CN1482057A - Method for preparing sulfuric acid by using five-section catalyst two-conversion and two-absorption of flue gas of lead bottom blowing furnace - Google Patents
Method for preparing sulfuric acid by using five-section catalyst two-conversion and two-absorption of flue gas of lead bottom blowing furnace Download PDFInfo
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- CN1482057A CN1482057A CNA031261744A CN03126174A CN1482057A CN 1482057 A CN1482057 A CN 1482057A CN A031261744 A CNA031261744 A CN A031261744A CN 03126174 A CN03126174 A CN 03126174A CN 1482057 A CN1482057 A CN 1482057A
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- 239000003546 flue gas Substances 0.000 title claims abstract description 82
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 239000003054 catalyst Substances 0.000 title claims abstract description 71
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 41
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 26
- 238000007664 blowing Methods 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims description 25
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title description 6
- 238000001816 cooling Methods 0.000 claims abstract description 28
- 239000007789 gas Substances 0.000 claims abstract description 15
- 239000002253 acid Substances 0.000 claims abstract description 13
- 238000001035 drying Methods 0.000 claims abstract description 9
- 239000012535 impurity Substances 0.000 claims abstract description 4
- 239000003595 mist Substances 0.000 claims abstract description 4
- 238000012856 packing Methods 0.000 claims description 22
- 239000012530 fluid Substances 0.000 claims description 19
- 239000000779 smoke Substances 0.000 claims description 11
- 230000008569 process Effects 0.000 claims description 10
- 238000012546 transfer Methods 0.000 claims description 8
- 230000005611 electricity Effects 0.000 claims description 6
- 238000005516 engineering process Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000006228 supernatant Substances 0.000 claims description 5
- 239000012717 electrostatic precipitator Substances 0.000 claims description 4
- 239000003500 flue dust Substances 0.000 claims description 4
- 239000008400 supply water Substances 0.000 claims description 4
- 230000001627 detrimental effect Effects 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 claims description 3
- 239000002826 coolant Substances 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract 2
- 238000006477 desulfuration reaction Methods 0.000 abstract 1
- 230000023556 desulfurization Effects 0.000 abstract 1
- 229940056932 lead sulfide Drugs 0.000 abstract 1
- 229910052981 lead sulfide Inorganic materials 0.000 abstract 1
- 230000001590 oxidative effect Effects 0.000 abstract 1
- 239000000428 dust Substances 0.000 description 24
- 239000012716 precipitator Substances 0.000 description 9
- 238000013461 design Methods 0.000 description 6
- 230000007613 environmental effect Effects 0.000 description 6
- 238000000746 purification Methods 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- 239000011800 void material Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000009413 insulation Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 238000003723 Smelting Methods 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000013517 stratification Methods 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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Abstract
The invention relates to SO-containing gas generated by oxidative desulfurization when lead sulfide ore is smelted by using a lead bottom blowing furnace2The flue gas of the lead bottom blowing furnace is dedusted and cooled, then enters a high-efficiency washer, is fully contacted with circulating liquid for dedusting and cooling, the flue gas discharged from the high-efficiency washer enters a packed tower and is in countercurrent contact with the circulating liquid cooled by a dilute acid plate heat exchanger for further cooling and dedusting, the flue gas discharged from the packed tower enters an electric demister for removing acid mist and other harmful impurities, and then is sent to a drying tower, and the dried flue gas is sent to an absorption tower for absorption and acid production after being sequentially subjected to five-section catalyst double-conversion and double-suction by a heat exchanger and a converter.
Description
Technical field
The invention belongs to the non-ferrous metal metallurgy industry, relate in particular to a kind of when the use lead bottom blowing furnace is plumbous to plumbous sulphide ores refining, the SO that contains of oxidation sweetening generation
2Flue gas adopt the five stage catalyst double conversion and double absorption to produce the vitriolic method.
Background technology
When refining lead with plumbous sulphide ores, need oxidation sweetening, generation contains SO
2Flue gas, the flue gas that traditional sintering pot-blast furnace refining splicer plants and produces, SO
2Concentration is very low and fluctuation is big, can not be used for relieving haperacidity; Adopt the enterprise of this technology, all with the direct emptying of flue gas, serious environment pollution.The flue gas that traditional sinter machine-blast furnace refining splicer plants and produces, SO
2Concentration is 1-3.5%, can not adopt ordinary method relieving haperacidity, can only adopt unstable state to transform or Top's rope method relieving haperacidity, and unstable state transforms relieving haperacidity and can only a commentaries on classics one inhale, and the tail gas after the relieving haperacidity does not still reach national environmental standard requirement, contaminate environment.Though Top's rope method can make tail gas up to standard, this method is a Danish Patent, and introduction and facility investment are huge, and general smelting enterprise is difficult to bear.Under this background, domestic nearest research has also been built up the industrialized unit of " oxygen bottom blowing stove oxidation-blast furnace reduction refines plumbous novel process ".Plumbous sulphide ores can output contain SO in the oxygen bottom blowing stove
2Flue gas about 15%, this flue-gas temperature up to 1000 ℃ about, contain flue dust up to more than the 250g/Nm3, in addition, also contain steam and 0.3% above SO about 15%
3This flue gas is behind the waste heat boiler and dust precipitator cooling dedusting of particular design, and composition is roughly as follows:
Dust precipitator outlet exhaust gas components (V%)
SO
2 SO
3 CO
2 N
2 O
2 H
2O
8.95 0.28 1.68 62.56 14.29 12.28
Below flue-gas temperature: 280-290 ℃ (design load)
Dust contained flue gas: 250mg/Nm
3About
Flue gas contains AS:0.68g/Nm
3About
Flue gas contains F:0.40g/Nm
3About
Because flue dust character is special in the plumbous flue gas during smelting, the cooling that waste heat boiler and electricity gather dust, the dust collection effect instability, gather dust exit gas temperature and dust content and design load of the electricity of actual measurement differs bigger, is respectively:
Flue-gas temperature: 320-350 ℃
Dust contained flue gas: 0.15-10g/Nm
3
To such flue gas, can adopt purification and four sections catalyst of conventional design, double conversion and double absorption relieving haperacidity, that is: purification is adopted: void tower-packing tower-inter cooler-one-level electricity demist-secondary electricity demist flow process, transform and adopt four sections catalyst, the general III+I flow process that adopts also has and adopt the II+II flow process, but effect is good not as the III+I flow process.This old process, to smoke of lead bottom blowing furnace, there are the following problems: 1, the dustiness fluctuation is too big, when dust-laden is high, is difficult to guarantee the requirement of blower export dust-laden less than 0.002g/Nm3, causes the infringement to catalyst.2, cause the obstruction of void tower shower nozzle in the conventional treating plant, packing tower, inter cooler etc. easily, and then cause system's operation undesired, even the cleaning that stops production.3, because gas is dense higher, adopt four sections catalyst, the tail gas of double conversion and double absorption relieving haperacidity, still difficulty reaches environmental protection standard less than 850mg/Nm
3Requirement, want to reach the environmental protection standard requirement, then need adopt the import catalyst.
The object of the invention is to overcome the deficiencies in the prior art and a kind of characteristic of plumbous flue gas during smelting after waste heat boiler and dust precipitator cooling dedusting that produces at the oxygen bottom blowing stove is provided, after effectively purifying, adopt five stage catalyst, double conversion and double absorption relieving haperacidity guarantees that the five stage catalyst double conversion and double absorption that tail gas after the relieving haperacidity reaches the requirement of national environmental standard produces the vitriolic method.
The present invention seeks to realize like this: smoke of lead bottom blowing furnace is through dedusting, after the cooling, enter in the high energy scrubber, fully contact with the circulation fluid that comes self-circulating pump and to carry out dedusting, cooling, the flue gas of being discharged by high energy scrubber enters packing tower again, with come self-circulating pump through diluted acid plate-type heat exchanger refrigerative circulation fluid counter current contact, further cooling, dedusting, the flue gas that packing tower is discharged enters electrostatic precipitator, after removing acid mist and other detrimental impurity, be sent to drying tower, dried flue gas is undertaken sending into the absorption tower behind the five stage catalyst double conversion and double absorption by interchanger and convertor successively and absorbs, relieving haperacidity.
The present invention has following positively effect:
1, can adapt to the fluctuation of the plumbous flue gas of oxygen bottom blowing stove refining performance after waste heat boiler and dust precipitator cooling receipts.Even Wen Gaoda 320-350 ℃, dust content reaches 10g/Nm
3About, also can guarantee the normal operation of purification system; Guarantee that the blower export flue gas reaches the requirement of sulfuric acid production process.Avoided conventional purification easily generation equipment stop up and the blower export flue gas contains the problem that does not reach processing requirement.
2, realized the catalyst production domesticization, and guaranteed that transformation efficiency reaches more than 99.6%.According to environmental administration's monitoring, SO in the sulfuric acid tail gas
2Content is lower than 100mg/Nm
3Than national environmental standard 850mg/Nm
3Also much lower.Can significantly reduce of the pollution of plumbous smeltery flue gas, create condition for plumbous smeltery realizes cleaner production to environment.
3, dust precipitator is exported to the herringbone tube that the suitable insulation of sufficient length is adopted in the high energy scrubber import, not only can guarantee the requirement of high energy scrubber entrance flue gas temperature, and avoid corrosive pipeline.
4, supply water to the high energy scrubber overflow weir by elevated tank, even the burst power outage can guarantee that also high energy scrubber is not damaged.
5, owing to reduced equipment failure rate, the feasible operating rate of the total system of bottom convertor that comprises improves, and labor condition improves, and labour intensity reduces, and then increases substantially economic benefit of enterprises.
Description of drawings
Fig. 1 is a purification process schema of the present invention.
Fig. 2 is an III+II type five stage catalyst double conversion and double absorption process flow sheet of the present invention.
Fig. 3 is an IV+I type five stage catalyst double conversion and double absorption process flow sheet of the present invention.
Embodiment
As shown in Figure 1, the present invention is cooled to below 280 ℃ through the herringbone tube of sufficient length by 320-350 ℃ of flue gas of dust precipitator outlet, herringbone tube and ash bucket thereof all need certain thickness lagging material insulation, and insulation layer thickness should guarantee that the inside pipe wall temperature is higher than flue gas dew point.
Flue gas after herringbone tube's cooling enters high energy scrubber 1, fully contact with the circulation fluid that comes self-circulating pump, dedusting, cooling effect take place, flue dust in the flue gas enters circulation fluid more than 90%, flue-gas temperature drops to below 80 ℃, the circulation fluid of discharging from the bottom of high energy scrubber 1 enters the subsider sedimentation, and supernatant liquor is squeezed into by recycle pump and recycled; For protection high energy scrubber 1 is supplied water to elevated tank 6 by working shaft; supply water to high energy scrubber 1 overflow weir by elevated tank 6 again; when the volume of elevated tank 6 should guarantee to have a power failure suddenly; the water of elevated tank 6 continues to supply water to the overflow weir of high energy scrubber 1, no longer enters high energy scrubber 1 until flue gas.
The flue gas of being discharged by the top of high energy scrubber 1 enters the bottom of packing tower 2, with come self-circulating pump through diluted acid plate-type heat exchanger 5 refrigerative circulation fluid counter current contact, further cooling, dedusting, require flue-gas temperature to drop to below 36 ℃, the circulation fluid that discharge the bottom of packing tower 2 advances circulation groove, and the supernatant liquor of circulation groove is squeezed into plate-type heat exchanger 5 by recycle pump, is cooled to below 34 ℃, enter the top of packing tower 2, recycle; Behind the water coolant process plate-type heat exchanger 5 from cooling water circulating pump, absorbed the heat of circulation fluid, need go to recycle after the cooling tower cooling.The middle and lower part not susceptible to plugging diameter of the filling 75 Haier ring of packing tower 2, the top filling is the rectangular saddle ring of conventional many one times diameter 25.
The flue gas of being discharged by packing tower 2 tops is successively by conventional first step electrostatic precipitator and the second stage electrostatic precipitator that purifies, remove acid mist and other detrimental impurity after, be sent to drying tower.
At dust precipitator outlet dust contained flue gas concentration instability, higher sometimes, the shortcoming that easily causes void tower nozzle, packing tower and inter cooler in the conventional design to stop up is with the void tower of high energy scrubber replacement conventional design; In the packing tower, the not susceptible to plugging filler of bottom filling; The cancellation inter cooler with the circulation fluid of diluted acid plate-type heat exchanger cooling packing tower, meets processing requirement thereby the flue-gas temperature of drying tower import is dropped to.
High energy scrubber is a kind of gas purifying equipment, and its allows solids content in circulation fluid up to about 20%, and does not stop up nozzle.Even the dust content in the flue gas up to 10g/Nm3 about, can not cause its nozzle to stop up yet, can move steadily in the long term.
The dedusting of high energy scrubber, temperature reduction performance are good especially, and its efficiency of dust collection is up to more than 90%, and the efficiency of dust collection of corresponding void tower has only 30-40%, and 280 ℃ flue gas just can drop to below 80 ℃ through behind the high energy scrubber.
Because high energy scrubber removes most of dirt, in the packing tower, the bottom inserts not susceptible to plugging major diameter Haier ring again, can prevent the obstruction of packing tower effectively.
Dust-laden is originally not high in the circulation fluid of packing tower, in circulation groove, do sedimentation slightly, supernatant liquor is squeezed into pump and is cooled to 34 ℃ in the diluted acid plate-type heat exchanger 5, drench from packing tower top down, with the direct contact heat-exchanging of flue gas adverse current, thereby guarantee that packing tower outlet flue gas under the situation of cancellation inter cooler, drops to below 36 ℃, satisfy manufacturing technique requirent.
Because the requirement of the inner impregnating material of high energy scrubber, the high energy scrubber entrance flue gas temperature should be lower than 280 ℃, the dust precipitator exit gas temperature is 320-350 ℃, need reduce 40-70 ℃ again, just can enter high energy scrubber, because contain more water and sulphur trioxide in the flue gas, the dew point of flue gas is higher,, dust precipitator needs certain thickness insulation so being exported to the flue of high energy scrubber inlet, otherwise, inner-walls of duct will generate condensation acid and corrosion pipeline should be incubated, again heat radiation, just require pipeline that enough length is arranged, consider electricity gather dust the outlet dust contained flue gas very high sometimes, easily cause the pipeline dust stratification, this segment pipe makes the herringbone tube, be provided with ash bucket in the herringbone tube bottom, do like this, promptly can in limited distance, increase duct length, can avoid the pipeline dust stratification again.
As shown in Figure 2, five stage catalyst double conversion and double absorption of the present invention is meant and adopts III+II type five stage catalyst double conversion and double absorption technology, be specially: from the flue gas of drying tower successively through four interchanger 7,8,9, between 10 pipe, after temperature is elevated to about 410 ℃, enter the catalyst chamber of convertor from the top of convertor, in convertor, from top to bottom, be followed successively by five stage catalyst, there is dividing plate separately between every adjacent two sections catalyst, flue gas through first section catalyst 11 after, enter in the pipe of interchanger 10, the heat transfer tube of interchanger 10 is connected with second section catalyst 12 again, enter behind the flue gas cool-down in second section catalyst 12, flue gas enters in the pipe of interchanger 16 behind second section catalyst 12, and the heat transfer tube of interchanger 16 is connected with the 3rd section catalyst 13 again, flue gas is behind the 3rd section catalyst 13, enter interchanger 17 successively, in 18 the pipe, temperature drops to below 180 ℃, delivers to first absorption tower and carries out absorbing the first time; Flue gas from first absorption tower through absorbing for the first time, pass through successively between the pipe of interchanger 18,17,16, temperature rises to more than 400 ℃, enters the 4th section catalyst 14 of convertor, behind the 4th section catalyst 14, enter in the pipe of interchanger 9, enter five stage catalyst 15 after the cooling, flue gas is behind five stage catalyst 15, enter successively in the pipe of interchanger 8,7, temperature drops to below 140 ℃, delivers to second absorption tower and carries out absorbing the second time tail gas emptying after absorbing for the second time.
As shown in Figure 3, five stage catalyst double conversion and double absorption of the present invention also can adopt IV+I type five stage catalyst double conversion and double absorption technology, be specially: from the flue gas of drying tower successively through four interchanger 7,8,9, between 10 pipe, after temperature is elevated to about 410 ℃, enter convertor from the top of convertor, flue gas through first section catalyst 11 after, enter in the pipe of interchanger 10, the heat transfer tube of interchanger 10 is connected with second section catalyst 12 again, flue gas is behind second section catalyst 12, enter in the pipe of interchanger 16, the heat transfer tube of interchanger 16 is connected with the 3rd section catalyst 13 again, flue gas enters in the pipe of interchanger 9 behind the 3rd section catalyst 13, delivers to the 4th section catalyst 14 after the cooling, after entering the 4th section catalyst 14, passing through interchanger 17 successively, in 18 the pipe, temperature drops to below 180 ℃, delivers to first absorption tower and carries out absorbing the first time; Flue gas from first absorption tower through absorbing for the first time, pass through successively between the pipe of interchanger 18,17,16, temperature rises to more than 400 ℃, enter the five stage catalyst 15 of convertor, behind five stage catalyst 15, enter successively in the pipe of interchanger 8,7, temperature drops to below 140 ℃, deliver to second absorption tower and carry out absorbing the second time tail gas emptying after absorbing for the second time.
Claims (6)
1, a kind of smoke of lead bottom blowing furnace five stage catalyst double conversion and double absorption system vitriolic method is characterized in that:
A, smoke of lead bottom blowing furnace are after dedusting, cooling, enter in the high energy scrubber (1), fully contact with the circulation fluid that comes self-circulating pump and to carry out dedusting, cooling, the flue gas of being discharged by high energy scrubber (1) enters packing tower (2) again, and comes self-circulating pump through diluted acid plate-type heat exchanger (5) refrigerative circulation fluid counter current contact, further cooling, dedusting, the flue gas that packing tower (2) is discharged enters electrostatic precipitator (3), (4), after removing acid mist and other detrimental impurity, be sent to drying tower
B, dried flue gas are undertaken sending into behind the five stage catalyst double conversion and double absorption that the absorption tower absorbs, relieving haperacidity successively by interchanger and convertor.
2, a kind of smoke of lead bottom blowing furnace five stage catalyst double conversion and double absorption system vitriolic method according to claim 1, it is characterized in that: described five stage catalyst double conversion and double absorption is meant and adopts III+II type five stage catalyst double conversion and double absorption technology, be specially: from the flue gas of drying tower successively through four interchanger (7), (8), (9), between pipe (10), after temperature is elevated to about 410 ℃, enter convertor from the top of convertor, flue gas through first section catalyst (11) after, enter in the pipe of interchanger (10), the heat transfer tube of interchanger (10) is connected with second section catalyst (12) again, enter second section catalyst (12) behind the flue gas cool-down, flue gas is behind second section catalyst (12), enter in the pipe of interchanger (16), the heat transfer tube of interchanger (16) is connected with the 3rd section catalyst (13) again, flue gas is behind the 3rd section catalyst (13), enter interchanger (17) successively, (18) in the pipe, temperature drops to below 180 ℃, delivers to first absorption tower and carries out absorbing the first time; Flue gas from first absorption tower through absorbing for the first time, pass through successively between the pipe of interchanger (18), (17), (16), temperature rises to more than 400 ℃, enter the 4th section catalyst (14) of convertor, behind the 4th section catalyst (14), enter in the pipe of interchanger (9), enter five stage catalyst (15) after the cooling, flue gas is behind five stage catalyst (15), enter successively in the pipe of interchanger (8), (7), temperature drops to below 140 ℃, delivers to second absorption tower and carries out absorbing the second time tail gas emptying after absorbing for the second time.
3, a kind of smoke of lead bottom blowing furnace five stage catalyst double conversion and double absorption system vitriolic method according to claim 1, it is characterized in that: described five stage catalyst double conversion and double absorption also can adopt IV+I type five stage catalyst double conversion and double absorption technology, be specially: from the flue gas of drying tower successively through four interchanger (7), (8), (9), between pipe (10), after temperature is elevated to about 410 ℃, enter convertor from the top of convertor, flue gas through first section catalyst (11) after, enter in the pipe of interchanger (10), the heat transfer tube of interchanger (10) is connected with second section catalyst (12) again, flue gas is behind second section catalyst (12), enter in the pipe of interchanger (16), the heat transfer tube of interchanger (16) is connected with the 3rd section catalyst (13) again, flue gas is behind the 3rd section catalyst (13), enter in the pipe of interchanger (9), deliver to the 4th section catalyst (14) after the cooling, after entering the 4th section catalyst (14), passing through interchanger (17) successively, (18) in the pipe, temperature drops to below 180 ℃, delivering to first absorption tower carries out absorbing for the first time: from the flue gas through absorbing for the first time on first absorption tower, pass through interchanger (18) successively, (17), between pipe (16), temperature rises to more than 400 ℃, enter the five stage catalyst (15) of convertor, behind five stage catalyst (15), enter interchanger (8) successively, (7) in the pipe, temperature drops to below 140 ℃, deliver to second absorption tower and carry out absorbing the second time tail gas emptying after absorbing for the second time.
4, a kind of smoke of lead bottom blowing furnace five stage catalyst double conversion and double absorption system vitriolic method according to claim 1, it is characterized in that: enter high energy scrubber (1) before at smoke of lead bottom blowing furnace through the dedusting of electricity receipts device, cooling, need be cooled to below 280 ℃ through the herring-bone pipeline.
5, a kind of smoke of lead bottom blowing furnace five stage catalyst double conversion and double absorption system vitriolic method according to claim 1, it is characterized in that: also be provided with elevated tank (6) in high energy scrubber (1) top, elevated tank (6) is connected by the subsider of recycle pump with high energy scrubber (1), be provided with overflow weir around the interior wall of high energy scrubber (1), flue gas after herringbone tube's cooling enters high energy scrubber 1, fully contact with the circulation fluid that comes self-circulating pump, carry out dedusting, cooling, flue dust in the control flue gas enters circulation fluid more than 90%, flue-gas temperature drops to below 80, the circulation fluid of discharging from the bottom of high energy scrubber 1 enters the subsider sedimentation, supernatant liquor is squeezed into by recycle pump and is recycled, when the volume of header tank 6 should guarantee to have a power failure suddenly, the water of header tank 6 continues to supply water to the overflow weir of high energy scrubber 1, no longer enters high energy scrubber 1 until flue gas.
6, a kind of smoke of lead bottom blowing furnace five stage catalyst double conversion and double absorption system vitriolic method according to claim 1, it is characterized in that: the flue gas of being discharged by the top of high energy scrubber 1 enters the bottom of packing tower 2, with come self-circulating pump through diluted acid plate-type heat exchanger 5 refrigerative circulation fluid counter current contact, further cooling, dedusting, require flue-gas temperature to drop to below 36 mouthfuls, the circulation fluid that discharge the bottom of packing tower 2 advances circulation groove, the supernatant liquor of circulation groove is squeezed into plate-type heat exchanger 5 by recycle pump, be cooled to below 34, enter the top of packing tower 2, recycle, behind the water coolant process plate-type heat exchanger 5 from cooling water circulating pump, absorbed the heat of circulation fluid, need go to recycle after the cooling tower cooling.
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|---|---|---|---|
| CN 03126174 CN1231413C (en) | 2003-05-16 | 2003-05-16 | Method for preparing sulfuric acid by using five-section catalyst two-conversion and two-absorption of flue gas of lead bottom blowing furnace |
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| CN 03126174 CN1231413C (en) | 2003-05-16 | 2003-05-16 | Method for preparing sulfuric acid by using five-section catalyst two-conversion and two-absorption of flue gas of lead bottom blowing furnace |
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| CN101143716B (en) * | 2006-09-15 | 2010-05-12 | 南化集团研究院 | Low concentration sulphur dioxide flue gas acid preparing heat using method |
| CN103011092A (en) * | 2012-12-28 | 2013-04-03 | 中国瑞林工程技术有限公司 | Technique for preparing sulfuric acid from SO2 by non-equilibrium state high-concentration twice conversion |
| CN101301567B (en) * | 2007-01-23 | 2013-08-07 | 琳德股份有限公司 | Process for removing contaminants from gas streams |
| CN103303878A (en) * | 2013-05-30 | 2013-09-18 | 福建省邵武市永飞化工有限公司 | Method for preparing sulfuric acid by iron pyrite |
| CN105399059A (en) * | 2015-11-26 | 2016-03-16 | 湖南华信稀贵科技有限公司 | Monitoring device for washer elevated tank in sulphuric acid workshop |
| CN107596844A (en) * | 2017-11-03 | 2018-01-19 | 天津市三木森电炉股份有限公司 | A kind of flue gas cleaning system |
| CN108970337A (en) * | 2018-07-26 | 2018-12-11 | 扬州嘉明环保科技有限公司 | Reduce dry method Sulphuric acid device wastewater discharge system and its application method |
| CN110124510A (en) * | 2019-01-29 | 2019-08-16 | 浙江天能电源材料有限公司 | A method of utilizing oxygen-enriched side-blowing smelting lead extracting sulfuric acid |
| CN111994878A (en) * | 2020-09-04 | 2020-11-27 | 太和县大华能源科技有限公司 | Method for recycling sulfuric acid from waste acid recovered from lead-acid battery |
| CN112957890A (en) * | 2021-02-09 | 2021-06-15 | 刘乾 | Closed pickling purification process for reducing total emission of dilute sulfuric acid and recovering condensed water |
| CN113213433A (en) * | 2021-04-14 | 2021-08-06 | 中国恩菲工程技术有限公司 | Method for directly preparing sulfuric acid for storage battery by using secondary lead smelting flue gas |
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2003
- 2003-05-16 CN CN 03126174 patent/CN1231413C/en not_active Expired - Fee Related
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| CN110124510A (en) * | 2019-01-29 | 2019-08-16 | 浙江天能电源材料有限公司 | A method of utilizing oxygen-enriched side-blowing smelting lead extracting sulfuric acid |
| CN111994878A (en) * | 2020-09-04 | 2020-11-27 | 太和县大华能源科技有限公司 | Method for recycling sulfuric acid from waste acid recovered from lead-acid battery |
| CN112957890A (en) * | 2021-02-09 | 2021-06-15 | 刘乾 | Closed pickling purification process for reducing total emission of dilute sulfuric acid and recovering condensed water |
| CN113213433A (en) * | 2021-04-14 | 2021-08-06 | 中国恩菲工程技术有限公司 | Method for directly preparing sulfuric acid for storage battery by using secondary lead smelting flue gas |
| CN114835089A (en) * | 2022-04-13 | 2022-08-02 | 中石化南京化工研究院有限公司 | Method for preparing sulfuric acid from flue gas containing high-concentration sulfur dioxide |
| CN114835089B (en) * | 2022-04-13 | 2024-01-16 | 中石化南京化工研究院有限公司 | Method for preparing sulfuric acid from flue gas containing high-concentration sulfur dioxide |
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