CN101543724A - Ammonia desulphurization method suitable for sintering flue gas treatment - Google Patents
Ammonia desulphurization method suitable for sintering flue gas treatment Download PDFInfo
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- CN101543724A CN101543724A CN200910029946A CN200910029946A CN101543724A CN 101543724 A CN101543724 A CN 101543724A CN 200910029946 A CN200910029946 A CN 200910029946A CN 200910029946 A CN200910029946 A CN 200910029946A CN 101543724 A CN101543724 A CN 101543724A
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Abstract
The invention relates to an ammonia desulphurization method suitable for sintering flue gas treatment, belonging to the process of desulphurization for atmospheric pollution control in the environmental protection field, in particular to a process of wet ammonia desulphurization of sintering flue gas in the field of steel. The method comprises the following steps: (a) waste ammonia is deliverd to a bubbling-type absorption tower (14) through an ammonia pump (1) and a pipeline system; (b) dedusted sintering flue gas is pressurized and delivered into a concentrating tower (11), the cooled sintering flue gas enters the bubbling-type absorption tower (14) for subsequent desulphurization, ammonium sulphate solution at the bottom of the concentrating tower (11) is redelivered to a spray layer (6) by a circulating pump (5) for atomization and concentration, and high-concentration ammonium sulphate meeting the concentration requirement is discharged through a high-concentration ammonium sulphate pump (8), and (c) sintering flue gas enters the bubbling-type absorption tower (14) through the concentrating tower (11) and is sprayed into absorption solution through a descending pipe (10) for bubbling reaction, desulphurized sintering flue gas enters a defogger (12) through an ascending pipe (11) so that droplets in the desulphurized sintering flue gas are removed, and the desulphurized sintering flue gas is discharged out of a chimney (15).
Description
Technical field
The present invention relates to field of environment protection air contaminant treatment sulfur removal technology technology, relate in particular to the wet ammonia process desulfurizing technology of steel industry sinter fume.
Background technology
The weak point of existing similar technology and existence:
1. limestone-gypsum wet desulphurization technology
Adopt lime stone slurry as desulfurizing agent, the absorption tower form is the spray void tower, by the systemic circulation slush pump doctor solution is delivered to the spraying layer atomizing of tower top, and meeting with flue gas adverse current reacts, and removes SO
2Generate calcium sulfite, the calcium sulfite of generation changes into calcium sulfate in the compressed air oxygen in slurries pond, generates the end product gypsum, and this method is widely used in the means of flue gas desulfurization of power plant at present.Compare sinter fume with power-plant flue gas and be very different, show that mainly load fluctuation reaches the complicated aspect of smoke components greatly.
There is following defective in this method:
1) adopt lime stone as absorbent, desulfurizing byproduct gypsum value is not high, and the operating cost of desulphurization system is too high;
2) adaptability to sinter fume is not high, the SO of sinter fume
2Concentration is compared low with power-plant flue gas, absorbing liquid phase in the spray column is discontinuous phase, and the neutralization reaction severe degree is not high, low SO
2The sinter fume reaction difficulty of concentration strengthens, and desulfuration efficiency reduces greatly;
3) system energy consumption is higher, and absorption liquid is delivered to tower top spraying layer by the recycle slurry liquid pump, and the electric energy of consumption is very big.
2. circulating fluidized bed dry technology
Flue gas enters from the bottom, absorption tower, reacts with the absorbent (calcium hydroxide), circulating ash (returning the absorption tower by the circulation skewed slot) and the water that add after Venturi tube is quickened, and removes the SO in the flue gas
x, HCl, HF, CO
2Deng gas.Absorbent of carrying secretly in the flue gas and circulating ash, when passing through the Venturi tube of bottom, absorption tower, be subjected to the acceleration of air-flow and suspend, form fierce turbulence state, make between particle and the flue gas and have very big relative landing speed, the particle reaction interface constantly rubs, collides renewal, thereby has greatly strengthened gas, conducts heat between solid, mass transfer.In order to reach best reaction temperature,, make flue-gas temperature be cooled to above about 20 ℃ of dew-point temperature simultaneously by in the absorption tower, spraying water.The flue gas that carries a large amount of absorbents, adsorbent and product is advanced into the desulfurization sack cleaner downwards from the absorption tower top side, carries out gas solid separation, and clean flue gas is discharged into atmosphere by chimney.
There is following defective in this method:
1) adopt calcium hydroxide as absorbent, desulfurizing byproduct is the calcium sulfite solid particle, and its utilization rate is very low;
2) if the injection flow rate deficiency can cause the system desulfuration efficiency to descend, spray water excessive then can blockage phenomenon, can cause very serious corrosion phenomenon in the time of seriously, system's operational reliability reduces greatly.
3. ammonia process sprays desulfur technology
Adopt ammoniacal liquor as desulfurizing agent, absorption liquid adopt the mode of spray to enter usually on the absorption tower in and flue gas in SO
2Reaction generates accessory substance ammonium sulfate and ammonium bisulfite, utilizes the method for air aeration that ammonium bisulfite is oxidized to ammonium sulfate in the desulfurizing tower bottom, after ammonium sulfate is discharged through producing ammonia sulfate crystal after filtration, dehydration, evaporation, the drying.
1) SO
2Processes such as absorption, ammonium sulfate concentrate, ammonium bisulfite oxidation concentrate on the absorption tower, make the absorption tower structure become complicated like this, and the body of the tower height is very high, and the tower body cost rises;
2) the absorber portion spray equipment is fragile, and system's operational reliability is not high;
3) circulating pump needs the top spray layer is delivered in the absorption liquid circulation, and system energy consumption is too high, and operating cost is bigger.
Summary of the invention
Technical problem: the operational reliability that exists at above technology is low, system energy consumption is high and problem such as cost of investment height, the present invention proposes a kind of high novel wet ammonia process desulfurizing technology of low energy consumption, reliability of suitable sintering flue gas desulfurization, self-produced or the deposed ammonia desulfurization of buying nearby of this process using iron and steel enterprise, desulfurizing byproduct is for making the ammonium sulfate of agricultural fertilizer, not only realized " treatment of wastes with processes of wastes against one another ", and can also reach the purpose of " turning waste into wealth ".Flow scheme design is optimized, and the desulfuration efficiency height also has certain denitration effect simultaneously.
Technical scheme: the ammonia method desulfurizing method that a kind of suitable sinter fume of the present invention is handled may further comprise the steps:
A). deposed ammonia is by being delivered in the bubbling absorption column for ammonia pump and pipe-line system;
B). the sinter fume after the dedusting is sent in the concentration tower after the blower fan supercharging, the dilute ammonium sulfate solution of being sent here by the tower excavationg pump atomizes through spraying layer, through packing layer and smoke contact heat exchange, utilize the moisture in the heat of vaporization dilute sulfuric acid ammonium in the high temperature sintering flue gas and then reach the purpose that it is concentrated, enter bubbling absorption column behind the flue gas cool-down and carry out follow-up desulfurization; Concentrate back concentration for improving flush distillation, the ammonium sulfate of concentration tower bottom is delivered to the spraying layer atomizing once more by circulating pump and concentrates, and the concentrated sulfuric acid ammonium that reaches concentration requirement is discharged through concentrated sulfuric acid ammonium pump;
C). sinter fume enters bubbling absorption column from concentration tower, is injected into by down-comer and carries out blistering reaction in the absorption liquid, fully contacts in this regional gas, liquid two-phase, and reaction is violent, finally finishes sweetening process; Flue gas after desulfurization enters demister through tedge and removes drop, by smoke stack emission.
Beneficial effect: owing to adopted above technical scheme, this patent to have that sintering flue gas ammonia method desulfurizing technology is simple, system is reliable, desulfuration efficiency is high, and have advantage such as part denitration function.Compare advantage such as this patent combines concentration tower with the JBR tower, it is low to give full play to JBR tower energy consumption, simple to operate with other technologies; The desulfurization product ammonium bisulfite carries out the low concentration oxidation, utilizes the heat of sinter fume that ammonium sulfate is carried out evaporation and concentration again, has both saved the consumption of steam, reaches energy-conservation purpose again.Desulfurizing byproduct ammonium sulfate has higher economic value, and this patent had both been realized environmental benefit, has realized economic benefit again to a certain extent.
Description of drawings
Accompanying drawing is the schematic diagram of this patent sintering flue gas desulfurization system.
Have among the figure: for ammonia pump 1, oxidation fan 2, agitator 3, tower excavationg pump 4, circulating pump 5, spraying layer 6, packing layer 7, concentrated sulfuric acid ammonium pump 8, booster fan 9, down-comer 10, tedge 11, demister 12, concentration tower 13, bubble tower 14, chimney 15.
The specific embodiment
Method of the present invention is specially:
A) deposed ammonia is by being delivered in the bubbling absorption column 14 for ammonia pump 1 and pipe-line system;
B) sinter fume after the dedusting is sent in the concentration tower 11 after blower fan 9 superchargings, the dilute ammonium sulfate solution of being sent here by tower excavationg pump 4 atomizes through spraying layer 6, through packing layer 7 and smoke contact heat exchange, utilize the moisture in the heat of vaporization dilute sulfuric acid ammonium in the high temperature sintering flue gas and then reach the purpose that it is concentrated, enter bubbling absorption column 14 behind the flue gas cool-down and carry out follow-up desulfurization.Can not reach expection concentration for preventing that flush distillation from concentrating, the ammonium sulfate of concentration tower 13 bottoms can be delivered to spraying layer 6 atomizings once more by circulating pump 5 and concentrate.The concentrated sulfuric acid ammonium that reaches concentration requirement is delivered to the subsequent treatment operation through concentrated sulfuric acid ammonium pump 8, finally obtains qualified ammonium sulfate product.
C) sinter fume enters bubbling absorption column 14 from concentration tower 11, is injected into by down-comer 10 and carries out blistering reaction in the absorption liquid, fully contacts in this regional gas, liquid two-phase, and reaction is violent, finally finishes sweetening process.Flue gas after desulfurization enters demister 12 through tedge 11 and removes drop, by chimney 15 dischargings.
D) prevent deposition of solids in the bubbling absorption column 14, agitator 3 is set makes solution mix.Oxidation fan 2 provides sufficient oxidation air that ammonium bisulfite is oxidized to ammonium sulfate to bubbling absorption column 12 bottoms.
Illustrate
Handling object is one of 198m2 sintering machine, exhaust gas volumn 800,000Nm3/h, 130 ℃ of flue-gas temperatures, SO2 concentration 1500mg/Nm3.
Desulfurization process such as accompanying drawing, this height of bubble tower 10.9m, diameter 10m, body is divided into 3 parts of upper, middle and lower by two-layer dividing plate, two-layer clapboard spacing 1.5m, two-layer dividing plate all by 35% percent opening perforate, are connected and installed tedge and down-comer, the tedge number is 10, and the down-comer number is 200.The stock tank section highly is 4.8 meters.The stock tank section is provided with the oxidation air distributor pipe, as air mixing plant and oxidation air ancillary equipment.
The concentration tower height is 8m, and diameter 7.5m, main absorber portion are the PP ripple packing, and packing layer top 2m is provided with one group of spraying layer, and the nozzle number is 9.The bottom is an enriching section, enriching section height 3m.The flue gas heat heating of utilization ammonium sulfate own concentrates the ammonium sulfate of bubble tower, reduces the concentration tower exit gas temperature simultaneously, protection bubble tower material installation safety.
Operating parameter:
Bubble tower: replenish ammoniacal liquor 892.5Kg/h, 50 ℃ of exhanst gas outlet temperature, demister flushing dose 350L/min (flushing at interval), oxidation air quantity: 2600Nm3/h, blast 6500Pa.
Concentration tower: slurries internal circulating load 60m3/h, ammonium sulfate discharge rate 5.5t/h (strength of fluid 15%), 78 ℃ of exhanst gas outlet temperature.
Result: SO2 concentration 100mg/Nm3 in the flue gas after desulfurization, ammonia≤3mg/Nm3 in the tail gas, desulphurization plant total pressure drop 2100pa.
Claims (1)
1. ammonia method desulfurizing method that suitable sinter fume is handled is characterized in that this method may further comprise the steps:
A). deposed ammonia is by being delivered in the bubbling absorption column (14) for ammonia pump (1) and pipe-line system;
B). the sinter fume after the dedusting is sent in the concentration tower (11) after blower fan (9) supercharging, the dilute ammonium sulfate solution of being sent here by tower excavationg pump (4) atomizes through spraying layer (6), through packing layer (7) and smoke contact heat exchange, utilize the moisture in the heat of vaporization dilute sulfuric acid ammonium in the high temperature sintering flue gas and then reach the purpose that it is concentrated, enter bubbling absorption column (14) behind the flue gas cool-down and carry out follow-up desulfurization; Concentrate back concentration for improving flush distillation, the ammonium sulfate of concentration tower (13) bottom is delivered to spraying layer (6) atomizing once more by circulating pump (5) and concentrates, and the concentrated sulfuric acid ammonium that reaches concentration requirement is discharged through concentrated sulfuric acid ammonium pump (8);
C). sinter fume enters bubbling absorption column (14) from concentration tower (11), is injected into by down-comer (10) and carries out blistering reaction in the absorption liquid, fully contacts in this regional gas, liquid two-phase, and reaction is violent, finally finishes sweetening process; Flue gas after desulfurization enters demister (12) through tedge (11) and removes drop, discharges by chimney (15).
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| Application Number | Priority Date | Filing Date | Title |
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| CN200910029946A CN101543724A (en) | 2009-03-25 | 2009-03-25 | Ammonia desulphurization method suitable for sintering flue gas treatment |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955193A (en) * | 2010-09-16 | 2011-01-26 | 上海电力学院 | Method for preparing hydrogen and fertilizer ammonium sulfate by desulfurizing coal-fired waste gas |
| CN101745299B (en) * | 2009-10-23 | 2012-02-29 | 清华大学 | Method and apparatus for capturing CO2 in flue gas by utilizing three-phase circulating fluidized bed and ammonia |
| CN103007753A (en) * | 2012-12-31 | 2013-04-03 | 上海电气石川岛电站环保工程有限公司 | Heterogeneous Fenton reagent and preparation method and application thereof |
| CN103846004A (en) * | 2012-12-03 | 2014-06-11 | 深圳市东圣林环境工程有限公司 | Acidic flue gas purifying method, apparatus and system |
| CN104061580A (en) * | 2014-06-16 | 2014-09-24 | 河南心连心化肥有限公司 | Ammonia desulphurization device for treating flue gas desulphurization and process thereof |
| CN104162357A (en) * | 2014-08-13 | 2014-11-26 | 北京源深节能技术有限责任公司 | Integrated spray flue gas waste heat recovery and denitration device |
| CN106621719A (en) * | 2017-01-19 | 2017-05-10 | 北京中航泰达环保科技股份有限公司 | Fluorine-containing sintering/pellet flue gas treatment method and system |
| CN106693600A (en) * | 2017-03-02 | 2017-05-24 | 合肥杰通环境技术有限公司 | Industrial waste gas treatment device utilizing novel energy source |
| CN112337281A (en) * | 2020-10-26 | 2021-02-09 | 北京首钢股份有限公司 | Sintering flue gas treatment method |
| CN115006967A (en) * | 2022-08-04 | 2022-09-06 | 浙江晨阳新材料有限公司 | Method and device for treating alcohol-containing waste gas in fuel cell production |
-
2009
- 2009-03-25 CN CN200910029946A patent/CN101543724A/en active Pending
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101745299B (en) * | 2009-10-23 | 2012-02-29 | 清华大学 | Method and apparatus for capturing CO2 in flue gas by utilizing three-phase circulating fluidized bed and ammonia |
| CN101955193B (en) * | 2010-09-16 | 2012-06-20 | 上海电力学院 | Method for preparing hydrogen and fertilizer ammonium sulfate by desulfurizing coal-fired waste gas |
| CN101955193A (en) * | 2010-09-16 | 2011-01-26 | 上海电力学院 | Method for preparing hydrogen and fertilizer ammonium sulfate by desulfurizing coal-fired waste gas |
| CN103846004B (en) * | 2012-12-03 | 2016-12-07 | 深圳市东圣林环境工程有限公司 | Acidic flue gas cleaning treatment system |
| CN103846004A (en) * | 2012-12-03 | 2014-06-11 | 深圳市东圣林环境工程有限公司 | Acidic flue gas purifying method, apparatus and system |
| CN103007753A (en) * | 2012-12-31 | 2013-04-03 | 上海电气石川岛电站环保工程有限公司 | Heterogeneous Fenton reagent and preparation method and application thereof |
| CN104061580A (en) * | 2014-06-16 | 2014-09-24 | 河南心连心化肥有限公司 | Ammonia desulphurization device for treating flue gas desulphurization and process thereof |
| CN104061580B (en) * | 2014-06-16 | 2016-11-23 | 河南心连心化肥有限公司 | Process ammonia desulfuration equipment and the technique thereof of flue gas desulfurization band liquid |
| CN104162357A (en) * | 2014-08-13 | 2014-11-26 | 北京源深节能技术有限责任公司 | Integrated spray flue gas waste heat recovery and denitration device |
| CN106621719A (en) * | 2017-01-19 | 2017-05-10 | 北京中航泰达环保科技股份有限公司 | Fluorine-containing sintering/pellet flue gas treatment method and system |
| CN106693600A (en) * | 2017-03-02 | 2017-05-24 | 合肥杰通环境技术有限公司 | Industrial waste gas treatment device utilizing novel energy source |
| CN112337281A (en) * | 2020-10-26 | 2021-02-09 | 北京首钢股份有限公司 | Sintering flue gas treatment method |
| CN115006967A (en) * | 2022-08-04 | 2022-09-06 | 浙江晨阳新材料有限公司 | Method and device for treating alcohol-containing waste gas in fuel cell production |
| CN115006967B (en) * | 2022-08-04 | 2022-11-18 | 浙江晨阳新材料有限公司 | Method and device for treating alcohol-containing waste gas in fuel cell production |
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Open date: 20090930 |