CN220194466U - Gas cleaning and recycling system - Google Patents
Gas cleaning and recycling system Download PDFInfo
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- CN220194466U CN220194466U CN202320774498.1U CN202320774498U CN220194466U CN 220194466 U CN220194466 U CN 220194466U CN 202320774498 U CN202320774498 U CN 202320774498U CN 220194466 U CN220194466 U CN 220194466U
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- 238000004064 recycling Methods 0.000 title claims abstract description 104
- 238000004140 cleaning Methods 0.000 title claims abstract description 94
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 534
- 239000007788 liquid Substances 0.000 claims abstract description 425
- 238000005406 washing Methods 0.000 claims abstract description 314
- 239000012528 membrane Substances 0.000 claims abstract description 281
- 239000002253 acid Substances 0.000 claims abstract description 271
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 267
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 267
- 238000000909 electrodialysis Methods 0.000 claims abstract description 249
- 239000000126 substance Substances 0.000 claims abstract description 119
- 238000002425 crystallisation Methods 0.000 claims abstract description 114
- 230000008025 crystallization Effects 0.000 claims abstract description 114
- 239000005416 organic matter Substances 0.000 claims abstract description 102
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 97
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 791
- 239000007789 gas Substances 0.000 claims description 420
- 239000003638 chemical reducing agent Substances 0.000 claims description 226
- 239000003513 alkali Substances 0.000 claims description 201
- 238000000926 separation method Methods 0.000 claims description 165
- 150000007524 organic acids Chemical class 0.000 claims description 128
- 239000013505 freshwater Substances 0.000 claims description 69
- 238000001728 nano-filtration Methods 0.000 claims description 68
- 238000004090 dissolution Methods 0.000 claims description 60
- 229910001385 heavy metal Inorganic materials 0.000 claims description 54
- 230000020477 pH reduction Effects 0.000 claims description 54
- 239000007787 solid Substances 0.000 claims description 50
- 238000011084 recovery Methods 0.000 claims description 45
- 230000001603 reducing effect Effects 0.000 claims description 35
- 238000000746 purification Methods 0.000 claims description 30
- 150000003839 salts Chemical class 0.000 claims description 22
- 238000010438 heat treatment Methods 0.000 claims description 21
- 238000005262 decarbonization Methods 0.000 claims description 14
- 230000000630 rising effect Effects 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 7
- 238000003421 catalytic decomposition reaction Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 200
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 116
- 229910000029 sodium carbonate Inorganic materials 0.000 description 100
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 96
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 96
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 76
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 description 68
- 238000001704 evaporation Methods 0.000 description 62
- 238000001223 reverse osmosis Methods 0.000 description 62
- 235000017557 sodium bicarbonate Nutrition 0.000 description 58
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 58
- 230000008020 evaporation Effects 0.000 description 57
- BMYNFMYTOJXKLE-UHFFFAOYSA-N 3-azaniumyl-2-hydroxypropanoate Chemical compound NCC(O)C(O)=O BMYNFMYTOJXKLE-UHFFFAOYSA-N 0.000 description 55
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 55
- 239000003344 environmental pollutant Substances 0.000 description 46
- 231100000719 pollutant Toxicity 0.000 description 46
- 239000000243 solution Substances 0.000 description 41
- 239000007864 aqueous solution Substances 0.000 description 37
- 150000001768 cations Chemical class 0.000 description 34
- 150000002500 ions Chemical class 0.000 description 32
- 235000011121 sodium hydroxide Nutrition 0.000 description 32
- 230000001502 supplementing effect Effects 0.000 description 32
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 30
- 150000001450 anions Chemical class 0.000 description 29
- 238000010521 absorption reaction Methods 0.000 description 28
- 238000007254 oxidation reaction Methods 0.000 description 23
- CPELXLSAUQHCOX-UHFFFAOYSA-N Hydrogen bromide Chemical compound Br CPELXLSAUQHCOX-UHFFFAOYSA-N 0.000 description 22
- 239000000047 product Substances 0.000 description 21
- 239000003463 adsorbent Substances 0.000 description 19
- 230000003647 oxidation Effects 0.000 description 18
- -1 sodium formate) Chemical compound 0.000 description 18
- 239000013589 supplement Substances 0.000 description 18
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 17
- 229910052794 bromium Inorganic materials 0.000 description 17
- 239000000706 filtrate Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 15
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 14
- 239000000203 mixture Substances 0.000 description 14
- 238000004519 manufacturing process Methods 0.000 description 13
- 239000007921 spray Substances 0.000 description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 0.000 description 12
- 239000012141 concentrate Substances 0.000 description 11
- 238000010586 diagram Methods 0.000 description 11
- 239000001257 hydrogen Substances 0.000 description 11
- 229910052739 hydrogen Inorganic materials 0.000 description 11
- 239000007800 oxidant agent Substances 0.000 description 11
- 239000004280 Sodium formate Substances 0.000 description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 10
- 238000006722 reduction reaction Methods 0.000 description 10
- HLBBKKJFGFRGMU-UHFFFAOYSA-M sodium formate Chemical compound [Na+].[O-]C=O HLBBKKJFGFRGMU-UHFFFAOYSA-M 0.000 description 10
- 235000019254 sodium formate Nutrition 0.000 description 10
- 239000002250 absorbent Substances 0.000 description 9
- 230000002745 absorbent Effects 0.000 description 9
- 230000002378 acidificating effect Effects 0.000 description 9
- 238000004458 analytical method Methods 0.000 description 9
- 238000001816 cooling Methods 0.000 description 9
- 238000002474 experimental method Methods 0.000 description 9
- 230000001590 oxidative effect Effects 0.000 description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 8
- 238000007599 discharging Methods 0.000 description 8
- 238000001179 sorption measurement Methods 0.000 description 8
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 7
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 7
- 229910001437 manganese ion Inorganic materials 0.000 description 7
- 230000003472 neutralizing effect Effects 0.000 description 7
- 238000005070 sampling Methods 0.000 description 7
- 229910001429 cobalt ion Inorganic materials 0.000 description 6
- 229910000042 hydrogen bromide Inorganic materials 0.000 description 6
- 229910001415 sodium ion Inorganic materials 0.000 description 6
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 5
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 5
- 230000003113 alkalizing effect Effects 0.000 description 5
- 238000007664 blowing Methods 0.000 description 5
- 239000000460 chlorine Substances 0.000 description 5
- 229910052801 chlorine Inorganic materials 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000010941 cobalt Substances 0.000 description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 4
- 230000005684 electric field Effects 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- 239000008213 purified water Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 3
- 239000002585 base Substances 0.000 description 3
- 229940006460 bromide ion Drugs 0.000 description 3
- 239000003518 caustics Substances 0.000 description 3
- 229910021446 cobalt carbonate Inorganic materials 0.000 description 3
- ZOTKGJBKKKVBJZ-UHFFFAOYSA-L cobalt(2+);carbonate Chemical compound [Co+2].[O-]C([O-])=O ZOTKGJBKKKVBJZ-UHFFFAOYSA-L 0.000 description 3
- 239000007859 condensation product Substances 0.000 description 3
- 235000006748 manganese carbonate Nutrition 0.000 description 3
- 239000011656 manganese carbonate Substances 0.000 description 3
- 229940093474 manganese carbonate Drugs 0.000 description 3
- 229910000016 manganese(II) carbonate Inorganic materials 0.000 description 3
- XMWCXZJXESXBBY-UHFFFAOYSA-L manganese(ii) carbonate Chemical compound [Mn+2].[O-]C([O-])=O XMWCXZJXESXBBY-UHFFFAOYSA-L 0.000 description 3
- 239000012466 permeate Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- MZZUATUOLXMCEY-UHFFFAOYSA-N cobalt manganese Chemical compound [Mn].[Co] MZZUATUOLXMCEY-UHFFFAOYSA-N 0.000 description 2
- XLJKHNWPARRRJB-UHFFFAOYSA-N cobalt(2+) Chemical compound [Co+2] XLJKHNWPARRRJB-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- GVLGAFRNYJVHBC-UHFFFAOYSA-N hydrate;hydrobromide Chemical compound O.Br GVLGAFRNYJVHBC-UHFFFAOYSA-N 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 229910000403 monosodium phosphate Inorganic materials 0.000 description 2
- 235000019799 monosodium phosphate Nutrition 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000012266 salt solution Substances 0.000 description 2
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 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 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- ZBICJTQZVYWJPB-UHFFFAOYSA-N [Mn].[Co].[Br] Chemical compound [Mn].[Co].[Br] ZBICJTQZVYWJPB-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 238000007259 addition reaction Methods 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 125000001246 bromo group Chemical group Br* 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 150000002431 hydrogen Chemical group 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a gas cleaning and recycling system which comprises gas organic matter removal equipment, a washing tower I, a carbon dioxide generator, a bipolar membrane electrodialysis system, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator, wherein the gas cleaning and recycling system comprises a gas inlet and a gas outlet; or the gas cleaning and recycling system comprises gas organic matter removing equipment, a washing tower I, a concentrating device I, a PH-reducing device, solid-liquid separating equipment, bipolar membrane electrodialysis, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator. After the gas is treated by the system, the gas is purified, valuable substances in the gas are recovered, and waste is avoided.
Description
Technical Field
The utility model belongs to the technical field of pollution gas treatment, and particularly relates to a gas cleaning and recycling system.
Background
Today, the environmental protection requirement is increasingly serious, the pollution of the gas to the atmosphere is very important, the conventional method is to treat and convert the polluted gas into harmless gas for emission, and valuable substances in the polluted gas can be rarely recovered. The utility model provides a system which can not only purify the polluted gas, but also recycle valuable materials in the polluted gas.
Disclosure of Invention
The utility model aims to provide a gas cleaning and recycling system, which is used for purifying gas and recycling valuable substances in the gas after the polluted gas is treated by the system, so that waste is avoided.
A gas cleaning and recycling system, the gas cleaning and recycling system comprising: a gaseous organic matter removing device, a washing tower I, a carbon dioxide generator, a bipolar membrane electrodialysis device, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator;
the gas organic matter removing device is provided with a gas inlet (namely a target gas source treated by the utility model), a gas outlet of the gas organic matter removing device is connected to a gas inlet of the washing tower I, a liquid discharge port of the washing tower I is connected to a water inlet of the carbon dioxide generator, and a liquid discharge port of the carbon dioxide generator is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
Or the gas cleaning and recycling system comprises: the device comprises gas organic matter removing equipment, a washing tower I, a concentrating device I, a PH reducing device, solid-liquid separation equipment, bipolar membrane electrodialysis equipment, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator;
the gas organic matter removing device is provided with a gas inlet (namely a target gas source treated by the method), a gas outlet of the gas organic matter removing device is connected to a gas inlet of the washing tower I, a liquid discharge outlet of the washing tower I is connected to a water inlet of the concentration device I, a concentrated liquid outlet of the concentration device I is connected to a water inlet of the PH-lowering device, a discharge outlet of the PH-lowering device is connected to a water inlet of the solid-liquid separation device, and a liquid outlet of the solid-liquid separation device is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
or the gas cleaning and recycling system comprises: gas organic matter removing equipment, a washing tower I, a concentrating device I, PH-lowering solid-liquid separation equipment (namely, acid substances are added into the solid-liquid separation equipment at the same time, one equipment plays roles in PH lowering and solid-liquid separation at the same time), and bipolar membrane electrodialysis equipment, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator;
The gas organic matter removing device is provided with a gas inlet, a gas outlet of the gas organic matter removing device is connected to a gas inlet of the washing tower I, a liquid discharge outlet of the washing tower I is connected to a water inlet of the concentrating device I, a concentrated liquid outlet of the concentrating device I is connected to a water inlet of the PH-reducing solid-liquid separation device, and a liquid outlet of the PH-reducing solid-liquid separation device is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator.
Based on the above system, it is preferable that the organic matter in the gas is treated by the organic matter removing apparatus, and the organic matter in the polluted gas is treated to reduce the organic matter content and the organic matter (VOC) content in the gas.
Based on the above system, it is preferable to wash the gas by the washing tower i, and alkali washing is generally performed by alkali liquor, that is, the alkali liquor is used to trap acidic gas in the gas, such as carbon dioxide gas, other anionic acid radicals (such as bromide ions) contained in the gas after the gas is treated by the organic matter removing device, and the like.
Based on the above system, preferably, the carbon dioxide generator refers to a device for generating carbon dioxide by reaction, and is used for converting carbonate and bicarbonate in gas into carbon dioxide, and reducing the content of carbonate and bicarbonate in the effluent of the washing tower I.
Based on the above system, preferably, the purpose of the PH-lowering device is to lower the PH of the aqueous solution, convert carbonate into bicarbonate (e.g., sodium carbonate→sodium bicarbonate), and at the same temperature, the solubility of sodium bicarbonate is much lower than that of sodium carbonate, so that the sodium bicarbonate can be separated into insoluble substances from water in the form of conversion into bicarbonate, which is advantageous for the subsequent solid-liquid separation.
Based on the above system, preferably, the solid-liquid separation device refers to a device for separating materials to obtain solids and filtrate.
Based on the above system, preferably, the solid-liquid separation apparatus refers to an apparatus capable of performing a solid-liquid separation such as a positive pressure filter, a negative pressure suction filter, a centrifuge, a filter press, a bag filter, or the like.
Based on the above system, preferably, the PH-lowering solid-liquid separation apparatus refers to an apparatus that performs PH-lowering and solid-liquid separation in the same apparatus. The purpose of lowering the pH is to lower the pH of an aqueous solution, convert carbonate into bicarbonate (such as sodium carbonate and sodium bicarbonate), and at the same temperature, the solubility of sodium bicarbonate is far lower than that of sodium carbonate, so that the sodium bicarbonate can be separated into insoluble substances from water in a mode of being converted into bicarbonate, and the insoluble substances are beneficial to the subsequent solid-liquid separation.
Based on the above system, preferably, the equipment for realizing the PH reduction and the solid-liquid separation in the same equipment, such as a positive pressure filter, a negative pressure suction filter, a centrifuge, a filter press, a bag filter and the like, can play a role in solid-liquid separation, and a single acid can be added into the positive pressure filter, the negative pressure suction filter, the centrifuge, the filter press and the bag filter, and simultaneously the PH reduction converts sodium carbonate into sodium bicarbonate and plays a role in solid-liquid separation.
Based on the above system, preferably, the concentration device I is used for increasing the concentration multiple as much as possible, increasing the concentration of sodium carbonate in the concentrated solution, and facilitating the generation of a larger total solid amount when the sodium bicarbonate is converted later, namely, the sodium bicarbonate is separated more thoroughly.
Based on the above system, preferably, the concentration device I is also provided with a heating device before, and the heating is used for improving the solubility of sodium carbonate in water and also improving the concentration of sodium carbonate in the concentrated solution of the concentration device I.
Based on the above system, preferably, the PH-lowering device, the solid-liquid separation device or the PH-lowering solid-liquid separation device is further provided with a cooling device, so that the solubility of sodium bicarbonate is reduced, and the separation of sodium bicarbonate is more thorough, namely the removal from liquid is more thorough.
Based on the above system, preferably, a cooling device is further arranged between the concentrated solution discharge port of the concentrating device I and the water inlet of the PH-lowering device, or between the discharge port of the PH-lowering device and the water inlet of the solid-liquid separation equipment, or between the concentrated solution discharge port of the concentrating device I and the PH-lowering solid-liquid separation equipment, or between the concentrating device I and the PH-lowering solid-liquid separation equipment, or the concentrating device I and the PH-lowering solid-liquid separation equipment, so that the solubility of sodium bicarbonate is reduced, and the more thorough separation of sodium bicarbonate is facilitated.
Based on the above system, it is preferable that the organic matter removal apparatus includes a gas incinerator (RTO) device, a gas organic matter catalytic decomposition processor (refer to decomposing organic matter), a gas organic matter adsorber, and the like.
Based on the above system, preferably, the gaseous organic matter adsorber mainly includes a resin adsorption tank (filled with a resin having an adsorption effect on organic matter), an activated carbon adsorption tank (filled with activated carbon), a molecular sieve adsorption tank, and the like.
Based on the above system, it is preferable that a catalyst is further added to the gas catalytic decomposition processor.
Based on the above system, preferably, a heat recovery device is further arranged between the gas outlet of the organic matter removal device and the gas inlet of the washing tower I.
Based on the above system, preferably, the organic matter removal apparatus is provided with a heat recovery device.
Based on the above system, preferably, the heat recovery device is a heat exchange device, that is, uses heat generated by catalysis or incineration to heat substances to be heated, so as to realize heat recovery and utilization.
Based on the above system, preferably, a cooling device is further arranged between the gas outlet of the organic matter removing device and the gas inlet of the washing tower I.
Based on the above system, preferably, the organic matter removing device is provided with a cooling device.
Based on the above system, preferably, the cooling device is a heat exchange device, i.e. the temperature of the gas is reduced, and the temperature of the gas entering the washing tower I is reduced.
Based on the above system, preferably, the carbon dioxide generator is preferably a carbon dioxide generating tank or a carbon dioxide generating tower.
Based on the above system, preferably, the carbon dioxide generator comprises a carbon dioxide generating tank or a carbon dioxide generating tower, and also comprises a decarbonization tower, and a liquid outlet of the tank or tower is connected to a water inlet of the decarbonization tower.
Based on the above system, preferably, the carbon dioxide generator is provided with a water inlet and a liquid discharge port, and is also provided with an exhaust port for discharging carbon dioxide gas.
Based on the above system, preferably, the carbon dioxide generator is provided with an air inlet for blowing out carbon dioxide gas.
Based on the above system, preferably, the PH-lowering device is an acid-base neutralization reaction tank or an acid-base neutralization reaction tower.
Based on the above system, preferably, a concentration device II and/or a concentration device III are further provided, wherein the liquid discharge port of the washing tower I is connected to the water inlet of the concentration device II, and the concentrated liquid outlet of the concentration device II is connected to the water inlet of the carbon dioxide generator; the liquid discharge port of the carbon dioxide generator is connected to the water inlet of the concentrating device III, and the concentrated solution outlet of the concentrating device III is connected to the water inlet of the bipolar membrane electrodialysis equipment, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator or the water inlet of the volatile acid generator;
the purpose of the concentrating device II and/or the concentrating device III is to concentrate, since the subsequent treatment requires an increase in the concentration of the aqueous solution.
Based on the system, the system is preferably further provided with an alkalization reactor I, wherein the alkalization reactor I is arranged between a liquid discharge port of the washing tower I and a water inlet of the concentration device I;
The purpose of the alkalization reactor I is to raise the pH of the aqueous solution in the alkalization reactor I, react with alkali, and convert the bicarbonate into carbonate, and because of the high solubility of sodium carbonate, the sodium carbonate can be concentrated by a high multiple (relative ratio of bicarbonate) through the concentration device I without precipitation in the concentration device I.
Based on the above system, preferably, a reducing agent reactor is further provided;
the reducing agent reactor is arranged between a liquid discharge port of the washing tower I and a water inlet of the carbon dioxide generator; or the reducing agent reactor is arranged between the liquid discharge port of the washing tower I and the water inlet of the concentrating device II; or the reducing agent reactor is arranged between a concentrated solution outlet of the concentrating device II and a water inlet of the carbon dioxide generator;
or the reducing agent reactor is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the concentrating device III;
or the reducing agent reactor is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
Or the reducing agent reactor is arranged between a concentrated solution outlet of the concentrating device III and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
or the reducing agent reactor is arranged between the liquid discharge port of the washing tower I and the water inlet of the concentrating device I; or the reducing agent reactor is arranged between the liquid discharge port of the washing tower I and the water inlet of the alkalization reactor I; or the reducing agent reactor is arranged between the water outlet of the alkalization reactor I and the water inlet of the concentration device I; or the reducing agent reactor is arranged between a concentrated solution discharge port of the concentrating device I and the PH reducing device; or the reducing agent reactor is arranged between the discharge port of the PH-reducing device and the water inlet of the solid-liquid separation equipment;
or the reducing agent reactor is arranged between a liquid outlet of the solid-liquid separation device and a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
Or the reducing agent reactor is arranged between a concentrated solution discharge port of the concentrating device I and a water inlet of the PH-lowering solid-liquid separation device; or the reducing agent reactor is arranged between a liquid outlet of the PH-lowering solid-liquid separation device and a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
the purpose of the reductant reactor is to react the oxidant in the aqueous solution with the reductant in the reductant reactor to reduce the damage of the oxidant to subsequent systems (e.g., the membrane system needs to control the oxidant of the feed water, which is detrimental to the membrane system).
Based on the above system, preferably, the reducing agent reactor refers to a device for reducing the oxidability of a water body by using a reducing agent, and is further provided with a reducing agent adding inlet for adding the reducing agent.
Based on the above system, it is preferable that the reducing agent such as sulfite, bisulfite, formic acid, formate (e.g., sodium formate), and the like is a substance having reducing property.
Based on the above system, preferably, a temperature raising device is further provided, and the temperature raising device is arranged between the liquid discharge port of the washing tower I and the water inlet of the reducing agent reactor; or the temperature rising device is arranged between a concentrated solution outlet of the concentrating device II and a water inlet of the reducing agent reactor; or the heating device is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the reducing agent reactor; or the temperature rising device is arranged between a concentrated solution outlet of the concentrating device III and a water inlet of the reducing agent reactor; or the heating device is arranged between the water outlet of the alkalization reactor I and the water inlet of the reducing agent reactor; or the heating device is arranged between a concentrated solution outlet of the concentrating device I and a water inlet of the reducing agent reactor; or the temperature rising device is arranged between the discharge port of the PH reducing device and the water inlet of the reducing agent reactor; or the heating device is arranged between a liquid outlet of the solid-liquid separation equipment and a water inlet of the reducing agent reactor; or the temperature rising device is arranged between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the reducing agent reactor.
Based on the above system, preferably, the temperature raising means refers to a means for heating and raising the temperature.
Based on the above system, preferably, the temperature raising device is arranged to raise the temperature of the aqueous solution, and the raising of the temperature is favorable for raising the reaction speed or efficiency of the reducing agent and for reducing the oxidability of the water body.
Based on the above system, it is preferable that the temperature raising means such as a temperature raising heat exchanger or the like.
Based on the above system, it is preferable that the temperature rising heat exchanger be such as a tube heat exchanger, a plate heat exchanger, or the like.
Based on the system, preferably, an alkalization reactor II is further arranged between the water outlet of the reducing agent reactor and the water inlet of the concentration device II; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the carbon dioxide generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the concentration device III; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the bipolar membrane electrodialysis; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the crystallization system I; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the electrolysis device; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the simple substance generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the volatile acid generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the concentration device I; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the PH-lowering device; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the solid-liquid separation equipment; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the PH-lowering solid-liquid separation device.
Based on the above system, it is preferable that the main purpose of the alkalization reactor II is to reduce the oxidability of the water again by alkali liquor, for example, the oxidation property is reduced by the reaction of elemental bromine (having oxidability) with alkali liquor.
Based on the above system, preferably, the carbon dioxide generator further has an acid adding port I; or the PH-lowering device is also provided with an acid adding port II; or the PH-lowering solid-liquid separation equipment is also provided with an acid adding port III; or the alkalization reactor I is provided with an alkali adding port I; or the alkalization reactor II is provided with an alkali adding port II; or the washing tower I is provided with an alkali adding port III.
Based on the above system, preferably, the exhaust port of the carbon dioxide generator is connected to the air inlet of the washing tower II, and is used for reacting carbon dioxide to generate sodium carbonate and/or sodium bicarbonate.
Based on the above system, preferably, the washing tower II is provided with an alkali adding port IV.
Based on the above system, preferably, the scrubber II has an exhaust port.
Based on the above system, preferably, the washing tower II is provided with a water supplementing port.
Based on the above system, preferably, the washing tower II has a liquid discharge port.
Based on the above system, preferably, the liquid discharge port of the washing column II is discharged.
Based on the above system, preferably, the liquid discharge port of the washing tower II is connected to the alkali adding port III of the washing tower I or the alkali adding port IV of the washing tower II, namely sodium carbonate is used as an adsorbent for carbon dioxide reaction to generate sodium bicarbonate.
Based on the above system, preferably, the liquid discharge of the washing column II is connected to the crystallization system II, resulting in a solid containing sodium carbonate and/or sodium bicarbonate.
Based on the above system, preferably, the liquid discharge port of the washing tower II is connected to an organic acid dissolution system (for example, an organic acid dissolution system), a heavy metal recovery system (for reacting with heavy metal cations to generate insoluble matters), an alkali adding port III of the washing tower I or an alkali adding port IV of the washing tower II (namely, sodium carbonate is used as an adsorbent for reacting with carbon dioxide to generate sodium bicarbonate).
Based on the above system, preferably, the liquid discharge port of the washing column II is connected to the water inlet of an alkalization reactor V in which sodium bicarbonate is converted into sodium carbonate, and the water outlet of the alkalization reactor V is connected to an organic acid dissolution system (e.g., an organic acid dissolution system), a crystallization system III, a heavy metal recovery system (for reacting with heavy metal cations to form insoluble matters), an alkali addition port III of the washing column I or an alkali addition port IV of the washing column II (i.e., sodium carbonate is used as an adsorbent for carbon dioxide reaction to form sodium bicarbonate).
Based on the above system, preferably, the liquid discharge port of the washing tower II is connected to the water inlet of the concentrating device IV, and the concentrated solution outlet of the concentrating device IV is connected to an organic acid dissolving system (such as an organic acid dissolving system), a heavy metal recovery system (for reacting with heavy metal cations to generate insoluble matters), the alkali adding port III of the washing tower I or the alkali adding port IV of the washing tower II (namely, sodium carbonate is used as an adsorbent for reacting carbon dioxide to generate sodium bicarbonate).
Based on the above system, preferably, the liquid discharge port of the washing tower II is connected to the water inlet of an alkalization reactor V, sodium bicarbonate is converted into sodium carbonate in the alkalization reactor V, the water outlet of the alkalization reactor V is connected to the water inlet of a concentration device IV, and the concentrated solution outlet of the concentration device IV is connected to an organic acid dissolving system (such as an organic acid dissolving system), a heavy metal recovery system (for reacting with heavy metal cations to generate insoluble matters), a crystallization system III, an alkali adding port III of the washing tower I or an alkali adding port IV of the washing tower II (namely sodium carbonate is used as an adsorbent for carbon dioxide reaction to generate sodium bicarbonate).
Based on the above system, preferably, the liquid discharge port of the washing tower II is connected to the water inlet of the concentrating device IV, sodium bicarbonate is converted into sodium carbonate in the alkalization reactor V, the concentrated solution outlet of the concentrating device IV is connected to the water inlet of the alkalization reactor V, and the water outlet of the alkalization reactor V is connected to an organic acid dissolving system (such as an organic acid dissolving system), a heavy metal recovery system (for reacting with heavy metal cations to generate insoluble matters), a crystallization system III, an alkali adding port III of the washing tower I or an alkali adding port IV of the washing tower II (namely sodium carbonate is used as an adsorbent for carbon dioxide reaction to generate sodium bicarbonate).
Based on the above system, preferably, the alkalization reactor v has an alkali addition port v.
Based on the above system, it is preferable that the organic acid dissolution system means dissolution by reacting sodium bicarbonate and/or sodium carbonate with an organic substance (e.g., an organic acid).
Based on the above system, preferably, the organic acid dissolved by the organic acid dissolution system is oxidation residue of oxidation reaction of terephthalic acid factory, and mainly contains heavy metals such as organic acid and cobalt manganese.
Based on the above system, preferably, the heavy metal recovery system refers to the use of sodium bicarbonate and/or sodium carbonate to react with heavy metal ions to form insoluble matter for precipitation.
Based on the above system, preferably, the concentrating device i, the concentrating device ii, the concentrating device iii, or the concentrating device iv means a device for concentrating an aqueous solution.
Based on the above system, preferably, the concentrating device I is a reverse osmosis concentrating device I, an electrodialysis concentrating device I or an evaporation concentrating device I; the concentrating device II is a reverse osmosis concentrating device II, an electrodialysis concentrating device II or an evaporation concentrating device II; the concentrating device III is a reverse osmosis concentrating device III, an electrodialysis concentrating device III or an evaporation concentrating device III; the concentrating device IV is a reverse osmosis concentrating device IV, an electrodialysis concentrating device IV or an evaporation concentrating device IV.
Based on the above system, preferably, the evaporation concentration device i, the evaporation concentration device ii, and the evaporation concentration device iii; or the evaporation concentration device IV comprises an evaporation concentration tower, a reboiler and a cooler.
Based on the above system, preferably, the fresh water outlet or the steam condensate outlet of the concentrating device i, the concentrating device ii, the concentrating device iii or the concentrating device iv is connected to the water replenishing pipe of the washing tower i and/or the water replenishing pipe of the washing tower ii.
Based on the system, a filtering device is preferably arranged at any position and is used for filtering and reducing SS and turbidity of the water body.
Based on the above system, it is preferable that a cooling device is further provided at an arbitrary position for protecting the subsequent stage (e.g., membrane system) from operating to lower or control the temperature.
Based on the above system, preferably, the washing tower I or the washing tower II comprises a spray washing tower, a circulating spray washing tower, a gas adsorption tank and other devices capable of washing gas.
Based on the above system, preferably, the gas adsorption tower is preferably a gas adsorption tank, and is provided with a gas inlet and a gas outlet, i.e. the gas is directly led below the liquid surface for adsorption, such as a water sealed tank.
Based on the above system, preferably, the target gas treated by the present utility model, such as terephthalic acid plant tail gas, is treated by the organic matter removal device to reduce the amount of organic matters therein (generally RTO incineration, catalytic oxidation, etc.), the rest of the tail gas mainly contains hydrogen bromide and carbon dioxide generated in the process of the RTO incineration or catalytic oxidation (and carbon dioxide originally contained in the tail gas), and the alkaline absorption liquid (exemplified by sodium hydroxide) is used in the washing tower i to obtain a mixed aqueous solution of sodium carbonate, sodium bicarbonate and sodium bromide.
Based on the above system, preferably, the oxidation reaction system is an oxidation reaction system for producing terephthalic acid, and paraxylene is reacted with oxygen in the feed air to produce terephthalic acid, acetic acid is used as a solvent in the process, cobalt manganese bromine is used as a three-way catalyst, and part of bromine is sourced from hydrobromic acid.
Based on the above system, preferably, the reverse osmosis concentration device at least comprises a reverse osmosis membrane of one stage and one section, and may also comprise a reverse osmosis membrane combination of one stage and multiple sections or a reverse osmosis membrane combination of one stage and a reverse osmosis membrane combination of multiple stages and multiple sections.
Based on the above system, preferably, the fresh water produced by the bipolar membrane electrodialysis device is circulated back to any position of the process according to the utility model, mainly to any position of the water inlet of the washing tower I, the water inlet of the reducing agent reactor, the water inlet of the alkalization reactor I, the water inlet of the carbon dioxide generator, the water inlet of the concentration device I, the water inlet of the concentration device II, the water inlet of the concentration device III, and the like.
Based on the above system, preferably, the crystallization system I or the crystallization system II is a system for evaporating and crystallizing an aqueous solution to obtain a solid.
Based on the above system, preferably, the crystallization system I or the crystallization system II comprises an evaporation tower, a heater and a second solid-liquid separation device, wherein a discharge hole of the evaporation tower is connected to an inlet of the second solid-liquid separation device, and the heater is used for heating liquid of the evaporation tower.
Based on the above system, it is preferable that the evaporation column (including the heater) of the crystallization system I or the crystallization system II is, for example, a single effect evaporator, a multiple effect evaporator, MVR, or the like.
Based on the above system, preferably, between the liquid outlet of the solid-liquid separation device and the water inlet of the bipolar membrane electrodialysis device, between the liquid outlet of the solid-liquid separation device and the water inlet of the crystallization system i, between the liquid outlet of the solid-liquid separation device and the water inlet of the simple substance generator, between the liquid outlet of the solid-liquid separation device and the water inlet of the volatile acid generator, between the liquid outlet of the reducing agent reactor and the water inlet of the bipolar membrane electrodialysis device, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the crystallization system i, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the electrolysis device, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the simple substance generator, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the volatile acid generator, between the water outlet of the reducing agent reactor and the water inlet of the bipolar membrane electrodialysis device, between the reducing agent reactor and the water inlet of the reducing agent generator or between the reducing agent reactor and the water inlet of the reducing agent generator and the water inlet of the reducing agent reactor and the water inlet of the reducing agent reactor:
The device is provided with an alkalization reactor III and a nanofiltration membrane group, wherein the water outlet of the alkalization reactor III is connected to the water inlet of a high-pressure pump, the water outlet of the high-pressure pump 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 equipment, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator or the water inlet of the volatile acid generator;
or an alkalization reactor III and a purification monovalent ion type electrodialysis device are arranged, wherein the water outlet of the alkalization reactor III is connected to the water inlet of the purification monovalent ion type electrodialysis device, and the water outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or an acidification tank is arranged, and the outlet of the acidification tank is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
Or an acidification tank and a decarbonization tower' are arranged, the outlet of the acidification tank is connected to the water inlet of the decarbonization tower, and the water outlet of the decarbonization tower is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or a salt separation unit is arranged, and the water outlet of the salt separation unit is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
Based on the above system, preferably, the electrodialysis device for purifying monovalent ions refers to a novel electrodialysis device with special effect, which is derived from conventional electrodialysis devices, and can obtain a salt solution mainly comprising monovalent cations and monovalent anions from an aqueous solution containing monovalent ions, divalent ions or more from an inlet, 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 refers to the outlet of a salt (e.g., an aqueous solution containing cobalt ions, manganese ions) consisting essentially of divalent cations or divalent anions, which is an aqueous solution of ions that do not permeate the membrane.
Based on the above system, preferably, the alkalization reactor III is provided with an alkalization port VI;
or the alkalization reactor III is provided with an alkali adding port VI and a water adding port;
or the salt separation unit comprises an evaporator ', a cooler', a solid-liquid separation device ', wherein a material discharge port of the evaporator' is connected to an inlet of the cooler ', an outlet of the cooler' is connected to an inlet of the solid-liquid separation device ', and a liquid outlet of the solid-liquid separation device' is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor.
Based on the above system, preferably, the solid-liquid separation device' refers to a device for separating materials to obtain solids and filtrate.
Based on the above system, preferably, an acidification tank I is arranged between the fresh water outlet of the nanofiltration membrane group and the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
Based on the above system, preferably, an acidification tank II is further arranged between the water outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
Based on the above system, preferably, an alkalization reactor IV is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the crystallization system I, or between a water outlet of the reducing agent reactor and a water inlet of the crystallization system I, or between an outlet of the acidification tank and a water inlet of the crystallization system I.
Based on the above system, preferably, the alkalization reactor IV is provided with an alkali adding port VII.
Based on the above system, preferably, the most dominant device in the nanofiltration membrane group is a nanofiltration membrane, the nanofiltration membrane is a membrane capable of intercepting divalent and more than divalent ions (refer to cations and/or anions) under pressure, the divalent and more than divalent ions (refer to cations and/or anions) are intercepted on a concentrate side, and a dilute side is a salt solution composed of monovalent cations and monovalent anions which mainly penetrate through the nanofiltration membrane; for example, if sodium carbonate and sodium bromide are contained in water, the nanofiltration fresh water is mainly sodium bromide aqueous solution, and the nanofiltration concentrated water is mainly sodium carbonate aqueous solution and also contains a little sodium bromide.
Based on the above system, preferably, the fresh water outlet of the nanofiltration membrane group is connected to the water inlet of the bipolar membrane electrodialysis, the water inlet of the crystallization system i, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
Based on the above system, preferably, the water outlet I of the purification monovalent ion electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
Based on the above system, preferably, the solid outlet of the solid-liquid separation device, the solid outlet of the PH-lowering solid-liquid separation device or the solid outlet of the solid-liquid separation device' is connected to the water inlet of the alkalization reactor v, i.e., sodium bicarbonate is converted into sodium carbonate in the alkalization reactor v.
Based on the above system, preferably, the alkalization reactor v is further provided with an alkali adding port v and/or a water adding port.
Based on the above system, preferably, the water outlet of the alkalization reactor v, the concentrated water outlet of the nanofiltration membrane group or the water outlet ii of the purification monovalent ion electrodialysis device is connected to an organic matter dissolving unit (for example, an organic acid dissolving system), a heavy metal recovery system (for reacting with heavy metal cations to generate insoluble matters), a crystallization system iii, an alkali adding port iii of the washing tower i or an alkali adding port iv of the washing tower ii (i.e., sodium carbonate is used as an adsorbent for reacting with carbon dioxide to generate sodium bicarbonate).
Based on the above system, preferably, the exhaust port of the carbon dioxide generator is connected to the air inlet of the scrubber II;
or the exhaust port of the carbon dioxide generator is connected to the air inlet of the washing tower II, and the liquid discharge port of the washing tower II is connected to the crystallization system II;
or the exhaust port of the carbon dioxide generator is connected to the air inlet of the washing tower II, and the liquid discharge port of the washing tower II is connected to the organic acid dissolving system or the heavy metal recovery system; or the exhaust port of the carbon dioxide generator is connected to the air inlet of the washing tower II, and the liquid discharge port of the washing tower II is connected to the water inlet of the alkalization reactor V;
or the solid outlet of the solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the solid-liquid separation device is connected to the organic acid dissolution system or the heavy metal recovery system;
or the solid outlet of the PH-lowering solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the PH-lowering solid-liquid separation device is connected to the organic acid dissolution system or the heavy metal recovery system;
or the solid outlet of the solid-liquid separation device' is connected to the inlet of the alkalization reactor V; or the solid outlet of the solid-liquid separation device' is connected to the organic acid dissolution system or the heavy metal recovery system.
Based on the above system, preferably, the carbon dioxide generator further has an acid adding port I; or the PH-lowering device is also provided with an acid adding port II; or the PH-lowering solid-liquid separation equipment is also provided with an acid adding port III; or the alkalization reactor I is provided with an alkali adding port I; or the alkalization reactor II is provided with an alkali adding port II; or the alkalization reactor III is provided with an alkalization port VI; or the washing tower I is provided with an alkali adding port III; or the washing tower II is provided with an alkali adding port IV; or the alkalization reactor V is provided with an alkali adding port V.
Based on the above system, preferably, the outlet of the alkalization reactor v is connected to the organic acid dissolving system or the heavy metal recovery system; or the outlet of the alkalization reactor V is connected to an alkali adding port III of the washing tower I; or the outlet of the alkalization reactor V is connected to an alkali adding port IV of the washing tower II; or the outlet of the alkalization reactor V is connected to a crystallization system III;
or the concentrated water outlet of the nanofiltration membrane group is connected with the organic acid dissolving system, the heavy metal recovery system, the alkali adding port III of the washing tower I, the alkali adding port IV of the washing tower II or the crystallization system III;
or the water outlet II of the purification monovalent ion electrodialysis device is connected with the organic acid dissolution system, the heavy metal recovery system, the alkali adding port III of the washing tower I, the alkali adding port IV of the washing tower II or the crystallization system III;
The solid outlet of the solid-liquid separation device is connected with the organic acid dissolution system, the heavy metal recovery system, the alkali adding port III of the washing tower I, the alkali adding port IV of the washing tower II or the crystallization system III.
Based on the above system, it is preferable that the crystallization system III is an apparatus that can evaporate and crystallize a liquid into a solid product, mainly comprising an evaporator and a solid-liquid separation apparatus (e.g., a centrifuge, etc.).
Based on the above system, preferably, the alkalization reactor I, the alkalization reactor II, the alkalization reactor III, the alkalization reactor IV, and the alkalization reactor V refer to a device for raising the pH of an aqueous solution to increase the alkalinity.
Based on the above system, preferably, the acid generator tank outlet of bipolar membrane electrodialysis, the acid generator tank outlet of the electrolysis apparatus, the acid generator tank outlet of the simple substance generator, or the acid generator tank outlet of the volatile acid generator is connected to at least one of the acid addition port i, the acid addition port ii, the acid addition port iii, the acid addition port of the acidification tank, or a discharge port (collecting as a product); the outlet of the alkali producing tank of the bipolar membrane electrodialysis is connected to at least one of an alkali adding port I, an alkali adding port II, an alkali adding port III, an alkali adding port IV, an alkali adding port V, an alkali adding port VI or a discharge port (collecting as a product).
Based on the above system, preferably, the method can be used for achieving the purposes of gas crystallization and recovery of valuable substances in the gas: the gas organic matter removing device is provided with a gas inlet (namely a target gas source treated by the utility model), and after the gas treated by the gas organic matter removing device is washed by the washing tower I, the effluent of the washing tower I is treated by the following method:
the method comprises the following steps: the concentrated water (sodium carbonate as a main component) of the first nanofiltration membrane group is recycled back to the washing tower I to be used as an adsorbent (sodium carbonate reacts with carbon dioxide in gas to generate sodium bicarbonate, sodium carbonate reacts with hydrobromic acid to generate sodium bromide), or the concentrated water (sodium carbonate as a main component) of the first nanofiltration membrane group is mixed with sodium hydroxide to be used as the adsorbent of the washing tower I), or other sodium carbonate users (such as an organic acid dissolving system (such as dissolution of oxidized residues), or a heavy metal recovery system (such as recovery of cobalt and manganese ions to form cobalt carbonate and manganese carbonate insoluble matters) are used as the adsorbent, and the fresh water of the first nanofiltration membrane group is connected to a water inlet of bipolar membrane electrodialysis equipment I, a water inlet of a crystallization system I, a water inlet of an electrolysis device I, a water inlet of an elemental generator I or a water inlet of a volatile acid generator I for treatment; before the effluent of the washing tower I enters the nanofiltration membrane group I, liquid alkali can be added to raise the pH value to convert bicarbonate into carbonate, so that the retention quantity of the nanofiltration membrane group I (the retention of divalent ions of the nanofiltration membrane group I, namely the divalent ions of the water quality are carbonate ions) is improved; or the discharged liquid of the washing tower I can be added with a reducing agent to reduce the oxidability in water (if the water is oxidability, the damage to a subsequent membrane system is caused) before entering the nanofiltration membrane group I, then added with liquid caustic soda to convert bicarbonate into carbonate, and the retention amount of the nanofiltration membrane group I is increased (the divalent ions are retained by the nanofiltration membrane group I- - - -the divalent ions of the water are carbonate ions); and in the process, a concentration system (such as reverse osmosis concentration, electrodialysis concentration, evaporation concentration) and/or a filtration system (such as a bag filter, a cartridge filter, ultrafiltration and the like) are designed according to the needs, so that in order to avoid the influence of carbon dioxide generated by the source water with carbonate and/or bicarbonate on the operation in bipolar membrane electrodialysis equipment and the like, the source water can be neutralized with acid in advance, and carbon dioxide gas can be released.
The second method is as follows: the water outlet II of the purification monovalent electrodialysis device II (namely, the water outlet mainly of divalent ions (carbonate ions)) is recycled back to the washing tower I to serve as an adsorbent (sodium carbonate reacts with carbon dioxide in gas to generate sodium bicarbonate and sodium carbonate reacts with hydrobromic acid to generate sodium bromide), or the water outlet II of the purification monovalent electrodialysis device II (mainly of sodium carbonate) and sodium hydroxide are mixed to serve as the adsorbent of the washing tower I, or other sodium carbonate users (such as an organic acid dissolving system (such as dissolution of oxidized residues), or a heavy metal recycling system (such as cobalt and manganese ions recycling to form cobalt carbonate and manganese carbonate insoluble substances) are used as the adsorbent), and the water outlet I of the purification monovalent electrodialysis device II (namely, the water outlet mainly of monovalent ions (bromide ions)) is connected to the water inlet of the bipolar membrane electrodialysis device II, the water inlet of the crystallization system II, the water inlet of the electrolysis device II, the water inlet of the simple substance generator II or the water inlet of the volatile acid generator II for treatment; wherein, before the effluent of the washing tower I enters the purification monovalent electrodialysis device II, liquid alkali can be added to raise the PH so as to convert bicarbonate into carbonate, so as to raise the interception amount of the purification monovalent electrodialysis device II (the purification monovalent electrodialysis device II intercepts divalent ions-the water divalent ions are carbonate ions); or the reducing agent can be added to reduce the oxidability in the water body before the effluent of the washing tower I enters the second electrodialysis device of the purification monovalent type (if the water body has oxidability, the subsequent membrane system is damaged), then the caustic soda is added to raise the PH value to convert bicarbonate into carbonate, so that the retention quantity of the second electrodialysis device of the purification monovalent type (the divalent ions of the water quality are carbonate ions) is improved; and in the process, a concentration system (such as reverse osmosis concentration, electrodialysis concentration, evaporation concentration) and/or a filtration system (such as a bag filter, a cartridge filter, ultrafiltration and the like) are designed according to the needs, so that in order to avoid the influence of carbon dioxide generated by carbonate and/or bicarbonate in source water in the operation of bipolar membrane electrodialysis equipment and the like, the operation can be neutralized by acid in advance, and carbon dioxide gas can be released.
And a third method: the method comprises the steps of evaporating, concentrating, cooling and solid-liquid separating, concentrating a water body by an evaporating system (sodium bicarbonate is converted into sodium carbonate+carbon dioxide, carbon dioxide is discharged), cooling (sodium bromide has higher solubility at the moment when the solubility of sodium carbonate is suddenly reduced along with the temperature reduction in the cooling process), and carrying out solid-liquid separation (such as a centrifugal machine), wherein the obtained solid is a solid mainly comprising sodium carbonate precipitates, and the filtrate is mainly sodium bromide aqueous solution. The obtained solid is a solid mainly comprising sodium carbonate precipitates, and is recycled back to the washing tower I as an adsorbent (or is recycled back to the washing tower I as an adsorbent after being dissolved in water), or the solid (sodium carbonate as a main component) of the solid-liquid separation (such as a centrifuge) is mixed with sodium hydroxide to be used as the adsorbent of the washing tower I (sodium carbonate reacts with carbon dioxide to generate sodium bicarbonate, sodium carbonate reacts with hydrobromic acid to generate sodium bromide), or other sodium carbonate users (such as an organic acid dissolving system (such as dissolution of oxidation residues), or a heavy metal recovery system (such as cobalt and manganese ions are recovered to form cobalt carbonate and manganese carbonate insoluble substances), and the filtrate (mainly sodium bromide aqueous solution) is connected to a water inlet of a bipolar membrane electrodialysis device III, a water inlet of a crystallization system III, a water inlet of an electrolysis device III, a water inlet of an elemental generator III or a water inlet of a volatile acid generator III for treatment; the effluent of the washing tower I can be added with caustic soda to raise pH before entering the evaporation and concentration equipment to convert bicarbonate into carbonate, so that the yield of sodium carbonate can be improved (sodium carbonate and carbon dioxide are converted into sodium carbonate by heating, and the yield of sodium carbonate is reduced by volatilizing carbon dioxide into air), and meanwhile, the problem that excessive carbon dioxide generated by the evaporation and concentration equipment (such as a multi-effect evaporation or MVR evaporator) cannot condense gas is avoided from influencing the operation of an evaporation system; or the reducing agent can be added to reduce the oxidability in the water body before the effluent of the washing tower I enters the evaporation and concentration equipment, and then the caustic soda liquid is added to raise the PH so as to convert bicarbonate into carbonate; and the concentration system (such as reverse osmosis concentration, electrodialysis concentration, evaporation concentration) and/or the filtration system (such as bag filter, cartridge filter, ultrafiltration, etc.) are designed according to the requirements in the process; before the filtrate is treated through the water inlet of the bipolar membrane electrodialysis device III, the water inlet of the crystallization system III, the water inlet of the electrolysis device III, the water inlet of the simple substance generator III or the water inlet of the volatile acid generator III, carbonate ions can be intercepted again by designing a nanofiltration membrane or purifying monovalent electrodialysis device; meanwhile, in order to avoid that carbon dioxide is generated if the source water has carbonate and/or bicarbonate to influence the operation in the operation of the bipolar membrane electrodialysis device III, the bipolar membrane electrodialysis device III can be neutralized by acid in advance, and carbon dioxide gas is released.
That is, an aqueous solution mainly containing sodium carbonate may be used as the adsorbent (or an aqueous solution mainly containing sodium carbonate may be used as the adsorbent in combination with sodium hydroxide), and the adsorbent may react with acidic substances in the gas, for example, HBr to produce sodium bromide, and carbon dioxide to produce sodium bicarbonate.
Based on the above system, preferably, the electrolysis apparatus refers to an apparatus for obtaining elemental bromine by electrolysis using an aqueous solution of sodium bromide.
Based on the above system, it is preferable that the elemental generator means a device for oxidizing bromide ions into elemental bromine with an oxidizing agent.
Based on the above system, it is preferable that the volatile acid generator means an apparatus for converting bromide ions into volatile hydrobromic acid with a non-volatile acid.
Based on the above system, preferably, the crystallization system I, the crystallization system II or the crystallization system III means a device for evaporating a solution to obtain a solid salt.
Based on the above system, it is preferable that the organic acid dissolution system is a device for dissolving solid organic acid (for example, PTA device oxidation residues, main organic acid components are TA, BA) with sodium carbonate and/or sodium bicarbonate.
Based on the above system, it is preferable that the heavy metal recovery system is a device in which heavy metal cations (for example, PTA oxidation residues, cobalt ions, manganese ions, etc. as main heavy metal cation components) are reacted with sodium carbonate and/or sodium bicarbonate to form insoluble matters.
Based on the above system, preferably, the simple substance generator may be a reaction tower or a reaction tank, or even a section of a pipeline for reaction, in which bromine ions are oxidized into bromine simple substances, so that the simple substance generator needs to be added with an oxidant to perform oxidation reaction.
Based on the above system, preferably, the simple substance generator is provided with a gas inlet, and an exhaust port of the simple substance generator is connected to a gas inlet of the absorption tank; or the outlet of the simple substance generator is connected to a blowout tower, and the gas outlet of the blowout tower is connected to the gas inlet of the absorption tank; or the exhaust port of the simple substance generator is connected to the inlet of the condenser (collecting bromine as a product); or the discharge port of the simple substance generator is connected to the inlet of the layering tank, and the bromine outlet of the layering tank is collected or connected to the inlet of the absorption tank.
Based on the above system, it is preferable that,
the simple substance generator is also provided with a feed inlet (oxidant such as chlorine, hydrogen peroxide, sulfuric acid and the like are fed, or acid required by acidification is also fed at the same time, or gas (such as air) is also required to be fed, and the feed inlet can be the same feed inlet or can be a plurality of feed inlets); blowing out elemental bromine from an exhaust port of the elemental generator by using gas, and then absorbing the elemental bromine by using the absorption tank, wherein an absorbent is arranged in the absorption tank;
Or the simple substance generator is also provided with a feed inlet (the feed inlet can be the same feed inlet or a plurality of feed inlets when oxidant such as chlorine, hydrogen peroxide, sulfuric acid and the like is fed or acid needed by acidification is also fed at the same time); the blowing tower is used for feeding gas (such as air), and the gas is used for blowing out the elemental bromine from the exhaust port of the elemental generator and then absorbing the elemental bromine through the absorption tank, wherein the absorption tank is internally provided with an absorbent.
Based on the above system, preferably, the oxidizing agent added in the simple substance generator is a conventional oxidizing agent.
Based on the above system, preferably, the conventional oxidant of the simple substance generator is chlorine, hydrogen peroxide, sulfuric acid, etc.
Based on the above system, preferably, the absorbent is alkali liquor, sulfur dioxide, sodium carbonate, etc.
Based on the above system, preferably, the simple substance generator is further provided with an acid-producing tank or a product tank, when the absorbent of the simple substance generator is sulfur dioxide, the absorption tank is provided with a heating device and/or an air inlet device, and a gas-phase condensing device, and the gas-phase condensing product (filled into the acid-producing tank) is hydrobromic acid; or the absorption tank is discharged to an evaporation tank III, the evaporation tank III is provided with a heating device and a gas phase condensing device, and a condensation product (filled into a product tank) is hydrobromic acid; or the absorption tank is discharged to an evaporation tank III, the evaporation tank III is provided with an oxidant (such as chlorine, hydrogen peroxide or sulfuric acid) inlet and a gas-phase condensing device, and a condensation product (a product tank) is elemental bromine.
Based on the above system, preferably, the electrolysis device comprises an electrolysis anode plate and an electrolysis cathode plate, and the electrolysis device is bromine for generating simple substance by electrolyzing bromine ions under the condition of direct current.
Based on the above system, preferably, the electrolysis device is provided with a gas inlet, and a gas outlet of the electrolysis device is connected to a gas inlet of the absorption tank; or the exhaust port of the electrolysis device is connected to a blowout tower, and the gas outlet of the blowout tower is connected to the gas inlet of the absorption tank; or the exhaust of the electrolyzer is connected to the inlet of the condenser (collecting bromine); the bromine outlet of the electrolysis device is collected or connected to the inlet of the absorption tank; or the discharge port of the electrolysis device is connected to the inlet of the layering tank, and the bromine outlet of the layering tank is collected or connected to the inlet of the absorption tank; or the bromine outlet of the electrolyzer is collected or the bromine outlet of the layering tank is connected to the inlet of an absorber tank (i.e., layering is performed in the electrolyzer).
Based on the above system, it is preferable that,
the gas inlet of the electrolysis device is used for feeding gas (such as air), elemental bromine is blown out from the exhaust port of the elemental generator by using the gas, and then the elemental bromine is absorbed by the absorption tank, and the absorption tank is internally provided with an absorbent.
Based on the above system, preferably, the absorbent is alkali liquor, sulfur dioxide, sodium carbonate, etc.
Based on the above system, preferably, the electrolysis device is further provided with an acid-producing tank or a product tank, and when the absorbent is sulfur dioxide, the absorption tank is provided with a heating device and/or an air inlet device and a gas-phase condensing device, and the condensed product (filled into the acid-producing tank) is hydrobromic acid; or the absorption tank is discharged to an evaporation tank III, the evaporation tank III is provided with a heating device and a gas phase condensing device, and the condensation product (filled into a product tank) is hydrobromic acid.
Based on the above system, preferably, the non-condenser of the gas phase condensing device of the electrolysis device is hydrogen, and the hydrogen is recycled.
Based on the above system, preferably, the volatile acid generator is provided with an acid inlet pipeline, an exhaust port and a liquid outlet; or the volatile acid generator is provided with an acid inlet pipeline, an exhaust port, a liquid outlet, an air inlet and/or a heater.
Based on the above system, preferably, the acid inlet pipe of the volatile acid generator is fed with a non-volatile acid.
Based on the above system, preferably, the acid inlet pipe of the volatile acid generator is fed with a non-volatile acid, such as phosphoric acid, and has the following reaction: sodium bromide + phosphoric acid- & gthydrobromic acid + sodium dihydrogen phosphate, the principle is that the non-volatile acid is used for preparing volatile acid, and hydrobromic acid is prepared and volatilized.
Based on the above system, preferably, hydrobromic acid is discharged from the vent of the volatile acid generator and collected into the acid-producing tank by a condenser.
Based on the above system, preferably, the liquid outlet of the volatile acid generator discharges sodium dihydrogen phosphate, and residual phosphoric acid and sodium bromide.
Based on the above system, it is preferable that the purpose of the air inlet (feed air or inert gas) and/or heater of the volatile acid generator is to facilitate evaporation of hydrobromic acid.
Based on the above system, preferably, the bipolar membrane electrodialysis device mainly comprises a positive electrode plate, a negative electrode plate, a bipolar membrane, a cation selective permeation membrane, an anion selective permeation membrane, a matched power supply, a pump, a tank, a control electric instrument and the like, wherein the bipolar membrane is used for hydrolyzing water into hydrogen ions and hydroxyl ions under the action of an electric field, and under the certain combined arrangement of the bipolar membrane, the cation selective permeation membrane and the anion selective permeation membrane, the cations in the feed liquid are combined with the hydroxyl ions generated by the water electrolysis to generate corresponding alkali (an alkali chamber formed between the membranes); anions in the feed liquid are combined with hydrogen ions generated by water electrolysis to generate corresponding acids (acid chambers formed between the membranes), namely bipolar membrane electrodialysis equipment can convert salts in the feed liquid into two products, namely corresponding acids (in an acid production tank) and corresponding bases (in an alkali production tank).
Based on the above system, preferably, the acid generator outlet of the bipolar membrane electrodialysis, the acid generator outlet of the electrolysis device, the acid generator outlet of the simple substance generator, or the acid generator outlet of the volatile acid generator is connected to at least one of the acid adding port i, the acid adding port ii, the acid adding port iii, the discharge port, the oxidation reaction system (i.e., one of users of acid), the acid adding port of the acidification tank one, or the acid adding port of the acidification tank two.
Based on the above system, preferably, the outlet of the alkali producing tank of the bipolar membrane electrodialysis is connected to at least one of the alkali adding port I, the alkali adding port II, the alkali adding port III, the alkali adding port IV, the alkali adding port V, the alkali adding port VI, the alkali adding port VII or the discharge port. 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.
Based on the above system, preferably, the acidification tank one or the acidification tank two refer to a device for acidifying an aqueous solution.
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 treat the gas by the system, so that the gas is purified, valuable substances in the gas are recovered, and waste is avoided.
Meanwhile, the utility model has simple operation, solves the environmental protection problem, realizes recycling and improves the economic value.
Drawings
Fig. 1: example 1 schematic diagram of a gas cleaning and recycling system;
fig. 2: example 2 schematic diagram of a gas cleaning and recycling system;
fig. 3: example 3 schematic diagram of a gas cleaning and recycling system;
fig. 4: example 4 schematic diagram of a gas cleaning and recycling system;
fig. 5: example 5 schematic diagram of a gas cleaning and recycling system;
fig. 6: a device connection mode schematic diagram of bipolar membrane electrodialysis device;
Fig. 7: schematic diagram of bipolar membrane electrodialysis apparatus;
fig. 8: example 6 schematic diagram of a gas cleaning and recycling system;
fig. 9: example 7 schematic diagram of a gas cleaning and recycling system;
fig. 10: example 8 schematic diagram of a gas cleaning and recycling system;
fig. 11: example 9 schematic diagram of a gas cleaning and recycling system;
legend:
Detailed Description
The target objects treated by the gas cleaning and recycling system in all the following embodiments are as follows: tail gas from terephthalic acid production equipment.
Example 1
As shown in fig. 1, 6 and 7, the system mainly comprises a gas organic matter removal device (incinerator in this embodiment), a scrubber i 004, a reducing agent reactor 015, a reverse osmosis concentration device ii 010, a carbon dioxide generator (carbon dioxide generation tank in this embodiment) 014, a bipolar membrane electrodialysis device 020, a scrubber ii 030, an alkalization reactor v 036, and an organic acid dissolution system (tank in this embodiment) 040.
The gas organic matter removing apparatus (the burner in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (the burner in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water supplementing port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to an inlet of a high pressure pump 029, an outlet of the high pressure pump 029 is connected to a water inlet 011 of a reverse osmosis concentration device II 010, a fresh water outlet 013 of the reverse osmosis concentration device II 010 is connected to the water supplementing port 008 of the washing tower I004 and the water supplementing port 034 of the washing tower II 030, the washing tower II 030 is also provided with an air inlet 031, an air outlet 032, an alkali adding port IV 033 and a liquid discharging port 035, a concentrated solution outlet 012 of the reverse osmosis concentration device II 010 is connected to an air inlet 016 of a carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014, an air inlet 019 and an air outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 are also provided, an air outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to the air inlet 031 of the washing tower II 030, a liquid discharging port 018 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to an air inlet of a bipolar membrane electrodialysis device 020, an acid outlet of the bipolar membrane electrodialysis device 020 is connected to an acid generating tank 021 and an alkali generating tank 022, an outlet of the acid generating tank 021 is connected to an inlet of an acid pump 023, the outlet of the acid pump 023 is connected to an acid addition port I026 of a carbon dioxide generator (a carbon dioxide generation tank in this embodiment) 014 and a product acid line 025, the outlet of the alkali generation tank 022 is connected to the inlet of an alkali pump 024, the outlet of the alkali pump 024 is connected to an alkali addition port III 009 of a washing tower I004, an alkali addition port IV 033 of a washing tower II 030, an alkali addition port V037 of an alkalization reactor V036, a liquid discharge port 035 of the washing tower II 030 is connected to a water inlet of the alkalization reactor V036, a liquid outlet 038 of the alkalization reactor V036 is connected to an inlet of an organic acid dissolution system 040, and the organic acid dissolution system 040 is further provided with an organic acid inlet 039 and a liquid outlet 041.
The fresh water outlet 027 of the bipolar membrane electrodialysis device 020 is connected to the water inlet of the fresh water producing tank 076 of the bipolar membrane electrodialysis device 020, the water outlet of the fresh water producing tank 076 of the bipolar membrane electrodialysis device 020 is connected to the water inlet of the fresh water pump 077, and the water outlet of the fresh water pump 077 is connected to the water inlet 078 of the reducing agent reactor 015.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; then, the produced fresh water is pumped into a reverse osmosis concentration device II 010 by a high-pressure pump 029, the fresh water is pumped into a washing tower I004 and a washing tower II 030 from a fresh water outlet 013, the concentrated solution of the reverse osmosis concentration device II 010 is led into a carbon dioxide generator (carbon dioxide generating tank) 014 from a concentrated solution outlet 012, and the acid produced by a back-stage bipolar membrane electrodialysis device 020 is added into the carbon dioxide generator (carbon dioxide generating tank) 014, and the carbon dioxide is blown out by feeding air into the carbon dioxide generator (carbon dioxide generating tank) 014, the part of the carbon dioxide is adsorbed by the washing tower II 030, and the alkali produced by the back-stage bipolar membrane electrodialysis device 020 is added into the washing tower II 030, and a part of the alkali produced by the back-stage bipolar membrane electrodialysis device 020 is led out and discharged into an alkalization reactor V036, and the liquid (sodium carbonate) in the alkalization reactor V036 is discharged into an organic acid dissolving unit 040 for neutralizing the organic acid in an organic acid inlet 039, and finally the organic acid is discharged from a liquid outlet 041 of the organic acid dissolving system.
The liquid in the carbon dioxide generator (carbon dioxide generation tank) 014 enters the bipolar membrane electrodialysis device 020 to generate hydrobromic acid (charged into the acid-producing tank 021) and sodium hydroxide (charged into the alkali-producing tank 022).
Fresh water from bipolar membrane electrodialysis device 020 is fed into reducing agent reactor 015 through fresh water producing tank 076.
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 020 mainly comprises an electrode plate anode 201, an electrode plate cathode 202, a bipolar membrane 203, a cathode membrane 204, an anode membrane 205, an acid chamber 206, a salt-losing chamber 207, an alkali chamber 208, a polar water chamber 225, a polar water tank 209, a circulating polar water pump 210, a salt-losing water tank 211, a circulating salt-losing 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-producing tank 021, an alkali-producing tank 022 and a fresh water-producing tank 076. 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 a salt-losing water tank (also called a water inlet tank) 211 is connected to an inlet of a circulating salt-losing water pump (also called a water inlet circulating pump) 212, an outlet of the circulating salt-losing water pump 212 is connected to an inlet of a salt-losing chamber 207, and an outlet of the salt-losing chamber 207 is connected to an inlet of the salt-losing water 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. A pure water pipe 217 is connected to an inlet (make-up pure water) of the recycle caustic tank 213, and the recycle caustic tank 213 overflows to the caustic tank 022; 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 021; 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 replenished) of the lost salt water tank 211, and the lost salt water tank 211 overflows to the fresh salt water tank 076.
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 salt-losing chamber 207 move towards the direction of the negative electrode 202 of the electrode plate through the positive film 205 to enter the alkaline chamber 208, and the anions 117 in the salt-losing chamber 207 move towards the direction of the positive electrode 201 of the electrode plate through the negative film 204 to enter the acid chamber 206, so that the ions in the salt-losing chamber 207 are always 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 coming from the salt-losing 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 coming from the salt-losing 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 salt-losing chamber 207 is continuously maintained to flow through the salt-losing tank 211 and the salt-losing circulating pump 212, so that ions in the salt-losing chamber need to be continuously replenished from the water inlet 221, water with low ion concentration is discharged to the dilute brine tank 076, and a partition board is arranged in the salt-losing chamber 211 so as to prevent the water inlet 221 with relatively high concentration from being directly mixed with backwater of the salt-losing circulating pump 212 (relatively low concentration), and the dilute brine tank 076 is led out and discharged from the backwater side of the salt-losing circulating pump 212 (relatively low concentration);
the acid chamber 206 is continuously maintained to flow water in the acid chamber 206 through the circulating acid tank 215 and the circulating acid pump 216, and as the acid concentration in the circulating acid tank 215 is continuously increased, 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 supplied with more volume and continuously overflows to the acid-producing tank 021;
the acid chamber 208 is continuously maintained in the flow of water in the alkali chamber 208 by the circulating alkali tank 213 and the circulating alkali pump 214, and since the alkali concentration in the circulating alkali tank 213 is continuously increased, 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 rate, and the purified water is supplied with a larger volume and continuously overflows to the alkali-producing tank 022;
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 NF270-400/34i, electrodialysis was EX-4S-ED by Hangzhou blue technology Co., ltd, bipolar membrane electrodialysis was EX-4S by Hangzhou blue technology Co., ltd, the reverse osmosis membrane used DuPont' S SW30HRLE-440i, commercially available 5um pore size pp cotton filter cartridges were installed in the security filter, and the monovalent ion type electrodialysis device was a proprietary device provided by Baishibang water treatment (patent numbers 2022204548706, 202220452996X).
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
The concentrate outlet 012 of reverse osmosis concentration device ii 010 (high pressure pump 029 given an outlet pressure of 6 MPa) was sampled and analyzed as follows: bicarbonate= 31537ppm, carbonate=7530 ppm, bromide=5878 ppm;
the liquid discharge 18 of the carbon dioxide generator (carbon dioxide generation tank in this example) 014 was sampled and analyzed (hydrobromic acid fed from the acid generator tank 021 of the bipolar membrane electrodialysis apparatus 020) as follows: ph=3.5, carbonate, bicarbonate, bromide= 75123ppm; and generates a large amount of carbon dioxide gas;
the acid pump 023 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: bromide 10.1%, hydrogen = 1.25mol/L;
the alkaline pump 024 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: sodium ion 4.4%, hydrogen ion=1.93 mol/L;
liquid discharge port 035 of scrubber II 030 samples analysis results: 9811ppm bicarbonate, 1225ppm carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=11.1, 11412ppm carbonate.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is treated by the gas organic matter removing device (the incinerator in the embodiment) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly sodium bromide (acidic and also contains free hydrobromic acid), the hydrobromic acid and sodium hydroxide products can be obtained by the bipolar membrane electrodialysis device 020, the purpose of recycling hydrobromic acid can be achieved, the carbon dioxide converted from bicarbonate and carbonate can be washed by the washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is completely converted into sodium carbonate after alkali addition and can be reused in the dissolution unit of organic acid.
Example 2
As shown in fig. 2, 6 and 7, the system mainly comprises a gas organic matter removal device (incinerator in this embodiment), a washing tower i 004, a reducing agent reactor 015, an electrodialysis concentration device ii 042, a carbon dioxide generator (carbon dioxide generation tank in this embodiment) 014, a bipolar membrane electrodialysis device 020, a washing tower ii 030, an alkalization reactor v 036, and an organic acid dissolution system (tank in this embodiment) 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water supplementing port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to a water inlet of an electrodialysis concentration device II 042, a water outlet I043 (fresh water outlet) of the electrodialysis concentration device II 042 is connected to the water supplementing port 008 of the washing tower I004 and the water supplementing port 034 of the washing tower II 030, the washing tower II 030 is also provided with an air inlet 031, an air outlet 032, an alkali adding port IV 033 and a liquid discharging port 035, a water outlet II 044 (concentrate outlet) of the electrodialysis concentration device II 042 is connected to a water inlet 016 of a carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014, an air inlet 019 and an air outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 are also provided, the air outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to the air inlet 031 of the washing tower II 030, the liquid discharging port 018 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to a water inlet of a bipolar membrane electrodialysis device 020, an acid outlet of the bipolar membrane electrodialysis device 020 is connected to an acid generating tank 021 and an alkali generating tank 022, an outlet of the acid generating tank 021 is connected to an inlet of an acid pump 023, the outlet of the acid pump 023 is connected to an acid addition port I026 of a carbon dioxide generator (a carbon dioxide generation tank in this embodiment) 014 and a product acid line 025, the outlet of the alkali generation tank 022 is connected to the inlet of an alkali pump 024, the outlet of the alkali pump 024 is connected to an alkali addition port III 009 of a washing tower I004, an alkali addition port IV 033 of a washing tower II 030, an alkali addition port V037 of an alkalization reactor V036, a liquid discharge port 035 of the washing tower II 030 is connected to a water inlet of the alkalization reactor V036, a liquid outlet 038 of the alkalization reactor V036 is connected to an inlet of an organic acid dissolution system 040, and the organic acid dissolution system 040 is further provided with an organic acid inlet 039 and a liquid outlet 041.
The fresh water outlet 027 of the bipolar membrane electrodialysis device 020 is connected to the water inlet of the fresh water producing tank 076 of the bipolar membrane electrodialysis device 020, the water outlet of the fresh water producing tank 076 of the bipolar membrane electrodialysis device 020 is connected to the water inlet of the fresh water pump 077, and the water outlet of the fresh water pump 077 is connected to the water inlet 078 of the reducing agent reactor 015.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; and then enters an electrodialysis concentration device II 042, the produced fresh water is pumped to a washing tower I004 and a washing tower II 030 from a water outlet I043, concentrated solution of the electrodialysis concentration device II 042 is led to a carbon dioxide generator (carbon dioxide generating tank) 014 from a water outlet II 044, acid generated by a back bipolar membrane electrodialysis device 020 is added to the carbon dioxide generator (carbon dioxide generating tank) 014, air is fed to the carbon dioxide generator (carbon dioxide generating tank) 014 to blow out carbon dioxide, the carbon dioxide is adsorbed by the washing tower II 030, alkali generated by the back bipolar membrane electrodialysis device 020 is added to the washing tower II 030, the washing tower II 030 is circularly sprayed and washed, a part of the alkali generated by the back bipolar membrane electrodialysis device 020 is led out and discharged to an alkalization reactor V036, liquid (sodium carbonate) in the alkalization reactor V036 is discharged to an organic matter dissolving unit 040 for neutralizing organic acid which is input 039, and finally the liquid is discharged from a liquid outlet 041 of an organic acid dissolving system.
The liquid in the carbon dioxide generator (carbon dioxide generation tank) 014 enters the bipolar membrane electrodialysis device 020 to generate hydrobromic acid (charged into the acid-producing tank 021) and sodium hydroxide (charged into the alkali-producing tank 022).
Fresh water from bipolar membrane electrodialysis device 020 is fed into reducing agent reactor 015 through fresh water producing tank 076.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
the water outlet II 044 of the electrodialysis concentration device II 042 is sampled and analyzed as follows: bicarbonate= 25543ppm, carbonate=6413 ppm, bromide=4998 ppm;
the liquid discharge 18 of the carbon dioxide generator (carbon dioxide generation tank in this example) 014 was sampled and analyzed (hydrobromic acid fed from the acid generator tank 021 of the bipolar membrane electrodialysis apparatus 020) as follows: ph=3.3, carbonate, bicarbonate, bromide= 67678ppm; and generates a large amount of carbon dioxide gas;
The acid pump 023 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: bromide 9.3%, hydrogen = 1.15mol/L;
the alkaline pump 024 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: sodium ion 4.2%, hydrogen ion=1.79 mol/L;
liquid discharge port 035 of scrubber II 030 samples analysis results: 13811ppm of bicarbonate, 1998ppm of carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=11.0, carbonate 16013ppm.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is treated by the gas organic matter removing device (the incinerator in the embodiment) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly sodium bromide (acidic and also contains free hydrobromic acid), the hydrobromic acid and sodium hydroxide products can be obtained by the bipolar membrane electrodialysis device 020, the purpose of recycling hydrobromic acid can be achieved, the carbon dioxide converted from bicarbonate and carbonate can be washed by the washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is completely converted into sodium carbonate after alkali addition and can be reused in the dissolution unit of organic acid.
It was also demonstrated by examples 1 and 2 that the reverse osmosis concentration device ii 010 and the electrodialysis concentration device ii 042 produced the same effect, but they could be used alternatively.
Example 3
As shown in fig. 3, 6 and 7, the system mainly comprises a gas organic matter removal device (incinerator in this embodiment) 001, a washing tower i 004, a reducing agent reactor 015, an evaporation and concentration device ii (including an evaporation and concentration tower 045, a reboiler 046 and a cooler 047), a carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014, a bipolar membrane electrodialysis device 020, a washing tower ii 030, an alkalization reactor v 036 and an organic acid dissolving system (tank in this embodiment) 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water supply port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to an inlet of a water supply pump 048, an outlet of the water supply pump 048 is connected to a water inlet of an evaporation concentration tower 045, the evaporation concentration tower 045 is further provided with a reboiler 046 for heating, a water outlet of the evaporation concentration tower 045 is connected to a water inlet of a discharge pump 049, a water outlet of the discharge pump 049 is connected to a water inlet of a cooler 047, the water outlet of the cooler 047 is connected to the water inlet 016 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014, the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is also provided with a gas inlet 019 and a gas outlet 017, the gas outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to the gas inlet 031 of the washing tower II 030, the washing tower II 030 is also provided with a gas outlet 032, an alkali addition port IV 033 and a liquid discharge port 035, the liquid discharge port 018 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to the water inlet of the bipolar membrane electrodialysis device 020, the acid outlet of the bipolar membrane electrodialysis device 020 is connected to the acid generating tank 021 and the alkali generating tank 022, the outlet of the acid generating tank 021 is connected to the inlet of the acid pump 023, the outlet of the acid pump 023 is connected to an acid addition port I026 of a carbon dioxide generator (a carbon dioxide generation tank in this embodiment) 014 and a product acid line 025, the outlet of the alkali generation tank 022 is connected to the inlet of an alkali pump 024, the outlet of the alkali pump 024 is connected to an alkali addition port III 009 of a washing tower I004, an alkali addition port IV 033 of a washing tower II 030, an alkali addition port V037 of an alkalization reactor V036, a liquid discharge port 035 of the washing tower II 030 is connected to a water inlet of the alkalization reactor V036, a liquid outlet 038 of the alkalization reactor V036 is connected to an inlet of an organic acid dissolution system 040, and the organic acid dissolution system 040 is further provided with an organic acid inlet 039 and a liquid outlet 041.
The fresh water outlet 027 of the bipolar membrane electrodialysis device 020 is connected to the water inlet of the fresh water producing tank 076 of the bipolar membrane electrodialysis device 020, the water outlet of the fresh water producing tank 076 of the bipolar membrane electrodialysis device 020 is connected to the water inlet of the fresh water pump 077, and the water outlet of the fresh water pump 077 is connected to the water inlet 078 of the reducing agent reactor 015.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; the concentrated solution obtained by concentrating the solution in the evaporation and concentration device II (comprising an evaporation and concentration tower 045, a reboiler 046, a steam heating device and a cooler 047) is introduced into a carbon dioxide generator (carbon dioxide generating tank) 014, acid generated by a back-stage bipolar membrane electrodialysis device 020 is added into the carbon dioxide generator (carbon dioxide generating tank) 014, air is introduced into the carbon dioxide generator (carbon dioxide generating tank) 014 to blow out carbon dioxide, the carbon dioxide is adsorbed by a washing tower II 030, alkali generated by the back-stage bipolar membrane electrodialysis device 020 is added into the washing tower II 030, the washing tower II 030 is circularly sprayed and washed, a part of the alkali generated by the back-stage bipolar membrane electrodialysis device 020 is led out, the alkali generated by the back-stage bipolar membrane electrodialysis device 020 is added into the alkalization reactor V036, the liquid (sodium carbonate) in the alkalization reactor V036 is discharged into an organic acid dissolution system 040 for neutralizing the organic acid of an organic acid inlet 039, and finally the organic acid is discharged from a liquid outlet 041 of the organic acid dissolution system 040.
The liquid in the carbon dioxide generator (carbon dioxide generation tank) 014 enters the bipolar membrane electrodialysis device 020 to generate hydrobromic acid (charged into the acid-producing tank 021) and sodium hydroxide (charged into the alkali-producing tank 022).
Fresh water from bipolar membrane electrodialysis device 020 is fed into reducing agent reactor 015 through fresh water producing tank 076.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
cooler 047 sampling analysis was as follows: bicarbonate=25579 ppm, carbonate=17255 ppm, bromide=7554 ppm;
the liquid discharge 18 of the carbon dioxide generator (carbon dioxide generation tank in this example) 014 was sampled and analyzed (hydrobromic acid fed from the acid generator tank 021 of the bipolar membrane electrodialysis apparatus 020) as follows: ph=3.6, carbonate, bicarbonate, bromide=94512 ppm; and generates a large amount of carbon dioxide gas;
the acid pump 023 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: bromide ion 12.8%, hydrogen ion=1.57 mol/L;
The alkaline pump 024 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: sodium ion 3.6%, hydrogen ion=1.56 mol/L;
liquid discharge port 035 of scrubber II 030 samples analysis results: 15312ppm bicarbonate, 2558ppm carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=11.66, 18055ppm carbonate.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is treated by the gas organic matter removing device (the incinerator in the embodiment) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly brominated (acidic and also contains free hydrobromic acid) sodium, the hydrobromic acid and sodium hydroxide products can be obtained by the bipolar membrane electrodialysis device 020, the purpose of recycling hydrobromic acid can be achieved, the carbon dioxide converted from bicarbonate and carbonate can be washed by the washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is completely converted into sodium carbonate after alkali addition and can be reused in the dissolution unit of organic acid.
It was also demonstrated by examples 1, 2 and 3 that the reverse osmosis concentration device ii 010, the electrodialysis concentration device ii 042 and the evaporation concentration device ii have the same effect, and they may be used alternatively.
Example 4
As shown in fig. 4, a system for cleaning and recycling gas mainly comprises a device for removing gaseous organic substances (in this embodiment, an incinerator) 001, a washing tower i 004, a reducing agent reactor 015, a reverse osmosis concentration device ii 010, a carbon dioxide generator (in this embodiment, a carbon dioxide generation tank) 014, a crystallization system i 050, a washing tower ii 030, an alkalization reactor v 036, and an organic acid dissolution system (in this embodiment, an organic acid dissolution tank) 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water supplementing port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to an inlet of a high pressure pump 029, an outlet of the high pressure pump 029 is connected to a water inlet 011 of a reverse osmosis concentration device II 010, a fresh water outlet 013 of the reverse osmosis concentration device II 010 is connected to the water supplementing port 008 of the washing tower I004 and the water supplementing port 034 of the washing tower II 030, the washing tower II 030 is further provided with a gas inlet 031, a gas outlet 032, an alkali addition port IV 033, a liquid discharge port 035, the concentrate outlet 012 of the reverse osmosis concentration device II 010 is connected to the water inlet 016 of the carbon dioxide generator (in this embodiment, the carbon dioxide generating tank) 014, the carbon dioxide generator (in this embodiment, the carbon dioxide generating tank) 014 also has the air inlet 019, the air outlet 017 of the carbon dioxide generator (in this embodiment, the carbon dioxide generating tank) 014 is connected to the air inlet 031 of the washing tower II 030, the liquid discharge 018 of the carbon dioxide generator (in this embodiment, the carbon dioxide generating tank) 014 is connected to the alkalization reactor IV 054, the alkalization reactor IV 054 is also provided with the alkali adding port VII 055, the water outlet of the alkalization reactor IV 055 is connected to the water inlet of the crystallization system I050, the crystallization system I050 includes the evaporator 051 of the crystallization system I050, the heater 052 of the evaporator 051 of the crystallization system I050, centrifuge feed pump 058, solid-liquid separation equipment two (this example is centrifuge 053), centrifuge 053 is equipped with solid outlet 056, filtrate outlet 057 is connected to crystallization system I050's evaporator 051.
The liquid discharge port 035 of the washing column II 030 is connected to the water inlet of the alkalization reactor V036, the alkalization reactor V036 is provided with an alkalization port V037, the liquid outlet 038 of the alkalization reactor V036 is connected to the inlet of the organic acid dissolution system 040, and the organic acid dissolution system 040 is also provided with an organic acid inlet 039 and a liquid outlet 041.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; then the fresh water is pumped into a reverse osmosis concentration device II 010 through a high-pressure pump 029, the produced fresh water is pumped into a washing tower I004 and a washing tower II 030 from a fresh water outlet 013, and the concentrated solution of the reverse osmosis concentration device II 010 is led into a carbon dioxide generator (carbon dioxide generating tank) 014 from a concentrated solution outlet 012;
Hydrobromic acid is added to the carbon dioxide generator (carbon dioxide generation tank) 014, air is added to the carbon dioxide generator (carbon dioxide generation tank) 014 to blow out carbon dioxide, this part of carbon dioxide is adsorbed by the washing column II 030, sodium hydroxide is added to the washing column II 030, the washing column II 030 is circularly spray-washed and a part of the liquid is discharged to the alkalization reactor V036, sodium hydroxide is added to the alkalization reactor V036, the liquid (sodium carbonate) in the alkalization reactor V036 is discharged to the organic matter dissolving unit 040 for neutralizing the organic acid coming in from the organic acid inlet 039, and finally the liquid is discharged from the liquid outlet 041 of the organic acid dissolving system 040.
The liquid in carbon dioxide generator (carbon dioxide generation tank) 014 is fed into alkalization reactor iv 054 to neutralize free hydrobromic acid, after which sodium bromide solid crystals are produced by crystallization system i 050 (concentration by heating with steam) (centrifuge 053 is provided with solid outlet 056).
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
The concentrate outlet 012 of reverse osmosis concentration device ii 010 (high pressure pump 029 given an outlet pressure of 6 MPa) was sampled and analyzed as follows: bicarbonate= 31537ppm, carbonate=7530 ppm, bromide=5878 ppm;
the liquid discharge port 18 of the carbon dioxide generator (carbon dioxide generation tank in this embodiment) 014 is sampled and analyzed as follows: ph=3.5, carbonate, bicarbonate, bromide= 69147ppm; and generates a large amount of carbon dioxide gas;
alkalization reactor iv 054 ph=7
Solid outlet 056 sample analysis of centrifuge 053: sodium bromide concentration 98.2%
Liquid discharge port 035 of scrubber II 030 samples analysis results: 8713ppm bicarbonate, 1113ppm carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=10.9, 9771ppm carbonate.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (the incinerator in this embodiment) 001 is treated by the gas organic matter removing device (the incinerator in this embodiment) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly sodium bromide (acidic and contains free hydrobromic acid), and after the free hydrobromic acid is neutralized by the alkalization reactor IV 054, sodium bromide solid is obtained from the solid outlet 056 of the centrifugal machine 053 by the crystallization system I050. The carbon dioxide converted from bicarbonate and carbonate is washed by a washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is converted into sodium carbonate after alkali addition, so that the sodium carbonate can be reused in a dissolution unit of organic acid.
And it has been demonstrated by examples 1, 2 and 3 that the reverse osmosis concentration device ii 010, the electrodialysis concentration device ii 042 and the evaporation concentration device ii have the same effect, and can be replaced by the electrodialysis concentration device ii 042 or the evaporation concentration device ii, so that the reverse osmosis concentration device ii 010 in this embodiment can be replaced by the evaporation concentration device ii.
Example 5
As shown in fig. 5, the system for cleaning and recycling gas mainly comprises a gas organic matter removal device (in this embodiment, an incinerator) 001, a washing tower i 004, a reducing agent reactor 015, a reverse osmosis concentration device ii 010, a carbon dioxide generator (in this embodiment, a carbon dioxide generation tank) 014, an electrolysis device 059, a washing tower ii 030, an alkalization reactor v 036, and an organic acid dissolution system (in this embodiment, a tank) 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water replenishment port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to an inlet of a high pressure pump 029, an outlet of the high pressure pump 029 is connected to a water inlet 011 of a reverse osmosis concentration device II 010, the fresh water outlet 013 of the reverse osmosis concentration device II 010 is connected to the water supplementing port 008 of the washing tower I004 and the water supplementing port 034 of the washing tower II 030, the washing tower II 030 is further provided with an air inlet 031, a gas outlet 032, an alkali adding port IV 033 and a liquid discharging port 035, the concentrated liquid outlet 012 of the reverse osmosis concentration device II 010 is connected to the water inlet 016 of a carbon dioxide generator (carbon dioxide generating tank in the embodiment), the carbon dioxide generator (carbon dioxide generating tank in the embodiment) 014 is further provided with an air inlet 019, a gas outlet 017 and an acid adding port I026, and the gas outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in the embodiment) 014 is connected to the air inlet 031 of the washing tower II 030;
The liquid discharge port 018 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is connected to the water inlet of the electrolyzer 059, the electrolyzer 059 is further provided with an air inlet 060, an anode 061, a cathode 062, the electrolyzer 060 is further provided with a water discharge port 063, the air discharge port of the electrolyzer 059 is connected to an absorption tank 064, the absorption tank 064 is further provided with a dosing port 065, the outlet of the absorption tank 064 is connected to the inlet of an evaporation tank III 066, the top gas phase of the evaporation tank III 066 is provided with a condenser 067, and the outlet of the condenser 067 is connected to an acid generating tank 021.
The liquid discharge port 035 of the washing column II 030 is connected to the water inlet of the alkalization reactor V036, the alkalization reactor V036 is provided with an alkalization port V037, the liquid outlet 038 of the alkalization reactor V036 is connected to the inlet of the organic acid dissolution system 040, and the organic acid dissolution system 040 is also provided with an organic acid inlet 039 and a liquid outlet 041.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
Washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; then the fresh water is pumped into a reverse osmosis concentration device II 010 through a high-pressure pump 029, the produced fresh water is pumped into a washing tower I004 and a washing tower II 030 from a fresh water outlet 013, and the concentrated solution of the reverse osmosis concentration device II 010 is led into a carbon dioxide generator (carbon dioxide generating tank) 014 from a concentrated solution outlet 012;
hydrobromic acid from the acid generator tank 021 is added to the carbon dioxide generator (carbon dioxide generation tank) 014, air is added to the carbon dioxide generator (carbon dioxide generation tank) 014 to blow out carbon dioxide, this part of the carbon dioxide is adsorbed by the washing tower II 030, sodium hydroxide is added to the washing tower II 030, the washing tower II 030 is circularly sprayed and washed and a part is discharged to the alkalization reactor V036, sodium hydroxide is added to the alkalization reactor V036, the liquid (sodium carbonate) in the alkalization reactor V036 is discharged to the organic acid dissolution system 040 for neutralizing the organic acid coming in from the organic acid inlet 039, and finally the liquid is discharged from the liquid outlet 041 of the organic acid dissolution system 040.
Liquid in a carbon dioxide generator (carbon dioxide generating tank) 014 enters an electrolysis device 059 for treatment, bromine simple substance is generated under the action of an electric field, pressurized air is fed into an air inlet 060 of the electrolysis device 059, simple substance bromine is blown out, simple substance bromine gas is absorbed by an absorption tank 064, sulfur dioxide and water are fed into the absorption tank 064 from a dosing port 065, aqueous solution in the absorption tank 064 is evaporated by an evaporation tank III 066 and then condensed by a condenser 067, and hydrobromic acid aqueous solution is collected into an acid generating tank 021.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
the concentrate outlet 012 of reverse osmosis concentration device ii 010 (high pressure pump 029 given an outlet pressure of 6 MPa) was sampled and analyzed as follows: bicarbonate= 31537ppm, carbonate=7530 ppm, bromide=5878 ppm;
the liquid discharge port 18 of the carbon dioxide generator (carbon dioxide generation tank in this example) 014 was sampled and analyzed (hydrobromic acid supplied from the acid generator tank 021 to which the electrolyzer 059 was added) as follows: ph=3.1, carbonate, bicarbonate, bromide= 88987ppm; and generates a large amount of carbon dioxide gas;
The acid generator 021 of the electrolyzer 059 analyzes the hydrobromic acid concentration of 16.1%.
Liquid discharge port 035 of scrubber II 030 samples analysis results: 18212ppm bicarbonate, 2998ppm carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=11.4, 21556ppm carbonate.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (incinerator in this embodiment) 001 is treated by the gas organic matter removing device (incinerator in this embodiment) 001 and is washed and discharged by the washing tower I004, the produced washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly sodium bromide (acidic and also contains free hydrobromic acid), and the obtained liquid is treated by the electrolysis device 059 to obtain aqueous hydrobromic acid solution. The carbon dioxide converted from bicarbonate and carbonate is washed by a washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is converted into sodium carbonate after alkali addition, so that the sodium carbonate can be reused in a dissolution unit of organic acid.
And it has been demonstrated by examples 1, 2 and 3 that the reverse osmosis concentration device ii 010, the electrodialysis concentration device ii 042 and the evaporation concentration device ii have the same effect, and can be replaced by the electrodialysis concentration device ii 042 or the evaporation concentration device ii, so that the reverse osmosis concentration device ii 010 in this embodiment can be replaced by the evaporation concentration device ii.
Example 6
As shown in fig. 8, a system for cleaning and recycling gas mainly comprises a device for removing organic matters from gas (in this embodiment, an incinerator) 001, a washing tower i 004, a reducing agent reactor 015, a reverse osmosis concentration device ii 010, a carbon dioxide generator (in this embodiment, a carbon dioxide generation tank) 014, a simple substance generator 068, a washing tower ii 030, an alkalization reactor v 036, and an organic acid dissolution system (in this embodiment, a tank) 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water replenishment port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to an inlet of a high pressure pump 029, an outlet of the high pressure pump 029 is connected to a water inlet 011 of a reverse osmosis concentration device II 010, the fresh water outlet 013 of the reverse osmosis concentration device II 010 is connected to the water supplementing port 008 of the washing tower I004 and the water supplementing port 034 of the washing tower II 030, the washing tower II 030 is further provided with an air inlet 031, a gas outlet 032, an alkali adding port IV 033 and a liquid discharging port 035, the concentrated liquid outlet 012 of the reverse osmosis concentration device II 010 is connected to the water inlet 016 of a carbon dioxide generator (carbon dioxide generating tank in the embodiment), the carbon dioxide generator (carbon dioxide generating tank in the embodiment) 014 is further provided with an air inlet 019, a gas outlet 017 and an acid adding port I026, and the gas outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in the embodiment) 014 is connected to the air inlet 031 of the washing tower II 030;
A liquid discharge port 018 of a carbon dioxide generator (a carbon dioxide generation tank in this embodiment) 014 is connected to a water inlet port of the simple substance generator 068; the simple substance generator 068 is also provided with a dosing port 069, the simple substance generator 068 is also provided with a water outlet 070, an exhaust port of the simple substance generator 068 is connected to the absorption tank 064, the absorption tank 064 is also provided with a dosing port 065, an outlet of the absorption tank 064 is connected to an inlet of the evaporation tank III 066, a gas phase at the top of the evaporation tank III 066 is provided with a condenser 067, and an outlet of the condenser 067 is connected to the acid production tank 021.
The liquid discharge port 035 of the washing column II 030 is connected to the water inlet of the alkalization reactor V036, the alkalization reactor V036 is provided with an alkalization port V037, the liquid outlet 038 of the alkalization reactor V036 is connected to the inlet of the organic acid dissolution system 040, and the organic acid dissolution system 040 is also provided with an organic acid inlet 039 and a liquid outlet 041.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
Washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; then the fresh water is pumped into a reverse osmosis concentration device II 010 through a high-pressure pump 029, the produced fresh water is pumped into a washing tower I004 and a washing tower II 030 from a fresh water outlet 013, and the concentrated solution of the reverse osmosis concentration device II 010 is led into a carbon dioxide generator (carbon dioxide generating tank) 014 from a concentrated solution outlet 012;
hydrobromic acid from the acid generator tank 021 is added to the carbon dioxide generator (carbon dioxide generation tank) 014, air is added to the carbon dioxide generator (carbon dioxide generation tank) 014 to blow out carbon dioxide, this part of the carbon dioxide is adsorbed by the washing tower II 030, sodium hydroxide is added to the washing tower II 030, the washing tower II 030 is circularly sprayed and washed and a part is discharged to the alkalization reactor V036, sodium hydroxide is added to the alkalization reactor V036, the liquid (sodium carbonate) in the alkalization reactor V036 is discharged to the organic acid dissolution system 040 for neutralizing the organic acid coming in from the organic acid inlet 039, and finally the liquid is discharged from the liquid outlet 041 of the organic acid dissolution system 040.
The liquid in the carbon dioxide generator (carbon dioxide generating tank) 014 enters the simple substance generator 068, chlorine and sulfuric acid are fed from the dosing port 069, and air with pressure is used for blowing out simple substance bromine, the simple substance bromine gas is absorbed by the absorbing tank 064, sulfur dioxide and water are fed from the dosing port 065 by the absorbing tank 064, and the water solution in the absorbing tank 064 is condensed by the condenser 067 after being evaporated by the evaporating tank III 066 and then is collected in the acid generating tank 021.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
the concentrate outlet 012 of reverse osmosis concentration device ii 010 (high pressure pump 029 given an outlet pressure of 6 MPa) was sampled and analyzed as follows: bicarbonate= 31537ppm, carbonate=7530 ppm, bromide=5878 ppm;
the liquid discharge port 18 of the carbon dioxide generator (carbon dioxide generation tank in this embodiment) 014 is sample-analyzed (hydrobromic acid supplied from the acid generator tank 021 to which the simple substance generator 068 is added) as follows: ph=3.4, carbonate, bicarbonate were undetectable, bromide=71011 ppm; and generates a large amount of carbon dioxide gas;
The acid generator 021 of the electrolyzer 059 analyzes hydrobromic acid concentration 9.8%.
Liquid discharge port 035 of scrubber II 030 samples analysis results: 17005ppm bicarbonate, 2891ppm carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=11.2, 19589ppm carbonate.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (incinerator in this embodiment) 001 is treated by the gas organic matter removing device (incinerator in this embodiment) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly sodium bromide (acidic and also contains free hydrobromic acid), and the aqueous solution of hydrobromic acid is obtained by the treatment of the simple substance generator 068. The carbon dioxide converted from bicarbonate and carbonate is washed by a washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is converted into sodium carbonate after alkali addition, so that the sodium carbonate can be reused in a dissolution unit of organic acid.
And it has been demonstrated by examples 1, 2 and 3 that the reverse osmosis concentration device ii 010, the electrodialysis concentration device ii 042 and the evaporation concentration device ii have the same effect, and can be replaced by the electrodialysis concentration device ii 042 or the evaporation concentration device ii, so that the reverse osmosis concentration device ii 010 in this embodiment can be replaced by the evaporation concentration device ii.
Example 7
As shown in fig. 9, the system for cleaning and recycling gas mainly comprises a device for removing gaseous organic substances (in this embodiment, an incinerator) 001, a washing tower i 004, a reducing agent reactor 015, a reverse osmosis concentration device ii 010, a carbon dioxide generator (in this embodiment, a carbon dioxide generation tank) 014, a volatile acid generator 071, a washing tower ii 030, an alkalization reactor v 036, and an organic acid dissolution system (in this embodiment, a tank) 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower I004, the washing tower I004 is further provided with a gas outlet 006, an alkali addition port III 009, a water replenishment port 008, a liquid discharge port 007 of the washing tower I004 is connected to a water inlet 078 of a reducing agent reactor 015, the reducing agent reactor 015 is further provided with a reducing agent addition inlet 028, a water outlet of the reducing agent reactor 015 is connected to an inlet of a high pressure pump 029, an outlet of the high pressure pump 029 is connected to a water inlet 011 of a reverse osmosis concentration device II 010, the fresh water outlet 013 of the reverse osmosis concentration device II 010 is connected to the water supplementing port 008 of the washing tower I004 and the water supplementing port 034 of the washing tower II 030, the washing tower II 030 is further provided with an air inlet 031, a gas outlet 032, an alkali adding port IV 033 and a liquid discharging port 035, the concentrated liquid outlet 012 of the reverse osmosis concentration device II 010 is connected to the water inlet 016 of a carbon dioxide generator (carbon dioxide generating tank in the embodiment), the carbon dioxide generator (carbon dioxide generating tank in the embodiment) 014 is further provided with an air inlet 019, a gas outlet 017 and an acid adding port I026, and the gas outlet 017 of the carbon dioxide generator (carbon dioxide generating tank in the embodiment) 014 is connected to the air inlet 031 of the washing tower II 030;
A liquid discharge port 018 of a carbon dioxide generator (a carbon dioxide generation tank in this embodiment) 014 is connected to a water inlet port of the volatile acid generator 071; the volatile acid generator 071 is further provided with an acid inlet pipe 072, the volatile acid generator 071 is further provided with a liquid outlet 073 and a heater 074, an exhaust port 075 of the volatile acid generator 071 is connected to a condenser 067, and an outlet of the condenser 067 is connected to an acid generating tank 021.
The liquid discharge port 035 of the washing column II 030 is connected to the water inlet of the alkalization reactor V036, the alkalization reactor V036 is provided with an alkalization port V037, the liquid outlet 038 of the alkalization reactor V036 is connected to the inlet of the organic acid dissolution system 040, and the organic acid dissolution system 040 is also provided with an organic acid inlet 039 and a liquid outlet 041.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is used for introducing the pollutant gas (namely the target object treated by the utility model) into the system, the pollutant gas is introduced into the washing tower I004 after the organic matters are removed by the gas organic matter removing device (the incinerator in the embodiment) 001, and the pollutant gas is discharged from the gas outlet 006 of the washing tower I004 after the pollutant gas is introduced into the washing tower I004 for washing;
Washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, after which a part of the washed liquid is circulated and sprayed and a part of the washed liquid is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding inlet 028 of reducing reactor 015 for reduction reaction; then the fresh water is pumped into a reverse osmosis concentration device II 010 through a high-pressure pump 029, the produced fresh water is pumped into a washing tower I004 and a washing tower II 030 from a fresh water outlet 013, and the concentrated solution of the reverse osmosis concentration device II 010 is led into a carbon dioxide generator (carbon dioxide generating tank) 014 from a concentrated solution outlet 012;
hydrobromic acid from an acid generating tank 021 is added to a carbon dioxide generator (tank) 014, air is added to the carbon dioxide generator (carbon dioxide generating tank) 014 to blow out carbon dioxide, this part of carbon dioxide is adsorbed by a washing tower II 030, sodium hydroxide is added to the washing tower II 030, the washing tower II 030 is circularly sprayed and washed and a part is led out to be discharged to an alkalization reactor V036, sodium hydroxide is added to the alkalization reactor V036, the liquid (sodium carbonate) in the alkalization reactor V036 is discharged to an organic acid dissolution system 040 for neutralizing the organic acid coming in from an organic acid inlet 039, and finally the liquid is discharged from a liquid outlet 041 of the organic acid dissolution system 040.
The liquid in the carbon dioxide generator (carbon dioxide generating tank) 014 enters the volatile acid generator 071, phosphoric acid is supplied to the acid adding pipe 072 and heated, hydrobromic acid is blown out, hydrobromic acid gas is condensed by the condenser 067 and then collected in the acid generating tank 021.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.7, bicarbonate=11037 ppm, carbonate=2512 ppm, bromide=1898ppm, orp=598 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=10998 ppm, carbonate=2507 ppm, bromide=1901 ppm, orp=128 MV;
the concentrate outlet 012 of reverse osmosis concentration device ii 010 (high pressure pump 029 given an outlet pressure of 6 MPa) was sampled and analyzed as follows: bicarbonate= 31537ppm, carbonate=7530 ppm, bromide=5878 ppm;
the liquid discharge port 18 of the carbon dioxide generator (carbon dioxide generating tank in this embodiment) 014 is sampled and analyzed (hydrobromic acid supplied from the acid generating tank 021 to which the volatile acid generator 071 is added) as follows: ph=3.7, carbonate, bicarbonate, bromide= 70030ppm; and generates a large amount of carbon dioxide gas;
The acid generator 021 of the electrolyzer 059 analyzed hydrobromic acid concentration 7.77%.
Liquid discharge port 035 of scrubber II 030 samples analysis results: 21021ppm bicarbonate, 3018ppm carbonate;
the liquid outlet 038 of the alkalization reactor v 036 is analyzed as follows: ph=11.7, 24249ppm carbonate.
Conclusion: the pollutant gas coming from the gas inlet 002 of the gas organic matter removing device (incinerator in this embodiment) 001 is treated by the gas organic matter removing device (incinerator in this embodiment) 001 and is washed and discharged by the washing tower I004, the produced washing liquid is subjected to oxidation removal and concentration, then bicarbonate and carbonate are converted into carbon dioxide, the obtained liquid is mainly sodium bromide (acidic and also contains free hydrobromic acid), and the aqueous solution of hydrobromic acid is obtained by the treatment of the volatile acid generator 071. The carbon dioxide converted from bicarbonate and carbonate is washed by a washing tower II 030 to obtain a mixture of sodium bicarbonate and sodium carbonate again, and the mixture is converted into sodium carbonate after alkali addition, so that the sodium carbonate can be reused in a dissolution unit of organic acid.
And it has been demonstrated by examples 1, 2 and 3 that the reverse osmosis concentration device ii 010, the electrodialysis concentration device ii 042 and the evaporation concentration device ii have the same effect, and can be replaced by the electrodialysis concentration device ii 042 or the evaporation concentration device ii, so that the reverse osmosis concentration device ii 010 in this embodiment can be replaced by the evaporation concentration device ii.
Example 8
As shown in fig. 10, a system for cleaning and recycling gas mainly comprises a gas organic matter removal device (incinerator in this embodiment) 001, a washing tower i 004, a reducing agent reactor 015, an alkalization reactor (tank) i 079, an electrodialysis concentration device i 100, a PH reduction device 085, a solid-liquid separation device (centrifuge) 089, an alkalization reactor (tank) iii 090, a nanofiltration membrane group 093, an acidification tank one 096, a bipolar membrane electrodialysis device 020, an alkalization reactor v 036, and an organic acid dissolution system 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower i 004, the washing tower i 004 is further provided with a gas outlet 006, an alkali addition port iii 009, a water replenishment port 008, a liquid discharge port 007 of the washing tower i 004 is connected to a reducing agent reactor 015, and the reducing agent reactor 015 is further provided with a reducing agent addition port 028;
the water outlet of the reducing agent reactor 015 is connected to the water inlet of an alkalization reactor (tank) I079, the alkalization reactor (tank) I079 is also provided with an alkali adding port I080, the water outlet of the alkalization reactor (tank) I079 is connected to the water inlet of a water supply pump 081 of an electrodialysis concentration device I100, the water outlet of the water supply pump 081 of the electrodialysis concentration device I100 is connected to the water inlet 082 of the electrodialysis concentration device I100, and a fresh water outlet 084 of the electrodialysis concentration device I100 is connected to a water supplementing port 008 of a washing tower I004;
The concentrated solution outlet 083 of the electrodialysis concentration device I100 is connected to the water inlet of the PH reducing device 085, the PH reducing device 085 is also provided with an acid adding port II 086, and the water outlet of the PH reducing device 085 is connected to the water inlet of the solid-liquid separation equipment (centrifugal machine) 087;
the filtrate outlet 088 of the solid-liquid separation device (centrifuge) 087 is connected to the water inlet of the alkalization reactor (tank) iii 090, the alkalization reactor (tank) iii 090 also has an alkalization port vi 091, the water outlet of the alkalization reactor (tank) iii 090 is connected to the water inlet of the high pressure pump 092 of the nanofiltration membrane group 093, and the water outlet of the high pressure pump 092 of the nanofiltration membrane group 093 is connected to the water inlet of the nanofiltration membrane group 093;
the concentrated water outlet 095 of the nanofiltration membrane group 093 is connected to the alkali adding port III 009 of the washing tower I004;
the fresh water outlet 094 of the nanofiltration membrane group 093 is connected to the inlet of the acidification tank one 096, the acidification tank one 096 is also provided with an acid adding port 097 and an exhaust port 099, the outlet 098 of the acidification tank one 096 is connected to the water inlet of the bipolar membrane electrodialysis device 020, the acid outlet of the bipolar membrane electrodialysis device 020 is connected to the acid generating tank 021, the alkali outlet is connected to the alkali generating tank 022, the outlet of the acid generating tank 021 is connected to the inlet of the acid pump 023, the outlet of the acid pump 023 is connected to the acid adding port II 086 of the PH lowering device 085, the acid adding port 097 of the acidification tank one 096 and the product acid pipeline 025, the outlet of the alkali generating tank 022 is connected to the inlet of the alkali pump 024, the outlet of the alkali pump 024 is connected to the alkali adding port III 009 of the washing tower I004, the alkali adding port I080 of the alkalizing reactor (tank) I079, the alkali adding port VI of the alkalizing reactor (tank) III and the alkali adding port V037 of the alkalizing reactor V036;
The solid outlet 089 of the solid-liquid separation device (centrifuge) 087 is connected to the water inlet of the alkalization reactor v 036, the alkalization reactor v 036 is also provided with an alkalization port v 037, the water outlet 038 of the alkalization reactor v 036 is connected to the inlet of the organic acid dissolving unit 040, and the organic acid dissolving unit 040 is also provided with an organic acid inlet 039 and a liquid outlet 041.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The pollutant gas entering the system through the gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is discharged from the gas outlet 006 of the washing tower I004 after being washed by the washing tower I004 after the organic matters are removed through the gas organic matter removing device (the incinerator in the embodiment) 001;
washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, then the washed liquid part circulation spray part is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding port 028 of reducing reactor 015 for reduction reaction;
Then sodium bicarbonate is converted into sodium carbonate through an alkalization reactor (tank) I079, then the sodium carbonate is concentrated through an electrodialysis concentration device I100 (the solubility of the sodium carbonate is higher than that of the sodium bicarbonate), fresh water of the electrodialysis concentration device I100 is returned to a washing tower I004 again to be reused as water, concentrated solution of the electrodialysis concentration device I100 is converted into sodium bicarbonate through a PH reduction device 085 (HBr aqueous solution generated by supplementing a back-stage bipolar membrane electrodialysis device 020), the sodium carbonate after concentration is separated out due to low solubility of the sodium bicarbonate, and solid-liquid separation is carried out through a solid-liquid separation device (centrifuge) 087, and filtrate is mainly sodium bicarbonate and sodium bromide; the solid of the solid-liquid separation device (centrifuge) 087 is mainly sodium bicarbonate, and is used for dissolving organic acid (namely residues of an oxidation system) in the organic acid dissolving unit 040 after adding alkali (supplementing sodium hydroxide aqueous solution generated by the back-stage bipolar membrane electrodialysis device 020) and recovering heavy metals (cobalt and manganese ions).
After the filtrate of the solid-liquid separation device (centrifuge) 087 is converted into sodium carbonate by an alkalization reactor III 090, the fresh water treated by the nanofiltration membrane group 093 is subjected to acid addition (supplementing HBr water solution generated by a back-end bipolar membrane electrodialysis device 020) in an acidification tank I096 to react sodium bicarbonate and sodium carbonate into carbon dioxide, the carbon dioxide is discharged from an exhaust port 099 of the acidification tank I096, the liquid enters the bipolar membrane electrodialysis device 020 to be treated, hydrobromic acid (loaded into an acid-producing tank 021) and sodium hydroxide (loaded into an alcaline-producing tank 022) are respectively carried out, and one part of acid in the acid-producing tank 021 is used for adding acid by a PH lowering device 085 and adding acid by the acidification tank I096, and the other part is collected; part of the alkali in the alkali producing tank 022 is used for adding alkali in the alkalization reactor (tank) I079, adding alkali in the washing tower I004, adding alkali in the alkalization reactor (tank) III 090 and adding alkali in the alkalization reactor V036, and fresh sodium hydroxide is not sufficiently supplemented.
Concentrated water of the nanofiltration membrane group 093 flows back into the washing tower I004 to be used as an absorbent of carbon dioxide, HBr and other acid gases.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=8.8, bicarbonate= 12313ppm, carbonate=2776 ppm, bromide=1505 ppm, orp=633 MV;
the outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.7, bicarbonate=11133 ppm, carbonate=2601 ppm, bromide=1489 ppm, orp=64 MV;
the outlet sampling of the alkalization reactor (tank) I was analyzed as follows: ph=11.2, bicarbonate=0 ppm, carbonate=13996 ppm, bromide=1455 ppm.
The concentrate outlet sampling of electrodialysis concentration device I100 was analyzed as follows: carbonate=15.1%, bromide=15001 ppm;
the PH value of the effluent of the PH value reducing device 085 is controlled to be PH=7;
the filtrate from the solid-liquid separation device (centrifuge) 087 was analyzed as follows: bicarbonate 5.8% and bromide 16646ppm.
Sampling at the outlet of the alkalization reactor III 090: ph=11.1, 5.6% carbonate, 16065ppm bromide ion
The fresh water outlet 094 of nanofiltration membrane stack 093 was analyzed as follows: 10311ppm carbonate, 17447ppm bromide;
the outlet 098 of the acidification tank one 096 is analyzed as follows: ph=3.6, carbonate=0 ppm, bromide= 43981ppm.
The acid pump 023 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: bromide ion 10.3%, hydrogen ion=1.3 mol/L;
the alkaline pump 024 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: sodium ion 4.5%, hydrogen ion=2.0 mol/L;
the outlet 038 of the alkalization reactor v 036 is analyzed as follows: 9.6% of carbonate radical.
Conclusion: the polluted gas coming in from the gas inlet 002 of the gas organic matter removing device (the incinerator) 001 is treated by the gas organic matter removing device (the incinerator) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and conversion of bicarbonate into carbonate and concentration, PH is reduced after concentration, sodium carbonate is converted into sodium bicarbonate to be separated out and subjected to solid-liquid separation by the solid-liquid separation device 087, the sodium bicarbonate is converted into sodium carbonate by filtrate and is treated by the nanofiltration membrane group 093, the nanofiltration fresh water is liquid after isolated carbonate, mainly sodium bromide and a small amount of sodium carbonate which passes through the nanofiltration membrane group 093, and two products of hydrobromic acid and sodium hydroxide can be obtained by the bipolar membrane electrodialysis device 020 after the acid addition reaction (carbon dioxide is formed and removed), so that the purpose of recycling hydrobromic acid can be achieved, and the solid sodium bicarbonate of the solid-liquid separation device 087 can be used for dissolving units of organic acids and heavy metal systems by adding alkali in the alkali adding reactor V036 to form sodium carbonate aqueous solution.
Meanwhile, the reverse osmosis concentration device, the electrodialysis concentration device and the evaporation concentration device which have been proved by the embodiments 1, 2 and 3 are interchangeable and have the same function, so that it can be deduced that the embodiment can replace the electrodialysis concentration device with the reverse osmosis concentration device or the evaporation concentration device with the same result.
Furthermore, it has been demonstrated by examples 1, 4, 5, 8, and 9 that the produced aqueous sodium bromide solution can be processed by the bipolar membrane electrodialysis device, the crystallization system I, the simple substance generator, the electrolysis device, and the volatile acid generator, and it can be deduced that the bipolar membrane electrodialysis device can be replaced by the crystallization system I, the simple substance generator, the electrolysis device, and the volatile acid generator.
Example 9
As shown in fig. 11, a system for cleaning and recycling gas mainly comprises a gas organic matter removal device (incinerator in this embodiment) 001, a washing tower i 004, a reducing agent reactor 015, an alkalization reactor (tank) i 079, an electrodialysis concentration device i 100, a PH-lowering solid-liquid separation device (centrifuge) 101, an alkalization reactor (tank) iii 090, a nanofiltration membrane group 093, an acidification tank one 096, a bipolar membrane electrodialysis device 020, an alkalization reactor v 036, and an organic acid dissolution system 040.
The gas organic matter removing apparatus (incinerator in this embodiment) 001 is provided with a gas inlet 002, a gas outlet 003 of the gas organic matter removing apparatus (incinerator in this embodiment) 001 is connected to a gas inlet 005 of a washing tower i 004, the washing tower i 004 is further provided with a gas outlet 006, an alkali addition port iii 009, a water replenishment port 008, a liquid discharge port 007 of the washing tower i 004 is connected to a reducing agent reactor 015, and the reducing agent reactor 015 is further provided with a reducing agent addition port 028;
the water outlet of the reducing agent reactor 015 is connected to the water inlet of an alkalization reactor (tank) I079, the alkalization reactor (tank) I079 is also provided with an alkali adding port I080, the water outlet of the alkalization reactor (tank) I079 is connected to the water inlet of a water supply pump 081 of an electrodialysis concentration device I100, the water outlet of the water supply pump 081 of the electrodialysis concentration device I100 is connected to the water inlet 082 of the electrodialysis concentration device I100, and a fresh water outlet 084 of the electrodialysis concentration device I100 is connected to a water supplementing port 008 of a washing tower I004;
the concentrated solution outlet 083 of the electrodialysis concentration device I100 is connected to the water inlet of the PH-lowering solid-liquid separation equipment (centrifugal machine) 101, and the PH-lowering solid-liquid separation equipment (centrifugal machine) 101 is also provided with an acid adding port III 104;
the filtrate outlet 102 of the PH-lowering solid-liquid separation device (centrifuge) 101 is connected to the water inlet of an alkalization reactor (tank) iii 090, the alkalization reactor (tank) iii 090 also has an alkalization port vi 091, the water outlet of the alkalization reactor (tank) iii 090 is connected to the water inlet of the high pressure pump 092 of the nanofiltration membrane group 093, and the water outlet of the high pressure pump 092 of the nanofiltration membrane group 093 is connected to the water inlet of the nanofiltration membrane group 093;
The concentrated water outlet 095 of the nanofiltration membrane group 093 is connected to the alkali adding port III 009 of the washing tower I004;
the fresh water outlet 094 of the nanofiltration membrane group 093 is connected to the inlet of the acidification tank one 096, the acidification tank one 096 is also provided with an acid adding port 097 and an exhaust port 099, the outlet 098 of the acidification tank one 096 is connected to the water inlet of the bipolar membrane electrodialysis device 020, the acid outlet of the bipolar membrane electrodialysis device 020 is connected to the acid generating tank 021, the alkali outlet is connected to the alkali generating tank 022, the outlet of the acid generating tank 021 is connected to the inlet of the acid pump 023, the outlet of the acid pump 023 is connected to the acid adding port III 104 of the PH-lowering solid-liquid separation device (centrifuge) 101, the acid adding port 097 of the acidification tank one 096 and the product acid pipeline 025, the outlet of the alkali generating tank 022 is connected to the inlet of the alkali pump 024, the outlet of the alkali pump 024 is connected to the alkali adding port III of the washing tower I004, the alkali adding port I080 of the alkalizing reactor I079, the alkali adding port 091 of the alkalizing reactor (tank) III 090 and the alkali adding port V036;
the solid outlet 103 of the PH-lowering solid-liquid separation apparatus (centrifuge) 101 is connected to the water inlet of the alkalization reactor v 036, the alkalization reactor v 036 also has an alkalization port v 037, the water outlet 038 of the alkalization reactor v 036 is connected to the inlet of the organic acid dissolving unit 040, and the organic acid dissolving unit 040 is also provided with an organic acid inlet 039 and a liquid outlet 041.
The gas cleaning and recycling system operates as follows:
the target of the treatment of the utility model is a pollutant gas, and the target of the treatment of all the embodiments of the utility model is the tail gas of a terephthalic acid production device.
The pollutant gas entering the system through the gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is discharged from the gas outlet 006 of the washing tower I004 after being washed by the washing tower I004 after the organic matters are removed through the gas organic matter removing device (the incinerator in the embodiment) 001;
washing tower I004 (circulation spray washing) supplements water from water supplementing port 008, supplements liquid alkali from alkali adding port III 009, then the washed liquid part circulation spray part is discharged from liquid discharge port 007 to reducing reactor 015, and reducing agent is added from reducing agent adding port 028 of reducing reactor 015 for reduction reaction;
then sodium bicarbonate is converted into sodium carbonate through an alkalization reactor (an alkalization reaction tank) I079, and then concentrated through an electrodialysis concentration device I100 (the solubility of sodium carbonate is higher than that of sodium bicarbonate), fresh water of the electrodialysis concentration device I100 is returned to a washing tower I004 again to be reused as water, concentrated solution of the electrodialysis concentration device I100 is subjected to PH-lowering solid-liquid separation equipment (a centrifugal machine) 101 (HBr aqueous solution generated by supplementing a back-stage bipolar membrane electrodialysis equipment 020) to convert the concentrated sodium carbonate into sodium bicarbonate and carry out solid-liquid separation (precipitation due to low solubility of sodium bicarbonate), and filtrate is mainly sodium bicarbonate and sodium bromide; the solid of the PH-lowering solid-liquid separation apparatus (centrifuge) 101 is mainly sodium bicarbonate, and after adding alkali (replenishing the sodium hydroxide aqueous solution generated by the post bipolar membrane electrodialysis apparatus 020), the solid is used for dissolving the organic acid (i.e., the residue of the oxidation system) in the organic acid dissolving unit 040, and recovering heavy metals (cobalt-manganese ions).
After the filtrate of the PH-lowering solid-liquid separation device (centrifuge) 101 is converted into sodium carbonate by an alkalization reactor III 090, the fresh water treated by the nanofiltration membrane group 093 is subjected to acid addition (supplementing HBr water solution generated by a post bipolar membrane electrodialysis device 020) in an acidification tank I096 to react sodium bicarbonate and sodium carbonate into carbon dioxide, the carbon dioxide is discharged from an exhaust port 099 of the acidification tank I096, the liquid enters the bipolar membrane electrodialysis device 020 to be treated, hydrobromic acid (loaded into an acid-producing tank 021) and sodium hydroxide (loaded into an alcaline-producing tank 022) are respectively carried out, and one part of acid in the acid-producing tank 021 is used for adding acid to the PH-lowering solid-liquid separation device (centrifuge) 101 and adding acid to the acidification tank I096, and the other part is collected; part of the alkali in the alkali producing tank 022 is used for adding alkali in the alkalization reactor (tank) I079, adding alkali in the washing tower I004, adding alkali in the alkalization reactor (tank) III 090 and adding alkali in the alkalization reactor V036, and fresh sodium hydroxide is not sufficiently supplemented.
Concentrated water of the nanofiltration membrane group 093 flows back into the washing tower I004 to be used as an absorbent of carbon dioxide, HBr and other acid gases.
The experiment was run using the system described above:
the liquid discharge port 007 of the wash column I004 was sampled and analyzed as follows: ph=9.1, bicarbonate=15511 ppm, carbonate=3113 ppm, bromide=1689 ppm, orp=601 MV;
The outlet of the reducing agent reactor 015 (sodium formate addition) was sampled and analyzed as follows: ph=8.9, bicarbonate=14878 ppm, carbonate=2912 ppm, bromide=1554 ppm, orp=38mv;
the outlet sampling of the alkalization reactor (tank) I was analyzed as follows: ph=11.0, bicarbonate=0 ppm, carbonate=17689 ppm, bromide=1513 ppm.
The concentrate outlet sampling of electrodialysis concentration device I100 was analyzed as follows: carbonate = 14.2%, bromide = 12415ppm;
the PH value of the effluent of the PH value reducing device 085 is controlled to be PH=7;
the filtrate of the PH-lowering solid-liquid separation apparatus (centrifuge) 101 was analyzed as follows: bicarbonate 5.3% and bromide 13321ppm.
Sampling at the outlet of the alkalization reactor III 090: ph=11.1, 5.6% carbonate, 16065ppm bromide.
The fresh water outlet 094 of nanofiltration membrane stack 093 was analyzed as follows: 13138ppm carbonate, 18269ppm bromide;
the outlet 098 of the acidification tank one 096 is analyzed as follows: ph=3.2, carbonate=0 ppm, bromide= 55154ppm.
The acid pump 023 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: bromide 8.1%, hydrogen = 1.0mol/L;
the alkaline pump 024 of bipolar membrane electrodialysis apparatus 020 was analyzed as follows: sodium ion 3.3%, hydrogen ion=1.4 mol/L;
the outlet 038 of the alkalization reactor v 036 is analyzed as follows: 8.4% of carbonate radical.
Conclusion: the polluted gas coming in from the gas inlet 002 of the gas organic matter removing device (the incinerator in the embodiment) 001 is treated by the gas organic matter removing device (the incinerator in the embodiment) 001 and is washed and discharged by the washing tower I004, the generated washing liquid is subjected to oxidation removal and conversion of bicarbonate into carbonate and concentration, after concentration, the sodium carbonate is converted into sodium bicarbonate by lowering the PH through the PH-lowering solid-liquid separation device (the centrifuge) 101 to separate out and carry out solid-liquid separation, the sodium bicarbonate is converted into sodium carbonate by filtrate and is treated by the nanofiltration membrane 093, the nanofiltration fresh water is liquid after isolated carbonate, mainly sodium bromide and a small amount of sodium carbonate which permeates the nanofiltration membrane 093, and two products of hydrobromic acid and sodium hydroxide can be obtained by the reaction of the bipolar membrane electrodialysis device 020 after the acid is added to react to form the carbonate (form carbon dioxide), so that the purpose of recycling hydrobromic acid can be achieved, and the solid sodium bicarbonate of the solid-liquid separation device 087 can be used in a dissolution unit of organic acid and a heavy metal recycling system by adding alkali in the alkali adding reactor V036.
Meanwhile, the reverse osmosis concentration device, the electrodialysis concentration device and the evaporation concentration device which have been proved by the embodiments 1, 2 and 3 are interchangeable and have the same function, so that it can be deduced that the embodiment can replace the electrodialysis concentration device with the reverse osmosis concentration device or the evaporation concentration device with the same result.
Furthermore, it has been demonstrated by examples 1, 4, 5, 8, and 9 that the produced aqueous sodium bromide solution can be processed by the bipolar membrane electrodialysis device, the crystallization system I, the simple substance generator, the electrolysis device, and the volatile acid generator, and it can be deduced that the bipolar membrane electrodialysis device can be replaced by the crystallization system I, the simple substance generator, the electrolysis device, and the volatile acid generator.
Claims (56)
1. A gas cleaning and recycling system, the gas cleaning and recycling system comprising: a gaseous organic matter removing device, a washing tower I, a carbon dioxide generator, a bipolar membrane electrodialysis device, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator;
the gas organic matter removing device is provided with a gas inlet, a gas outlet of the gas organic matter removing device is connected to a gas inlet of the washing tower I, a liquid discharge port of the washing tower I is connected to a water inlet of the carbon dioxide generator, and a liquid discharge port of the carbon dioxide generator is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
Or the gas cleaning and recycling system comprises: the device comprises gas organic matter removing equipment, a washing tower I, a concentrating device I, a PH reducing device, solid-liquid separation equipment, bipolar membrane electrodialysis equipment, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator;
the gas organic matter removing device is provided with a gas inlet, a gas outlet of the gas organic matter removing device is connected to a gas inlet of the washing tower I, a liquid discharge port of the washing tower I is connected to a water inlet of the concentration device I, a concentrated liquid outlet of the concentration device I is connected to a water inlet of the PH-lowering device, a discharge port of the PH-lowering device is connected to a water inlet of the solid-liquid separation device, and a liquid outlet of the solid-liquid separation device is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
or the gas cleaning and recycling system comprises: the device comprises gas organic matter removing equipment, a washing tower I, a concentrating device I, PH-lowering solid-liquid separation equipment, bipolar membrane electrodialysis equipment, a crystallization system I, an electrolysis device, a simple substance generator or a volatile acid generator;
The gas organic matter removing device is provided with a gas inlet, a gas outlet of the gas organic matter removing device is connected to a gas inlet of the washing tower I, a liquid discharge outlet of the washing tower I is connected to a water inlet of the concentrating device I, a concentrated liquid outlet of the concentrating device I is connected to a water inlet of the PH-reducing solid-liquid separation device, and a liquid outlet of the PH-reducing solid-liquid separation device is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator.
2. The system for cleaning and recycling gas according to claim 1, further comprising a concentrating device ii and/or a concentrating device iii;
the liquid discharge port of the washing tower I is connected to the water inlet of the concentrating device II, and the concentrated liquid outlet of the concentrating device II is connected to the water inlet of the carbon dioxide generator;
the liquid discharge port of the carbon dioxide generator is connected to the water inlet of the concentrating device III, and the concentrated liquid outlet of the concentrating device III is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator or the water inlet of the volatile acid generator.
3. The system for cleaning and recycling gas according to claim 1, further comprising an alkalization reactor i, wherein the alkalization reactor i is disposed between a liquid discharge port of the washing tower i and a water inlet port of the concentrating device i.
4. The gas cleaning and recycling system according to claim 1, further comprising a reducing agent reactor;
the reducing agent reactor is arranged between a liquid discharge port of the washing tower I and a water inlet of the carbon dioxide generator;
or the reducing agent reactor is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
or the reducing agent reactor is arranged between the liquid discharge port of the washing tower I and the water inlet of the concentrating device I; or the reducing agent reactor is arranged between a concentrated solution discharge port of the concentrating device I and the PH reducing device; or the reducing agent reactor is arranged between the discharge port of the PH-reducing device and the water inlet of the solid-liquid separation equipment;
Or the reducing agent reactor is arranged between a liquid outlet of the solid-liquid separation device and a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator;
or the reducing agent reactor is arranged between a concentrated solution discharge port of the concentrating device I and a water inlet of the PH-lowering solid-liquid separation device; or the reducing agent reactor is arranged between a liquid outlet of the PH-reducing solid-liquid separation device and a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator.
5. The gas cleaning and recycling system according to claim 2, further comprising a reducing agent reactor;
the reducing agent reactor is arranged between a liquid discharge port of the washing tower I and a water inlet of the concentrating device II; or the reducing agent reactor is arranged between a concentrated solution outlet of the concentrating device II and a water inlet of the carbon dioxide generator;
Or the reducing agent reactor is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the concentrating device III;
or the reducing agent reactor is arranged between a concentrated solution outlet of the concentrating device III and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator or a water inlet of the volatile acid generator.
6. The gas cleaning and recycling system according to claim 3, further comprising a reducing agent reactor;
the reducing agent reactor is arranged between a liquid discharge port of the washing tower I and a water inlet of the alkalization reactor I; or the reducing agent reactor is arranged between the water outlet of the alkalization reactor I and the water inlet of the concentration device I.
7. The gas cleaning and recycling system according to claim 4, 5 or 6, wherein the reducing agent reactor is further provided with a reducing agent addition inlet.
8. The system for cleaning and recycling gas according to claim 5, further comprising a temperature raising device, wherein the temperature raising device is arranged between the liquid discharge port of the washing tower I and the water inlet of the reducing agent reactor; or the temperature rising device is arranged between a concentrated solution outlet of the concentrating device II and a water inlet of the reducing agent reactor; or the heating device is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the reducing agent reactor; or the temperature rising device is arranged between a concentrated solution outlet of the concentrating device III and a water inlet of the reducing agent reactor.
9. The system for cleaning and recycling gas according to claim 4, further comprising a temperature raising device, wherein the temperature raising device is arranged between the liquid discharge port of the washing tower I and the water inlet of the reducing agent reactor; or the heating device is arranged between a liquid discharge port of the carbon dioxide generator and a water inlet of the reducing agent reactor; or the heating device is arranged between a concentrated solution outlet of the concentrating device I and a water inlet of the reducing agent reactor; or the temperature rising device is arranged between the discharge port of the PH reducing device and the water inlet of the reducing agent reactor; or the heating device is arranged between a liquid outlet of the solid-liquid separation equipment and a water inlet of the reducing agent reactor; or the temperature rising device is arranged between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the reducing agent reactor.
10. The system for cleaning and recycling gas according to claim 6, further comprising a temperature raising device, wherein the temperature raising device is arranged between the liquid discharge port of the washing tower I and the water inlet of the reducing agent reactor; or the heating device is arranged between the water outlet of the alkalization reactor I and the water inlet of the reducing agent reactor.
11. The system for cleaning and recycling gas according to claim 4, further comprising an alkalization reactor II, wherein the alkalization reactor II is arranged between a water outlet of the reducing agent reactor and a water inlet of the carbon dioxide generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the bipolar membrane electrodialysis; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the crystallization system I; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the electrolysis device; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the simple substance generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the volatile acid generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the concentration device I; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the PH-lowering device; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the solid-liquid separation equipment; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the PH-lowering solid-liquid separation device.
12. The system for cleaning and recycling gas according to claim 5, further comprising an alkalization reactor II, wherein the alkalization reactor II is arranged between a water outlet of the reducing agent reactor and a water inlet of the concentrating device II; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the carbon dioxide generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the concentration device III; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the bipolar membrane electrodialysis; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the crystallization system I; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the electrolysis device; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the simple substance generator; or the alkalization reactor II is arranged between the water outlet of the reducing agent reactor and the water inlet of the volatile acid generator.
13. The system for cleaning and recycling gas according to claim 6, further comprising an alkalization reactor ii, wherein the alkalization reactor ii is disposed between the water outlet of the reducing agent reactor and the water inlet of the concentrating device i.
14. The gas cleaning and recycling system according to claim 4 or 11, wherein between the liquid outlet of the solid-liquid separation device and the water inlet of the bipolar membrane electrodialysis device, between the liquid outlet of the solid-liquid separation device and the water inlet of the crystallization system i, between the liquid outlet of the solid-liquid separation device and the water inlet of the electrolysis device, between the liquid outlet of the solid-liquid separation device and the water inlet of the simple substance generator, between the liquid outlet of the solid-liquid separation device and the water inlet of the volatile acid generator, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the bipolar membrane electrodialysis device, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the crystallization system i, between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the electrolysis device, or between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the simple substance generator, and the water inlet of the volatile acid generator:
The device is provided with an alkalization reactor III and a nanofiltration membrane group, wherein the water outlet of the alkalization reactor III is connected to the water inlet of a high-pressure pump, the water outlet of the high-pressure pump 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 equipment, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or an alkalization reactor III and a purification monovalent ion type electrodialysis device are arranged, wherein the water outlet of the alkalization reactor III is connected to the water inlet of the purification monovalent ion type electrodialysis device, and the water outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or an acidification tank is arranged, and the outlet of the acidification tank is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
Or an acidification tank and a decarbonization tower' are arranged, the outlet of the acidification tank is connected to the water inlet of the decarbonization tower, and the water outlet of the decarbonization tower is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or a salt separation unit is arranged, and the water outlet of the salt separation unit is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
15. The gas cleaning and recycling system according to claim 4, 5, 11 or 12, wherein the water outlet of the reducing agent reactor is connected to the water inlet of the bipolar membrane electrodialysis device, the water outlet of the reducing agent reactor is connected to the water inlet of the crystallization system i, the water outlet of the reducing agent reactor is connected to the water inlet of the electrolysis device, the water outlet of the reducing agent reactor is connected to the water inlet of the simple substance generator or the water outlet of the reducing agent reactor is connected to the water inlet of the volatile acid generator:
The device comprises an alkalization reactor III and a nanofiltration membrane group, wherein a water outlet of the alkalization reactor III is connected to a water inlet of a high-pressure pump, a water outlet of the high-pressure pump is connected to a water inlet of the nanofiltration membrane group, and a fresh water outlet of the nanofiltration membrane group is connected to a water inlet of bipolar membrane electrodialysis equipment, a water inlet of a crystallization system I, a water inlet of an electrolysis device, a water inlet of a simple substance generator, a water inlet of a volatile acid generator or a water inlet of a reducing agent reactor;
or an alkalization reactor III and a purification monovalent ion type electrodialysis device are arranged, wherein the water outlet of the alkalization reactor III is connected to the water inlet of the purification monovalent ion type electrodialysis device, and the water outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or an acidification tank is arranged, and the outlet of the acidification tank is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
Or an acidification tank and a decarbonization tower' are arranged, the outlet of the acidification tank is connected to the water inlet of the decarbonization tower, and the water outlet of the decarbonization tower is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or a salt separation unit is arranged, and the water outlet of the salt separation unit is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
16. The gas cleaning and recycling system according to claim 4, 9 or 11, wherein between the liquid outlet of the solid-liquid separation device and the water inlet of the reducing agent reactor or between the liquid outlet of the PH-lowering solid-liquid separation device and the water inlet of the reducing agent reactor:
the device comprises an alkalization reactor III and a nanofiltration membrane group, wherein a water outlet of the alkalization reactor III is connected to a water inlet of a high-pressure pump, a water outlet of the high-pressure pump is connected to a water inlet of the nanofiltration membrane group, and a fresh water outlet of the nanofiltration membrane group is connected to a water inlet of bipolar membrane electrodialysis equipment, a water inlet of a crystallization system I, a water inlet of an electrolysis device, a water inlet of a simple substance generator, a water inlet of a volatile acid generator or a water inlet of a reducing agent reactor;
Or an alkalization reactor III and a purification monovalent ion type electrodialysis device are arranged, wherein the water outlet of the alkalization reactor III is connected to the water inlet of the purification monovalent ion type electrodialysis device, and the water outlet I of the purification monovalent ion type electrodialysis device is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or an acidification tank is arranged, and the outlet of the acidification tank is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or an acidification tank and a decarbonization tower' are arranged, the outlet of the acidification tank is connected to the water inlet of the decarbonization tower, and the water outlet of the decarbonization tower is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
Or a salt separation unit is arranged, and the water outlet of the salt separation unit is connected to the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor.
17. The gas cleaning and recycling system according to claim 14, wherein,
an acidification tank I is arranged between a fresh water outlet of the nanofiltration membrane group and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor;
or an acidification tank II is arranged between the water outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or the salt separation unit comprises an evaporator ', a cooler', a solid-liquid separation device ', wherein a material discharge port of the evaporator' is connected to an inlet of the cooler ', an outlet of the cooler' is connected to an inlet of the solid-liquid separation device ', and a liquid outlet of the solid-liquid separation device' is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor.
18. The gas cleaning and recycling system according to claim 15, wherein,
an acidification tank I is arranged between a fresh water outlet of the nanofiltration membrane group and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor;
or an acidification tank II is arranged between the water outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or the salt separation unit comprises an evaporator ', a cooler', a solid-liquid separation device ', wherein a material discharge port of the evaporator' is connected to an inlet of the cooler ', an outlet of the cooler' is connected to an inlet of the solid-liquid separation device ', and a liquid outlet of the solid-liquid separation device' is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor.
19. The gas cleaning and recycling system according to claim 16, wherein,
an acidification tank I is arranged between a fresh water outlet of the nanofiltration membrane group and a water inlet of the bipolar membrane electrodialysis equipment, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor;
or an acidification tank II is arranged between the water outlet I of the purification monovalent ion type electrodialysis device and the water inlet of the bipolar membrane electrodialysis device, the water inlet of the crystallization system I, the water inlet of the electrolysis device, the water inlet of the simple substance generator, the water inlet of the volatile acid generator or the water inlet of the reducing agent reactor;
or the salt separation unit comprises an evaporator ', a cooler', a solid-liquid separation device ', wherein a material discharge port of the evaporator' is connected to an inlet of the cooler ', an outlet of the cooler' is connected to an inlet of the solid-liquid separation device ', and a liquid outlet of the solid-liquid separation device' is connected to a water inlet of the bipolar membrane electrodialysis device, a water inlet of the crystallization system I, a water inlet of the electrolysis device, a water inlet of the simple substance generator, a water inlet of the volatile acid generator or a water inlet of the reducing agent reactor.
20. The system for cleaning and recycling a gas according to claim 1, 2, 4, 5, 8, 9, 11 or 12, wherein the exhaust port of the carbon dioxide generator is connected to the inlet port of the scrubber ii;
or the exhaust port of the carbon dioxide generator is connected to the air inlet of a washing tower II, and the liquid discharge port of the washing tower II is connected to a crystallization system II;
or the exhaust port of the carbon dioxide generator is connected to the air inlet of the washing tower II, and the liquid discharge port of the washing tower II is connected to an organic acid dissolving system or a heavy metal recovery system; or the exhaust port of the carbon dioxide generator is connected to the air inlet of the washing tower II, and the liquid discharge port of the washing tower II is connected to the water inlet of the alkalization reactor V.
21. The gas cleaning and recycling system according to claim 1, 4, 9 or 11, wherein,
the solid outlet of the solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the solid-liquid separation equipment is connected to an organic acid dissolving system or a heavy metal recovery system;
or the solid outlet of the PH-lowering solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the PH-lowering solid-liquid separation device is connected with an organic acid dissolving system or a heavy metal recovery system.
22. The gas cleaning and recycling system according to claim 14, wherein,
the solid outlet of the solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the solid-liquid separation equipment is connected to an organic acid dissolving system or a heavy metal recovery system;
or the solid outlet of the PH-lowering solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the PH-lowering solid-liquid separation device is connected with an organic acid dissolving system or a heavy metal recovery system.
23. The gas cleaning and recycling system according to claim 16, wherein,
the solid outlet of the solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the solid-liquid separation equipment is connected to an organic acid dissolving system or a heavy metal recovery system;
or the solid outlet of the PH-lowering solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the PH-lowering solid-liquid separation device is connected with an organic acid dissolving system or a heavy metal recovery system.
24. The gas cleaning and recycling system according to claim 17, 18 or 19, wherein,
The solid outlet of the solid-liquid separation device is connected to the inlet of the alkalization reactor V; or the solid outlet of the solid-liquid separation device' is connected to an organic acid dissolution system or a heavy metal recovery system.
25. The gas cleaning and recycling system according to claim 1, 2, 4, 5, 8, 9, 11 or 12, wherein the carbon dioxide generator further comprises an acid adding port i.
26. The gas cleaning and recycling system according to claim 20, wherein the carbon dioxide generator further comprises an acid addition port i.
27. The gas cleaning and recycling system according to claim 1, 4, 9 or 11, wherein the PH reducing device further comprises an acid adding port ii; or the PH-lowering solid-liquid separation equipment is also provided with an acid adding port III.
28. The gas cleaning and recycling system according to claim 14, wherein the PH-lowering solid-liquid separation device further comprises an acid addition port iii.
29. The gas cleaning and recycling system according to claim 16, wherein the PH-lowering solid-liquid separation device further comprises an acid addition port iii.
30. The gas cleaning and recycling system according to claim 21, wherein the PH-lowering solid-liquid separation device further comprises an acid addition port iii.
31. The gas cleaning and recycling system according to claim 22 or 23, wherein the PH-lowering solid-liquid separation apparatus further comprises an acid addition port iii.
32. The system for cleaning and recycling gas according to claim 3, 6, 10 or 13, wherein the alkalization reactor i has an alkalization port i.
33. The system for cleaning and recycling gas according to claim 11, 12 or 13, wherein the alkalization reactor ii has an alkalization port ii.
34. The system for cleaning and recycling gas according to claim 14, wherein the alkalization reactor iii has an alkalization port vi.
35. The system for cleaning and recycling gas according to claim 15, wherein the alkalization reactor iii has an alkalization port vi.
36. The system for cleaning and recycling gas according to claim 16, wherein the alkalization reactor iii has an alkalization port vi.
37. The gas cleaning and recycling system according to claim 1, 2, 3, 4, 5, 6, 8, 9, 10, 11, 12 or 13, wherein the scrubber i has an alkaline inlet iii.
38. The gas cleaning and recycling system according to claim 20, wherein the scrubber ii has an alkaline inlet iv.
39. The system for cleaning and recycling gas according to claim 21, wherein the alkalization reactor v is provided with an alkali adding port v.
40. The system for cleaning and recycling of gases according to claim 22 or 23, characterized in that the alkalization reactor v is provided with an alkalization port v.
41. The system for cleaning and recycling gas according to claim 24, wherein the alkalization reactor v is provided with an alkali adding port v.
42. The system for cleaning and recycling of gases according to claim 21, characterized in that the outlet of the alkalization reactor v is connected to an organic acid dissolution system or a heavy metal recovery system.
43. The system for cleaning and recycling of gases according to claim 22 or 23, characterized in that the outlet of the alkalization reactor v is connected to an organic acid dissolution system or a heavy metal recovery system.
44. The system for cleaning and recycling of gases according to claim 24, characterized in that the outlet of the alkalization reactor v is connected to an organic acid dissolution system or a heavy metal recovery system.
45. The gas cleaning and recycling system according to claim 39, characterized in that the outlet of the alkalization reactor v is connected to an organic acid dissolving system or a heavy metal recovery system.
46. The gas cleaning and recycling system according to claim 40, wherein the outlet of the alkalization reactor v is connected to an organic acid dissolving system or a heavy metal recovery system.
47. The gas cleaning and recycling system according to claim 41, characterized in that the outlet of the alkalization reactor v is connected to an organic acid dissolving system or a heavy metal recovery system.
48. The gas cleaning and recycling system according to claim 17, 18 or 19, wherein,
the solid outlet of the solid-liquid separation device is connected to an organic acid dissolution system, a heavy metal recovery system or a crystallization system III.
49. The gas cleaning and recycling system according to claim 14, wherein,
the concentrated water outlet of the nanofiltration membrane group is connected to an organic acid dissolving system, a heavy metal recovery system or a crystallization system III;
or the water outlet II of the purification monovalent ion electrodialysis device is connected to an organic acid dissolving system, a heavy metal recovery system or a crystallization system III.
50. The gas cleaning and recycling system according to claim 15, wherein,
the concentrated water outlet of the nanofiltration membrane group is connected to an organic acid dissolving system, a heavy metal recovery system or a crystallization system III;
Or the water outlet II of the purification monovalent ion electrodialysis device is connected to an organic acid dissolving system, a heavy metal recovery system or a crystallization system III.
51. The gas cleaning and recycling system according to claim 16, wherein,
the concentrated water outlet of the nanofiltration membrane group is connected to an organic acid dissolving system, a heavy metal recovery system or a crystallization system III;
or the water outlet II of the purification monovalent ion electrodialysis device is connected to an organic acid dissolving system, a heavy metal recovery system or a crystallization system III.
52. The system of claim 1, wherein the organic removal device comprises at least one of a gas incinerator, a gas organic catalytic decomposition processor, and a gas organic adsorber.
53. The gas cleaning and recycling system according to claim 1, 4, 9, 11, 22 or 23, wherein,
the solid-liquid separation equipment refers to at least one of a positive pressure filter, a negative pressure suction filter, a centrifugal machine, a filter press and a bag filter;
or the PH-lowering solid-liquid separation equipment is at least one of a positive pressure filter, a negative pressure suction filter, a centrifuge, a filter press and a bag filter with PH-lowering function.
54. The gas cleaning and recycling system according to claim 14, wherein,
the solid-liquid separation equipment refers to at least one of a positive pressure filter, a negative pressure suction filter, a centrifugal machine, a filter press and a bag filter;
or the PH-lowering solid-liquid separation equipment is at least one of a positive pressure filter, a negative pressure suction filter, a centrifuge, a filter press and a bag filter with PH-lowering function.
55. The gas cleaning and recycling system according to claim 16, wherein,
the solid-liquid separation equipment refers to at least one of a positive pressure filter, a negative pressure suction filter, a centrifugal machine, a filter press and a bag filter;
or the PH-lowering solid-liquid separation equipment is at least one of a positive pressure filter, a negative pressure suction filter, a centrifuge, a filter press and a bag filter with PH-lowering function.
56. The gas cleaning and recycling system according to claim 21, wherein,
the solid-liquid separation equipment refers to at least one of a positive pressure filter, a negative pressure suction filter, a centrifugal machine, a filter press and a bag filter;
or the PH-lowering solid-liquid separation equipment is at least one of a positive pressure filter, a negative pressure suction filter, a centrifuge, a filter press and a bag filter with PH-lowering function.
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| CN202320774498.1U CN220194466U (en) | 2023-04-10 | 2023-04-10 | Gas cleaning and recycling system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320774498.1U CN220194466U (en) | 2023-04-10 | 2023-04-10 | Gas cleaning and recycling system |
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