CN104258722A - Method for removing SO2 in tail gas - Google Patents
Method for removing SO2 in tail gas Download PDFInfo
- Publication number
- CN104258722A CN104258722A CN201410496692.3A CN201410496692A CN104258722A CN 104258722 A CN104258722 A CN 104258722A CN 201410496692 A CN201410496692 A CN 201410496692A CN 104258722 A CN104258722 A CN 104258722A
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- China
- Prior art keywords
- ore pulp
- tail gas
- gas
- phosphate ore
- dynamic wave
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- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000000126 substance Substances 0.000 claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 229910019142 PO4 Inorganic materials 0.000 claims description 77
- 239000010452 phosphate Substances 0.000 claims description 77
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 72
- 239000007788 liquid Substances 0.000 claims description 27
- 239000007787 solid Substances 0.000 claims description 23
- 238000005201 scrubbing Methods 0.000 claims description 18
- 238000010521 absorption reaction Methods 0.000 claims description 13
- 230000005484 gravity Effects 0.000 claims description 8
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 claims description 8
- 239000006260 foam Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 239000013067 intermediate product Substances 0.000 claims description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 22
- 230000008901 benefit Effects 0.000 abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 abstract description 5
- 230000023556 desulfurization Effects 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 239000002686 phosphate fertilizer Substances 0.000 abstract description 4
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 abstract description 2
- 229910001447 ferric ion Inorganic materials 0.000 abstract description 2
- 229910001428 transition metal ion Inorganic materials 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 79
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 14
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 12
- 239000000203 mixture Substances 0.000 description 8
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 229910052698 phosphorus Inorganic materials 0.000 description 7
- 239000012066 reaction slurry Substances 0.000 description 7
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 6
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 239000011574 phosphorus Substances 0.000 description 6
- 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 5
- 239000002367 phosphate rock Substances 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 239000011734 sodium Substances 0.000 description 5
- 229910052708 sodium Inorganic materials 0.000 description 5
- 238000001238 wet grinding Methods 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000011800 void material Substances 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 238000005188 flotation Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 208000027418 Wounds and injury Diseases 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- YYRMJZQKEFZXMX-UHFFFAOYSA-N calcium;phosphoric acid Chemical compound [Ca+2].OP(O)(O)=O.OP(O)(O)=O YYRMJZQKEFZXMX-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000004035 construction material Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 208000014674 injury Diseases 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 125000002467 phosphate group Chemical group [H]OP(=O)(O[H])O[*] 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a method for removing SO2 in tail gas and belongs to the technical field of inorganic chemical industry and environment engineering. The method is characterized in that phosphoric ore pulp contains transition metal ions such as Fe3+ and the like, and SO2 in the tail gas is catalyzed and oxidized into sulfuric acid by a series of reactions, so that the purpose of desulfurization is achieved; the mass transferring process is enhanced by adopting a dynamic wave scrubber, so that the mass transferring coefficient is greatly increased, the reaction rate of SO2 with the phosphoric ore pulp is increased, and the removing rate and efficiency of SO2 are improved. Compared with the other methods for removing SO2 in the tail gas, the method disclosed by the invention has the characteristics of high desulfurization efficiency, simple process, less investment, small occupied area, large operating flexibility, safe and reliable operation and low cost; reaction pulp after absorbing SO2 can enter the next production procedure for phosphate fertilizer production directly, so that sulfuric acid is saved, and secondary pollution is avoided; and the method has obvious economic and environmental benefits and is a method for high-efficiency removal of SO2 in the tail gas.
Description
Technical field
The open one of the present invention removes SO in tail gas
2method, belong to inorganic chemical industry and field of environment engineering technology.
Background technology
Along with the raising of industrial expansion and people's living standard, environmental quality is subject to people's attention day by day, SO
2be a kind of main atmosphere pollution, be the main cause causing acid rain, haze, cause huge injury to health, country has formulated stricter regulation to SO
2pollution controls.Remove SO in tail gas at present
2method a lot, but its desulfur technology to there is investment large, technological process is numerous and diverse, and perishable, blocking, operating cost is high, produces the series of problems such as a large amount of accessory substances, hinders the development of desulfurization industry always.Therefore, in the urgent need to developing a kind of desulfur technology of simple efficient, low cost, to meet the requirement of environmental protection and production.
" phosphate ore pulp catalytic oxidative desulfurization low concentration SO that publication number CN 1899668A discloses
2method ", this method: " what ground phosphate rock is milled to granularity≤154 μm accounts for 85% ~ 100%; Be that 0.5 ~ 2.5:1 prepares by ground phosphate rock and water by solid-liquid mass ratio, mix to obtain phosphate ore pulp, and to control phosphate ore pulp pH value be 3 ~ 7; Phosphate ore pulp centrifugal pump is squeezed in reactor, sulfuric acid tail gas also passes in reactor continuously, control temperature of reactor 20 ~ 65 DEG C, under in phosphate ore pulp, divalence and ferric ion exist situation, the sulfur dioxide in phosphoric acid tail gas and oxygen generation catalytic oxidation generate H
2sO
4, when the exit concentration of reactor sulfur dioxide drops to≤300mg/m
3, during pH value≤1.1 of phosphate ore pulp, reaction completes; Phosphorus ore in phosphate ore pulp and the H of generation
2sO
4generate phosphoric acid and losing efficacy after reaction, now in phosphate ore pulp phosphoric acid concentration rise to>=3% ".
Publication number CN103191637 A has applied for " a kind of industrial tail gas desulfurizer ", this method is on the basis of CN 1899668A, propose " a kind of industrial tail gas desulfurizer ", it is characterized in that described device comprises desulfurizing tower, phosphate ore pulp circulating slot, scrubbing tower, subsider, clear liquid groove, air-introduced machine, desulfurizing tower; From bottom to top, phosphate ore pulp is counter current contacting from top to bottom for the tail gas of scrubbing tower, controls phosphate ore pulp solid content 58% ~ 66%, P
2o
5mass percentage 30% ~ 38%, Fe
2o
3mass percentage 0.2% ~ 0.5%.
Publication number CN 1899668A proposes and utilizes phosphate ore pulp to absorb SO in sulfuric acid tail gas
2method and Technology principle, but the industrial technology method and access realizing the method is not proposed; Publication number CN103191637 A is to phosphate ore pulp solid content, P
2o
5, Fe
2o
3mass percentage proposes high requirement, and described desulfurizing tower, scrubbing tower exist empty tower gas velocity low (general≤5m/s), single-stage individual layer shower nozzle SO
2the rate of recovery low (≤65%), floor space is large, the deficiency that equipment investment is large.Adopt dynamic wave scrubber significantly can improve SO
2the rate of recovery, reduces equipment volume and floor space thereof.Its core technology of dynamic wave scrubber is the absorption of froth zone, namely absorbing liquid is contrary with flue gas flow direction, flue gas from top to bottom, absorbing liquid from bottom to top, make absorbing liquid and flue gas keep momentum balance, form the stable froth bed of strong turbulence, in froth bed, the turbulence film of absorbing liquid and gaseous contaminant react rapidly, reach and reclaim tail gas SO
2object.
Summary of the invention
The object of the invention is to propose a kind of utilize phosphate ore pulp and dynamic wave scrubber to combine remove SO in tail gas
2method, adopt in phosphorous chemical industry production process intermediate material---phosphate ore pulp is absorbent, combine with effectively power ripple washer, not only increase SO
2removal efficiency, directly make use of SO
2; And do not consume extra raw material (as sodium method needs NaOH, calcium method needs calcium hydroxide, and ammonia process needs synthetic ammonia etc.), decrease equipment volume, decrease plant area area, reduce investment.
Of the present inventionly remove SO in tail gas
2method, specifically comprise the following steps:
(1) by SO
2tail gas enters from the top of dynamic wave scrubber medium power ripple cylindric washer, and it flows to from top to bottom, meanwhile;
(2) phosphate ore pulp carrying out self-circulating pump enters from the Dynawave nozzle of dynamic wave cylindric washer middle and lower part, its flow direction from bottom to top, and and SO
2exhaust gas counter current contacting, collision, absorption are absorbed SO
2after phosphate ore pulp;
(3) SO is absorbed
2after reaction slurry fall into circulating slot by gravity, reacting gas enters behind the gas-liquid separation space on circulating slot top and discharges from circulating slot top, more emptying after gas-liquid separator foam removal;
(4) phosphate ore pulp after absorbing, the phosphate ore pulp of 60% ~ 90% continues SO in circularly removing tail gas
2, 10% ~ 40% is delivered to other production process of phosphorous chemical industry enterprise as intermediate products.
The mass percent of the solid content of phosphate ore pulp of the present invention is 10% ~ 45%, and phosphate ore pulp solids fineness≤100 object mass percent accounts for more than 80% of total solid matters.
The mass percent of the main chemical compositions of phosphate ore pulp of the present invention is P
2o
512% ~ 38%, MgO 0.5% ~ 10%, Fe
2o
30.1% ~ 10%.
Absorption SO of the present invention
2after phosphate ore pulp pH be 4.0-6.0, in dynamic wave scrubber, whitewashing amount and the gas volume of cylindric washer are than being 0.002:1 ~ 0.040:1, gas speed 10 ~ 40m/s.
Dynamic wave scrubber of the present invention is one-level, two-stage or three grades.
Dynamic wave scrubber of the present invention comprises air-introduced machine, dynamic wave scrubbing cylinder, Dynawave nozzle, circulating slot, circulating pump, gas-liquid separator, phosphate ore pulp make-up tank.
The equipment composition tail gas SO such as dynamic wave scrubber of the present invention, blower fan, circulating pump, gas-liquid separator
2remove system; Blower fan is for providing the transmitting power of gas phase, before blower fan can be arranged in dynamic wave scrubber, also after can being arranged in dynamic wave scrubber, the cylindric washer top of tail gas automatic Reeb washer enters, and phosphate ore pulp sprays in cylindric washer against air-flow from bottom to top by nozzle, and air-flow and liquid clash into, strong turbulence froth zone is formed in liquid-vapor interface region, in froth zone, because gas contacts with liquid surface that is great and that upgrade rapidly, SO in gas
2react rapidly with phosphate ore pulp, reach and remove SO
2effect.
The present invention adopts the feature that dynamic wave absorption efficiency is high, strengthening SO
2remove, improve the removal efficiency in FU volume significantly; The cylindric washer of dynamic wave scrubber and circulating slot can be overall, also cylindric washer, circulating slot can be arranged, respectively containing SO
2tail gas entered the cylindric washer of dynamic wave scrubber by top.
Principle of the present invention: the SO that need process
2tail gas sends into the top of dynamic wave scrubber medium power ripple cylindric washer through exhaust fan, contacts, collides, absorbs with the circulation slip carrying out self-circulating pump through Dynawave nozzle in dynamic wave scrubbing cylinder with back flow of gas, absorbs SO
2after reaction slurry, fall into circulating slot by gravity; Re-circulate in dynamic wave scrubbing cylinder through circulating pump part, part sends into other production process (phosphoric acid by wet process extraction equipment, or flotation unit, or Production of Single Superphosphate device) of phosphorous chemical industry enterprise; Fresh supplemented phosphate ore pulp needed for dynamic wave scrubber derives from phosphate ore pulp make-up tank, to guarantee the stable of production; Phosphate ore pulp needed for groove with slurry or ground phosphate rock derive from the ore grinding workshop section of phosphorous chemical industry enterprise; The tail gas absorbed through dynamic wave scrubber is emptying after gas-liquid separator foam removal.The mass flow of other production process of circulating pump feeding phosphorous chemical industry enterprise is substantially suitable with the amount of fresh supplemented phosphate ore pulp.
Circulating slot of the present invention is provided with the agitating device preventing phosphate ore pulp sedimentation.
The advantage that the present invention is compared with prior art had or good effect:
(1) compared with existing calcium method, sodium method, ammonia process, no coupling product of the present invention produces, good in economic efficiency; The present invention is specially adapted to phosphorous chemical industry garden or phosphorous chemical industry enterprise (coal-burning boiler, sulfuric acid etc.) tail gas SO
2remove, compared with existing calcium method, sodium method, ammonia process, there is no the generation of accessory substance; Relative calcium method, does not have solid waste to produce, and takes full advantage of SO
2; Relative sodium method, ammonia process, the present invention has significant economic benefit, and the cost of material of sodium method, ammonia process is high, and the value of sodium sulfate byproduct, ammonium sulfate is low, unable to make ends meet; Present invention achieves the efficiency utilization of sulphur, not only add the economic benefit of enterprise, and there is significant environmental benefit;
(2) compared with void tower, dynamic wave scrubber improves single-stage SO
2removal efficiency, SO
2removal efficiency reaches 90% ~ 99%, reduces equipment volume, reduces plant area area, reduces plant investment; The present invention adopts dynamic wave scrubber equipment, improves SO in unit volume
2removal efficiency, improves single-stage SO
2removal efficiency, significantly reduces the harmful substance contents in outside emission; Compare with void tower, at the identical tail gas amount of process and SO
2during content, single-stage SO
2removal efficiency improve 20% ~ 50%, reactor volume is only 1/5 ~ 1/20 of void tower, saves equipment construction material, reduces plant area area, reduces process units investment;
(3) phosphate ore pulp and dynamic wave scrubber effectively combine by the present invention, and desulfuration efficiency is high, and operating flexibility is large, and reliability is strong.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of single-stage dynamic wave scrubber described in embodiment 1 ~ 2;
Fig. 2 is the process flow diagram of two-stage dynamic wave scrubber;
Fig. 3 is the structural representation of single-stage dynamic wave scrubber described in embodiment 4;
In Fig. 1: 1-air-introduced machine, 2-dynamic wave scrubber I, 3-dynamic wave scrubbing cylinder I, 4-Dynawave nozzle I, 5-circulating slot I, 6-circulating pump I, 7-gas-liquid separator I, 8-phosphate ore pulp make-up tank I;
In Fig. 2: 9-first order kinetics ripple washer, 10-second motive force ripple washer, 11-primary cycle pump, 12-first order kinetics ripple cylindric washer, 13-first order kinetics ripple shower nozzle, 14-primary cycle groove, 15-one-level gas-liquid separator, 16-secondary cycle pump, 17-second motive force ripple shower nozzle, 18-second motive force ripple cylindric washer, 19-secondary gas-liquid separator, 20-blower fan, 21-phosphate ore pulp make-up tank II, 22-secondary cycle groove;
In Fig. 3: 23-air exhauster, 24-dynamic wave scrubbing cylinder II, 25-Dynawave nozzle II, 26-circulating slot II, 27-circulating pump II, 28-gas-liquid separator II, 29-phosphate ore pulp make-up tank III.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the invention will be further described, but protection scope of the present invention is not limited to described content.
Embodiment 1
The present embodiment with the sulfuric acid tail gas from double-absorption conversion section for handling object, SO in tail gas
2content be 600 ~ 900mg/m
3, described dynamic wave scrubber is one-level, and because sulfuric acid apparatus is equiped with sulfuric acid blower fan, the present embodiment installs exhaust fan no longer separately;
Specifically comprise the steps: SO
2tail gas enters from the top of dynamic wave scrubber I 2 medium power ripple cylindric washer I 3, and it flows to from top to bottom, meanwhile; The phosphate ore pulp carrying out self-circulating pump I 6 enters from the Dynawave nozzle I 4 of dynamic wave cylindric washer I 3 middle and lower part, its flow direction from bottom to top, and and SO
2exhaust gas counter current contacting, collision, absorption; Absorb SO
2after reaction slurry, fall into circulating slot I 5 by gravity, after absorbing, gas then enters the gas-liquid separation space on circulating slot I 5 top, and discharges from circulating slot I 5 top, more emptying after gas-liquid separator I 7 foam removal; Controlled circulation groove I 5 phosphate ore pulp pH is 6.0, and in circulating slot I 5, most of phosphate ore pulp re-circulates in dynamic wave scrubbing cylinder I 3, delivers to phosphate rock floating device outside small part, as Fig. 1 (cylindric washer and the circulating slot of dynamic wave scrubber are as a whole);
Phosphate ore pulp described in the present embodiment derives from the wet milling workshop section of enterprise, and the mass percent of phosphorus ore main chemical compositions is P
2o
512%, MgO 10%, Fe
2o
310%, the mass percent of phosphate ore pulp solid content is 10%, and phosphate ore pulp solids fineness≤100 object mass percent accounts for more than 80% of total solid matters.
The whitewashing amount controlling cylindric washer in dynamic wave scrubber is 0.002:1 with gas volume ratio, gas speed 10m/s, tail gas SO
2removal efficiency 93%.
Embodiment 2
Sulfuric acid tail gas from double-absorption conversion section, tail gas SO
2content is 800 ~ 1000mg/m
3, the blower fan of dependence sulfuric acid apparatus will containing SO
2800 ~ 1000mg/m
3tail gas send into the top of dynamic wave scrubbing cylinder I 3 of dynamic wave scrubber I 2, contact with back flow of gas in dynamic wave scrubbing cylinder I 3 through Dynawave nozzle I 4 with the circulation slip carrying out self-circulating pump I 6, collide, absorb, absorption SO
2after reaction slurry, fall into circulating slot I 5 by gravity; Controlled circulation groove I 5 phosphate ore pulp pH is 4.0, phosphate ore pulp after a part absorbs by circulating pump I 6 re-circulates in dynamic wave scrubbing cylinder I 3, phosphate ore pulp after partially absorbing in addition sends into phosphate fertilizer phosphoric acid by wet process extraction equipment, as Fig. 1 (cylindric washer and the circulating slot of dynamic wave scrubber are as a whole);
Fresh supplemented phosphate ore pulp needed for dynamic wave scrubber I 2 derives from phosphate ore pulp make-up tank I 8; Phosphate ore pulp needed for groove I 8 with slurry derives from the wet milling workshop section of enterprise, and the mass percent of its phosphorus ore main chemical compositions is P
2o
538%, MgO 0.5%, Fe
2o
30.1%; The mass percent of phosphate ore pulp solid content is 30%, and phosphate ore pulp solids fineness≤100 object mass percent accounts for 95% of total solid matters, and in dynamic wave scrubber, the whitewashing amount of cylindric washer is 0.006:1 with the ratio (volume ratio) of gas, gas speed 30m/s.
Through the tail gas that dynamic wave scrubber I 2 absorbs, enter the gas-liquid separation space on circulating slot I 5 top, and discharge from circulating slot I 5 top, more emptying after gas-liquid separator I 7 foam removal, its SO
2concentration≤100mg/m
3, SO in tail gas
2removal efficiency 90%.
Embodiment 3
As Fig. 2, since the present embodiment, the boiler exhaust gas of self-fluidized type bed coal-burning boiler is handling object, tail gas SO
2content is 2500 ~ 3000mg/m
3, described dynamic wave scrubber is secondary.
Specifically comprise the steps: that tail gas enters the top of first order kinetics ripple cylindric washer 12 in first order kinetics ripple washer 9 through the coal-fired boiler tail gas that blower fan 20 aspirates, contact with back flow of gas with the circulation slip from primary cycle pump 11 in first order kinetics ripple cylindric washer 12 through first order kinetics ripple shower nozzle 13, collide, absorb, absorb SO
2after reaction slurry, fall into primary cycle groove 14 by gravity; Slip re-circulates in first order kinetics ripple cylindric washer 12 through primary cycle pump 11 part, and part is sent into phosphate rock floating device and carried out reverse flotation and remove MgO in phosphorus ore; Supplementary phosphate ore pulp needed for first order kinetics ripple washer 9 derives from secondary cycle pump 16; SO in first order kinetics ripple washer 9
2removal efficiency 65% ~ 75%, in first order kinetics ripple washer, the whitewashing amount of cylindric washer is 0.04 with the ratio (volume ratio) of gas, gas speed 40m/s; Tail gas after absorption is through one-level gas-liquid separator 15, enter the top of second motive force ripple cylindric washer 18 in second motive force ripple washer 10 again, contact with back flow of gas with the circulation slip from secondary cycle pump 16 in second motive force ripple cylindric washer 18 through second motive force ripple shower nozzle 17, collide, absorb, absorb SO
2after reaction slurry, fall into secondary cycle groove 22 by gravity; Slip re-circulates in second motive force ripple cylindric washer 18 through secondary cycle pump 16 part, and part sends into primary cycle groove 14; Second motive force ripple washer SO
2removal efficiency 90% ~ 95%, in second motive force ripple washer, the whitewashing amount of cylindric washer is 0.005 with the ratio (volume ratio) of gas, gas speed 10m/s; Tail gas after absorption, through secondary gas-liquid separator 19, enters exhaust fan 20, and the tail gas after purification, containing SO
2be down to 60 ~ 90 mg/m
3, by smoke stack emission to air; Supplementary phosphate ore pulp needed for second motive force ripple washer 10 derives from phosphate ore pulp make-up tank II 21; Phosphate ore pulp needed for groove II 21 with slurry derives from the wet milling workshop section of enterprise; In groove with slurry, the mass percent of phosphate ore pulp main chemical compositions is P
2o
526%, MgO 5%, Fe
2o
31.5%; The mass percent of phosphate ore pulp solid content is 30%, and phosphate ore pulp solids fineness≤100 object mass percent accounts for 95% of total solid matters.
Embodiment 4
Sulfuric acid tail gas from coal-fired boiler tail gas, tail gas SO
2content is 1000 ~ 1200mg/m
3, dependence air exhauster 23 will containing SO
21000 ~ 1200mg/m
3tail gas send into the top of dynamic wave scrubbing cylinder II 24, contact with back flow of gas in dynamic wave scrubbing cylinder II 24 through Dynawave nozzle II 25 with the circulation slip carrying out self-circulating pump II 27, collide, absorb, absorption SO
2after reaction slurry, fall into circulating slot II 26 by gravity; Phosphate ore pulp after a part absorbs by circulating pump II 27 re-circulates in dynamic wave scrubbing cylinder II 24, phosphate ore pulp after remainder absorbs sends into phosphate fertilizer phosphoric acid by wet process extraction equipment, as shown in Figure 3 (cylindric washer, the circulating slot of dynamic wave scrubber are arranged respectively);
Fresh supplemented phosphate ore pulp needed for dynamic wave scrubber II 25 derives from phosphate ore pulp make-up tank III 29; Phosphate ore pulp needed for groove III 29 with slurry derives from the wet milling workshop section of enterprise, and the mass percent of its phosphorus ore main chemical compositions is P
2o
529%, MgO 0.7%, Fe
2o
31.5%; The mass percent of phosphate ore pulp solid content is 45%, and phosphate ore pulp solids fineness≤100 object mass percent accounts for 95% of total solid matters, and the whitewashing amount of cylindric washer is 0.007 with the ratio (volume ratio) of gas, gas speed 25m/s.
Through the tail gas that dynamic wave scrubbing cylinder II 24 absorbs, derive from the side pipe of cylindric washer bottom, emptying after entering gas-liquid separator II 28 foam removal; Its SO
2concentration≤120mg/m
3, tail gas SO
2removal efficiency>=90%.
Embodiment 5
Since the present embodiment, the boiler exhaust gas of self-fluidized type bed coal-burning boiler is handling object, tail gas SO
2content is 3500 ~ 5000mg/m
3, described dynamic wave scrubber is three grades.
Specifically comprise the steps: from fluidized bed combustion coal burning boiler SO
2tail gas enters first order kinetics ripple washer, and the whitewashing amount controlling first order kinetics ripple cylindric washer is 0.03 with the ratio (volume ratio) of gas, gas speed 40m/s, and primary cycle slip pH is 4.5; Absorb SO
2after phosphate ore pulp, major part re-circulates in the cylindric washer of first order kinetics ripple washer, delivers to phosphate fertilizer phosphoric acid by wet process extraction equipment outside small part; The tail gas of discharging from first order kinetics ripple circulating slot top enters second motive force ripple washer, and the whitewashing amount controlling second motive force ripple cylindric washer is 0.02 with the ratio (volume ratio) of gas, gas speed 30m/s, and secondary cycle slip pH is 5; The tail gas of discharging from second motive force ripple circulating slot top enters three grades of dynamic wave scrubbers, and controlling the whitewashing amount of three grades of dynamic wave scrubbing cylinders is 0.01 with the ratio (volume ratio) of gas, gas speed 12m/s, and three grades of circulation slip pH are 5.5; Needed for three grades of circulating slots, phosphate ore pulp derives from the wet milling workshop section of enterprise, and the mass percent of phosphorus ore main chemical compositions is P
2o
529%, MgO 0.6%, Fe
2o
31.9%, the mass percent of phosphate ore pulp solid content is 20%, and phosphate ore pulp solids fineness≤100 object mass percent accounts for 90% of total solid matters.
The SO of the present embodiment
2removal efficiency is respectively one-level 60%, secondary 70%, three grade 90%; Total SO
2removal efficiency 98.8%.
Claims (6)
1. one kind removes SO in tail gas
2method, it is characterized in that: adopt phosphate ore pulp and SO
2reaction, dynamic wave scrubber removes the SO in tail gas as reactor
2.
2. remove SO in tail gas according to claim 1
2method, it is characterized in that, specifically comprise the following steps:
(1) by SO
2tail gas enters from the top of dynamic wave scrubber medium power ripple cylindric washer, and it flows to from top to bottom, meanwhile;
(2) phosphate ore pulp carrying out self-circulating pump enters from the Dynawave nozzle of dynamic wave cylindric washer middle and lower part, its flow direction from bottom to top, and and SO
2be absorbed after exhaust gas counter current contacting, collision, absorption SO
2after phosphate ore pulp;
(3) SO is absorbed
2after phosphate ore pulp fall into circulating slot by gravity, reacting gas enters behind the gas-liquid separation space on circulating slot top and discharges from circulating slot top, more emptying after gas-liquid separator foam removal;
(4) phosphate ore pulp after absorbing, the phosphate ore pulp of 60% ~ 90% continues SO in circularly removing tail gas
2, 10% ~ 40% is delivered to other production process of phosphorous chemical industry enterprise as intermediate products.
3. according to claim 1ly remove SO in tail gas
2method, it is characterized in that: the mass percent of the solid content of described phosphate ore pulp is 10% ~ 45%, phosphate ore pulp solids fineness≤100 object mass percent accounts for more than 80% of total solid matters.
4. according to claim 1ly remove SO in tail gas
2method, it is characterized in that: described absorption SO
2after phosphate ore pulp pH be 4.0-6.0, in dynamic wave scrubber, whitewashing amount and the gas volume of cylindric washer are than being 0.002:1 ~ 0.040:1, gas speed 10 ~ 40m/s.
5. according to claim 1ly remove SO in tail gas
2method, it is characterized in that: described dynamic wave scrubber is one-level, two-stage or three grades.
6. according to claim 1ly remove SO in tail gas
2method device used, it is characterized in that: described dynamic wave scrubber comprises air-introduced machine, dynamic wave scrubbing cylinder, Dynawave nozzle, circulating slot, circulating pump, gas-liquid separator, phosphate ore pulp make-up tank, wherein, circulating slot is provided with agitating device.
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| CN201410496692.3A CN104258722A (en) | 2014-09-25 | 2014-09-25 | Method for removing SO2 in tail gas |
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| CN201410496692.3A CN104258722A (en) | 2014-09-25 | 2014-09-25 | Method for removing SO2 in tail gas |
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| CN105536493A (en) * | 2015-12-28 | 2016-05-04 | 昆明理工大学 | Method for removing SO2 and NOX from flue gas of coal-fired boiler by virtue of phosphoric ore pulp and phosphorus sludge |
| CN106310932A (en) * | 2015-07-07 | 2017-01-11 | 云南民族大学 | Method for removing NO in industrial waste gas by phosphorite slurry phase catalytic oxidation |
| CN109772134A (en) * | 2019-01-10 | 2019-05-21 | 昆明理工大学 | A kind of circularly removing H2S and SO2And the method for recycling sulphur |
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| CN106310932B (en) * | 2015-07-07 | 2019-02-22 | 云南民族大学 | A kind of method that phosphate ore pulp liquid phase catalytic oxidation removes NO in industrial waste gas |
| CN105536493A (en) * | 2015-12-28 | 2016-05-04 | 昆明理工大学 | Method for removing SO2 and NOX from flue gas of coal-fired boiler by virtue of phosphoric ore pulp and phosphorus sludge |
| CN105536493B (en) * | 2015-12-28 | 2018-04-06 | 昆明理工大学 | One kind utilizes SO in phosphate ore pulp and mud phosphorus removing fire coal boiler fume2And NOXMethod |
| CN109772134A (en) * | 2019-01-10 | 2019-05-21 | 昆明理工大学 | A kind of circularly removing H2S and SO2And the method for recycling sulphur |
| CN109772134B (en) * | 2019-01-10 | 2021-12-28 | 昆明理工大学 | Circulation desorption H2S and SO2And process for recovering sulfur |
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Application publication date: 20150107 |