ultimate production.The method of liquid salt processed (bittern) mainly contains two kinds: saltpan method and multiple-effect evaporation method.Saltpan method comprises receives tide and the step such as brewed brine, and affected by environment very large, the factor such as salinity, geographical position, rainfall amount, steam output of seawater all directly can affect the output of bittern (liquid salt), while product impurity (Ca
2+, Mg
2+, SO
4 2-) content is high.Multiple-effect evaporation method, be take seawater as raw material, produce liquid salt by multistage forced evaporation, its energy consumption is high.
Patent CN200510021859.1 discloses the method for a kind of hydrazine hydrate production byproduct in process salt recycling, the method comprises slurrying, being separated of salt slurry and alkali slurry, the treatment step of salt slurry, the treatment step of alkali slurry and the step such as recycling of mother liquor, complex process, and the treatment process not relating to phosphorus-containing matter in this technique.
Patent CN200510031311.5 discloses a kind of processing method recycled containing volatile or easy decomposition organic impurity Industrial Salts such as amine, phenol, ethers, industrial by-product salt after the method process only can reach industrial salt requirement, the high request of ion film caustic soda salt can not be met, and calcination time be 4 ~ 10 hours, processing cost is high.
Utility model content
For the problems referred to above, it is raw material with seawater that the purpose of this utility model is to provide a kind of, utilizes the system of electrodialysis salt manufacturing.
The technical solution of the utility model is as follows:
A system for preparing salt by working up seawater, it comprises settling pit, nano-filtration membrane filter, ionic membrane reactor and evaporative crystallizer; Described settling pit is communicated with described nano-filtration membrane filter, and described nano-filtration membrane filter is communicated with described ionic membrane reactor, and described ionic membrane reactor is communicated with described evaporative crystallizer;
Seawater enters described nanofiltration membrane reactor after settling pit water intaking, ED water inlet is obtained after described nanofiltration membrane reactor for treatment, described ED water inlet obtains ED strong brine and ED light salt brine after described ionic membrane reactor for treatment, and described ED strong brine enters described evaporative crystallizer process can obtain salt.
Wherein, the aperture of the filter membrane of described nano-filtration membrane filter is 0.2 ~ 0.5 μm, and the transmembrane pressure of described nano-filtration membrane filter is 60 ~ 90Kpa.
Wherein, the working pressure of described nano-filtration membrane filter is 0.5 to 2.0MPa.
Wherein, the nanofiltration membrane that described nano-filtration membrane filter adopts is monovalent ion selective membrane.
Wherein, the flow condition of described ionic membrane reactor is COD≤200mg/L, hardness≤50mg/L, SS≤1.
Wherein, described ionic membrane reactor comprises membrane stack, polar region and hold-down gear, and the anionic membrane that wherein said membrane stack adopts is homogeneous phase ion-selective membrane ACS, and cationic membrane is homogeneous phase monovalent ion selective membrane CIMS.
Wherein, described ionic membrane reactor comprises a hold-down gear and four groups of membrane stacks, and described four groups of membrane stacks are arranged in a hold-down gear.
Wherein, described ionic membrane reactor comprises primary ion membrane reactor and secondary ion membrane reactor, the fresh water pipe of described primary ion membrane reactor is communicated with described secondary ion membrane reactor, and the dense water pipe of described secondary ion membrane reactor and the dense water pipe of described primary ion membrane reactor are all communicated with described evaporative crystallizer.
Wherein, the system of described preparing salt by working up seawater also comprises mechanical filter, described mechanical filter is arranged between described settling pit and described nano-filtration membrane filter, and described seawater enters described mechanical filter after described settling pit water intaking, and then enters described nano-filtration membrane filter.
Further, described mechanical filter is also provided with medicament addition device.
The beneficial effects of the utility model are:
(1) the utility model is that raw material carrys out salt manufacturing with seawater, is proposed a kind of salt extraction process of economical rationality by rational technological design; Compared with existing salt extraction process, the cleanliness factor of the salt that salt making system of the present utility model obtains is high, whole salt-making process is almost discharged without wastewater and waste materials, the by product ED light salt brine obtained can as the former water water inlet of desalimtor, or industrial production circulating water system, and the pouring water of coastland salt-tolerant plant.Whole salt extraction process environmental protection and energy saving, have very high economic benefit and social benefit; Have employed membrane process, omnidistance pollution-free, salt manufacturing efficiency is high, the high purity 98% of obtained salt simultaneously;
(2) the ED strong brine that the utility model obtains after adopting ionic membrane reactor for treatment ED water inlet has the feature of high-cleanness, high, directly can prepare high-quality salt.Adopt method of the present utility model that subsequent evaporation crystallizer treatment scale can be made to reduce 75%, can reduce the overall investment of more than 20%, after evaporation area significantly reduces, system can save the steam consumption quantity of 60%, reduces by more than 40% operation energy consumption.
Accompanying drawing explanation
Fig. 1 is the overall schematic of an embodiment of the system of preparing salt by working up seawater of the present utility model;
Fig. 2 is the overall schematic of another embodiment of the system of preparing salt by working up seawater of the present utility model.
Embodiment
In order to make the object of the system of preparing salt by working up seawater of the present utility model, technical scheme and advantage clearly understand, below in conjunction with concrete drawings and the specific embodiments, the utility model is further elaborated.
It should be noted that, when not conflicting, the embodiment in the application and the feature in embodiment can combine mutually.
See Fig. 1, the utility model provides a kind of method of preparing salt by working up seawater, and it comprises settling pit, nano-filtration membrane filter, ionic membrane reactor and evaporative crystallizer; Described settling pit is communicated with described nano-filtration membrane filter, and described nano-filtration membrane filter is communicated with described ionic membrane reactor, and described ionic membrane reactor is communicated with described evaporative crystallizer; Seawater enters described nanofiltration membrane reactor after settling pit water intaking, ED water inlet is obtained after described nanofiltration membrane reactor for treatment, described ED water inlet obtains ED strong brine and ED light salt brine after described ionic membrane reactor for treatment, and described ED strong brine enters described evaporative crystallizer process can obtain salt.Below be described respectively.
Settling pit, adopts settling pit water intaking and obtains pre-treating seawater after carrying out pre-treatment to seawater; The silt etc. in seawater mainly removed by settling pit.Adopt settling pit in the present embodiment, settling pit can be fetched water on the one hand, can be filtered on the other hand by the mode of natural filtration to seawater;
Nanofiltration membrane reactor, enters after nanofiltration membrane reactor carries out hard-off process from settling pit pre-treating seawater out and obtains ED water inlet, the COD≤200mg/L of wherein said ED water inlet, hardness≤50mg/L (i.e. calcium ions and magnesium ions form A a
2+≤ 25mg/L, Mg
2+≤ 25mg/L); Arranging nanofiltration membrane reactor in the present embodiment is meet ionic membrane flow condition to make ED intake.
Ionic membrane reactor, adopts ionic membrane reactor to carry out concentration to described ED, and described ED water inlet obtains ED strong brine and ED light salt brine after ionic membrane reactor for treatment; TDS in wherein said ED strong brine is 8000mg/L ~ 12000mg/L, pH is 6.5 ~ 8, COD≤200mg/L, SS≤1mg/L; ED light salt brine can as the water inlet of reverse osmosis operation or industrial production circulating water system, and the pouring water of coastland salt-tolerant plant.Through test, ED fresh water accounts for more than 85% of the flooding quantity of whole technique mutually, and this part ED fresh water phase reuse can make the water use efficiency of desalinator improve about 40%.The ED strong brine simultaneously produced can be used for the refined brine of direct evaporative crystallizer or PVC industrial caustic soda electrolyzer.
Evaporative crystallizer, adopts evaporative crystallizer to carry out evaporative crystallization process to described ED strong brine and can obtain salt.Carrying out evaporative crystallization process to ED strong brine and controlling final temperature when normal pressure is 105.5 ~ 107.0 DEG C, solid sodium chloride and concentration and evaporation liquid can be obtained, keep input and output material balance and control the mass percentage 8% ~ 11% of sodium-chlor in concentration and evaporation liquid, the mass percentage 12% ~ 15% of Repone K simultaneously; Here the numerical value of final temperature is under true pressure, and actual temperature is converted into the numerical value under normal pressure according to Charles law; Preferably, evaporation and crystallization mode is forced evaporation or multiple-effect evaporation, final temperature is 106.3 DEG C, this process preferably uses MVR steam heat Compression Evaporation crystallizer or Multi-effect evaporation crystallizer, optimum is MVR steam heat Compression Evaporation crystallizer, improve heat utilization rate, decrease steam consumption, thus consequently reduce CO2 emissions; By the described solid sodium chloride that obtains through dehydration, dry, purified salt can also be obtained.
Salt making system of the present utility model adopts ionodialysis method to be that salt prepared by raw material with seawater, ionodialysis method is a kind of new salt extraction process produced along with electrodialytic membranes technical progress development, it produces bittern by ion-exchange membrane electrodialysis is concentrated, follow-up can vacuum-evaporation purified salt, also liquid salt mode can be supplied to industrial production and directly adopt.This method floor space is few, not the impact of climate condition, and product purity is high.1/10 ~ 1/20 of the saltpan method that personnel needed for electrodialysis ionic membrane method only have China's salt manufacturing to adopt.
Ionic membrane method is a kind of technological line adopting special concentrated ionic membrane in electroosmose process, its technical characterstic carries out high power simmer down to object to dissolved salt in water, its principle be ion-exchange membrane under DC electric field to solution in electrolytical zwitterion select through, namely positively charged ion can through anode membrane, and negatively charged ion can through cavity block.The compartment be made up of dividing plate and film is generally included in ionic membrane reactor, negatively charged ion anode direction in its dense room migrates across former and by the anode membrane detention in light room in light room, positively charged ion then migrates across anode membrane and by the cavity block detention in dense room in dense room to cathode direction, solution thus in light room can be desalinated, solution in dense room then increases concentration, thus cross desalination, concentrated, refining object.Ion-exchange membrane is the most critical part of ion-exchange membrane facility.It is generally acknowledged that practical ion-exchange membrane should possess: selective penetrated property is good, and membrane resistance is little, good chemical stability, higher physical strength and good dimensional stability, lower diffusion and low price etc.In addition, the overall energy consumption level of technique of the present utility model is low, the process energy consumption of ionic membrane reactor depends on the degree that the electric current in membrane stack intermediate ion migration course utilizes, it directly affects electrodialysis and current efficiency and desalting effect, membrane stack average current efficiency >=85% in this technique after tested, far above the current efficiency level of general electrodialysis unit.
The utility model mainly adopts ionic membrane desalination/concentration technique process seawater, the operational condition of ionic membrane can be carried out under normal temperature, normal pressure, and its environmental friendliness, operational process is shockproof, no waste discharge, and operational condition as mild as a dove, the strong brine produced is the salt solution of high-cleanness, high, COD≤50, can direct high-quality Industrial Salt processed, ionic membrane system is to the better tolerance of influent quality, water yield change simultaneously, has the wide advantage of applicable elements.The NaCl content of the ED strong brine that the utility model produces is high, adopt method of the present utility model that subsequent evaporation crystallizer treatment scale can be made to reduce 75%, the overall investment of more than 20% can be reduced, after evaporation area significantly reduces, system can save the steam consumption quantity of 60%, reduces by more than 40% operation energy consumption.
Simultaneously in order to improve the life-span of ionic membrane reactor, improve the processing efficiency of ionic membrane reactor, reduce the working cost of ionic membrane reactor, the flow condition of the utility model to ionic membrane enrichment process limits, it is below 200mg/L that the utility model restriction ED water inlet should meet COD content, SS content is below 1mg/L, and hardness≤50mg/L, ED water inlet can not be oxidisability water body etc.In order to reach ED flow condition, the utility model have employed pre-treatment process (settling pit) and hard-off operation (nano-filtration membrane filter) before ED water inlet.The utility model adopts nano-filtration membrane filter and ionic membrane reactor to organically combine, and farthest improves the processing efficiency of seawater, makes the degree of crystallinity of the ED strong brine obtained high simultaneously, is applicable to very much salt manufacturing and uses.Adopt salt making system of the present utility model the water inlet of of the present utility model more than 90% can be purified as fresh water, the very high salt manufacturing raw material of purity can be obtained simultaneously.
Preferably, as a kind of embodiment, wherein, the aperture of the filter membrane of described nano-filtration membrane filter is 0.2 ~ 0.5 μm, and the transmembrane pressure of described nano-filtration membrane filter is 60 ~ 90Kpa.According to the feature of seawater, the present embodiment adopts nanofiltration membrane divalence or polyvalent ion and the organism of molecular weight between 200 ~ 1000 being had to higher decreasing ratio.Described nanofiltration membrane aperture is nano level, can retain particle diameter 0.001 μm, molecular weight 200 ~ 1000 material.In order to make the treatment effect of ionic membrane reactor good in the utility model, long service life, is provided with the water quality parameter of the water inlet entering ionic membrane reactor, i.e. COD≤the 200mg/L of hard-off strong brine, hardness≤50mg/L, SS≤1.Such flow condition can improve the work-ing life of ionic membrane reactor to greatest extent, thus reduces working cost.
Further, the working pressure of described nano-filtration membrane filter is 0.5 to 2.0MPa.
Further, the nanofiltration membrane that described nano-filtration membrane filter adopts is monovalent ion selective membrane.Monovalent ion nano-filtration membrane filter is have employed as preprocessor in the system of preparing salt by working up seawater of the present utility model, the requirement making the water inlet of ionic membrane reactor meet ionic membrane reactor on the one hand, thus extend the life-span of ionic membrane reactor, most of non-monovalent ion can be retained on the other hand, thus alleviate the processing pressure of follow-up ionic membrane reactor, improve processing efficiency and the work-ing life of subsequent ion membrane reactor.
Preferably, as a kind of embodiment, described ionic membrane reactor comprises membrane stack, polar region and hold-down gear, and the anionic membrane that wherein said membrane stack adopts is the anionic membrane that wherein said membrane stack adopts is homogeneous phase monovalent ion selective membrane ACS, and cationic membrane is homogeneous phase monovalent ion selective membrane CIMS.Monovalent ion permselectivity membrane (the positive and negative adopted in the utility model, hereinafter referred to as monovalence permselective membrane) refer in electrodialysis process, preferential through monovalence (positive and negative) ion, and stop the film of divalence (positive and negative) ion.
In one embodiment, described ionic membrane reactor comprises a hold-down gear and four groups of membrane stacks, and described four groups of membrane stacks are arranged in a hold-down gear.Ionic membrane membrane stack is adopted in ionic membrane reactor; As the ionic membrane membrane stack of nucleus equipment, be made up of 4 groups of membrane stacks in 1 hold-down gear, its a whole set of size is only 2.5m × 0.8m × 1.6m, and complete assembly structure is compact, a people can complete and disassembles and install, be convenient to field management and maintenance during cleaning.(conversion of ton salt power consumption)≤160kWh/tNaCl of ionic membrane reactor of the present utility model, convert≤3kWh/t in amount of inlet water (ton), energy consumption and performance reaches domestic (world) advanced level.Ionic membrane reactor utilizes ion-exchange membrane to the selective penetrated property energy of zwitterion, under the effect of DC electric field, makes zwitterion generation directional migration, thus reach solution separating, purification and concentrated object.
Preferably, as another kind of embodiment, see Fig. 2, described ionic membrane reactor comprises primary ion membrane reactor and secondary ion membrane reactor, the fresh water pipe of described primary ion membrane reactor is communicated with described secondary ion membrane reactor, and the dense water pipe of described secondary ion membrane reactor and the dense water pipe of described primary ion membrane reactor are all communicated with described evaporative crystallizer.
Preferably, as a kind of preferred embodiment, see Fig. 2, the system of preparing salt by working up seawater described in the present embodiment also comprises mechanical filter, described mechanical filter is arranged between described settling pit and described nano-filtration membrane filter, described seawater enters described mechanical filter after described settling pit water intaking, and then enters described nano-filtration membrane filter.Water inlet of the present utility model is seawater, and the water quality of water inlet is generally: TDS:30000 ~ 50000, hardness: 500 ~ 800, COD:300 ~ 500, and the TDS content of this part water inlet is very high, and hardness is very high, and may contain organism in the former water of seawater.Therefore, the present embodiment was also provided with mechanical filter before nanofiltration strainer.Mechanical filter is set and can removes calcium, magnesium ion and organism in seawater by adding flocculation agent.More excellent, can also add sterilant in mechanical filter, the water outlet of the present embodiment setting mechanical filter should reach SS≤1, You Li Lv≤1.5.
Further, described mechanical filter is also provided with medicament addition device.This medicament addition device is used for adding the medicament such as flocculation agent, sterilant.
Further illustrate below by way of specific embodiment.
Embodiment one
See Fig. 1, the system of the preparing salt by working up seawater of the present embodiment comprises:
Settling pit, settling pit is arranged on beach, is fetched water by settling pit, and seawater sends into mechanical filter through carrying pump water station after settling pit natural filtration;
Mechanical filter, at the sea intake place of mechanical filter design medicament toss area, drop into the appropriate medicament such as sterilant, flocculation agent by metering and sterilization, flocculation sediment and filtration treatment are carried out to seawater, make the water outlet of mechanical filter meet SS≤1, You Li Lv≤1.5;
Nano-filtration membrane filter; The water inlet of nano-filtration membrane filter is the seawater through mechanical filter process, and (in the present embodiment, the amount of inlet water of nano-filtration membrane filter is 2.46m
3/ h, can obtain 0.83m after nano-filtration membrane filter process
3the filtrate of/h and 1.63m
3the ED water inlet of/h, the aperture of the nanofiltration membrane in the present embodiment is 10 nanometers, and working pressure is generally 1.0MPa; Nanofiltration membrane operation mainly carries out certain removing, nanofiltration membrane filtering liquid water quality design variable: flow (m to COD organism, hardness ions etc. in seawater quality
3/ h) 0.83, TDS (mg/L) 33981, COD40, hardness (mg/L) 870.Nanofiltration membrane operation selects the extraordinary nanofiltration membrane of customization, has higher decreasing ratio, require Ca in water divalence or polyvalent ion and the organism of molecular weight between 200 ~ 1000
2+, Mg
2+plasma reaches the decreasing ratio of 90%, simultaneously to the Li Yong of water Shuai≤80%.
Ionic membrane reactor; The water inlet of ionic membrane reactor is ED water inlet, can obtain 0.2m after ionic membrane reactor for treatment
3the ED strong brine (TDS is 201200mg/L) of/h and 1.43m
3the ED light salt brine (TDS is 11061mg/L) of/h;
Evaporative crystallizer, adopts evaporative crystallizer to carry out evaporative crystallization process to ED strong brine and can obtain salt.
Ionic membrane reactor in the present embodiment adopts anion/cation film to be respectively monovalent ion selective membrane ACS-CIMS composition ionic membrane device, four membrane stacks are the arrangement of one-level one-part form, under steady-working state, two-phase concentration difference multiple can reach 15 times, membrane stack average current efficiency >=85% in this technique, far above the current efficiency level of general electrodialysis unit.The ionic membrane adopted in ionic membrane reactor is Japan's product homogeneous phase monovalent ion film diaphragm, and four membrane stacks are the arrangement of one-level one-part form.
Water inlet in the present embodiment is seawater outside Bohai Sea Gulf, and the water quality of seawater is in table 1
Seawater water quality parameter outside table 1 Bohai Sea Gulf
| Index name | Index content | Index name | Index content |
| pH | 7.8-8.5 | K +(mg·L -1) | 393-405 |
| Turbidity (NTU) | 10 | Na +(mg·L -1) | 11,042-11,451 |
| TDS(mg·L -1) | 34,227-35,562 | Ca 2+(mg·L -1) | 404-419 |
| SDI | >5 | Mg 2+(mg·L -1) | 1289-1325 |
| COD(mg·L -1) | 70 | Cl -(mg·L -1) | 18,906-19,565 |
| Total hardness (mgL -1) | 597 | SO 4 2-(mg·L -1) | 2342-2396 5 --> |
| Total alkalinity (mgL -1) | 200 | HCO 3 -(mg·L -1) | 142-148 |
The water quality of the ED strong brine that the present embodiment obtains is in table 2.
The water quality parameter of table 2ED strong brine
| Index name | Index content | Index name | Index content |
| pH | 7.8-8.5 | K +(mg·L -1) | 393-405 |
| Turbidity (NTU) | 10 | Na +(mg·L -1) | 55,172-56,081 |
| TDS(mg·L -1) | 201200-218453 | Ca 2+(mg·L -1) | 762-773 |
| SDI | <2 | Mg 2+(mg·L -1) | 471-498 |
| COD(mg·L -1) | 0 | Cl -(mg·L -1) | 92,249-93,381 |
| Total hardness (mgL -1) | 5 | SO 4 2-(mg·L -1) | 286-301 |
| Total alkalinity (mgL -1) | 350 | HCO 3 -(mg·L -1) | 279-285 |
The TDS of the ED strong brine that the present embodiment obtains is 201200mg/L, and wherein 93% is NaCl, and each proportion of composing is more stable, meets QB/T1879-2001 industry standard.
Embodiment two
Other equipment of the present embodiment are identical with embodiment one, and difference is that the ionic membrane reactor in the present embodiment comprises primary ion membrane reactor and secondary ion membrane reactor.The one-level ED light salt brine of primary ion membrane reactor enters secondary ion membrane reactor and processes further and obtain secondary ED light salt brine and secondary ED strong brine.Evaporative crystallizer is entered after one-level ED strong brine and the mixing of secondary ED strong brine.Secondary ED light salt brine can as the water inlet of reverse osmosis operation or industrial production circulating water system, and the pouring water of coastland salt-tolerant plant.
The water quality parameter of the ED strong brine (always) that embodiment two obtains is in table 3.
The water quality parameter of the ED strong brine of table 3 embodiment two
Embodiment two have employed two-stage ionic membrane and filters, and through test under the condition of equal flooding quantity, can obtain the total light salt brine amount of ED for water inlet 1.51m after two-stage ionic membrane filters
3/ h, the reclamation rate of so overall ED light salt brine can reach more than 90%.
This technique continuous and stable production, the steady quality of product liquid salt (NaCl content 200g/L).Electrodialysis preparing salt by concentrating sea water process current efficiency 80 ~ 84%, ratio of desalinization is 20 ~ 30%, and in obtained liquid salt, the content of NaCl can reach 200g/L, and the direct current consumption of NaCl per ton is 160 ~ 180kWh.
Data as can be seen from above:
(1) ED light salt brine and the salt solution concentration difference multiple of ED strong brine are than >=10, and concentration difference multiple is larger.
(2) the application's technique is disposed seawater is concentrated through ionic membrane reactor, produce ED light salt brine and the two kinds of water outlets of ED strong brine respectively, wherein the water outlet water yield of ED light salt brine accounts for 85% of ED water inlet total amount, TDS≤27061mg/L, the water outlet water yield of ED strong brine accounts for into water total amount 15%, TDS >=228820mg/L, system water utilization ratio >=93% of whole ionic membrane reactor.
The above embodiment only have expressed several embodiment of the present utility model, and it describes comparatively concrete and detailed, but therefore can not be interpreted as the restriction to the utility model the scope of the claims.It should be pointed out that for the person of ordinary skill of the art, without departing from the concept of the premise utility, can also make some distortion and improvement, these all belong to protection domain of the present utility model.Therefore, the protection domain of the utility model patent should be as the criterion with claim.
Claims (10)
1. a system for preparing salt by working up seawater, is characterized in that, comprises settling pit, nano-filtration membrane filter, ionic membrane reactor and evaporative crystallizer; Described settling pit is communicated with described nano-filtration membrane filter, and described nano-filtration membrane filter is communicated with described ionic membrane reactor, and described ionic membrane reactor is communicated with described evaporative crystallizer;
Seawater enters described nanofiltration membrane reactor after settling pit water intaking, ED water inlet is obtained after described nanofiltration membrane reactor for treatment, described ED water inlet obtains ED strong brine and ED light salt brine after described ionic membrane reactor for treatment, and described ED strong brine enters described evaporative crystallizer process can obtain salt.
2. the system of preparing salt by working up seawater according to claim 1, is characterized in that, the aperture of the filter membrane of described nano-filtration membrane filter is 0.2 ~ 0.5 μm, and the transmembrane pressure of described nano-filtration membrane filter is 60 ~ 90Kpa.
3. the system of preparing salt by working up seawater according to claim 1, is characterized in that, the working pressure of described nano-filtration membrane filter is 0.5 to 2.0MPa.
4. the system of preparing salt by working up seawater according to claim 1, is characterized in that, the nanofiltration membrane that described nano-filtration membrane filter adopts is monovalent ion selective membrane.
5. the system of preparing salt by working up seawater according to claim 1, is characterized in that, the flow condition of described ionic membrane reactor is COD≤200mg/L, hardness≤50mg/L, SS≤1.
6. the system of preparing salt by working up seawater according to claim 1, it is characterized in that, described ionic membrane reactor comprises membrane stack, polar region and hold-down gear, and the anionic membrane that wherein said membrane stack adopts is homogeneous phase ion-selective membrane ACS, and cationic membrane is homogeneous phase monovalent ion selective membrane CIMS.
7. the system of preparing salt by working up seawater according to claim 6, is characterized in that, described ionic membrane reactor comprises a hold-down gear and four groups of membrane stacks, and described four groups of membrane stacks are arranged in a hold-down gear.
8. the system of preparing salt by working up seawater according to claim 1, it is characterized in that, described ionic membrane reactor comprises primary ion membrane reactor and secondary ion membrane reactor, the fresh water pipe of described primary ion membrane reactor is communicated with described secondary ion membrane reactor, and the dense water pipe of described secondary ion membrane reactor and the dense water pipe of described primary ion membrane reactor are all communicated with described evaporative crystallizer.
9. the system of the preparing salt by working up seawater according to claim 1 to 8 any one, it is characterized in that, the system of described preparing salt by working up seawater also comprises mechanical filter, described mechanical filter is arranged between described settling pit and described nano-filtration membrane filter, described seawater enters described mechanical filter after described settling pit water intaking, and then enters described nano-filtration membrane filter.
10. the system of preparing salt by working up seawater according to claim 9, is characterized in that, described mechanical filter is also provided with medicament addition device.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108503109A (en) * | 2017-02-28 | 2018-09-07 | 吴世阳 | Utilize the natural salt production process of seawater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108503109A (en) * | 2017-02-28 | 2018-09-07 | 吴世阳 | Utilize the natural salt production process of seawater |
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