CN205346850U - Two embrane method salt refining devices in perhalogeno system alkali - Google Patents
Two embrane method salt refining devices in perhalogeno system alkali Download PDFInfo
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Abstract
The utility model relates to a two embrane method salt refining devices in perhalogeno system alkali belongs to salt refining technical field, including consecutive brine reaction barrel I (1), hollow fiber diffusion barrier I (2), receive and strain subassembly (3), duolite system device (4) and ionic membrane system alkali device (5). The utility model discloses a refining plant can reduce the membrane and pollute, improve membrane throughput, the technique is more advanced, process is simple in addition, resource utilization rate is high, investment and low in production cost operate safe and simplely, economy and social are showing.
Description
Technical field
The present invention relates to bi-membrane method salt refining device in a kind of total halogenated caustic production, particularly relate to a kind of hollow-fibre membrane in conjunction with NF membrane bi-membrane method salt refining device.
Background technology
At present, domestic chlor-alkali industry mainly adopts ionic membrane method alkaline, and with saturated brine for raw material, electrolysis produces the product such as sodium hydroxide, if containing impurity such as substantial amounts of calcium, magnesium, sulfate radicals in saline, calcium, magnesium ion can in electrolytic process with the OH on anode-Reaction generates insoluble matter and is deposited on ionic membrane, have a strong impact on service life of ion-exchange membrane, and sulfate radical cannot pass through ionic membrane, brine system accumulates, can at anode discharge after reaching finite concentration, the oxygen producing free state can produce comparatively serious destruction by antianode, and therefore, salt refining is particularly important in ionic membrane method alkaline production process.
Domestic chlor-alkali enterprises tradition primary refined brine is generally adopted " barrel type reactor+dongle settling tank+sand filter " technique, with NaOH and Na2CO3For finishing agent, TXY is settling agent, and hydrochloric acid is nertralizer refined brine；Secondary brine rectification is generally adopted " carbon element filter+chelate resin tower " technique, but traditional handicraft exist affected greatly by salt quality, brine quality instability, the solid suspension of saline exceeds standard and the problem such as filter easily blocking after filtration.
Membrane separation technique, as a kind of emerging isolation technics, has that technique is simple, separation efficiency advantages of higher, receives significant attention in chlor-alkali industry salt refining.Relatively early the membrane process for chlorine industry salt refining mainly has gore film method, HVM tubular membrane two kinds.Gore film method refined brine technique adopts and first adds sodium hydroxide and barium chloride in saline, reaction generates magnesium hydroxide, barium sulfate, add sodium carbonate and generate calcium carbonate solid material, send into Gore membrane filtra-tion technology and filter prepared primary brine, Gore membrane filtra-tion technology adopts PTFE filter membrane/PP composite tube filter membrane, exist filter membrane combined strength bination low, easily by problems such as brine corrosion are damaged.HVM tubular membrane is the tubular membrane of the full PTFE material of Hyflux, compensate for the defect of PTFE filter membrane/PP composite tube filter membrane, but HVM tubular membrane brine rectification process is the same with gore film method refined brine technique, still adopt end-filtration, filter cake is easily gathered on film surface, flux declines fast, and technique adopts the method that calcium carbonate and magnesium hydroxide substep separate, and production stage is complicated.
Above two membrane process all adopts end-filtration form, process fouling membrane is serious, ZL200610038868.6 proposes a kind of method of refining salt by membrane filtration, adopt inoranic membrane crossflow filtration technique, feedstock direction is parallel with film surface, face is had good souring, it is effectively reduced filter cake deposition, improve membrane flux, its technique is as follows: add sodium hydroxide in saline, the reaction of the finishing agent such as sodium carbonate and barium chloride generates magnesium hydroxide, calcium carbonate and barium sulfate solid matter, add solidifying auxiliary agent and carry out pretreatment with oxidant, magnesium hydroxide colloidal and fraction solids granule thereof is removed with co-precipitation by adsorbing, with inoranic membrane cross-flow filter, saline is filtered, penetrating fluid through inoranic membrane enters into ion exchange resin, obtain refined brine after treatment, do not return pretreatment through the saline rich in impurity of film.Though this technique adopts inoranic membrane crossflow filtration technique, effectively reducing fouling membrane, but still there is problems in that (1) barium chloride removes sulfate radical as finishing agent, barium chloride is poisonous and expensive；(2) substantial amounts of barium sulfate mud is produced, subsequent treatment difficulty；(3) ceramic membrane operation energy consumption is big, and cost of investment is high.
Along with membrane technology develops, NF membrane is due to big to the ion rejection difference on effect of different valence state, it is applied in chlorine industry salt refining gradually, the technique that ZL201210118653.0 proposes a kind of bi-membrane method salt refining: pending saline enters filter after pretreatment and obtains high glass gall and refined brine；Pretreatment refers to that pending saline is successively through deliming, magnesium ion program, except ammonium program, reducing program and pH regulator program；Filter is that saline after pretreatment pumps into stripping tube formula membrane module and carries out ultrafiltration, thus the organic impurities in saline, suspended material and partly precipitated thing are retained, being directly entered nanofiltration membrane component after high-pressure pump adherence pressure through the saline of tubular membrane and carry out nanofiltration, the saline through tubular membrane does not then return deliming, magnesium ion program；In a high voltage state, sulfate ion is retained down by NF membrane and obtains high glass gall, chloride ion and sodium ion and pass through NF membrane and obtain refined brine.This technique adopts air stripping tubular membrane component to carry out ultrafiltration, alleviate fouling membrane, reduce operating cost, adopt NF membrane to retain sulfate ion, replace tradition to add barium chloride and remove sulfate radical method, more environmental protection, but still there is problems in that (1) adopts tubular membrane component, membrane module filling area is little, and equipment investment is big, and floor space is big；(2) refined brine obtained after nanofiltration still contains certain calcium, magnesium ion, it is difficult to reach electrolysis with ion-exchange film refined brine requirement.
Summary of the invention
The present invention solves the technical problem that the deficiency being in that existing separation film filling area is little and film disposal ability is weak, and the high unserviceable defect of salt made from earth containing a comparatively high percentage of sodium chloride water that nanofiltration obtains, the purpose of this utility model is in that to provide bi-membrane method salt refining device in a kind of total halogenated caustic production.
Concrete technical scheme is as follows:
Bi-membrane method brine rectification process device in a kind of total halogenated caustic production, including the salt reaction container I being sequentially connected, hollow fiber separating film I, nanofiltration assembly, ion exchange resin system device and ionic exchange membrane caustic soda units.
The discharging opening that retains of described hollow fiber separating film I connects filter-pressing device.
Described nanofiltration assembly retains discharging opening and connects calcium desulfurization device, and high strength gypsum is prepared in calcium desulfurization device production, and calcium desulfurization device is connected with reaction container II, and the charging aperture that reaction container II exports with hollow fiber separating film II is connected.
The discharging opening that retains of described hollow fiber separating film II is connected with filter-pressing device.
The pressing filtering liquid discharging opening of described filter-pressing device is connected with salt reaction container I.
The light salt brine discharging opening of described ionic exchange membrane caustic soda units is connected with MVR vaporizer, and MVR vaporizer is that discharging opening is connected with the charging aperture of the charging aperture of nanofiltration membrane component and ion exchange resin system device respectively.
Hollow-fibre membrane in described hollow fiber separating film I and hollow fiber separating film II combines by 1～100 hollow fiber film assembly series, parallel or series-parallel connection mode, and filter type is interior press filtration, operates pressure 0.1 ~ 0.3MPa.
Described hollow-fibre membrane is encapsulated in putamina sealant by many hollow fiber film thread two ends and forms, and hollow-fibre membrane is anisotropic membrane, molecular cut off 1000 ~ 1000000Da, film filament diameter 1-4mm, long 0.5-2m.
NF membrane aperture in described nanofiltration assembly is 1nm, molecular cut off 50 ~ 1000Da, operates pressure 1.0 ~ 4.0MPa.
Beneficial effect
This utility model bi-membrane method brine rectification process device adopts hollow-fibre membrane as separating film, and hollow fiber film assembly filling area is much larger than ceramic membrane, tubular membrane, and floor space is little, and equipment investment expense reduces；And hollow fiber film assembly adopts backwash technique, it is possible to decrease fouling membrane, improving film disposal ability, technology is more advanced, can directly refine 305g/L saturated bittern.
In addition adopt nanofiltration denitrating technique, instead of traditional barium method denitration, decrease the adding of agent kind in saline, saved reagent cost, avoid the intractable problem of barium sulfate mud simultaneously；What is more important solves the existing high unserviceable predicament of salt made from earth containing a comparatively high percentage of sodium chloride water, high salt made from earth containing a comparatively high percentage of sodium chloride water is prepared high value added product α-high strength gypsum by calcium desulfurization system by the technique that the present invention adopts, product 2h rupture strength is more than 6MPa, dry comprcssive strength more than 50MPa, reach JC/T2038-2010 standard α 50 highest level, can selling, utilization of resources, economic benefit is obvious.
Accompanying drawing explanation
Fig. 1 is bi-membrane method salt refining apparatus structure schematic diagram in this utility model total halogenated caustic production.
In figure: 1, salt reaction container I；2, hollow fiber separating film I；3, nanofiltration membrane component；4, ion exchange resin system device；5, ionic exchange membrane caustic soda units；6, MVR vaporizer；7, calcium desulfurization device；8, reaction container II；9, hollow fiber separating film II；10, filter-pressing device.
Detailed description of the invention
In order to be further appreciated by the present invention, below in conjunction with embodiment, the preferred embodiment of the invention is described, but it is to be understood that these describe simply as further illustrating the features and advantages of the present invention, rather than limiting to the claimed invention.
Below in conjunction with accompanying drawing 1, this utility model is described in detail:
Former halogen is pumped directly into salt reaction container by this utility model, by refining reaction, generates CaCO3、Mg(OH)2By hollow fiber separating film I after solid matter, hollow fiber separating film I is combined by 1～100 hollow fiber film assembly series, parallel or series-parallel connection mode, for anisotropic membrane, molecular cut off 1000 ~ 1000000Da, film filament diameter 1-4mm, long 0.5-2m, membrane material selects Kynoar, polyether sulfone, polysulfones or polyacrylonitrile；Filtering precipitation through hollow fiber separating film I, filtrate enters nanofiltration membrane component, NF membrane aperture 1nm, molecular cut off 50 ~ 1000Da, operates pressure 1.0 ~ 4.0MPa；Filtrate processes through NF membrane denitration, SO4 2-Retained by NF membrane, SO in the low salt made from earth containing a comparatively high percentage of sodium chloride water after nanofiltration processes4 2-Content≤2g/L, SO in high salt made from earth containing a comparatively high percentage of sodium chloride water4 2-Content >=30g/L；The high salt made from earth containing a comparatively high percentage of sodium chloride water retained adds Ca2+Generate calcium sulfate, obtain calcium sulphate solid then through solid-liquid separation, after the permeate of nanofiltration adsorbs then through exchanger resin, obtain refined brine, send into ionic membrane alkaline system；
Solid and concentrated solution that hollow fiber separating film I retains send into press filteration system, and the body refuse outward transport of extrusion processes, and pressing filtering liquid is sent into salt reaction container and recycled；
The mother solution that calcium desulfurization system solid-liquid separation obtains, then through adding CO3 2-And OH-, make Ca2+、Mg2+Precipitation, adsorbs then through ion exchange resin after hollow fiber separating film II filters, is re-fed into ionic membrane alkaline system；Solid and concentrated solution that hollow fiber separating film II retains are sent into filter-pressing device and are recycled；
Refined brine, after ionic membrane alkaline system alkaline, obtains remaining light salt brine, through dechlorination, concentration, obtains saline, is divided into saline I and saline II, and saline I returns nanofiltration membrane system and is circulated, and saline II and low salt made from earth containing a comparatively high percentage of sodium chloride water are mixed into salt refining operation.
Embodiment 1
Bi-membrane method salt refining device in this utility model total halogenated caustic production:
S1: be pumped directly into salt reaction container I from the former halogen of well ore deposit extraction, the NaCl concentration of the former halogen in well ore deposit is 305g/L, calcium content 0.53g/L, content of magnesium 0.1g/L, sulfate radical content 17g/L, in salt reaction container I, metering adds sodium carbonate 1.80g/L and sodium hydroxide 0.52g/L, respectively with the Ca in feed liquid2+、Mg2+Reaction generates CaCO3Precipitate and Mg (OH)2Colloid, carries out ultrafiltration through hollow fiber separating film I, operates pressure 0.15MPa, membrane flux 85L/m2H, in permeate saline, calcium, magnesium total content are less than 4mg/L；
S2: the permeate of ultrafiltration enters nanofiltration membrane component after high-pressure pump adherence pressure and carries out nanofiltration, operates pressure 2.4MPa, membrane flux 25L/m2H, major part SO4 2-It is retained down, saline is divided into low salt made from earth containing a comparatively high percentage of sodium chloride water and high salt made from earth containing a comparatively high percentage of sodium chloride water two parts by NF membrane, through sulfate radical content 2.0g/L in the low salt made from earth containing a comparatively high percentage of sodium chloride water of NF membrane, the sulfate anion in brine system content 34.8g/L retained, in the high salt made from earth containing a comparatively high percentage of sodium chloride water retained, add calcium chloride 45.2g/L, obtain dihydrate gypsum then through solid-liquid separation process；
S3: the low salt made from earth containing a comparatively high percentage of sodium chloride water through NF membrane obtains the content of calcium and magnesium refined brine less than 20PPb by ion exchange resin system device after chelating resin adsorbs；Refined brine enters ionic exchange membrane caustic soda units electrolysis.
Embodiment 2
Bi-membrane method salt refining device in this utility model total halogenated caustic production:
S1: be pumped directly into salt reaction container I from the former halogen of well ore deposit extraction, the NaCl concentration of the former halogen in well ore deposit is 305g/L, calcium content 0.53g/L, content of magnesium 0.1g/L, sulfate radical content 17g/L, in salt reaction container I, metering adds sodium carbonate 1.80g/L and sodium hydroxide 0.52g/L, respectively with the Ca in feed liquid2+、Mg2+Reaction generates CaCO3Precipitate and Mg (OH)2Colloid, carries out ultrafiltration through hollow fiber separating film I, operates pressure 0.15MPa, membrane flux 85L/m2H, in permeate saline, calcium, magnesium total content are less than 4mg/L；The concentrated solution that hollow fiber separating film I retains sends into filter-pressing device, and the body refuse outward transport of extrusion processes, and pressing filtering liquid recycles；
S2: the permeate of ultrafiltration enters nanofiltration membrane component after high-pressure pump adherence pressure and carries out nanofiltration, operates pressure 2.4MPa, membrane flux 25L/m2H, major part SO4 2-It is retained down, saline is divided into low salt made from earth containing a comparatively high percentage of sodium chloride water and high salt made from earth containing a comparatively high percentage of sodium chloride water two parts by NF membrane, through sulfate radical content 2.0g/L in the low salt made from earth containing a comparatively high percentage of sodium chloride water of NF membrane, the sulfate anion in brine system content 34.8g/L retained, calcium chloride 45.2g/L is added in the high salt made from earth containing a comparatively high percentage of sodium chloride water retained, through calcium desulfurization device inner filtration, turn brilliant, dehydration and the prepared α-high strength gypsum powder of drying process, product 2h rupture strength 7.2MPa, dry comprcssive strength 57.5MPa；
S3: the low salt made from earth containing a comparatively high percentage of sodium chloride water through NF membrane obtains the content of calcium and magnesium refined brine less than 20PPb by ion exchange resin system device after chelating resin adsorbs；Refined brine enters ionic exchange membrane caustic soda units electrolysis.
Embodiment 3
Bi-membrane method salt refining device in this utility model total halogenated caustic production:
S1: be pumped directly into salt reaction container I from the former halogen of well ore deposit extraction, the NaCl concentration of the former halogen in well ore deposit is 305g/L, calcium content 0.53g/L, content of magnesium 0.1g/L, sulfate radical content 17g/L, in salt reaction container I, metering adds sodium carbonate 1.80g/L and sodium hydroxide 0.52g/L, respectively with the Ca in feed liquid2+、Mg2+Reaction generates CaCO3Precipitate and Mg (OH)2Colloid, carries out ultrafiltration through hollow fiber separating film I, operates pressure 0.15MPa, membrane flux 85L/m2H, in permeate saline, calcium, magnesium total content are less than 4mg/L；The concentrated solution that hollow fiber separating film I retains sends into filter-pressing device, and the body refuse outward transport of extrusion processes, and pressing filtering liquid recycles；
S2: the permeate of ultrafiltration enters nanofiltration membrane component after high-pressure pump adherence pressure and carries out nanofiltration, operates pressure 2.4MPa, membrane flux 25L/m2H, major part SO4 2-It is retained down, saline is divided into low salt made from earth containing a comparatively high percentage of sodium chloride water and high salt made from earth containing a comparatively high percentage of sodium chloride water two parts by NF membrane, through sulfate radical content 2.0g/L in the low salt made from earth containing a comparatively high percentage of sodium chloride water of NF membrane, the sulfate anion in brine system content 34.8g/L retained, calcium chloride 45.2g/L is added in the high salt made from earth containing a comparatively high percentage of sodium chloride water retained, through calcium desulfurization device inner filtration, turn brilliant, dehydration and the prepared α-high strength gypsum powder of drying process, product 2h rupture strength 7.2MPa, dry comprcssive strength 57.5MPa；Mother solution after calcium desulfurization enters reaction container II, sends into hollow fiber separating film II and filter after refining reaction, sulfate radical content 3.3g/L in the mother liquid filtrate passed through, sulfate radical content 5g/L after mixing with low salt made from earth containing a comparatively high percentage of sodium chloride water, saline II；
S3: low salt made from earth containing a comparatively high percentage of sodium chloride water, saline II and mother liquid filtrate mixed liquor obtain the content of calcium and magnesium refined brine less than 20PPb by ion exchange resin system device after chelating resin adsorbs；Refined brine enters ionic exchange membrane caustic soda units electrolysis, light salt brine sodium chloride concentration out is 200g/L, chlorine residue 200mg/L, sulfate radical content 6.67g/L, metering add sodium sulfite 0.03g/L dechlorination after through MVR vapo(u)rization system evaporation and concentration to sodium chloride concentration be the saline of 300g/L, being divided into two parts to recycle the saline of concentration again, saline I returns nanofiltration program and is circulated, and saline II, mother liquid filtrate and low salt made from earth containing a comparatively high percentage of sodium chloride water are mixed into salt refining later process.
Embodiment 4
Bi-membrane method salt refining device in this utility model total halogenated caustic production:
S1: being pumped directly into salt reaction container I from the former halogen of well ore deposit extraction, the NaCl concentration of the former halogen in well ore deposit is 200g/L, calcium content 0.54g/L, content of magnesium 0.08g/L, sulfate radical content 16.5g/L.In salt reaction container I, metering adds sodium carbonate 1.82g/L and sodium hydroxide 0.45g/L, respectively with the Ca in feed liquid2+、Mg2+Reaction generates CaCO3Precipitate and Mg (OH)2Colloid, after squeeze into hollow fiber separating film I through pump and carry out ultrafiltration, operate pressure 0.1MPa, membrane flux 60L/m2H, in permeate saline, calcium, magnesium total content are less than 4mg/L；The concentrated solution that hollow fiber separating film I retains sends into press filteration system, and the body refuse outward transport of extrusion processes, and pressing filtering liquid recycles；
S2: the permeate of ultrafiltration enters nanofiltration membrane component after high-pressure pump adherence pressure after mixing with saline I and carries out nanofiltration, operates pressure 1.8MPa, membrane flux 20L/m2H, through sulfate radical content 1.9g/L in the low salt made from earth containing a comparatively high percentage of sodium chloride water of NF membrane, the sulfate anion in brine system content 105.0g/L retained, calcium chloride 125.1g/L is added in the high salt made from earth containing a comparatively high percentage of sodium chloride water retained, through calcium desulfurization device inner filtration, turn crystalline substance, dehydration and drying process prepare α-high strength gypsum powder, product 2h rupture strength 8.0MPa, dry comprcssive strength 72.4MPa, mother solution after calcium desulfurization enters reaction container II, after refining reaction, send into hollow fiber separating film II filter, sulfate radical content 3.4g/L in the mother liquid filtrate passed through, with low salt made from earth containing a comparatively high percentage of sodium chloride water, sulfate radical content 4.8g/L after saline II mixing；
S3: low salt made from earth containing a comparatively high percentage of sodium chloride water, saline II and mother liquid filtrate mixed liquor obtain the content of calcium and magnesium refined brine less than 20PPb by ion exchange resin system device after chelating resin adsorbs；Refined brine is entered ionic exchange membrane caustic soda units electrolysis, light salt brine sodium chloride concentration out is 150g/L, chlorine residue 180mg/L, sulfate radical content 6.34g/L, metering add sodium sulfite 0.01g/L dechlorination after through MVR vapo(u)rization system evaporation and concentration to sodium chloride concentration be the saline of 200g/L, being divided into two parts to recycle the saline of concentration again, saline I returns nanofiltration program and is circulated, and saline II, low salt made from earth containing a comparatively high percentage of sodium chloride water and mother liquid filtrate are mixed into salt refining later process.
Embodiment 5
Bi-membrane method salt refining device in this utility model total halogenated caustic production:
S1: being pumped directly into salt reaction container I from the former halogen of well ore deposit extraction, the NaCl concentration of the former halogen in well ore deposit is 280g/L, calcium content 0.2g/L, content of magnesium 0.32g/L, sulfate radical content 15g/L.In salt reaction container I, metering adds sodium carbonate 0.85g/L and sodium hydroxide 1.30g/L, respectively with the Ca in feed liquid2+、Mg2+Reaction generates CaCO3Precipitate and Mg (OH)2Colloid, after squeeze into hollow fiber separating film I through pump and carry out ultrafiltration, operate pressure 0.2MPa, membrane flux 120L/m2H, in permeate saline, calcium, magnesium total content are less than 4mg/L；The concentrated solution that hollow fiber separating film I retains sends into filter-pressing device, and the body refuse outward transport of extrusion processes, and pressing filtering liquid recycles；
S2: the permeate of ultrafiltration enters nanofiltration membrane component after high-pressure pump adherence pressure after mixing with saline I and carries out nanofiltration, operates pressure 3.2MPa, membrane flux 35L/m2H, through sulfate radical content 1.9g/L in the low salt made from earth containing a comparatively high percentage of sodium chloride water of NF membrane, the sulfate anion in brine system content 54.2g/L retained, calcium chloride 66.4g/L is added in the high salt made from earth containing a comparatively high percentage of sodium chloride water retained, α-high strength gypsum powder is prepared through calcium desulfurization device, product 2h rupture strength 7.8MPa, dry comprcssive strength 64.2MPa, mother solution after calcium desulfurization enters reaction container II, after refining reaction, send into hollow fiber separating film II filter sulfate radical content 3.5g/L, sulfate radical content 4.8g/L after mixing with low salt made from earth containing a comparatively high percentage of sodium chloride water, saline II in the mother liquid filtrate passed through；The concentrated solution that hollow fiber separating film II retains is sent into filter-pressing device and is recycled；
S3: low salt made from earth containing a comparatively high percentage of sodium chloride water, saline II and mother liquid filtrate mixed liquor obtain the content of calcium and magnesium refined brine less than 20PPb by ion exchange resin system device after chelating resin adsorbs；Refined brine is entered ionic exchange membrane caustic soda units electrolysis, light salt brine sodium chloride concentration out is 200g/L, chlorine residue 200mg/L, sulfate radical content 6.52g/L, metering add sodium sulfite 0.02g/L dechlorination after through MVR vapo(u)rization system evaporation and concentration to sodium chloride concentration be the saline of 280g/L, being divided into two parts to recycle the saline of concentration again, saline I returns nanofiltration system and is circulated, and saline II and low salt made from earth containing a comparatively high percentage of sodium chloride water are mixed into salt refining later process.
Claims (9)
1. bi-membrane method salt refining device in a total halogenated caustic production, it is characterised in that: include the salt reaction container I (1), hollow fiber separating film I (2), nanofiltration assembly (3), ion exchange resin system device (4) and the ionic exchange membrane caustic soda units (5) that are sequentially connected.
2. bi-membrane method salt refining device in total halogenated caustic production according to claim 1, it is characterised in that: the discharging opening that retains of described hollow fiber separating film I (2) connects filter-pressing device (10).
3. bi-membrane method salt refining device in total halogenated caustic production according to claim 1, it is characterised in that: described nanofiltration assembly (3) retains discharging opening and connects calcium desulfurization device (7), and calcium desulfurization device (7) is connected with reaction container II (8)；Reaction container II (8) discharging opening is connected with the charging aperture of hollow fiber separating film II (9).
4. bi-membrane method salt refining device in total halogenated caustic production according to claim 3, it is characterised in that: the discharging opening that retains of described hollow fiber separating film II (9) is connected with filter-pressing device (10).
5. bi-membrane method salt refining device in total halogenated caustic production according to claim 4, it is characterised in that: the pressing filtering liquid discharging opening of described filter-pressing device (10) is connected with salt reaction container I (1).
6. bi-membrane method salt refining device in total halogenated caustic production according to claim 1, it is characterized in that: the light salt brine discharging opening of described ionic exchange membrane caustic soda units (5) is connected with MVR vaporizer (6), MVR vaporizer (6) is that discharging opening is connected with the charging aperture of the charging aperture of nanofiltration membrane component (3) and ion exchange resin system device (4) respectively.
7. bi-membrane method salt refining device in total halogenated caustic production according to claim 1, it is characterized in that: the hollow-fibre membrane in described hollow fiber separating film I and hollow fiber separating film II combines by 1～100 hollow fiber film assembly series, parallel or series-parallel connection mode, filter type is interior press filtration, operates pressure 0.1 ~ 0.3MPa.
8. bi-membrane method salt refining device in total halogenated caustic production according to claim 7, it is characterized in that: described hollow-fibre membrane is encapsulated in putamina sealant by many hollow fiber film thread two ends and forms, hollow-fibre membrane is anisotropic membrane, molecular cut off 1000 ~ 1000000Da, film filament diameter 1-4mm, long 0.5-2m.
9. bi-membrane method salt refining device in total halogenated caustic production according to claim 1, it is characterised in that: NF membrane aperture 1nm, molecular cut off 50 ~ 1000Da in described nanofiltration assembly, operate pressure 1.0 ~ 4.0MPa.
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| CN110372012A (en) * | 2019-07-02 | 2019-10-25 | 马鞍山星奇达新材料科技有限公司 | A kind of embrane method total halogenated caustic production method of no solid waste discharge |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110372012A (en) * | 2019-07-02 | 2019-10-25 | 马鞍山星奇达新材料科技有限公司 | A kind of embrane method total halogenated caustic production method of no solid waste discharge |
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