CN108569810A - A kind of sea water desalination and concentrated seawater processing method and system - Google Patents
A kind of sea water desalination and concentrated seawater processing method and system Download PDFInfo
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- CN108569810A CN108569810A CN201710901827.3A CN201710901827A CN108569810A CN 108569810 A CN108569810 A CN 108569810A CN 201710901827 A CN201710901827 A CN 201710901827A CN 108569810 A CN108569810 A CN 108569810A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/09—Bromine; Hydrogen bromide
- C01B7/096—Bromine
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/14—Magnesium hydroxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/26—Magnesium halides
- C01F5/30—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/40—Magnesium sulfates
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
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Abstract
The present invention provides a kind of sea water desalination and concentrated seawater processing methods, include sequentially that sea water desalination, low bittern air blow after bromine, bromine that water neutralizes, prepares edible salt, prepare magnesium sulfate, prepare potassium chloride, height bittern air blows bromine and prepares magnesium chloride.The system of sea water desalination provided by the invention and concentrated seawater processing method includes that the heat power generating system being sequentially connected to, low temperature distillation system, low brine blow bromine system, neutralization department, edible salt preparation system, freezing and crystallizing system, potassium chloride preparation system, height brine and blows bromine system and magnesium chloride preparation system.Compared with prior art; sea water desalination provided by the invention and concentrated seawater processing method and system make full use of seawater resources, heat resource and kinetic energy resource in sea water desalination; make full use of the value of seawater; realize sea water desalination zero-emission; effective protection environment; it solves the problems, such as that marine environmental pollution is caused in concentrated seawater discharge sea, takes full advantage of seawater resources.
Description
Technical field
It is a kind of sea water desalination and concentrated seawater processing method and system the present invention relates to field of seawater desalination, more particularly to
The method and system that a kind of desalination of low temperature seawater and concentrated seawater recycle.
Background technology
Sea water desalination industry is the industry greatly developed, revitalized in country 13, and field of seawater desalination faces at present
Main predicament includes：
1, desalination water production cost is excessively high, constrains the development of sea water desalination industry, the development of sea water desalination industry technology
One important directions is effective reduction sea water desalination water cost.
2, as sea water desalination industry is risen, discharge harmful effect caused by environment of byproduct concentrated seawater is gradually shown
Dew, the environmental issue that sea water desalination industry is faced is also more and more prominent, and sea water desalination treated concentrated seawater, generally use is returned
The mode of defeated ocean is handled, and the concentrated seawater concentration after desalinating is higher than former concentration of seawater, and concentrated seawater temperature is higher after desalination,
In line ocean, can be unfavorable to the balance of the marine eco-environment and protection, while the heat that concentrated seawater carries also is wasted.
It is to solve the effective way of concentrated seawater emission problem using concentrated seawater salt manufacturing.But existing desalinator institute is secondary
The concentrated seawater of production will produce calcium sulfate scaling in further evaporating concentration process, vaporising device caused to be unable to operate normally.By
In that cannot solve the problems, such as that calcium sulfate scaling, concentrated seawater all return to sea substantially, very big pollution is caused to the marine eco-environment.China
Application for a patent for invention CN 106186498A disclose it is a kind of using frequently pole-reversing electroosmosis carry out concentrated seawater utilization system and
Method belongs to concentrated seawater and utilizes technical field；The system concentrated seawater continues to concentrate dense by autofrequently changing pole electro dialysis device
Seawater stops divalent ion using the selective penetrated property of amberplex, prevents fouling of evaporator.Although the system utilizes compact
High-performance device recycles sea water desalination by-product concentrated seawater, but the system is discharged the divalent ion in concentrated seawater as waste material,
Seawater can not be still utilized to greatest extent.
The present invention is directed to by technological innovation, by by sea water desalination and sea water desalination byproduct high fever concentrated seawater handle into
Row is integrated, integrates, and has not only realized that concentrated seawater zero-emission, production process is pollution-free, but also can pass through sea water desalination and concentrated seawater processing
Between it is mutual using reaching the maximized effect of seawater resources utilization rate.
Invention content
The purpose of the present invention is overcoming the above-mentioned prior art, one kind is provided, is used for.
To achieve the goals above, technical solution provided by the invention is：
A kind of sea water desalination and concentrated seawater processing method, include the following steps：
Seawater is delivered to low temperature distillation system and carries out sea water desalination by step a), and byproduct concentrated seawater is spare；
Concentrated seawater obtained by step b) steps a) carries out low bittern air and blows bromine, and water is spare after bromine；
Water is neutralized with magnesia after step c) steps b) gained bromines, and neutral brine is obtained after filtering off precipitation, spare；
Neutral brine obtained by step c) is carried out beach field and shone again by step d), and solid phase is precipitated and prepares edible salt, after shining again
Magnesium sulfate solid phase is precipitated in the freezing of high temperature mother liquor, and slurry settles after remaining liquid phase cold mother liquor heating evaporation, obtains height halogen
Water and potassium chloride；
Height brine obtained by step e) steps d) carries out height bittern air and blows bromine, and liquid is spare after bromine；
Liquid heating evaporation prepares magnesium chloride after bromine obtained by step f) steps e).
As a further improvement of the above technical scheme：
Preferably, the concrete operations of the step a) are：It is carried out using sea water pump extracting seawater supply low temperature distillation system
Sea water desalination obtains fresh water and concentrated seawater (i.e. low brine)；Wherein, the fresh water that low temperature distillation system generates can be divided in portion
It is delivered to municipal network water supply, factory industry uses water or is delivered to back boiler as boiler feedwater, and such heat supply back boiler (or
Chemical plant, steam power plant) output low-grade steam circulation supply low temperature distillation system to continue sea water desalination.
Preferably, the concrete operations of the step b) are：(i.e. by high temperature concentrated seawater obtained by low temperature distillation system in step a)
Low brine) it is delivered to low brine and blows bromine system, bromine is produced, and water after the bromine after tentatively extracting bromine is spare.
Preferably, the concrete operations of the step c) are：Water after bromine obtained by step b) is sent into neutralization department, to neutralization vehicle
Between middle addition magnesia neutralize, generate magnesium hydrate precipitate, it is spare to obtain neutral brine.
The concrete operations that edible salt is prepared in the step d) are：Neutral brine obtained by step c) is pumped into beach field to carry out
It is in saturation state that solarization natural evaporation, which is concentrated into sodium chloride, and the neutral brine after concentration is discharged into crystallizing pond, and solid sodium chloride mutually takes off
Halogen obtains high temperature mother liquor, and solid sodium chloride mutually prepares edible salt, and it is spare that rear liquid is got rid of in edible salt production.
The concrete operations that magnesium sulfate is prepared in the step d) are：High temperature mother liquor obtained by solid sodium chloride phase dehalogenation is passed through
Contra-flow heat exchanger, high temperature mother liquor cool down with cold mother liquor heat exchange in contra-flow heat exchanger, and gained solution containing nucleus after cooling is delivered to
Freezing and crystallizing device circulates to obtain magma, and magma is discharged into concentrator, obtains solid phase epsom salt, and liquid phase cold mother liquor is spare.
The concrete operations that potassium chloride is prepared in the step d) are：Liquid phase cold mother liquor obtained by magnesium sulfate will be prepared to be delivered to
Potassium chloride preparation system, heating evaporation generate slurry, and sedimentation is separated by solid-liquid separation, output solid potassium chloride phase and height brine.
Preferably, the concrete operations of the step e) are：Height brine transportation obtained by step d) is entered into height brine and blows bromine
System, liquid after output bromine and bromine.
Preferably, the concrete operations of the step f) are：Liquid after bromine obtained by step e) is conveyed into single-effect evaporating equipment, bromine
Water evaporation is concentrated to give magma afterwards, and film-making or cooling pelletization, output magnesium chloride are evaporated to magma.
It is a further object of the present invention to provide the systems for above-mentioned sea water desalination and concentrated seawater processing method, including sequentially
Heat power generating system, low temperature distillation system, the low brine of connection blow bromine system, neutralization department, edible salt preparation system, freezing
Crystal system, potassium chloride preparation system, height brine blow bromine system and magnesium chloride preparation system.
The low temperature distillation system includes the multi-effect evaporating device of more Falling Film Evaporator of Horizontal Tube composition, is installed on multiple-effect
Major diameter both vapor compression pump at the top of vaporising device and corresponding more preheaters for being installed on multi-effect evaporating device both sides side wall, institute
The evaporator for stating multi-effect evaporating device joins end to end, first evaporator head, the tail portion closing of tail effect evaporator.
The minuent brine blow bromine system or height brine to blow bromine system include the blowout absorption tower being sequentially connected to and distillation
Tower, the destilling tower also install bromine water -separating bottle.
The minuent brine blow bromine system or height brine to blow bromine system further include being connected to the preheater on blowout absorption tower
And buffer pool.
The blowout absorption tower includes a stripping tower and an absorption tower, and major diameter is connected between the stripping tower and absorption tower
Wind turbine is installed at pipeline, pipeline middle part, and the absorb the bottom of the tower pipeline is connected to buffer pool, and the completion liquid pump in the buffer pool is sent
Enter destilling tower, cooler be installed at the top of the destilling tower, the destilling tower also installs bromine water -separating bottle, separating bottle bottom collection at
Product bromine.
The freezing and crystallizing system includes the contra-flow heat exchanger being sequentially connected to, cooler, freezing and crystallizing device and concentrator, institute
The external series connection cooler of contra-flow heat exchanger is stated into a cycle heat exchange heat sink, the cooler series connection freezing and crystallizing device is described
Freezing and crystallizing device series connection concentrator.
The potassium chloride preparation system includes the heat exchanger being sequentially connected to, evaporator, crystallizer and concentrator, the heat exchange
The external cascade evaporation device of device is connected dense at a circulating-heating vaporising device, the evaporator series crystallizer, the crystallizer
Machine.
The magnesium chloride preparation system includes the vaporising device of preheating device and two sets or two sets or more, the vaporising device
Heat exchanger, connection cycle leg and evaporator, the vaporising device including being sequentially connected to are additionally provided with circulating pump.
Compared with prior art, sea water desalination provided by the invention and concentrated seawater processing method and system to seawater resources into
Row is fully excavated and is utilized, and carries out flow dynamic allocation and balance, that is, uses low temperature multiple-effect distillation sea water desalting and brine is comprehensive
Close by the way of handle seawater, emphasis plays that low brine blows bromine system and height brine blows bromine system effectiveness, utilizes bromine
Cost is low, advantage that profit is high, share desalination water production cost, and distinguished using reasonable distribution is carried out desalination water
With cities and towns drinking water water supply, factory industry water, thermal power plant boiler water supply is given to, closed loop is formed it into, reduces waste, according to
According to the difference of various desalination water purposes water prices, desalination water profit is excavated, balances desalination water cost.Pass through the high sea of productive profit rate
Aquation chemical product balances sea water desalination production cost, makes sea water desalination efficiency maximum, resource allocation optimizes, by multi-faceted
Integration, make yield maximization, minimization of cost, realize extensive sea water desalination and urban water supply, industrial water, boiler to
Water and salt chemical engineering production integration realize that seawater resources efficiently utilize, most by the economic benefit of seawater resources and social benefit
Bigization.
To sum up, the present invention makes full use of the sea in sea water desalination by opening up the purposes channel in cities and towns, power plant, chemical plant
Water resource, heat resource and kinetic energy resource, fully balance and utilize between three.And it is the high fever generated after sea water desalination is dense
Seawater produces all kinds of salt as raw material, digests the concentrated seawater after sea water desalination, makes full use of the value of concentrated seawater, realizes that seawater is light
Change zero-emission, effective protection environment solves the problems, such as that marine environmental pollution is caused in concentrated seawater discharge sea, takes full advantage of sea
Water resource.
Description of the drawings
Fig. 1 is the sea water desalination and concentrated seawater treatment process route map that the embodiment of the present invention 1 provides；
Fig. 2 is the fresh water purposes and utilization of steam figure that the embodiment of the present invention 1 provides；
Fig. 3 is that the steam that the embodiment of the present invention 1 provides uses route schematic diagram；
Fig. 4 is the sea water desalination and concentrated seawater processing system structural schematic diagram that the embodiment of the present invention 2 provides；
Wherein, 10, heat power generating system；11, boiler；20, low temperature distillation system；21, multi-effect evaporating device；30, low
Brine blows bromine system；31, absorption tower is blown out；32, destilling tower；33, preheater；40, neutralization department；50, edible salt preparation system；
51, crystallizing pond；60, freezing and crystallizing system；61, contra-flow heat exchanger；62, cooler；63, freezing and crystallizing device；64, first is dense
Machine；65, the second concentrator；70, potassium chloride preparation system；71, heat exchanger；72, evaporator；73, crystallizer；74, third is dense
Machine；80, height brine blows bromine system；90, magnesium chloride preparation system；91, preheating device；92, vaporising device.
Specific implementation mode
In order to more clearly describe the technology contents of the present invention, carried out with reference to specific embodiment further
Description.
Embodiment 1
Sea water desalination provided in this embodiment and concentrated seawater processing method, specifically include following steps：
S1, sea water desalination：975m is extracted using sea water pump3Seawater (2.7 ° of Be of salinity) supply low temperature distillation system 20 into
Row sea water desalination, obtains 417m3Fresh water and 558m3High temperature concentrated seawater (i.e. low brine, 5 ° of Be of salinity or so)；Wherein, low temperature
The fresh water that Distallation systm 20 generates can be divided in portion and be delivered to municipal network water supply, factory industry uses water or as boiler feedwater
It is delivered to back boiler, and the low-grade steam circulation of such heat supply back boiler (or chemical plant, steam power plant) output supply low temperature steams
System 20 is evaporated to continue sea water desalination, and fresh water and route for steam are as shown in Figure 2.
S2, low bittern air blow bromine：By 20 gained 558m of low temperature distillation system in S13Low brine (5 ° of Be of salinity
Left and right) it is delivered to low brine and blows bromine system 30 and produce bromine, and by the 512m after tentatively extracting bromine3Water (contains after bromine
7 ° of Be of salinity or so) it is spare.
Water neutralizes after S3, bromine：By 512m obtained by S23Water (7 ° of Be of salinity or so) is sent into neutralization department 40, Xiang Zhong after bromine
It is 7 or so with 89.8T magnesium oxide powders are added in workshop 40 to be neutralized to PH, the magnesium hydroxide of generation is fully heavy in neutralization department 40
It forms sediment, obtains 795.6m3Neutral brine (8 ° of Be of salinity or so) is spare.
S4, edible salt is prepared：By 795.6m obtained by S33Neutral brine (8 ° of Be of salinity or so) is pumped into salt pan and carries out day
It is in saturation state to shine natural evaporation to be concentrated into sodium chloride, and the neutral brine (25-26 ° of Be of salinity) after concentration is discharged into crystallizing pond
51, solid sodium chloride phase dehalogenation obtains 291.7m3High temperature mother liquor (31 ° of Be of salinity), solid sodium chloride mutually prepares edible salt, food
It is spare that rear liquid is got rid of with salt production.
S5, magnesium sulfate is prepared：The high temperature mother liquor (31 ° of Be of salinity) that temperature is 20 DEG C or so obtained by S4 is passed through countercurrent flow
Device 61 and forced circulation cooler 62, high temperature mother liquor (31 ° of Be of salinity) and liquid phase cold mother liquor (saliferous in contra-flow heat exchanger 61
33 ° of Be of degree) after heat exchange is cooled to -20 DEG C or so, epsom salt crystal, which is saturated, to be simultaneously constantly precipitated, but small is only precipitated at this time
Gained solution containing nucleus after cooling is delivered to two-stage DTB freezing and crystallizings device 63, circulated by grain crystal (or being nucleus)
Magma, magma are discharged into the first concentrator 64 and the thickening of the second concentrator 65, knot are added by a certain percentage in the second concentrator 65
Rear liquid is got rid of in high temperature mother liquor (31 ° of Be of salinity) and the edible salt production in brilliant pond 51, detaches solid phase and liquid phase, seven water of solid phase
Magnesium sulfate carries out finished product packing, and liquid phase cold mother liquor (33 ° of Be of salinity) is back to contra-flow heat exchanger 61 and high temperature mother liquor (saliferous
Spend 31 ° of Be) heat exchange.
S6, potassium chloride is prepared：By 71 external cascade evaporation device 72 of heat exchanger at a circulating-heating vaporising device, three sets of cycles
Heating and evaporating unit forms three-effect counter flow evaporation plant, and the liquid phase cold mother liquor (33 ° of Be of salinity) after heat exchange obtained by S5 is defeated
Send to three-effect counter flow evaporation plant, three-effect counter flow evaporation plant series-connected crystallizers 73, after heating evaporation in crystallizer 73 cycle
Slurry is flowed to obtain, magma is discharged into sedimentation in third concentrator 74 and is separated by solid-liquid separation, output solid potassium chloride phase and saturated solution
(i.e. height brine, 35 ° of Be of salinity).
S7, height bittern air blow bromine：Height brine (35 ° of Be of salinity) obtained by S6 is conveyed into height brine and blows bromine system
System, output bromine and 117m3Liquid (36 ° of Be of salinity) after bromine.
S8, magnesium chloride is prepared：By 117m obtained by S73Liquid (36 ° of Be of salinity) preheats after bromine, is conveyed into two groups of single effect evaporations
Device 92, water evaporation is concentrated into obtain magma after bromine, and film-making or cooling pelletization, output magnesium chloride, evaporation are evaporated to magma
Vapor enter after liquid after preheater 91 and bromine carries out heat exchange and collect into low temperature distillation system 20 as low product steam
One of source.
Embodiment 2
The present embodiment provides sea water desalination and concentrated seawater processing systems, including the heat power generating system 10, low being sequentially connected to
Warm Distallation systm 20, low brine blow bromine system 30, neutralization department 40, edible salt preparation system 50, freezing and crystallizing system 60, chlorine
Change potassium preparation system 70, height brine blows bromine system 80 and magnesium chloride preparation system 90.
In the present embodiment, low temperature distillation system 20 includes the multi-effect evaporating device of six Falling Film Evaporator of Horizontal Tube composition
21, specially：1st effective evaporator tail portion connects 2nd effect evaporator head, and 2nd effect evaporator tail portion connects triple effect evaporation
Device head, third effect evaporator tail portion connect fourth evaporator head, and fourth evaporator tail portion connects quintuple effect evaporator
Head, quintuple effect evaporator tail portion connect sextuple effect head, 1st effective evaporator head, sextuple effect tail portion envelope
It closes, first to sextuple effect head and the tail connection composition low-temperature multiple-effect seawater desalination evaporates master device --- multi-effect evaporating device 21；
21 top installation major diameter both vapor compression pump of multi-effect evaporating device, 21 both sides side wall of multi-effect evaporating device install six preheaters,
Above-mentioned multi-effect evaporating device 21, both vapor compression pump and six preheaters form low-temperature multiple-effect seawater desalination main system --- and low temperature steams
Evaporate system 20.
Referring to FIG. 2, low temperature distillation system 20 provided by the invention produces fresh water, production process using hot method sea water desalination
In obtained byproduct --- the concentrated seawater for carrying heat, low brine can be directly fed and blow bromine system 30 as low brine
Air blows bromine raw material, reduces the heat for blowing required offer in bromine device；Steam used in low temperature distillation system 20 is low-grade steam,
Vapour source is the low-grade steam that generates after thermal power plant boiler use, driving both vapor compression pump production fresh water and concentrated seawater, fresh water after
Continuous supply municipal network water supply, factory industry water or various boilers.
In the present embodiment, low brine blow bromine system 30 include sequentially be connected to the first buffer pool (not shown),
Blowout absorption tower 31, the second buffer pool (not shown), destilling tower 32, preheater 33 and third buffer pool (do not show in figure
Go out), blowout absorption tower 31 includes a stripping tower and an absorption tower, and large-diameter pipeline is connected between two towers, wind is installed in the middle part of pipeline
Machine；The concentrated seawater that low temperature distillation system 20 is discharged, is delivered to stripping tower, concentrated seawater passes through by the first buffer pool of irrigation canals and ditches channel
Absorb the bottom of the tower pipeline flow is to the second buffer pool；Pipeline is stretched into buffer pool, and concentrated seawater is pumped into destilling tower 34；Destilling tower
34 top install coolers, behind bromine water -separating bottle is installed, water is in preheater 33 after separating bottle bottom collection finished product bromine, bromine
In exchange heat with the concentrated seawater that is conveyed in low temperature distillation system 20, water is delivered to spare in third buffer pool after bromine.
Minuent brine provided by the invention blows the bromine that bromine system 30 produces a large amount of high profit margins, can balance low temperature distillation system
The fresh water of the low profit margin of 20 production of system effectively solves the excessively high operation quagmire of sea water desalination water factory cost, makes bromine and fresh water
Average profit be able to maintain that the operation cost of sea water desalination, make seawater resources value maximization.
In the present embodiment, neutralization department 40 is the operation room of any progress magnesia neutralization in the prior art, herein not
It repeats.
The present invention is using in magnesium oxide powder and after bromine by the way of water, at low cost, simple for process, convenient operation and control, dress
It is small to set investment, while the magnesium hydroxide subsequently generated can be used as resources reserve exploitation.
In the present embodiment, edible salt preparation system 50 includes several salt pans for being sequentially connected to and crystallizing pond 51, water after bromine
Flow into salt pan, salt pan is open pool construction, every piece of salt field trench canal connection, after bromine water in salt Tanaka's natural evaporation,
It is increased with its concentration, flows into subordinate salt pan step by step, crystallizing pond 51 is conveyed into eventually by irrigation canals and ditches channel when bittern concentration is enough,
It is crystallized in crystallizing pond 51, gained solid sodium chloride mutually produces edible salt, and 51 high temperature mother liquor of crystallizing pond turns to expect into freezing and crystallizing
System 60, it is spare that rear liquid is got rid of in edible salt production.
For the present invention during preparing edible salt, neutral brine enters 51 knot of crystallizing pond after entering salt pan natural evaporation
Crystalline substance can reduce evaporation periods when edible salt production, reduce land area needed for salt pan.
In the present embodiment, freezing and crystallizing system 60 include sequentially be connected to three sets of external cycle heat exchange heat sinks,
Two level freezing and crystallizing device 63, the first concentrator 64 and the second concentrator 65, the high temperature mother liquor in crystallizing pond 51 flow into external and follow
Ring heat exchange heat sink, cycle heat exchange heat sink are forced to follow by 61 external series connection forced circulation cooler 62 of contra-flow heat exchanger
Ring cooler 62 is that vertical cylinder describes device, bottom and side-wall hole, is connect with contra-flow heat exchanger 61 using circulation pipe, adverse current
Heat exchanger 61 is placed in outside forced circulation cooler 62, therefore referred to as external cycle heat exchange heat sink, one in the device
Contra-flow heat exchanger 61 and a forced circulation cooler 62 form a whole device, totally three single unit systems series connection, every strong
62 circulation pipe bottom opening of circulation temperature lowering device processed turns to expect that, into next forced circulation cooler 62, last platform pressure follows using taking over
62 circulation pipe bottom nozzles of ring cooler turn to expect that freezing and crystallizing device 63 is DTB crystallizer forms into first order freezing and crystallizing device 63,
63 bottom opening of first order freezing and crystallizing device, which is taken over, to be turned to expect into second level freezing and crystallizing device 63,63 bottom of second level freezing and crystallizing device
Opening-nozzle turns to expect successively, into the first concentrator 64 and the second concentrator 65, to obtain epsom salt solid and liquid phase cold mother liquor.
The present invention utilizes freezing and crystallizing system 60, produces epsom salt using freeze crystallization, final crystallization temperature is
Subzero 24 DEG C, steam is not consumed, only consumes electric energy, on the one hand lower than prior art operating cost (steam cost is high), another party
Steam resource is saved in face, makes the more, bigger using space of steam resource；It is molten that freezing and crystallizing device 63 conveys epsom salt suspension
Liquid is separated by solid-liquid separation in the first concentrator 64, the upper layer clarified mother liquor isolated and the crystallizing pond from edible salt preparation system 50
51 high temperature mother liquor and edible salt production is got rid of rear liquid and is mixed in the second concentrator 65 according to a certain percentage.In second concentrator 65
Solid-liquid two-phase laminated flow is carried out, deionization is on the one hand further removed, detaches solid phase materials, extracts seawater resources, balance seawater is light
Chemical conversion is originally；On the other hand, the high temperature heat that the high temperature mother liquor that Mother liquor and crystallizing pond 51 convey is got rid of using edible salt production, and it is cold
Liquid phase cold mother liquor exchanges heat after jelly, solves the processing of low-temperature material, the heat recovery of high-temperature material；Take full advantage of heat.
In the present embodiment, potassium chloride preparation system 70 includes heat exchanger 71, evaporator 72, the crystallizer 73 being sequentially connected to
With third concentrator 74,72 external heat exchangers in series 71 of evaporator is at a forced circulation heating and evaporating unit, 72 bottom of evaporator
And side-wall hole, connection cycle leg are taken over, which installs heat exchanger 71, and forced circulation pump is installed in cycle leg bottom,
The liquid phase cold mother liquor sequence of pumping flows through cycle leg, heat exchanger 71, evaporator 72 and cycle leg；Liquid phase cold mother liquor constantly follows
Ring is heated when flowing through heat exchanger 71, the explosive vaporization in evaporator 72, completes evaporating, concentrating and crystallizing process, evaporator 72
Series-connected crystallizers 73, the series connection third of the crystallizer 73 concentrator 74；In addition, forced circulation heating and evaporating unit is triple effect,
In, 72 heat source of 1st effective evaporator is the life steam from boiler, and the secondary gas that 1st effective evaporator 72 generates is as the second effect
The heat source of evaporator 72,72 top of 1st effective evaporator, which is taken over, is connected and installed in the first effect heat exchanger 71；2nd effect evaporator 72
Heat source of the secondary gas as third effect evaporator 72 generated is taken at the top of 2nd effect evaporator 72 and is connected and installed in the second effect and changes
Hot device 71,72 top of third effect evaporator, which is taken over, is connected and installed in three-effect heat exchanger 71；Third effect evaporator 72 recycles leg bottom
Portion's opening-nozzle connection first order crystallizer 73,73 bottom opening of first order crystallizer takes over connection second level crystallizer 73, the
73 bottom opening of secondary crystallizer takes over connection third concentrator 74, and the material containing potassium chloride is in third concentrator 74
It is separated by solid-liquid separation.
The present invention produces potassium chloride, triple effect using triple effect forced circulation heating and evaporating unit using bittern comprehensive utilization technique
Forced circulation heating and evaporating unit is the external forced-circulation evaporator on contra-flow heat exchanger, which uses triple effect
Series connection, first heating evaporation material, obtain concentration pyrosol, then be equipped with two-stage cooling DTB decrease temperature crystallines device to high temperature concentrate it is molten
Liquid cools down, and magma material is discharged into concentrator, and potassium chloride crystallization is precipitated, solid-liquid two-phase laminated flow；Height brine is eliminated at this time
Potassium ion in (35 ° of Be of salinity) provides conveniently for subsequent technique production, while producing valuable production using seawater resources
Product balance sea water desalination cost.
In the present embodiment, height brine blows bromine system 80 and low brine to blow 30 structure of bromine system identical, does not do herein
It repeats；The clear liquid being separated in the concentrator 74 of KCl production preparation system 70 is conveyed into height brine and blows bromine system 80,
Liquid is spare after gained bromine.
Height brine of the present invention enters buffer pool, and the raw material that bromine system 80 is blown as height brine produces bromine, further
Fully extraction is worth higher bromine, takes full advantage of seawater resources, balances sea water desalination cost, avoids brominated discharge of wastewater
Environment is damaged.
In the present embodiment, magnesium chloride preparation system 90 includes the preheating device 91 being sequentially connected to and two sets of single effect evaporation dresses
92 are set, it includes that a heat exchanger, connection cycle leg, an evaporator and a forced circulation pump (do not show in figure often to cover vaporising device 92
Go out)；Evaporator is external heat exchanger forced circulation structure, base of evaporator and side-wall hole, and connection cycle leg is taken over, the cycle
Midleg installs heat exchanger, and forced circulation pump is installed in cycle leg bottom, and wherein evaporimeter thermal source gives birth to steam, evaporator from boiler
The indirect steam of generation is connected to preheating device 91 using pipeline, and indirect steam is transmitted back to low temperature distillation after flowing through preheating device 91
System 20 discharges thermal energy therein, is condensed into condensed water.
Liquid is conveyed into magnesium chloride preparation system 90 after bromine of the present invention, and magnesium chloride preparation system 90 is filled using two sets of single effect evaporations
92 to be set, liquid after bromine is concentrated completely, produces industrial hex-ammoniate, gained vapor is used for low temperature distillation system 20 when preparation,
So far sea water desalination and concentrated seawater full utilization are completed, realizes zero-emission.
Each component in seawater is classified and is completed by sea water desalination provided by the invention and concentrated seawater processing method and system
Production of multiple product, including desalination water, bromine, Nacl, epsom salt, potassium chloride, magnesium chloride etc., make full use of seawater
Resource realizes the maximization of the economic benefit and social benefit of seawater resources.
In this description, the present invention is described with reference to its specific embodiment.But it is clear that can still make
Various modifications and alterations are without departing from the spirit and scope of the invention.Therefore, the description and the appended drawings should be considered as illustrative
And not restrictive.
Claims (10)
1. a kind of sea water desalination and concentrated seawater processing method, which is characterized in that include the following steps：
Seawater is delivered to low temperature distillation system (20) and carries out sea water desalination by step a), and byproduct concentrated seawater is spare；
Concentrated seawater obtained by step b) steps a) carries out low bittern air and blows bromine, and water is spare after bromine；
Water is neutralized with magnesia after step c) steps b) gained bromines, and neutral brine is obtained after filtering off precipitation, spare；
Neutral brine obtained by step c) is carried out beach field and shone again by step d), and solid phase is precipitated and prepares edible salt, the high temperature after shining again
Magnesium sulfate solid phase is precipitated in mother liquor freezing, and slurry settles after remaining liquid phase cold mother liquor heating evaporation, obtain height brine with
Potassium chloride；
Height brine obtained by step e) steps d) carries out height bittern air and blows bromine, and liquid is spare after bromine；
Liquid heating evaporation prepares magnesium chloride after bromine obtained by step f) steps e).
2. sea water desalination described in claim 1 and concentrated seawater processing method, which is characterized in that prepared in the step d) edible
The concrete operations of salt are：Neutral brine obtained by step c) is pumped into beach field to carry out solarization natural evaporation to be concentrated into sodium chloride being in full
And state, the neutral brine after concentration are discharged into crystallizing pond, solid sodium chloride phase dehalogenation obtains high temperature mother liquor, and solid sodium chloride is mutually prepared
Edible salt.
3. sea water desalination described in claim 1 and concentrated seawater processing method, which is characterized in that prepare sulfuric acid in the step d)
The concrete operations of magnesium are：High temperature mother liquor obtained by step c) is passed through contra-flow heat exchanger (61), high temperature mother liquor and contra-flow heat exchanger
(61) gained solution containing nucleus after cooling is delivered to freezing and crystallizing device (63) and circulates brilliant by interior cold mother liquor heat exchange cooling
Slurry, magma are discharged into concentrator, obtain solid phase epsom salt, and liquid phase cold mother liquor is spare.
4. sea water desalination described in claim 1 and concentrated seawater processing method, which is characterized in that prepare chlorination in the step d)
The concrete operations of potassium are：Liquid phase cold mother liquor obtained by magnesium sulfate will be prepared and be delivered to potassium chloride preparation system (70), heating evaporation
Slurry is generated, sedimentation is separated by solid-liquid separation, output solid potassium chloride phase and height brine.
5. the system for sea water desalination and concentrated seawater processing method described in Claims 1 to 4, it is characterised in that：Including suitable
The heat power generating system (10) of secondary connection, low temperature distillation system (20), low brine blow bromine system (30), neutralization department (40),
Edible salt preparation system (50), freezing and crystallizing system (60), potassium chloride preparation system (70), height brine blow bromine system (80) and
Magnesium chloride preparation system (90).
6. the sea water desalination described in claim 5 and concentrated seawater processing system, it is characterised in that：The low temperature distillation system (20)
Including more Falling Film Evaporator of Horizontal Tube composition multi-effect evaporating device (21), be installed on it is big at the top of multi-effect evaporating device (21)
Diameter both vapor compression pumps and corresponding more preheaters for being installed on multi-effect evaporating device (21) both sides side wall, the multiple-effect evaporation dress
The evaporator for setting (21) joins end to end, first evaporator head, the tail portion closing of tail effect evaporator.
7. the sea water desalination described in claim 5 and concentrated seawater processing system, it is characterised in that：The minuent brine blows bromine system
(30) or height brine to blow bromine system (80) include the blowout absorption tower (31) being sequentially connected to and destilling tower (32), the destilling tower
(32) bromine water -separating bottle is also installed.
8. the sea water desalination described in claim 5 and concentrated seawater processing system, it is characterised in that：The freezing and crystallizing system (60)
Including contra-flow heat exchanger (61), cooler, freezing and crystallizing device (63) and the concentrator being sequentially connected to, the contra-flow heat exchanger (61)
For external series connection cooler (62) at a cycle heat exchange heat sink, cooler (62) the series connection freezing and crystallizing device (63) is described
Freezing and crystallizing device (63) series connection concentrator.
9. the sea water desalination described in claim 5 and concentrated seawater processing system, it is characterised in that：The potassium chloride preparation system
(70) include the heat exchanger (71) being sequentially connected to, evaporator (72), crystallizer (73) and concentrator, the heat exchanger (71) is external
Cascade evaporation device (72) is at a circulating-heating vaporising device, evaporator (72) series-connected crystallizers (73), the crystallizer
(73) series connection concentrator.
10. the sea water desalination described in claim 5 and concentrated seawater processing system, it is characterised in that：The magnesium chloride preparation system
(90) include preheating device (91) and two sets or two sets or more vaporising device (92), the vaporising device (92) include sequentially connect
Logical heat exchanger, connection cycle leg and evaporator, the vaporising device (92) are additionally provided with circulating pump.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101704560A (en) * | 2009-07-29 | 2010-05-12 | 林晓山 | Technique for desalting sea water, making salt and comprehensively using by-products thereof by utilizing wind energy, solar energy and heat pump technologies |
| CN103253818A (en) * | 2013-04-19 | 2013-08-21 | 金逹行有限公司 | Seawater desalination, resource comprehensive utilization and zero discharge processing system |
| CN104528766A (en) * | 2014-11-26 | 2015-04-22 | 李树生 | Apparatus and method for producing potassium chloride and co-producing magnesium sulfate by mixing brine |
| CN105819401A (en) * | 2016-03-18 | 2016-08-03 | 中国中轻国际工程有限公司 | LNG cold energy seawater desalination and concentrated saltwater comprehensive utilization technology |
-
2017
- 2017-09-28 CN CN201710901827.3A patent/CN108569810A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101704560A (en) * | 2009-07-29 | 2010-05-12 | 林晓山 | Technique for desalting sea water, making salt and comprehensively using by-products thereof by utilizing wind energy, solar energy and heat pump technologies |
| CN103253818A (en) * | 2013-04-19 | 2013-08-21 | 金逹行有限公司 | Seawater desalination, resource comprehensive utilization and zero discharge processing system |
| CN104528766A (en) * | 2014-11-26 | 2015-04-22 | 李树生 | Apparatus and method for producing potassium chloride and co-producing magnesium sulfate by mixing brine |
| CN105819401A (en) * | 2016-03-18 | 2016-08-03 | 中国中轻国际工程有限公司 | LNG cold energy seawater desalination and concentrated saltwater comprehensive utilization technology |
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