CN104645816A - Wet desulphurization synergist - Google Patents
Wet desulphurization synergist Download PDFInfo
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- CN104645816A CN104645816A CN201510044710.9A CN201510044710A CN104645816A CN 104645816 A CN104645816 A CN 104645816A CN 201510044710 A CN201510044710 A CN 201510044710A CN 104645816 A CN104645816 A CN 104645816A
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- 239000007800 oxidant agent Substances 0.000 claims abstract description 13
- 150000007524 organic acids Chemical class 0.000 claims abstract description 10
- 239000003444 phase transfer catalyst Substances 0.000 claims abstract description 7
- KFSLWBXXFJQRDL-UHFFFAOYSA-N Peracetic acid Chemical group CC(=O)OO KFSLWBXXFJQRDL-UHFFFAOYSA-N 0.000 claims description 34
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 claims description 30
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical group [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 28
- NHGXDBSUJJNIRV-UHFFFAOYSA-M tetrabutylammonium chloride Chemical compound [Cl-].CCCC[N+](CCCC)(CCCC)CCCC NHGXDBSUJJNIRV-UHFFFAOYSA-M 0.000 claims description 20
- 239000001361 adipic acid Substances 0.000 claims description 15
- 235000011037 adipic acid Nutrition 0.000 claims description 15
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 14
- 230000001590 oxidative effect Effects 0.000 claims description 13
- 239000003638 chemical reducing agent Substances 0.000 claims description 9
- 229940074404 sodium succinate Drugs 0.000 claims description 9
- ZDQYSKICYIVCPN-UHFFFAOYSA-L sodium succinate (anhydrous) Chemical compound [Na+].[Na+].[O-]C(=O)CCC([O-])=O ZDQYSKICYIVCPN-UHFFFAOYSA-L 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 6
- 239000000344 soap Substances 0.000 claims description 6
- KDYFGRWQOYBRFD-UHFFFAOYSA-N succinic acid Chemical compound OC(=O)CCC(O)=O KDYFGRWQOYBRFD-UHFFFAOYSA-N 0.000 claims description 5
- ODIGIKRIUKFKHP-UHFFFAOYSA-N (n-propan-2-yloxycarbonylanilino) acetate Chemical compound CC(C)OC(=O)N(OC(C)=O)C1=CC=CC=C1 ODIGIKRIUKFKHP-UHFFFAOYSA-N 0.000 claims description 4
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 claims description 4
- JHJLBTNAGRQEKS-UHFFFAOYSA-M sodium bromide Chemical compound [Na+].[Br-] JHJLBTNAGRQEKS-UHFFFAOYSA-M 0.000 claims description 4
- RTBFRGCFXZNCOE-UHFFFAOYSA-N 1-methylsulfonylpiperidin-4-one Chemical compound CS(=O)(=O)N1CCC(=O)CC1 RTBFRGCFXZNCOE-UHFFFAOYSA-N 0.000 claims description 3
- JFCQEDHGNNZCLN-UHFFFAOYSA-N anhydrous glutaric acid Natural products OC(=O)CCCC(O)=O JFCQEDHGNNZCLN-UHFFFAOYSA-N 0.000 claims description 3
- 150000003983 crown ethers Chemical class 0.000 claims description 2
- 235000003642 hunger Nutrition 0.000 claims description 2
- 150000002978 peroxides Chemical group 0.000 claims description 2
- 150000003242 quaternary ammonium salts Chemical group 0.000 claims description 2
- 150000004671 saturated fatty acids Chemical class 0.000 claims description 2
- KDYFGRWQOYBRFD-UHFFFAOYSA-L succinate(2-) Chemical compound [O-]C(=O)CCC([O-])=O KDYFGRWQOYBRFD-UHFFFAOYSA-L 0.000 claims description 2
- 239000001384 succinic acid Substances 0.000 claims description 2
- 238000006477 desulfuration reaction Methods 0.000 abstract description 67
- 230000023556 desulfurization Effects 0.000 abstract description 48
- 238000000034 method Methods 0.000 abstract description 24
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- -1 organic acid salt Chemical class 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 41
- 239000003546 flue gas Substances 0.000 description 41
- 235000019738 Limestone Nutrition 0.000 description 30
- 239000006028 limestone Substances 0.000 description 30
- 239000002002 slurry Substances 0.000 description 29
- 238000005259 measurement Methods 0.000 description 22
- 239000007789 gas Substances 0.000 description 15
- 238000010521 absorption reaction Methods 0.000 description 14
- 238000013461 design Methods 0.000 description 13
- 239000000047 product Substances 0.000 description 12
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 11
- 239000002994 raw material Substances 0.000 description 11
- 230000000694 effects Effects 0.000 description 7
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 6
- 239000010440 gypsum Substances 0.000 description 6
- 229910052602 gypsum Inorganic materials 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 3
- 235000010261 calcium sulphite Nutrition 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000012747 synergistic agent Substances 0.000 description 2
- 206010001052 Acute respiratory distress syndrome Diseases 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 206010016807 Fluid retention Diseases 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
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 208000013616 Respiratory Distress Syndrome Diseases 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
- 238000009825 accumulation Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- KDYFGRWQOYBRFD-NUQCWPJISA-N butanedioic acid Chemical compound O[14C](=O)CC[14C](O)=O KDYFGRWQOYBRFD-NUQCWPJISA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 150000003463 sulfur Chemical class 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention provides a wet desulphurization synergist. The wet desulphurization synergist is characterized by containing the following components by weight percentage: 40%-60% of organic acid; 30%-40% of organic acid salt; 1%-2% of a water retention agent; 5%-20% of a phase transfer catalyst; and 4%-8% of an oxidizing agent. The wet desulphurization synergist provided by the invention is simple in formula and low in cost, and as the scaling phenomenon in a desulfurization process can be reduced, the synergy of various substances of the formula can shorten the desulfurization time and improve the operation efficiency of equipment under the condition of guaranteeing relatively high desulfurization efficiency, so that a desulfurization system can operate economically and stably.
Description
Technical field
The invention provides a kind of wet desulphurization synergist, belong to flue gas desulfurization field.
Background technology
Industrially can give off a large amount of sulfur dioxide gas and some other sulfurous gas in the process of coal combustion, this can pollute air, even can cause Acid Rain Effect water environment.Because the industrial energy major part of China also depends on coal combustion, so the sulfurous gas administered in the flue gas given off is even more important.Present fume desulphurization method has a variety of, can be divided into wet method, dry method, semi-dry desulfurization, ammonia process, Sea water respiratory distress syndrome and other fume desulphurization method according to its processing procedure and material state.Wet fuel gas desulfurizing technology has that reaction speed is fast, equipment is less, desulfuration efficiency comparatively advantages of higher.Under the links such as the process of the absorption of wet desulphurization and regeneration and accessory substance are all carried out at wet condition.Wet-type calcium, wet-type magnesium method, sodium alkali and wet type ammonium method etc. can be divided into again in this technology.In addition Wei Erman-Luo De technique, zinc oxide method, manganese oxide method and organic acid sodium-gypsum is also had.Technical comparing is ripe and widely used is among those methods Wet Limestone-desulfurization of gypsum technique, and it runs very reliable and stable, and absorbent utilization ratio is higher, and when Ca/S ratio is 1.2, desulfuration efficiency can reach more than 90%.In conventional wet sulfur removal technology, main employing limestone-gypsum doctor treatment, its operation principle is with lime stone as absorbent, absorbs the SO in flue gas
2, generate calcium sulfite, calcium sulfite is oxidized to calcium sulfate by air or under the promotion of micro amount of oxygen agent in oxidizing tower, i.e. gypsum.In traditional limestone-gypsum sulfur method, the lime stone cost as absorbent is low, and desulfuration byproduct can fully utilize, and therefore the application of this sulfur method is wider.
Along with a large amount of exploitation and the use of coal resources, coal quality reduces gradually, the amount of sulfur contenting in smoke of generating plant pulverized coal boiler is raised gradually, far exceedes the design load of desulphurization system amount of sulfur contenting in smoke, make desulfurization equipment overload operation, cause system can not continuously, stable operation.In prior art, under the prerequisite not transforming original desulphurization plant, it is comparatively effective method that application Desulfurization synergist improves the desulfuration efficiency of desulphurization system.
The synergist that can be used for Limestone-gypsum Wet Flue Gas Desulfurization Process at present mainly contains inorganic builders, organic synergistic agent and compound synergist, the advantage of inorganic Desulfurization synergist is that reaction speed is fast, can improve desulfuration efficiency rapidly, shortcoming is that the duration is short, is expendable synergist; The advantage of organic Desulfurization synergist is that acting duration is long, and directly do not consume synergist, consumption is few, and shortcoming is that onset time is comparatively slow, is generally 25h; Although compound synergist overcomes the shortcoming of inorganic builders and organic synergistic agent, formula is complicated, and expensive, consumption is large.And reflect according to many enterprises, it is long in use to there is desulfurization time in current most wet desulphurization synergist, and the easy scale effect equipment of calcium sulfate of generation runs.Therefore how to use most economical effective means, not only make de-effective, and can allow desulphurization system stable operation, those skilled in the art need the problem of solution badly to become row.
Summary of the invention
The object of the invention is to the shortcoming overcoming above wet desulphurization synergist, there is provided a kind of can when ensure compared with high desulfurization efficiency, accomplish to fill a prescription simple, with low cost, desulfurization time is shorter, the wet desulphurization synergist of scale inhibition and features high scale-removing effect, run with enabling desulphurization system economic stability.
For achieving the above object, present invention employs following technical scheme:
A kind of wet desulphurization synergist, is characterized in that, comprise following component by weight percentage: organic acid 40-60%; Acylate 30-40%; Water-loss reducer 1-2%; Phase transfer catalyst 5-20%; Oxidant 4-8%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and described organic acid percentage by weight is 40-50%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and the percentage by weight of described tetrabutylammonium chloride is 7-14%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and the percentage by weight of described oxidant is 5-6%.
Preferably, wet desulphurization synergist of the present invention, such feature can also be had: wherein, described organic acid is binary acid, described acylate is the soap that full conjunction or insatiable hunger are closed, described phase transfer catalyst is quaternary ammonium salt or crown ether, and described water-loss reducer is the inorganic salts of good hygroscopicity, and described oxidant is peroxide.
Preferably, wet desulphurization synergist of the present invention, such feature can also be had: wherein, described binary acid is any one in adipic acid, succinic acid or glutaric acid, described soap is the Salt of saturated fatty acid of C4-C10, described water-loss reducer is magnesium chloride or sodium bromide, and described oxidant is Peracetic acid or hypochlorite.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and described binary acid is adipic acid, and described soap is succinate, and described water-loss reducer is magnesium chloride, and described oxidant is Peracetic acid.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and the concentration of described Peracetic acid is 20%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and by weight percentage, the content of each component is: adipic acid: 45%; Sodium succinate: 38%; Magnesium chloride: 2%; The Peracetic acid of 20% concentration: 5%; Tetrabutylammonium chloride: 10%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and by weight percentage, the content of each component is: adipic acid: 50%; Sodium succinate: 36%; Magnesium chloride: 1%; The Peracetic acid of 20% concentration: 6%; Tetrabutylammonium chloride: 7%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and by weight percentage, the content of each component is: adipic acid: 45%; Sodium succinate: 34%; Magnesium chloride: 1%; The Peracetic acid of 20% concentration: 6%; Tetrabutylammonium chloride: 14%.
Preferably, wet desulphurization synergist of the present invention, can also have such feature: wherein, and by weight percentage, the content of each component is: adipic acid: 50%; Sodium succinate: 30%; Magnesium chloride: 1%; The Peracetic acid of 20% concentration: 5%; Tetrabutylammonium chloride: 14%.
Each composition role in flue gas desulfurization synergist of the present invention is as follows:
Adipic acid is a kind of organic acid, character is relatively stable, can ionize in water and obtain hydrogen ion, it and sodium succinate acting in conjunction are as buffer, for the pH value in stable slurry serves as the effect of cushioning liquid, energy stable maintenance desulfurization slurry pH value is at 5-6, and this pH value is also the pH scope of this formula the best, at this ph, SO can be strengthened
2absorption, promote the dissolving of calcium carbonate, thus improve the effect of desulfurization.Certainly, the present invention can adopt multiple organic acid, such as glutaric acid, adipic acid or succinic acid, preferred adipic acid.
Magnesium chloride is the reasonable inorganic salts of hygroscopicity, has reasonable moisture-absorption water-retention, and desulfurizing agent can be made in desulphurization plant to keep moistening for a long time, improves the efficiency of de-agent; On the other hand, it also plays the effect of oxidant in sweetening process.Water-loss reducer in the present invention refers to the good inorganic salts of hygroscopicity, preferred magnesium chloride.
Tetrabutylammonium chloride is a kind of phase transfer catalyst, mainly reduces the surface tension of water, promotes SO on the one hand
2dissolving, make on the other hand the calcium sulfate generated be not easy fouling, ensure the effect of scale inhibition and scale removal like this, make normal operation and then the minimizing desulfurization time of equipment.
Peracetic acid mainly plays oxidation, and the sulfite oxidation of sweetening process product is become corresponding sulfate, which reduces the accumulation of the calcium sulfite because producing in sweetening process and the fouling caused.Certainly, the present invention can adopt multiple oxidant, such as clorox and Peracetic acid etc., preferably the Peracetic acid of 20% concentration.
The beneficial effect of the invention
Formula of the present invention is simple, with low cost, each material of this formula acts synergistically when ensureing compared with high desulfurization efficiency, due to the scale formation of sweetening process can be reduced, thus shorten the time of desulfurization, improve the operational efficiency of equipment, run with enabling desulphurization system economic stability.
Detailed description of the invention
Below in conjunction with specific embodiment, technical scheme of the present invention is explained in detail.
The Adding Way of flue gas desulfurization synergist of the present invention is: after first being mixed by the formula in table 1 by flue gas desulfurization synergist, be added to lime stone slurry, addition be lime stone slurry weight 0.4-1.0%, make it to stir in lime stone slurry case, then squeeze in desulfuration absorbing tower through limestone slurry liquid pump.SO
2absorbed by lime stone in desulfuration absorbing tower, purified gas is discharged from flue.Continuous mensuration imports and exports SO
2concentration, according to circumstances change the addition of lime stone slurry concentration, flow and Desulfurization synergist at any time, the efficiency of desulfurization can be controlled thus more accurately.
Wet desulphurization synergist provided by the invention can be applied to inlet flue gas SO
2concentration design load be 1500-1700mg/Nm
3desulphurization system in.
The formula group one of table 1 Desulfurization synergist (each component all by weight percentage, %)
The formula group two of table 2 Desulfurization synergist (each component all by weight percentage, %)
Embodiment one
After various raw material is re-dubbed finished product by the proportioning in embodiment one in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can add according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2430mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 141mg/Nm
3, liquid-gas ratio 10.6, calcium sulfur ratio 1.03, desulfuration efficiency is 94.2%.
Embodiment two
After various raw material is re-dubbed finished product by the proportioning in embodiment two in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2310mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 115mg/Nm
3, liquid-gas ratio 10.6, calcium sulfur ratio 1.03, desulfuration efficiency 95%.
Embodiment three
After various raw material is re-dubbed finished product by the proportioning in embodiment three in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.06 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2720mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 156mg/Nm
3, liquid-gas ratio 10.8, calcium sulfur ratio 1.05, desulfuration efficiency 94.3%.
Embodiment four
After various raw material is re-dubbed finished product by the proportioning in embodiment four in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.05 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2640mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 164mg/Nm
3, liquid-gas ratio 10.4, calcium sulfur ratio 1.04, desulfuration efficiency 93.8%.
Embodiment five
After various raw material is re-dubbed finished product by the proportioning in embodiment five in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2810mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 163mg/Nm
3, liquid-gas ratio 10.4, calcium sulfur ratio 1.06, desulfuration efficiency 94.2%.
Embodiment six
After various raw material is re-dubbed finished product by the proportioning in embodiment six in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.06 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2960mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 146mg/Nm
3, liquid-gas ratio 10.6, calcium sulfur ratio 1.04, desulfuration efficiency 95.1%.
Embodiment seven
After various raw material is re-dubbed finished product by the proportioning in embodiment seven in above-mentioned table 1, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2730mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 162mg/Nm
3, liquid-gas ratio 10.5, calcium sulfur ratio 1.03, desulfuration efficiency is 94%.
Embodiment eight
After various raw material is re-dubbed finished product by the proportioning in embodiment eight in above-mentioned table 2, join in absorption tower, initial incremental amount is the weight 0.06 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2530mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 149mg/Nm
3, liquid-gas ratio 10.4, calcium sulfur ratio 1.04, desulfuration efficiency is 94.1%.
Embodiment nine
After various raw material is re-dubbed finished product by the proportioning in embodiment nine in above-mentioned table 2, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2670mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 147mg/Nm
3, liquid-gas ratio 10.5, calcium sulfur ratio 1.03, desulfuration efficiency is 94.5%.
Embodiment ten
After various raw material is re-dubbed finished product by the proportioning in embodiment ten in above-mentioned table 2, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2490mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 154mg/Nm
3, liquid-gas ratio 10.5, calcium sulfur ratio 1.05, desulfuration efficiency is 93.8%.
Embodiment 11
After various raw material is re-dubbed finished product by the proportioning in embodiment 11 in above-mentioned table 2, join in absorption tower, initial incremental amount is the weight 0.07 ‰ of lime stone slurry; After desulphurization system runs a period of time, such as, after 30 minutes, can carry out suitable adding according to desulfurization situation, additional amount is the weight 0.005-0.015 ‰ of lime stone slurry.This wet desulphurization synergist is applied to inlet flue gas SO
2concentration design load be 1681mg/Nm
3in.Flue gas SO at that time
2concentration value actual measurement for 2350mg/Nm
3, after desulfurization, exiting flue gas SO
2concentration value actual measurement for 134mg/Nm
3, liquid-gas ratio 10.5, calcium sulfur ratio 1.03, desulfuration efficiency is 94.3%.
Claims (9)
1. a wet desulphurization synergist, is characterized in that, comprises following component by weight percentage:
Organic acid 40-60%; Acylate 30-40%; Water-loss reducer 1-2%; Phase transfer catalyst 5-20%; Oxidant 4-8%.
2. wet desulphurization synergist according to claim 1, is characterized in that:
Wherein, described organic acid percentage by weight is 40-50%.
3. wet desulphurization synergist according to claim 1, is characterized in that:
Wherein, the percentage by weight of described phase transfer catalyst is 7-14%.
4. wet desulphurization synergist according to claim 1, is characterized in that:
Wherein, the percentage by weight of described oxidant is 5-6%.
5., according to the wet desulphurization synergist in claim 1-4 described in any one, it is characterized in that:
Wherein, described organic acid is binary acid, and described acylate is the soap that full conjunction or insatiable hunger are closed, and described phase transfer catalyst is quaternary ammonium salt or crown ether, and described water-loss reducer is the inorganic salts of good hygroscopicity, and described oxidant is peroxide.
6. wet desulphurization synergist according to claim 5, is characterized in that:
Wherein, described binary acid is any one in adipic acid, succinic acid or glutaric acid, and described soap is the Salt of saturated fatty acid of C4-C10, and described water-loss reducer is magnesium chloride or sodium bromide, and described oxidant is Peracetic acid or hypochlorite.
7. wet desulphurization synergist according to claim 6, is characterized in that:
Wherein, described binary acid is adipic acid, and described soap is succinate, and described water-loss reducer is magnesium chloride, and described oxidant is Peracetic acid.
8. wet desulphurization synergist according to claim 6, is characterized in that:
Wherein, the concentration of described Peracetic acid is 20%.
9. wet desulphurization synergist according to claim 1, is characterized in that:
Wherein, by weight percentage, the content of each component is:
Adipic acid: 45%; Sodium succinate: 38%; Magnesium chloride: 2%; The Peracetic acid of 20% concentration: 5%; Tetrabutylammonium chloride: 10%,
Or adipic acid: 50%; Sodium succinate: 36%; Magnesium chloride: 1%; The Peracetic acid of 20% concentration: 6%; Tetrabutylammonium chloride: 7%,
Or adipic acid: 45%; Sodium succinate: 34%; Magnesium chloride: 1%; The Peracetic acid of 20% concentration: 6%; Tetrabutylammonium chloride: 14%,
Or adipic acid: 50%; Sodium succinate: 30%; Magnesium chloride: 1%; The Peracetic acid of 20% concentration: 5%; Tetrabutylammonium chloride: 14%.
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