CN102344219A - Method of total halogenated caustic production - Google Patents
Method of total halogenated caustic production Download PDFInfo
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- CN102344219A CN102344219A CN2011101851036A CN201110185103A CN102344219A CN 102344219 A CN102344219 A CN 102344219A CN 2011101851036 A CN2011101851036 A CN 2011101851036A CN 201110185103 A CN201110185103 A CN 201110185103A CN 102344219 A CN102344219 A CN 102344219A
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- China
- Prior art keywords
- brine
- light salt
- salt brine
- perhalogeno
- sulfate radical
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 67
- 238000004519 manufacturing process Methods 0.000 title abstract description 14
- 239000003518 caustics Substances 0.000 title abstract description 5
- 239000012267 brine Substances 0.000 claims abstract description 132
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 132
- 150000003839 salts Chemical class 0.000 claims abstract description 116
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000000460 chlorine Substances 0.000 claims abstract description 32
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 32
- 239000011347 resin Substances 0.000 claims abstract description 21
- 229920005989 resin Polymers 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000003513 alkali Substances 0.000 claims description 45
- 238000005868 electrolysis reaction Methods 0.000 claims description 19
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 150000001412 amines Chemical class 0.000 claims description 8
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 8
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 8
- 229910001069 Ti alloy Inorganic materials 0.000 claims description 6
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 239000010936 titanium Substances 0.000 claims description 6
- 229910052719 titanium Inorganic materials 0.000 claims description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000003014 ion exchange membrane Substances 0.000 abstract description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 abstract 1
- 230000007423 decrease Effects 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 abstract 1
- 230000008020 evaporation Effects 0.000 abstract 1
- 238000009776 industrial production Methods 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000012528 membrane Substances 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 7
- 241001131796 Botaurus stellaris Species 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 235000011121 sodium hydroxide Nutrition 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 230000005587 bubbling Effects 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 150000001768 cations Chemical class 0.000 description 3
- 239000012266 salt solution Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- QDHHCQZDFGDHMP-UHFFFAOYSA-N Chloramine Chemical compound ClN QDHHCQZDFGDHMP-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 235000017550 sodium carbonate Nutrition 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 150000001457 metallic cations Chemical class 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
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- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention relates to a method of total halogenated caustic production, and belongs to the chemical field. In order to solve the problem of high cost of dilute brine recovery in the prior art, the invention provides a method of total halogenated caustic production; secondary brine is obtained by free chlorine removal, sulfite and sulfate removal, evaporation concentration, and resin treatment, and thus the purpose of dilute brine recovery is reached. Based on integrated innovation, the invention provides a set of industrial production process, adopts reasonable process steps and process parameter design, solves the recovery and utilization problem of dilute brine generated in caustic production by an ion-exchange membrane method, decreases the cost, reduces process outflanking of producing salts by brine and then dissolving the salts in water, saves a lot of energy consumption in salt production, and also protect the environment.
Description
Technical field
The present invention relates to a kind of method of industry system alkali, more particularly, the present invention relates to a kind of method of ionic membrane method perhalogeno system alkali.
Background technology
Traditional chlor-alkali production technology is that salt is soluble in water, removes impurity such as calcium, magnesium, sulfate radical, ammonia nitrogen.The input electrolyzer carries out electrolysis and makes chlorine, hydrogen and sodium hydroxide.Adopt the water-soluble production energy consumption that causes salt of salt, 140 yuan of the production costs of one ton of salt of every production in the technology.Wherein, energy consumption folding standard coal is 0.25 ton.Adopt energy consumption and cost that perhalogeno system alkali can saving salt production.
Ionic membrane method alkali-making process process is:
1, removal of impurities: bittern adds soda ash and removes Ca
2+, Sr
2+, Ba
2+, Al
3+, Hg
2+Etc. most ion, get into the baffling groove, add the NaClO of some amount, in removing the ammonia react groove, accomplish reaction and generate monochloramine;
2, stripping is handled: and Xiang Tazhong is blown into pressurized air and carries out stripping and handle, and monochloramine is taken out of system by air;
3, system alkali: after removing most metal ion and total amine; Remove nitre technology removal sulfate radical with embrane method and obtain primary brine; Primary brine further removes metallic cations such as calcium-magnesium removing through Ao's resin complexing absorption; Secondary brine after resin tower is handled reaches ion-exchange membrane electrolyzer to the brinish quality standard; Secondary brine gets into electrolyzer and under the effect of electric current, reacts, and makes caustic soda, chlorine and hydrogen.
The qualified secondary brine of being processed into the light salt brine that produces in the ion-exchange membrane electrolyzer (salts contg is at 15-21%) reclaims that to be used for electrolyzer be the key that can perhalogeno system alkali be realized; There is enterprise's employing to re-inject salt mine on the industry and handles, but be subjected to the mine to be directed at the increase of energy consumption and the rising of cost apart from the production that produces transportation cost or salt with the method that adds solid salt.So it is most economical and method for saving energy that light salt brine is directly handled reuse.
Summary of the invention
The present invention is intended to solve the high problem of light salt brine cost recovery in the prior art; Realize a kind of method of ionic membrane method perhalogeno system alkali; Present method efficiently solves and adopts the technical problem that reclaims light salt brine in the bittern direct production caustic soda; Being applied in the state-of-the-art ionic membrane method perhalogeno system alkali of success reaches economic, energy-conservation effect.
In order to realize the foregoing invention purpose, concrete technical scheme of the present invention is following:
A kind of method of perhalogeno system alkali; Comprise that removal of impurities, stripping processing amine and ammonia nitrogen, preparation primary brine, resin system prepare secondary brine and electrolysis system alkali; It is characterized in that: detect the free chlorine in the light salt brine of described electrolysis system alkali generating step; The S-WAT that in light salt brine, adds light salt brine quality 0.1-2%; Adding the salt acid for adjusting pH value again is 8-9; Circulating reaction 1-8 hour, remove the free chlorine that produces in the electrolytic process; Feed pressurized air again, excessive inferior sulfate radical is oxidized to sulfate radical; The light salt brine of removing free chlorine and inferior sulfate radical gets into embrane method and removes the nitre device; Remove behind the sulfate radical light salt brine with get into vapo(u)rization system in the lump without the light salt brine that removes nitre; Remove portion water; Improve salts contg and obtain reclaiming light salt brine to advancing the groove concentration requirement; Get into resin processing system in the lump with primary brine; Make that to meet into the refined brine of slot standard be secondary brine (secondary brine continues into groove electrolysis system alkali, and cost is practiced thrift in recycle).
Above-mentioned circulating reaction is to mix from flowing, and need not heat exchange, and it is 60-75 ℃ that light salt brine goes out the groove temperature.
The pressurized air of above-mentioned adding is the pressurized air of 0.15-0.3MPa.
The compressed-air actuated amount of above-mentioned feeding is that light salt brine and the volume ratio of air of removing behind the free chlorine are 1:8-12.
Above-mentioned entering embrane method is removed the light salt brine of removing free chlorine and inferior sulfate radical of nitre device, accounts for the 25-100% of the light salt brine total amount of removing free chlorine and inferior sulfate radical.
The above-mentioned light salt brine of removing behind the sulfate radical gets into vapo(u)rization system and removes portion water, and salts contg is increased to 250-320g/l.
The standard of the above-mentioned recovery secondary brine that makes is:
NaCl=290-310g/l、I
-≤0.1ppm、Ca
2++Mg
2+＜20ppb、Ba
2+＜0.1ppm、Fe
2++Fe
3+＜0.15ppm、Al
3+?＜0.1ppm、Sr
2+?＜0.1ppm、Mn
2+?＜0.05ppm、Ni
2+?＜0.01ppm。
The above-mentioned material that is used for the used container of spissated vapo(u)rization system is titanium or titanium alloy.
The useful technique effect that the present invention brings:
The present invention is based on integrated innovation one cover industrialized producing technology is provided; Utilization reasonable technology step and process parameters design; Solved the recycling problem of ionic membrane legal system alkali generation light salt brine; Reduced cost; Having reduced bittern, to process salt circuitous by the water-soluble technology of salt again; Save the mass energy consumption of salt manufacturing, also protected environment.
Description of drawings
Fig. 1 is a Total Halogenated Caustic Production schema of the present invention.
Embodiment
Embodiment 1
The ionic membrane method perhalogeno system alkali that light salt brine is reclaimed:
A kind of method of ionic membrane method perhalogeno system alkali; Comprise that removal of impurities, stripping processing amine and ammonia nitrogen, preparation primary brine, resin system prepare secondary brine and electrolysis system alkali; It is characterized in that: detect the free chlorine in the light salt brine of described electrolysis system alkali generating step; The excessive S-WAT that in light salt brine, adds light salt brine quality 0.1%; Adding the salt acid for adjusting pH value again is 8; Circulating reaction 1 hour is removed the free chlorine that produces in the electrolytic process; Feed pressurized air again, excessive inferior sulfate radical is oxidized to sulfate radical; The light salt brine of removing free chlorine and inferior sulfate radical gets into embrane method and removes the nitre device; The light salt brine of removing behind the sulfate radical gets into vapo(u)rization system; Remove portion water; Improve salts contg and obtain reclaiming light salt brine to advancing the groove concentration requirement; Get into resin processing system in the lump with primary brine, make and meet into that the refined brine of slot standard is a secondary brine.
Embodiment 2
The ionic membrane method perhalogeno system alkali that light salt brine is reclaimed:
A kind of method of ionic membrane method perhalogeno system alkali; Comprise that removal of impurities, stripping processing amine and ammonia nitrogen, preparation primary brine, resin system prepare secondary brine and electrolysis system alkali; It is characterized in that: detect the free chlorine in the light salt brine of described electrolysis system alkali generating step; The excessive S-WAT that in light salt brine, adds light salt brine quality 2%; Adding the salt acid for adjusting pH value again is 9; Circulating reaction 8 hours is removed the free chlorine that produces in the electrolytic process; Feed pressurized air again, excessive inferior sulfate radical is oxidized to sulfate radical; The light salt brine of removing free chlorine and inferior sulfate radical gets into embrane method and removes the nitre device; The light salt brine of removing behind the sulfate radical gets into vapo(u)rization system; Remove portion water; Improve salts contg and obtain reclaiming light salt brine to advancing the groove concentration requirement; Get into resin processing system in the lump with primary brine, make and meet into that the refined brine of slot standard is a secondary brine.
Embodiment 3
The ionic membrane method perhalogeno system alkali that light salt brine is reclaimed:
A kind of method of ionic membrane method perhalogeno system alkali; Comprise that removal of impurities, stripping processing amine and ammonia nitrogen, preparation primary brine, resin system prepare secondary brine and electrolysis system alkali; It is characterized in that: detect the free chlorine in the light salt brine of described electrolysis system alkali generating step; The excessive S-WAT that in light salt brine, adds light salt brine quality 0.6%; Adding the salt acid for adjusting pH value again is 8.5; Circulating reaction 4 hours is removed the free chlorine that produces in the electrolytic process; Feed pressurized air again, excessive inferior sulfate radical is oxidized to sulfate radical; Remove 1/3rd of free chlorine and inferior sulfate radical light salt brine and get into embrane methods and remove the nitre device, the light salt brine of removing behind the sulfate radical gets into vapo(u)rization system.Two of its excess-three branch also gets into vapo(u)rization system and removes portion water, improves salts contg and obtains reclaiming light salt brine to advancing the groove concentration requirement, gets into resin processing system in the lump with primary brine, makes to meet into that the refined brine of slot standard is a secondary brine.
Embodiment 4
The ionic membrane method perhalogeno system alkali that light salt brine is reclaimed:
A kind of method of ionic membrane method perhalogeno system alkali; Comprise that removal of impurities, stripping processing amine and ammonia nitrogen, preparation primary brine, resin system prepare secondary brine and electrolysis system alkali; It is characterized in that: detect the free chlorine in the light salt brine of described electrolysis system alkali generating step; The excessive S-WAT that in light salt brine, adds light salt brine quality 1.6%; Adding the salt acid for adjusting pH value again is 8.8; Circulating reaction 2 hours is removed the free chlorine that produces in the electrolytic process; Feed pressurized air again, excessive inferior sulfate radical is oxidized to sulfate radical; The light salt brine 1/2nd of removing free chlorine and inferior sulfate radical gets into embrane method and removes the nitre device; The light salt brine of removing behind the sulfate radical gets into vapo(u)rization system; All the other also entering vapo(u)rization systems of 1/2nd; Remove portion water; Improve salts contg and obtain reclaiming light salt brine to advancing the groove concentration requirement; Get into resin processing system in the lump with primary brine, make and meet into that the refined brine of slot standard is a secondary brine.
Embodiment 5
On the basis of embodiment 1-4, further preferred version is:
The pressurized air that in removing the step of excessive inferior sulfate radical, adds is the pressurized air of 0.15MPa; The amount of bubbling air is that light salt brine and the volume ratio of air of removing behind the free chlorine are 1:8;
Account for 25% of the light salt brine total amount that produces in the electrolysis system alkali step getting into light salt brine that embrane method removes the nitre device;
Remove light salt brine behind the sulfate radical and get into vapo(u)rization system and remove portion water, salts contg is increased to 250g/l, obtain reclaiming light salt brine;
Reclaim light salt brine and primary brine and get into resin processing system in the lump, make secondary brine.
The material that is used for the used container of spissated vapo(u)rization system is titanium or titanium alloy.
Embodiment 6
On the basis of embodiment 1-4, further preferred version is:
The pressurized air that in removing the step of excessive inferior sulfate radical, adds is the pressurized air of 0.3MPa; The amount of bubbling air is that light salt brine and the volume ratio of air of removing behind the free chlorine are 1:12;
Account for 100% of the light salt brine total amount that produces in the electrolysis system alkali step getting into light salt brine that embrane method removes the nitre device;
Remove light salt brine behind the sulfate radical and get into vapo(u)rization system and remove portion water, salts contg is increased to 320g/l, obtain reclaiming light salt brine;
Reclaim light salt brine and primary brine and get into resin processing system in the lump, make secondary brine.
The material that is used for the used container of spissated vapo(u)rization system is titanium or titanium alloy.
Embodiment 7
On the basis of embodiment 1-4, further preferred version is:
The pressurized air that in removing the step of excessive inferior sulfate radical, adds is the pressurized air of 0.25MPa; The amount of bubbling air is that light salt brine and the volume ratio of air of removing behind the free chlorine are 1:10;
Account for 63% of the light salt brine total amount that produces in the electrolysis system alkali step getting into light salt brine that embrane method removes the nitre device;
Remove light salt brine behind the sulfate radical and get into vapo(u)rization system and remove portion water, salts contg is increased to 280g/l, obtain reclaiming light salt brine;
Reclaim light salt brine and primary brine and get into resin processing system in the lump, make secondary brine.
The material that is used for the used container of spissated vapo(u)rization system is titanium or titanium alloy.
Embodiment 8
On the basis of embodiment 1-4, further preferred version is:
The pressurized air that in removing the step of excessive inferior sulfate radical, adds is the pressurized air of 0.17MPa; The amount of bubbling air is that light salt brine and the volume ratio of air of removing behind the free chlorine are 1:11;
Account for 90% of the light salt brine total amount that produces in the electrolysis system alkali step getting into light salt brine that embrane method removes the nitre device;
Remove light salt brine behind the sulfate radical and get into vapo(u)rization system and remove portion water, salts contg is increased to 260g/l, obtain reclaiming light salt brine;
Reclaim light salt brine and primary brine and get into resin processing system in the lump, make secondary brine.
The material that is used for the used container of spissated vapo(u)rization system is titanium or titanium alloy.
Embodiment 9
According to Figure of description Fig. 1 perhalogeno system alkali method is described:
1500 cubic metres of bittern are preheating to 55 ℃ through plate-type heat exchangers, get into the baffling groove and add 25 kilograms of 4.5 tons in 30% sodium hydroxide and clorox, reactive tank before getting into stirs.Pump into pressurized tank and on pipeline, feed the empty fully sudden and violent gas (0.18MPa, 2.5 ten thousand mark sides) of compression.(this process is got rid of organic amine in the bittern and ammonia nitrogen with the mode of ammonia),
After removing denitrification; Be mixed into settling bowl 1 with iron trichloride; The upper clear supernate overflow gets into the divalent cation treater; 880 kilograms of the sodium carbonate solutions of adding 15%; Fully stir; Get into settling bowl 2; The pressurization of upper clear supernate pump gets into film filter; (brine quality per-cent is thousandth to see through liquid adding S-WAT; Excessive 4%) and hydrochloric acid; Regulate pH value 8-9 and remove that excessive free chlorine is laggard goes into resin tower secondary treatment salt solution, further remove divalent cation, reach into groove salt water quality standard (in calcium≤20ppb).
Qualified refined brine after secondary treatment gets into ion-exchange membrane electrolyzer, current density 5.5A/CM
2, under the effect of electric current, produce 840 tons in 32% sodium hydroxide and produce 1100 tons of light salt brines simultaneously.
Add S-WAT in 1100 tons of light salt brines and remove the free chlorine that produces in the electrolysis with hydrochloric acid adjusting pH8.5; Feed the sudden and violent gas (0.18MPA of pressurized air; 1.5 make inferior sulfate radical be converted into sulfate radical ten thousand mark sides); Remove nitre through embrane method and change (settling bowl 2 outlets of two effect concentration systems over to; Get into resin tower secondary treatment salt solution; Further remove divalent cation, reached groove salt water quality standard (20PPB).After making concentration bring up to 275g/l, get into embrane method and remove nitre system removal sulfate radical, incorporate the salt solution of secondary settlement again into.
Claims (8)
1. the method for a perhalogeno system alkali; Comprise that removal of impurities, stripping processing amine and ammonia nitrogen, preparation primary brine, resin system prepare secondary brine and electrolysis system alkali; It is characterized in that: detect the free chlorine in the light salt brine of described electrolysis system alkali generating step; The S-WAT that in light salt brine, adds light salt brine quality 0.1-2%; Adding the salt acid for adjusting pH value again is 8-9; Circulating reaction 1-8 hour, remove the free chlorine that produces in the electrolytic process; Feed pressurized air again, excessive inferior sulfate radical is oxidized to sulfate radical; The light salt brine of removing free chlorine and inferior sulfate radical gets into embrane method and removes the nitre device; The light salt brine of removing behind the sulfate radical gets into vapo(u)rization system; Remove portion water; Improve salts contg and obtain reclaiming light salt brine to advancing the groove concentration requirement; Get into resin processing system in the lump with primary brine, make and meet into that the refined brine of slot standard is a secondary brine.
2. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: described circulating reaction is for mixing from flowing, and it is 60-75 ℃ that light salt brine goes out the groove temperature.
3. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: the pressurized air of described adding is the pressurized air of 0.15-0.3MPa.
4. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: the compressed-air actuated amount of described feeding is that light salt brine and the volume ratio of air of removing behind the free chlorine are 1:8-12.
5. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: described entering embrane method accounts for the 25-100% of its total amount except that the light salt brine of removing free chlorine and inferior sulfate radical of nitre device.
6. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: the described light salt brine of removing behind the sulfate radical gets into vapo(u)rization system and removes portion water, is meant salts contg is increased to 250-320g/l.
7. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: the standard of the described secondary brine that makes is:
NaCl=290-310g/l、I
-≤0.1ppm、Ca
2++Mg
2+＜20ppb、Ba
2+＜0.1PPm、Fe
2++Fe
3+＜0.15PPm、Al
3+?＜0.1PPm、Sr
2+?＜0.1PPm、Mn
2+?＜0.05PPm、Ni
2+?＜0.01PPm。
8. the method for a kind of perhalogeno system alkali according to claim 1 is characterized in that: described vapo(u)rization system is for adopting the vapo(u)rization system of titanium or titanium alloy container.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102851684A (en) * | 2012-09-17 | 2013-01-02 | 广州新普利节能环保科技有限公司 | Process and device for preparing alkali by full-brine mechanical steam recompression method |
| CN104532283A (en) * | 2014-12-17 | 2015-04-22 | 济宁金威煤电有限公司 | Method and device for producing caustic soda through electrolysis by replacing part of fine brine with light salt brine |
| CN104695252A (en) * | 2015-02-13 | 2015-06-10 | 中盐金坛盐化有限责任公司 | Method for preparing dyeing accelerant from high liquid glauber salt |
| CN106906485A (en) * | 2017-03-31 | 2017-06-30 | 四川永祥股份有限公司 | A kind of total Halogenated Caustic Production |
| CN107366005A (en) * | 2016-05-11 | 2017-11-21 | 江苏井神盐化股份有限公司 | A kind of process of sodium sulphate type bittern perhalogeno ionic membrane caustic soda by-product glauber salt |
| CN110723742A (en) * | 2019-11-26 | 2020-01-24 | 江西富达盐化有限公司 | Novel process for producing liquid salt by using sodium carbonate distillate |
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| Publication number | Priority date | Publication date | Assignee | Title |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102851684A (en) * | 2012-09-17 | 2013-01-02 | 广州新普利节能环保科技有限公司 | Process and device for preparing alkali by full-brine mechanical steam recompression method |
| CN102851684B (en) * | 2012-09-17 | 2015-08-05 | 广州新普利节能环保科技有限公司 | A kind of perhalogeno water function of mechanical steam recompression method alkali-making process and device |
| CN104532283A (en) * | 2014-12-17 | 2015-04-22 | 济宁金威煤电有限公司 | Method and device for producing caustic soda through electrolysis by replacing part of fine brine with light salt brine |
| CN104532283B (en) * | 2014-12-17 | 2016-01-13 | 济宁金威煤电有限公司 | A method and device for producing caustic soda by electrolysis of light brine instead of part of refined brine |
| CN104695252A (en) * | 2015-02-13 | 2015-06-10 | 中盐金坛盐化有限责任公司 | Method for preparing dyeing accelerant from high liquid glauber salt |
| CN104695252B (en) * | 2015-02-13 | 2016-06-29 | 中盐金坛盐化有限责任公司 | A kind of method adopting high glass gall to prepare accelerant |
| CN107366005A (en) * | 2016-05-11 | 2017-11-21 | 江苏井神盐化股份有限公司 | A kind of process of sodium sulphate type bittern perhalogeno ionic membrane caustic soda by-product glauber salt |
| CN107366005B (en) * | 2016-05-11 | 2019-03-26 | 江苏苏盐井神股份有限公司 | A kind of process of sodium sulphate type bittern perhalogeno ionic membrane caustic soda by-product anhydrous sodium sulphate |
| CN106906485A (en) * | 2017-03-31 | 2017-06-30 | 四川永祥股份有限公司 | A kind of total Halogenated Caustic Production |
| CN110723742A (en) * | 2019-11-26 | 2020-01-24 | 江西富达盐化有限公司 | Novel process for producing liquid salt by using sodium carbonate distillate |
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