CN220201659U - Sewage treatment system - Google Patents
Sewage treatment system Download PDFInfo
- Publication number
- CN220201659U CN220201659U CN202320137814.4U CN202320137814U CN220201659U CN 220201659 U CN220201659 U CN 220201659U CN 202320137814 U CN202320137814 U CN 202320137814U CN 220201659 U CN220201659 U CN 220201659U
- Authority
- CN
- China
- Prior art keywords
- water inlet
- outlet
- water
- eliminator
- oxidizing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 239000010865 sewage Substances 0.000 title claims abstract description 323
- 238000011282 treatment Methods 0.000 title claims abstract description 217
- 239000012528 membrane Substances 0.000 claims abstract description 600
- 238000000909 electrodialysis Methods 0.000 claims abstract description 450
- 238000001728 nano-filtration Methods 0.000 claims abstract description 300
- 230000001590 oxidative effect Effects 0.000 claims abstract description 244
- 150000003839 salts Chemical class 0.000 claims abstract description 238
- 238000000926 separation method Methods 0.000 claims abstract description 115
- 239000000126 substance Substances 0.000 claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 1446
- 239000003513 alkali Substances 0.000 claims description 198
- 238000006386 neutralization reaction Methods 0.000 claims description 181
- 239000002253 acid Substances 0.000 claims description 178
- 239000000872 buffer Substances 0.000 claims description 168
- 239000005416 organic matter Substances 0.000 claims description 162
- 238000010438 heat treatment Methods 0.000 claims description 155
- 238000000746 purification Methods 0.000 claims description 151
- 239000013505 freshwater Substances 0.000 claims description 132
- 238000003379 elimination reaction Methods 0.000 claims description 124
- 230000008030 elimination Effects 0.000 claims description 121
- 239000007788 liquid Substances 0.000 claims description 118
- 239000007864 aqueous solution Substances 0.000 claims description 114
- 238000005261 decarburization Methods 0.000 claims description 93
- 238000007254 oxidation reaction Methods 0.000 claims description 72
- 230000003647 oxidation Effects 0.000 claims description 67
- 239000000243 solution Substances 0.000 claims description 61
- 239000007787 solid Substances 0.000 claims description 58
- 238000001704 evaporation Methods 0.000 claims description 51
- 230000008020 evaporation Effects 0.000 claims description 51
- 239000012267 brine Substances 0.000 claims description 34
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 34
- 238000004065 wastewater treatment Methods 0.000 claims description 31
- 238000000605 extraction Methods 0.000 claims description 30
- 238000001816 cooling Methods 0.000 claims description 29
- 239000011347 resin Substances 0.000 claims description 23
- 229920005989 resin Polymers 0.000 claims description 23
- 239000003638 chemical reducing agent Substances 0.000 claims description 22
- 239000000463 material Substances 0.000 claims description 18
- 230000020477 pH reduction Effects 0.000 claims description 16
- 238000004090 dissolution Methods 0.000 claims description 15
- 238000005262 decarbonization Methods 0.000 claims description 13
- 239000012141 concentrate Substances 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 10
- 230000003113 alkalizing effect Effects 0.000 claims description 4
- 238000005273 aeration Methods 0.000 claims description 3
- 230000003472 neutralizing effect Effects 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims 2
- 238000004064 recycling Methods 0.000 abstract description 25
- 239000002699 waste material Substances 0.000 abstract description 2
- 150000002500 ions Chemical class 0.000 description 134
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 90
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 76
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 description 76
- 239000007789 gas Substances 0.000 description 64
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 61
- 238000000034 method Methods 0.000 description 58
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 52
- 238000001223 reverse osmosis Methods 0.000 description 51
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 48
- 229910000029 sodium carbonate Inorganic materials 0.000 description 45
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 39
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 38
- 235000017557 sodium bicarbonate Nutrition 0.000 description 38
- 150000001768 cations Chemical class 0.000 description 35
- 238000010521 absorption reaction Methods 0.000 description 34
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 32
- 150000001450 anions Chemical class 0.000 description 32
- 238000004519 manufacturing process Methods 0.000 description 25
- CPELXLSAUQHCOX-UHFFFAOYSA-N Hydrogen bromide Chemical compound Br CPELXLSAUQHCOX-UHFFFAOYSA-N 0.000 description 24
- 239000001569 carbon dioxide Substances 0.000 description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 description 24
- BMYNFMYTOJXKLE-UHFFFAOYSA-N 3-azaniumyl-2-hydroxypropanoate Chemical compound NCC(O)C(O)=O BMYNFMYTOJXKLE-UHFFFAOYSA-N 0.000 description 21
- 230000003197 catalytic effect Effects 0.000 description 19
- -1 etc.) Chemical compound 0.000 description 19
- 230000000694 effects Effects 0.000 description 15
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 14
- 230000008569 process Effects 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 13
- 239000000047 product Substances 0.000 description 13
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 12
- 229910052794 bromium Inorganic materials 0.000 description 12
- 229910000042 hydrogen bromide Inorganic materials 0.000 description 12
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 11
- 238000001556 precipitation Methods 0.000 description 11
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 10
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 10
- 239000000460 chlorine Substances 0.000 description 10
- 229910052801 chlorine Inorganic materials 0.000 description 10
- 239000007800 oxidant agent Substances 0.000 description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 9
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 9
- 239000000920 calcium hydroxide Substances 0.000 description 9
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 9
- 239000001257 hydrogen Substances 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 9
- 229910001415 sodium ion Inorganic materials 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- 238000000108 ultra-filtration Methods 0.000 description 8
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 7
- 159000000007 calcium salts Chemical class 0.000 description 7
- 238000002425 crystallisation Methods 0.000 description 7
- 230000008025 crystallization Effects 0.000 description 7
- 235000019253 formic acid Nutrition 0.000 description 7
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- 229920006395 saturated elastomer Polymers 0.000 description 7
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 6
- 239000002585 base Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 5
- 229910017052 cobalt Inorganic materials 0.000 description 5
- 239000010941 cobalt Substances 0.000 description 5
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 5
- 230000005684 electric field Effects 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 5
- 229910052748 manganese Inorganic materials 0.000 description 5
- 239000011572 manganese Substances 0.000 description 5
- 238000012544 monitoring process Methods 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 4
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 238000007664 blowing Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 238000005868 electrolysis reaction Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 4
- 239000000347 magnesium hydroxide Substances 0.000 description 4
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 4
- 159000000003 magnesium salts Chemical class 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 239000008213 purified water Substances 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 239000011343 solid material Substances 0.000 description 4
- 239000008247 solid mixture Substances 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- 229910021575 Iron(II) bromide Inorganic materials 0.000 description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 3
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- 239000003518 caustics Substances 0.000 description 3
- 229940046149 ferrous bromide Drugs 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- GYCHYNMREWYSKH-UHFFFAOYSA-L iron(ii) bromide Chemical compound [Fe+2].[Br-].[Br-] GYCHYNMREWYSKH-UHFFFAOYSA-L 0.000 description 3
- 229910001425 magnesium ion Inorganic materials 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000012265 solid product Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical class [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000011552 falling film Substances 0.000 description 2
- 239000010408 film Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 2
- 229910001410 inorganic ion Inorganic materials 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 239000004277 Ferrous carbonate Substances 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- NPYPAHLBTDXSSS-UHFFFAOYSA-N Potassium ion Chemical compound [K+] NPYPAHLBTDXSSS-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- 239000004280 Sodium formate Substances 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- MCDLETWIOVSGJT-UHFFFAOYSA-N acetic acid;iron Chemical compound [Fe].CC(O)=O.CC(O)=O MCDLETWIOVSGJT-UHFFFAOYSA-N 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- NKWPZUCBCARRDP-UHFFFAOYSA-L calcium bicarbonate Chemical compound [Ca+2].OC([O-])=O.OC([O-])=O NKWPZUCBCARRDP-UHFFFAOYSA-L 0.000 description 1
- 229910000020 calcium bicarbonate Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910001429 cobalt ion Inorganic materials 0.000 description 1
- XLJKHNWPARRRJB-UHFFFAOYSA-N cobalt(2+) Chemical compound [Co+2] XLJKHNWPARRRJB-UHFFFAOYSA-N 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- IRXRGVFLQOSHOH-UHFFFAOYSA-L dipotassium;oxalate Chemical compound [K+].[K+].[O-]C(=O)C([O-])=O IRXRGVFLQOSHOH-UHFFFAOYSA-L 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- RAQDACVRFCEPDA-UHFFFAOYSA-L ferrous carbonate Chemical compound [Fe+2].[O-]C([O-])=O RAQDACVRFCEPDA-UHFFFAOYSA-L 0.000 description 1
- 235000019268 ferrous carbonate Nutrition 0.000 description 1
- 229960004652 ferrous carbonate Drugs 0.000 description 1
- 229940062993 ferrous oxalate Drugs 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- OWZIYWAUNZMLRT-UHFFFAOYSA-L iron(2+);oxalate Chemical compound [Fe+2].[O-]C(=O)C([O-])=O OWZIYWAUNZMLRT-UHFFFAOYSA-L 0.000 description 1
- 229910000015 iron(II) carbonate Inorganic materials 0.000 description 1
- 229910021506 iron(II) hydroxide Inorganic materials 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- 229910001437 manganese ion Inorganic materials 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 229940039748 oxalate Drugs 0.000 description 1
- 235000006408 oxalic acid Nutrition 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- DJEHXEMURTVAOE-UHFFFAOYSA-M potassium bisulfite Chemical compound [K+].OS([O-])=O DJEHXEMURTVAOE-UHFFFAOYSA-M 0.000 description 1
- 229940099427 potassium bisulfite Drugs 0.000 description 1
- WFIZEGIEIOHZCP-UHFFFAOYSA-M potassium formate Chemical compound [K+].[O-]C=O WFIZEGIEIOHZCP-UHFFFAOYSA-M 0.000 description 1
- 235000010259 potassium hydrogen sulphite Nutrition 0.000 description 1
- 229910001414 potassium ion Inorganic materials 0.000 description 1
- BHZRJJOHZFYXTO-UHFFFAOYSA-L potassium sulfite Chemical compound [K+].[K+].[O-]S([O-])=O BHZRJJOHZFYXTO-UHFFFAOYSA-L 0.000 description 1
- 235000019252 potassium sulphite Nutrition 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- HLBBKKJFGFRGMU-UHFFFAOYSA-M sodium formate Chemical compound [Na+].[O-]C=O HLBBKKJFGFRGMU-UHFFFAOYSA-M 0.000 description 1
- 235000019254 sodium formate Nutrition 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- ZNCPFRVNHGOPAG-UHFFFAOYSA-L sodium oxalate Chemical compound [Na+].[Na+].[O-]C(=O)C([O-])=O ZNCPFRVNHGOPAG-UHFFFAOYSA-L 0.000 description 1
- 229940039790 sodium oxalate Drugs 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
The utility model discloses a sewage treatment system which mainly comprises a sewage pipeline, an oxidizing eliminator, a nanofiltration membrane group or salt separation equipment, a bipolar membrane electrodialysis equipment or a crystallizer. After the sewage is treated by the system, the system can meet the national macroscopic requirement on recycling economy, and the waste in the sewage is extracted and converted into useful substances.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, and particularly relates to a sewage treatment system.
Background
Industrial plants can produce a lot of sewage, the main components of the sewage are generally chemical products used in the plants, so that the national environment greatly advances the recycling economy and saves energy, and for the call of the corresponding country, necessary innovative recycling economy routes are often used, useful substances are extracted from the sewage and purified into products, the consumption of resources is reduced, and the effect of recycling economy is achieved.
Disclosure of Invention
The utility model aims to provide a sewage treatment system, which is used for treating sewage, reduces the environmental pollution of the sewage and simultaneously recovers the economic value of beneficial substances in the sewage.
A sewage treatment system comprising: a sewage pipeline, an oxidizing eliminator, a nanofiltration membrane group or a monovalent ion purification electrodialysis device, a bipolar membrane electrodialysis device or a crystallizer,
the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the nanofiltration membrane group, and the fresh water outlet of the nanofiltration membrane group is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer (the concentrated water of the nanofiltration membrane group is discharged or subjected to other treatments or other uses); or the concentrated water outlet of the nanofiltration membrane group is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer (fresh water discharge of the nanofiltration membrane group or other treatment or other utilization); the nanofiltration membrane group comprises at least one stage of one section nanofiltration membrane, and can also be multistage and multistage nanofiltration membranes, for example, if fresh water of a first nanofiltration membrane is treated by the nanofiltration membrane, the treated nanofiltration membrane is called a second-stage nanofiltration membrane, if concentrated water of the first nanofiltration membrane is treated by the nanofiltration membrane, the treated nanofiltration membrane is called a second-stage nanofiltration membrane, and the like is called a multistage nanofiltration membrane or multistage nanofiltration membrane, or multistage and multistage nanofiltration membrane; or the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the purifying monovalent ion type electrodialysis device, and the outlet I of the purifying monovalent ion type electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer; or the outlet II of the purification monovalent ion electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
The purification monovalent ion type electrodialysis device is a novel electrodialysis device with special effect, which is derived from a conventional electrodialysis device, and can obtain a salt solution mainly comprising monovalent cations and monovalent anions from an outlet I from an aqueous solution containing monovalent ions, divalent or more than divalent ions, and can also have a concentration effect; the main action principle is that monovalent cation selective permeable membranes, monovalent anion selective permeable membranes or nanofiltration membranes are introduced into anion selective permeable membranes and cation selective permeable membranes of conventional electrodialysis according to the requirements and the ion characteristics of the inlet water, the monovalent cation selective permeable membranes only allow monovalent cations to pass through in theory, the monovalent anion selective permeable membranes only allow monovalent anions to pass through in theory, and the nanofiltration membranes only allow monovalent cations and monovalent anions to pass through in theory; for example, if sodium carbonate and sodium bromide are present in the water, an electrodialysis device for purifying monovalent ions corresponding to a membrane stack consisting of a cation selective permeable membrane and a monovalent anion selective permeable membrane or a cation selective permeable membrane and a nanofiltration membrane is used (remark, the principle of ion permeation through each membrane is the same as that of conventional electrodialysis, except that among anions, carbonate is a divalent anion, the monovalent anion selective permeable membrane and the nanofiltration membrane are theoretically impossible to permeate, only bromide is permeable, so that anions permeating through the monovalent anion selective permeable membrane and the nanofiltration membrane are only bromide and combine with sodium ions permeating through the cation selective permeable membrane, and a sodium bromide aqueous solution is mainly obtained at the outlet I), the outlet I is a sodium bromide aqueous solution, and the other outlet (i.e., the outlet II) is a sodium carbonate aqueous solution and contains a small amount of sodium bromide; and (3) injection: in the electrodialysis device for purifying monovalent ions, the outlet I refers to an outlet containing monovalent cations and monovalent anions (such as sodium bromide aqueous solution) and consists of an aqueous solution of ions penetrating through a membrane; outlet II is the outlet of a salt (such as an aqueous solution containing cobalt ions and manganese ions) mainly containing divalent cations or divalent anions, and consists of an aqueous solution of ions which do not penetrate the membrane; an aqueous solution of predominantly sodium ions (for example sodium bromide) exiting from the fresh water outlet of the nanofiltration unit v or from the outlet i of the electrodialysis device for purifying monovalent ions, in order to reduce the sodium ion content entering the oxidation reaction system;
Or the sewage treatment system comprises: a sewage pipeline, a salt separation unit and a crystallizer; the sewage pipeline is connected to the water inlet of the salt separating unit, and the water solution outlet of the salt separating unit is connected to the water inlet of the crystallizer;
or the sewage treatment system comprises: sewage pipes, oxidative eliminators, salifying units, bipolar membrane electrodialysis devices or crystallizers; the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the salt separating unit, and the water solution outlet of the salt separating unit is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer; or the sewage pipeline is connected to the water inlet of the salt separation unit, the water solution outlet of the salt separation unit is connected to the water inlet of the oxidizing eliminator, and the water outlet of the oxidizing eliminator is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
for the salt separation unit, salt separation is to remove a part of ionic solid matters of a kind in the water solution discharged from the sewage pipeline from the water solution;
the sewer line provides sewage to be treated.
Based on the sewage treatment system, the sewage treatment system preferably further comprises a concentration device c, namely, the water outlet of the oxidizing eliminator is connected to the water inlet of the concentration device c, and the concentrated water outlet of the concentration device c is connected to the water inlet of the salt separation unit, namely, the water solution at the water outlet of the oxidizing eliminator is concentrated, so that the subsequent salt separation operation of the salt separation unit is facilitated.
Based on the above sewage treatment system, it is preferable that the sewage pipe may be wash sewage discharged from a tail gas absorption tank (the tail gas is directly contacted with the absorption liquid in the tank), a tail gas absorption tower (the tail gas is directly contacted with the absorption liquid in the tower), a tail gas spray absorption tower (the tail gas is sprayed with the absorption liquid), a tail gas circulation spray absorption tower (the tail gas is sprayed with the absorption liquid and the absorption liquid is circulated and sprayed with a pump), or the like.
Based on the above sewage treatment system, it is preferable that the absorption of a part of the substances in the exhaust gas with an absorption liquid forms an aqueous solution in the sewage pipe, the absorption liquid comprising: alkaline absorption liquid, acidic absorption liquid or water is used as the absorption liquid, and the alkaline absorption liquid or the water is generally used as the absorption liquid when substances contained in the tail gas react with alkaline substances to generate salts (for example, when the tail gas contains acidic substances); generally, an acidic absorption liquid or water is used as the absorption liquid when substances contained in the tail gas react with acidic substances to form salts (for example, when alkaline substances are contained in the tail gas);
Based on the above sewage treatment system, preferably, the common alkaline absorption liquid is an aqueous solution of hydroxide, carbonate, bicarbonate and the like;
based on the above sewage treatment system, it is preferable that common cations of hydroxide, carbonate, bicarbonate, such as sodium ion, potassium ion, and the like.
Based on the above sewage treatment system, preferably, the common acidic absorption liquid is organic acid, hydrochloric acid, sulfuric acid, nitric acid, or the like.
Based on the above sewage treatment system, preferably, the source sewage of the sewage pipeline is sewage of a terephthalic acid plant, for example, after the tail gas of the terephthalic acid plant is treated by an RTO incineration method, a catalytic oxidation method (HPCCU or lpacu, etc.), the amount of the organic matters in the sewage is reduced (i.e. VOC is reduced), the rest tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of the RTO incineration method or the catalytic oxidation method, the residual tail gas is absorbed by an alkaline absorption liquid (exemplified by sodium hydroxide and generally used by a circulating absorption tower), the obtained mixed water solution mainly contains sodium carbonate, sodium bicarbonate and sodium bromide, the circulating absorption tower is required to be discharged so as to control the concentration of the mixed water solution in the circulating absorption tower not to be too high (stable concentration), and thus, the mixed water solution discharged by the circulating absorption tower (namely an alkaline absorption liquid) can be used as a sewage source of the sewage pipeline, but substances contained in the sewage are also valuable (bromine, sodium carbonate, etc.), and bromine, bromine and the bromine and sodium bromide and the economic recycling of the bromine and the sodium bromide can be realized if the bromine and the sodium bromide are more are wasted (the bromine and the sodium bromide are recycled; the recycling of sodium carbonate is achieved by extracting the sodium carbonate, so that recycling economy is achieved, and carbon emission reduction is achieved (if recycling economy is not achieved, the sodium carbonate enters a sewage treatment unit and is partially converted into carbon dioxide to enter the atmosphere).
Based on the sewage treatment system, preferably, the crystallizer (refers to heating the solvent to obtain a solid solute product) obtains a solid product, and the solid product is treated by a drying device to obtain an absolute dry product.
Based on the above sewage treatment system, preferably, the oxidizing property eliminator refers to a device for eliminating the oxidizing property of the sewage itself.
Based on the above sewage treatment system, preferably, the purpose of setting the oxidizing eliminator is to reduce the oxidizing property of the sewage, otherwise, the operation of the downstream nanofiltration membrane group and the reverse osmosis membrane is damaged (the nanofiltration membrane group and the reverse osmosis membrane generally require ORP < 150mv or residual chlorine < 0.1ppm, namely, the oxidizing property of the water body is reduced, otherwise, the nanofiltration membrane group and the reverse osmosis membrane are oxidized and rapidly fail); at the same time, the oxidizing property is harmful to the membrane stack of the bipolar membrane electrodialysis device.
Based on the above sewage treatment system, preferably, the oxidizing eliminator is preferably an oxidizing eliminator (oxidizing elimination reaction tank), a pipe mixer, or a pipe connection point.
Based on the above sewage treatment system, it is preferable that the reducing agent supply line is connected to the oxidation eliminator (oxidation elimination reaction tank), the pipe mixer, or the pipe connection point.
Based on the above sewage treatment system, preferably, the reducing agent dosing line is from a reducing agent supply pump or a reducing agent supply pressure pipe.
Based on the above sewage treatment system, it is preferable that the reducing agent be such as sulfite (e.g., sodium sulfite, potassium sulfite), bisulfite (e.g., sodium bisulfite, potassium bisulfite), formate (e.g., sodium formate, potassium formate), formic acid, aldehydes (e.g., formaldehyde, acetaldehyde, etc.), oxalic acid, oxalate (e.g., sodium oxalate, potassium oxalate), ferrous salts (e.g., ferrous oxalate, ferrous acetate, ferrous bromide, ferrous carbonate, ferrous formate, ferrous hydroxide), etc.
Based on the above sewage treatment system, preferably, the oxidizing property eliminator preferably comprises a buffer tank, and the sewage is kept in the buffer tank for a certain retention time, so that the oxidizing property of the sewage can be reduced.
Based on the above sewage treatment system, preferably, the oxidizing eliminator is preferably an aeration buffer tank, the sewage is retained in the buffer tank for a certain retention time, the oxidizing property of the sewage can be reduced, and the aeration helps to reduce the retention time.
Based on the sewage treatment system, preferably, the nanofiltration membrane group is mainly a nanofiltration membrane, the nanofiltration membrane is a device for separating monovalent ions and multivalent ions in a solution, and for inorganic matters, the nanofiltration membrane allows the monovalent ions to pass through the nanofiltration membrane to intercept divalent and more valent ions, so that the nanofiltration membrane fresh water rich in monovalent ions and the nanofiltration membrane concentrated water rich in divalent and more valent ions can be obtained after passing through the nanofiltration membrane group; for example, if sodium bromide and sodium carbonate are to be separated, after the nanofiltration membrane is used for treatment, the nanofiltration membrane fresh water is rich in sodium bromide and the nanofiltration membrane concentrated water is rich in sodium carbonate, so that the separation of monovalent bromide ions and divalent carbonate ions is realized, but the nanofiltration membrane fresh water and the nanofiltration membrane concentrated water are electrically neutral, so that the concentration of sodium ions is paired according to the charge concentration of anions in the nanofiltration fresh water and the nanofiltration concentrated water; or separating monovalent cations and divalent cations by using a nanofiltration membrane, wherein the nanofiltration membrane fresh water is rich in monovalent cations, the nanofiltration membrane concentrated water is rich in divalent cations, and the anion concentration is paired with the charge concentration of the respective cations in the nanofiltration fresh water and the nanofiltration concentrated water.
For example, after the organic matters in the tail gas of the terephthalic acid factory are treated (generally, an RTO incineration method, a catalytic oxidation method and the like), the amount of the organic matters is reduced, and the rest of the tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of the RTO incineration method or the catalytic oxidation method, and an alkaline absorption liquid (exemplified by sodium hydroxide) is used for obtaining a mixed solution of sodium carbonate, sodium bicarbonate and sodium bromide. The nanofiltration fresh water obtained by treating the mixed solution through a nanofiltration membrane group is mainly sodium bicarbonate and sodium bromide, the nanofiltration concentrated water is mainly sodium carbonate, and the purpose of the sewage treatment system is to obtain hydrobromic acid finally, so the nanofiltration fresh water is treated through bipolar membrane electrodialysis equipment to obtain acid, namely hydrobromic acid, and obtain alkali, namely sodium hydroxide. The nanofiltration concentrate (mainly sodium carbonate) can be used as an alkaline substance, for example, in a terephthalic acid plant for dissolving residues in an oxidation step of the terephthalic acid plant, and a process for recovering cobalt and manganese by a precipitation method.
Based on the above sewage treatment system, preferably, for example, after the tail gas of a terephthalic acid factory is treated by organic matters in the tail gas (generally, an RTO incineration method, a catalytic oxidation method and the like), the quantity of the organic matters is reduced, the rest tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of the RTO incineration method or the catalytic oxidation method, an alkaline absorption liquid (exemplified by sodium hydroxide) is used for obtaining a mixed aqueous solution of sodium carbonate, sodium bicarbonate and sodium bromide, the sodium bromide in the mixed aqueous solution has the highest solubility, the sodium carbonate is secondary, the sodium bicarbonate has the lowest solubility, and most of the sodium bicarbonate is converted into sodium carbonate and most of sodium carbonate after being heated by a salt separating unit (or by a salt separating unit after being concentrated) and separated out, and the sodium carbonate and the sodium bicarbonate in the mixed aqueous solution have lower precipitated proportion and the sodium bromide accounts for higher proportion; the solid (sodium carbonate solid) obtained by the salt separation unit can be used for dissolving residues in the oxidation process of terephthalic acid factories, recovering cobalt and manganese by a precipitation method and other processes; the solid of the salt separation unit obtained after the treatment of the tail gas of the terephthalic acid plant is mainly sodium carbonate, and the sodium carbonate is better used in dissolving residues of oxidation processes of the terephthalic acid plant and recovering cobalt and manganese by a precipitation method, so sodium bicarbonate can be added with sodium hydroxide to be converted into sodium carbonate for use.
Based on the above sewage treatment system, preferably, for example, after the tail gas of a terephthalic acid factory is treated by organic matters in the tail gas (generally, an RTO incineration method, a catalytic oxidation method and the like), the content of the organic matters is reduced, the rest tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of the RTO incineration method or the catalytic oxidation method, an alkaline absorption liquid (exemplified by sodium hydroxide) is used for obtaining a mixed aqueous solution of sodium carbonate, sodium bicarbonate and sodium bromide, a chemical is added to form a solid salt separation unit, and a chemical (such as calcium salt, magnesium salt, calcium hydroxide, magnesium hydroxide and the like, preferably calcium hydroxide) is added to the mixed aqueous solution to form a part of sodium bicarbonate and sodium carbonate into insoluble matters to be separated out, and sodium hydroxide, potassium hydroxide and the like can be added at the same time, so that the solubility of the bicarbonate, for example, calcium carbonate is far less than that of the calcium bicarbonate is easy to be separated out, at the moment, the ratio of the bicarbonate and the carbonate in the aqueous solution is reduced, and the ratio of the sodium bromide is high.
Based on the sewage treatment system, preferably, the bipolar membrane electrodialysis device is characterized in that under the action of a direct current electric field, water is electrolyzed into hydrogen ions and hydroxyl ions by using a bipolar membrane, strong brine can be converted into acid and alkali by skillfully combining the bipolar membrane with a positive membrane and a negative membrane, and positive ions in the brine are converted into hydroxides corresponding to the positive ions, namely alkali; converting anions in the brine into hydrides corresponding to the anions, namely acids; meanwhile, after the concentration of anions and cations in the strong brine is reduced after the anions and cations are converted into corresponding alkali and acid, the strong brine is called dilute brine;
Based on the above sewage treatment system, preferably, when it is desired to convert the fresh water outlet (salt rich in monovalent ions) of the nanofiltration membrane group into the corresponding acid-base, then connecting the fresh water outlet of the nanofiltration membrane group to the water inlet treatment of the bipolar membrane electrodialysis apparatus; when it is desired to convert the concentrated water outlet of the nanofiltration membrane module (salt enriched with ions of divalent and higher valence) to the corresponding acid-base, the concentrated water outlet of the nanofiltration membrane module is connected to the water inlet treatment of the bipolar membrane electrodialysis device.
Based on the above sewage treatment system, it is preferable that: still be equipped with add sour unit I:
the outlet of the acid adding unit I is connected to a fresh water outlet of the nanofiltration membrane group or a pipeline between the outlet I of the purification monovalent ion electrodialysis device and the water inlet of the bipolar membrane electrodialysis device; or the outlet of the acid adding unit I is connected to a fresh water outlet of the nanofiltration membrane group or a pipeline between the outlet I of the purification monovalent ion electrodialysis device and the water inlet of the crystallizer; or the outlet of the acid adding unit I is connected to a pipeline between the water solution outlet of the salt separating unit and the water inlet of the bipolar membrane electrodialysis device; or the outlet of the acid adding unit I is connected to a pipeline between the water solution outlet of the salt separating unit and the water inlet of the crystallizer; or the outlet of the acid adding unit I is connected to a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the bipolar membrane electrodialysis device; or the outlet of the acid adding unit I is connected to a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the crystallizer, and the connection position is called a pipeline connection point a;
Or a neutralization tank b is arranged between the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device, and the outlet of the acid adding unit I is connected to the water inlet of the neutralization tank b; or a neutralization tank b is arranged between the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the crystallizer, the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the crystallizer, and the outlet of the acid adding unit I is connected to the water inlet of the neutralization tank b;
or a neutralization tank b is arranged between the water solution outlet of the salt separation unit and the water inlet of the bipolar membrane electrodialysis device, the water solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b; or a neutralization tank b is arranged between the water solution outlet of the salt separation unit and the water inlet of the crystallizer, the water solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the crystallizer, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b; or a neutralization tank b is arranged between the water outlet of the oxidizing eliminator and the water inlet of the bipolar membrane electrodialysis device, the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b; or a neutralization tank b is arranged between the water outlet of the oxidizing eliminator and the water inlet of the crystallizer, the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the crystallizer, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b.
The acid adding unit I is used for adding acid, the purpose of acid adding is to neutralize a small amount of carbonate and bicarbonate remained in the aqueous solution by using acid, and the pH is generally controlled to be 1-7;
if the aqueous solution before finally entering the bipolar membrane electrodialysis device still contains a certain concentration of carbonate or bicarbonate, carbonic acid is generated in an acid chamber during the operation of the bipolar membrane electrodialysis device and is converted into carbon dioxide gas, and the operation stability of the bipolar membrane electrodialysis device is affected by the generation of gas in the acid chamber. If the aqueous solution before finally entering the crystallizer still contains carbonate or bicarbonate with a certain concentration, the purity of the product sodium bromide can be influenced, the sodium bromide is required to be reacted by HBr to obtain the sodium bromide, the purity of the sodium bromide is improved, and the impurity content of sodium carbonate and sodium bicarbonate is reduced.
Based on the above sewage treatment system, preferably, the inlet of the acid adding unit i is connected to an acid tank or an acid pipeline or an acid generating tank of the bipolar membrane electrodialysis device;
based on the sewage treatment system, preferably, the acid added by the acid adding unit I is hydrobromic acid or acetic acid;
an inlet of the acid adding unit I is connected to an acid tank or an acid production tank of the bipolar membrane electrodialysis device, and a conveying power pump or an acid production recycling pump of the bipolar membrane electrodialysis device is used as conveying power;
The inlet of the acid adding unit I is connected to an acid pipeline, and the self-pressure of the acid pipeline is used as conveying power;
based on the above sewage treatment system, preferably,
the acid tank or the acid producing tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the acid adding unit I, the pH value of the aqueous solution after acid addition is automatically monitored, the quantity of variable frequency discharge quantity of the conveying power pump or the acid producing recycling pump of the bipolar membrane electrodialysis equipment is controlled in a chain manner, or the reflux quantity of the conveying power pump or the acid producing recycling pump of the bipolar membrane electrodialysis equipment is controlled, and finally the purpose of automatically adjusting the acid adding quantity by the pH value is achieved, so that the pH value of the aqueous solution after acid addition is stably controlled;
and the pH value of the aqueous solution after acid addition is controlled by automatically monitoring and controlling a control valve on the acid pipeline in a linkage manner to control the amount of the acid addition so as to stably control the pH value of the aqueous solution after acid addition.
Based on the sewage treatment system, preferably, a pipeline mixer is further arranged at the position of the pipeline connection point a.
Based on the above sewage treatment system, preferably, a concentration device a is provided;
the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the pipeline connection point a, and the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the water inlet of the neutralization tank b (the neutralization tank b is provided with an acid provided by an acid adding unit I for neutralization), and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the neutralization tank b (the neutralization tank b is provided with an acid provided by an acid adding unit I for neutralization), the water outlet of the neutralization tank b is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
Based on the above sewage treatment system, preferably, a decarburization tower b is further provided:
when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the pipeline connection point a, and the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, a decarburization tower b is arranged at the following position: the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the pipeline connection point a, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, a decarburization tower b is arranged according to the following positions: the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, the water outlet of the decarburization tower b is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer; or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is firstly connected to the water inlet of the decarbonization tower b, and the water outlet of the decarbonization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the water inlet of the neutralization tank b (the neutralization tank b is provided with an acid provided by an acid adding unit I for neutralization), and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, a decarburization tower b is arranged according to the following positions: the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b (the neutralization tank b is provided with an acid provided by an acid adding unit I for neutralization), the water outlet of the neutralization tank b is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, a decarburization tower b is arranged according to the following positions: the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is firstly connected to the water inlet of the decarburization tower b, the water outlet of the decarburization tower b is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer; or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the water outlet of the neutralization tank b is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
Based on the above sewage treatment system, preferably, a concentration device a is provided;
when the aqueous solution outlet of the salt separation unit is connected to the pipe connection point a, which is connected to the water inlet of the bipolar membrane electrodialysis device and the water inlet of the crystallizer, a decarburization tower b is arranged at the following position: the water solution outlet of the salt separation unit is connected to the pipeline connection point a, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device and the water inlet of the crystallizer;
Or when the aqueous solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b (the neutralization tank b is provided with an acid supply unit I for neutralization), and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device and the water inlet of the crystallizer, a decarburization tower b is arranged according to the following positions: the water solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device and the water inlet of the crystallizer;
or when the water outlet of the oxidability eliminator is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank b, and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the water outlet of the neutralization tank b is connected to the water inlet of the decarburization tower b first, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
The decarbonization tower is operated by spraying the aqueous solution from top to bottom, and the compressed air convects with the aqueous solution from bottom to top to blow out the free carbon dioxide in the aqueous solution into the air.
Based on the sewage treatment system, a concentration device b is preferably arranged, and the concentration device b is arranged between the nanofiltration membrane group or the purification monovalent ion electrodialysis device and the water inlet of the bipolar membrane electrodialysis device and the water inlet of the crystallizer; the fresh water outlet or the concentrated water outlet of the nanofiltration membrane group is connected to the water inlet of the concentrating device b, and the concentrated water outlet of the concentrating device b is connected to the water inlet of the bipolar membrane electrodialysis equipment and the water inlet of the crystallizer; or the outlet I or the outlet II of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device b, and the concentrated water outlet of the concentration device b is connected to the water inlet of the bipolar membrane electrodialysis device and the water inlet of the crystallizer.
Based on the above sewage treatment system, preferably, an alkali adding unit I is provided, and the alkali adding unit I is used for adding an alkaline substance:
when the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, the outlet of the alkali adding unit I is connected with a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and the connection position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the oxidizing eliminator, and the connection position is called a pipeline connection point c; or a buffer tank I is arranged, the water outlet of the oxidizing eliminator is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the oxidizing eliminator, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the oxidizing eliminator;
Or when the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the salt separating unit, the outlet of the alkali adding unit I is connected with a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the salt separating unit, and the connected position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the oxidizing eliminator, and the connection position is called a pipeline connection point c; or the device is provided with a buffer tank I, the water outlet of the oxidizing eliminator is connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the salt separation unit, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the oxidizing eliminator, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the salt separating unit; or the outlet of the alkali adding unit I is connected to the oxidizing eliminator;
Or when the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the concentrating device c, and the concentrated water outlet of the concentrating device c is connected to the water inlet of the salt separating unit, the outlet of the alkali adding unit I is connected with a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the concentrating device c, and the connection position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline from the concentrated water outlet of the concentrating device c to the water inlet of the salt separating unit, and the connection position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the oxidizing eliminator, and the connection position is called a pipeline connection point c; or a buffer tank I is arranged, the water outlet of the oxidizing eliminator is connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the concentrating device c, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the concentrated water outlet of the concentrating device c is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the salt separation unit, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the oxidizing eliminator, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the salt separating unit; or the outlet of the alkali adding unit I is connected to the oxidizing eliminator;
Or when the sewage pipeline is connected to the water inlet of the salt separating unit, the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the salt separating unit, and the connected position is called a pipeline connection point c; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the salt separation unit, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the salt separating unit; or the outlet of the alkalizing unit I is connected to the oxidizing eliminator.
Based on the above sewage treatment system, it is preferable that the position of the pipe connection point c uses a pipe mixer. The purpose of designing the alkali adding unit I is as follows: when the aqueous solution entering the nanofiltration membrane group contains bicarbonate, the pH value can be raised by adding alkaline substances (exemplified by sodium hydroxide) into the aqueous solution before the aqueous solution enters the nanofiltration membrane group, the bicarbonate is converted into carbonate, and the carbonate converted from the bicarbonate can be intercepted on the concentrated water side of the nanofiltration membrane group by utilizing the monovalent and divalent ion separation effect of the nanofiltration membrane group so as to reduce the bicarbonate concentration at the fresh water outlet of the nanofiltration membrane group;
For example, the tail gas of terephthalic acid factory, because the organic matters in the tail gas are removed by an RTO incineration method or a catalytic oxidation method, the rest tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of the RTO incineration method or the catalytic oxidation method, alkali is used as absorption liquid (sodium hydroxide is taken as an example) to obtain a mixed solution of sodium carbonate, sodium bicarbonate and sodium bromide, alkaline matters are added into the mixed solution, the pH is raised (generally pH=8.5-13 is controlled), sodium bicarbonate is converted into sodium carbonate, the concentration of sodium bicarbonate in water is greatly reduced, the concentration of sodium bromide in fresh water is greatly increased, the concentration of sodium bromide in fresh water outlet of the obtained nanofiltration membrane is almost unchanged after passing through the nanofiltration membrane group, but the concentration of sodium bicarbonate in the fresh water outlet of the nanofiltration membrane group is reduced because the sodium bicarbonate is converted into sodium carbonate and is intercepted on the concentrated water side of the nanofiltration membrane group, so that the ratio of sodium bromide in fresh water of the nanofiltration membrane group is raised;
the purpose of designing the alkali adding unit I is as follows: when the aqueous solution contains bicarbonate, the alkaline substance (exemplified by sodium hydroxide) is added to the aqueous solution to raise the pH, so that the bicarbonate is converted into carbonate, most of the solids obtained by separating the salt from the concentrated and precipitated solid type salt separating unit are carbonate, the concentration of bicarbonate is low (for example, when the cation is sodium ion, most of the solids are sodium carbonate, and the concentration of sodium bicarbonate is low), the recovery rate of sodium carbonate is increased, and otherwise, the recovery rate of sodium carbonate is reduced because the bicarbonate is converted into carbonate+carbon dioxide when the concentrated and precipitated solid type salt separating unit is concentrated, so that the purpose of the design is to obtain sodium carbonate solids, such as terephthalic acid factories, and the sodium carbonate can be used as dissolved oxidation residues, and the effect of recovering cobalt and manganese is superior to that of sodium bicarbonate.
Based on the above sewage treatment system, preferably, the inlet of the alkali adding unit I is connected to an alkali tank or an alkali pipeline or an alkali producing tank of the bipolar membrane electrodialysis device;
an inlet of the alkali adding unit I is connected to an alkali tank or an alkali producing tank of the bipolar membrane electrodialysis device, and a conveying power pump or an alkali producing recycling pump of the bipolar membrane electrodialysis device is used as conveying power;
the inlet of the alkali adding unit I is connected to an alkali pipeline, and the self-pressure of the alkali pipeline is used as conveying power;
based on the above sewage treatment system, preferably,
the method comprises the steps that an alkali tank or an alkali producing tank of bipolar membrane electrodialysis equipment is connected to an inlet of an alkali adding unit I, the pH value of an aqueous solution after alkali addition is automatically monitored and controlled to control the quantity of variable frequency discharge quantity of the conveying power pump or an alkali producing recycling pump of the bipolar membrane electrodialysis equipment or the quantity of reflux quantity of the conveying power pump or the alkali producing recycling pump of the bipolar membrane electrodialysis equipment in a linkage mode, and finally the pH value is used for automatically controlling the quantity of alkali addition so as to stably control the pH value of the aqueous solution after alkali addition;
and the control valve on the alkali pipeline is used for controlling the quantity of the alkali to be added by automatically monitoring and controlling the pH value of the aqueous solution after alkali addition in a chain manner so as to stably control the pH value of the aqueous solution after alkali addition.
Based on above sewage treatment system, preferably, agitating unit is set up in the buffer tank I.
Based on the above sewage treatment system, preferably, the stirring device includes a stirrer, compressed gas stirring, and the like.
Based on the above sewage treatment system, preferably, a heating unit is further provided:
the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the heating unit is installed between the sewage pipe and the water inlet of the oxidizing canceller; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the salt separating unit; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentration device c; or the heating unit is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit; or the heating unit is installed between the sewage pipe and the water inlet of the oxidizing canceller; or the heating unit is arranged between the sewage pipeline and the water inlet of the salt separating unit;
Or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the heating unit is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the oxidizing eliminator; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the salt separating unit; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentrating device c, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the concentrating device c; or the heating unit is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the salt separating unit; or the heating unit is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the oxidizing eliminator; or the heating unit is arranged between the sewage pipeline and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the salt separating unit;
Or a buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the water outlet of the oxidizing eliminator and the water inlet of the salt separating unit; or the buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentration device c; or the buffer tank III is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the salt separating unit, and the heating unit is used for heating the buffer tank III;
or a buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion type electrodialysis device, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion type electrodialysis device; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the salt separating unit; or the buffer tank III is arranged between the water outlet of the oxidizing eliminator and the water inlet of the concentrating device c, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the concentrating device c; or the buffer tank III is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the salt separating unit; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the salt separation unit, a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the salt separation unit, and the heating unit is used for heating the buffer tank III.
Based on the above sewage treatment system, preferably, the connection order of the cooler and the decarburization tower a may be the cooler and the decarburization tower a in order of the process flow, or the decarburization tower a and the cooler in order of the process flow.
The purpose of designing the heating unit is: when the aqueous solution entering the nanofiltration membrane group contains bicarbonate, the bicarbonate is converted into carbonate and carbon dioxide through heating, the carbon dioxide can be dissipated into the air and is removed from the water (the concentration of the bicarbonate in the water is reduced at the moment), and then the carbonate converted from the bicarbonate through heating can be intercepted on the concentrated water side of the nanofiltration membrane group by utilizing the separation effect of the nanofiltration membrane group on monovalent ions and divalent ions so as to reduce the concentration of the bicarbonate at the fresh water outlet of the nanofiltration membrane group; and heating is beneficial to improving the oxidation-reduction reaction speed of the oxidizing agent and the oxidizing agent in the sewage in the oxidizing eliminator.
For example, the tail gas of terephthalic acid factory, because the organic matters in the tail gas are removed by RTO incineration method or catalytic oxidation method, the rest tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of RTO incineration method or catalytic oxidation method, sodium carbonate, sodium bicarbonate and sodium bromide mixture are obtained by using alkali as absorption liquid (sodium hydroxide is taken as an example), sodium bicarbonate can be converted into sodium carbonate and carbon dioxide by heating the solution (for example, the temperature is 50-100 ℃), the concentration of sodium bicarbonate in water is reduced (carbon dioxide also escapes into air and is removed from water), the concentration of sodium bromide in the fresh water outlet of the nanofiltration membrane group is almost unchanged after passing through the nanofiltration membrane group, but the concentration of sodium bicarbonate in the fresh water outlet of the nanofiltration membrane group is reduced because the sodium bicarbonate is converted into sodium carbonate and is intercepted on the concentrated water side of the nanofiltration membrane group, so that the ratio of sodium bromide in the fresh water of the nanofiltration membrane group is improved; further, the heating is beneficial to improving the oxidation-reduction reaction speed of the oxidizing agent (such as formic acid) and the oxidizing agent in the sewage in the oxidizing eliminator.
The purpose of designing the heating unit is: when the aqueous solution contains bicarbonate, the bicarbonate is converted into carbonate and carbon dioxide through heating, the carbon dioxide can be dissipated into the air, namely, the carbon dioxide is removed from the water (the concentration of the bicarbonate in the water is reduced), most of the solids obtained by concentrating and separating out the salt separating units of the solid are carbonate, the concentration of the bicarbonate is low (for example, the cations are sodium ions, most of the cations are sodium carbonate, and the concentration of the sodium bicarbonate is low), and the purpose of the design is to obtain sodium carbonate solids, for example, a terephthalic acid factory, and the sodium carbonate can be used as dissolved oxidation residues, and has better cobalt and manganese recovery effect than sodium bicarbonate.
Based on the sewage treatment system, preferably, the heating device is a heat exchanger, a reboiler (the reboiler and the buffer tank III form integral heating equipment), coil heating, jacket heating and the like, and the heat source can be steam, electricity and the like, or can be an aqueous solution which needs to be cooled before entering the nanofiltration membrane group.
Based on the sewage treatment system, preferably, the cooler is arranged to ensure the operation of the nanofiltration membrane group and avoid the damage to the nanofiltration membrane caused by high temperature.
Based on the above sewage treatment system, the cooler may be a heat exchanger or the like, and the cold source may be cooling water, chilled water or the like, or may be an aqueous solution that needs to be heated.
Based on the above sewage treatment system, preferably, a concentration device d is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator; or a concentration device d is arranged between the sewage pipeline and the water inlet of the salt separating unit.
Based on the above sewage treatment system, preferably, the concentrating device a, the concentrating device b, the concentrating device c, or the concentrating device d is: the device comprises a reverse osmosis concentration device, an electrodialysis concentration device or an evaporation concentration device, wherein a concentrated water outlet of the reverse osmosis concentration device is a concentrated water outlet of the concentration device a, the concentration device b, the concentration device c or the concentration device d; the concentrated water outlet of the electrodialysis concentration device is the concentrated water outlet of the concentration device a, the concentration device b, the concentration device c or the concentration device d; the concentrated water outlet of the evaporation concentration device (i.e. the concentrated water solution outlet at the bottom after concentration) is the concentrated water outlet of the concentration device a, the concentration device b, the concentration device c or the concentration device d.
Based on the above sewage treatment system, preferably, when the concentrating device a, the concentrating device b, the concentrating device c or the concentrating device d is: when the temperature of the aqueous solution is high due to a heating unit and the like before the aqueous solution enters the reverse osmosis concentration device or the electrodialysis concentration device, a cooling device is required to be designed to reduce the temperature so as to protect the reverse osmosis concentration device or the electrodialysis concentration device.
Based on the above sewage treatment system, preferably, the evaporation and concentration device is further provided with a cooler a, the concentrated water outlet of the evaporation and concentration device is firstly connected to the water inlet of the cooler a, and the cold concentrated water outlet of the cooler a is further connected to the pipeline connection point a, the pipeline mixer a, the water inlet of the neutralization tank b, the water inlet of the bipolar membrane electrodialysis device or the water inlet of the decarburization tower b.
Based on the above sewage treatment system, preferably, the fresh water outlet of the reverse osmosis concentration device discharges or performs other treatment or other utilization (can be used as deionized water); the fresh water outlet of the electrodialysis concentration device discharges or carries out other treatments or other uses; or the fresh water outlet of the electrodialysis concentration device is connected to the water inlet of the reverse osmosis concentration device, the fresh water outlet of the reverse osmosis concentration device is discharged or subjected to other treatment or other utilization (can be used as deionized water), and the concentrated water outlet of the reverse osmosis concentration device enters the electrodialysis concentration device or the bipolar membrane electrodialysis equipment for treatment; or the fresh water outlet of the electrodialysis concentration device is connected to the sewage conduit.
Based on the above sewage treatment system, preferably, the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the concentration device a or the concentration device b; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the concentration device c; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the salt separation unit; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the pipeline connection point c; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the buffer tank I; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the heating unit; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the sewage conduit; or the dilute brine outlet of the bipolar membrane electrodialysis device is directly discharged to the outside of the battery.
Because the dilute brine of the bipolar membrane electrodialysis device still contains a certain concentration of salt, the bipolar membrane electrodialysis device can be used for regenerating acid and alkali after concentration, so that more economic value is obtained, and the direct discharge waste is preferably avoided. The recovery method comprises concentrating the dilute brine of bipolar membrane electrodialysis, concentrating, and treating with bipolar membrane electrodialysis equipment; or the dilute brine of the bipolar membrane electrodialysis device is beaten into a sewage pipeline, namely, the dilute brine of the bipolar membrane electrodialysis device is mixed into the sewage pipeline again, and the mixture enters the later-stage flow path of the system again from the sewage pipeline for treatment.
Based on the above sewage treatment system, preferably, a water feeding pump and a filter are arranged between the buffer tank I and the high-pressure pump, a water outlet of the buffer tank I is connected to a water inlet of the water feeding pump, a water outlet of the water feeding pump is connected to a water inlet of the filter, and a water outlet of the filter is connected to a water inlet of the high-pressure pump.
Based on the above sewage treatment system, preferably, the filter includes ultrafiltration, microfiltration, a cartridge filter, and the like.
Based on the above sewage treatment system, preferably, the salt separation unit is a concentrated precipitation solid type salt separation unit or a solid type salt separation unit formed by adding chemicals:
the concentrated solid-separating salt separating unit comprises an evaporation device and a solid-liquid separator: in the evaporation device, the salt with relatively low solubility is concentrated continuously and then exceeds the saturated solubility to generate crystallization solid, the material outlet of the evaporation device is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the water inlet of the evaporation device is the water inlet of the salt separation unit, and the aqueous solution outlet of the solid-liquid separator is the aqueous solution outlet of the salt separation unit; for example, when the tail gas of a terephthalic acid production plant is treated by the present invention after removing organic substances (for example, RTO incineration, catalytic oxidation, etc.), the solid obtained here is mainly sodium carbonate and/or sodium bicarbonate, and the sodium bromide ratio in the obtained aqueous solution becomes high.
Or the salt separation unit for concentrating and separating out the solid comprises an evaporation device, a cooling device (for example, cooling to-10 ℃ to 80 ℃ and adopting a cooler and/or a refrigerator) and a solid-liquid separator: the material outlet of the evaporation device is connected to the inlet of the cooling device (crystallization precipitated solids are generated in the evaporation device due to the fact that the salt with relatively low solubility is concentrated and exceeds the saturated solubility of the salt after being concentrated, and/or the solubility of the salt is reduced with the reduction of temperature after being cooled), the outlet of the cooling device is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the water inlet of the evaporation device is just the water inlet of the salt separation unit, the aqueous solution outlet of the solid-liquid separator is just the aqueous solution outlet of the salt separation unit, for example, when tail gas of the terephthalic acid production device is treated by the invention, the obtained solid is mainly sodium carbonate and/or sodium bicarbonate, and the obtained aqueous solution has higher sodium bromide ratio; or the solid-liquid separator comprises a first solid-liquid separator and a second solid-liquid separator, wherein the material outlet of the evaporation device (the crystallization precipitated solid is generated in the evaporation device due to the fact that the salt with relatively low solubility is concentrated and exceeds the saturated solubility of the salt) is continuously concentrated in the evaporation device, the first solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the aqueous solution outlet of the first solid-liquid separator is connected to the inlet of the cooling device, the outlet of the cooling device is provided with an aqueous solution outlet and a solid outlet after passing through the second solid-liquid separator, the water inlet of the evaporation device is the water inlet of the salt separation unit, the aqueous solution outlet after the second solid-liquid separator is the aqueous solution outlet of the salt separation unit, for example, when the tail gas of the terephthalic acid production device is treated by the method of removing organic matters (such as RTO incineration method, catalytic oxidation method and the like), the obtained solid is mainly sodium carbonate and/or sodium bromide, and the obtained aqueous solution is high in percentage sodium bicarbonate (the second solid-liquid separator is the second solid-liquid separator);
Or the concentrated and solid separating salt separating unit comprises an evaporation device, a solid-liquid separator and a nanofiltration membrane group 'or a water inlet of a monovalent ion type purifying electrodialysis device': the evaporation device is internally concentrated, wherein salt with relatively low solubility exceeds saturated solubility to generate crystallization precipitated solid after being concentrated, a material outlet of the evaporation device is connected to an inlet of a solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the aqueous solution outlet of the solid-liquid separator is connected to a water inlet of a nanofiltration membrane group or a water inlet of a purification monovalent ion type electrodialysis device, the nanofiltration membrane group is provided with a fresh water outlet and a concentrated water outlet, the water inlet of the evaporation device is the water inlet of a salt separation unit, the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is the aqueous solution outlet of the salt separation unit, for example, the tail gas of a terephthalic acid production device is subjected to organic matter removal (such as RTO incineration method, catalytic oxidation method and the like) firstly, and when the tail gas is treated by the method, the obtained solid and the concentrated water outlet of the nanofiltration membrane group are mainly sodium carbonate and/or sodium bicarbonate, and the obtained aqueous solution have high sodium bromide ratio;
Or the salt separation unit for concentrating and separating out the solid comprises an evaporation device, a cooling device (for example, cooling to-10 ℃ to 80 ℃ and adopting a cooler and/or a refrigerator), a solid-liquid separator and a nanofiltration membrane group' or a water inlet of a monovalent ion type electrodialysis purification device: the material outlet of the evaporation device is connected to the inlet of the cooling device (the evaporation device is internally provided with a water inlet of the nanofiltration membrane group 'or a water inlet of a purified monovalent ion type electrodialysis device', the nanofiltration membrane group 'is provided with a fresh water outlet and a concentrated water outlet, the water inlet of the evaporation device is the water inlet of the salt separation unit, the fresh water outlet of the nanofiltration membrane group' or the outlet I of the purified monovalent ion type electrodialysis device 'is the water solution outlet of the salt separation unit, for example, the tail gas of the terephthalic acid production device is subjected to the treatment of the invention, such as the tail gas of the terephthalic acid production device after the organic matters are removed (e.g. RTO incineration, catalytic oxidation and the like), and the obtained solid and the obtained outlet of the nanofiltration membrane group' are mainly sodium carbonate and/or sodium bicarbonate and the obtained sodium bicarbonate are high in water ratio when the tail gas of the terephthalic acid production device is treated by the invention; or the solid-liquid separator comprises a first solid-liquid separator and a second solid-liquid separator, wherein the material outlet of the evaporation device (crystallization precipitated solid is generated in the evaporation device due to the fact that salt with relatively low solubility is concentrated and exceeds the saturated solubility of the salt) is connected to the inlet of the first solid-liquid separator, the first solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the aqueous solution outlet of the first solid-liquid separator is connected to the inlet of the cooling device, the outlet of the cooling device is provided with an aqueous solution outlet and a solid outlet after passing through the second solid-liquid separator, the aqueous solution outlet after passing through the second solid-liquid separator is connected to the water inlet of the nanofiltration membrane group ', the water inlet of the evaporation device is the water inlet of the salt separation unit, the fresh water outlet of the nanofiltration membrane group' is the aqueous solution outlet of the salt separation unit, for example, when the tail gas of the terephthalic acid production device is subjected to the incineration of organic matters (for example, the RTO method, the catalytic oxidation method is sodium bicarbonate and the solid-liquid is the sodium bicarbonate solution and the solid-liquid is obtained by the invention, and the sodium bicarbonate is the second filter membrane is the sodium bicarbonate is the main separation solution or the solid-liquid is the second filter, the invention is the sodium bicarbonate solution or the second filter is the concentrated solution or the solid-liquid is obtained by the solid-liquid separation of the sodium bicarbonate and the second filter device is the sodium bicarbonate or the solid-liquid is the solid waste water or the solid waste water is the solid waste or the solid waste water is high;
Or the salt separating unit for adding chemicals to form solid comprises a mixing tank and a solid-liquid separator, wherein the mixing tank is also provided with a chemical adding port, a water inlet and a material outlet, the material outlet of the mixing tank is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, and the aqueous solution outlet of the solid-liquid separator is the aqueous solution outlet of the salt separating unit. Adding chemicals into a mixing tank of the chemical adding and solid salt separating unit, reacting part of ions in the aqueous solution entering from a water inlet of the chemical adding and solid salt separating unit to generate insoluble salt and separating out the insoluble salt, and then carrying out solid-liquid separation by the solid-liquid separator to achieve the aim of reducing the concentration of specific types of salt in the aqueous solution, wherein specific examples are as follows: for example, when the tail gas of the terephthalic acid production device is treated by the method, calcium salt, magnesium salt, calcium hydroxide, magnesium hydroxide and the like (preferably calcium hydroxide or calcium hydroxide and sodium hydroxide) are added into a mixing tank to form calcium salt insoluble matters of carbonate and bicarbonate in the aqueous solution and separate out the calcium salt insoluble matters, the concentration of the carbonate and the bicarbonate in the aqueous solution obtained by the solid-liquid separator is greatly reduced, the proportion of sodium bromide in the aqueous solution is increased, namely the aqueous solution outlet of the solid-liquid separator is the aqueous solution outlet of the salt separation unit; the water inlet of the mixing tank is the water inlet of the salt separating unit.
Based on the above sewage treatment system, preferably, the cooling device in the salt separation unit is a jacket type cooler (including a jacket type stirring tank), a tube array heat exchanger or a cooling type OSLO crystallizer, and the cold source is cooling water or chilled water.
Based on the above sewage treatment system, preferably, the evaporation device in the salt separation unit is a falling film evaporator, a forced circulation evaporator or a forced circulation evaporation crystallizer, an evaporation type OSLO crystallizer, and the most important difficulty of the falling film evaporator, the forced circulation evaporator or the forced circulation evaporation crystallizer, the evaporation type OSLO crystallizer is that the problem of blockage caused by salt precipitation, and in order to overcome the problem, a high flow rate, for example, a high flow rate of about 1.5-3 m/s is preferably controlled in a tube array.
Based on the above sewage treatment system, it is preferable that the cooling device in the salt separation unit is to control a high flow rate, for example, a high flow rate of about 1.5 to 3m/s, in the column tube of the reboiler in order to solve the clogging problem.
Based on the above sewage treatment system, it is preferable that the crystallizer is to control a high flow rate, for example, a high flow rate of about 1.5 to 3m/s, in the column tube of the reboiler in order to solve the clogging problem.
Based on the above sewage treatment system, preferably, the cooling device in the salt separation unit is a jacket cooler (comprising a jacket stirring tank), and the most important difficulty is that the problem of blockage and wall formation caused by salt precipitation is solved, and in order to overcome the problem, a scraper is preferably designed at a proper stirring line speed and/or on the inner wall of the stirring tank.
Based on the above sewage treatment system, it is preferable that the cooling device in the salt separation unit is in the form of a tube-in-tube heat exchanger or a cooler such as a cooled OSLO crystallizer, and the most important difficulty is in blocking caused by precipitation of salt, and to overcome this problem, it is preferable to control a high flow rate in the tube-in-tube, for example, about 3m/s.
Based on the sewage treatment system, preferably, the concentrated and solid-separated salt separating unit is further provided with an acid adding unit II, and an outlet of the acid adding unit II is connected to an inlet of the evaporation device; or the outlet of the acid adding unit II is connected to a pipeline between the material outlet of the evaporation device and the inlet of the solid-liquid separator; or the outlet of the acid adding unit II is connected to a pipeline between the material outlet of the evaporation device and the inlet of the cooling device; or the outlet of the acid adding unit II is connected to a pipeline between the outlet of the cooling device and the inlet of the solid-liquid separator; or two solid-liquid separators are arranged, wherein the water solution outlet of one solid-liquid separator is connected to the inlet of the other solid-liquid separator, and the outlet of the acid adding unit II is connected to a pipeline between the water solution outlet of one solid-liquid separator and the inlet of the other solid-liquid separator; or the outlet of the acid adding unit II is connected to the water inlet of the concentrating device c, and the purpose of the acid adding unit II is to convert carbonate into bicarbonate (for example, controlling pH=6-10, optimally 8.3), because the solubility of sodium bicarbonate is far smaller than that of sodium carbonate, the conversion into sodium bicarbonate is more beneficial to concentrating and crystallizing, and the inlet of the acid adding unit II is connected to an acid tank or an acid pipeline, an acid producing tank of the bipolar membrane electrodialysis device or a gas pipeline containing carbon dioxide (the carbon dioxide reacts with the sodium carbonate to form the sodium bicarbonate).
Based on the above sewage treatment system, preferably, the acid added by the acid adding unit II is hydrobromic acid, acetic acid or carbonic acid (including carbon dioxide-containing gas, and the reaction of carbon dioxide and carbonic acid radical can generate bicarbonate radical);
an inlet of the acid adding unit II is connected to an acid tank or an acid production tank of the bipolar membrane electrodialysis device, and a conveying power pump or an acid production recycling pump of the bipolar membrane electrodialysis device is used as conveying power;
the inlet of the acid adding unit II is connected to an acid pipeline or a gas pipeline containing carbon dioxide, and the self-pressure of the acid pipeline or the gas pipeline containing carbon dioxide is used as conveying power;
based on the above sewage treatment system, preferably,
the acid tank or the acid producing tank of the bipolar membrane electrodialysis equipment is connected to the inlet of the acid adding unit II, the pH value of the aqueous solution after acid addition is automatically monitored, the quantity of variable frequency discharge quantity of the conveying power pump or the acid producing recycling pump of the bipolar membrane electrodialysis equipment is controlled in a chain manner, or the reflux quantity of the conveying power pump or the acid producing recycling pump of the bipolar membrane electrodialysis equipment is controlled, and finally the aim of automatically adjusting the acid adding quantity by using the pH value is achieved, so that the pH value of the aqueous solution after acid addition is stably controlled;
And the pH value of the aqueous solution after acid addition is controlled by automatically monitoring and controlling a control valve on the acid pipeline or the gas pipeline containing carbon dioxide in a linkage manner so as to control the amount of the acid addition, thereby stably controlling the pH value of the aqueous solution after acid addition.
Based on the sewage treatment system, preferably, the concentrated and solid-separated salt separation unit is further provided with an alkali adding unit II, and the outlet of the alkali adding unit II is connected to a pipeline between the water solution outlet of the solid-liquid separator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the outlet of the alkali adding unit II is connected with the water solution outlet of the solid-liquid separator through a pipeline mixer to a pipeline between the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the water solution outlet of the solid-liquid separator is connected to the water inlet of a middle tank, the water outlet of the middle tank is connected to the water inlet of the nanofiltration membrane group ' or the water inlet of the purification monovalent ion electrodialysis device ', the outlet of the alkali adding unit II is connected to the water inlet of the middle tank, the purpose of adding alkali to the front section of the nanofiltration membrane group ' or the purification monovalent ion electrodialysis device ' is to convert the residual bicarbonate in the water solution into carbonate, the function of the nanofiltration membrane group ' or the purification monovalent ion electrodialysis device ' is facilitated, the concentration of the bicarbonate in the fresh water outlet of the nanofiltration membrane group ' is reduced, and the obtained sodium bromide in the fresh water outlet of the nanofiltration membrane group ' has lower bicarbonate content (bicarbonate is converted into carbonate due to alkali addition and is intercepted on the concentrated water side of the nanofiltration membrane group ');
Based on the above sewage treatment system, preferably, the inlet of the alkali adding unit II is connected to an alkali tank or an alkali pipeline or an alkali producing tank of the bipolar membrane electrodialysis device;
the inlet of the alkali adding unit II is connected to an alkali tank or an alkali producing tank of the bipolar membrane electrodialysis device, and a conveying power pump or an alkali producing recycling pump of the bipolar membrane electrodialysis device is used as conveying power;
the inlet of the alkali adding unit II is connected to an alkali pipeline, and the self-pressure of the alkali pipeline is used as conveying power;
based on the above sewage treatment system, preferably,
the method comprises the steps of connecting an alkali tank or an alkali producing tank of bipolar membrane electrodialysis equipment to an inlet of an alkali adding unit II, automatically monitoring the pH value of an aqueous solution after alkali addition, and controlling the quantity of variable frequency discharge quantity of the conveying power pump or an alkali producing recycling pump of the bipolar membrane electrodialysis equipment or the quantity of reflux quantity of the conveying power pump or the alkali producing recycling pump of the bipolar membrane electrodialysis equipment in a chain manner, wherein the final purpose is to automatically control the quantity of alkali addition by the pH value so as to stably control the pH value of the aqueous solution after alkali addition;
and the control valve on the alkali pipeline is used for controlling the quantity of the alkali addition by automatically monitoring and controlling the pH value of the aqueous solution after the alkali addition in a chain manner so as to stably control the pH value of the aqueous solution after the alkali addition.
Based on the above sewage treatment system, preferably, the chemical added by the chemical adding forming solid salt separating unit comprises at least one of calcium salt, magnesium salt, calcium hydroxide, magnesium hydroxide, or a mixture of at least one of the calcium salt, magnesium salt, calcium hydroxide, magnesium hydroxide and sodium hydroxide or potassium hydroxide, and the purpose of adding hydroxide is to facilitate the conversion of bicarbonate into carbonate.
Based on the above sewage treatment system, preferably, when the salt separation unit is a chemical addition-forming solid-type salt separation unit, the position of the concentration device c is interchanged with the position of the chemical addition-forming solid-type salt separation unit, specifically: the water solution outlet of the chemical adding and forming solid salt separating unit is connected to the water inlet of the concentrating device c, and the concentrated water outlet of the concentrating device c is connected to the water inlet of the bipolar membrane electrodialysis device, the pipeline connection point a or the water inlet of the neutralization tank b. The calcium salt and the like are added into the aqueous solution to precipitate insoluble substances such as carbonate, bicarbonate and the like, and the aqueous solution after solid-liquid separation is concentrated.
Based on the above sewage treatment system, preferably, the solid-liquid separator includes: sedimentation tank, positive pressure filter, centrifuge, negative pressure suction filter, gravity filter.
Based on the sewage treatment system, preferably, the nanofiltration membrane group and the nanofiltration membrane group' comprise a high-pressure pump in front of the nanofiltration membrane group and a nanofiltration membrane shell, and the nanofiltration membrane shell is internally provided with the nanofiltration membrane.
Based on the above sewage treatment system, it is preferable that water should be added to dilute at the water inlet of the nanofiltration membrane set 'in order to avoid precipitation of salt concentration (bicarbonate and/or carbonate) on the concentrated water side of the nanofiltration membrane set' too high.
Based on the above sewage treatment system, preferably, the outlet I of the alkali producing tank of the bipolar membrane electrodialysis device is connected to the sewage pipeline or the inlet of the alkali adding unit I or the alkali adding unit II, and the outlet II of the alkali producing tank of the bipolar membrane electrodialysis device is a product alkali recovery outlet.
Based on the above sewage treatment system, preferably, the outlet I of the acid producing tank of the bipolar membrane electrodialysis device is connected to the inlet of the neutralization tank b or the inlet of the acid adding unit II, and the outlet II of the acid producing tank of the bipolar membrane electrodialysis device is a product acid recovery outlet.
Based on the above treatment system, preferably, the acid generating tank of the bipolar membrane electrodialysis device is provided with a heating device (for example, heating to a boiling point temperature of 20 ℃ below the hydrobromic acid concentration) and/or a blowing device, when a small amount of chlorine element is in the water solution discharged from the sewage pipeline, the chlorine element is also accompanied with bromine element to be finally treated by the bipolar membrane electrodialysis device, and the obtained hydrobromic acid is mixed with low-concentration hydrogen chloride, which is more volatile than hydrogen bromide, so that the hydrogen chloride can be discharged into a gas phase through the heating device and/or the blowing device, the concentration of hydrogen chloride impurities in the hydrobromic acid in a liquid phase is reduced, and the hydrobromic acid in the liquid phase is purer;
Based on the above treatment system, preferably, the acid-producing tank of the bipolar membrane electrodialysis device is discharged to a chlorine removal tank (i.e. final HBr product recovery), the chlorine removal tank is provided with a heating device (for example, heating to a boiling point temperature of 20 ℃ to the hydrobromic acid concentration) and/or a blowing device, when a small amount of chlorine element is in the aqueous solution discharged from the sewage pipeline, the chlorine element is also accompanied by bromine element to be finally treated by the bipolar membrane electrodialysis device, the obtained hydrobromic acid is mixed with low-concentration hydrogen chloride, the hydrogen chloride is more volatile than hydrogen bromide, so that the hydrogen chloride can be discharged into a gas phase through the heating device and/or the blowing device, the concentration of hydrogen chloride impurities in the hydrobromic acid in a liquid phase is reduced, and the hydrobromic acid in the liquid phase is purer.
Based on the sewage treatment system, preferably, the nanofiltration membrane group' or reverse osmosis is adopted, and the produced water in operation is fresh water or concentrated water; part of the concentrated water can be recycled to the inlet water of the corresponding high-pressure pump to increase the cross-flow velocity of the nanofiltration membrane or the reverse osmosis membrane, and part of the concentrated water is discharged from the nanofiltration membrane group, the nanofiltration membrane group' or the reverse osmosis membrane.
Based on the above treatment system, preferably, a nanofiltration membrane group I or a purified monovalent ion electrodialysis device I is further provided, wherein the water outlet of the oxidizing eliminator is connected to the water inlet of the nanofiltration membrane group I or the water inlet of the purified monovalent ion electrodialysis device I, and the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purified monovalent ion electrodialysis device I is connected to the pipeline connection point a; or the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purification monovalent ion electrodialysis device I is connected to the water inlet of the neutralization tank b; or the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purification monovalent ion electrodialysis device I is connected to the water inlet of the heating unit; or the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purification monovalent ion electrodialysis device I is connected to the water inlet of the bipolar membrane electrodialysis device; or the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purification monovalent ion electrodialysis device I is connected to the water inlet of the crystallizer.
Based on the above treatment system, it is preferable that an alkali adding unit iii or a heating unit is further provided, an outlet of the alkali adding unit iii being connected to the oxidizing eliminator; or the outlet of the alkali adding unit III is connected to a pipeline between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group I or the water inlet of the purification monovalent ion electrodialysis device I, and the pipeline is called pipeline connection d; or the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank I, the water outlet of the neutralization tank I is connected to the water inlet of the nanofiltration membrane group I or the water inlet of the purification monovalent ion electrodialysis device I, and the outlet of the alkali adding unit III is connected to the neutralization tank I; or the water outlet of the oxidability eliminator is connected to the water inlet of the heating unit, and the water outlet of the heating unit is connected to the water inlet of the nanofiltration membrane group I or the water inlet of the purification monovalent ion electrodialysis device I.
Based on the above treatment system, preferably, the outlet of the alkali adding unit iv is connected to a pipeline between the fresh water outlet of the nanofiltration membrane group and the water inlet of the crystallizer, or the outlet of the alkali adding unit iv is connected to a pipeline between the concentrated water outlet of the nanofiltration membrane group and the water inlet of the crystallizer, or the outlet of the alkali adding unit iv is connected to a pipeline between the outlet i of the purification monovalent ion electrodialysis device and the water inlet of the crystallizer, or the outlet of the alkali adding unit iv is connected to a pipeline between the outlet ii of the purification monovalent ion electrodialysis device and the water inlet of the crystallizer, or the outlet of the alkali adding unit iv is connected to a pipeline between the pipeline connection point a and the water inlet of the crystallizer, or the outlet of the alkali adding unit iv is connected to a pipeline between the water outlet of the neutralization tank b and the water inlet of the crystallizer, or the pipeline between the outlet of the alkali adding unit iv is connected to the water inlet of the crystallizer, or the pipeline between the outlet of the alkali adding unit iv is called as the water inlet of the decarbonization tower;
Or fresh water outlet of the nanofiltration membrane group is connected with the water inlet of the crystallizer, concentrated water outlet of the nanofiltration membrane group is connected with the water inlet of the crystallizer, outlet I of the purification monovalent ion type electrodialysis device is connected with the water inlet of the crystallizer, outlet II of the purification monovalent ion type electrodialysis device is connected with the water inlet of the crystallizer, pipeline connection point a is connected with the water inlet of the crystallizer, water outlet of the neutralization tank b is connected with the water inlet of the crystallizer, water outlet of the heating unit is connected with the water inlet of the crystallizer, concentrated water outlet of the concentration device a is connected with the water inlet of the crystallizer or water outlet of the decarburization tower b is connected with the water inlet of the crystallizer, and a neutralization tank c is further arranged between the outlet II of the purification monovalent ion type electrodialysis device and the water inlet of the crystallizer, and the outlet of the alkali adding unit IV is connected with the neutralization tank c.
Based on the above processing system, preferably, an organic matter elimination device is further provided:
the organic matter elimination device is arranged between the sewage pipeline and the pipeline connection point c, between the sewage pipeline and the water inlet of the buffer tank I, between the sewage pipeline and the water inlet of the heating unit, between the sewage pipeline and the water inlet of the oxidizing eliminator, between the pipeline connection point c and the water inlet of the oxidizing eliminator, between the water outlet of the buffer tank I and the water inlet of the oxidizing eliminator, between the water outlet of the heating unit and the water inlet of the oxidizing eliminator, between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration unit, between the water outlet of the oxidizing eliminator and the water inlet of the purification monovalent ion type ion exchange unit, between the water outlet of the oxidizing eliminator and the water inlet of the buffer tank I, between the water outlet of the oxidizing eliminator and the water inlet of the heating unit, between the pipeline connection point c and the water inlet of the nanofiltration membrane group, between the monovalent pipeline connection point c and the water inlet of the electrodialysis unit, between the purification unit and the water inlet of the purification unit, between the purification unit and the fresh water inlet of the purification unit, between the purification unit and the water inlet of the purification unit Or between the fresh water outlet of the nanofiltration unit and the water inlet of the crystallizer, or between the outlet I of the purified monovalent ion electrodialysis unit and the water inlet of the bipolar membrane electrodialysis unit, or between the outlet I of the purified monovalent ion electrodialysis unit and the water inlet of the crystallizer, or between the conduit connection point a, or between the outlet I of the purified monovalent ion electrodialysis unit and the conduit connection point a, or between the outlet I of the nanofiltration unit and the neutralization tank b, or between the outlet I of the purified monovalent ion electrodialysis unit and the neutralization tank b, or between the outlet I of the nanofiltration unit and the water inlet of the heating unit, or between the conduit connection point a and the water inlet of the bipolar membrane electrodialysis unit, or between the conduit connection point a and the water inlet of the crystallizer, or between the inlet of the electrodialysis unit, between the outlet I of the purified monovalent ion electrodialysis unit and the water inlet of the heating unit, between the concentration device a and the concentration device, or between the concentration device a and the water inlet of the heating unit, or between the concentration device a and the water inlet of the concentration device, or between the concentrate outlet of the concentrating device a to the water inlet of the heating unit, or between the pipe connection point a to the water inlet of the concentrating device a, or between the neutralization tank b to the water inlet of the concentrating device a, or between the concentrate outlet of the concentrating device a to the water inlet of the bipolar membrane electrodialysis device, or between the concentrate outlet of the concentrating device a to the crystallizer, or between the pipe connection point a to the water inlet of the decarbonating tower b, or between the neutralization tank b to the water inlet of the decarbonating tower b, or between the water outlet of the heating device to the water inlet of the decarbonating tower b, or between the water outlet of the decarbonating tower b to the water inlet of the concentrating device a, or between the concentrate outlet of the concentrating device a to the water inlet of the decarbonating tower b, or between the water outlet of the bipolar membrane electrodialysis device to the crystallizer, or between the water outlet of the oxidating tower b to the water inlet of the water separator, or between the water outlet of the concentrating device c to the water inlet of the concentrating device c, or between the water inlet of the concentrating device c to the water inlet of the concentrating device c, or between the water outlet of the buffer unit, or between the water inlet of the concentrating device c to the concentrating device c and the water inlet of the concentrating device, or between the concentrated water outlet of the concentrating device c and the water inlet of the buffer tank I, or between the concentrated water outlet of the concentrating device c and the water inlet of the heating unit, or between the pipeline connection point c and the water inlet of the salt separating unit, or between the water outlet of the buffer tank I and the water inlet of the salt separating unit, or between the water outlet of the heating unit and the water inlet of the salt separating unit, or between the water outlet of the salt separating unit and the water inlet of the bipolar membrane electrodialysis device, or between the water outlet of the salt separating unit and the water inlet of the crystallizer, or between the water outlet of the salt separating unit and the pipeline connection point a, or between the water outlet of the salt separating unit and the water inlet of the neutralization tank b, or between the water outlet of the salt separating unit and the water inlet of the heating unit or between the sewage pipeline and the water inlet of the salt separating unit, or between the pipeline connection point c and the water inlet of the salt separating unit, or between the water outlet of the buffer tank I and the water inlet of the salt separating unit, or between the water outlet of the heating unit and the water inlet of the salt separating unit, or between the water outlet of the salt separating unit and the water inlet of the oxidizing suppressor, or between the water outlet of the oxidizing suppressor and the pipeline connection point a, or between the water outlet of the oxidizing suppressor and the water inlet of the neutralization tank b, or between the water outlet of the oxidizing suppressor and the water inlet of the heating unit, or between the water outlet of the oxidizing suppressor and the water inlet of the nanofiltration membrane group I, or between the water outlet of the oxidizing suppressor and the water inlet of the purifying monovalent ion type electrodialysis device I, or between the water outlet of the oxidative suppressor to the pipe connection point d, or between the water outlet of the oxidative suppressor to the water inlet of the neutralization tank I, or between the water outlet of the oxidative suppressor to the water inlet of the heating unit, or between the pipe connection point d to the water inlet of the nanofiltration membrane group I, or between the pipe connection point d to the water inlet of the purification monovalent ion electrodialysis device I, or between the water outlet of the neutralization tank I to the water inlet of the nanofiltration membrane group I, or between the water outlet of the neutralization tank I to the water inlet of the purification monovalent ion electrodialysis device I, or between the water outlet of the heating unit to the water inlet of the nanofiltration membrane group I, or between the fresh water outlet of the heating unit to the water inlet of the purification monovalent ion electrodialysis device I, or between the fresh water outlet of the nanofiltration membrane group I to the water inlet of the bipolar electrodialysis device I, or between the fresh water outlet of the purification monovalent ion electrodialysis device I to the water inlet of the purification tank b, or between the water outlet of the purification monovalent ion electrodialysis device I to the water inlet of the purification unit a, or between the fresh water outlet of the purification monovalent ion electrodialysis device I to the water inlet of the purification unit b, or between the fresh water outlet of the purification monovalent ion electrodialysis device I to the water inlet of the purification monovalent ion filtration membrane group I Or between the outlet I of the purified monovalent ion electrodialysis device I and the water inlet of the pipeline connection point a, or between the outlet I of the purified monovalent ion electrodialysis device I and the water inlet of the heating unit, or between the fresh water outlet of the nanofiltration membrane group and the water inlet of the middle and tank c, or between the pipeline connection point a and the water inlet of the middle and tank c, or between the water outlet of the middle and tank b and the pipeline connection point e, or between the water outlet of the heating unit and the pipeline connection point e, or between the concentrated water outlet of the concentrating device a and the pipeline connection point e, or between the water outlet of the decarbonization tower b and the water inlet of the pipeline connection point e, or between the fresh water outlet of the nanofiltration membrane group and the water inlet of the middle and tank c, or between the outlet I of the purified monovalent ion electrodialysis device and the water inlet of the middle and tank c, or between the pipeline connection point a and the water inlet of the middle and tank c, or between the concentrated water outlet of the middle and tank b and the water inlet of the crystallizer, or between the water inlet of the middle and tank c and the water inlet of the middle and the water inlet of the water separator, or between the concentrating device a and the water inlet of the middle and tank c, or between the water inlet of the concentrating device b and the water inlet of the water separator and the water inlet of the middle and the water separator, or the water solution outlet of the solid-liquid separator is connected with the water inlet of the nanofiltration membrane group 'or the water solution outlet of the solid-liquid separator is connected with the water inlet of the purification monovalent ion electrodialysis device';
Or the oxidizing eliminator is the organic matter eliminating device, namely the oxidizing eliminator is used as the organic matter eliminating device, and the organic matter is eliminated in the oxidizing eliminator.
Based on the above processing system, preferably, the organic matter elimination apparatus includes: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
When the organic matter elimination device is combined by two or more of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank, an electrodialysis device, an incineration device and an incineration residue dissolution tank, a water outlet of the former is connected to a water inlet of the latter, for example, a water outlet of the extraction device is connected to a water inlet of the acidification device.
Based on the above technical scheme, preferably, the extraction device:
comprises an extraction tank, wherein the extraction tank is provided with an extractant inlet, a water outlet and an extractant discharge outlet (the water outlet of the extraction tank is the water outlet of the extraction device); or comprises an extraction tank and a separation tank, wherein the extraction tank is provided with an extractant inlet, an extractant inlet and an extractant outlet, the separation tank of the extraction equipment is provided with an inlet, an outlet and an extractant discharge outlet, the outlet of the extraction tank is connected to the inlet of the separation tank (the outlet of the separation tank is the outlet of the extraction device), that is, after the extraction in the extraction tank is finished, the extraction tank is fed into the separation tank to be layered up and down, and then separation is carried out;
The extraction requires the addition of an extractant.
Based on the recovery system, preferably, the extractant is used for extracting the organic matters in the aqueous solution, so that the content of the organic matters in the aqueous solution is reduced, namely the COD content is reduced.
Based on the above technical solution, preferably, the advanced oxidation device:
comprises a high-grade oxidation reactor, wherein the high-grade oxidation reactor is provided with a precipitation overflow port or a water outlet, and a filter screen is arranged on the precipitation overflow port or the water outlet (the precipitation overflow port or the water outlet is the water outlet of the high-grade oxidation equipment);
or comprises a high-grade oxidation reactor, a filter VIII or a sedimentation tank, wherein the high-grade oxidation reactor is provided with a water inlet and a water outlet, the water outlet of the high-grade oxidation reactor is connected with the water inlet of the filter VIII or the water inlet of the sedimentation tank, and the filter VIII or the sedimentation tank is provided with a water outlet (the water outlet of the filter VIII or the water outlet of the sedimentation tank is the water outlet of the high-grade oxidation equipment);
the advanced oxidation reactor is an oxidation reaction (under the condition of adding the medicament required by the advanced oxidation reaction) which is used for decomposing organic matters and reduces the content of the organic matters and the COD value, and the advanced oxidation reaction comprises Fenton reaction, fenton-like reaction and other advanced oxidation reaction and other principles.
Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the advanced oxidation reactor is provided with a dosing port for adding a medicament required by the advanced oxidation reactor.
Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for a solid mixture, the agent required by the advanced oxidation reactor has an oxidizing agent.
Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the oxidant needed by the advanced oxidation reactor is preferably ferrous bromide and hydrogen peroxide.
Based on the above technical scheme, preferably, when the purification and reuse system is the purification and reuse system for solid mixture, the oxidant required by the advanced oxidation reactor is preferably ferrous bromide, hydrogen peroxide, and acid (such as hydrobromic acid or acetic acid) is also required.
Based on the above technical solution, preferably, the advanced oxidation device: comprises an ozone oxidation reactor, an ultraviolet oxidation reactor, an electrocatalytic oxidation reactor and the like.
Based on the above technical scheme, preferably, the biochemical treatment device can be mixed with other water sources to perform biochemical treatment, namely, the water sources on the route of the utility model are mixed with other water sources to perform biochemical treatment.
Based on the above technical solution, preferably, the biochemical treatment device:
comprises at least one of an anaerobic biochemical treatment device, an anoxic biochemical treatment device and an oxygen consumption biochemical treatment device, and reduces COD by using a biochemical sludge method, namely decomposing organic matters in water by using the activity of the biochemical sludge, and reducing COD.
Based on the above technical scheme, preferably, the organic matter elimination device is a resin tank:
the resin tank is filled with resin with adsorption effect on organic matters and is used for adsorbing the organic matters.
Based on the above technical scheme, preferably, the resin having adsorption effect on organic matters is regenerated by a regeneration liquid after being saturated in adsorption.
Based on the above technical scheme, preferably, the regeneration liquid is, for example, alkali liquor or the like.
Based on the above technical scheme, preferably, the organic matter elimination device is an electrodialysis device:
the electrodialysis equipment is in operation, organic molecules are not affected by charges and cannot enter the concentrated water side of the electrodialysis; the organic ions are influenced by charges and enter the concentrated water side of the electrodialysis, but the migration speed of the organic ions is obviously slower than that of the inorganic ions, so that the quantity of the organic ions entering the concentrated water side of the electrodialysis is small, the concentrated water side of the electrodialysis is mainly inorganic ions, and the effect of separating the organic matters is achieved (organic molecules and/or ions are still mainly in a water inlet chamber of the electrodialysis device and finally discharged).
Based on the above technical scheme, preferably, the organic matter elimination device is the organic matter incineration device and an incineration residue dissolving tank:
the organic matter incineration equipment such as an incinerator or RTO (real time organic matter) is used for eliminating the organic matter by incineration, the residual incineration residues are mainly inorganic salt ions, and then the organic matter is removed through the incineration residues are dissolved into solution by adding a solvent (such as water) into the incineration residues dissolving tank.
Based on the above sewage treatment system, preferably, a hardness removal device is provided:
when the water solution discharged by the sewage pipeline contains hardness, a hardness removing device is also arranged, and the hardness removing device is arranged at any position between the sewage pipeline and the water inlet of the nanofiltration membrane group, so that the hardness removing device is arranged to avoid scaling and blocking caused by hardness on the concentrated water side of the nanofiltration membrane group; specific examples are:
when the sewage pipeline is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion type electrodialysis device, the hardness removal device is arranged in the following manner: a hardness removal device is arranged between the sewage pipeline and a water inlet of the nanofiltration membrane group or a water inlet of the purification monovalent ion electrodialysis device;
Or when the sewage pipeline is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion type electrodialysis device through the high pressure pump, the hardness removal device is arranged in the following manner: a hardness removing device is arranged between the sewage pipeline and the high-pressure pump; or a hardness removing device is arranged between the high-pressure pump and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device;
or when the sewage pipeline is connected to the water inlet of the buffer tank I, and the water outlet of the buffer tank I is connected to the water inlet of the nanofiltration membrane group through the high-pressure pump, the hardness removing device is arranged in the following manner: a hardness removing device is arranged between the sewage pipeline and the buffer tank I; a hardness removing device is arranged on a pipeline between the water outlet of the buffer tank I and the high-pressure pump; or a hardness removing device is arranged on a pipeline between the high-pressure pump and the water inlet of the nanofiltration membrane group.
Or when the sewage pipeline is connected to the water inlet of the buffer tank I, and the water outlet of the buffer tank I is connected to the water inlet of the purifying monovalent ion type electrodialysis device through a pump, the hardness removing device is arranged in the following way: a hardness removing device is arranged between the sewage pipeline and the buffer tank I; a hardness removing device is arranged on a pipeline between a water outlet of the buffer tank I and the pump; or a hardness removing device is arranged on a pipeline between the pump and the water inlet of the purifying monovalent ion type electrodialysis device.
Or the hardness removing device is arranged at any position between the sewage pipeline and the water inlet of the salt separating unit; or the hardness removing device is arranged at any position between the water solution outlet of the salt separating unit and the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, and if the water solution entering the bipolar membrane electrodialysis device contains some hardness, insoluble matters such as calcium hydroxide and the like can be generated in an alkali chamber of the bipolar membrane electrodialysis device to influence the operation of the bipolar membrane electrodialysis device; particularly, when the salt separation unit is a solid type salt separation unit formed by adding chemicals, the hardness is contained in the aqueous solution outlet of the solid type salt separation unit formed by adding chemicals, and in order to protect the normal operation of the bipolar membrane electrodialysis device (the hardness is removed by the water inlet of the bipolar membrane electrodialysis device, otherwise, insoluble matters such as calcium hydroxide are generated in the alkali chamber of the bipolar membrane electrodialysis device), the hardness removing device needs to be installed at any position between the aqueous solution of the solid type salt separation unit formed by adding chemicals and the water inlet of the bipolar membrane electrodialysis device; and if the aqueous solution entering the crystallizer contains hardness, the quality of the solid product (containing calcium and magnesium ion impurities) of the crystallizer is affected. Or the hardness removing device is arranged at any position between the sewage pipeline and the water inlet of the oxidizing eliminator; or the hardness removing device is arranged at any position between the water outlet of the oxidizing eliminator and the water inlet of the bipolar membrane electrodialysis equipment or the water inlet of the crystallizer.
Based on the above sewage treatment system, preferably, the hardness removal device may be a resin column, and the resin column is filled with resin of calcium and magnesium ions in water.
Based on the above sewage treatment system, preferably, the resin for removing calcium and magnesium ions in water is regenerated by salt or acid after being saturated by adsorption.
Based on the above sewage treatment system, preferably, the sewage treated by the sewage treatment system is discharged sewage (alkaline washing liquid) of the oxidation tail gas of the terephthalic acid production device after alkaline absorption; or the tail gas oxidized by the terephthalic acid production device is subjected to the treatment of organic matters removal (such as an RTO incineration method, a catalytic oxidation method and the like) and then is subjected to the alkali absorption to discharge sewage (alkali washing liquid).
Based on the above sewage treatment system, preferably, the crystallizer is further provided with a heater.
Based on the above sewage treatment system, preferably, the crystallizer is further provided with a forced circulation pump.
Based on the sewage treatment system, preferably, the crystallizer is further provided with a discharge pump.
Based on the above sewage treatment system, preferably, the crystallizer is further provided with a centrifuge, a discharge pump of the crystallizer is connected to a feed inlet of the centrifuge, and the centrifuge has a solid outlet and a filtrate outlet.
Based on the above sewage treatment system, it is preferable that a plurality of buffer tanks and/or transfer pumps, or dilution water tanks may be provided for smooth operation of the present sewage treatment system.
Based on the sewage treatment system, preferably, in order to reduce the hydraulic load (i.e. the load of the treated water amount) of each device of the system, a concentration device is designed at any position of the system, and the concentrated water outlet of the concentration device enters the next stage of process treatment to reduce the treated water amount.
Based on the above sewage treatment system, preferably, the type of the concentrating device includes a reverse osmosis concentrating device, an evaporation concentrating device, or an electrodialysis concentrating device.
Based on the above sewage treatment system, preferably, a heater is further provided between the sewage pipe and the water intake of the oxidizing canceller.
Based on the above sewage treatment system, preferably, the filtering apparatus includes at least one of a bag filter, a cartridge filter, and an ultrafiltration.
Based on the above sewage treatment system, preferably, the tank is provided with a stirrer.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the polar water chamber of the electrodialysis device for purifying monovalent ions is fed with gas, and the discharged gas from the polar water chamber is led to high-point safe discharge for diluting the hydrogen concentration in the polar water.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the electrodialysis device for purifying monovalent ions, and the polar water chamber is preferably provided with a flammable gas concentration detector or a hydrogen concentration detector.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the electrodialysis device for purifying monovalent ions, the polar water chamber is fed with a gas, preferably compressed air or compressed nitrogen.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the electrodialysis device for purifying monovalent ions, the polar water chamber is preferably sealed.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the electrodialysis device for purifying monovalent ions is supplied with gas from an acid chamber, an alkali chamber, a chamber I or a chamber II, and the discharged gas is led to high-point safe discharge.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the electrodialysis device for purifying monovalent ions, the acid compartment, the base compartment, the compartment i or the compartment ii is fed with a gas, preferably compressed air or compressed nitrogen.
Based on the above sewage treatment system, preferably, the bipolar membrane electrodialysis device, the electrodialysis device or the electrodialysis device for purifying monovalent ions, the acid compartment, the base compartment, the compartment i or the compartment ii are preferably sealed.
The following is noted: as described herein:
bipolar membrane electrodialysis apparatus (see fig. 7, 8 for details: bipolar membrane electrodialysis is a device capable of decomposing salt in source water to obtain corresponding acid and alkali (positive ions in the salt in the source water are converted into corresponding alkali, negative ions in the salt in the source water are converted into corresponding acid, for example, source water contains sodium bromide, then the converted alkali is sodium hydroxide corresponding to sodium ions, the converted acid is hydrobromic acid corresponding to bromine ions), bipolar membrane electrodialysis device has two compartments and three compartments, the two compartments are a combination of bipolar membrane + positive membrane or negative membrane, the three compartments are a combination of bipolar membrane + positive membrane + negative membrane (high transfer efficiency), the structure and operation principle of the three-compartment bipolar membrane electrodialysis device are described as follows, firstly, the bipolar membrane can convert water into hydrogen ions and hydroxyl ions, the bipolar membrane, the negative membrane and the positive membrane are orderly arranged to form a plurality of alternate membrane stacks, under the action of a direct current electric field, for all ions, cations migrate to the negative electrode and anions migrate to the positive electrode, cations in a water inlet chamber move to the negative electrode through the positive membrane and enter an alkaline chamber, anions in the water inlet chamber move to the positive electrode through the negative membrane and enter an acid chamber, so that ions in the water inlet chamber always lose, hydroxyl ions generated by the electrolysis of the bipolar membrane move to the positive electrode and enter the alkaline chamber (form alkali with the cations coming from the water inlet chamber), hydrogen ions generated by the electrolysis of the bipolar membrane move to the negative electrode and enter an acid chamber (form acid with the anions coming from the water inlet chamber), since the direct current electric field is always present, the acid concentration in the acid chamber is gradually increased, and the alkali concentration in the alkali chamber is also gradually increased. The specific principle is shown in fig. 7 and 8.
The discharge is discharged from the process route of the utility model after the treatment of the utility model, and no matter what specific treatment method is adopted after the discharge, the protection of the content of the utility model is not affected.
The purposes of different steps, units and the like designed by the utility model are different and mutually independent, each step, unit and the like can be independently applied, can be selected and combined in different sequences according to actual demands, and can be only selected and applied to a part of steps, units and the like, and the steps, the units and the like are all within the scope of the patent protection of the utility model.
Advantageous effects
The utility model aims to provide a sewage treatment system, which can realize the effect of circular economy after sewage is treated by the system, extract valuable substances from the sewage and purify the substances to obtain target products, reduce the consumption of resources in the operation of enterprises and very accord with the national macroscopic circular economy;
meanwhile, the design of the oxidizing eliminator has the effect of reducing the oxidizing property of the source sewage, otherwise, the oxidizing property can damage the subsequent nanofiltration membrane group and reverse osmosis membrane rapidly, so that the nanofiltration membrane group and the reverse osmosis membrane can be destroyed in a short time to lose the effect (the common nanofiltration membrane group and the reverse osmosis membrane require residual chlorine in water to be less than 0.1 ppm), and the oxidizing property is harmful to the membrane stack of the bipolar membrane electrodialysis device, so that the design of the oxidizing eliminator is needed to reduce the oxidizing property of the sewage.
Drawings
FIG. 1 is a schematic diagram of a sewage treatment system according to an embodiment.
FIG. 2 is a schematic diagram of a sewage treatment system according to a second embodiment.
FIG. 3 is a schematic diagram of a sewage treatment system according to a third embodiment.
FIG. 4 is a schematic diagram of a fourth embodiment of a wastewater treatment system.
FIG. 5 is a schematic diagram of a fifth sewage treatment system according to an embodiment.
FIG. 6 is a schematic diagram of a sixth sewage treatment system.
Fig. 7 is an apparatus flow diagram of a bipolar membrane electrodialysis apparatus.
Fig. 8 is a schematic diagram of a bipolar membrane electrodialysis apparatus (principle of combination of a cathode membrane, an anode membrane, a bipolar membrane and an electrode, i.e., principle of operation inside a membrane stack).
Legend:
Detailed Description
The objects treated by the sewage treatment system in all the following embodiments are: the tail gas of the terephthalic acid production device firstly passes through the tail gas (namely the tail gas after VOC removal) after removing organic matters (HPCCU by a catalytic oxidation method), and then is washed by alkali (sodium hydroxide) (a circulating washing tower, and acid washing substances and other substances of the tail gas are trapped by alkali) and then is discharged; the cooling device in the salt separating unit in all the following embodiments is a jacket cooler of one of the cooling device types; the solid-liquid separator in the salt separation unit of all the following embodiments is a centrifuge of one of the solid-liquid separator types; all acids used for adding acid are hydrobromic acid, and all bases used for adding base are sodium hydroxide.
Example 1
As shown in fig. 1, 7 and 8, a sewage treatment system mainly comprises a sewage pipeline 001, an oxidizing eliminator (tank) 003, a nanofiltration membrane group 012, a reverse osmosis membrane group i 017 and a bipolar membrane electrodialysis device 024.
The sewage pipe 001 is connected to the ultrafiltration membrane group 002, the water outlet of the ultrafiltration membrane group 002 is connected to the water inlet of the heater 011, the water outlet of the heater 011 is connected to the oxidizing eliminator (tank) 003, the reducing agent reservoir 004 is connected to the inlet of the reducing agent dosing pump 005, the outlet of the reducing agent dosing pump 005 is also connected to the oxidizing eliminator (tank) 003, the outlet of the oxidizing eliminator (tank) 003 is connected to the buffer tank I006, the alkali adding unit I037 is also connected to the buffer tank I006, the outlet of the buffer tank I006 is connected to the water feed pump I008, the outlet of the water feed pump I008 is connected to the water inlet of the cooler 009, the water outlet of the cooler 009 is connected to the water inlet of the high pressure pump I010, the water outlet of the high pressure pump I010 is connected to the nanofiltration membrane group 012, the nanofiltration membrane group 012 has the concentrate outlet 013 and the fresh water outlet 014, the fresh water outlet 014 of the nanofiltration membrane group 012 is connected to the nanofiltration water production tank 015, the concentrated water outlet 013 of the nanofiltration membrane group 012 is discharged, the outlet of the nanofiltration water production tank 015 is connected to the water inlet of the high-pressure pump II 016, the water outlet of the high-pressure pump II 016 is connected to the reverse osmosis membrane group I017, the reverse osmosis membrane group I017 has a reverse osmosis fresh water outlet 019, a reverse osmosis concentrated water outlet 018 of the reverse osmosis membrane group I017 is connected to the neutralization tank b 020, the reverse osmosis fresh water outlet 019 of the reverse osmosis membrane group I017 is discharged, the outlet of the neutralization tank b 020 is connected to the water inlet of the water supply pump II 023, the water outlet of the water supply pump II 023 is connected to the bipolar membrane electrodialysis device 024, the acid production tank 031 of the bipolar membrane electrodialysis device is connected to the inlet of the recycling pump 035 of the acid production tank, and the outlet of the recycling pump 035 of the acid production tank is connected to the neutralization tank b 020; collecting overflow 034 of acid production tank 031 of bipolar membrane electrodialysis device; the alkali producing tank 032 of the bipolar membrane electrodialysis device is connected to the inlet of the recycling pump 036 of the alkali producing tank, and the outlet of the recycling pump 036 of the alkali producing tank is connected to the buffer tank I006; the fresh brine tank 033 of the bipolar membrane electrodialysis device is connected to the water inlet of the high-pressure pump III 047, the water outlet of the high-pressure pump III 047 is connected to the water inlet of the reverse osmosis membrane group II 048, the reverse osmosis membrane group II 048 is provided with a fresh water outlet 049 and a concentrated water outlet 050, the concentrated water outlet 050 of the reverse osmosis membrane group II 048 is connected to the electrodialysis device 051, the concentrated water outlet 052 of the electrodialysis device 051 is connected to the neutralization tank b 020, and the fresh water outlet 049 of the reverse osmosis membrane group II 048 is discharged.
The sewage treatment system operates as follows:
after being discharged from a sewage pipeline 001 to an ultrafiltration membrane group 002, sewage enters an oxidizing eliminator (tank) 003 through a heater 011, a reducing agent is pumped into the oxidizing eliminator (tank) 003 from a reducing agent dosing pump 005 to be stirred and mixed for reaction, then the oxidizing eliminator (tank) 003 overflows to a buffer tank I006, alkali liquor is also added into the buffer tank I006 from an alkali adding unit I037 and stirred and mixed for reaction, after the reaction is finished, a water supply pump I008 pumps out acid generated by the bipolar membrane electrodialysis equipment through a cooler 009 and a high-pressure pump I010 to enter a nanofiltration membrane group 012, concentrated water of the nanofiltration membrane group 012 is discharged, fresh water of the nanofiltration membrane group 012 enters a nanofiltration product tank 015, aqueous solution of the nanofiltration product tank 015 enters a reverse osmosis membrane group I017 through a high-pressure pump II 016, fresh water of the reverse osmosis membrane group I017 is discharged, concentrated water of the reverse osmosis membrane group I017 enters a neutralization tank b 020, the acid generated by the bipolar membrane electrodialysis equipment 024 is treated after the acid adding reaction in the neutralization tank b 020, the acid generated by the bipolar membrane electrodialysis equipment 024 is loaded into an acid generating tank 031, and the acid generated by the bipolar membrane electrodialysis equipment is recycled through an overflow acid generating tank 031 as a bipolar acid generating part of the bipolar membrane bridge 031; the alkali in the alkali producing tank 032 of the bipolar membrane electrodialysis device 024 is pumped to the buffer tank I006 through the alkali producing tank recycling pump 036; the fresh brine tank 033 of the bipolar membrane electrodialysis device 024 is driven into the reverse osmosis membrane group II 048 through the high-pressure pump III 047, fresh water of the reverse osmosis membrane group II 048 is discharged, concentrated water of the reverse osmosis membrane group II 048 enters the electrodialysis device 051 for treatment, and a concentrated water outlet 052 of the electrodialysis device 051 enters the neutralization tank b 020.
When the system does not operate, the bipolar membrane electrodialysis equipment does not produce acid and alkali, fresh hydrobromic acid is added into the neutralization tank b 020, and residual carbonate and bicarbonate in the water body are neutralized.
Remarks: the internal construction and operation principle of the bipolar membrane electrodialysis device (remark: the internal construction flow of bipolar membrane electrodialysis in all examples is the same), the bipolar membrane electrodialysis device has two kinds of two-compartment and three-compartment, the two-compartment is a combination of bipolar membrane+cation membrane or anion membrane, the three-compartment is a combination of bipolar membrane+cation membrane+anion membrane (transfer efficiency is high), and the three-compartment bipolar membrane electrodialysis device is described as follows:
the bipolar membrane electrodialysis device 024 mainly comprises an electrode plate anode 201, an electrode plate cathode 202, a bipolar membrane 203, a cathode membrane 204, a anode membrane 205, an acid chamber 206, an inlet chamber 207, an alkali chamber 208, a polar water chamber 225, a polar water tank 209, a circulating polar water pump 210, a water inlet tank 211, a circulating water inlet water pump 212, a circulating alkali tank 213, a circulating alkali pump 214, a circulating acid tank 215, a circulating acid pump 216, an acid production tank 031, an alkali production tank 032 and a fresh brine tank 033. The outlet of the polar water tank 209 is connected to the inlet of the circulating polar water pump 210, the outlet of the circulating polar water pump 210 is connected to the inlet of the polar water chamber 225, and the outlet of the polar water chamber 225 is connected to the inlet of the polar water tank 209 to form a circulation; an outlet of the water intake tank (also called water intake tank) 211 is connected to an inlet of a circulating water intake pump (also called water intake circulating pump) 212, an outlet of the circulating water intake pump 212 is connected to an inlet of the water intake chamber 207, and an outlet of the water intake chamber 207 is connected to an inlet of the water intake tank 211 to form a circulation; the outlet of the circulating alkali tank 213 is connected to the inlet of the circulating alkali pump 214, the outlet of the circulating alkali pump 214 is connected to the inlet of the alkali chamber 208, and the outlet of the alkali chamber 208 is connected to the inlet of the circulating alkali tank 213 to form a circulation; the outlet of the recycle acid tank 215 is connected to the inlet of the recycle acid pump 216, the outlet of the recycle acid pump 216 is connected to the inlet of the acid chamber 206, and the outlet of the acid chamber 206 is connected to the inlet of the recycle acid tank 215 to constitute a cycle. The pure water pipe 217 is connected to the inlet (make-up pure water) of the recycle caustic tank 213, and the recycle caustic tank 213 overflows to the caustic production tank 032; pure water pipe 217 is connected to the inlet of recycle acid tank 215 (make-up pure water), recycle acid tank 215 overflows to acid generator tank 031; the water inlet 221 (i.e., the aqueous solution to be treated entering the bipolar membrane electrodialysis apparatus 030) is connected to the inlet make-up aqueous solution (i.e., ions are made up) of the water inlet tank 211, and the water inlet tank 211 overflows to the fresh brine tank 033.
First, bipolar membrane 203 is capable of dissociating water into hydrogen ions 223 and hydroxide ions 224, bipolar membrane 203, negative membrane 204, and positive membrane 205 are sequentially arranged to form a plurality of alternating membrane stacks, and cations 116 (cations contained in the treated salt, i.e., cations in the salt fed from water supply 221) and hydrogen ions 223 migrate toward electrode plate negative electrode 202, anions 117 (anions contained in the treated salt, i.e., anions in the salt fed from water supply 221) and hydroxide ions 224 migrate toward electrode plate positive electrode 201 under the action of a direct current electric field.
The cations 116 and hydrogen ions 223 can pass through the cation membrane 205 and cannot pass through the anion membrane 204; anions 117 and hydroxide ions 224 can pass through the negative film 204 and cannot pass through the positive film 205.
The cations 116 in the inlet chamber 207 move in the direction of the negative electrode 202 of the electrode plate through the cation membrane 205 to enter the alkali chamber 208, and the anions 117 in the inlet chamber 207 move in the direction of the positive electrode 201 of the electrode plate through the cathode membrane 204 to enter the acid chamber 206, so that the ions in the inlet chamber 207 are lost. In contrast, hydroxide ions 224 generated by electrolysis of water in the bipolar membrane 203 move toward the electrode plate positive electrode 201 to enter the alkali chamber 208 (form alkali with the cations 116 from the water inlet chamber 207), and hydrogen ions 223 generated by electrolysis of water in the bipolar membrane 203 move toward the electrode plate negative electrode 202 to enter the acid chamber 206 (form acid with the anions 117 from the water inlet chamber 207), and the direct current electric field is always present, so that the acid concentration in the acid chamber 206 is gradually increased, and the alkali concentration in the alkali chamber 208 is also gradually increased.
The water inlet chamber 207 is used for maintaining the water flow of the water inlet chamber 207 through the water inlet tank 211 and the water inlet circulating pump 212, so that the water containing ions is required to be continuously replenished from the water inlet 221 for replenishing ions of the water inlet chamber, and the water with low ion concentration is discharged to the fresh brine tank 033, so that the water inlet 221 with relatively high concentration is prevented from being directly mixed with the backwater of the water inlet circulating pump 212 (relatively low concentration), a partition plate is arranged in the water inlet chamber 211, and the fresh brine tank 033 is also led out and discharged from the backwater side of the water inlet circulating pump 212 (relatively low concentration);
the acid chamber 206 is continuously maintained by the circulating acid tank 215 and the circulating acid pump 216, and the acid concentration of the circulating acid tank 215 is continuously increased, so that the circulating acid tank 215 is kept stable in acid concentration, the circulating acid tank 215 is supplied with the purified water 217 with the controlled flow, and the purified water is overflowed to the acid generating tank 031 more than the circulating acid tank 215;
the acid chamber 208 is continuously maintained by the circulating alkali tank 213 and the circulating alkali pump 214, and the alkali concentration of the circulating alkali tank 213 is continuously increased, so that the circulating alkali tank 213 is kept stable in alkali concentration, the circulating alkali tank 213 is supplied with the purified water 217 with a controlled flow, and the purified water is supplied with a larger volume and continuously overflows to the alkali generation tank 032;
In order to ensure conductivity, water is provided between the electrode plate positive electrode 201 and the adjacent bipolar membrane 203 and between the electrode plate negative electrode 202 and the adjacent bipolar membrane 203, and the water is usually an aqueous sodium hydroxide solution and circulated by the water tank 209 and the water circulation pump 210.
Note that: the nanofiltration membrane used in all examples of the present utility model was DuPont brand FilmTec TM NF270-400/34i, electrodialysis was EX-4S-ED provided by Hangzhou blue technology Co., ltd, bipolar membrane electrodialysis was EX-4S provided by Hangzhou blue technology Co., ltd, reverse osmosis membrane was DuPont' S SW30HRLE-440i, commercially available pp cotton filter cartridges with 5um pore size were installed in the security filter, and the monovalent ion type electrodialysis device was a proprietary device provided by Baishibang water treatment environmental protection technology (Dalian) Co., and formic acid was industrial formic acid (85% concentration). The experiment was run using the system described above:
the sewage line 001 sampling analysis is as follows: ph=9.1, total bromine 1251ppm, bromide 1203ppm, bicarbonate 7531ppm, carbonate 1221ppm, orp=781 MV (indicating that ORP is a parameter used to characterize the oxidability and reducibility of a water body, and is generally automatically detected by an ORP meter, the ORP value being positive to indicate that the water body is oxidability, and the ORP being negative to indicate that the water body is reducibility, and when ORP is positive to indicate that the water body is oxidability, a larger value indicates that the oxidability is stronger).
The reducing agent storage tank 004 is filled with industrial formic acid as a reducing agent, the reducing agent dosing pump is controlled to add formic acid to the oxidizing elimination tank 003 (formic acid addition amount=500 ppm of sewage pipeline 001 flow), the buffer tank i 006 is fed with liquid alkali to control ph=11, and the buffer tank i 006 is analyzed as follows: ph=11.1, total bromine 1257ppm, bromide 1261ppm, carbonate 8772ppm, orp=110mv (equivalent orp=781 MV, oxidation is greatly reduced, residual chlorine corresponding to general ORP < 150MV is < 0.1ppm, it is safe for nanofiltration, reverse osmosis membrane, nanofiltration, reverse osmosis membrane will be oxidized and destroyed if the oxidation of the feed water is too high and will fail, so general nanofiltration, reverse osmosis membrane requires residual chlorine of feed water < 0.1ppm, this is the case);
the concentrate outlet 013 of nanofiltration membrane stack 012 was analyzed as follows: ph=11.3, bromide=232 ppm, carbonate=35323 ppm;
the fresh water outlet 014 of the nanofiltration membrane module 012 was analyzed as follows: ph=11.0, bromide=1331 ppm, 481ppm carbonate, 12ppm bicarbonate;
the neutralization tank b 020 was sampled and analyzed as follows: ph=3.2, bromide=24231 ppm;
the overflow 034 of the acid generator 031 of bipolar membrane electrodialysis apparatus 024 is sampled and analyzed as follows: bromide=91233 ppm; sodium ion=45 ppm, hydrogen ion=1.15 mol/L, and HBr (having hydrogen ion being acidic and having a bromine ion concentration of about 9%) was confirmed as a final product.
Conclusion: a sewage treatment system is constructed according to the first embodiment, and HBr can be obtained by treatment with bipolar membrane electrodialysis equipment.
Example two
As shown in fig. 2, a sewage treatment system mainly comprises a sewage pipeline 001, an oxidizing eliminator (tank) 003, a nanofiltration membrane group 012, a reverse osmosis membrane group i 017 and a crystallizer 046.
The sewage pipe 001 is connected to the ultrafiltration membrane group 002, the water outlet of the ultrafiltration membrane group 002 is connected to the water inlet of the heater 011, the water outlet of the heater 011 is connected to the oxidizing agent eliminator (tank) 003, the reducing agent storage tank 004 is connected to the inlet of the reducing agent dosing pump 005, the outlet of the reducing agent dosing pump 005 is also connected to the oxidizing agent eliminator (tank) 003, the outlet of the oxidizing agent eliminator (tank) 003 is connected to the buffer tank I006, the alkali adding unit I037 is also connected to the buffer tank I006, the outlet of the buffer tank I006 is connected to the water feed pump I008, the outlet of the water feed pump I008 is connected to the water inlet of the cooler 009, the water outlet of the cooler 009 is connected to the water inlet of the high-pressure pump I010, the water outlet of the high-pressure pump I010 is connected to the nanofiltration membrane group 012, the nanofiltration membrane group 012 has a concentrate outlet 013 and a fresh water outlet 014, the fresh water outlet 014 of the nanofiltration membrane group 012 is connected to the nanofiltration product water tank 015, the concentrated water outlet 013 of the nanofiltration membrane group 012 is discharged, the outlet of the nanofiltration water producing tank 015 is connected to the water inlet of the high-pressure pump II 016, the water outlet of the high-pressure pump II 016 is connected to the reverse osmosis membrane group I017, the reverse osmosis membrane group I017 is provided with a reverse osmosis fresh water outlet 019 and a reverse osmosis concentrated water outlet 018, the reverse osmosis concentrated water outlet 018 of the reverse osmosis membrane group I017 is connected to the neutralization tank b 020, the water outlet of the neutralization tank b 020 is connected to the water inlet of the neutralization tank c 080, the alkali adding unit IV 079 is also connected to the neutralization tank c 080, the reverse osmosis fresh water outlet 019 of the reverse osmosis membrane group I017 is discharged, the outlet of the neutralization tank c 080 is connected to the water inlet of the water feeding pump II 023, the water outlet of the water feeding pump II 023 is connected to the water inlet of the crystallizer 046, a reboiler 040 is further arranged on the crystallizer 046, the reboiler 040 is prevented from being blocked by the forced circulation pump 039, the discharge pump 041 of the crystallizer 046 is connected to the inlet of a centrifuge 042, the centrifuge 042 is provided with a centrifuge solids outlet 043, the liquid outlet of the centrifuge 042 is connected to a centrifuge filtrate tank 044, the centrifuge filtrate tank 044 is connected to the inlet of a filtrate pump 045, and the outlet of the filtrate pump 045 is connected to the inlet of the crystallizer 046.
The sewage treatment system operates as follows:
after sewage is discharged from a sewage pipeline 001 to an ultrafiltration membrane group 002, the sewage enters an oxidizing eliminator (tank) 003 through a heater 011, a reducing agent is pumped into the oxidizing eliminator (tank) 003 from a reducing agent adding pump 005 to be stirred and mixed for reaction, then the oxidizing eliminator (tank) 003 overflows to a buffer tank I006, alkali liquor is also added to the buffer tank I006 from an alkali adding unit I037 and stirred and mixed for reaction, after the reaction is finished, the sewage is pumped out through a water supply pump I008 through a cooler 009 and a high-pressure pump I010 to enter a nanofiltration membrane group 012, concentrated water of the nanofiltration membrane group 012 is discharged, fresh water of the nanofiltration membrane group 012 enters a nanofiltration product water tank 015, aqueous solution of the nanofiltration product water tank 015 enters a reverse osmosis membrane group I017 through a high-pressure pump II 016, fresh water of the reverse osmosis membrane group I017 enters a neutralization tank b 020, after the neutralization tank b 020 is subjected to acid adding reaction, the alkali is added to be neutralized in the neutralization tank c 080, the crystallization tank 046 enters a crystallizer 043, the crystallization 043 is heated and concentrated through a water supply pump I008, the discharge pump is pumped out through a discharge pump 042, and the solid material is discharged from a centrifuge 043 through a solid material outlet 043, namely the solid material is discharged from a centrifuge 043, and the solid material is discharged from the centrifuge 043.
Fresh hydrobromic acid and sodium hydroxide (firstly hydrobromic acid and then sodium hydroxide) are added into a neutralization tank b 020, the purpose of firstly adding hydrobromic acid is to remove residual carbonate and bicarbonate (the PH is reduced to about 3-4.5) in the inlet water, and the purpose of adding sodium hydroxide and adjusting the pH to be neutral is that the pH is required to be reduced to about 3-4.5 by adding hydrobromic acid before neutralizing the carbonate and the bicarbonate, at the moment, free hydrobromic acid exists in the water, and sodium hydroxide is required to be used for neutralizing the free hydrobromic acid in order to promote the purity of the finally crystallized sodium bromide.
The experiment was run using the system described above:
the sewage line 001 sampling analysis is as follows: ph=9.1, total bromine 1251ppm, bromide 1203ppm, bicarbonate 7531ppm, carbonate 1221ppm, orp=781 MV.
The reducing agent storage tank 004 is filled with industrial formic acid as a reducing agent, the reducing agent dosing pump is controlled to add formic acid to the oxidizing elimination tank 003 (formic acid addition amount=500 ppm of sewage pipeline 001 flow), the buffer tank i 006 is fed with liquid alkali to control ph=11, and the buffer tank i 006 is analyzed as follows: ph=11.1, total bromine 1257ppm, bromide 1261ppm, carbonate 8772ppm, orp=110 MV;
the concentrate outlet 013 of nanofiltration membrane stack 012 was analyzed as follows: ph=11.3, bromide=232 ppm, carbonate=35323 ppm;
The fresh water outlet 014 of the nanofiltration membrane module 012 was analyzed as follows: ph=11.0, bromide=1331 ppm, 481ppm carbonate, 12ppm bicarbonate;
immediately after the acid addition to neutralization tank b 020 was reacted to acidity, the sample was analyzed as follows: ph=3.2, bromide=24231 ppm, carbonate, bicarbonate cannot be detected;
after the neutralization tank c 080 was reacted to neutrality by adding a base, the sample was analyzed as follows: ph=6.9, bromide=22187 ppm, carbonate, bicarbonate cannot be detected;
the solids outlet 043 of centrifuge 042 was sampled and analyzed as follows: sodium bromide content 98.1% as final product.
Conclusion: constructing a sewage treatment system according to the second embodiment, and finally obtaining sodium bromide solid; it has also been demonstrated that it is feasible to produce HBr by passing through the nanofiltration treatment and then through the neutralization tank b, and finally to enter the bipolar membrane electrodialysis apparatus 024 or enter the crystallizer 046 system to obtain sodium bromide, but the selection of the final product is different, and it is also possible that the final product is HBr or sodium bromide can be selected in a folding manner according to the actual situation, i.e. the bipolar membrane electrodialysis apparatus 024 or the crystallizer 046 can be exchanged.
Example III
As shown in fig. 3, 7 and 8, a sewage treatment system mainly comprises a sewage pipe 001, an oxidizing eliminator (tank) 003, an electrodialysis device 053 for purifying monovalent ions, a reverse osmosis membrane group i 017 and a bipolar membrane electrodialysis device 024.
The sewage pipeline 001 is connected to the ultrafiltration membrane group 002, the water outlet of the ultrafiltration membrane group 002 is connected to the water inlet of the heater 011, the water outlet of the heater 011 is connected to the oxidizing eliminator (tank) 003, the reducing agent storage tank 004 is connected to the inlet of the reducing agent dosing pump 005, the outlet of the reducing agent dosing pump 005 is also connected to the oxidizing eliminator (tank) 003, the outlet of the oxidizing eliminator (tank) 003 is connected to the buffer tank I006, the alkali adding unit I037 is also connected to the buffer tank I006, the outlet of the buffer tank I006 is connected to the feed pump I008, the outlet of the feed pump I008 is connected to the water inlet of the cooler 009, the water outlet of the cooler 009 is connected to the water inlet of the monovalent ion purification electrodialysis device 053, the monovalent ion purification electrodialysis device 053 is discharged from the outlet II 054, the monovalent ion purification electrodialysis device 055 is connected to the neutralization tank b 020, the outlet of the neutralization tank b 020 is connected to the water inlet of the feed pump II 023, the water outlet of the 024 II is connected to the membrane electrodialysis device, the acid production tank 031 is connected to the acid production tank 035 of the bipolar acid recovery tank and the acid production tank is connected to the bipolar acid recovery tank 035; collecting overflow 034 of acid production tank 031 of bipolar membrane electrodialysis device; the alkali producing tank 032 of the bipolar membrane electrodialysis device is connected to the inlet of the recycling pump 036 of the alkali producing tank, and the outlet of the recycling pump 036 of the alkali producing tank is connected to the buffer tank I006; the fresh brine tank 033 of the bipolar membrane electrodialysis device is connected to the water inlet of the high-pressure pump III 047, the water outlet of the high-pressure pump III 047 is connected to the water inlet of the reverse osmosis membrane group II 048, the reverse osmosis membrane group II 048 is provided with a fresh water outlet 049 and a concentrated water outlet 050, the concentrated water outlet 050 of the reverse osmosis membrane group II 048 is connected to the electrodialysis device 051, the concentrated water outlet 052 of the electrodialysis device 051 is connected to the neutralization tank b 020, and the fresh water outlet 049 of the reverse osmosis membrane group II 048 is discharged.
The sewage treatment system operates as follows:
after being discharged from a sewage pipeline 001 to an ultrafiltration membrane assembly 002, sewage enters an oxidizing eliminator (tank) 003 through a heater 011, a reducing agent is pumped into the oxidizing eliminator (tank) 003 from a reducing agent dosing pump 005 to be stirred and mixed for reaction, then the oxidizing eliminator (tank) 003 overflows to a buffer tank I006, alkali liquor is also added into the buffer tank I006 from an alkali adding unit I037 and stirred and mixed for reaction, after the reaction is finished, a water supply pump I008 pumps out an electrodialysis device 053 for purifying monovalent ions through a cooler 009, an outlet II of the electrodialysis device 053 for purifying monovalent ions is discharged, salt mainly consisting of monovalent ions obtained from the outlet I of the electrodialysis device 053 for purifying monovalent ions enters a neutralization tank b020, acid generated by the bipolar membrane electrodialysis device 024 is pumped into an acid generating tank 031 of the bipolar membrane electrodialysis device 024 after the acid adding reaction, and the acid generating tank 031 of the bipolar membrane electrodialysis device 024 is pumped into a finished product of the acid generating tank 031 of the bipolar membrane electrodialysis device b through an overflow acid generating tank 031 of the other electrodialysis device; the alkali in the alkali producing tank 032 of the bipolar membrane electrodialysis device 024 is pumped to the buffer tank I006 through the alkali producing tank recycling pump 036; the fresh brine tank 033 of the bipolar membrane electrodialysis device 024 is driven into the reverse osmosis membrane group II 048 through the high-pressure pump III 047, fresh water of the reverse osmosis membrane group II 048 is discharged, concentrated water of the reverse osmosis membrane group II 048 enters the electrodialysis device 051 for treatment, and a concentrated water outlet 052 of the electrodialysis device 051 enters the neutralization tank b020.
When the system is not in operation, the bipolar membrane electrodialysis equipment does not produce acid and alkali, and fresh hydrobromic acid is added into the neutralization tank b 020 to neutralize carbonate and bicarbonate in the inlet water.
Remarks: the internal construction and operation principle of the bipolar membrane electrodialysis device (remark: the internal construction flow of bipolar membrane electrodialysis in all examples is the same), the bipolar membrane electrodialysis device has two kinds of two-compartment and three-compartment, the two-compartment is a combination of bipolar membrane+cation membrane or anion membrane, the three-compartment is a combination of bipolar membrane+cation membrane+anion membrane (transfer efficiency is high), and the three-compartment bipolar membrane electrodialysis device is described as follows:
the bipolar membrane electrodialysis device 030 mainly comprises an electrode plate positive electrode 201, an electrode plate negative electrode 202, a bipolar membrane 203, a cathode membrane 204, a anode membrane 205, an acid chamber 206, an inlet chamber 207, an alkali chamber 208, a polar water chamber 225, a polar water tank 209, a circulating polar water pump 210, an inlet water tank 211, a circulating inlet water pump 212, a circulating alkali tank 213, a circulating alkali pump 214, a circulating acid tank 215, a circulating acid pump 216, an acid production tank 031, an alkali production tank 032 and a fresh brine tank 033. The outlet of the polar water tank 209 is connected to the inlet of the circulating polar water pump 210, the outlet of the circulating polar water pump 210 is connected to the inlet of the polar water chamber 225, and the outlet of the polar water chamber 225 is connected to the inlet of the polar water tank 209 to form a circulation; the outlet of the water inlet tank 211 is connected to the inlet of the circulating water inlet pump 212, the outlet of the circulating water inlet pump 212 is connected to the inlet of the water inlet chamber 207, and the outlet of the water inlet chamber 207 is connected to the inlet of the water inlet tank 211 to form a circulation; the outlet of the circulating alkali tank 213 is connected to the inlet of the circulating alkali pump 214, the outlet of the circulating alkali pump 214 is connected to the inlet of the alkali chamber 208, and the outlet of the alkali chamber 208 is connected to the inlet of the circulating alkali tank 213 to form a circulation; the outlet of the recycle acid tank 215 is connected to the inlet of the recycle acid pump 216, the outlet of the recycle acid pump 216 is connected to the inlet of the acid chamber 206, and the outlet of the acid chamber 206 is connected to the inlet of the recycle acid tank 215 to constitute a cycle. The pure water pipe 217 is connected to the inlet (make-up pure water) of the recycle caustic tank 213, and the recycle caustic tank 213 overflows to the caustic production tank 032; pure water pipe 217 is connected to the inlet of recycle acid tank 215 (make-up pure water), recycle acid tank 215 overflows to acid generator tank 031; the water inlet 221 (i.e., the aqueous solution to be treated entering the bipolar membrane electrodialysis apparatus 030) is connected to the inlet make-up aqueous solution (i.e., ions are made up) of the water inlet tank 211, and the water inlet tank 211 overflows to the fresh brine tank 033.
First, the bipolar membrane 203 is capable of electrolyzing water into hydrogen ions 223 and hydroxide ions 224, and the bipolar membrane 203, the cathode membrane 204 and the anode membrane 205 are sequentially arranged to form a plurality of alternating membrane stacks, and cations 116 (cations contained in the treated salt, i.e., cations in the salt fed from the water fed 221) and hydrogen ions 223 migrate toward the negative electrode 202 of the electrode plate, and anions 117 (anions contained in the treated salt, i.e., anions in the salt fed from the water fed 221) and hydroxide ions 224 migrate toward the positive electrode 201 of the electrode plate for all ions under the action of a direct current electric field.
The cations 116 and hydrogen ions 223 can pass through the cation membrane 205 and cannot pass through the anion membrane 204; anions 117 and hydroxide ions 224 can pass through the negative film 204 and cannot pass through the positive film 205.
The cations 116 in the inlet chamber 207 move in the direction of the negative electrode 202 of the electrode plate through the cation membrane 205 to enter the alkali chamber 208, and the anions 117 in the inlet chamber 207 move in the direction of the positive electrode 201 of the electrode plate through the cathode membrane 204 to enter the acid chamber 206, so that the ions in the inlet chamber 207 are lost. In contrast, hydroxide ions 224 generated by electrolysis of water in the bipolar membrane 203 move toward the electrode plate positive electrode 201 to enter the alkali chamber 208 (form alkali with the cations 116 from the water inlet chamber 207), and hydrogen ions 223 generated by electrolysis of water in the bipolar membrane 203 move toward the electrode plate negative electrode 202 to enter the acid chamber 206 (form acid with the anions 117 from the water inlet chamber 207), and the direct current electric field is always present, so that the acid concentration in the acid chamber 206 is gradually increased, and the alkali concentration in the alkali chamber 208 is also gradually increased.
The water inlet chamber 207 is used for maintaining the water flow of the water inlet chamber 207 through the water inlet tank 211 and the water inlet circulating pump 212, so that the water containing ions is required to be continuously replenished from the water inlet 221 for replenishing ions of the water inlet chamber, and the water with low ion concentration is discharged to the fresh brine tank 033, so that the water inlet 221 with relatively high concentration is prevented from being directly mixed with the backwater of the water inlet circulating pump 212 (relatively low concentration), a partition plate is arranged in the water inlet chamber 211, and the fresh brine tank 033 is also led out and discharged from the backwater side of the water inlet circulating pump 212 (relatively low concentration);
the acid chamber 206 is continuously maintained by the circulating acid tank 215 and the circulating acid pump 216, and the acid concentration of the circulating acid tank 215 is continuously increased, so that the circulating acid tank 215 is kept stable in acid concentration, the circulating acid tank 215 is supplied with the purified water 217 with the controlled flow, and the purified water is overflowed to the acid generating tank 031 more than the circulating acid tank 215;
the acid chamber 208 is continuously maintained by the circulating alkali tank 213 and the circulating alkali pump 214, and the alkali concentration of the circulating alkali tank 213 is continuously increased, so that the circulating alkali tank 213 is kept stable in alkali concentration, the circulating alkali tank 213 is supplied with the purified water 217 with a controlled flow, and the purified water is supplied with a larger volume and continuously overflows to the alkali generation tank 032;
In order to ensure conductivity, water is provided between the electrode plate positive electrode 201 and the adjacent bipolar membrane 203 and between the electrode plate negative electrode 202 and the adjacent bipolar membrane 203, and the water is usually an aqueous sodium hydroxide solution and circulated by the water tank 209 and the water circulation pump 210.
When the system is not in operation, the bipolar membrane electrodialysis device does not produce acid or alkali, and fresh hydrobromic acid is added into the neutralization tank b 020.
The experiment was run using the system described above:
the sewage line 001 sampling analysis is as follows: ph=9.1, total bromine 1251ppm, bromide 1203ppm, bicarbonate 7531ppm, carbonate 1221ppm, orp=781 MV.
The reducing agent storage tank 004 is filled with industrial formic acid as a reducing agent, the reducing agent dosing pump is controlled to add formic acid to the oxidizing elimination tank 003 (formic acid addition amount=500 ppm of sewage pipeline 001 flow), the buffer tank i 006 is fed with liquid alkali to control ph=11, and the buffer tank i 006 is analyzed as follows: ph=11.1, total bromine 1257ppm, bromide 1261ppm, carbonate 8772ppm, orp=110 MV;
outlet i of electrodialysis device 053 for purification of monovalent ions was analyzed as follows: ph=11.3, bromide=18897 ppm, carbonate 2324ppm, bicarbonate 66ppm;
the neutralization tank b 020 was sampled and analyzed as follows: ph=3.1, bromide=22285 ppm;
The overflow 034 of the acid generator 031 of bipolar membrane electrodialysis apparatus 024 is sampled and analyzed as follows: bromide= 103014ppm; sodium ion=63 ppm, hydrogen ion=1.28 mol/L, and HBr (having hydrogen ion being acidic and having a bromide concentration of about 10%) was confirmed as a final product.
Conclusion: the sewage treatment system is constructed according to the third embodiment, HBr can be obtained by treatment with bipolar membrane electrodialysis equipment, and the effect of the nanofiltration membrane group 012 and the effect of the monovalent ion type electrodialysis equipment 053 are the same, namely monovalent sodium bromide aqueous solution is extracted from mixed aqueous solution of sodium carbonate and sodium bromide, the monovalent sodium bromide aqueous solution and the sodium carbonate aqueous solution and the monovalent sodium bromide aqueous solution can be exchanged randomly, and the selection can also be deduced that on the basis of the embodiment, the bipolar membrane electrodialysis equipment 024 is replaced by a crystallizer 046, and the final product is not HBr but sodium bromide.
Example IV
As shown in FIG. 4, a sewage treatment system mainly comprises a sewage pipeline 001, an oxidizing eliminator (tank) 003, a reverse osmosis membrane group I017, an evaporation device 056, a cooling device 060, a solid-liquid separator (centrifuge I065), a nanofiltration membrane group' 071 and a crystallizer 046.
The sewage pipe 001 is connected to the ultrafiltration membrane group 002, the water outlet of the ultrafiltration membrane group 002 is connected to the water inlet of the heater 011, the water outlet of the heater 011 is connected to the oxidizing eliminator (tank) 003, the reducing agent reservoir 004 is connected to the inlet of the reducing agent dosing pump 005, the outlet of the reducing agent dosing pump 005 is also connected to the oxidizing eliminator (tank) 003, the outlet of the oxidizing eliminator (tank) 003 is connected to the buffer tank I006, the alkali adding unit I037 is also connected to the buffer tank I006, the outlet of the buffer tank I006 is connected to the water feed pump I008, the outlet of the water feed pump I008 is connected to the water inlet of the cooler 009, the water outlet of the cooler 009 is connected to the water inlet of the high pressure pump I010, the water outlet of the high pressure pump I010 is connected to the water inlet of the reverse osmosis membrane group I017, the reverse osmosis membrane group I017 has the fresh water outlet 019 and the concentrate outlet 018, the fresh water outlet 019 of the reverse osmosis membrane group I017 is discharged, the concentrated water outlet 018 of the reverse osmosis membrane group I017 is connected to the water inlet of the evaporation plant 056, the evaporation plant 056 is further provided with a forced circulation pump I057, a reboiler I058, the discharge pump I059 of the evaporation plant 056 is connected to the water inlet of the cooling plant 060, the cooling plant 060 is further provided with a forced circulation pump II 061, a cooling heat exchanger 062 (a chilled water pipeline 064 is also connected to the shell side of the cooling heat exchanger 062), the discharge pump II 063 of the cooling plant 060 is connected to a solid-liquid separator (a centrifuge I065), the centrifuge I065 is provided with a solid outlet 066, the filtrate outlet of the centrifuge I065 is connected to an intermediate tank 067, the alkalizing plant II 069 is connected to the intermediate tank 067, the outlet of the intermediate tank 067 is connected to a high pressure pump IV 068, the outlet of the high pressure pump IV 068 is connected to the water inlet of the nanofiltration membrane group 071', and the nanofiltration membrane group 071 is provided with a fresh water outlet 3, the concentrated water outlet 072, the concentrated water outlet 072 of the nanofiltration membrane set 071 is connected to the evaporation device 056, the fresh water outlet 073 of the nanofiltration membrane set 071 is connected to the neutralization tank b 020, the acid adding device I074 is also connected to the neutralization tank b 020, the water outlet of the neutralization tank b 020 is connected to the water inlet of the neutralization tank c 080, the alkali adding unit IV 079 is also connected to the neutralization tank c 080, the outlet of the neutralization tank c 080 is connected to the water feeding pump II 23, the outlet of the water feeding pump II 23 is connected to the water inlet of the crystallizer 046, a reboiler 040 is further arranged on the crystallizer 046, the reboiler 040 is prevented from being blocked by the forced circulation pump 039, the discharging pump 041 of the crystallizer 046 is connected to the inlet of the centrifuge 042, the centrifuge 042 is provided with a solid outlet 043, the liquid outlet of the centrifuge 042 is connected to the centrifuge filtrate tank 044, the centrifuge filtrate tank 044 is connected to the inlet of the filtrate pump 045, and the outlet of the filtrate pump 045 is connected to the inlet of the crystallizer 046.
The sewage treatment system operates as follows:
sewage is discharged from a sewage pipeline 001 to an ultrafiltration membrane group 002, then enters an oxidizing eliminator (tank) 003 through a heater 011, a reducing agent is pumped into the oxidizing eliminator (tank) 003 from a reducing agent dosing pump 005 to be stirred and mixed for reaction, then the oxidizing eliminator (tank) 003 overflows to a buffer tank I006, alkali liquor is also added into the buffer tank I006 from an alkali adding unit I037 to be stirred and mixed for reaction, after the reaction is finished, a feed water pump I008 pumps fresh water which passes through a cooler 009 and a high-pressure pump I010 to enter a reverse osmosis membrane group I017, the reverse osmosis membrane group I017 is discharged, concentrated water of the reverse osmosis membrane group I017 enters an evaporation device 056 to be evaporated and concentrated, the evaporation device 056 is heated and concentrated by steam through a reboiler I058, circulation quantity is provided by a forced circulation pump I057 to avoid crystallization blockage in the reboiler I058, materials of the evaporation device 056 are pumped into a cooling device 060 through a discharge pump I059, the cooling device 060 uses chilled water provided by a chilled water pipeline 064 as a cold source, the chilled water is pumped out to a centrifugal machine I065 by a discharge pump II 063 for solid-liquid separation, the solid is sodium carbonate solid, alkali liquid provided by an alkali adding device II 069 is added into filtrate in an intermediate tank 067, the filtrate is pumped into a nanofiltration membrane group '071 for treatment by a high-pressure pump IV 068, concentrated water of the nanofiltration membrane group '071 returns to an evaporation device 056, fresh water of the nanofiltration membrane group '071 enters a neutralization tank b 020, acid is firstly added into the neutralization tank b 020 for reaction to remove carbonate and bicarbonate, alkali provided by an alkali adding unit IV 079 is added into a neutralization tank c 080 for neutralization (free HBr in the process of being acid is prepared before neutralization, so as to improve the purity of sodium carbonate), the sodium carbonate) enters a crystallizer 046, the material is pumped out by the discharge pump 041 and enters a centrifugal machine 042, the solids of centrifuge 042 are collected by draining from solids outlet 043, and the filtrate from centrifuge 042 is fed to filtrate tank 044 and returned to crystallizer 046 by filtrate pump 045, i.e. all product is discharged from solids outlet 043 of centrifuge 042 as solids.
Fresh hydrobromic acid and sodium hydroxide (firstly hydrobromic acid and then sodium hydroxide) are added into a neutralization tank b 020, the purpose of firstly adding hydrobromic acid is to remove residual carbonate and bicarbonate (the PH is reduced to about 3-4.5) in the inlet water, and the purpose of adding sodium hydroxide and adjusting the pH to be neutral is that the pH is required to be reduced to about 3-4.5 by adding hydrobromic acid before neutralizing the carbonate and the bicarbonate, at the moment, free hydrobromic acid exists in the water, and sodium hydroxide is required to be used for neutralizing the free hydrobromic acid in order to promote the purity of the finally crystallized sodium bromide.
The experiment was run using the system described above:
the sewage line 001 sampling analysis is as follows: ph=9.1, total bromine 1251ppm, bromide 1203ppm, bicarbonate 7531ppm, carbonate 1221ppm, orp=781 MV.
The reducing agent storage tank 004 is filled with industrial formic acid as a reducing agent, the reducing agent dosing pump is controlled to add formic acid to the oxidizing elimination tank 003 (formic acid addition amount=500 ppm of sewage pipeline 001 flow), the buffer tank i 006 is fed with liquid alkali to control ph=11, and the buffer tank i 006 is analyzed as follows: ph=11.1, total bromine 1257ppm, bromide 1261ppm, carbonate 8772ppm, orp=110 MV;
the concentrate outlet 018 of reverse osmosis membrane module i 017 was analyzed as follows: ph=11.3, total bromine 6033ppm, bromide 6097ppm, carbonate 43512ppm;
Control the temperature of cooling device 060 = 3 ℃, analyze solids outlet 066 of centrifuge i 065: 52 ppm of sodium carbonate and 1121ppm of bromide ions;
the ph=11 of the intermediate tank 067 was controlled, and immediately after the neutralization tank b 020 was charged with acid to be reacted to be acidic, the sample was analyzed as follows: ph=3.2, bromide=33278 ppm, carbonate, bicarbonate cannot be detected;
after the neutralization tank c 080 was reacted to neutrality by adding a base, the sample was analyzed as follows: ph=6.9, bromide= 30131ppm, carbonate, bicarbonate cannot be detected;
the solids outlet 043 of centrifuge 042 was sampled and analyzed as follows: sodium bromide content 98.4% as final product.
Conclusion: a sewage treatment system is constructed according to the fourth embodiment, and finally sodium bromide solid and sodium carbonate solid can be obtained; while example two demonstrates that crystallizer 046 is interchangeable with bipolar membrane electrodialysis apparatus 024, it can be deduced that substitution of crystallizer 046 for bipolar membrane electrodialysis apparatus 024 is feasible, except that the final product is chosen to be HBr instead of sodium bromide of this example; meanwhile, the third embodiment proves that the nanofiltration membrane group and the electrodialysis device for purifying monovalent ions are interchangeable, so that the nanofiltration membrane group 071 can be deduced to be interchangeable by the electrodialysis device for purifying monovalent ions, and the effect of extracting sodium bromide water solution from sodium carbonate and sodium bromide water solution can be achieved, namely, the nanofiltration membrane group 071 can be replaced by the electrodialysis device for purifying monovalent ions in the embodiment, and the same effect can be achieved.
Example five
As shown in FIG. 5, a sewage treatment system mainly comprises a sewage pipeline 001, an oxidizing eliminator (tank) 003, an evaporation device 056, a cooling device 060, a solid-liquid separator (a centrifugal machine I065), a nanofiltration membrane group I075 and a crystallizer 046.
The sewage pipeline 001 is connected to the ultrafiltration membrane group 002, the water outlet of the ultrafiltration membrane group 002 is connected to the water inlet of the evaporation device 056, the evaporation device 056 is also provided with a forced circulation pump I057 and a reboiler I058, the discharge pump I059 of the evaporation device 056 is connected to the water inlet of the cooling device 060, the cooling device 060 is also provided with a forced circulation pump II 061 and a cooling heat exchanger 062 (the cooling water pipeline 064 is also connected to the shell side of the cooling heat exchanger 062), the discharge pump II 063 of the cooling device 060 is connected to the solid-liquid separator (centrifuge I065), the centrifuge I065 is provided with a solid outlet 066, the filtrate outlet of the centrifuge I065 is connected to the inlet of the oxidizing eliminator (tank) 003, the reducing agent storage tank 004 is connected to the inlet of the reducing agent dosing pump 005, the outlet of the reducing agent dosing pump 005 is also connected to the oxidizing eliminator (tank) 003, the outlet of the oxidizing eliminator (tank) 003 is connected to a high-pressure pump V078, the outlet of the high-pressure pump IV 078 is connected to the water inlet of a nanofiltration membrane group I075, the nanofiltration membrane group I075 is provided with a fresh water outlet 077 and a concentrated water outlet 076, the concentrated water outlet 076 of the nanofiltration membrane group I075 is connected to an evaporation device 056, the fresh water outlet 077 of the nanofiltration membrane group I075 is connected to a neutralization tank b 020, an acid adding device I074 is also connected to the neutralization tank b 020, the water outlet of the neutralization tank b 020 is connected to the water inlet of a neutralization tank c 080, an alkali adding unit IV 079 is also connected to the neutralization tank c 080, the outlet of the neutralization tank c 080 is connected to a water feeding pump II 23, the outlet of the water feeding pump II 23 is connected to the water inlet of a crystallizer 046, a reboiler 040 is further provided on the crystallizer 046, the reboiler 040 is prevented from being blocked by a forced circulation pump 039, the discharge pump 041 of the crystallizer 046 is connected to the inlet of a centrifuge 042, the centrifuge 042 is provided with a centrifuge solids outlet 043, the liquid outlet of the centrifuge 042 is connected to a centrifuge filtrate tank 044, the centrifuge filtrate tank 044 is connected to the inlet of a filtrate pump 045, and the outlet of the filtrate pump 045 is connected to the inlet of a crystallizer 046.
The sewage treatment system operates as follows:
the sewage is discharged from a sewage pipeline 001 to an ultrafiltration membrane group 002 and then enters an evaporation device 056 for evaporation concentration, the evaporation device 056 utilizes a reboiler I058 for heating and concentration by steam, a forced circulation pump I057 is used for providing circulation to avoid crystallization blockage in the reboiler I058, the material of the evaporation device 056 is pumped into a cooling device 060 by a discharge pump I059, the cooling device 060 uses chilled water provided by a chilled water pipeline 064 as a cold source, the chilled water is pumped out by a discharge pump II 063 and fed into a centrifugal machine I065 for solid-liquid separation, the obtained solid is sodium carbonate solid, the filtrate enters an oxidability eliminator (tank) 003, a reducing agent is pumped into the oxidability eliminator (tank) 003 from a reducing agent storage tank 004 by a reducing agent dosing pump for stirring and mixing reaction, then the liquid in the oxidability eliminator (tank) 003 is pumped into a high-pressure pump V078 for treatment by a nanofiltration membrane group I075, the concentrated water of the nanofiltration membrane group I is returned to the evaporation device 056, fresh water of the nanofiltration membrane group I075 enters a medium and tank b 020, the medium and the tank b is firstly added with acid and reacted with carbonate, the hydrogen carbonate is pumped into the centrifugal machine I065 for solid-liquid separation, the obtained solid is in the form is pumped out of the centrifugal machine I043, the solid is pumped into the centrifugal machine 042 from the centrifugal machine 042 after the solid is pumped into the solid 042, and the solid is discharged from the centrifugal machine 042, namely the solid is discharged from the solid 042, the solid is pumped into the solid 042, and finally enters the solid 042 for the solid 040404042.
Fresh hydrobromic acid and sodium hydroxide (firstly hydrobromic acid and then sodium hydroxide) are added into a neutralization tank b 020, the purpose of firstly adding hydrobromic acid is to remove residual carbonate and bicarbonate (the PH is reduced to about 3-4.5) in the inlet water, and the purpose of adding sodium hydroxide and adjusting the pH to be neutral is that the pH is required to be reduced to about 3-4.5 by adding hydrobromic acid before neutralizing the carbonate and the bicarbonate, at the moment, free hydrobromic acid exists in the water, and sodium hydroxide is required to be used for neutralizing the free hydrobromic acid in order to promote the purity of the finally crystallized sodium bromide.
The experiment was run using the system described above:
the sewage line 001 sampling analysis is as follows: ph=9.1, total bromine 1251ppm, bromide 1203ppm, bicarbonate 7531ppm, carbonate 1221ppm, orp=781 MV.
Control the temperature of cooling device 060 = 3 ℃, analyze solids outlet 066 of centrifuge i 065: 58% sodium carbonate, 976ppm bromide;
the reducing agent storage tank 004 is filled with industrial formic acid as a reducing agent, the reducing agent dosing pump is controlled to add formic acid to the oxidizing elimination tank 003 (formic acid addition amount=500 ppm of sewage pipeline 001 flow), the buffer tank i 006 is fed with liquid alkali to control ph=11, and the buffer tank i 006 is analyzed as follows: ph=11.3, total bromine 41212ppm, bromide 4186 ppm, carbonate 35008ppm, bicarbonate 3515ppm, orp=87 MV;
Immediately after the acid addition to neutralization tank b 020 was reacted to acidity, the sample was analyzed as follows: ph=3.0, bromide=48919 ppm, carbonate, bicarbonate cannot be detected;
after the neutralization tank c 080 was reacted to neutrality by adding a base, the sample was analyzed as follows: ph=7.0, bromide= 46533ppm, carbonate, bicarbonate cannot be detected;
the solids outlet 043 of centrifuge 042 was sampled and analyzed as follows: sodium bromide content 98.8%.
Conclusion: a sewage treatment system is constructed according to the fifth embodiment, and finally sodium bromide solid and sodium carbonate solid (sodium bicarbonate is converted into sodium carbonate and carbon dioxide in the process of heating and concentrating, and carbon dioxide is dissipated into the air and runs off) can be obtained; while example two demonstrates that crystallizer 046 is interchangeable with bipolar membrane electrodialysis apparatus 024, it can be deduced that substitution of crystallizer 046 for bipolar membrane electrodialysis apparatus 024 is feasible, except that the final product is chosen to be HBr instead of sodium bromide of this example; meanwhile, the third embodiment proves that the nanofiltration membrane group and the monovalent ion purification electrodialysis device are interchangeable, so that the nanofiltration membrane group I075 can be deduced to be interchangeable by the monovalent ion purification electrodialysis device I, and the effect of extracting the sodium bromide aqueous solution from the sodium carbonate and sodium bromide aqueous solution can be achieved, namely, the nanofiltration membrane group I075 can be replaced by the monovalent ion purification electrodialysis device I in the embodiment, and the same effect can be achieved.
Example six
As shown in FIG. 6, a sewage treatment system mainly comprises a sewage pipeline 001, an evaporation device 056, a cooling device 060, a solid-liquid separator (a centrifugal machine I065) and a crystallizer 046.
The sewage pipeline 001 is connected to the ultrafiltration membrane group 002, the delivery port of ultrafiltration membrane group 002 is connected to the water inlet of evaporation plant 056, evaporation plant 056 still is equipped with forced circulation pump I057, reboiler I058, evaporation plant 056's discharge pump I059 is connected to the water inlet of cooling device 060, cooling device 060 still is equipped with forced circulation pump II 061, cooling heat exchanger 062 (chilled water pipeline 064 also is connected to the shell side of cooling heat exchanger 062), cooling device 060's discharge pump II 063 is connected to solid-liquid separator (centrifuge I065), centrifuge I065 is equipped with solid outlet 066, centrifuge I065's filtrate outlet is connected to neutralization tank b020, acidification device I074 also is connected to neutralization tank b020, neutralization tank b's delivery port is connected to neutralization tank c 080's water inlet, alkalization unit IV 079 also is connected to neutralization tank c 080, neutralization tank c 080's outlet is connected to pump II 23, pump II 23's outlet is connected to crystallizer 046's water inlet, crystallizer 046 is equipped with reboiler 046 still, centrifuge I065 is equipped with centrifugal pump I066 is equipped with solid outlet 066, centrifuge I is equipped with filtrate outlet is connected to centrifuge 042, centrifuge inlet 044 is connected to centrifuge inlet 044, centrifuge inlet is connected to pump 044 outlet is connected to centrifuge inlet 044.
The sewage treatment system operates as follows:
the sewage is discharged from a sewage pipeline 001 to an ultrafiltration membrane group 002 and then enters an evaporation device 056 for evaporation concentration, the evaporation device 056 utilizes a reboiler I058 for heating and concentration by steam, a forced circulation pump I057 is used for providing circulation to avoid crystallization blockage in the reboiler I058, the material of the evaporation device 056 is pumped into a cooling device 060 by a discharge pump I059, the cooling device 060 uses chilled water provided by a chilled water pipeline 064 as a cold source and is pumped out by a discharge pump II 063 to a centrifuge I065 for solid-liquid separation, the obtained solid is sodium carbonate solid, the filtrate enters a neutralization tank b 020, the neutralization tank b 020 is firstly added with acid to react with carbonate and bicarbonate, then is added with alkali to react with free HBr in a neutralization tank c 080, then enters a crystallizer 046, the crystallizer 046 is heated and concentrated by a reboiler 040, the material is pumped out by the discharge pump 042, the solid of the centrifuge 042 is discharged and collected from a solid outlet 043, the filtrate of the centrifuge 042 enters a filtrate tank 044 and is pumped back into the crystallizer 046 by a filtrate pump 045, namely all the product is discharged from the solid outlet of the centrifuge 043 in the form.
Fresh hydrobromic acid and sodium hydroxide (firstly hydrobromic acid and then sodium hydroxide) are added into a neutralization tank b 020, the purpose of firstly adding hydrobromic acid is to remove residual carbonate and bicarbonate (the PH is reduced to about 3-4.5) in the inlet water, and the purpose of adding sodium hydroxide and adjusting the pH to be neutral is that the pH is required to be reduced to about 3-4.5 by adding hydrobromic acid before neutralizing the carbonate and the bicarbonate, at the moment, free hydrobromic acid exists in the water, and sodium hydroxide is required to be used for neutralizing the free hydrobromic acid in order to promote the purity of the finally crystallized sodium bromide.
The experiment was run using the system described above:
the sewage line 001 sampling analysis is as follows: ph=9.1, total bromine 1251ppm, bromide 1203ppm, bicarbonate 7531ppm, carbonate 1221ppm, orp=781 MV.
Control the temperature of cooling device 060 = 3 ℃, analyze solids outlet 066 of centrifuge i 065: 58% sodium carbonate, 976ppm bromide;
immediately after the acid was added to the neutralization tank b 020 to react to be acidic, the neutralization tank b 020 was sampled and analyzed as follows: ph=3.2, bromide=51121 ppm, carbonate, bicarbonate cannot be detected;
after the neutralization tank c 080 was reacted to neutrality by adding a base, the sample was analyzed as follows: ph=7.0, bromide= 49811ppm, carbonate, bicarbonate cannot be detected;
the solids outlet 043 of centrifuge 042 was sampled and analyzed as follows: sodium bromide content 97.7%.
Conclusion: a sewage treatment system is constructed according to the sixth embodiment, and finally sodium bromide solid and sodium carbonate solid (sodium bicarbonate is converted into sodium carbonate and carbon dioxide in the process of heating and concentrating, and the carbon dioxide is dissipated into the air to be lost) can be obtained.
Claims (82)
1. A sewage treatment system, the sewage treatment system comprising: a sewage pipeline, an oxidizing eliminator, a nanofiltration membrane group or a purification monovalent ion electrodialysis device or a salt separation unit, a bipolar membrane electrodialysis device or a crystallizer;
The sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the nanofiltration membrane group, and the fresh water outlet or the concentrated water outlet of the nanofiltration membrane group is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer; or the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the purifying monovalent ion electrodialysis device, and the outlet I or the outlet II of the purifying monovalent ion electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the salt separating unit, and the water solution outlet of the salt separating unit is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer; or the sewage pipeline is connected to the water inlet of the salt separation unit, the water solution outlet of the salt separation unit is connected to the water inlet of the oxidizing eliminator, and the water outlet of the oxidizing eliminator is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or the sewage treatment system comprises: a sewage pipeline, a salt separation unit and a crystallizer; the sewage pipeline is connected to the water inlet of the salt separation unit, and the water solution outlet of the salt separation unit is connected to the water inlet of the crystallizer.
2. The sewage treatment system according to claim 1, further comprising a concentrating device c, a water outlet of the oxidizing eliminator being connected to a water inlet of the concentrating device c, a concentrate outlet of the concentrating device c being connected to a water inlet of the salt separating unit.
3. The sewage treatment system according to claim 1, wherein an acid adding unit i:
the outlet of the acid adding unit I is connected to a fresh water outlet of the nanofiltration membrane group or a pipeline between the outlet I of the purification monovalent ion electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, and the connection position is called a pipeline connection point a; or the outlet of the acid adding unit I is connected to a fresh water outlet of the nanofiltration membrane group or a pipeline between the outlet I of the purification monovalent ion electrodialysis device and the water inlet of the crystallizer, and the connection position is called a pipeline connection point a; or the outlet of the acid adding unit I is connected to a pipeline between the water solution outlet of the salt separating unit and the water inlet of the bipolar membrane electrodialysis device, and the connection position is called a pipeline connection point a; or the outlet of the acid adding unit I is connected to a pipeline between the water solution outlet of the salt separating unit and the water inlet of the crystallizer, and the connection position is called a pipeline connection point a; or the outlet of the acid adding unit I is connected to a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the bipolar membrane electrodialysis device, and the connection position is called a pipeline connection point a; or the outlet of the acid adding unit I is connected to a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the crystallizer, and the connection position is called a pipeline connection point a;
Or a neutralization tank b is arranged between the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device, and the outlet of the acid adding unit I is connected to the water inlet of the neutralization tank b; or a neutralization tank b is arranged between the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the crystallizer, the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the crystallizer, and the outlet of the acid adding unit I is connected to the water inlet of the neutralization tank b;
or a neutralization tank b is arranged between the water solution outlet of the salt separation unit and the water inlet of the bipolar membrane electrodialysis device, the water solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b; or a neutralization tank b is arranged between the water solution outlet of the salt separation unit and the water inlet of the crystallizer, the water solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the crystallizer, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b; or a neutralization tank b is arranged between the water outlet of the oxidizing eliminator and the water inlet of the bipolar membrane electrodialysis device, the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b; or a neutralization tank b is arranged between the water outlet of the oxidizing eliminator and the water inlet of the crystallizer, the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the crystallizer, and the outlet of the acid adding unit I is connected to the inlet of the neutralization tank b.
4. A sewage treatment system according to claim 3, wherein a concentration device a is provided;
the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the pipeline connection point a, and the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the water inlet of the neutralization tank b, and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
5. The sewage treatment system according to claim 4, further comprising a decarburization tower b:
when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the pipeline connection point a, and the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the concentration device a; or the concentrated water outlet of the concentrating device a is firstly connected to the water inlet of the decarbonization tower b, and the water outlet of the decarbonization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device a, the concentrated water outlet of the concentration device a is connected to the water inlet of the neutralization tank b, and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer: the water outlet of the neutralization tank b is connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the concentration device a, and the concentrated water outlet of the concentration device a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the water outlet of the neutralization tank b is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the concentration device a; or the concentrated water outlet of the concentrating device a is firstly connected to the water inlet of the decarbonization tower b, and the water outlet of the decarbonization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
6. A sewage treatment system according to claim 3, further provided with a decarbonization tower b:
when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion electrodialysis device is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the fresh water outlet of the nanofiltration membrane group or the outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the neutralization tank b, and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the water outlet of the neutralization tank b is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
7. A sewage treatment system according to claim 3, further provided with a decarbonization tower b:
When the water solution outlet of the salt separation unit is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the water solution outlet of the salt separation unit is connected to the water inlet of the neutralization tank b, the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the water outlet of the neutralization tank b is connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
or when the water outlet of the oxidability eliminator is connected to the pipeline connection point a, the pipeline connection point a is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the pipeline connection point a is firstly connected to the water inlet of the decarburization tower b, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer;
Or when the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank b, and the water outlet of the neutralization tank b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer, the water outlet of the neutralization tank b is connected to the water inlet of the decarburization tower b first, and the water outlet of the decarburization tower b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
8. The sewage treatment system according to claim 1, wherein a concentrating device b is provided:
a concentration device b is arranged between the nanofiltration membrane group or the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device; or a concentration device b is arranged between the nanofiltration membrane group or the purification monovalent ion electrodialysis device and the water inlet of the crystallizer; the fresh water outlet or the concentrated water outlet of the nanofiltration membrane group is connected to the water inlet of the concentrating device b, and the concentrated water outlet of the concentrating device b is connected to the water inlet of the bipolar membrane electrodialysis equipment or the water inlet of the crystallizer; or the outlet I or the outlet II of the purification monovalent ion electrodialysis device is connected to the water inlet of the concentration device b, and the concentrated water outlet of the concentration device b is connected to the water inlet of the bipolar membrane electrodialysis device or the water inlet of the crystallizer.
9. The sewage treatment system according to claim 1, further comprising an alkali adding unit i:
when the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, the outlet of the alkali adding unit I is connected with a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and the connection position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the oxidizing eliminator, and the connection position is called a pipeline connection point c; or a buffer tank I is arranged, the water outlet of the oxidizing eliminator is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the oxidizing eliminator, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the oxidizing eliminator;
Or when the sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the salt separating unit, the outlet of the alkali adding unit I is connected with a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the salt separating unit, and the connected position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the oxidizing eliminator, and the connection position is called a pipeline connection point c; or the device is provided with a buffer tank I, the water outlet of the oxidizing eliminator is connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the salt separation unit, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the oxidizing eliminator, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the salt separating unit; or the outlet of the alkali adding unit I is connected to the oxidizing eliminator;
Or when the sewage pipeline is connected to the water inlet of the salt separating unit, the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the salt separating unit, and the connected position is called a pipeline connection point c; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the salt separation unit, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the salt separating unit; or the outlet of the alkalizing unit I is connected to the oxidizing eliminator.
10. The sewage treatment system according to claim 2, further comprising an alkali adding unit i:
when a sewage pipeline is connected to the water inlet of the oxidizing eliminator, the water outlet of the oxidizing eliminator is connected to the water inlet of the concentrating device c, and the concentrated water outlet of the concentrating device c is connected to the water inlet of the salt separating unit, the outlet of the alkali adding unit I is connected with a pipeline between the water outlet of the oxidizing eliminator and the water inlet of the concentrating device c, and the connection position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline from the concentrated water outlet of the concentrating device c to the water inlet of the salt separating unit, and the connection position is called a pipeline connection point c; or the outlet of the alkali adding unit I is connected with a pipeline between the sewage pipeline and the water inlet of the oxidizing eliminator, and the connection position is called a pipeline connection point c; or a buffer tank I is arranged, the water outlet of the oxidizing eliminator is connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the concentrating device c, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the concentrated water outlet of the concentrating device c is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the salt separation unit, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the sewage pipeline is firstly connected to the water inlet of the buffer tank I, the water outlet of the buffer tank I is connected to the water inlet of the oxidizing eliminator, and the outlet of the alkali adding unit I is connected with the buffer tank I; or the outlet of the alkali adding unit I is connected to the salt separating unit; or the outlet of the alkalizing unit I is connected to the oxidizing eliminator.
11. The sewage treatment system according to claim 1, further comprising a heating unit:
the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the heating unit is installed between the sewage pipe and the water inlet of the oxidizing canceller; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the salt separating unit; or the heating unit is installed between the sewage pipe and the water inlet of the oxidizing canceller; or the heating unit is arranged between the sewage pipeline and the water inlet of the salt separating unit;
or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the heating unit is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the oxidizing eliminator; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the salt separating unit; or the heating unit is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the oxidizing eliminator; or the heating unit is arranged between the sewage pipeline and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the salt separating unit;
Or a buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and the heating unit is used for heating the buffer tank III; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and the heating unit is used for heating the buffer tank III; or the buffer tank III is arranged between the water outlet of the oxidizing eliminator and the water inlet of the salt separating unit, and the heating unit is used for heating the buffer tank III; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and the heating unit is used for heating the buffer tank III; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the salt separating unit, and the heating unit is used for heating the buffer tank III;
or a buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the salt separating unit, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the salt separating unit; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the sewage pipeline and the water inlet of the salt separation unit, a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the salt separation unit, and the heating unit is used for heating the buffer tank III.
12. The sewage treatment system according to claim 2, further comprising a heating unit:
the heating unit is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentration device c; or the heating unit is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit;
or the heating unit is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the oxidizing eliminator; or the heating unit is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentrating device c, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the concentrating device c; or the heating unit is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit, and a cooler and/or a decarburization tower a is arranged between the heating unit and the water inlet of the salt separating unit;
or a buffer tank III is arranged between a sewage pipeline and a water inlet of the oxidizing eliminator, and the heating unit is used for heating the buffer tank III; or the buffer tank III is arranged between the water outlet of the oxidizing eliminator and the water inlet of the concentrating device c, and the heating unit is used for heating the buffer tank III; or the buffer tank III is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit, and the heating unit is used for heating the buffer tank III;
Or a buffer tank III is arranged between a sewage pipeline and a water inlet of the oxidizing eliminator, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the oxidizing eliminator; or the buffer tank III is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentrating device c, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the concentrating device c; or the buffer tank III is arranged between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit, the heating unit is used for heating the buffer tank III, and a cooler and/or a decarburization tower a is arranged between the buffer tank III and the water inlet of the salt separating unit.
13. The wastewater treatment system of claim 4 or 5, wherein the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the concentration device a.
14. The wastewater treatment system of claim 8, wherein the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the concentration device b.
15. A sewage treatment system according to claim 2, wherein the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the concentration device c.
16. A sewage treatment system according to claim 1, 3 or 7, wherein the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the salt separation unit.
17. The wastewater treatment system of claim 1, wherein a dilute brine outlet of the bipolar membrane electrodialysis device is connected to the wastewater conduit; or the dilute brine outlet of the bipolar membrane electrodialysis device discharges outside the boundary.
18. The wastewater treatment system of claim 1, 3 or 7, wherein a dilute brine outlet of the bipolar membrane electrodialysis device is connected to the oxidative suppressor.
19. A sewage treatment system according to claim 9 or 10, wherein the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the pipe connection point c; or the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the buffer tank I.
20. A sewage treatment system according to claim 11 or 12, wherein the dilute brine outlet of the bipolar membrane electrodialysis device is connected to the water inlet of the heating unit.
21. The sewage treatment system according to claim 1, 2, 3, 7, 9, 10, 11 or 12, wherein the salt separation unit is a concentrated solid-precipitated salt separation unit or a solid-added salt separation unit formed by adding chemicals:
the concentrated solid-separating salt separating unit comprises an evaporation device and a solid-liquid separator: the material outlet of the evaporation device is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the water inlet of the evaporation device is the water inlet of the salt separation unit, and the aqueous solution outlet of the solid-liquid separator is the aqueous solution outlet of the salt separation unit;
or the salt separating unit for concentrating and separating out the solid comprises an evaporation device, a cooling device and a solid-liquid separator: the material outlet of the evaporation device is connected to the inlet of the cooling device, the outlet of the cooling device is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the water inlet of the evaporation device is the water inlet of the salt separation unit, and the aqueous solution outlet of the solid-liquid separator is the aqueous solution outlet of the salt separation unit;
Or the salt separation unit for concentrating and separating out the solid comprises an evaporation device, a solid-liquid separator and a nanofiltration membrane group 'or a monovalent ion type electrodialysis purification device': the material outlet of the evaporation device is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the aqueous solution outlet of the solid-liquid separator is connected to the water inlet of the nanofiltration membrane group ' or the water inlet of the purified monovalent ion electrodialysis device ', the nanofiltration membrane group ' is provided with a fresh water outlet and a concentrated water outlet, the water inlet of the evaporation device is the water inlet of the salt separation unit, and the fresh water outlet of the nanofiltration membrane group ' or the outlet I of the purified monovalent ion electrodialysis device ' is the aqueous solution outlet of the salt separation unit;
or the salt separation unit for concentrating and separating out the solid comprises an evaporation device, a cooling device, a solid-liquid separator and a nanofiltration membrane group 'or a monovalent ion type electrodialysis purification device': the material outlet of the evaporation device is connected to the inlet of the cooling device, the outlet of the cooling device is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, the aqueous solution outlet of the solid-liquid separator is connected to the water inlet of the nanofiltration membrane group ' or the water inlet of the purification monovalent ion electrodialysis device ', the nanofiltration membrane group ' is provided with a fresh water outlet and a concentrated water outlet, the water inlet of the evaporation device is the water inlet of the salt separation unit, and the fresh water outlet of the nanofiltration membrane group ' or the outlet I of the purification monovalent ion electrodialysis device ' is the aqueous solution outlet of the salt separation unit;
Or the salt separating unit for adding chemicals to form solid comprises a mixing tank and a solid-liquid separator, wherein the mixing tank is also provided with a chemical adding port, a water inlet and a material outlet, the material outlet of the mixing tank is connected to the inlet of the solid-liquid separator, the solid-liquid separator is provided with an aqueous solution outlet and a solid outlet, and the aqueous solution outlet of the solid-liquid separator is the aqueous solution outlet of the salt separating unit; the water inlet of the mixing tank is the water inlet of the salt separating unit.
22. The sewage treatment system according to claim 21, wherein when the salt separation unit is the concentrated and precipitated solid type salt separation unit, an acid adding unit ii is further provided, and an outlet of the acid adding unit ii is connected to an inlet of the evaporation device; or the outlet of the acid adding unit II is connected to a pipeline between the material outlet of the evaporation device and the inlet of the solid-liquid separator; or the outlet of the acid adding unit II is connected to a pipeline between the material outlet of the evaporation device and the inlet of the cooling device; or the outlet of the acid adding unit II is connected to a pipeline between the outlet of the cooling device and the inlet of the solid-liquid separator; or the outlet of the acid adding unit II is connected to the water inlet of the concentrating device c; and the inlet of the acid adding unit II is connected to an acid tank or an acid pipeline.
23. The sewage treatment system according to claim 21, wherein when the salt separation unit is the concentrated and precipitated solid type salt separation unit, an alkali adding unit ii is further provided, and an outlet of the alkali adding unit ii is connected to a pipeline between an aqueous solution outlet of the solid-liquid separator and a water inlet of the nanofiltration membrane group 'or a water inlet of the purification monovalent ion electrodialysis device'; or the outlet of the alkali adding unit II is connected with a pipeline between the water solution outlet of the solid-liquid separator and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device through a pipeline mixer; or the water solution outlet of the solid-liquid separator is connected to the water inlet of a middle tank, the water outlet of the middle tank is connected to the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device, and the outlet of the alkali adding unit II is connected to the inlet of the middle tank.
24. The sewage treatment system according to claim 3 or 7, further comprising a nanofiltration membrane group i or a purified monovalent ion electrodialysis device i, wherein the water outlet of the oxidizing eliminator is connected to the water inlet of the nanofiltration membrane group i or the purified monovalent ion electrodialysis device i, and wherein the fresh water outlet of the nanofiltration membrane group i or the purified monovalent ion electrodialysis device i is connected to the pipe connection point a; or the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purification monovalent ion electrodialysis device I is connected to the water inlet of the neutralization tank b.
25. The sewage treatment system according to claim 11 or 12, further comprising a nanofiltration membrane group i or a purified monovalent ion electrodialysis device i, wherein the water outlet of the oxidation eliminator is connected to the water inlet of the nanofiltration membrane group i or the purified monovalent ion electrodialysis device i, and wherein the fresh water outlet of the nanofiltration membrane group i or the purified monovalent ion electrodialysis device i is connected to the water inlet of the heating unit.
26. The sewage treatment system according to claim 1, 3 or 7, further comprising a nanofiltration membrane group i or a purified monovalent ion electrodialysis device i, wherein the water outlet of the oxidation eliminator is connected to the water inlet of the nanofiltration membrane group i or the purified monovalent ion electrodialysis device i, and wherein the fresh water outlet of the nanofiltration membrane group i or the purified monovalent ion electrodialysis device i is connected to the water inlet of the bipolar membrane electrodialysis device; or the fresh water outlet of the nanofiltration membrane group I or the outlet I of the purification monovalent ion electrodialysis device I is connected to the water inlet of the crystallizer.
27. The sewage treatment system according to claim 26, wherein an alkali adding unit iii or a heating unit is further provided, an outlet of the alkali adding unit iii being connected to the oxidizing eliminator; or the outlet of the alkali adding unit III is connected to a pipeline between the water outlet of the oxidability eliminator and the water inlet of the nanofiltration membrane group I or the water inlet of the purification monovalent ion electrodialysis device I, which is called a pipeline connection point d; or the water outlet of the oxidizing eliminator is connected to the water inlet of the neutralization tank I, the water outlet of the neutralization tank I is connected to the water inlet of the nanofiltration membrane group I or the water inlet of the purification monovalent ion electrodialysis device I, and the outlet of the alkali adding unit III is connected to the neutralization tank I; or the water outlet of the oxidability eliminator is connected to the water inlet of the heating unit, and the water outlet of the heating unit is connected to the water inlet of the nanofiltration membrane group I or the water inlet of the purification monovalent ion electrodialysis device I.
28. The sewage treatment system according to claim 1, 3, 4, 5 or 6, characterized in that an alkali adding unit iv is further provided, the outlet of which is connected to a pipe between the fresh water outlet of the nanofiltration membrane group and the water inlet of the crystallizer, or the outlet of which is connected to a pipe between the concentrate outlet of the nanofiltration membrane group and the water inlet of the crystallizer, or the outlet of which is connected to a pipe between the outlet i of the purified monovalent ion electrodialysis device and the water inlet of the crystallizer, or the outlet of which is connected to a pipe between the outlet ii of the purified monovalent ion electrodialysis device and the water inlet of the crystallizer, called a pipe connection point e;
or the fresh water outlet of the nanofiltration membrane group is connected with the water inlet of the crystallizer, the concentrated water outlet of the nanofiltration membrane group is connected with the water inlet of the crystallizer, the outlet I of the purification monovalent ion electrodialysis device is connected with the water inlet of the crystallizer, the outlet II of the purification monovalent ion electrodialysis device is connected with the water inlet of the crystallizer, a neutralization tank c is further arranged, and the outlet of the alkali adding unit IV is connected with the neutralization tank c.
29. The sewage treatment system according to claim 3, 4, 5, 6 or 7, characterized in that an alkali adding unit iv is further provided, the outlet of which is connected to the pipe between the pipe connection point a and the water inlet of the crystallizer or the outlet of which is connected to the pipe between the water outlet of the neutralization tank b and the water inlet of the crystallizer, called pipe connection point e;
or the pipeline connecting point a is arranged between the water inlet of the crystallizer and the water outlet of the neutralization tank b is arranged between the water inlet of the crystallizer, and the neutralization tank c is further arranged, and the outlet of the alkali adding unit IV is connected to the neutralization tank c.
30. The sewage treatment system according to claim 11 or 12, further comprising an alkalizing unit iv, the outlet of which is connected to a pipe between the water outlet of the heating unit and the water inlet of the crystallizer, called a pipe connection point e;
or a neutralization tank c is arranged between the water outlet of the heating unit and the water inlet of the crystallizer, and the outlet of the alkali adding unit IV is connected to the neutralization tank c.
31. The sewage treatment system according to claim 4 or 5, further comprising an alkali adding unit iv, wherein the outlet of the alkali adding unit iv is connected to a pipe between the concentrate outlet of the concentrating device a and the water inlet of the crystallizer, called a pipe connection point e;
Or a neutralizing tank c is arranged between the concentrated water outlet of the concentrating device a and the water inlet of the crystallizer, and the outlet of the alkali adding unit IV is connected to the neutralizing tank c.
32. The sewage treatment system according to claim 5, 6 or 7, further comprising an alkali adding unit iv, wherein an outlet of the alkali adding unit iv is connected to a pipe between a water outlet of the decarburization tower b and a water inlet of the crystallizer, which is called a pipe connection point e;
or a neutralization tank c is arranged between the water outlet of the decarburization tower b and the water inlet of the crystallizer, and the outlet of the alkali adding unit IV is connected to the neutralization tank c.
33. The sewage treatment system according to claim 9 or 10, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between the sewage pipeline and the pipeline connection point c, or between the sewage pipeline and the water inlet of the buffer tank I, or between the pipeline connection point c and the water inlet of the oxidizing eliminator, or between the water outlet of the buffer tank I and the water inlet of the oxidizing eliminator, or between the water outlet of the oxidizing eliminator and the pipeline connection point c, or between the water outlet of the oxidizing eliminator and the water inlet of the buffer tank I, or between the water outlet of the buffer tank I and the water inlet of the salt separation unit, or between the pipeline connection point c and the water inlet of the salt separation unit, or between the water outlet of the buffer tank I and the water inlet of the salt separation unit;
Or the organic matter elimination device is an oxidizing eliminator.
34. The sewage treatment system according to claim 11 or 12, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between the sewage pipeline and the water inlet of the heating unit, or between the water outlet of the heating unit and the water inlet of the oxidizing eliminator, or between the water outlet of the oxidizing eliminator and the water inlet of the heating unit, or between the water outlet of the heating unit and the water inlet of the salt separation unit, or between the water outlet of the oxidizing eliminator and the water inlet of the heating unit, or between the water outlet of the salt separation unit and the water inlet of the heating unit;
or the organic matter elimination device is an oxidizing eliminator.
35. The sewage treatment system according to claim 2, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator;
or the organic matter elimination device is an oxidizing eliminator.
36. A sewage treatment system according to claim 1 or 3, wherein an organic matter elimination device is further provided,
The organic matter elimination device is arranged between the sewage pipeline and the water inlet of the oxidizing eliminator, or between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration membrane group, or between the water outlet of the oxidizing eliminator and the water inlet of the purifying monovalent ion electrodialysis device;
or the organic matter elimination device is an oxidizing eliminator.
37. The sewage treatment system according to claim 1, 3, 4, 5 or 6, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between a fresh water outlet of the nanofiltration membrane group and a water inlet of the bipolar membrane electrodialysis device, or between a fresh water outlet of the nanofiltration membrane group and a water inlet of the crystallizer, or between an outlet I of the purification monovalent ion electrodialysis device and a water inlet of the bipolar membrane electrodialysis device, or between an outlet I of the purification monovalent ion electrodialysis device and a water inlet of the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
38. The sewage treatment system according to claim 3, 4, 5 or 6, wherein an organic matter elimination device is further provided,
The organic matter elimination device is arranged between a fresh water outlet of the nanofiltration membrane group and the pipeline connection point a, or between an outlet I of the purification monovalent ion type electrodialysis device and the pipeline connection point a, or between an outlet I of the nanofiltration membrane group and the neutralization tank b, or between an outlet I of the purification monovalent ion type electrodialysis device and the neutralization tank b, or between the pipeline connection point a and a water inlet of the bipolar membrane electrodialysis device, or between the pipeline connection point a and a water inlet of the crystallizer, or between the neutralization tank b and a water inlet of the bipolar membrane electrodialysis device, or between the neutralization tank b and a water inlet of the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
39. The sewage treatment system according to claim 11, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between a fresh water outlet of the nanofiltration membrane group and a water inlet of the heating unit or between an outlet I of the purifying monovalent ion electrodialysis device and a water inlet of the heating unit;
or the organic matter elimination device is an oxidizing eliminator.
40. The wastewater treatment system of claim 30, further comprising an organic matter elimination device,
the organic matter eliminating device is arranged between the water outlet of the heating unit and the water inlet of the crystallizer, or between the water outlet of the heating unit and the pipeline connecting point e, or between the water outlet of the heating unit and the water inlet of the neutralization tank c, or between the pipeline connecting point e and the crystallizer, or between the water outlet of the neutralization tank c and the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
41. The sewage treatment system according to claim 4 or 5, wherein an organic matter elimination device is further provided,
the organic matter elimination equipment is arranged between a fresh water outlet of the nanofiltration membrane group and a water inlet of the concentration device a, between an outlet I of the purification monovalent ion electrodialysis equipment and a water inlet of the concentration device a, between a concentrated water outlet of the concentration device a and the pipeline connection point a, between a concentrated water outlet of the concentration device a and the neutralization tank b, between the pipeline connection point a and a water inlet of the concentration device a, between the neutralization tank b and a water inlet of the concentration device a, between a concentrated water outlet of the concentration device a and a water inlet of the bipolar membrane electrodialysis equipment, or between a concentrated water outlet of the concentration device a and the crystallizer;
Or the organic matter elimination device is an oxidizing eliminator.
42. The sewage treatment system according to claim 5 or 6, wherein an organic matter elimination device is further provided,
the organic matter elimination equipment is arranged between the pipeline connection point a and the water inlet of the decarburization tower b or between the neutralization tank b and the water inlet of the decarburization tower b;
or the organic matter elimination device is an oxidizing eliminator.
43. The sewage treatment system according to claim 5, wherein an organic matter elimination device is further provided,
the organic matter elimination equipment is arranged between the water outlet of the decarburization tower b and the water inlet of the concentrating device a or between the concentrated water outlet of the concentrating device a and the water inlet of the decarburization tower b;
or the organic matter elimination device is an oxidizing eliminator.
44. The sewage treatment system according to claim 5, 6 or 7, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water outlet of the decarbonization tower b and the water inlet of the bipolar membrane electrodialysis device or between the water outlet of the decarbonization tower b and the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
45. The sewage treatment system according to claim 1, 2, 9, 10, 11 or 12, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between the water outlet of the oxidizing eliminator and the water inlet of the salt separation unit or between the water outlet of the salt separation unit and the water inlet of the oxidizing eliminator;
or the organic matter elimination device is an oxidizing eliminator.
46. The sewage treatment system according to claim 10 or 12, wherein an organic matter elimination device is further provided,
the organic matter elimination equipment is arranged between the water outlet of the oxidability eliminator and the water inlet of the concentrating device c or between the concentrated water outlet of the concentrating device c and the water inlet of the salt separating unit;
or the organic matter elimination device is an oxidizing eliminator.
47. The sewage treatment system according to claim 10, wherein an organic matter elimination device is further provided,
the organic matter elimination equipment is arranged between the pipeline connection point c and the water inlet of the concentration device c, between the water outlet of the buffer tank I and the water inlet of the concentration device c, between the concentrated water outlet of the concentration device c and the pipeline connection point c, between the concentrated water outlet of the concentration device c and the water inlet of the buffer tank I, or between the pipeline connection point c and the water inlet of the salt separation unit;
Or the organic matter elimination device is an oxidizing eliminator.
48. The sewage treatment system according to claim 12, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water outlet of the heating unit and the water inlet of the concentrating device c or between the concentrated water outlet of the concentrating device c and the water inlet of the heating unit;
or the organic matter elimination device is an oxidizing eliminator.
49. The sewage treatment system according to claim 1 or 7, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water outlet of the salt separating unit and the water inlet of the bipolar membrane electrodialysis device or between the water outlet of the salt separating unit and the water inlet of the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
50. The sewage treatment system according to claim 3 or 7, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water outlet of the salt separating unit and the pipeline connecting point a or between the water outlet of the salt separating unit and the water inlet of the neutralization tank b;
Or the organic matter elimination device is an oxidizing eliminator.
51. The sewage treatment system according to claim 1, 9, 10, 11 or 12, wherein an organic matter elimination device is further provided,
the organic matter elimination equipment is arranged between the sewage pipeline and the water inlet of the salt separation unit;
or the organic matter elimination device is an oxidizing eliminator.
52. A sewage treatment system according to claim 3, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between the water outlet of the oxidizing eliminator and the pipeline connection point a or between the water outlet of the oxidizing eliminator and the water inlet of the neutralization tank b;
or the organic matter elimination device is an oxidizing eliminator.
53. The wastewater treatment system according to claim 24, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration membrane group I or between the water outlet of the oxidizing eliminator and the water inlet of the purifying monovalent ion electrodialysis device I;
or the organic matter elimination device is an oxidizing eliminator.
54. The wastewater treatment system of claim 25, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration membrane group I or between the water outlet of the oxidizing eliminator and the water inlet of the purifying monovalent ion electrodialysis device I;
or the organic matter elimination device is an oxidizing eliminator.
55. The wastewater treatment system of claim 26, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between the water outlet of the oxidizing eliminator and the water inlet of the nanofiltration membrane group I or between the water outlet of the oxidizing eliminator and the water inlet of the purifying monovalent ion electrodialysis device I;
or the organic matter elimination device is an oxidizing eliminator.
56. The wastewater treatment system of claim 27, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between the water outlet of the oxidizing eliminator and the pipeline connection point d, between the water outlet of the oxidizing eliminator and the water inlet of the neutralization tank I, between the water outlet of the oxidizing eliminator and the water inlet of the heating unit, between the pipeline connection point d and the water inlet of the nanofiltration membrane group I, between the pipeline connection point d and the water inlet of the purification monovalent ion type electrodialysis device I, between the water outlet of the neutralization tank I and the water inlet of the nanofiltration membrane group I, between the water outlet of the neutralization tank I and the water inlet of the purification monovalent ion type electrodialysis device I, between the water outlet of the heating unit and the water inlet of the nanofiltration membrane group I, or between the water outlet of the heating unit and the water inlet of the purification monovalent ion type electrodialysis device I;
Or the organic matter elimination device is an oxidizing eliminator.
57. The wastewater treatment system of claim 26, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between a fresh water outlet of the nanofiltration membrane group I and a water inlet of the bipolar membrane electrodialysis device, or between a fresh water outlet of the nanofiltration membrane group I and a water inlet of the crystallizer, or between an outlet I of the purification monovalent ion electrodialysis device I and a water inlet of the bipolar membrane electrodialysis device, or between an outlet I of the purification monovalent ion electrodialysis device I and a water inlet of the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
58. The wastewater treatment system according to claim 24, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between a fresh water outlet of the nanofiltration membrane group I and a water inlet of the neutralization tank b, or between a fresh water outlet of the nanofiltration membrane group I and a water inlet of the pipeline connection point a, or between an outlet I of the purification monovalent ion electrodialysis device I and a water inlet of the neutralization tank b, or between an outlet I of the purification monovalent ion electrodialysis device I and a water inlet of the pipeline connection point a;
Or the organic matter elimination device is an oxidizing eliminator.
59. The wastewater treatment system of claim 25, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between a fresh water outlet of the nanofiltration membrane group I and a water inlet of the heating unit, or between an outlet I of the purification monovalent ion electrodialysis device I and a water inlet of the heating unit;
or the organic matter elimination device is an oxidizing eliminator.
60. The wastewater treatment system of claim 28, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between a fresh water outlet of the nanofiltration membrane group and the pipeline connection point e, or between an outlet I of the purification monovalent ion type electrodialysis device and the pipeline connection point e, or between a fresh water outlet of the nanofiltration membrane group and a water inlet of the neutralization tank c, or between an outlet I of the purification monovalent ion type electrodialysis device and a water inlet of the neutralization tank c, or between the pipeline connection point e and the crystallizer, or between a water outlet of the neutralization tank c and the crystallizer;
Or the organic matter elimination device is an oxidizing eliminator.
61. The wastewater treatment system of claim 29, further comprising an organic matter elimination device,
the organic matter elimination device is arranged between the pipeline connection point a and the pipeline connection point e, or between the water outlet of the neutralization tank b and the pipeline connection point e, or between the pipeline connection point a and the water inlet of the neutralization tank c, or between the water outlet of the neutralization tank b and the water inlet of the neutralization tank c, or between the pipeline connection point e and the crystallizer, or between the water outlet of the neutralization tank c and the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
62. The wastewater treatment system of claim 31, further comprising an organic matter elimination device,
the organic matter elimination equipment is arranged between a concentrated water outlet of the concentration device a and the pipeline connecting point e, or between a concentrated water outlet of the concentration device a and a water inlet of the neutralization tank c, or between the pipeline connecting point e and the crystallizer, or between a water outlet of the neutralization tank c and the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
63. The wastewater treatment system of claim 32, further comprising an organic matter elimination device,
the organic matter eliminating device is arranged between the water outlet of the decarburization tower b and the pipeline connecting point e, or between the water outlet of the decarburization tower b and the water inlet of the neutralization tank c, or between the pipeline connecting point e and the crystallizer, or between the water outlet of the neutralization tank c and the crystallizer;
or the organic matter elimination device is an oxidizing eliminator.
64. The sewage treatment system according to claim 21, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water solution outlet of the solid-liquid separator and the water inlet of the nanofiltration membrane group or between the water solution outlet of the solid-liquid separator and the water inlet of the purification monovalent ion electrodialysis device;
or the organic matter elimination device is an oxidizing eliminator.
65. The sewage treatment system according to claim 23, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water solution outlet of the solid-liquid separator and the water inlet of the nanofiltration membrane group or between the water solution outlet of the solid-liquid separator and the water inlet of the purification monovalent ion electrodialysis device;
Or the organic matter elimination device is an oxidizing eliminator.
66. The sewage treatment system according to claim 9, wherein an organic matter elimination device is further provided,
the organic matter elimination device is arranged between the pipeline connection point c and the water inlet of the nanofiltration membrane group, or between the pipeline connection point c and the water inlet of the purification monovalent ion electrodialysis device, or between the water outlet of the buffer tank I and the water inlet of the nanofiltration membrane group, or between the water outlet of the buffer tank I and the water inlet of the purification monovalent ion electrodialysis device;
or the organic matter elimination device is an oxidizing eliminator.
67. The sewage treatment system according to claim 11, wherein an organic matter elimination device is further provided,
the organic matter eliminating device is arranged between the water outlet of the heating unit and the water inlet of the nanofiltration membrane group or between the water outlet of the heating unit and the water inlet of the purification monovalent ion electrodialysis device;
or the organic matter elimination device is an oxidizing eliminator.
68. The wastewater treatment system of claim 33, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
69. The wastewater treatment system of claim 34, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
70. The wastewater treatment system of claim 35, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
71. The wastewater treatment system of claim 36, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
72. The wastewater treatment system of claim 37, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
73. The wastewater treatment system of claim 38, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
74. The wastewater treatment system of claim 39, 40, 43, 47, 48, 52, 53, 54, 55, 56, 57, 58, 59, 60, 61, 62, 63, 64, 65, 66, or 67, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
75. The wastewater treatment system of claim 44, wherein the organic matter elimination device comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
76. The wastewater treatment system of claim 45, wherein the organic matter elimination device comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
77. The wastewater treatment system of claim 46, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
78. The wastewater treatment system of claim 49, wherein the organic matter elimination apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
79. The wastewater treatment system of claim 50, wherein the organic matter removal apparatus comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
80. The wastewater treatment system of claim 51, wherein the organic matter elimination device comprises: at least one of a biochemical treatment device, a high-grade oxidation device, an extraction device, an acidification device, a resin tank and an electrodialysis device; or the organic matter elimination device comprises an organic matter incineration device and an incineration residue dissolution tank.
81. The sewage treatment system according to claim 1, wherein a hardness removal device is provided:
a hardness removal device is arranged at any position between the sewage pipeline and the water inlet of the nanofiltration membrane group or the water inlet of the purification monovalent ion electrodialysis device;
or the hardness removing device is arranged at any position between the sewage pipeline and the water inlet of the salt separating unit; or the hardness removing device is arranged at any position between the water solution outlet of the salt separating unit and the water inlet of the bipolar membrane electrodialysis equipment or the water inlet of the crystallizer;
or the hardness removing device is arranged at any position between the sewage pipeline and the water inlet of the oxidizing eliminator; or the hardness removing device is arranged at any position between the water outlet of the oxidizing eliminator and the water inlet of the bipolar membrane electrodialysis equipment or the water inlet of the crystallizer.
82. The wastewater treatment system of claim 1, wherein the oxidation eliminator is at least one of an oxidation elimination reaction tank, a pipe mixer, a pipe connection point, and a reducing agent supply pipe is further provided, the reducing agent supply pipe being connected to the oxidation eliminator, the reducing agent supply pipe supplying a reducing agent to react the oxidizing property of the aqueous solution of the wastewater pipe;
or the oxidizing eliminator is a buffer tank or an aeration buffer tank.
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| CN202320137814.4U CN220201659U (en) | 2023-01-29 | 2023-01-29 | Sewage treatment system |
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| CN202320137814.4U CN220201659U (en) | 2023-01-29 | 2023-01-29 | Sewage treatment system |
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