CN219050834U - Gas extraction and recovery system - Google Patents
Gas extraction and recovery system Download PDFInfo
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- CN219050834U CN219050834U CN202220454807.2U CN202220454807U CN219050834U CN 219050834 U CN219050834 U CN 219050834U CN 202220454807 U CN202220454807 U CN 202220454807U CN 219050834 U CN219050834 U CN 219050834U
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- 238000011084 recovery Methods 0.000 title claims abstract description 85
- 238000000605 extraction Methods 0.000 title claims abstract description 84
- 239000012528 membrane Substances 0.000 claims abstract description 482
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 412
- 238000000909 electrodialysis Methods 0.000 claims abstract description 76
- 238000005406 washing Methods 0.000 claims abstract description 55
- 238000000746 purification Methods 0.000 claims abstract description 21
- 239000002253 acid Substances 0.000 claims description 92
- 239000003513 alkali Substances 0.000 claims description 87
- 238000010438 heat treatment Methods 0.000 claims description 52
- 238000010521 absorption reaction Methods 0.000 claims description 43
- 238000001728 nano-filtration Methods 0.000 claims description 24
- 238000007254 oxidation reaction Methods 0.000 claims description 19
- 230000020477 pH reduction Effects 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 14
- 239000005416 organic matter Substances 0.000 claims description 13
- 238000002156 mixing Methods 0.000 claims description 4
- 239000000126 substance Substances 0.000 abstract description 12
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 154
- 150000001450 anions Chemical class 0.000 description 110
- 150000001768 cations Chemical class 0.000 description 104
- 239000000243 solution Substances 0.000 description 68
- 150000002500 ions Chemical class 0.000 description 62
- 239000007864 aqueous solution Substances 0.000 description 59
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 39
- 239000007788 liquid Substances 0.000 description 27
- 239000007921 spray Substances 0.000 description 27
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 23
- 238000010586 diagram Methods 0.000 description 22
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 21
- 230000003113 alkalizing effect Effects 0.000 description 21
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 description 20
- 239000002585 base Substances 0.000 description 19
- 239000000047 product Substances 0.000 description 19
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 18
- 238000001223 reverse osmosis Methods 0.000 description 18
- 239000012141 concentrate Substances 0.000 description 17
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 14
- 239000012267 brine Substances 0.000 description 14
- 230000000694 effects Effects 0.000 description 14
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 14
- BMYNFMYTOJXKLE-UHFFFAOYSA-N 3-azaniumyl-2-hydroxypropanoate Chemical group NCC(O)C(O)=O BMYNFMYTOJXKLE-UHFFFAOYSA-N 0.000 description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
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- 238000002474 experimental method Methods 0.000 description 9
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- 238000005192 partition Methods 0.000 description 7
- 239000012466 permeate Substances 0.000 description 7
- CPELXLSAUQHCOX-UHFFFAOYSA-N Hydrogen bromide Chemical compound Br CPELXLSAUQHCOX-UHFFFAOYSA-N 0.000 description 6
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 239000013505 freshwater Substances 0.000 description 6
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 6
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 6
- 229910001415 sodium ion Inorganic materials 0.000 description 6
- 230000002378 acidificating effect Effects 0.000 description 5
- 238000005261 decarburization Methods 0.000 description 5
- -1 hydrogen ions Chemical class 0.000 description 5
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- 238000007789 sealing Methods 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- 125000000129 anionic group Chemical group 0.000 description 4
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- 230000001276 controlling effect Effects 0.000 description 4
- 238000005262 decarbonization Methods 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- 230000001502 supplementing effect Effects 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910000042 hydrogen bromide Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
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- 229920005989 resin Polymers 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 229940006460 bromide ion Drugs 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 229910001424 calcium ion Inorganic materials 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000006298 dechlorination reaction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
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- 238000005070 sampling Methods 0.000 description 2
- 241000894007 species Species 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-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
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- NPYPAHLBTDXSSS-UHFFFAOYSA-N Potassium ion Chemical compound [K+] NPYPAHLBTDXSSS-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- ACVYVLVWPXVTIT-UHFFFAOYSA-M phosphinate Chemical compound [O-][PH2]=O ACVYVLVWPXVTIT-UHFFFAOYSA-M 0.000 description 1
- OJMIONKXNSYLSR-UHFFFAOYSA-N phosphorous acid Chemical compound OP(O)O OJMIONKXNSYLSR-UHFFFAOYSA-N 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 229910001414 potassium ion Inorganic materials 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a gas extraction and recovery system, which comprises: a washing tower, a purifying ion type electrodialysis device and a bipolar membrane device; the water solution discharge port of the washing tower is connected to the water inlet of the purified ion electrodialysis device, and the concentrated solution discharge port of the purified ion electrodialysis device is connected to the water inlet of the bipolar membrane device; the purification ion electrodialysis device comprises a membrane assembly, wherein the membrane assembly is arranged between an electrode positive plate and an electrode negative plate; the membrane assembly includes a single female membrane sheet, yang Mopian; or the membrane assembly comprises a single male membrane sheet and a female membrane sheet; or the membrane assembly comprises a single male membrane sheet and a single female membrane sheet. After the gas is treated by the system, the economic value of partial beneficial substances in the recovered gas can be extracted.
Description
Technical Field
The utility model belongs to the technical field of resource extraction and reuse, and particularly relates to a gas extraction and recovery system.
Background
At present, a lot of industrial gases are directly discharged into the atmosphere after simple treatment, so that the environment is polluted, and valuable substances in the gases are wasted.
Organic matters in the gas can contribute VOC, can cause harm to the respiration of people and animals, and can also aggravate the higher eutrophication of COD of natural water bodies such as rivers and the like; when the gas contains acid, acid rain may occur.
Disclosure of Invention
The utility model aims to provide a gas extraction and recovery system, which is used for treating gas, reducing the environmental pollution of the gas and simultaneously recovering the economic value of beneficial substances in the gas.
The ions in water can be divided into four types according to the yin-yang property and the ion valence state: monovalent cations (e.g., sodium, potassium, ammonia, lithium, hydrogen, etc.), monovalent anions (e.g., chloride, bromide, fluoride, iodide, hydroxide, nitrate, nitrite, monovalent organic acid, bicarbonate, etc.), divalent cations (e.g., calcium, magnesium, copper, zinc, iron, ferrous, cobalt, manganese, molybdenum, chromium, nickel, aluminum, titanium, barium, etc.), divalent anions (e.g., sulfate, carbonate, sulfite, phosphate, hypophosphite, phosphite, silicate, etc.), all ". Gtoreq.divalent cations" in the present application include divalent cations as well as trivalent, tetravalent, etc. > divalent cations; all ". Gtoreq.dianions" in the same sense include dianions, and trivalent, tetravalent, etc. > dianions, valence refers to valence.
A gas extraction recovery system comprising: a washing tower, a purifying ion type electrodialysis device and a bipolar membrane device;
the water solution discharge port of the washing tower is connected to the water inlet of the purified ion electrodialysis device, and the concentrated solution discharge port of the purified ion electrodialysis device is connected to the water inlet of the bipolar membrane device;
the purifying ionic electrodialysis device comprises a membrane assembly, wherein the membrane assembly is arranged between an electrode positive plate and an electrode negative plate;
the membrane assembly includes a single female membrane sheet, yang Mopian;
or the membrane assembly comprises a single male membrane sheet and a female membrane sheet;
or the membrane assembly comprises a single male membrane sheet and a single female membrane sheet;
namely, the purification ionic electrodialysis device is characterized in that the combination of the negative membrane and the positive membrane of the conventional electrodialysis device is replaced by the combination of the single negative membrane and the positive membrane; a combination of the single male membrane and the female membrane; or the combination of the single-positive membrane and the single-negative membrane has the function of extracting the aqueous solution consisting of monovalent cations and monovalent anions from the aqueous solution containing divalent cations and/or divalent anions, whereas the conventional electrodialysis equipment only has the function of concentration and cannot realize the separation process according to the valence of the ions.
Based on the above gas extraction recovery system, it is preferable that the scrubber may be a gas scrubber (gas is directly contacted with the absorption liquid in the tank), a gas scrubber (gas is directly contacted with the absorption liquid in the column), a gas spray scrubber (gas is sprayed with the absorption liquid), a gas circulation spray scrubber (gas is sprayed with the absorption liquid, and the absorption liquid is circulated and sprayed with a pump), or the like.
Based on the above gas extraction recovery system, it is preferable that a part of the substances in the gas is absorbed with an absorption liquid, which contains: alkaline absorption liquid, acidic absorption liquid or water is used as the absorption liquid, and the alkaline absorption liquid or water is generally used as the absorption liquid when substances contained in the gas react with alkaline substances to generate salts (for example, when the gases contain acidic substances); acidic absorption liquids or water are generally used as absorption liquids when substances contained in the gas react with acidic substances to form salts (e.g. when basic substances are contained in the gas);
based on the above gas extraction recovery system, preferably, the common alkaline absorption liquid is an aqueous solution of hydroxide, carbonate, bicarbonate, etc.;
based on the above gas extraction recovery system, preferably, common cations of hydroxide, carbonate, bicarbonate, such as sodium ion, potassium ion, and the like.
Based on the above gas extraction recovery system, preferably, the common acidic absorption liquid is an organic acid, hydrochloric acid, sulfuric acid, nitric acid, or the like.
Based on the gas extraction and recovery system, preferably, the bipolar membrane equipment is characterized in that under the action of a direct current electric field, water is electrolyzed into hydrogen ions and hydroxyl ions by utilizing a bipolar membrane, and strong brine can be converted into acid and alkali by skillfully combining the bipolar membrane with a positive membrane and a negative membrane, and positive ions in the brine are converted into hydroxides corresponding to the positive ions, namely alkali; converting anions in the brine into hydrides corresponding to the anions, namely acids; meanwhile, after the concentration of anions and cations in the strong brine is reduced after being converted into corresponding alkali and acid, the strong brine is called weak brine;
based on the above gas extraction recovery system, preferably, the membranes in the membrane module are arranged in the order of the direction from the positive electrode plate to the negative electrode plate:
when the two or more combinations are arranged, the latter combination is close to the former combination and is arranged between the former combination and the electrode negative plate, namely the membrane component I-1;
or at least one group of combinations sequentially comprising a female diaphragm and a single male diaphragm, wherein when more than or equal to two combinations are arranged, the latter combination is close to the former combination and is arranged between the former combination and the electrode negative plate, namely the membrane component I-2;
Or at least one group of combinations formed by single-negative films and single-positive films in sequence, when more than or equal to two combinations are arranged, the latter combination is close to the former combination and is arranged between the former combination and the electrode negative plate, namely the membrane component I-3.
Based on the above membrane module, preferably, the membrane module I-1 is used for treating the water to be treated with the following water quality, and the following effects are achieved:
(1) when the aqueous solution to be treated contains monovalent cations, monovalent anions and divalent anions or more, the membrane components are alternately combined (the single-negative membrane and Yang Mopian can be repeated for a plurality of times) from the positive electrode plate direction to the negative electrode plate direction, wherein a single-negative membrane, yang Mopian, a single-negative membrane and a positive membrane are arranged in the membrane component, an inlet chamber is formed between the single-negative membrane and the positive membrane in the sequence from the positive electrode plate direction to the negative electrode plate direction, and a concentrating chamber is formed between the Yang Mopian single-negative membrane (the specific connection mode and the principle refer to the figure I-1):
the monovalent anions in the water inlet chamber move towards the positive electrode plate direction and pass through the single negative film (because the single negative film cannot intercept the monovalent anions) to enter the concentration chamber, and the monovalent anions in the concentration chamber are blocked by the positive film when the monovalent anions move towards the positive electrode plate direction, so that the monovalent anions are left in the concentration chamber;
The divalent anions which are more than or equal to in the water inlet chamber move towards the positive plate direction of the electrode and cannot pass through the single-negative membrane and be blocked by the single-negative membrane (because the single-negative membrane can intercept the divalent anions which are more than or equal to) and cannot enter the concentration chamber, so that the divalent anions which are more than or equal to remain in the water inlet chamber;
monovalent cations in the water inlet chamber move towards the electrode negative plate and pass through the positive membrane to enter the concentration chamber, and when the monovalent cations in the concentration chamber move towards the electrode negative plate again, the monovalent cations are blocked by the single negative membrane and remain in the concentration chamber;
the final concentrating chamber yields a concentrate containing monovalent cations and monovalent anions.
(2) When the aqueous solution to be treated contains monovalent cations, divalent cations, monovalent anions and divalent anions, the single-negative membrane and the positive membrane are alternately combined (the single-negative membrane and Yang Mopian can be repeated for many times) from the direction of the positive electrode plate to the direction of the negative electrode plate, and a water inlet chamber is formed between the single-negative membrane and the positive membrane in the sequence of the direction of the positive electrode plate and the direction of the negative electrode plate, and a concentrating chamber is formed between the Yang Mopian single-negative membrane and the positive membrane (the specific connection mode and the principle refer to the diagram I-1-1):
The monovalent anions in the water inlet chamber move towards the positive electrode plate direction and pass through the single negative film (because the single negative film cannot intercept the monovalent anions) to enter the concentration chamber, and the monovalent anions in the concentration chamber are blocked by the positive film when the monovalent anions move towards the positive electrode plate direction, so that the monovalent anions are left in the concentration chamber;
the divalent anions which are more than or equal to in the water inlet chamber move towards the positive plate direction of the electrode and cannot pass through the single-negative membrane and be blocked by the single-negative membrane (because the single-negative membrane can intercept the divalent anions which are more than or equal to) and cannot enter the concentration chamber, so that the divalent anions which are more than or equal to remain in the water inlet chamber;
monovalent cations and more than or equal to divalent cations in the water inlet chamber move towards the negative electrode plate direction, pass through the positive membrane and enter the concentration chamber;
the final concentration chamber is obtained as a concentrated solution containing monovalent cations and divalent cations or more and monovalent anions.
Based on the above gas extraction and recovery system, preferably, the membrane module I-2 is used for treating the water solution to be treated with the following water quality, and the following effects are achieved:
(1) when the aqueous solution to be treated contains monovalent cations, divalent cations and monovalent anions, the membrane component is arranged in the direction from the positive electrode plate to the negative electrode plate and comprises a combination of negative membranes, single positive membranes, negative membranes and single positive membranes alternately (the combination unit of the negative membranes and the single positive membranes can be repeated for a plurality of times), an intake chamber is formed between the negative membranes and the single positive membranes in the sequence from the direction of the positive electrode plate to the direction of the negative electrode plate, and a concentration chamber is formed between the single positive membranes and the negative membranes (the specific connection mode and the principle refer to the diagram I-2):
Monovalent cations in the water inlet chamber move towards the electrode negative plate and pass through the single-cation membrane (because the single-cation membrane cannot intercept the monovalent cations) to enter the concentration chamber, and the monovalent cations in the concentration chamber are blocked by the negative membrane when the monovalent cations move towards the electrode negative plate, so that the monovalent cations are left in the concentration chamber;
the divalent cations in the water inlet chamber can not pass through the single-cation membrane (because the single-cation membrane can intercept the divalent cations) and can not enter the concentration chamber when moving towards the negative electrode plate, and the divalent cations remain in the water inlet chamber;
monovalent anions in the water inlet chamber move towards the positive electrode plate direction of the electrode, pass through the negative film piece and enter the concentration chamber;
the final concentrating chamber yields a concentrate containing monovalent cations and monovalent anions.
(2) When the aqueous solution to be treated contains monovalent cations, monovalent anions, divalent anions or divalent cations, the membrane component is arranged in the direction from the positive electrode plate to the negative electrode plate and comprises a combination of negative membranes, single-positive membranes, negative membranes and single-positive membranes (the combination unit of the negative membranes and the single-positive membranes can be repeated for a plurality of times), a water inlet chamber is formed between the negative membranes and the single-positive membranes in sequence from the direction of the positive electrode plate to the direction of the negative electrode plate, and a concentration chamber is formed between the single-positive membranes and the negative membranes (the specific connection mode and the principle refer to the diagram I-2-1):
Monovalent cations in the water inlet chamber move towards the electrode negative plate and pass through the single-cation membrane (because the single-cation membrane cannot intercept the monovalent cations) to enter the concentration chamber, and the monovalent cations in the concentration chamber are blocked by the negative membrane when the monovalent cations move towards the electrode negative plate, so that the monovalent cations are left in the concentration chamber;
the divalent cations in the water inlet chamber can not pass through the single-cation membrane (because the single-cation membrane can intercept the divalent cations) and can not enter the concentration chamber when moving towards the negative electrode plate, and the divalent cations remain in the water inlet chamber;
monovalent anions and more than or equal to divalent anions in the water inlet chamber move towards the positive electrode plate direction of the electrode, pass through the negative film piece and enter the concentration chamber;
the final concentrating chamber is the concentrated solution containing monovalent cations, monovalent anions and divalent anions or more.
Based on the above gas extraction and recovery system, preferably, the membrane module I-3 is used for treating the water solution to be treated with the following water quality, and the following effects are achieved:
(1) when the aqueous solution to be treated contains monovalent cations, monovalent anions and divalent anions or more, the membrane components are alternately combined (the single-negative membrane and single-positive membrane can be repeated for a plurality of times) from the positive electrode plate direction to the negative electrode plate direction, wherein a single-negative membrane, a single-positive membrane and a single-positive membrane are arranged in the membrane component, an inlet chamber is formed between the single-negative membrane and the single-positive membrane in the sequence of the positive electrode plate direction to the negative electrode plate direction, and a concentration chamber is formed between the single-positive membrane and the single-negative membrane (the specific connection mode and the principle refer to the diagram I-3):
The monovalent anions in the water inlet chamber move towards the positive electrode plate direction of the electrode and pass through the single negative film (because the single negative film cannot intercept the monovalent anions) to enter the concentration chamber, and the monovalent anions in the concentration chamber are blocked by the single positive film when the monovalent anions move towards the positive electrode plate direction, so that the monovalent anions are left in the concentration chamber;
the divalent anions which are more than or equal to in the water inlet chamber move towards the positive plate direction of the electrode and cannot pass through the single-negative membrane and be blocked by the single-negative membrane (because the single-negative membrane can intercept the divalent anions which are more than or equal to) and cannot enter the concentration chamber, so that the divalent anions which are more than or equal to remain in the water inlet chamber;
monovalent cations in the water inlet chamber move towards the electrode negative plate and pass through the single-cation membrane to enter the concentration chamber, and the monovalent cations in the concentration chamber are blocked by the single-cathode membrane when the monovalent cations move towards the electrode negative plate;
the final concentrating chamber yields a concentrate containing monovalent cations and monovalent anions.
(2) When the water solution to be treated contains monovalent cations, divalent cations and monovalent anions, the membrane components are alternately combined (the single-negative membrane and single-positive membrane can be repeated for a plurality of times) from the positive electrode plate direction to the negative electrode plate direction, wherein a single-negative membrane, a single-positive membrane and a single-positive membrane are arranged in the membrane component, an inlet chamber is formed between the single-negative membrane and the single-positive membrane in the sequence of the positive electrode plate direction to the negative electrode plate direction, and a concentration chamber is formed between the single-positive membrane and the single-negative membrane (the specific connection mode and the principle refer to the diagram I-3-1):
Monovalent cations in the water inlet chamber move towards the electrode negative plate and pass through the single-cation membrane (because the single-cation membrane cannot intercept the monovalent cations) to enter the concentration chamber, and the monovalent cations in the concentration chamber are blocked by the single-cathode membrane when the monovalent cations move towards the electrode negative plate, so that the monovalent cations are left in the concentration chamber;
the divalent cations in the water inlet chamber can not pass through the single-cation membrane (because the single-cation membrane can intercept the divalent cations) and can not enter the concentration chamber when moving towards the negative electrode plate, and the divalent cations remain in the water inlet chamber;
monovalent anions in the water inlet chamber move towards the positive electrode plate direction of the electrode and pass through the single negative film piece to enter the concentration chamber;
the final concentrating chamber yields a concentrate containing monovalent cations and monovalent anions.
(3) When the water solution to be treated contains monovalent cations, divalent cations, monovalent anions and divalent anions, the water solution to be treated contains alternate combination (a combination unit which can repeatedly form a single negative film and a single positive film for many times) of single negative film, single positive film, single negative film and single positive film which are arranged in the film component from the direction of the positive electrode plate to the direction of the negative electrode plate, wherein an inlet chamber is formed between the single negative film and the single positive film in the sequence of the direction of the positive electrode plate to the direction of the negative electrode plate, and a concentration chamber is formed between the single positive film and the single negative film (specific connection mode and principle reference diagram I-3-2):
The monovalent anions in the water inlet chamber move towards the positive electrode plate direction of the electrode and pass through the single negative film (because the single negative film cannot intercept the monovalent anions) to enter the concentration chamber, and the monovalent anions in the concentration chamber are blocked by the single positive film when the monovalent anions move towards the positive electrode plate direction, so that the monovalent anions are left in the concentration chamber;
the divalent anions which are more than or equal to in the water inlet chamber move towards the positive plate direction of the electrode and cannot pass through the single-negative membrane and be blocked by the single-negative membrane (because the single-negative membrane can intercept the divalent anions which are more than or equal to) and cannot enter the concentration chamber, so that the divalent anions which are more than or equal to remain in the water inlet chamber;
monovalent cations in the water inlet chamber move towards the electrode negative plate and pass through the single-cation membrane to enter the concentration chamber, and when the monovalent cations in the concentration chamber move towards the electrode negative plate again, the monovalent cations are blocked by the single-anion membrane, so that the monovalent cations are left in the concentration chamber;
the divalent cations in the water inlet chamber move towards the negative electrode plate direction and cannot pass through the single-cation membrane to remain in the water inlet chamber;
the final concentrating chamber yields a concentrate containing monovalent cations and monovalent anions.
Based on the above gas extraction recovery system, preferably, the membrane module I-1: a positive diaphragm (corresponding to a figure III-1) is arranged between the positive electrode plate and the combination of the first single negative diaphragm and the positive diaphragm;
Or membrane module I-1: a single-negative membrane is arranged between the last single-negative membrane, the combination of the positive membrane and the electrode negative plate (corresponding to the figure III-1-1);
or membrane module I-2: a female diaphragm (corresponding to the figure III-2) is arranged between the last female diaphragm, the combination of the single male diaphragms and the electrode negative plate;
or membrane module I-2: a single-positive membrane (corresponding to the figure III-2-1) is arranged between the positive electrode plate and the first combination of the negative membrane and the single-positive membrane;
or membrane module I-3: a single-negative membrane is arranged between the last single-negative membrane, the combination of the single-positive membrane and the electrode negative plate (corresponding to the figure III-3);
or membrane module I-3: a single-positive membrane (corresponding to the figure III-3-1) is arranged between the positive electrode plate and the first single-negative membrane and single-positive membrane combination.
Based on the above gas extraction recovery system, preferably,
the membrane component I-1 is arranged from the direction of the positive electrode plate to the direction of the negative electrode plate: an intake chamber is formed between the single negative membrane and the positive membrane, and a concentration chamber is formed between Yang Mopian and the single negative membrane;
or the membrane component I-2 is arranged from the positive electrode plate direction to the negative electrode plate direction: an intake chamber is formed between the female membrane and the single-male membrane, and a concentration chamber is formed between the single-male membrane and the female membrane;
Or the membrane component I-3 is arranged from the positive electrode plate direction to the negative electrode plate direction: an intake chamber is formed between the single-negative membrane and the single-positive membrane, and a concentration chamber is formed between the single-positive membrane and the single-negative membrane;
or the electrode positive plate and one membrane closest to the electrode positive plate form a polar water chamber I, and the electrode negative plate and one membrane closest to the electrode negative plate form a polar water chamber II (the closest membrane is called as a membrane no matter a positive membrane, a negative membrane, a single positive membrane or a single negative membrane, etc., namely, the closest membrane can refer to the positive membrane, the negative membrane, the single positive membrane or the single negative membrane, etc., as long as the closest membrane is positioned closest to the electrode positive plate or the electrode negative plate).
Based on the above gas extraction recovery system, it is preferred, or when the membrane module I-1: when a positive diaphragm is arranged between the positive electrode plate and the first single-negative diaphragm and the positive diaphragm combination: yang Mopian adjacent to the positive electrode plate and/or adjacent to the negative electrode plate is replaced with a nanofiltration membrane or mono Yang Mopian; when the aqueous solution to be treated contains only monovalent cations, the Yang Mopian adjacent to the positive electrode plate and/or adjacent to the negative electrode plate is replaced by a nanofiltration membrane or a single Yang Mopian, the effect being the same; when the aqueous solution to be treated contains divalent cations or more, the Yang Mopian adjacent to the positive electrode plate of the electrode cannot be replaced by a nanofiltration membrane or a single Yang Mopian; the polar water may be a base corresponding to a monovalent cation or a salt formed with a monovalent anion;
Or when the membrane module I-1: when the single-negative membrane is arranged between the last single-negative membrane, the combination of the positive membrane and the combination of the electrode negative plate: the single negative membrane sheet close to the positive electrode plate and/or close to the negative electrode plate is replaced by a negative membrane sheet or a nanofiltration membrane sheet; when the anions contained in the aqueous solution to be treated are monovalent anions, the single negative film sheet close to the positive electrode plate and/or the single negative film sheet close to the negative electrode plate is replaced by the negative film sheet, and the effects are the same; when the water solution to be treated contains divalent anions or more, only the single negative membrane close to the electrode negative plate is replaced by the negative membrane; the single negative membrane sheet can be replaced by the nanofiltration membrane sheet under any condition; the polar water may be an acid corresponding to a monovalent anion or a salt formed with a monovalent cation;
or when the membrane module I-2: and when the last female diaphragm is arranged between the female diaphragm and the electrode negative plate, the single male diaphragm is combined with the female diaphragm: the negative film sheet near the positive electrode plate and/or near the negative electrode plate is replaced by a nanofiltration film sheet or a single negative film sheet; when the anions contained in the aqueous solution to be treated are monovalent anions, the negative film close to the positive electrode plate and/or the negative film close to the negative electrode plate is replaced by a nanofiltration film or a single negative film, and the effects are the same; when the water solution to be treated contains divalent anions or more, the negative film close to the electrode negative plate cannot be replaced by a nanofiltration film or a single negative film; the polar water may be an acid corresponding to a monovalent anion or a salt formed with a monovalent cation;
Or when the membrane module I-2: when a single-positive membrane is arranged between the positive electrode plate and the first combination of the negative membrane and the single-positive membrane: the single positive membrane adjacent to the positive electrode plate and/or adjacent to the negative electrode plate is replaced by a nanofiltration membrane or a positive membrane; when the water solution to be treated contains cations only with monovalent cations, the single-positive membrane close to the positive electrode plate and/or the single-positive membrane close to the negative electrode plate is replaced by the positive membrane, and the effect is the same; when the water solution to be treated contains divalent cations or more, only the single-positive membrane close to the positive plate of the electrode is replaced by the positive membrane; the single-cation membrane can be replaced by the nanofiltration membrane under any condition; the polar water may be a base corresponding to a monovalent cation or a salt formed with a monovalent anion;
or when the membrane module I-3: and when the single negative film is arranged between the last single negative film, the combination of the single positive film and the electrode negative plate: the single negative film sheet near the positive electrode plate and/or near the negative electrode plate is replaced by a nanofiltration film sheet or a negative film sheet; when the anions contained in the aqueous solution to be treated are monovalent anions, the single negative film sheet close to the positive electrode plate and/or the single negative film sheet close to the negative electrode plate is replaced by the negative film sheet, and the effects are the same; when the water solution to be treated contains divalent anions or more, only the single negative membrane close to the electrode negative plate is replaced by the negative membrane; the single negative membrane sheet can be replaced by the nanofiltration membrane sheet under any condition; the polar water may be an acid corresponding to a monovalent anion or a salt formed with a monovalent cation;
Or when the membrane module I-3: when a single-positive membrane is arranged between the positive electrode plate and the first single-negative membrane and the single-positive membrane combination: the single positive membrane close to the positive electrode plate and/or close to the negative electrode plate is replaced by a positive membrane or a nanofiltration membrane; when the water solution to be treated contains cations only with monovalent cations, the single-positive membrane close to the positive electrode plate and/or the single-positive membrane close to the negative electrode plate is replaced by the positive membrane, and the effect is the same; when the water solution to be treated contains divalent cations or more, only the single-positive membrane close to the positive plate of the electrode is replaced by the positive membrane; the single-cation membrane can be replaced by the nanofiltration membrane under any condition; the polar water may be a base corresponding to the monovalent cation or a salt with the monovalent anion.
Based on the above gas extraction and recovery system, preferably, the outlet of the water inlet chamber is connected to the inlet of the water inlet tank, the outlet of the water inlet tank is connected to the water inlet circulating pump, and the outlet of the water inlet circulating pump is connected to the inlet of the water inlet chamber to form a circulation;
or the outlet of the concentration chamber is connected to the inlet of the concentration tank, the outlet of the concentration tank is connected to the concentration circulating pump, and the outlet of the concentration circulating pump is connected to the inlet of the concentration chamber to form a circulation;
Or the outlet of the polar water chamber I is connected to the inlet of the polar water tank I, the outlet of the polar water tank I is connected to the polar water circulating pump I, and the outlet of the polar water circulating pump I is connected to the inlet of the polar water chamber I to form circulation; the outlet of the polar water chamber II is connected to the inlet of the polar water tank II, the outlet of the polar water tank II is connected to the polar water circulating pump II, and the outlet of the polar water circulating pump II is connected to the inlet of the polar water chamber II to form circulation;
or the outlet of the polar water chamber I and the outlet of the polar water chamber II are connected to the inlet of the polar water tank, the outlet of the polar water tank is connected to the polar water circulating pump, and the outlet of the polar water circulating pump is connected to the inlet of the polar water chamber I and the inlet of the polar water chamber II to form circulation.
Based on the gas extraction and recovery system, preferably, the concentration tank is provided with a water inlet pipe and a discharge port;
or the water inlet tank is provided with a water inlet pipe and a discharge port;
or the water tank I is provided with a water inlet pipe, and the water tank II is provided with a water inlet pipe;
or the polar water tank is provided with a water inlet pipe.
Based on the above gas extraction recovery system, preferably,
the polar water chamber I can be independently provided with a set of polar water tank and a polar water circulating pump; the polar water chamber II can be independently provided with a set of polar water tank and polar water circulating pump, namely the polar water of the polar water chamber I is not mixed with the polar water of the polar water chamber II;
Or the polar water chamber I and the polar water chamber II can share a set of polar water tank and a polar water circulating pump, namely, the polar water of the polar water chamber I and the polar water of the polar water chamber II are mixed.
Based on the above gas extraction and recovery system, it is preferable that the electrode positive electrode plate and the electrode negative electrode plate function as a power source for supplying direct current voltage.
Based on the above gas extraction recovery system, preferably,
the ion contained in the aqueous solution in the direction of the electrode negative plate at the joint of the membrane and the membrane closest to the electrode positive plate can also correspond to the characteristics of the membrane according to the valence state and the cathode and anode of the ion, and the ion species which can penetrate the membrane into the polar water chamber I; similarly, the ion contained in the aqueous solution in the direction of the positive electrode plate at the joint of the membrane and the electrode plate closest to the negative electrode plate can also correspond to the characteristics of the membrane according to the valence state and the yin-yang property of the ion, and the ion species which can penetrate the membrane into the polar water chamber II.
Based on the above gas extraction recovery system, preferably,
the replacement of the type of membrane according to the invention, which does not lead to a change in the type of chamber, occurs on the membrane closest to the positive electrode plate and/or on the membrane closest to the negative electrode plate, in particular:
The original position is the water inlet chamber, the membrane is still the water inlet chamber after being replaced, the original position is the concentration chamber, the membrane is still the concentration chamber after being replaced, the original position is the polar water chamber I, the membrane is still the polar water chamber I after being replaced, the original position is the polar water chamber II, and the membrane is still the polar water chamber II after being replaced.
Based on the above gas extraction recovery system, preferably,
the concentration tank is provided with a water inlet pipe and a discharge port (generally an overflow port), pure water is replenished to the concentration tank, and concentrated solution is discharged: because the concentration of the concentrated solution in the concentration tank is higher and higher continuously in the concentration chamber, the concentrated solution is required to be discharged to be used as a concentrated solution product, and in order to control the concentration of the concentrated solution of the product with stable concentration, the pure water is generally added into the concentration tank to control the water quantity, so that the concentration of the concentrated solution in the concentration tank is ensured to be expanded in a fixed volume, and the overflow of the concentrated solution of the product with fixed concentration is used as the product to be collected in an overflow mode of the concentration tank;
or the water inlet tank is provided with a water inlet pipe and a discharge port (generally an overflow port), the water inlet tank is supplemented with a target aqueous solution to be treated, the supplementing aqueous solution is also supplemented with ions, and a part of treated aqueous solution is discharged from the water inlet tank, specifically:
The ion in the water inlet chamber is always reduced and lost, so that new ions are required to be continuously supplemented to ensure the ion concentration, the target aqueous solution to be treated is required to be supplemented to the water inlet chamber to supplement the amount of fresh ions, and meanwhile, the volume in the water inlet chamber is expanded after the target aqueous solution to be treated is supplemented, so that a part of dilute brine with reduced ion concentration is overflowed from the water inlet chamber in an overflow mode;
the water inlet pipe of the water inlet tank is the water inlet of the whole electrodialysis device.
Or a water inlet pipe is arranged on the polar water tank, the polar water tank I or the polar water tank II.
Based on the above gas extraction recovery system, preferably,
the water inlet tank is internally provided with a partition plate, a water inlet pipe (for supplementing the water solution to be treated) of the water inlet tank is arranged on one side, backwater of the water inlet chamber and an overflow port are arranged on the other side, and ions are supplemented for the water inlet tank, so that the ion concentration in the water solution to be treated, which is supplemented by the water inlet pipe, is higher, the ion concentration of backwater of the water inlet chamber is low, the partition plate is used for separating the high-concentration water solution supplemented by the water inlet pipe from the backwater of the water inlet chamber with low concentration (overflows from the backwater side of the water inlet chamber), so that the high-concentration water solution just supplemented by the water inlet pipe is prevented from being directly overflowed and discharged, and two sides are locally communicated (refer to a specific figure II-1);
Or a partition plate is arranged in the concentration tank, a water inlet pipe (supplementing pure water or supplementing water solution to be treated) of the concentration tank is arranged on one side, a backwater and an overflow port of the concentration chamber are arranged on the other side, the concentration of ions of water fed in from the water inlet pipe is low, the concentration of ions of backwater of the concentration chamber is high (overflow is carried out from the backwater side of the concentration chamber), the purpose of the partition plate is to obtain concentrated solution, so that the purpose of the partition plate is to avoid direct overflow discharge of the low-concentration water fed in from the water inlet pipe, the concentration of the concentrated solution is reduced, and the two sides are locally communicated (refer to a specific figure II-2);
based on the gas extraction and recovery system, preferably, the left side and the right side of any membrane are provided with a partition plate between the membranes; the purpose of the separator is to separate the equipment (e.g., membrane and membrane, membrane and electrode plate) on both sides of the separator into a space through which the water flows.
Based on the gas extraction and recovery system, preferably, the nanofiltration membrane is used for allowing monovalent anions and monovalent cations to permeate, and has the effect of preventing permeation (interception) of divalent cations and divalent anions; according to the operation principle of the nanofiltration membrane, some nanofiltration membranes only intercept divalent cations and some nanofiltration membranes only intercept divalent anions.
Based on the above gas extraction recovery system, preferably, the Yang Mopian refers to a cation exchange membrane that allows cations to permeate therethrough and has a permeation (interception) blocking effect on anions; the negative film refers to an anion exchange film, which allows anions to permeate and has the function of preventing cations from permeating (intercepting);
based on the gas extraction and recovery system, preferably, the single-cation membrane is used for allowing monovalent cations to permeate and preventing passing (interception) of divalent cations and anions; the monoanionic membrane is used for allowing monovalent anions to permeate, and has the effect of preventing (intercepting) divalent anions and cations.
Based on the above gas extraction recovery system, preferably, the electrode positive plate is capable of attracting anions; the electrode negative plate can attract cations.
Based on the above gas extraction recovery system, preferably, the electrode positive plate is connected to a direct current positive power supply; the electrode negative plate is connected to a direct current negative power supply to supply power.
Based on the above gas extraction recovery system, it is preferable that the membrane module further has conventional components such as a fixing member, a pressing member, a sealing member, etc., common components, existing components, etc. (i.e., the membrane module further includes common components used for conventional electrodialysis membrane modules) to complete the assembly of the membrane module.
Based on the above gas extraction and recovery system, preferably, an alkali adding unit or a heating unit is further provided:
the outlet of the alkali adding unit is connected to a pipeline between the water solution discharge port of the washing tower and the water inlet of the purified ion electrodialysis device; or an alkalization tank is arranged on a pipeline between the water solution discharge port of the washing tower and the water inlet of the purifying ionic electrodialysis device, and the outlet of the alkalization unit is connected to the inlet of the alkalization tank;
or a heating unit is arranged on a pipeline between the water solution discharge port of the washing tower and the water inlet of the purifying ionic electrodialysis device;
the purpose of designing the alkali adding unit is as follows: when the treated aqueous solution contains bicarbonate, the pH can be raised by adding alkaline substances (exemplified by sodium hydroxide) to the treated aqueous solution, so that the bicarbonate is converted into carbonate, namely, monovalent anions are converted into divalent anions;
based on the above gas extraction recovery system, preferably, the inlet of the alkalizing unit is connected to an alkali tank or an alkali pipeline or an alkali producing tank of the bipolar membrane device;
the inlet of the alkali adding unit is connected to an alkali tank or an alkali producing tank of the bipolar membrane equipment, and a conveying power pump or an alkali recycling pump of the bipolar membrane equipment is used as conveying power;
The inlet of the alkali adding unit is connected to an alkali pipeline, and the self-pressure of the alkali pipeline is used as conveying power;
based on the above gas extraction recovery system, preferably,
the method comprises the steps of connecting an alkali tank or an alkali producing tank of the bipolar membrane equipment to an inlet of an alkali adding unit, automatically monitoring and controlling the quantity of variable frequency discharge quantity of the conveying power pump or an alkali recycling pump of the bipolar membrane equipment or the quantity of reflux quantity of the conveying power pump or the alkali recycling pump of the bipolar membrane equipment by using the pH of an aqueous solution after alkali addition in a chain manner, and finally, automatically controlling the quantity of alkali addition by using the pH to stably control the pH of the aqueous solution after alkali addition;
and the control valve on the alkali pipeline is used for controlling the quantity of the alkali addition by automatically monitoring and controlling the pH value of the aqueous solution after the alkali addition in a chain manner so as to stably control the pH value of the aqueous solution after the alkali addition.
Based on the above gas extraction and recovery system, preferably, a stirring device is arranged in the alkalizing tank.
Based on the above gas extraction recovery system, preferably, the stirring device includes a stirrer, compressed gas stirring, and the like.
Based on the above gas extraction recovery system, preferably, a heating unit is further provided:
The heating unit is arranged on a pipeline between an aqueous solution discharge port of the washing tower and a water inlet of the purifying ion electrodialysis device and is used for heating (for example, a heating heat exchanger is arranged);
or the heating unit is arranged on a pipeline between the water solution discharge port of the washing tower and the water inlet of the purifying ionic electrodialysis device and is used for heating (for example, a heating heat exchanger is arranged), and a decarburization tower is arranged between the heating unit and the water inlet of the purifying ionic electrodialysis device;
or a heating tank is arranged, the solution discharge port of the washing tower is connected to the water inlet of the heating tank, the water outlet of the heating tank is connected to the water inlet of the purification ion electrodialysis device, and the heating unit is used for heating the heating tank;
or a heating tank and a decarburization tower are arranged, the solution discharge port of the washing tower is connected to the water inlet of the heating tank, the heating unit is used for heating the heating tank, the water outlet of the heating tank is connected to the water inlet of the decarburization tower, and the water outlet of the decarburization tower is connected to the water inlet of the purified ion electrodialysis device;
the purpose of designing the heating unit is: when the aqueous solution entering the purified ion electrodialysis device contains bicarbonate, the bicarbonate is converted into carbonate and carbon dioxide through heating energy, and the carbon dioxide can be dissipated into the air and removed from the water (the concentration of the bicarbonate in the water is reduced at the moment), namely, monovalent anions are converted into divalent anions;
Based on the above gas extraction and recovery system, preferably, the heating device is a heat exchanger, a reboiler (the reboiler and the heating tank form an integral heating device), coil heating, jacket heating and the like, and the heat source can be steam, electricity and the like.
Based on the above extraction recovery system, preferably, a cooler is further provided:
the cooler is arranged on a pipeline between the heating unit and the water inlet of the purifying ionic electrodialysis device;
or the cooler is arranged on a pipeline between the decarburization tower and the water inlet of the purified ion electrodialysis device;
or the cooler is arranged on a pipeline between the heating tank and the water inlet of the purifying ionic electrodialysis device.
Based on the above gas extraction and recovery system, the cooler may be a heat exchanger, etc., and the cold source may be cooling water, chilled water, etc., or an aqueous solution that needs to be heated.
Based on the above gas extraction and recovery system, preferably, an acid adding unit is further provided:
an outlet of the acid adding unit is connected to a pipeline between a concentrated solution discharge port of the purified ion electrodialysis device and a water inlet of the bipolar membrane device; or an acidification tank is arranged on a pipeline between a concentrated solution discharge port of the purification ion type electrodialysis device and a water inlet of the bipolar membrane device, and an outlet of the acidification unit is connected to an inlet of the acidification tank. The acid adding unit is used for adding acid, and the purpose of acid adding is to neutralize a small amount of carbonate and bicarbonate remained in the aqueous solution by using acid, and the pH is generally controlled to be 1-7;
If the aqueous solution before finally entering the bipolar membrane device still contains a certain concentration of carbonate or bicarbonate, carbonic acid is generated in an acid chamber during the operation of the bipolar membrane device and is converted into carbon dioxide gas, and the operation stability of the bipolar membrane device is affected by the generation of gas in the acid chamber.
Based on the above gas extraction recovery system, preferably, the inlet of the acid adding unit is connected to an acid tank or an acid pipe or an acid producing tank of the bipolar membrane electrodialysis apparatus;
based on the above gas extraction recovery system, preferably, the acid added by the acid adding unit is hydrobromic acid or acetic acid;
based on the above gas extraction and recovery system, preferably, an inlet of the acid adding unit is connected to an acid tank or an acid tank of the bipolar membrane device, and a conveying power pump or an acid recycling pump of the bipolar membrane device is used as conveying power;
and an inlet of the acid adding unit is connected to an acid pipeline, and the self-contained pressure of the acid pipeline is used as conveying power.
Based on the above gas extraction recovery system, preferably,
the pH value of the aqueous solution after acid addition is automatically monitored by using an acid tank or an acid producing tank of the bipolar membrane equipment and connected to the inlet of the acid adding unit, and the quantity of variable frequency discharge quantity of the conveying power pump or the acid recycling pump of the bipolar membrane equipment is controlled in a chain manner or the reflux quantity of the conveying power pump or the acid recycling pump of the bipolar membrane equipment is controlled, so that the aim of automatically adjusting the acid adding quantity by using the pH value is finally achieved, and the pH value of the aqueous solution after acid addition is stably controlled;
And the pH value of the aqueous solution after acid addition is controlled by using a control valve on the acid pipeline to control the amount of the acid to be added in a linkage manner.
Based on the above gas extraction and recovery system, preferably, a decarbonization tower is further provided: the decarbonization tower is connected to a pipeline between a concentrated solution discharge port of the purified ion electrodialysis device and a water inlet of the bipolar membrane device and a connection point of an outlet of an acid adding unit to a pipeline between the water inlet of the bipolar membrane device;
or the decarbonization tower is connected to a pipeline between the acidification tank and a water inlet of the bipolar membrane device.
Based on the above gas extraction and recovery system, preferably, the decarbonization tower is operated by spraying the aqueous solution from top to bottom, and the compressed air convects with the aqueous solution from bottom to top to blow out free carbon dioxide in the aqueous solution into the air.
Based on the above gas extraction and recovery system, preferably, a concentration device I is further provided, wherein a dilute brine outlet of the purified ion electrodialysis device is connected to a water inlet of the concentration device I, and a concentrated solution outlet of the concentration device I is connected to a water inlet of the alkalization tank or a water inlet of the purified ion electrodialysis device.
Based on the above gas extraction and recovery system, preferably, a concentration device II is further provided, wherein the dilute brine outlet of the bipolar membrane device is connected to the water inlet of the concentration device II, and the concentrate outlet of the concentration device II is connected to the water inlet of the acidification tank or the water inlet of the bipolar membrane device.
Because the dilute brine of the bipolar membrane equipment still contains a certain concentration of salt, the bipolar membrane equipment can be used for regenerating acid and alkali after concentration, so that more economic value is obtained, and the direct discharge waste is preferably avoided.
Based on the above gas extraction recovery system, preferably, the outlet I of the alkali producing tank of the bipolar membrane device is connected to the inlet of the washing tower or the alkali adding unit, and the outlet II of the alkali producing tank of the bipolar membrane device is a product alkali recovery outlet.
Based on the above gas extraction recovery system, preferably, the acid recovery pump of the bipolar membrane device is connected to the inlet of the acid adding unit; or the acid product pump of the bipolar membrane device is connected to the feed inlet of the oxidation reaction system; or the acid product pump of the bipolar membrane device is connected to the feed inlet of a mixing tank, and the discharge outlet of the mixing tank is connected to the feed inlet of an oxidation reaction system.
Based on the gas extraction and recovery system, preferably, the acid generating tank of the bipolar membrane device is provided with a heating device (for example, the heating device is heated to the boiling point temperature under the concentration of 20 ℃ to the hydrobromic acid) and/or a blowing device, when a small amount of chlorine element is in the aqueous solution discharged from the solution discharge port of the washing tower, the chlorine element is accompanied with bromine element, and finally, the obtained hydrobromic acid is treated by the bipolar membrane device, and the hydrogen chloride with low concentration is mixed, so that the hydrogen chloride is more volatile than the hydrogen bromide, and can be discharged into a gas phase through the heating device and/or the blowing device, so that the concentration of hydrogen chloride impurities in the hydrobromic acid in a liquid phase is reduced, and the hydrobromic acid in the liquid phase is purer.
Based on the above gas extraction recovery system, preferably, the acid-producing tank of the bipolar membrane device is discharged to a dechlorination tank (i.e. final HBr product recovery), the dechlorination tank is provided with a heating device (for example, heating to a boiling point temperature of 20 ℃ below the hydrobromic acid concentration) and/or a blowing device, when a small amount of chlorine element is contained in the aqueous solution discharged from the solution discharge port of the washing tower, the chlorine element is also accompanied by bromine element to be finally treated by the bipolar membrane device, and the obtained hydrobromic acid is mixed with low-concentration hydrogen chloride, which is more volatile than hydrogen bromide, so that the hydrogen chloride can be discharged into a gas phase through the heating device and/or the blowing device, thereby reducing the impurity concentration of the hydrogen chloride in the hydrobromic acid in a liquid phase and ensuring that the hydrobromic acid in the liquid phase is purer.
Based on the above gas extraction recovery system, preferably, a hardness removal device is provided:
when the water solution discharged from the solution discharge port of the washing tower contains hardness, the device for removing hardness is also arranged, and the device for removing hardness is arranged at any position between the water solution discharge port of the washing tower and the water inlet of the purified ion electrodialysis device.
Based on the above gas extraction recovery system, preferably, the hardness removal device may be a resin column, in which a resin of calcium and magnesium ions in water is filled.
Based on the above gas extraction recovery system, preferably, the resin for removing calcium and magnesium ions in water is regenerated with salt or with acid after being saturated by adsorption.
Based on the above gas extraction and recovery system, preferably, the exhaust gas discharge port of the oxidation reaction system is connected to the gas inlet of the cooling device, the gas outlet of the cooling device is connected to the gas inlet of the absorption tower, the gas outlet of the absorption tower is connected to the gas inlet of the gas organic matter removing device (such as a gas incineration device or a gas oxidation device, for reducing the organic matter content of other VOCs), and the gas outlet of the gas organic matter removing device is connected to the gas inlet pipeline of the washing tower; or the tail gas discharge port of the oxidation reaction system is connected to the gas inlet of the cooling device, the gas outlet of the cooling device is connected to the gas inlet of the absorption tower, the gas outlet of the absorption tower is connected to the gas inlet of the turbine, the gas outlet of the turbine is connected to the gas inlet of the gas organic matter removing device (such as the gas burning device or the gas oxidizing device, and the content of other VOC organic matters is reduced), and the gas outlet of the gas organic matter removing device is connected to the gas inlet pipeline of the washing tower.
Based on the above gas extraction and recovery system, preferably, the gas treated by the extraction and recovery system refers to the gas corresponding to the aqueous solution containing divalent cations and/or divalent anions generated after the gas is absorbed by the absorption liquid.
Based on the gas extraction and recovery system, preferably, the gas treated by the extraction and recovery system is tail gas of an oxidation reaction system of a terephthalic acid production device.
Based on the above gas extraction recovery system, preferably, a plurality of buffer tanks and/or transfer pumps may be provided for smooth operation of the present extraction recovery system.
The emission is emitted from the process route of the utility model after being treated by the utility model, and no matter what specific treatment method is adopted after the emission, the protection of the content of the utility model is not affected.
The purposes of different steps, units and the like designed by the utility model are different and mutually independent, each step, unit and the like can be independently applied, can be selected and combined in different sequences according to actual demands, and can be only selected and applied to a part of steps, units and the like, and the steps, the units and the like are all within the scope of the patent protection of the utility model.
Advantageous effects
The utility model aims to provide a gas extraction and recovery system, which can reduce the pollution of the gas to the environment and recover the economic value of beneficial substances in the gas after the gas is treated by the system.
The system is simple to operate and equipment, fully considers recycling and reusing as much as possible, and greatly helps to reduce the running cost of enterprises.
Meanwhile, the purification ionic electrodialysis device applied in the utility model can extract the aqueous solution only containing monovalent ions (namely, the aqueous solution consisting of monovalent cations and monovalent anions) from the aqueous solution containing multivalent ions (the aqueous solution discharged from a washing tower), and concentrate the ion concentration (namely, the ion concentration of the aqueous solution consisting of monovalent cations and monovalent anions) to obtain concentrated solution (for example, carbon dioxide and hydrobromic acid are contained in gas, sodium hydroxide is used as an absorption solution to obtain the aqueous solution rich in sodium bromide, sodium bicarbonate and sodium carbonate, and the monovalent anionic bicarbonate is firstly converted into divalent anionic carbonate, so that only monovalent anionic bromide ions, divalent anionic carbonate ions and monovalent cationic sodium ions in water can be obtained through the purification ionic electrodialysis device of the utility model, namely, sodium bromide and sodium carbonate are separated, namely, the purification of the aqueous solution of monovalent ions is realized through one device of the purification ionic electrodialysis device, and the double functions of concentrating the aqueous solution of monovalent ions (the conventional electrodialysis device has the functions of only one membrane 57assembly, namely, the purification unit is simple, and the whole system cannot be maintained, and the whole purification device can not be produced easily and has the functions of only has the functions of the membrane Yang Mopian. In addition, the concentration effect in the purification ionic electrodialysis device is reflected without using steam for heating, so that the operation cost is low and the heat energy is not consumed.
Drawings
FIG. I-1: the membrane component is arranged in the direction from the positive electrode plate to the negative electrode plate and comprises single-negative membrane sheets, yang Mopian, single-negative membrane sheets and positive membrane sheets which are alternately combined, and a schematic diagram of the principle of treating an aqueous solution containing monovalent cations, divalent anions or more and monovalent anions is treated;
FIG. I-1-1: the principle schematic diagram of treating the aqueous solution containing monovalent cations, divalent cations, monovalent anions and divalent anions is arranged in the membrane component from the direction of the positive electrode plate to the direction of the negative electrode plate, wherein the membrane component comprises single-negative membrane, yang Mopian, single-negative membrane and positive membrane;
FIG. I-2: the principle schematic diagram of treating the aqueous solution containing monovalent cations, divalent cations or more and monovalent anions is that the membrane component is arranged in the direction from the positive electrode plate to the negative electrode plate and comprises a combination of negative membrane, single-positive membrane, negative membrane and single-positive membrane alternately;
FIG. I-2-1: the principle schematic diagram of treating the aqueous solution containing monovalent cations, divalent cations, monovalent anions and divalent anions is arranged in the membrane component from the direction of the positive electrode plate to the direction of the negative electrode plate, wherein the alternative combination comprises a negative membrane, a single-positive membrane, a negative membrane and a single-positive membrane;
FIG. I-3: the principle schematic diagram of treating the aqueous solution containing monovalent cations, divalent anions or more and monovalent anions by alternately combining the single negative membrane, the single positive membrane, the single negative membrane and the single positive membrane from the direction of the positive electrode plate to the direction of the negative electrode plate;
FIG. I-3-1: the principle schematic diagram of treating the aqueous solution containing monovalent cations, divalent cations or more and monovalent anions is that the membrane component is arranged in the direction from the positive electrode plate to the negative electrode plate and comprises single negative membrane, single positive membrane, single negative membrane and single positive membrane;
FIG. I-3-2: the principle schematic diagram of treating the aqueous solution containing monovalent cations, divalent cations, monovalent anions and divalent anions is arranged in the membrane component from the direction of the positive electrode plate to the direction of the negative electrode plate, wherein the membrane component comprises single negative membrane, single positive membrane, single negative membrane and single positive membrane;
FIG. II-1: a schematic diagram of a water inlet tank and a water inlet chamber;
figure ii-2: schematic of a concentration tank and a concentration chamber;
drawing II-3: schematic diagrams of a polar water tank, a polar water chamber I and a polar water chamber II;
fig. ii-4: a schematic diagram of a polar water tank I and a polar water chamber I;
Fig. ii-5: a schematic diagram of a polar water tank II and a polar water chamber II;
drawing ii-6: a schematic diagram of an alkali tank and an alkali chamber;
fig. ii-7: schematic diagram of acid tank and acid chamber;
FIG. III-1: schematic of a first membrane module;
FIG. III-1-1: schematic of a second membrane module;
FIG. III-2: schematic of a third membrane module;
FIG. III-2-1: schematic of a fourth membrane module;
FIG. III-3: schematic of a fifth membrane module;
FIG. III-3-1: schematic of a sixth membrane module;
FIG. IV-1: example I schematic of a gas extraction recovery system;
FIG. IV-2: example II schematic diagram of a gas extraction recovery system;
figure v: schematic diagram of an apparatus for purifying ionic electrodialysis;
figure VI: schematic diagram of bipolar membrane apparatus;
legend:
Detailed Description
The following non-limiting examples will enable those of ordinary skill in the art to more fully understand the utility model and are not intended to limit the utility model in any way.
All of the example scrub columns described below are cyclic spray scrub columns of one scrub column type; the target object treated by the extraction and recovery system in all the following embodiments is the tail gas of the oxidation reaction system of the terephthalic acid production device; all acids used for adding acid are hydrobromic acid, and all bases used for adding base are sodium hydroxide.
The male membrane used in the following examples of the present invention was 1m sheet supplied by Hangzhou blue technology Co., ltd 2 Yang Mopian; the negative film is 1m sheet of Hangzhou blue technology Co., ltd 2 A female diaphragm; the partition between the films is provided by Hangzhou blue technology Co., ltd; the positive electrode plate and the negative electrode plate are electrodes provided by Hangzhou blue technology Co., ltd; the single-positive membrane and the single-negative membrane are respectively SELEMION CSO membrane and SELEMION ASV membrane provided by AGC engineering Co., ltd., each of which is 1m 2 The method comprises the steps of carrying out a first treatment on the surface of the The bipolar membrane device was EX-4S available from Hangzhou blue technology Co.
Example 1
As shown in FIG. I-1, FIG. II-2, FIG. II-3, FIG. II-6, FIG. II-7, FIG. III-1-1, FIG. IV-1, FIG. V, and FIG. VI, a gas extraction and recovery system mainly comprises a washing tower 33, a purifying ion electrodialysis device 39 (the membrane assembly used in the present embodiment comprises single-cathode membranes 41 and Yang Mopian), a bipolar membrane device 20, the washing tower 33 is a circulating spray washing tower 33,
the connection mode is as follows:
the exhaust gas discharge port 101 of the oxidation reaction system 100 is connected to the gas inlet of the cooling device 102, the gas outlet of the cooling device 102 is connected to the gas inlet of the absorption tower 103, the gas outlet of the absorption tower 103 is connected to the gas inlet of the turbine 105, the gas outlet of the turbine 105 is connected to the gas inlet of the organic matter removing device 104 (incinerator), the gas outlet of the organic matter removing device 104 (incinerator) is connected to the gas inlet pipeline 32 of the circulating spray scrubber 33, the gas inlet pipeline 32 enters the circulating spray scrubber 33, and the gas discharge port 34 is arranged above the circulating spray scrubber 33. The bottom of the circulating spray washing tower 33 is connected with the circulating spray pump 3, the outlet of the circulating spray pump 3 is divided into two paths, one path is connected with the circulating spray pipe 4, and the other path is a solution discharge port 35 of the washing tower.
The solution discharge port 35 of the washing tower is connected to an alkalizing tank 37, and the outlet pipe of the alkalizing unit 36 is also connected to the alkalizing tank 37.
The outlet of the alkalizing tank 37 is connected to the water inlet of a feed pump 38, and the water outlet of the feed pump 38 is connected to the water inlet pipe 50 of the water inlet tank 48 of the purified ion electrodialysis apparatus 39.
The interior of the purifying ion electrodialysis apparatus 39 mainly includes a membrane module mainly comprising single-cathode membranes 41, yang Mopian, and subsidiary equipment mainly comprising an electrode positive plate 52, an electrode negative plate 53, clamping members (in all embodiments, the clamping members function to clamp the membranes), sealing members (in all embodiments, the sealing members function to seal the respective chambers formed by the electrodes and the membranes from leakage), fixing members, a power source, an electrical instrument control system, a pump, a tank, and the like. The arrangement mode is that the electrode positive plate 52, 10 repeated 'single-negative films 41 and Yang Mopian' are combined, the single-negative film 41 and the electrode negative plate 53 are sequentially arranged, and the separator 40 is arranged on two sides of each film. The membrane assembly is utilized to form equipment: the electrode positive plate 52 and the single negative film 41 form a polar water chamber I68, the single negative film 41 and the positive film 42 form water inlet chambers 5 and Yang Mopian, and the single negative film 41 form a concentration chamber 6 in the sequence of the direction of the electrode positive plate 52 and the direction of the electrode negative plate 53, so that a polar water chamber II 89 is formed between the last single negative film 41 and the electrode negative plate 53.
For the purification ionic electrodialysis device 39: the water inlet chamber 5, the outlet of the water inlet chamber 5 is connected to the inlet of the water inlet tank 48, the outlet of the water inlet tank 48 is connected to the water inlet circulating pump 49, the outlet of the water inlet circulating pump 49 is connected to the inlet of the water inlet chamber 5 to form circulation, and the water inlet tank 48 is further provided with a water inlet pipe 50 and an overflow port 51; for the concentrating chamber 6, the outlet of the concentrating chamber 6 is connected to the inlet of the concentrating tank 46, the outlet of the concentrating tank 46 is connected to the concentrating circulating pump 47, the outlet of the concentrating circulating pump 47 is connected to the inlet of the concentrating chamber 6 to form a circulation, and the concentrating tank 46 is also provided with a water inlet pipe 69 and an overflow port 70; for the polar water chamber I68, the outlet of the polar water chamber I68 is connected to the inlet of the polar water tank 66, the outlet of the polar water tank 66 is connected to the polar water pump 67, and the outlet of the polar water pump 67 is connected to the inlet of the polar water chamber I68 to form a circulation; for the polar water chamber II 89, the outlet of the polar water chamber II 89 is connected to the inlet of the polar water tank 66, the outlet of the polar water tank 66 is connected to the polar water circulating pump 67, and the outlet of the polar water circulating pump 67 is connected to the inlet of the polar water chamber II 89 to form a circulation;
the fresh water outlet 11 of the purified ion electrodialysis device 39 (namely the overflow port 51 of the water inlet tank 48 of the purified ion electrodialysis device 39) is connected to the water inlet of the high-pressure pump I14 through the water inlet tank 13 of the reverse osmosis I15, the water outlet of the high-pressure pump I14 is connected to the reverse osmosis I15, and the fresh water outlet 16 of the reverse osmosis I15 is connected to the circulating spray washing tower 33; the concentrate outlet 17 of the reverse osmosis i 15 is connected to the water inlet 50 of the water inlet tank 48 of the purified ion electrodialysis device 39;
The concentrate outlet 12 of the purified ion electrodialysis device 39 (i.e. the overflow 70 of the concentration tank 46 of the purified ion electrodialysis device 39) is connected to the water inlet of the acidification tank 18, the outlet pipe of the acid adding unit 19 is also connected to the inlet of the acidification tank 18, and the water outlet of the acidification tank 18 is connected to the water inlet pipe 50 of the water inlet tank 48 of the bipolar membrane device 20;
the interior of the bipolar membrane device 20 mainly includes a membrane module mainly including bipolar membranes 65, yang Mopian 42, a cathode membrane 43, and auxiliary devices mainly including an electrode positive plate 52, an electrode negative plate 53, clamping members (in all embodiments, the clamping members function to clamp the membranes), sealing members (in all embodiments, the sealing members function to seal the respective chambers formed by the electrodes and the membranes from leakage), fixing members, power supplies, electrical instrument control systems, pumps, tanks, and the like. The electrode positive plates 52, yang Mopian 42, the 10 repeated bipolar membranes 65, the cathode membranes 43, yang Mopian 42 and the electrode negative plates 53 are arranged in sequence, and the separators 40 are arranged on two sides of each membrane. The membrane assembly is utilized to form equipment: in the order of the direction of the positive electrode plate 52 and the direction of the negative electrode plate 53, a polar water chamber I68 is formed between the positive electrode plate 52 and the positive electrode plate 42, an alkali chamber 54 is formed between the bipolar electrode plate 65 and the bipolar electrode plate 65, an acid chamber 55 is formed between the bipolar electrode plate 65 and the negative electrode plate 43, an intake chamber 5 is formed between the negative electrode plate 43 and the positive electrode plate 42, and a polar water chamber II 89 is formed between the last positive electrode plate 42 and the negative electrode plate 53.
For bipolar membrane device 20: the water inlet chamber 5, the outlet of the water inlet chamber 5 is connected to the inlet of the water inlet tank 48, the outlet of the water inlet tank 48 is connected to the water inlet circulating pump 49, the outlet of the water inlet circulating pump 49 is connected to the inlet of the water inlet chamber 5 to form circulation, and the water inlet tank 48 is further provided with a water inlet pipe 50 and an overflow port 51; for the alkali chamber 54, the outlet of the alkali chamber 54 is connected to the inlet of the alkali tank 57, the outlet of the alkali tank 57 is connected to the alkali circulating pump 58, the outlet of the alkali circulating pump 58 is connected to the inlet of the alkali chamber 54 to form circulation, and the alkali tank 57 is also provided with a water inlet pipe 59 and an overflow port 60; for the acid chamber 55, the outlet of the acid chamber 55 is connected to the inlet of the acid tank 61, the outlet of the acid tank 61 is connected to the acid circulating pump 62, the outlet of the acid circulating pump 62 is connected to the inlet of the acid chamber 55 to form a circulation, and the acid tank 61 is also provided with a water inlet pipe 63 and an overflow port 64; for the polar water chamber I68, the outlet of the polar water chamber I68 is connected to the inlet of the polar water tank 66, the outlet of the polar water tank 66 is connected to the polar water pump 67, and the outlet of the polar water pump 67 is connected to the inlet of the polar water chamber I68 to form a circulation; for the polar water chamber II 89, the outlet of the polar water chamber II 89 is connected to the inlet of the polar water tank 66, the outlet of the polar water tank 66 is connected to the polar water circulating pump 67, and the outlet of the polar water circulating pump 67 is connected to the inlet of the polar water chamber II 89 to form a circulation;
The acid outlet 21 of the bipolar membrane apparatus 20 (i.e., the overflow port 64 of the acid tank 61 of the bipolar membrane apparatus 20) is connected to the inlet of the acid recycle pump 22 and the inlet of the acid product pump 23, the outlet of the acid recycle pump 22 is connected to the inlet of the acid adding unit 19, and the outlet of the acid product pump 23 is connected to the feed port 106 of the oxidation reaction system 100; the alkali outlet 24 of the bipolar membrane device 20 (i.e. the overflow 60 of the alkali tank 57 of the bipolar membrane device 20) is connected to the inlet of the alkali recycle pump 25 and the inlet of the alkali product pump 26, the outlet of the alkali recycle pump 25 is connected to the inlet of the alkali adding unit 36, and the outlet of the alkali product pump 26 is collected with a container;
the dilute brine outlet 27 of the bipolar membrane device 20 (i.e. the overflow 51 of the water inlet tank 48 of the bipolar membrane device 20) is connected to the water inlet of the high pressure pump ii 28, the water outlet of the high pressure pump ii 28 is connected to the water inlet of the reverse osmosis ii 29, the dilute brine outlet 30 of the reverse osmosis ii 29 is connected to the circulating spray scrubber 33, and the concentrate outlet 31 of the reverse osmosis ii 29 is connected to the inlet of the acidification tank 18.
The above system operates as follows:
the target of the treatment in this example is gas, and the target of the treatment in all examples of the present utility model is the tail gas of the oxidation reaction system 100 of the terephthalic acid production apparatus.
The tail gas of the oxidation reaction system 100 is discharged into the cooling device 102 from the tail gas discharge port 101, then enters the absorption tower 103, organic matters in the tail gas are absorbed by acetic acid in the absorption tower 103, the tail gas in the absorption tower 103 is further washed by water, the pressure of the gas discharged by the absorption tower 103 is reduced by the turbine 105, the gas enters the organic matter removing device 104 (incinerator), the gas discharged by the organic matter device 104 (incinerator) is introduced into the circulating spray washing tower 33 through the gas inlet pipeline 32, and then the (treated gas) is discharged from the gas discharge port 34 above the circulating spray washing tower 33.
The absorption liquid (sodium hydroxide is taken as absorption liquid in the embodiment) is pre-filled in the circulating spray washing tower 33, the absorption liquid is sprayed circularly from the bottom of the circulating spray washing tower 33 by a circulating spray pump 3, and for stabilizing the pH value of the circulating absorption liquid, an online pH meter is used for automatically measuring the pH value of the absorption liquid, and the addition amount of the sodium hydroxide is automatically controlled; to stabilize the ion concentration of the circulating absorption liquid, the conductivity of the absorption liquid is automatically measured by an on-line conductivity meter, and the discharge amount of the solution discharge port 35 of the washing tower is automatically controlled.
The absorption liquid (i.e., aqueous solution) discharged from the solution discharge port 35 of the washing tower is first introduced into the alkalizing tank 37, and at the same time, the alkali solution is also added into the alkalizing tank 37 through the outlet pipe of the alkali adding unit 36 (the alkali adding unit 36 automatically controls the discharge amount of the alkali adding pump according to the pH value of the alkalizing tank 37 by using an automatic alkali adding metering pump for sodium hydroxide, and finally, the pH of the alkalizing tank 37 is stabilized within a set range).
The aqueous solution in the alkalizing tank 37 is fed by a feed pump 38 to a feed tank 50 of a feed tank 48 of the purifying ionic electrodialysis device 39, and the inside of the purifying ionic electrodialysis device 39 is operated as follows: the water solution in the water inlet tank 48 returns to the water inlet tank 48 to form circulation through the water inlet circulating pump 49 and the water inlet chamber 5, and overflows and is discharged from the overflow port 51; pure water enters the concentration tank 46 from the water inlet pipe 69 of the concentration tank 46, and the solution in the concentration tank 46 returns to the concentration tank 46 to form circulation through the concentration circulation pump 47 and the concentration chamber 6, and overflows and is discharged from the overflow port 70; the polar water in the polar water tank 66 returns to the polar water tank 66 to form circulation through the polar water circulating pump 67, the polar water chamber I68 and the polar water chamber II 89.
The dilute brine of the purified ion type electrodialysis device 39 enters the reverse osmosis I water inlet tank 13 from the overflow port 51 of the water inlet tank 50 and is pumped into the reverse osmosis I15 through the high-pressure pump I14 for concentration, and the fresh water of the reverse osmosis I15 is pumped into the circulating spray washing tower 33 from the fresh water outlet 16 of the reverse osmosis I15; the concentrate of reverse osmosis i 15 is directed from the concentrate outlet 17 of reverse osmosis i 15 to the inlet pipe 50 of the inlet tank 48 of the purified ion electrodialysis device 39.
The concentrate of the purified ion electrodialysis device 39 enters the acidification tank 18 from the overflow port 70 of the concentration tank 46, the outlet of the acid adding unit 19 also enters the acidification tank 18, and the aqueous solution in the acidification tank 18 is pumped into the water inlet pipe 50 of the water inlet tank 48 of the bipolar membrane device 20, and the inside of the bipolar membrane device 20 operates as follows: the water solution in the water inlet tank 48 returns to the water inlet tank 48 to form circulation through the water inlet circulating pump 49 and the water inlet chamber 5, and overflows and is discharged from the overflow port 51; pure water enters the alkali tank 57 from the water inlet pipe 59 of the alkali tank 57, and the solution in the alkali tank 57 returns to the alkali tank 57 to form circulation through the alkali circulation pump 58 and the alkali chamber 54, and overflows and is discharged from the overflow port 60; pure water enters the acid tank 61 from the water inlet pipe 63 of the acid tank 61, and the solution in the acid tank 61 returns to the acid tank 61 to form circulation through the acid circulating pump 62 and the acid chamber 55, and overflows and is discharged from the overflow port 64; the polar water in the polar water tank 66 returns to the polar water tank 66 to form circulation through the polar water circulating pump 67, the polar water chamber I68 and the polar water chamber II 89.
The dilute brine of the bipolar membrane device 20 is pumped into the reverse osmosis II 29 from an overflow port 51 of the water inlet tank 50 through the high-pressure pump II 28 for concentration, and the fresh water of the reverse osmosis II 29 is pumped into the circulating spray washing tower 33 from a fresh water outlet 30 of the reverse osmosis II 29; the concentrate from reverse osmosis ii 29 is directed from concentrate outlet 31 of reverse osmosis ii 29 to acidification tank 18.
Acid of the bipolar membrane device 20 is pumped from one part of an overflow port 64 of the acid tank 61 to an inlet of the acid adding unit 19 through the acid recycling pump 22, and the other part of the acid is pumped to a feed port 106 of the oxidation reaction system 100 through the acid product pump 23 to enter the oxidation reaction system 100; the base of the bipolar membrane apparatus 20 is pumped from the overflow 60 of the base tank 57 partly to the inlet of the base addition unit 36 by the base recycle pump 25 and partly to the vessel by the base product pump 26 for collection.
The experiment was run using the system described above:
Step 1: setting value of each point
The temperature of the oxidation reaction system 100 is generally 185-205 ℃, and the operation temperature is 191 ℃ in the experiment; the outlet temperature of the cooling device 102 is generally 50-100 ℃ and the temperature is 58 ℃ in the experiment; the absorption tower is used for absorbing with acetic acid, and then the acetic acid in the gas is washed with water; the gas pressure after the turbine 105 is slightly positive, the incinerator is generally 600-1000 ℃, and 781 ℃ is adopted in the experiment;
The pH of the circulating spray scrubber 33 is set to 8.8-9.2 (pH lower than 8.8 will automatically add alkali, and pH higher than 9.2 will stop the alkali adding pump);
the discharge amount of the solution discharge port 35 of the washing tower is automatically set and regulated by the conductivity value of the circulating spray washing tower 33, and the conductivity value of the circulating spray washing tower 33 is 12000-14000 us/cm;
the pH of the alkalizing tank 37 is set to 10.3-10.7, and sodium hydroxide is automatically added, and in the embodiment, the industrial 32% sodium hydroxide is used, and a metering pump is used for variable frequency discharge amount addition;
the pH of the acidification tank 18 is set to 2.5-3, and the variable-frequency discharge amount of the acid recycling pump 22 of the bipolar membrane electrodialysis device is controlled.
The polar water tank 66 of the purifying ion electrodialysis apparatus 39 is charged with 1mol/L sodium bromide and given a voltage of 48V, and the polar water tank 66 of the bipolar membrane apparatus 20 is charged with 1mol/L sodium hydroxide and given a voltage of 48V, and the system is operated.
Step 2: sampling water sample analysis data in normal operation
Water sample at solution discharge port 35 of the scrubber: ph=8.81, conductivity=13500 us/cm, carbonate=1625 ppm, bicarbonate=6886 ppm, bromide=2553 ppm;
water sample from alkalizing tank 37: ph=10.5, carbonate=7599 ppm, bicarbonate=131 ppm, bromide=2332 ppm, i.e. conversion of bicarbonate (monoanion) to carbonate (dianion) by raising PH with alkali;
Concentrate discharge 12 water sample from purification ionic electrodialysis device 39: carbonate=88 ppm, bicarbonate=755 ppm, bromide= 14532ppm (i.e. carbonate is divalent anion and cannot pass through the single-anion membrane, so cannot reach the concentrating chamber and can only be intercepted and left in the water inlet chamber, i.e. the purification ion electrodialysis device 39 realizes the separation of sodium bromide from sodium carbonate and sodium bromide (the purpose of adding alkali is that the monovalent anion can permeate the single-anion membrane and be converted into divalent carbonate single-anion membrane and have the intercepting effect), and the concentration of sodium bromide is also concentrated);
acidifying tank 18 water sample: ph=2.8, no detectable carbonate, no detectable bicarbonate, 18122ppm bromide;
the acid outlet 21 of the bipolar membrane device 20 is water-sampled: the concentration of hydrogen ions is 1.2mol/L, bromide=9.7%, and sodium ions 122ppm are hydrobromic acid;
the base outlet 24 of bipolar membrane apparatus 20 is water-sampled: hydroxide concentration 1.9mol/L, sodium ion=4.4%, bromide ion 311ppm, sodium hydroxide.
Example two
As shown in FIG. I-1, FIG. II-2, FIG. II-3, FIG. II-6, FIG. II-7, FIG. III-1-1, FIG. IV-2, FIG. V, and FIG. VI, a gas extraction and recovery system mainly comprises a washing tower 33, a purifying ion electrodialysis device 39 (the membrane assembly used in the present embodiment comprises single-cathode membranes 41 and Yang Mopian), a bipolar membrane device 20, the washing tower 33 is a circulating spray washing tower 33,
The connection mode is as follows:
on the basis of the first embodiment, "the solution discharge port 35 of the washing tower is connected to the alkalizing tank 37, and the outlet pipe of the alkalizing unit 36 is also connected to the alkalizing tank 37. The outlet of the alkalizing tank 37 is connected to the water inlet of a feed pump 38, and the water outlet of the feed pump 38 is connected to the water inlet pipe 50 of the water inlet tank 48 of the purified ion electrodialysis apparatus 39. The solution discharge port 35 of the "replaced" washing tower is connected to the heating tank 56, an exhaust port 71 is arranged above the heating tank 56, a heater 73 is arranged in the heating tank 56, the outlet of the heating tank 56 is connected to the delivery pump 72, the outlet of the delivery pump 72 is connected to the water inlet of the cooler 74, and the water outlet of the cooler 74 is connected to the water inlet pipe 50 "of the water inlet tank 48 of the purifying ion electrodialysis device 39; the alkali outlet 24 of the bipolar membrane device 20 (namely, the overflow port 60 of the alkali tank 57 of the bipolar membrane device 20) is connected to the inlet of the alkali recycling pump 25 and the inlet of the alkali product pump 26, and the outlet of the alkali recycling pump 25 is connected to the inlet of the alkali adding unit 36 and the outlet of the alkali product pump 26 is collected by a container; the base outlet 24 of the "replacement" bipolar membrane apparatus 20 (i.e., the overflow 60 of the base tank 57 of the bipolar membrane apparatus 20) is connected to the inlet of the base product pump 26, the outlet of the base product pump 26 being collected with a container; ", the rest is exactly the same as in example one;
The above system operates as follows:
on the basis of the first embodiment, "the absorption liquid (i.e., the aqueous solution) discharged from the solution discharge port 35 of the washing tower is first fed into the alkalizing tank 37, and at the same time, the alkali liquid is also added into the alkalizing tank 37 through the outlet pipe of the alkali adding unit 36 (the alkali adding unit 36 automatically controls the discharge amount of the alkali adding pump according to the pH value of the alkalizing tank 37 by using an automatic alkali adding metering pump of sodium hydroxide, and finally, the pH of the alkalizing tank 37 is stabilized within a set range). The water solution in the alkalization tank 37 is pumped into a water inlet tank 50 of a water inlet tank 48 of the purification ionic electrodialysis device 39 through a water feed pump 38, the water inlet tank 50 of the water inlet tank 48 of the purification ionic electrodialysis device 39 is replaced by the absorption liquid discharged from a solution discharge port 35 of a washing tower (namely, the water solution) firstly enters a heating tank 56, the heating tank 56 is heated by a heater 73, gas is discharged from an air outlet 71 above the heating tank 56, the water solution in the heating tank 56 is pumped into a cooler 74 through a conveying pump 72 for cooling, and then enters the water inlet tank 50' of the water inlet tank 48 of the purification ionic electrodialysis device 39; the "alkali of bipolar membrane apparatus 20 is pumped from overflow 60 of alkali tank 57 to the inlet of alkali addition unit 36 via alkali recycle pump 25 in part and to the vessel via alkali product pump 26 in part for collection. The base "replaced" with bipolar membrane device 20 is pumped from overflow 60 of base tank 57 to the vessel for collection by base product pump 26. ", the rest is exactly the same as in example one;
Step 1: setting value of each point
The temperature of the oxidation reaction system 100 is generally 185-205 ℃, and the operation temperature is 191 ℃ in the experiment; the outlet temperature of the cooling device 102 is generally 50-100 ℃ and the temperature is 58 ℃ in the experiment; the absorption tower is used for absorbing with acetic acid, and then the acetic acid in the gas is washed with water; the gas pressure after the turbine 105 is slightly positive, the incinerator is generally 600-1000 ℃, and 781 ℃ is adopted in the experiment;
the pH of the circulating spray scrubber 33 is set to 8.8-9.2 (pH lower than 8.8 will automatically add alkali, and pH higher than 9.2 will stop the alkali adding pump);
the discharge amount of the solution discharge port 35 of the washing tower is automatically set and regulated by the conductivity value of the circulating spray washing tower 33, and the conductivity value of the circulating spray washing tower 33 is 12000-14000 us/cm;
control heating tank 56 temperature = 95 ℃;
control cooler 74 outlet temperature = 30 ℃;
the pH of the acidification tank 18 is set to 2.5-3, and the variable-frequency discharge amount of the acid recycling pump 22 of the bipolar membrane electrodialysis device is controlled.
The polar water tank 66 of the purifying ion electrodialysis apparatus 39 is charged with 1mol/L sodium bromide and given a voltage of 48V, and the polar water tank 66 of the bipolar membrane apparatus 20 is charged with 1mol/L sodium hydroxide and given a voltage of 48V, and the system is operated.
Step 2: sampling water sample analysis data in normal operation
Water sample at solution discharge port 35 of the scrubber: ph=8.81, conductivity=13500 us/cm, carbonate=1625 ppm, bicarbonate=6886 ppm, bromide=2553 ppm;
water sample from cooler 74: carbonate=5221 ppm, bicarbonate=1088 ppm, bromide=2915 ppm, i.e. conversion of bicarbonate (monoanion) to carbonate (dianion) by heating, and carbon dioxide (volatilization);
concentrate discharge 12 water sample from purification ionic electrodialysis device 39: carbonate=112 ppm, bicarbonate=4223 ppm, bromide=12134 ppm (i.e. carbonate is divalent anion, cannot pass through the single-anion membrane and cannot reach the concentrating chamber, and can only be intercepted and left in the water inlet chamber, i.e. the purification ion electrodialysis device 39 realizes the separation of sodium bromide from sodium carbonate and sodium bromide (the purpose of heating is that the monovalent anion can permeate the single-anion membrane, the single-anion membrane of divalent carbonate can be intercepted after being converted by heating), and the concentration of sodium bromide is also concentrated);
acidifying tank 18 water sample: ph=2.7, no detectable carbonate, no detectable bicarbonate, 22015ppm bromide;
the acid outlet 21 of the bipolar membrane device 20 is water-sampled: the concentration of hydrogen ions is 1.4mol/L, bromide ions=11%, and sodium ions 86ppm are hydrobromic acid;
The base outlet 24 of bipolar membrane apparatus 20 is water-sampled: hydroxide concentration 1.5mol/L, sodium ion=3.5%, bromide ion 198ppm, sodium hydroxide.
Claims (11)
1. A gas extraction and recovery system is characterized in that,
the extraction recovery system comprises: a washing tower, a purifying ion type electrodialysis device and a bipolar membrane device;
the water solution discharge port of the washing tower is connected to the water inlet of the purified ion electrodialysis device, and the concentrated solution discharge port of the purified ion electrodialysis device is connected to the water inlet of the bipolar membrane device;
the purification ion electrodialysis device comprises a membrane assembly, wherein the membrane assembly is arranged between an electrode positive plate and an electrode negative plate;
the membrane assembly includes a single female membrane sheet, yang Mopian;
or the membrane assembly comprises a single male membrane sheet and a female membrane sheet;
or the membrane assembly comprises a single male membrane sheet and a single female membrane sheet.
2. The gas extraction and recovery system of claim 1, wherein the membranes in the membrane module are arranged in a sequence from positive electrode plate to negative electrode plate:
when the two or more combinations are arranged, the latter combination is close to the former combination and is arranged between the former combination and the electrode negative plate, namely the membrane component I-1;
Or at least one group of combinations sequentially comprising a female diaphragm and a single male diaphragm, wherein when more than or equal to two combinations are arranged, the latter combination is close to the former combination and is arranged between the former combination and the electrode negative plate, namely the membrane component I-2;
or at least one group of combinations formed by single-negative films and single-positive films in sequence, when more than or equal to two combinations are arranged, the latter combination is close to the former combination and is arranged between the former combination and the electrode negative plate, namely the membrane component I-3.
3. The gas extraction recovery system of claim 2, wherein: in the direction from the positive electrode plate to the negative electrode plate:
membrane module I-1: a positive diaphragm is arranged between the positive electrode plate and the first single negative diaphragm and between the positive electrode plate and the first single negative diaphragm;
or membrane module I-1: a single-negative membrane is arranged between the last single-negative membrane, the combination of the positive membrane and the electrode negative plate;
or membrane module I-2: a female diaphragm is arranged between the last female diaphragm, the combination of the single-male diaphragm and the electrode negative plate;
or membrane module I-2: a single-positive membrane is arranged between the positive electrode plate and the first combination of the negative membrane and the single-positive membrane;
Or membrane module I-3: a single-negative membrane is arranged between the last single-negative membrane, the combination of the single-positive membrane and the electrode negative plate;
or membrane module I-3: a single-positive membrane is arranged between the positive electrode plate and the first single-negative membrane and single-positive membrane combination.
4. A gas extraction recovery system as claimed in claim 2 or claim 3, wherein, for each membrane, between:
the membrane component I-1 is arranged from the direction of the positive electrode plate to the direction of the negative electrode plate: an intake chamber is formed between the single negative membrane and the positive membrane, and a concentration chamber is formed between Yang Mopian and the single negative membrane;
or the membrane component I-2 is arranged from the positive electrode plate direction to the negative electrode plate direction: an intake chamber is formed between the female membrane and the single-male membrane, and a concentration chamber is formed between the single-male membrane and the female membrane;
or the membrane component I-3 is arranged from the positive electrode plate direction to the negative electrode plate direction: an intake chamber is formed between the single-negative membrane and the single-positive membrane, and a concentration chamber is formed between the single-positive membrane and the single-negative membrane;
or a water pole chamber I is formed between the positive electrode plate and a diaphragm closest to the positive electrode plate, and a water pole chamber II is formed between the negative electrode plate and a diaphragm closest to the negative electrode plate.
5. A gas extraction recovery system as defined in claim 3, wherein:
or when the membrane module I-1: when a positive diaphragm is arranged between the positive electrode plate and the first single-negative diaphragm and the positive diaphragm combination: yang Mopian adjacent to the positive electrode plate and/or adjacent to the negative electrode plate is replaced with a nanofiltration membrane or mono Yang Mopian;
or when the membrane module I-1: when the single-negative membrane is arranged between the last single-negative membrane, the combination of the positive membrane and the combination of the electrode negative plate: the single negative membrane sheet close to the positive electrode plate and/or close to the negative electrode plate is replaced by a negative membrane sheet or a nanofiltration membrane sheet;
or when the membrane module I-2: and when the last female diaphragm is arranged between the female diaphragm and the electrode negative plate, the single male diaphragm is combined with the female diaphragm: the negative film sheet near the positive electrode plate and/or near the negative electrode plate is replaced by a nanofiltration film sheet or a single negative film sheet;
or when the membrane module I-2: when a single-positive membrane is arranged between the positive electrode plate and the first combination of the negative membrane and the single-positive membrane: the single positive membrane adjacent to the positive electrode plate and/or adjacent to the negative electrode plate is replaced by a nanofiltration membrane or a positive membrane;
or when the membrane module I-3: and when the single negative film is arranged between the last single negative film, the combination of the single positive film and the electrode negative plate: the single negative film sheet near the positive electrode plate and/or near the negative electrode plate is replaced by a nanofiltration film sheet or a negative film sheet;
Or when the membrane module I-3: when a single-positive membrane is arranged between the positive electrode plate and the first single-negative membrane and the single-positive membrane combination: the single positive membrane sheet adjacent to the positive electrode plate and/or adjacent to the negative electrode plate is replaced with a positive membrane sheet or nanofiltration membrane sheet.
6. The gas extraction recovery system of claim 4,
the outlet of the water inlet chamber is connected to the inlet of the water inlet tank, the outlet of the water inlet tank is connected to the water inlet circulating pump, and the outlet of the water inlet circulating pump is connected to the inlet of the water inlet chamber to form circulation;
or the outlet of the concentration chamber is connected to the inlet of the concentration tank, the outlet of the concentration tank is connected to the concentration circulating pump, and the outlet of the concentration circulating pump is connected to the inlet of the concentration chamber to form a circulation;
or the outlet of the polar water chamber I is connected to the inlet of the polar water tank I, the outlet of the polar water tank I is connected to the polar water circulating pump I, and the outlet of the polar water circulating pump I is connected to the inlet of the polar water chamber I to form circulation; the outlet of the polar water chamber II is connected to the inlet of the polar water tank II, the outlet of the polar water tank II is connected to the polar water circulating pump II, and the outlet of the polar water circulating pump II is connected to the inlet of the polar water chamber II to form circulation;
or the outlet of the polar water chamber I and the outlet of the polar water chamber II are connected to the inlet of the polar water tank, the outlet of the polar water tank is connected to the polar water circulating pump, and the outlet of the polar water circulating pump is connected to the inlet of the polar water chamber I and the inlet of the polar water chamber II to form circulation.
7. The gas extraction recovery system of claim 6, wherein,
the concentration tank is provided with a water inlet pipe and a discharge port;
or the water inlet tank is provided with a water inlet pipe and a discharge port;
or the water tank I is provided with a water inlet pipe, and the water tank II is provided with a water inlet pipe;
or the polar water tank is provided with a water inlet pipe.
8. The gas extraction and recovery system according to claim 1, 2, 3, 5, 6 or 7, further comprising an alkali adding unit or a heating unit:
the outlet of the alkali adding unit is connected to a pipeline between the water solution discharge port of the washing tower and the water inlet of the purified ion electrodialysis device; or an alkalization tank is arranged on a pipeline between the water solution discharge port of the washing tower and the water inlet of the purifying ionic electrodialysis device, and the outlet of the alkalization unit is connected to the inlet of the alkalization tank;
or a heating unit is arranged on a pipeline between the water solution discharge port of the washing tower and the water inlet of the purifying ionic electrodialysis device.
9. The gas extraction and recovery system according to claim 1, 2, 3, 5, 6 or 7, further comprising an acid adding unit:
the outlet of the acid adding unit is connected to a pipeline between the concentrated solution discharge port of the purified ion electrodialysis device and the water inlet of the bipolar membrane device; or an acidification tank is arranged on a pipeline between a concentrated solution discharge port of the purification ion type electrodialysis device and a water inlet of the bipolar membrane device, and an outlet of the acidification unit is connected to an inlet of the acidification tank.
10. The gas extraction and recovery system according to claim 1, 2, 3, 5, 6 or 7, wherein a hardness removal device is provided:
and a hardness removing device is arranged between the water solution discharge port of the washing tower and the water inlet of the purified ion electrodialysis device.
11. The gas extraction recovery system of claim 1, 2, 3, 5, 6 or 7,
the tail gas discharge port of the oxidation reaction system is connected to the gas inlet of the cooling device, the gas outlet of the cooling device is connected to the gas inlet of the absorption tower, the gas outlet of the absorption tower is connected to the gas inlet of the gas organic matter removing device, and the gas outlet of the gas organic matter removing device is connected to the gas inlet pipeline of the washing tower; or the tail gas discharge port of the oxidation reaction system is connected to the gas inlet of the cooling device, the gas outlet of the cooling device is connected to the gas inlet of the absorption tower, the gas outlet of the absorption tower is connected to the gas inlet of the turbine, the gas outlet of the turbine is connected to the gas inlet of the gas organic matter removing device, and the gas outlet of the gas organic matter removing device is connected to the gas inlet pipeline of the washing tower;
or an acid recycle pump of the bipolar membrane device is connected to an inlet of an acid adding unit; or the acid product pump of the bipolar membrane device is connected to the feed inlet of the oxidation reaction system; or the acid product pump of the bipolar membrane device is connected to the feed inlet of a mixing tank, and the discharge outlet of the mixing tank is connected to the feed inlet of an oxidation reaction system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220454807.2U CN219050834U (en) | 2022-03-03 | 2022-03-03 | Gas extraction and recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220454807.2U CN219050834U (en) | 2022-03-03 | 2022-03-03 | Gas extraction and recovery system |
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| Publication Number | Publication Date |
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| CN219050834U true CN219050834U (en) | 2023-05-23 |
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ID=86374254
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
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| CN202220454807.2U Active CN219050834U (en) | 2022-03-03 | 2022-03-03 | Gas extraction and recovery system |
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| Country | Link |
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| CN (1) | CN219050834U (en) |
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