CN209652063U - A kind of processing system of high temperature film method for removing sulfate ion - Google Patents
A kind of processing system of high temperature film method for removing sulfate ion Download PDFInfo
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- CN209652063U CN209652063U CN201920139909.3U CN201920139909U CN209652063U CN 209652063 U CN209652063 U CN 209652063U CN 201920139909 U CN201920139909 U CN 201920139909U CN 209652063 U CN209652063 U CN 209652063U
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Abstract
The utility model relates to a kind of processing systems of high temperature film method for removing sulfate ion, including film separation unit and the crystallization-separative unit being connected with the concentrated solution outlet of film separation unit, the upgrading unit being connected is exported with the penetrating fluid of film separation unit, further includes the fine tune temperature unit sequentially connected by pipeline, for the dechlorination clean unit of the high-temperature electrolysis light salt brine removing free chlorine to electrolysis with ion-exchange film and for carrying out fine tune temperature processing to the high-temperature electrolysis light salt brine after dechlorination before film separation unit is set.The temperature of the light salt brine of the engaging sulphate processing system processing of the utility model is high, just can be carried out engaging sulphate processing it is not necessary that the temperature of light salt brine to be reduced to after 45 DEG C or less, significantly saving cooling water amount；And the temperature of the filtered penetrating fluid of film is higher, reduces heat consumption when subsequent MVR evaporation or salt dissolving, reduces energy consumption in MVR concentration process, through above-mentioned integrated treatment, reach efficient, stable, energy-efficient purpose.
Description
Technical field
The utility model relates to a kind of high temperature membrane separating sulfate ion processing system and method, in particular to a kind of salt
The separation sulfate ion processing system and method for water belong to chlor-alkali equipment technology field.
Background technique
Chlorine industry refers to that the method for electricity consumption solution saturation NaCl solution produces caustic soda, chlorine and the industrial production of hydrogen,
It is important one of Essential Chemistry industry.Electrolysis carries out in vertical diaphragm electrolytic cell, and electrolytic cell is separated into anode chamber by diaphragm
And cathode chamber.After the power is turned on, under the action of electric field, electronegative Cl-Shift to anode, positively charged H+Shift to cathode, In
Following reaction occurs under the conditions of this, on electrode:
Anode: 2Cl-- 2e=Cl2↑
Cathode: 2H++ 2e=H2↑
Cl is released in anode chamber2, cathode chamber releasing H2.Due to H+Constantly electric discharge, destroys the ionization equilibrium of water, promotes
Water constantly ionizes, and causes OH in solution-Enrichment.It is formed NaOH solution in cathode chamber in this way, it is flowed from cathode chamber bottom
Out.Anode chamber will cause the reduction of sodium chloride concentration due to the decomposition of NaCl, generate light salt brine.
When being produced by the above method, the light salt brine that electrolysis with ion-exchange film generates is usually to flow back into brine system to carry out salt dissolving
Processing passes through MVR (i.e. mechanical steam recompression technology, mechanical vapor recompression) technology, dense
Contracting light salt brine is directly used as electric slot refined brine use after improving the concentration of salt water.Salt water can recycle in systems, system
Middle sulfate concentration can be higher and higher, when sulfate concentration is more than 7g/L in system, will impact to the electrolysis of salt water,
So needing to remove the sulfate radical in salt water in time.
This technology is exactly, by pressurization, to be mentioned using high-temperature nano membrane filtration technique by carrying out proper treatment to light salt brine
Sulfate radical content in high light salt brine is to 30g/L or more.Light salt brine (concentrate) temperature of high-concentration sulfuric acid radical content is reduced to 0
DEG C hereinafter, sulfate radical solubility is made to be reduced to 8g/L, a large amount of sulfate radical is precipitated in the form of sal glauberi in saltpetre sinking device,
It is centrifuged, is precipitated as granular sal glauberi.The light salt brine (penetrating fluid) of low-concentration sulfuric acid radical content accounts for about entire light salt
The 90% of water, sulfate radical (SO in fresh water4 2-) content about 1g/L, film, which filters fresh water, can be directly used as the molten of salt (i.e. sodium chloride)
Agent carries out salt dissolving processing, or carries out concentration, to improve sodium chloride content, continues electrolysis and uses.
In existing chlorine industry, in a large amount of light salt brine treatment process that electrolysis saturated sodium-chloride generates, it is required to light
Salt water carries out cooling processing to after lower than 45 DEG C, then carries out corresponding engaging sulphate processing, light salt brine cooling is needed a large amount of
Cooling water, energy consumption are high.High temperature UF membrane sulfate radical system just can be carried out separation at relatively high temperatures (60-80 DEG C).
Utility model content
The purpose of this utility model is in order to solve the above technical problems, providing a kind of high temperature film method for removing sulfate ion
Processing system (i.e. removing object in ionic membrane electrolysis depleted brine in sulfate ion processing system), the engaging sulphate of the utility model
System removes the sulfate radical in electrolysis light salt brine with high temperature nanofiltration technique, and the treatment temperature of the light salt brine of system processing is high, is not necessarily to
The temperature of light salt brine, which is reduced to after 45 DEG C or less, just can be carried out engaging sulphate processing, significantly saving cooling water amount；And film
The temperature of filtered penetrating fluid is higher, reduces heat consumption when MVR evaporation or salt dissolving, reduces in MVR concentration process
Energy consumption has saved the energy.
To realize the purpose of this utility model, on the one hand the utility model provides a kind of high temperature film method for removing sulfate ion
The processing system processing system of object in ionic membrane electrolysis depleted brine engaging sulphate ion (remove), including film separation unit and with
Crystallization-separative unit that the concentrated solution outlet of film separation unit is connected is connected with the outlet of the penetrating fluid of film separation unit
Upgrading unit further includes being sequentially connected dechlorination clean unit and fine tune temperature list by pipeline before film separation unit is arranged in
Member, in which:
Dechlorination clean unit, for removing free chlorine to the high-temperature electrolysis light salt brine of electrolysis with ion-exchange film；
Fine tune temperature unit, for carrying out fine tune temperature processing to the high-temperature electrolysis light salt brine after dechlorination.
The processing system of the utility model high temperature film method for removing sulfate ion is to remove object in ionic membrane electrolysis depleted brine
The processing system of middle sulfate ion, that is, in the case where temperature is 60-80 DEG C of hot conditions, removing electrolysis with ion-exchange film is obtained
The processing system of sulfate ion in light salt brine.
Wherein, the dechlorination clean unit selects activated carbon adsorption device.
In particular, the activated carbon adsorption device selection activated carbon adsorber, absorbent charcoal adsorption tank or active carbon adsorber.
To reach treatment effect under higher temperature conditions, adsorbent equipment is set as two-stage series connection.
Especially, the high-temperature electrolysis light salt brine of the electrolysis with ion-exchange film is high after the dechlorination of dechlorination clean unit processing
Warm Free Chlorine in Brine content is 0.
In particular, further including that treated that light salt brine is passed through pH adjustment unit to dechlorination clean unit, light salt brine is adjusted
After pH to 4-7, then it is passed through the fine tune temperature unit.
Especially, the pH adjustment unit is the component of injection acid additives in Xiang Guandao or container.
In particular, it is described into pipeline or container inject acid additives component be connected with pipeline or container add
Teat pipette and medical fluid storage tank (such as hydrochloric acid tank).
Wherein, the fine tune temperature Unit selection heat-exchanger rig.
In particular, the heat-exchanger rig selects plate heat exchanger.Light salt brine cleanliness is high, is suitble to high using heat exchange efficiency
Plate heat exchanger.Heat-exchanger rig selection plate heat exchanger or the accurate deployment unit of high/low temperature (using low-temperature centrifugation mother liquor with
High temperature light salt brine is accurately deployed).
Especially, the high-temperature electrolysis light salt brine after dechlorination clean unit dechlorination carries out temperature by fine tune temperature unit
The temperature of high temperature light salt brine after trim process is 60-80 DEG C.It does not need to reduce 40-45 DEG C (traditional treatment method).
In particular, further including the pressurization list being connected by pipeline between the fine tune temperature unit and film separation unit
Member.
Especially, the presser unit selects high-pressure pump, flows through high-pressure pump by the high temperature light salt brine that fine tune temperature is handled,
The pressure value for promoting high temperature light salt brine, so that pressure >=1.0MPa of high temperature light salt brine.
In particular, filter is arranged before presser unit, light salt brine flows through filter, and filtering and impurity removing reduces light salt brine
In SS (suspended solid), removal of impurities.
Especially, the filter selects cartridge filter.
Wherein, the film separation unit selects nanofiltration membrane component.
In particular, the film separation unit is preferably high temperature nanofiltration membrane component, preferably adapts to higher temperatures condition and reach
The high temperature nanofiltration membrane component for the treatment of effect.
Wherein, the film separation unit selects 3-5 grades of concatenated nanofiltration membrane components.
In particular, the high temperature film separation unit selects 3-5 grades of concatenated high temperature nanofiltration membrane components.
Wherein, the nanofiltration membrane component adapts to 60-80 DEG C of high temperature light salt brine.
In particular, the high temperature nanofiltration membrane component adapts to the high temperature light salt brine of 60-80 DEG C (adjustable).
Wherein, the crystallization-separative unit includes passing through the sequentially connected saltpetre sinking device of pipeline, centrifuge.
In particular, the upgrading unit selects MVR inspissator.
On the other hand the utility model provides a kind of object in ionic membrane electrolysis depleted brine engaging sulphate processing system, including UF membrane
Unit and the crystallization-separative unit being connected with the concentrated solution outlet of film separation unit, go out with the penetrating fluid of film separation unit
The upgrading unit that is connected of mouth, further includes the dechlorination clean unit before being connected to film separation unit by pipeline, for from
The high-temperature electrolysis light salt brine of sub- film electrolysis removes free chlorine.
The engaging sulphate processing system of the utility model can be without significantly Temperature Treatment, directly under the high temperature conditions
Carry out membrane separation.
The utility model has the following beneficial effects:
1, chlorine industry, light salt brine temperature >=80 DEG C generated using electrolysis with ion-exchange film sodium chloride solution, and it is existing light
The recycling system of salt water is both needed to be reduced to the temperature of light salt brine after 45 DEG C or less and can just be further processed, and this is practical new
The light salt brine that the engaging sulphate processing unit of type directly generates electrolysis with ion-exchange film carries out engaging sulphate processing at high temperature, is not required to
Cooling processing is carried out to light salt brine, reduce energy consumption, saved the energy.
2, the sulphate-containing ion after the high temperature nanofiltration membrane separation of the engaging sulphate processing system of the utility model is dense
The temperature for spending low penetrating fluid is high (being higher than 60 DEG C), can directly be back to brine section and carry out salt dissolving processing, save at salt dissolving
Manage the energy of step.
3, the sulphate-containing ion after the high temperature nanofiltration membrane separation of the engaging sulphate processing system of the utility model is dense
The temperature for spending low penetrating fluid is high (being higher than 60 DEG C), when carrying out MVR concentration to penetrating fluid, saves the heat that heating needs
Amount, saves a large amount of energy, reduces processing energy consumption.
4, the desulfurization acid for the light salt brine that the engaging sulphate processing system of the utility model generates electrolysis with ion-exchange film sodium chloride
Root processing does not need to carry out light salt brine cooling processing to 45 DEG C hereinafter, keeping the temperature of light salt brine at least at 60 DEG C or more, can
To save the dosage of cooling water, energy consumption is reduced.
5, the engaging sulphate processing system structure of the utility model is simple, complicated cooling system is not needed, to former high temperature
The light salt brine that generates of electrolysis with ion-exchange film sodium chloride solution directly carry out separating treatment, and it is higher using still having after separation
The light salt brine of temperature is concentrated or the direct salt dissolving of salt dissolving process, and multi-step is energy saving, reduces energy consumption, has been reduced significantly to light salt brine
Processing cost.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the processing system of the utility model high temperature film method for removing sulfate ion；
Figure 1A is the structural representation of the processing system of the utility model high temperature film method for removing sulfate ion in embodiment 1
Figure；
Fig. 2 is to carry out engaging sulphate processing using the processing system of the utility model high temperature film method for removing sulfate ion
Process flow chart；
Fig. 3 is the structural schematic diagram of the processing system of the utility model high temperature film method for removing sulfate ion in embodiment 2.
Description of symbols
10, dechlorination clean unit；1, fine tune temperature unit；2, presser unit；3, film separation unit；4, crystallization-separation list
Member；41, centrifuge；5, upgrading unit.
Specific embodiment
Further describe the utility model combined with specific embodiments below, the advantages of the utility model and feature will be with
Description and it is apparent.But examples are merely exemplary for these, does not constitute any restrictions to the scope of the utility model.
It will be understood by those skilled in the art that can be to the utility model skill under the spirit and scope without departing from the utility model
The details and form of art scheme are modified or are replaced, but these modifications and replacement each fall within the protection scope of the utility model
It is interior.
The utility model is further illustrated with specific embodiment with reference to the accompanying drawings, but these examples are only to illustrate this reality
With the novel any restrictions that but should not be understood as to the scope of the utility model.
As shown in Figure 1, 2, processing system (the i.e. removing ionic membrane of the high temperature film method for removing sulfate ion of the utility model
It is electrolysed the processing system of engaging sulphate ion in light salt brine) it include: sequentially through the sequentially connected dechlorination clean unit of pipeline
10, fine tune temperature unit 1, presser unit 2, film separation unit 3；And the knot being connected with the concentrated solution outlet of membrane filter unit
Crystalline substance-separative unit 4 exports the upgrading unit 5 being connected with the penetrating fluid of membrane filter unit, wherein
Dechlorination clean unit, for removing free chlorine to the high-temperature electrolysis light salt brine of electrolysis with ion-exchange film；Fine tune temperature unit,
For carrying out fine tune temperature processing to the high-temperature electrolysis light salt brine after dechlorination.
Each processing unit is accomplished continuously or intermittently carried out when handling light salt brine, and light salt brine temperature is positively retained at 60-80 DEG C (can
Adjust), the light salt brine sent from electrolysis cells directly uses or simple cooling.Go the low sulfate radical content light salt brine of MVR directly into
Row MVR concentration, saves the consumption of heating energy source.
The processing system of the utility model carries out the light salt brine for using electrolysis with ion-exchange film sodium chloride to generate in chlorine industry
Engaging sulphate processing, the light salt brine temperature that wherein electrolysis with ion-exchange film sodium chloride generates are 80-85 DEG C, pH value about 7-10；Sulfate radical
Ion concentration >=7g/L.
The dechlorination clean unit 10 selects activated carbon adsorption device, carries out to the free chlorine being passed through in light salt brine therein
Absorption reduces the free chlorine contents in light salt brine, obtains dechlorination light salt brine；Dechlorination clean unit adjusts light salt in the utility model
Free chlorine contents are zero in water, and existing known dechlorination method is suitable for the present invention in this field；Activated carbon adsorption device choosing
Activated carbon adsorber, absorbent charcoal adsorption tank or active carbon adsorber etc. are selected, the existing known active carbon that contains is inhaled in this field
Attached dose of device or equipment is suitable for the utility model.
High temperature light salt brine after dechlorination clean unit removing free chlorine passes through pH adjustment unit (attached to be not shown in the figure) to pipe
Acid additives (such as hydrochloric acid) is added in light salt brine in road, after the pH to 4-7 for adjusting high temperature light salt brine, then carries out fine tune temperature
It is whole.PH adjustment unit includes the acid additives storage tank (such as hydrochloric acid tank) that dosing pump is connected with by pipeline, passes through dosing
Acid additives in storage tank are added in the high temperature light salt brine after dechlorination by pump.
The fine tune temperature unit 1 selects heat-exchanger rig, and by the dechlorination of dechlorination clean unit, treated that high-temperature electrolysis is light
Salt water is passed through fine tune temperature unit and carries out fine tune temperature processing, by the fine tune temperature of high temperature light salt brine to 60-80 DEG C.It does not need to drop
It is low 40-45 DEG C (traditional treatment method).Heat-exchanger rig is selected plate heat exchanger or (is used using the accurate deployment unit of high/low temperature
Low-temperature centrifugation mother liquor and high temperature light salt brine are accurately deployed), existing known heat-exchanger rig or equipment are fitted in this field
For the utility model.
The presser unit 2 selects high-pressure pump, and it is single that fine tune temperature treated high temperature light salt brine through piping is passed through pressurization
Member 2 promotes the pressure value of high temperature light salt brine, so that pressure >=1.0MPa of high temperature light salt brine.
Treated that high temperature light salt brine can also be first filtered through piping for fine tune temperature, and it is (attached to be passed through cartridge filter
It is not shown in the figure), it is filtered, reduces the SS (suspended solid) in light salt brine, after removal of impurities, then through pipeline be passed through presser unit 2,
The pressure value for promoting high temperature light salt brine, so that pressure >=1.0MPa of high temperature light salt brine.Usual presser unit selects high-pressure pump.
The film separation unit 3 selects nanofiltration membrane component (high temperature nanofiltration membrane component), using concatenated 3-5 grades of nanofiltration membrane group
Part.High temperature light salt brine after pressurization is passed through film separation unit after Multistage Membranes filtering through pipeline and obtains the light salt of high sulfate radical content
The light salt brine (i.e. penetrating fluid) of water (i.e. concentrate) and low sulfate radical content, film separation unit treated concentrate, that is, high sulfuric acid
The light salt brine of radical content enters crystallization-separative unit, film separation unit treated the light salt of penetrating fluid, that is, low sulfate radical content
Water is passed through upgrading unit, goes that MVR is concentrated or the light salt brine of film separation unit treated the i.e. low sulfate radical content of penetrating fluid is straight
Connect salt dissolving.
The filter membrane of the nanofiltration membrane component of film separation unit 3 selects high temperature nanofiltration membrane, the light salt that adaptive temperature is 60-80 DEG C
Water.High temperature light salt brine is after multistage nanofiltration membrane component, until sulfate ion concentration >=30g/l of concentrate is (usually
For 30-80g/l)；Sulfate ion concentration≤1g/l of penetrating fluid；Pressure >=1.0MPa is controlled (usually in membrane filtration processes
1.0-3.0MPa), light salt brine temperature is 60-80 DEG C.
Crystallization-the separative unit 4 to film separation unit treated concentrate, that is, high sulfate radical content light salt brine in
Crystallisation by cooling is carried out in saltpetre sinking device, is then passed through in centrifuge and is centrifuged again.Concentrate is delivered in saltpetre sinking device, is passed through
Circulating pump, cryopanel are changed to exchange heat with cold water, so that concentrate temperature is reduced to 5 DEG C or less, (usual concentrate temperature is reduced
It is suitable for the present invention to 0 DEG C or less), sal glauberi crystallization is precipitated, and sal glauberi crystallization is deposited to saltpetre sinking device bottom,
Then sal glauberi crystal is produced through centrifuge separation, the mother liquor reflux after centrifugation to brine section carries out salt dissolving processing,
After melting sodium chloride or concentration, continue engaging sulphate processing.
The temperature of centrifugate is high, is directly back to brine section and carries out salt dissolving processing, the salt dissolving processing of usual brine section
In the process, the temperature of salt dissolving water needs to reach 60 DEG C or more, and the mother liquor temperature after centrifugal treating of the present invention is high, does not need to add again
Heat can both carry out salt dissolving processing, save the energy, reduce energy consumption.
Upgrading unit 5 is to film separation unit treated penetrating fluid, that is, low sulfate radical content light salt brine is passed through MVR concentration
Concentration is carried out in device, the light salt brine temperature of the low sulfate radical content after UF membrane keeps higher temperature, reduces MVR evaporation
Or heat consumption when salt dissolving.
Or the penetrating fluid after film filtration treatment is inputted into salt dissolving unit, penetrating fluid directly returns to brine section salt dissolving, dissolves
Sodium chloride.
Light salt brine temperature does not need 40-45 DEG C that is reduced to conventional method 60-80 DEG C (adjustable) in the present invention, can be with
Cooling water amount is saved, energy consumption is reduced.
The working principle of the processing system of sulfate ion in the removing object in ionic membrane electrolysis depleted brine of the utility model:
1, the dechlorination processing of light salt brine
Dechlorination clean unit is passed through to chlorine industry object in ionic membrane electrolysis depleted brine, carries out dechlorination processing, removing free chlorine is (i.e.
Dechlorination processing), adjust pH (i.e. pH adjusting handle), fine tuning temperature (i.e. adjusting Temperature Treatment) and filtering and impurity removing, high temperature is made
Pre-process light salt brine, in which:
During pretreatment removing free chlorine, high temperature light salt brine is passed through dechlorination processing unit 10, is adjusted in light salt brine
Free chlorine contents are zero, and existing known dechlorination method is suitable for the present invention in this field；
Light salt brine is passed through in activated carbon adsorption component (usually activated carbon tower, charcoal canister etc.), activated carbon adsorption is light
Free chlorine in salt water, the free chlorine contents for adjusting light salt brine are 0, obtain dechlorination light salt brine；
2, light salt brine pH is adjusted
Be passed through pH adjustment unit to dechlorination light salt brine, by dosing pump by the acid additives in hydrochloric acid tank (usually
Hydrochloric acid) it is added in dechlorination light salt brine, adjust the pH to 4-7 of light salt brine；
High-temperature electrolysis light salt brine pH value is adjusted after dechlorination processing, pH adjusting processing is carried out, is added in pH adjustment process
Alkali or hydrochloric acid adjust the pH to 4-7 of light salt brine, and the existing known method for adjusting pH value of solution is suitable for the present invention in this field；
3, light salt brine fine tune temperature is handled
After adjusting pH value, the temperature of high-temperature electrolysis light salt brine is finely adjusted, drops electrolysis light salt brine temperature slightly
Low high temperature light salt brine；Light salt brine after pH will be adjusted by fine tune temperature unit 1 (fine tune temperature Unit selection heat exchanger,
Usually plate heat exchanger or the accurate deployment unit of high/low temperature (are accurately adjusted using low-temperature centrifugation mother liquor and high temperature light salt brine
With), existing known heat exchanger is suitable for the present invention in this field) it is changed with the light salt brine of recirculated water or time brine section
Heat, the temperature for adjusting light salt brine is 70 DEG C (being usually also applied for the present invention for 60-80 DEG C)；
4, filtering and impurity removing is handled
The high temperature light salt brine that temperature slightly reduces is passed through filter (usually cartridge filter), is filtered removal of impurities,
Pretreatment light salt brine is obtained, the temperature for pre-processing light salt brine is 70 DEG C (usually 60-80 DEG C)；PH is 4-7；
The temperature that the heat exchange processing of preprocessing process only slightly adjusts light salt brine is 60-80 DEG C, avoids water (i.e. chlorine
Alkali industrial ionic film is electrolysed light salt brine) temperature fluctuation it is big, heat exchange processing can also be carried out without using heat exchanger, only pass through activity
Charcoal adsorbs free chlorine, and adjusting Free Chlorine in Brine content is zero；Acid adding adjusts the pH of light salt brine directly to be protected after 4-7
Peace filtering, the i.e. pretreatment of light salt brine are successively to carry out removing free chlorine to light salt brine, adjust pH, or successively carrying out to light salt brine
It removes free chlorine, adjust pH, filtering and impurity removing.
With activated carbon adsorption in the present invention, free chlorine is removed, in this field the side of other existing known removing free chlorines
Method is suitable for the present invention；The acid additives of light salt brine pH are adjusted other than hydrochloric acid, it is existing known acid in this field
Additive is suitable for the present invention；Light salt brine Temperature Treatment is adjusted to use except plate heat exchanger, it is existing known in this field
The heat exchanger of other forms is suitable for the present invention；Filtering and impurity removing other than using cartridge filter, in this field it is existing
Other filters known are suitable for the present invention.
5, the pressurized treatments of light salt brine
Pretreatment light salt brine is inputted into presser unit 2, by high-pressure pump, it is (logical to >=1.0MPa to promote the pressure of light salt brine
Often being forced into pressure is that 1.0-3.0MPa is suitable for the present invention), obtain pressurization light salt brine；
7, the membrane separation of light salt brine
Pressurization light salt brine is inputted into film separation unit 3, nanofiltration membrane component (the high temperature nanofiltration membrane group of film separation unit
Part) will pressurization light salt brine be filtered into concentrate (i.e. the highly concentrated light salt brine of containing sulfate radicals) and penetrating fluid (i.e. containing sulfate radicals concentration
Low light salt brine), by 3-5 grades of multistage membrane filtration module, until sulfate ion concentration >=30g/l of concentrate is (usually
For 30-80g/l)；Sulfate ion concentration≤1g/l of penetrating fluid；Pressure >=1.0MPa is controlled (usually in membrane filtration processes
1.0-3.0MPa), light salt brine temperature is 60-80 DEG C；
8, crystallization-separating treatment
Concentrate after film filtration treatment is inputted into crystallization-separative unit 4, concentrate is delivered in saltpetre sinking device, by following
Ring pump, low-temperature plate heat exchanger and cold water exchange heat, so that concentrate temperature is reduced to 5 DEG C or less (usual concentrate temperature
It is reduced to 0 DEG C or less to be suitable for the present invention), sal glauberi crystallization is precipitated, and sal glauberi crystallization is deposited to saltpetre sinking device bottom
Then portion produces sal glauberi crystal through centrifuge separation, the mother liquor reflux after centrifugation to brine section carries out at salt dissolving
Reason enters the accurate deployment unit of high/low temperature by conveying equipment, after melting sodium chloride or concentration, continues engaging sulphate
Processing.
The temperature of centrifugate is high, is directly back to brine section and carries out salt dissolving processing, the salt dissolving processing of usual brine section
In the process, the temperature of salt dissolving water needs to reach 60 DEG C or more, and the mother liquor temperature after centrifugal treating of the present invention is high, does not need to add again
Heat can both carry out salt dissolving processing, save the energy, reduce energy consumption.
9, MVR upgrading unit or salt dissolving unit
Penetrating fluid after film filtration treatment is inputted into MVR upgrading unit 5, penetrating fluid enters MVR enrichment facility, is concentrated
Processing improves the concentration of penetrating fluid, then carries out film filtration treatment again；
Or the penetrating fluid after film filtration treatment is inputted into salt dissolving unit, penetrating fluid directly returns to brine section salt dissolving, melts
Sodium chloride.
Penetrating fluid temperature after high temperature nanofiltration membrane is high, into MVR brine concentration device, saves the heat that heating needs
Amount, saves a large amount of energy, reduces processing energy consumption；If penetrating fluid directly carries out salt dissolving processing, due to the temperature of penetrating fluid
High (60-80 DEG C) is spent, salt dissolving processing can be directly carried out, not need additional heating, the temperature of salt dissolving water is provided, can carry out
Salt dissolving processing, saves the energy, reduces energy consumption.
Embodiment 1
Such as Fig. 1,1A, object in ionic membrane electrolysis depleted brine engaging sulphate processing system includes sequentially connected sequentially through pipeline
Dechlorination clean unit 10, fine tune temperature unit 1, presser unit 2, film separation unit 3；And go out with the concentrate of membrane filter unit
Connected crystallization-the separative unit 4 of mouth exports the upgrading unit 5 being connected with the penetrating fluid of membrane filter unit, and wherein dechlorination purification is single
Member selection activated carbon adsorber, the high temperature light salt brine that electrolysis with ion-exchange film generates flow through activated carbon adsorber, and activated carbon adsorption is free
Chlorine reduces the free chlorine of high temperature light salt brine to 0；Fine tune temperature Unit selection plate heat exchanger, to the high temperature light salt brine after dechlorination
Temperature be finely adjusted processing, make to be electrolysed the high temperature light salt brine that slightly reduces of light salt brine temperature；Presser unit selects high-pressure pump,
The high temperature light salt brine that temperature slightly reduces flows through high-pressure pump, promotes pressure >=1.0MPa of light salt brine；Film separation unit selection string
The 3-5 grade nanofiltration membrane component (/ high temperature nanofiltration membrane component) of connection carries out membrane separation to high temperature light salt brine, at film separation unit
The light salt brine (i.e. concentrate) of high sulfate radical content after reason enters crystallization-separative unit, and concentrate is delivered in saltpetre sinking device, leads to
Cross circulating pump, cryopanel is changed and is exchanged heat with cold water so that concentrate temperature is reduced to 5 DEG C or less (usual concentrate temperature drops
It is suitable for the present invention down to 0 DEG C or less), sal glauberi crystallization is precipitated, and sal glauberi crystallization is deposited to saltpetre sinking device bottom
Then portion produces sal glauberi crystal through centrifuge separation；The light salt of film separation unit treated low sulfate radical content
Water (i.e. penetrating fluid) is passed through upgrading unit, and penetrating fluid enters MVR enrichment facility, MVR is gone to be concentrated；Or after film separation unit processing
The direct salt dissolving of penetrating fluid, that is, low sulfate radical content light salt brine.
Embodiment 2
Such as Fig. 3, object in ionic membrane electrolysis depleted brine engaging sulphate processing system includes sequentially connected de- sequentially through pipeline
Chlorine clean unit 10, presser unit 2, film separation unit 3；And the crystallization-point being connected with the concentrated solution outlet of membrane filter unit
From unit 4, the upgrading unit 5 being connected with the water outlet of membrane filter unit, other than not including fine tune temperature unit, remaining
It is same as Example 1.
Claims (11)
1. a kind of processing system of high temperature film method for removing sulfate ion, including film separation unit and dense with film separation unit
Contracting liquid exports the crystallization-separative unit being connected, and exports the upgrading unit being connected, feature with the penetrating fluid of film separation unit
Being further includes being sequentially connected dechlorination clean unit and fine tune temperature unit by pipeline before film separation unit is arranged in,
In:
Dechlorination clean unit, for removing free chlorine to the high-temperature electrolysis light salt brine of electrolysis with ion-exchange film；
Fine tune temperature unit, for carrying out fine tune temperature processing to the high-temperature electrolysis light salt brine after dechlorination.
2. a kind of processing system of high temperature film method for removing sulfate ion, including film separation unit and dense with film separation unit
Contracting liquid exports the crystallization-separative unit being connected, and exports the upgrading unit being connected, feature with the penetrating fluid of film separation unit
Being further includes dechlorination clean unit before being connected to film separation unit by pipeline, for the high-temperature electric to electrolysis with ion-exchange film
It solves light salt brine and removes free chlorine.
3. processing system as claimed in claim 1 or 2, which is characterized in that the dechlorination clean unit selects activated carbon adsorption
Device.
4. processing system as claimed in claim 3, which is characterized in that the activated carbon adsorption device selects activated carbon adsorption
Tower, absorbent charcoal adsorption tank or active carbon adsorber.
5. processing system as described in claim 1, which is characterized in that the fine tune temperature Unit selection heat-exchanger rig.
6. processing system as claimed in claim 5, which is characterized in that the heat-exchanger rig selection plate heat exchanger or high/low temperature
Accurate deployment unit.
7. processing system as claimed in claim 1 or 2, which is characterized in that the film separation unit selects nanofiltration membrane component.
8. processing system as claimed in claim 7, which is characterized in that the film separation unit selects 3-5 grades of concatenated nanofiltrations
Membrane module.
9. processing system as claimed in claim 7, which is characterized in that the film separation unit selects 3-5 grades of concatenated high temperature
Nanofiltration membrane component.
10. processing system as claimed in claim 1 or 2, which is characterized in that the crystallization-separative unit includes passing through pipeline
Sequentially connected saltpetre sinking device, centrifuge.
11. processing system as claimed in claim 1 or 2, which is characterized in that the upgrading unit selects MVR inspissator.
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| CN201920139909.3U CN209652063U (en) | 2019-01-25 | 2019-01-25 | A kind of processing system of high temperature film method for removing sulfate ion |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920139909.3U CN209652063U (en) | 2019-01-25 | 2019-01-25 | A kind of processing system of high temperature film method for removing sulfate ion |
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| Publication Number | Publication Date |
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| CN209652063U true CN209652063U (en) | 2019-11-19 |
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