CN103253818A - Seawater desalination, resource comprehensive utilization and zero discharge processing system - Google Patents

Seawater desalination, resource comprehensive utilization and zero discharge processing system Download PDF

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CN103253818A
CN103253818A CN2013101380342A CN201310138034A CN103253818A CN 103253818 A CN103253818 A CN 103253818A CN 2013101380342 A CN2013101380342 A CN 2013101380342A CN 201310138034 A CN201310138034 A CN 201310138034A CN 103253818 A CN103253818 A CN 103253818A
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salt
water
swro
reverse osmosis
seawater
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韦相亮
马崇维
余丽雅
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JINDAXING CO Ltd
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JINDAXING CO Ltd
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124Water desalination
    • Y02A20/131Reverse-osmosis

Abstract

The invention discloses a seawater desalination, resource comprehensive utilization and zero discharge processing system. The system comprises an ultrafiltration (UF) system, a seawater reverse osmosis (SWRO) system, a deionized water processing system, namely an UPW system, a mechanical compression system capable of preventing scaling and a salt manufacturing and salt chemical engineering system, wherein the UF system is used for generating pure seawater; the SWRO system is used for generating desalted water and concentrated seawater; the concentrated seawater can be produced into calcium sulfate, sodium chloride, potassium chloride, magnesium sulfate, bromine, magnesium chloride and steam condensed water by virtue of the mechanical compression system and the salt manufacturing and salt chemical engineering system; and the steam condensed water and a part of desalted water flow into the UPW system to generate deionized water. According to the processing system, the relevant projects of seawater desalination, energy source utilization, industrial salt manufacturing and salt chemical engineering are organically combined, so that reasonable allocation and utilization of resources are realized, and the aims of energy conservation, emission reduction, circular economy and zero discharge are fulfilled.

Description

Sea water desaltination, comprehensive utilization of resources and zero discharge treatment system
Technical field
The invention relates to seawater comprehensive utilization, relate in particular to the treatment system of a kind of sea water desaltination, comprehensive utilization of resources and zero release.
Background technology
The global range inner face is resource problem near water, and the safety of water supply faces a severe challenge, the water resources worsening shortages, and water environment situation goes from bad to worse.China accelerates seawater and comprehensive utilization of resources, reduces running cost, and new and high technology and the industrialization of development seawater utilization have the important strategic meaning.
The method of sea water desaltination mainly contains distillation method, electroosmose process and reverse osmosis method, and the rate of recovery is generally at 40-45%.The rate of recovery is low, and energy consumption is big, has caused cost pressure big, has limited expanding economy.
Present SWRO concentrated seawater mainly flows back to sea, surface irrigation or enters Sewage treatment systems, temporarily big problem also do not occur, but its potential harm has caused extensive concern.
Increasing is to supersalinity seawater research and utilize dynamics, makes the SWRO concentrated seawater resource utilization that produces in the desalting process, reaches zero release as far as possible, drops to minimum to the disadvantageous effect of environment and the ecosystem SWRO concentrated seawater.
Adopt technological innovation and combination technique to improve the white war advantage of sea water desaltination, imperative.
Summary of the invention
Purpose of the present invention is to overcome the technical deficiency of sea water desaltination in the past, and a kind of sea water desaltination, comprehensive utilization of resources and zero discharge treatment system are provided.
For achieving the above object, the present invention adopts following technical scheme:
A kind of sea water desaltination, comprehensive utilization of resources and zero discharge treatment system comprise ultrafiltration system, are called for short UF system and seawater reverse osmosis permeable system, are called for short the SWRO system, it is characterized in that described UF system (1) is connected with SWRO system (2); The strong brine that SWRO system (2) produces partly is connected to mechanically compress evaporation concentration system (5), mechanically compress evaporation concentration system (5) is connected with salt manufacturing and salt chemical engineering system (15), and described salt manufacturing and salt chemical engineering system (15) connect institute successively by multiple-effect evaporation salt making system (6), multiple-effect evaporation Repone K processed system (7), bromine system (8), evaporation magnesium chloride system processed (9) and form; The desalination water part that SWRO system (2) produces is transported to the client, after mixing, the water of condensation that another part desalination water and mechanically compress evaporation concentration system (5) and salt manufacturing and salt chemical engineering system (11) produce is transported to the deionized water treatment system, be called for short UPW system (10), described UPW system (10) is by the two-pass reverse osmosis system, be called for short BWRO system (3) and electrodeionization system, be called for short EDI system (4) and form;
Press or the external pressure form in described UF system (1) adopts, material is PVC or PVDF, 0.1 micron of membrane filtration aperture Xiao Yu; This UF system (1) is made up of water inlet system, UF film system, water exhaust system, backwash system, medicine system, airing system, chemical cleaning system and eight unit of robot control system(RCS).
Described SWRO system (2) is two sections seawater reverse osmosis permeable systems of one-level, adopt 58% above superelevation rate of recovery desalination treatment system, working pressure is greater than 5.5MPa, the length of reverse osmosis membrane is 1 meter, the ratio of desalinization of single film is minimum 99.5%, and this SWRO system (2) is made up of security personnel's strainer, high-pressure pump, reverse osmosis membrane assembly, energy recycle device, medicine system, flushing cleaning system and control instruments.
Described BWRO system (3) adopts superelevation rate of recovery RO device, and working pressure is greater than 1.5MPa, and the length of reverse osmosis membrane is 1 meter, the ratio of desalinization of single film minimum 99.8%; This BWRO system is made up of security personnel's strainer, high-pressure pump, reverse osmosis membrane assembly, medicine system, cleaning system and control instruments.
Described EDI system (4).The rate of recovery is 95%, produces water conductivity [ (25 ± 1) ℃ ]≤0.1 μ S/cm; This EDI system (4) is made up of security personnel's strainer, intake pump, EDI membrane module, cleaning system and control instruments.
Described mechanically compress evaporation concentration system (5) adopts crystallization crystal de-sludging method, makes calcium sulfate and silicon-dioxide accelerate salt slurry crystal growth and be not deposited on the surface of heat transfer pipe, effectively prevents the scale problems in the concentration process; This mechanically compress evaporation concentration system (5) is made up of interchanger, degassing tower, vaporizer, compressor, recycle pump, hydrocyclone and plate and frame(type)filter press.
Salt manufacturing and salt chemical engineering system (11) are made up of multiple-effect evaporation salt making system (6), multiple-effect evaporation Repone K processed system (7), bromine system (8), evaporation magnesium chloride system processed (9), utilize steam to adopt multi-effect evaporation system, chemical reaction, single-effect evaporation respectively, produce sodium-chlor, Repone K, sal epsom, bromine and magnesium chloride, produce water of condensation simultaneously.
The invention has the beneficial effects as follows:
(1) takes full advantage of the heat energy of salt manufacturing and salt chemical engineering system, thereby save the energy of salt and salt chemical engineering system, also do not take steam resource in short supply.
(2) adopt superelevation to reclaim reverse osmosis unit and external advanced energy recycle device, to guarantee the fresh water quality, has the superelevation rate of recovery (more than 58%), the characteristic of less energy-consumption (less than 3kwh/m3) and high density concentrated seawater (8.9 ten thousand ppm), high density concentrated seawater can reduce the energy consumption of mechanically compress evaporation concentration unit again as the raw material of salt and salt chemical engineering.
(3) be the calcium sulfate scaling in the concentrated seawater when preventing the mechanically compress evaporation concentration, native system adopts crystallization crystal de-sludging method, and this is to guarantee the operation steady in a long-term of mechanically compress evaporation concentration system.
(4) concentrated seawater carries out salt manufacturing, does not discharge go back to the sea, so the sea is not polluted.
(5) do not add Scale inhibitors in the SWRO water inlet, guaranteed salt and salt chemical product quality.
(6) water constituent in the seawater is made into fresh water and deionized water fully, realizes the comprehensive utilization of water and improves its economic worth.Element in the seawater is effectively extracted, and realizes energy-saving and emission-reduction, recycling economy and zero release target.
(7) to utilize the salt chemical engineering waste heat be that former seawater improves temperature to native system, and the waste heat that utilizes the mechanically compress evaporation concentration to produce heats for strong brine, and salt and salt chemical engineering adopt the multiple-effect evaporation principle, and the effect secondary steam is followed successively by down the heating steam of effect utilizations in.
(8) by treatment system of the present invention, associated item such as energy utilization, sea water desaltination, industrial salt manufacturing and salt chemical engineering are organically combined, realize the reasonable resources configuration using, waste recycling, resource utilization and circulation comprehensive utilization.
Description of drawings
Fig. 1 is the workflow diagram of sea water desaltination of the present invention, comprehensive utilization of resources and zero discharge treatment system.
Reference numeral is as follows:
Figure BDA00003075214600031
Embodiment
Below in conjunction with accompanying drawing the present invention is further described.
The characteristics of seawater are inexhaustible, contain elements such as fresh water and salt, potassium, bromine, magnesium.Utilize the reverse osmosis process production fresh water that desalinizes seawater, and utilize steam to produce Chemicals such as deionized water and salt, calcium sulfate, Repone K, bromine, sal epsom, magnesium chloride for thermal source evaporates, form sea water desaltination-marine chemical industry industry recycling economy chain ring.
As shown in Figure 1, a kind of sea water desaltination of the present invention, comprehensive utilization of resources and zero discharge treatment system, having ultrafiltration system and be UF system 1, SWRO system 2, deionized water treatment system is UPW system 10, a kind of mechanically compress system 5 and salt manufacturing and salt chemical engineering system 11 that can prevent fouling.UF system 1 produces pure seawater, produce desalination water and concentrated seawater through high-recovery SWRO system 2, concentrated seawater is produced calcium sulfate, sodium-chlor, Repone K, sal epsom, bromine, magnesium chloride and steam condensate through preventing the mechanically compress system 5 of fouling and salt manufacturing and salt chemical engineering system 11, steam condensate and part desalination water enter UPW system 10, produce deionized water.
By treatment system of the present invention, associated item such as energy utilization, sea water desaltination, industrial salt manufacturing and salt chemical engineering are organically combined, realize the reasonable resources configuration using, waste recycling, resource utilization and circulation comprehensive utilization.
UF system 1 is made up of water inlet system, UF film system, water exhaust system, backwash system, medicine system, airing system, chemical cleaning system and eight unit of robot control system(RCS).
UF filtering membrane technology has good turbidity removal ability, and unit surface water rate processed height adopts the external pressure form, material is PVC, the membrane filtration aperture is between 0.03-0.2 μ m, and is also littler than the bacterium (0.3 μ m) of the minimum of knowing at present, removes various pathogenic bacterium and bacterium so can sieve up hill and dale.The UF filtering membrane can effectively be removed particulate material, comprises microorganism, also can by reduce to a certain extent disinfection byproduct (DBP) precursor concentration and the restriction sterilizing process in the oxygenant demand reduce disinfection byproduct (DBP).
Because UF filtering membrane, SWRO filtering membrane operational efficiency under 25 ℃ of temperature are the highest, so native system utilizes the waste heat of salt and salt chemical engineering as thermal source, improve seawater temperature, to save the energy consumption of seawater desalination system.
UF system 1 produces pure seawater and enters SWRO system 2.
SWRO system 2 is made up of security personnel's strainer, high-pressure pump, reverse osmosis membrane assembly, energy recycle device, medicine system, flushing cleaning system and control instruments.
Reverse osmosis membrane assembly is the topworks of whole desalination system.It is responsible for removing solubility salinity, colloid, organism and microorganism in the water, makes effluent quality reach user's requirement.According to the water quality situation, adopt ratio of desalinization up to 99.5%.For the rate of recovery that reaches reverse osmosis unit surpasses 58%, best reverse osmosis design scheme is the arrangement that every cover reverse osmosis membrane group adopts two sections of one-levels.Reverse osmosis is no phase transition process, so energy consumption is low, by adopting the energy recovery technology, fresh water power consumption per ton is dropped to below 3.0 degree; Construction period is short, but modular design, and unit scale is flexible.Adopt high reverse osmosis unit and the external advanced energy recycle device of reclaiming, to guarantee fresh water quality, high-recovery, the dense water of less energy-consumption and high density.The dense water of high density can reduce the energy consumption of mechanically compress evaporation concentration unit again as the raw material of salt and salt chemical engineering.Reverse osmosis can be reduced to the saltiness of seawater less than 500mg/l by 32000mg/l.
It is that reverse osmosis was produced water and is supplied to the water user as desalination water after SWRO system 2 handled that the pure seawater that produces by UF system 1 enters two sections reverse osmosis systems of one-level, and strong brine goes to mechanically compress evaporation concentration workshop.
The present invention carries out salt chemical engineering salt manufacturing with the concentrated seawater that SWRO system 2 discharges, and the row of returning sea is not avoided the sea is polluted, and realizes the comprehensive utilization of water and improves its economic worth.Element in the seawater is effectively extracted, and realizes recycling economy and zero release target.In water inlet, do not add Scale inhibitors in the SWRO technology of the present invention, having guaranteed salt and salt chemical product quality, and can save resource, energy-saving and emission-reduction and realize recycling economy.
Mechanically compress evaporation concentration vapo(u)rization system 5 is made up of interchanger, degassing tower, vaporizer, compressor, recycle pump, hydrocyclone and plate and frame(type)filter press.
Owing to contain calcium and vitriol in the high density strong brine, can generate calcium sulfate precipitation, cause scale problems.For avoiding this problem, can from strong brine, isolate calcium and silicon selectively by the way of preferential precipitation.The high density strong brine enters the mechanically compress evaporation concentration device after improving temperature, and mix with concentrated solution by the bottom cycle device, flow to the device top through decollator, be back to bottom of device through heat exchanger again, behind the compressed machine of boiling steam on evaporating pot top, outside heat exchanger tube, condense, and flow out with the condensed water form, remove to produce deionized water.
For the calcium fouling is accumulated in the evaporating pot, calcium sulfate can continue the wetted surface cocycle at evaporating pot.When the salt solution thin film evaporation of moisture in manage, the over-saturation that can become of remaining salt solution film, calcium sulfate and silicon-dioxide can begin to condense.The growth of the material quickening salt oar crystal of precipitation rather than calcium dirt deposition are on heat conducting surface.This fouling precautionary approach is called the preferential precipitation method, for effectively preventing the method for thermal conductor surface scale.
The high density strong brine that the SWRO reverse osmosis system is discharged, the waste heat that utilizes mechanically compress evaporation concentration system 5 to produce improves temperature by one-level heat exchange and secondary heat exchange and carries out heat energy recycling, the high density concentrated seawater can reduce the energy consumption of mechanically compress evaporation concentration unit as the raw material of salt and salt chemical engineering, and this is one of feature.Strong brine after improving temperature enters the mechanically compress evaporation concentration system, and the calcium sulfate, dissolved salt and other composite salt that contain precipitation are separated out from 25 ° of B é circulation bittern.The calcium sulfate of precipitation is separated by hydrocyclone, and 25 ° of B é of part bittern is transported to the salt manufacturing workshop as raw material.In order to keep the concentration of the crystal in the vaporizer, the calcium sulfate that part is separated by whizzer will be back to evaporating pot.
The waste residue that is produced by crystal de-sludging method can be fully utilized and be material of construction, as the calcium sulfate product, thus the element in the seawater is effectively extracted, and realizes recycling economy and zero release target.
In multiple-effect evaporation salt making system 6,25 ° of B é saturated bitterns are through salt manufacturing vapo(u)rization system multiple-effect evaporation crystallization precipitated sodium chloride.It is thermal source steam that steam imitate is adopted in evaporation one, on imitate the heating steam that secondary steam is followed successively by down effect, this is one of feature.It is the finished product purified salt after elutriation, dehydration, drying that the salt manufacturing evaporating pot is discharged the salt slurry; The control of salt-making mother liquor bittern concentration (at this moment salts out about 80%) below 30-32 ° of B é.Salt-making mother liquor (being called bittern) separates Repone K (KCl), magnesium chloride (MgC12), sal epsom (MgSO4) and bromine salt chemical products such as (Br2) for comprehensive utilization.
Characteristics: the quality product height, production rate is fast, the cycle is short, and the production floor space is little, and is affected by environment little, steam, electric power etc. need be arranged as main energy sources.
Gypsum seed concentration and salt solid-to-liquid ratio control method adds a certain amount of solid granularity less than 20 microns gypsum in the salt manufacturing evaporating pot, make vaporizer inner suspension solid amount of gypsum control 4%, play a part nucleus, the status nascendi gypsum of separating out from feed liquid is attached to its surface, prevents that gypsum from separating out fouling at heating tube; The salt of controlling simultaneously in the salt manufacturing evaporating pot is starched solid-to-liquid ratio at 15-30%, and the evaporating pot heating chamber is played souring, slows down the heating tube fouling.
Saturated bittern mixes through the multiple-effect evaporation crystallization with recovery high and tow temperature salt (separating magnesium sulphate) separates out salt, and the salt slurry is the finished product purified salt through dehydration, drying, and salt-making mother liquor (bittern) goes comprehensive utilization to produce salt chemical product.
After imitating the high-temperature condensation water that evaporation produces and the high-temperature condensation water that other salt chemical engineerings produce mixed from the end, through heat exchanger the UF system is intake and to heat, this heat energy recycling is one of this system features.Condensation flow after the cooling is toward the deionized water production technique.
Multiple-effect evaporation Repone K processed system 7 comprises preparation byproduct sal epsom.Bittern is that main dense halogen mixes and converts halogen with containing magnesium chloride, because the chlorine ion concentration raising makes sodium-chlor further separate out because of common-ion effcet.Mix halogen evaporation (128~130 ℃) and separate out high temp. salt (main component is sodium-chlor and magnesium sulfate monohydrate).The separation of two steps obtains sodium-chlor and sal epsom respectively to high temp. salt through tryepan blue formula whizzer.
30-32 ° of B é saturated bittern carries out multiple-effect evaporation through Repone K vapo(u)rization system processed.It is thermal source steam that steam imitate is adopted in evaporation one, on imitate the heating steam that secondary steam is followed successively by down effect, this is one of feature.Mother liquid evaporation clarification clear liquid is cooled to 30-35 ℃ of carnallitite (KCl.MgCl2.6H2O) crystallization and separates out.Because the solubleness of magnesium chloride in water is very big, in carnallitite, add about 50% water after, decompose and make rough Repone K, rough Repone K makes refined potassium chloride after purifying.
High temp. salt is separated into magnesia magma and crude salt with it after diluting with circulation fluid, and crude salt becomes highly industry salt after washing dries.The magnesium sulfate monohydrate that must wet after magnesia magma filter done, circulation fluid removes to dilute high temp. salt.Wet magnesium sulfate monohydrate must be done the sulfuric acid monohydrate magnesium products by dry.
Imitate after the high-temperature condensation water that evaporation produces and the high-temperature condensation water that other salt chemical engineerings produce mix from the end, through heat exchanger seawater is heated to improve the operational efficiency of UF, SWRO, this heat energy recycling is one of this system features.The recirculated cooling water of condenser flows to the deionized water production technique.
In the bromine system 8, because the old halogen bromine content that extracts behind the Repone K improves, mainly the form with magnesium bromide and Sodium Bromide exists, with chlorine oxidation, water vapour distillation bromine.Vapor distillation legal system bromine is with the dense halogen preheating in the Repone K processed, feeds chlorine in reaction tower, with bromine with steam steam, condensation, rectifying, get product.This method is applicable to brominated higher feed liquid, extracts than being easier to.The main raw material of distillation method production bromine is the dense halogen after salt-making mother liquor is obtained through refining Repone K, and concentration is 36~38 ° of B é, and brominated amount can reach 7 ± 0.5g/l, and the pH value is 3.2.As making raw material with bittern, need add sulfuric acid or hydrochloric acid, be acidified to pH value 3~3.5.Ingredient requirement does not contain insolubles.The feed liquid of bromine processed need through preheating, oxidation, distillation, bromine air cooling coagulate, bromine water is separated and process such as rectifying.
Evaporate in the magnesium chloride processed system 9, in order to utilize the waste heat of bromine system, the high temperature bromine extraction waste brine enters evaporating pot automatically from the pressured difference of halogen groove, the water vapor that the is evaporated seawater institute condensation in the device that is condensed, and cause negative pressure to evaporating pot.Complete evaporation of liquid enters the insulation storage tank, and the salt of separating out in the evaporative process sinks to awl and regularly discharges at the end.The clear liquid of the upper strata heat liquid-level controller of flowing through enters flaker.Through the water quench cooling, be condensed into the halogen sheet rapidly, also give the screw input feeder feed by the scraper of rotation with the fragmentation of halogen sheet, the halogen sheet enters storage bunker through spiral conveyer, packs packing at last, namely gets the sheet magnesium chloride product.
The high-temperature condensation water that produces from evaporative process is with after the high-temperature condensation water that other salt chemical engineerings produce mixes, and through heat exchanger seawater heated to improve the operational efficiency of UF, SWRO, and this heat energy recycling is one of this system features.Condensation flow after the cooling is toward the deionized water production technique.
The deionized water treatment system, namely in the UPW system 10, the mechanically compress evaporation concentration obtains the water of condensation of water of condensation and salt manufacturing and salt chemical engineering system, and the desalination water that produces with the SWRO system is mixed into UPW system production deionized water product.
UPW system 10 is made up of BWRO system 3 and EDI system 4, wherein BWRO system works principle and SWRO system similarity.
The EDI system is for after the reverse osmosis system, in order to cancel the acid-alkali regeneration process, replaces traditional hybrid ionic switching technology (MB-DI) with EDI and produces stable deionized water.The EDI system is made up of security personnel's strainer, intake pump, EDI membrane module, cleaning system and control instruments.The advantage of EDI technology is that water quality is relatively stable, than being easier to automatic control, does not need chemical regeneration, the low and without sewage discharge of working cost.

Claims (7)

1. a sea water desaltination, comprehensive utilization of resources and zero discharge treatment system comprise ultrafiltration system, are called for short UF system and seawater reverse osmosis permeable system, are called for short the SWRO system, it is characterized in that described UF system (1) is connected with SWRO system (2); The strong brine that SWRO system (2) produces partly is connected to mechanically compress evaporation concentration system (5), mechanically compress evaporation concentration system (5) is connected with salt manufacturing and salt chemical engineering system (15), and described salt manufacturing and salt chemical engineering system (15) connect institute successively by multiple-effect evaporation salt making system (6), multiple-effect evaporation Repone K processed system (7), bromine system (8), evaporation magnesium chloride system processed (9) and form; The desalination water part that SWRO system (2) produces is transported to the client, after mixing, the water of condensation that another part desalination water and mechanically compress evaporation concentration system (5) and salt manufacturing and salt chemical engineering system (11) produce is transported to the deionized water treatment system, be called for short UPW system (10), described UPW system (10) is by the two-pass reverse osmosis system, be called for short BWRO system (3) and electrodeionization system, be called for short EDI system (4) and form;
2. according to sea water desaltination, comprehensive utilization of resources and the zero discharge treatment system of claim 1, it is characterized in that press or the external pressure form in described UF system (1) adopts, material is PVC or PVDF, 0.1 micron of membrane filtration aperture Xiao Yu; This UF system (1) is made up of water inlet system, UF film system, water exhaust system, backwash system, medicine system, airing system, chemical cleaning system and eight unit of robot control system(RCS).
3. according to sea water desaltination, comprehensive utilization of resources and the zero discharge treatment system of claim 1, it is characterized in that, described SWRO system (2) is two sections seawater reverse osmosis permeable systems of one-level, adopt 58% above superelevation rate of recovery desalination treatment system, working pressure is greater than 5.5MPa, the length of reverse osmosis membrane is 1 meter, the ratio of desalinization of single film is minimum 99.5%, and this SWRO system (2) is made up of security personnel's strainer, high-pressure pump, reverse osmosis membrane assembly, energy recycle device, medicine system, flushing cleaning system and control instruments.
4. according to sea water desaltination, comprehensive utilization of resources and the zero discharge treatment system of claim 1, it is characterized in that described BWRO system (3) adopts superelevation rate of recovery RO device, working pressure is greater than 1.5MPa, the length of reverse osmosis membrane is 1 meter, the ratio of desalinization of single film minimum 99.8%; This BWRO system is made up of security personnel's strainer, high-pressure pump, reverse osmosis membrane assembly, medicine system, cleaning system and control instruments.
5. according to sea water desaltination, comprehensive utilization of resources and the zero discharge treatment system of claim 1, it is characterized in that described EDI system (4).The rate of recovery is 95%, produces water conductivity [ (25 ± 1) ℃ ]≤0.1 μ S/cm; This EDI system (4) is made up of security personnel's strainer, intake pump, EDI membrane module, cleaning system and control instruments.
6. according to sea water desaltination, comprehensive utilization of resources and the zero discharge treatment system of claim 1, it is characterized in that, described mechanically compress evaporation concentration system (5) adopts crystallization crystal de-sludging method, make calcium sulfate and silicon-dioxide accelerate salt slurry crystal growth and be not deposited on the surface of heat transfer pipe, effectively prevent the scale problems in the concentration process; This mechanically compress evaporation concentration system (5) is made up of interchanger, degassing tower, vaporizer, compressor, recycle pump, hydrocyclone and plate and frame(type)filter press.
7. according to sea water desaltination, comprehensive utilization of resources and the zero discharge treatment system of claim 1, it is characterized in that, salt manufacturing and salt chemical engineering system (11) are made up of multiple-effect evaporation salt making system (6), multiple-effect evaporation Repone K processed system (7), bromine system (8), evaporation magnesium chloride system processed (9), utilize steam to adopt multi-effect evaporation system, chemical reaction, single-effect evaporation respectively, produce sodium-chlor, Repone K, sal epsom, bromine and magnesium chloride, produce water of condensation simultaneously.
CN2013101380342A 2013-04-19 2013-04-19 Seawater desalination, resource comprehensive utilization and zero discharge processing system Pending CN103253818A (en)

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CN106276976A (en) * 2015-06-12 2017-01-04 金達行有限公司 A kind of recovery method of magnesium sulfate monohydrate cleaning mixture
CN106698495A (en) * 2016-12-06 2017-05-24 河南同伟建材有限公司 Cleaning system for removing sodium chloride in salt gypsum
CN106745157A (en) * 2016-12-06 2017-05-31 河南同伟建材有限公司 A kind of purging system for bunt gypsum cleaning
CN108046361A (en) * 2017-12-26 2018-05-18 国家海洋局天津海水淡化与综合利用研究所 A kind of high power concentration distillation system for desalination and method based on induction crystallisation
CN108569810A (en) * 2017-09-28 2018-09-25 泰富海洋工程装备(天津)有限公司 A kind of sea water desalination and concentrated seawater processing method and system
CN111423018A (en) * 2020-04-21 2020-07-17 山东海化集团有限公司 Efficient seawater desalination method by membrane method
CN111484178A (en) * 2019-01-29 2020-08-04 洁海瑞泉膜技术(天津)有限公司 Comprehensive treatment method for seawater or strong brine
WO2021000516A1 (en) * 2019-07-02 2021-01-07 江苏科技大学 Swro and mcdi coupled seawater desalination system with energy recovery
CN112707414A (en) * 2020-12-16 2021-04-27 云南科力环保股份公司 Method for removing bromine from high-salinity wastewater
CN114031238A (en) * 2021-12-02 2022-02-11 靖江市亚泰新机电科技有限公司 Process method for realizing comprehensive utilization of seawater resources
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Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003035550A1 (en) * 2001-10-22 2003-05-01 Council Of Scientific And Industrial Research Recovery of sodium chloride and other salts from brine
CN201065345Y (en) * 2007-06-26 2008-05-28 中国电力工程顾问集团华东电力设计院 Device for producing ultra-pure water by desalinizing sea water
CN101234767A (en) * 2008-02-29 2008-08-06 天津长芦海晶集团有限公司 Thick seawater comprehensive utilization technique after seawater desalination
CN101381147A (en) * 2008-10-24 2009-03-11 吴宗生 Sea water calcium-removing concentration utilization method
WO2010077895A1 (en) * 2008-12-30 2010-07-08 General Electric Company Water desalination plant and system for the production of pure water and salt
CN102139891A (en) * 2011-01-27 2011-08-03 山西大学 Method for rapidly manufacturing industrial salt by utilizing sylvine mine and device
CN102659272A (en) * 2012-05-24 2012-09-12 北京赛诺水务科技有限公司 Novel membrane-process sea water desalination and fresh water and salt preparation system and technique
CN202440401U (en) * 2012-01-20 2012-09-19 安纳社环保工程(苏州)有限公司 Anti-scaling disposal system for concentrating high-concentrated seawater into saturated bittern
CN202576139U (en) * 2012-04-01 2012-12-05 烟台洁通水处理技术有限公司 Base-prying sea water desalting plant
CN203229436U (en) * 2013-04-19 2013-10-09 金逹行有限公司 Seawater desalination, resources comprehensive utilization and zero discharge treatment system

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003035550A1 (en) * 2001-10-22 2003-05-01 Council Of Scientific And Industrial Research Recovery of sodium chloride and other salts from brine
CN201065345Y (en) * 2007-06-26 2008-05-28 中国电力工程顾问集团华东电力设计院 Device for producing ultra-pure water by desalinizing sea water
CN101234767A (en) * 2008-02-29 2008-08-06 天津长芦海晶集团有限公司 Thick seawater comprehensive utilization technique after seawater desalination
CN101381147A (en) * 2008-10-24 2009-03-11 吴宗生 Sea water calcium-removing concentration utilization method
WO2010077895A1 (en) * 2008-12-30 2010-07-08 General Electric Company Water desalination plant and system for the production of pure water and salt
CN102139891A (en) * 2011-01-27 2011-08-03 山西大学 Method for rapidly manufacturing industrial salt by utilizing sylvine mine and device
CN202440401U (en) * 2012-01-20 2012-09-19 安纳社环保工程(苏州)有限公司 Anti-scaling disposal system for concentrating high-concentrated seawater into saturated bittern
CN202576139U (en) * 2012-04-01 2012-12-05 烟台洁通水处理技术有限公司 Base-prying sea water desalting plant
CN102659272A (en) * 2012-05-24 2012-09-12 北京赛诺水务科技有限公司 Novel membrane-process sea water desalination and fresh water and salt preparation system and technique
CN203229436U (en) * 2013-04-19 2013-10-09 金逹行有限公司 Seawater desalination, resources comprehensive utilization and zero discharge treatment system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
赵国华等: "《海水淡化工程技术与工艺》", 30 April 2012, article "海水淡化技术设计", pages: 21-71 *

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106276976A (en) * 2015-06-12 2017-01-04 金達行有限公司 A kind of recovery method of magnesium sulfate monohydrate cleaning mixture
CN106276976B (en) * 2015-06-12 2018-07-06 金達行有限公司 A kind of recovery method of magnesium sulfate monohydrate cleaning solution
CN106698495A (en) * 2016-12-06 2017-05-24 河南同伟建材有限公司 Cleaning system for removing sodium chloride in salt gypsum
CN106745157A (en) * 2016-12-06 2017-05-31 河南同伟建材有限公司 A kind of purging system for bunt gypsum cleaning
CN106745157B (en) * 2016-12-06 2018-07-06 河南同伟建材有限公司 A kind of cleaning system for bunt gypsum cleaning
CN108569810A (en) * 2017-09-28 2018-09-25 泰富海洋工程装备(天津)有限公司 A kind of sea water desalination and concentrated seawater processing method and system
CN108046361A (en) * 2017-12-26 2018-05-18 国家海洋局天津海水淡化与综合利用研究所 A kind of high power concentration distillation system for desalination and method based on induction crystallisation
CN108046361B (en) * 2017-12-26 2021-03-30 国家海洋局天津海水淡化与综合利用研究所 High-concentration distillation desalination system and method based on induced crystallization method
CN111484178A (en) * 2019-01-29 2020-08-04 洁海瑞泉膜技术(天津)有限公司 Comprehensive treatment method for seawater or strong brine
WO2021000516A1 (en) * 2019-07-02 2021-01-07 江苏科技大学 Swro and mcdi coupled seawater desalination system with energy recovery
US11339073B2 (en) 2019-07-02 2022-05-24 Jiangsu University Of Science And Technology SWRO and MCDI coupled seawater desalination device system with energy recovery
CN111423018A (en) * 2020-04-21 2020-07-17 山东海化集团有限公司 Efficient seawater desalination method by membrane method
CN112707414A (en) * 2020-12-16 2021-04-27 云南科力环保股份公司 Method for removing bromine from high-salinity wastewater
CN114031238A (en) * 2021-12-02 2022-02-11 靖江市亚泰新机电科技有限公司 Process method for realizing comprehensive utilization of seawater resources
CN115159602A (en) * 2022-07-14 2022-10-11 天津国投津能发电有限公司 Low-temperature multi-effect seawater desalination cleaning sludge online removal system
CN115159602B (en) * 2022-07-14 2023-12-05 天津国投津能发电有限公司 Low-temperature multi-effect seawater desalination cleaning sludge on-line removal system

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