CN101116791A - Resource iron recovery method flue gas desulfurization technics and the integration device thereof - Google Patents
Resource iron recovery method flue gas desulfurization technics and the integration device thereof Download PDFInfo
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- CN101116791A CN101116791A CNA2007100128503A CN200710012850A CN101116791A CN 101116791 A CN101116791 A CN 101116791A CN A2007100128503 A CNA2007100128503 A CN A2007100128503A CN 200710012850 A CN200710012850 A CN 200710012850A CN 101116791 A CN101116791 A CN 101116791A
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Abstract
The invention discloses a resource recycling iron FGD process and attached integration device, in a desulfurizing process, the sulfur dioxide fume in the desulfurizing process is removed in two continuous reacting stages, a mechanically processed iron cutting is used as the desulfurizing agent in the first reacting stage, the primary desulfurizing absorption liquid is clean water, part of sulfur dioxide in the fume is removed to make into iron sulfate which is used as the desulfurizing agent in the second reacting stage, the remainder sulfur dioxide in the fume can be removed to make into polyferric sulfate to be the side-product of desulfurizing process; when the fume temperature is lower than 160 DEG C, the integration device is divided into two sections which can execute the processes of desulfurization and synthesization of polyferric sulfate, when the fume temperature is higher than 160 DEG C, the integration device is divided into three sections which can execute the processes of desulfurization, the synthesization of polyferric sulfate and drying; the invention can recycle the sulfur resource in the fume, the footprint of which is small, the invention can reasonably take use of the waste heat of the fume to save energy consumption.
Description
Technical field
The invention belongs to the flue gases purification field, relate to a kind of resource iron recovery method flue gas desulfurization technics and integrated apparatus thereof.
Background technology
China is poor sulphur country, and existing sulfuric acid resource can not satisfy the needs that national economy increases fast, all needs every year imported sulphur to produce surplus the sulfuric acid 600 ten thousand tons.Administering flue gas SO
2Fully recycle the sulphur resource when polluting, carry out the resource work of sulphur in the flue gas energetically, development sulphur resource technology has great significance.
The flue gas desulfurization technique of China's application at present is based on the limestone/lime wet desulphurization, but by-product gypsum.But according to existing national conditions, China's plaster of paris aboundresources, and also the plastering level of consumption is low, causes the by-product gypsum selling market limited, the resource that still is difficult to accomplish desulfurated plaster at present.Desirable flue gas desulfurization technique is that desulfurizing agent is renewable recycling, and non-secondary pollution can reclaim high-quality, the desulfuration byproduct of wide market application foreground is arranged.
Chinese patent (application number 92111928.3) discloses iron filings and has added water absorb SO in the flue gas in the presence of catalyst
2Make it to generate the process route of ferrous sulfate, and having designed the desulfurization of multifunctional ceiling receiving apparatus, this patent is placed on iron filings on the sieve plate in the desulfuration absorbing tower, can make the desulphurization system resistance bigger, easily stop up, and iron filings and absorption liquid weak point time of contact, the dilute sulfuric acid that desulfurization produces may have little time and the iron filings complete reaction, and long-play can cause the accumulation of dilute sulfuric acid, desulfurization degree is descended, so the long-time running meeting shows the problem of poor operability.
Chinese patent (patent No. 00101556.7) also is to utilize iron filings as desulfurizing agent, at first obtain the ferrous sulfate crystal in the sweetening process, again the ferrous sulfate crystal is oxidized to solid ferric polysulfate in the oxidizing tower of high temperature, use this ferrous oxidation technology and one-step method to produce the resemble process of solid ferric polysulfate, do not need to add other oxidants, but may have the incomplete problem of ferrous ion oxidation.
The desulfurization policy present according to China, some power plant of China have built up unit and smelter and have built up sintering system and all need to set up desulfurizer, but these enterprises do not reserve the desulfurization land used when founding the factory, so have run into the difficulty aspect the place when considering sulfur method.With iron filings is desulfurizing agent, has tangible economic benefit by flue gas desulfurization of iron ion liquid phase catalytic oxidation and by-product polymerizing iron sulfate technology, but a whole set of desulphurization system comprises sweetening process, bodied ferric sulfate is synthetic and dry run, if each unit independently is provided with, floor space is bigger, may be in practice because the place problem limit the application of this method, if with desulfurization, product is synthetic even the obstacle of product drying process aspect realizing in a device with can reducing applications fields undoubtedly.
And, in the bodied ferric sulfate building-up process, need be raw material with ferrous sulfate and sulfuric acid, carry out oxidation according to a certain percentage, hydrolysis and polymerisation finally obtain bodied ferric sulfate, if with iron filings is desulfurizing agent, whole system is not additionally added sulfuric acid, sulfate radical in needed ferrous sulfate of synthesizing polymeric ferric sulfate and the sulfuric acid all will derive from sulfur dioxide in flue gas, so need realize two stages of reaction, a stage desulfurization produces behind the sulfuric acid and iron filings reaction generation ferrous sulfate, produce sulfuric acid after another stage desulfurization, because desulfurization realizes total desulfuration efficiency of realization 90% two stages of reaction, each stage desulfuration efficiency is all relatively low, greatly about about 70%, each stage of reaction equipment volume is all smaller and liquid-gas ratio is also less like this, can reduce equipment investment and operating cost.
Additionally do not add sulfuric acid can be in sweetening process by-product polymerizing iron sulfate, device is realized integrated, can make with iron filings is that the absorption method sulfur removal technology of desulfurization material more has application prospect.
Summary of the invention
The purpose of this invention is to provide a kind of resource iron recovery method flue gas desulfurization technics and integrated apparatus thereof, can make whole desulfurization and by-product polymerizing iron sulfate technical process more reasonable, reduce floor space, reduced equipment investment and operating cost, had very much operability.
Technical scheme of the present invention is as follows:
First stage of reaction of desulfurization is called desulfurization-ferrous sulfate and generates section, and second stage of reaction of desulfurization is called desulfurization-bodied ferric sulfate synthesis stage.
The desulfurization degree of whole technology reaches 90%～98%, and the ratio that desulfurization-ferrous sulfate generates section and desulfurization-sulfur dioxide that the bodied ferric sulfate synthesis stage removes is 1: 0.2～1: 0.45.
It is 30～60 ℃ that desulfurization-ferrous sulfate generates section absorption liquid temperature, Fe
2+Concentration is 0.1～1.5mol/L, absorption liquid pH between 2.5～5.5, liquid-gas ratio 1～20L/Nm
3
Desulfurization-bodied ferric sulfate synthesis stage absorption liquid temperature is 30～60 ℃, and total concentration of iron is 1.0～3.0mol/L, liquid-gas ratio 1～20L/Nm
3
Desulfurization-ferrous sulfate generates section and desulfurization-bodied ferric sulfate synthesis stage absorption tower type is a kind of of packed tower, spray column or sieve-plate tower.
Desulfurization-ferrous sulfate generates the section correspondence and independently is equipped with iron filings in the iron filings reaction tank, and the time of staying of desulfurization absorption liquid in the pond is 5～30min, and the sulfurous acid that produces in this desulfurization is sulfuric acid by air oxidation, and sulfuric acid and iron filings reaction generate ferrous sulfate.
Desulfurization-bodied ferric sulfate synthesis stage is provided with independently circular response pond, the time of staying of desulfurization absorption liquid in the pond is 5～20min, add oxidant at this, the oxidant that adds is one or more combinations of sodium chlorate, potassium chlorate, hydrogen peroxide, and the addition of oxidant need consider that this conversion zone removes SO in the flue gas
2Amount and the amount of the ferrous sulfate that adds of this conversion zone, when using sodium chlorate or potassium chlorate to make oxidant, oxidant and remove SO
2The mol ratio of amount is 1: 3, and the mol ratio of the ferrous sulfate amount that oxidant and this conversion zone add is 1: 6, when using hydrogen peroxide to make oxidant, and oxidant and remove SO
2The amount mol ratio be 1: 1, the mol ratio of the ferrous sulfate amount that oxidant and this conversion zone add is 1: 2.
When the flue gas initial temperature greater than 160 ℃, when utilizing flue gas drying liquid polymeric ferric sulfate product, drying nest independently be provided with or and desulfurizer be integral structure, enter sweetening process after dry back flue-gas temperature is reduced to 100～120 ℃.
Resource reclaims iron processes flue gas desulfurization integrated apparatus, it is characterized in that: when flue-gas temperature during less than 160 ℃, device is divided into two sections, first section is desulfurization-ferrous sulfate generation section, second section is desulfurization-bodied ferric sulfate synthesis stage, and both are connected as a single entity, and middle distribution grid by setting separates, two sections have separately independently reaction tank, and device is called the desulfurization synthetic tower.When flue-gas temperature during greater than 160 ℃, device is divided into three sections, and first section is the spray-drying section, second section is desulfurization-ferrous sulfate generation section, the 3rd section is desulfurization-bodied ferric sulfate synthesis stage, all separates by distribution grid between three sections, and device is called the synthetic drying tower of desulfurization.
The integrated apparatus distributing plate structure is as follows: cover tower diameter fully along tower diameter direction distribution grid, the distribution grid periphery is welded on Ta Bishang, evenly have a plurality of circular holes on the distribution grid as gas passage, each circular hole top is welded with the equal altitudes steel pipe identical with Circularhole diameter, the steel pipe height is by absorption liquid storage setting value decision on the distribution grid, and the liquid on the distribution grid is flowed out by the liquid outlet pipeline on the tower body of distribution grid top.Each steel pipe upper side all has the duct, be used for as the gas vent passage, the block that each steel pipe top respectively has a resistant material to make, and block prevents that with the perforate road coating of steel pipe upper side institute absorption liquid from entering steel duct and flowing into next conversion zone from the duct of being offered.
When flue-gas temperature during greater than 160 ℃, the spray-drying section top of the synthetic drying tower of desulfurization is cylindrical structural, the bottom is a conical structure, flue gas enters from the cylindrical structural bottom, discharge from the distribution grid of cylinder-shaped top, be provided with discharge port in the circular cone bottom, be used for dried solid by-product bodied ferric sulfate is discharged from system.
Effect of the present invention and benefit are:
Sulfur dioxide in flue gas is removed two stages of reaction, though total desulfuration efficiency greater than 90%, the desulfuration efficiency that each stage of reaction requires is all lower, so liquid-gas ratio, absorption tower volume all can reduce, and has reduced equipment investment and operating cost.And when flue-gas temperature is higher, can utilize that heat carries out product drying in the flue gas, conserve energy consumption has reduced operating cost.
In addition, two stages of reaction even the liquid by-product dry run of desulfurization are all finished in an integrated apparatus, the technological process compactness has reduced floor space, is fit to very much the narrow and small old generator set desulfurization improvement project in place.
Description of drawings
Fig. 1 is the process chart of the present invention when using desulfurization synthetic tower integrated apparatus.
Among the figure: 1 desulfurization blower fan; 2 distribution of gas versions; 3 desulfurization-ferrous sulfate generates section; 4 distribution grids; 5 desulfurization-bodied ferric sulfate synthesis stage; 6 demisters; 7 exhaust pass; 8 iron filings reaction tanks; 9 ferrous sulfate solution circulating pumps; 10 iron filings dosing systems; 11 oxidation fans; 12 circular response ponds; 13 bodied ferric sulfate liquid circulating pumps; 14 oxidant storage tanks; 15 oxidant delivery pumps; 16 filter pumps; 17 filter presses; 18 finished fluids storage pond; 19 finished fluid measuring pumps; 20 spray dryers; 21 packing machines.
Fig. 2 is the process chart of the present invention when using the synthetic drying tower integrated apparatus of desulfurization.
Among the figure: 1 desulfurization blower fan; 2 gas distribution grids; 3 desulfurization-ferrous sulfate generates section; 4 ground floor distribution grids; 5 desulfurization-bodied ferric sulfate synthesis stage; 6 demisters; 7 exhaust pass; 8 iron filings reaction tanks; 9 ferrous sulfate solution circulating pumps; 10 iron filings dosing systems; 11 oxidation fans; 12 circular response ponds; 13 bodied ferric sulfate liquid circulating pumps; 14 oxidant storage tanks; 15 oxidant delivery pumps; 16 filter pumps; 17 filter presses; 18 finished fluids storage pond; 19 finished fluid measuring pumps; 20 spray-drying sections; 21 packing machines; 22 second layer distribution grids.
Fig. 3 is a distribution grid vertical view in the integrated apparatus of the present invention.
Among the figure: 1 porous plate; 2 gas outlet tubes; 3 pipe caps.
Fig. 4 is a distribution grid side view in the integrated apparatus of the present invention.
Among the figure: 1 porous plate; 2 gas outlet tubes; 3 pipe caps; Duct on 4 gas outlet tubes.
The specific embodiment
Be described in detail the specific embodiment of the present invention below in conjunction with technical scheme and accompanying drawing.
With Fig. 1 is example, by the desulfurization blower fan that is provided with in the technology 1 flue gas is sent into integrated apparatus, evenly enter desulfurization-ferrous sulfate through gas distribution grid 2 flue gases and generate section 3, at this initial desulfurization absorption liquid is clear water, sulfur dioxide in flue gas is absorbed dissolving and produces acid in tower, in iron filings reaction tank 8, the acid effect that iron filings and desulfurization produce produces ferrous sulfate, subsequently by the catalysed oxidn of iron ion to inferior sulfate radical, the inferior sulfate radical that the sulfur dioxide dissolving produces is oxidized to sulfate radical, thereby the part sulfur dioxide in the flue gas is removed.The absorption liquid of this conversion zone generates constantly circulation between section and the iron filings reaction tank by ferrous sulfate solution circulating pump 9 at desulfurization-ferrous sulfate, when ferrous sulfate concentration reaches certain value in the absorption liquid, absorption liquid is discharged into circular response pond 12 carries out a series of processes such as desulfurization and bodied ferric sulfate be synthetic.This stage of reaction needs iron filings dosing system 10 constantly to replenish iron filings in the iron filings reaction tank, need oxidation fan 11 constantly in the iron filings reaction tank aeration carry out to promote the reaction of iron ion catalytic oxidation inferior sulfate radical.
Flue gas enters desulfurization-bodied ferric sulfate synthesis stage 5 through distribution grid 4 after removing part sulfur dioxide, be desulfurization absorbent at this ferrous sulfate that utilizes desulfurization-ferrous sulfate to generate the section generation, by oxidant delivery pump 15 oxidant in the oxidant storage tank 14 is quantitatively added circular response pond 12, flue gas and the absorption liquid counter current contacting that flows down by tower top, remove another part sulfur dioxide in the flue gas, absorption liquid constantly circulates in desulfurization-bodied ferric sulfate synthesis stage and circular response pond by bodied ferric sulfate liquid circulating pump 13, and a series of oxidations can take place in the sulfuric acid that ferrous sulfate and desulfurization produce, hydrolysis and polymerisation, obtain liquid polymeric ferric sulfate primary product, primary product are filtered by filter pump 16 filter presses 17 and are removed dust and impurity, enter finished fluid storage pond 18 subsequently, the liquid polymeric ferric sulfate byproduct that will reach state quality standard by finished fluid measuring pump 19 is sent into spray dryer 20 dryings, pulverous dry products is discharged from the outlet of spray-drying pars infrasegmentalis, and solid by-product can put in storage or sell after packing machine 21 packings.Flue gas after being purified is removed in the flue gas through demister 6 and is entered fume emission passage 7 behind institute's moisture of be with and afterwards discharge, and controls the certain time of staying of flue gas in integrated apparatus, can obtain the desulfurization degree more than 90%.
By above-mentioned technical process, sulfur in smoke is removed, and obtains the desulfurizing byproduct solid ferric polysulfate.
With Fig. 2 is example, by the desulfurization blower fan that is provided with in the technology 1 flue gas is sent into integrated apparatus, evenly enter spray-drying section 20 through gas distribution grid 2 flue gases, utilize flue gas heat with liquid polymeric ferric sulfate byproduct drying at this, pulverous dry products is discharged from the outlet of spray-drying pars infrasegmentalis, and solid by-product can put in storage or sell after packing machine 21 packings.
Flue gas enters desulfurization-ferrous sulfate through ground floor distribution grid 4 and generates section 3 after the cooling of spray-drying section, at this initial desulfurization absorption liquid is clear water, sulfur dioxide in flue gas is absorbed dissolving and produces acid in tower, in iron filings reaction tank 8, the acid effect that iron filings and desulfurization produce produces iron ion, by the catalysed oxidn of iron ion to inferior sulfate radical, the inferior sulfate radical that the sulfur dioxide dissolving produces is oxidized to sulfate radical subsequently, thereby the part sulfur dioxide in the flue gas is removed.The absorption liquid of this conversion zone generates constantly circulation between section and the iron filings reaction tank by ferrous sulfate solution circulating pump 9 at desulfurization-ferrous sulfate, when ferrous sulfate concentration reaches certain value in the absorption liquid, absorption liquid is discharged into circular response pond 12 carries out a series of processes such as desulfurization and bodied ferric sulfate be synthetic.This stage of reaction needs iron filings dosing system 10 constantly to replenish iron filings in the iron filings reaction tank, need oxidation fan 11 constantly in the iron filings reaction tank aeration carry out to promote the reaction of iron ion catalytic oxidation inferior sulfate radical.
Flue gas enters desulfurization-bodied ferric sulfate synthesis stage 5 by second layer distribution grid 22 after removing part sulfur dioxide, be desulfurization absorbent at this ferrous sulfate that utilizes desulfurization-ferrous sulfate to generate the section generation, by oxidant delivery pump 15 oxidant in the oxidant storage tank 14 is quantitatively added circular response pond 12, flue gas and the absorption liquid counter current contacting that flows down by tower top, remove another part sulfur dioxide in the flue gas, absorption liquid constantly circulates in desulfurization-bodied ferric sulfate synthesis stage and circular response pond by bodied ferric sulfate liquid circulating pump 13, and a series of oxidations can take place in the sulfuric acid that ferrous sulfate and desulfurization produce, hydrolysis and polymerisation, obtain liquid polymeric ferric sulfate primary product, primary product are filtered through filter press 17 by filter pump 16 and are removed dust and impurity, enter finished fluid storage pond 18 subsequently, the liquid polymeric ferric sulfate byproduct that will reach state quality standard by finished fluid measuring pump 19 is sent into spray-drying section drying.Flue gas after being purified is removed in the flue gas through demister 6 and is entered fume emission passage 7 behind institute's moisture of be with and afterwards discharge, and controls the certain time of staying of flue gas in integrated apparatus, can obtain the desulfurization degree more than 90%.
By above-mentioned technical process, sulfur in smoke is removed, and the waste heat in the flue gas is rationally utilized, and obtains the desulfurizing byproduct solid ferric polysulfate.
The coal-fired thermal power boiler of a 75t/h, flue gas flow are 100,000 Nm
3/ h, SO
2Content is 1500mg/Nm
3, flue-gas temperature is 130 ℃, according to technology of the present invention, and when leaving desulfurizing tower, SO in the desulfidation tail gas
2Content 150mg/Nm
3, flue-gas temperature is 50 ℃, desulfuration efficiency 90%.
The integrated apparatus diameter is 6m, and height overall is 30m, and two stages of reaction are filling-material structure, and filler is a cascade ring, RPP material, nominal diameter 50mm
Desulfurizing tower gas is total, and effectively the time of staying is 11s
Two stages of reaction of desulfurizing tower liquid-gas ratio are 5L/Nm
3, each stage absorption liquid flow is 500m
3/ h
The reaction pressure of two stages of reaction of desulfurizing tower, circular response pond and iron filings reaction tank is a normal pressure, and reaction temperature is 50 ℃
Oxidant is a sodium chlorate, and initial concentration solution is 20%, and magnitude of recruitment is 180L/h
The circular response pond absorption liquid time of staying is 6min
The iron filings reaction tank absorption liquid time of staying is 15min
The desulfurization amount mol ratio of desulfurization-ferrous sulfate synthesis stage and desulfurization-bodied ferric sulfate synthesis stage is 1: 0.3
The mol ratio that removes sulfur dioxide in flue gas amount and iron filings addition is 1.3: 1
Remove 972 tons/year of sulfur dioxide in flue gas amounts
654.3 tons/year of iron filings consumptions
338.50 tons/year of the industrial sodium chlorate demands of oxidant 98% purity
Bodied ferric sulfate output: 3443.5 tons/year of 5947.9 tons/year of fluid products or solid products
The coal-fired thermal power boiler of a 220t/h, flue gas flow are 250,000 Nm
3/ h, SO
2Content is 1500mg/Nm
3, flue-gas temperature is 130 ℃, according to technology of the present invention, and when leaving desulfurizing tower, SO in the desulfidation tail gas
2Content 150mg/Nm
3, flue-gas temperature is 50 ℃, desulfuration efficiency 90%.
The integrated apparatus diameter is 8.5m, and height overall is 34m, and two stages of reaction are filling-material structure, and filler is a cascade ring, RPP material, nominal diameter 50mm
Desulfurizing tower gas is total, and effectively the time of staying is 11s
Two stages of reaction of desulfurizing tower liquid-gas ratio are 5L/Nm
3, each stage absorption liquid flow is 1250m
3/ h
The reaction pressure of two stages of reaction of desulfurizing tower, circular response pond and iron filings reaction tank is a normal pressure, and reaction temperature is 50 ℃
Oxidant is a sodium chlorate, and initial concentration solution is 20%, and magnitude of recruitment is 450L/h
The circular response pond absorption liquid time of staying is 6min
The iron filings reaction tank absorption liquid time of staying is 15min
The desulfurization amount mol ratio of desulfurization-ferrous sulfate synthesis stage and desulfurization-bodied ferric sulfate synthesis stage is 1: 0.3
The mol ratio that removes sulfur dioxide in flue gas amount and iron filings addition is 1.3: 1
Remove 2430 tons/year of sulfur dioxide in flue gas amounts
1635.6 tons/year of iron filings consumptions
846.40 tons/year of the industrial sodium chlorate demands of oxidant 98% purity
Bodied ferric sulfate output: 8608.5 tons/year of 14869.2 tons/year of fluid products or solid products.
Claims (12)
1. resource iron recovery method flue gas desulfurization technics, it is characterized in that: sulfur dioxide in flue gas is removed in two continuous stages of reaction, first stage of reaction is a desulfurizing agent with the machining iron filings, initial desulfurization absorption liquid is a clear water, remove part sulfur dioxide generation sulfuric acid in the flue gas, sulfuric acid and iron filings reaction generate ferrous sulfate; The copperas solution that second stage of reaction generates after with first stage of reaction desulfurization is a desulfurizing agent, remove remaining sulfur dioxide in the flue gas, under the oxidant existence condition, inferior sulfate radical that desulfurization produces and ferrous ion are simultaneously oxidized, and ferric sulfate that produces after the oxidation and sulfuric acid are hydrolyzed and polymerisation obtains liquid polymeric ferric sulfate; When flue gas initial temperature during greater than 160 ℃, utilize the liquid polymeric ferric sulfate drying of the heat of flue gas itself with the desulfurization by-product, obtain the solid ferric polysulfate product, when flue gas initial temperature during less than 160 ℃, the liquid polymeric ferric sulfate that obtains obtains solid product by other thermal source dryings.
2. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1 is characterized in that first stage of reaction of desulfurization is called desulfurization-ferrous sulfate generation section, and second stage of reaction of desulfurization is called desulfurization-bodied ferric sulfate synthesis stage.
3. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1, the desulfurization degree that it is characterized in that whole technology reaches 90%～98%, and the ratio that desulfurization-ferrous sulfate generates section and desulfurization-sulfur dioxide that the bodied ferric sulfate synthesis stage removes is 1: 0.2～1: 0.45.
4. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1 is characterized in that it is 30～60 ℃ that desulfurization-ferrous sulfate generates section absorption liquid temperature, Fe
2+Concentration is 0.1～1.5mol/L, absorption liquid pH between 2.5～5.5, liquid-gas ratio 1～20L/Nm
3
5. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1 is characterized in that desulfurization-bodied ferric sulfate synthesis stage absorption liquid temperature is 30～60 ℃, and total concentration of iron is 1.0～3.0mol/L, liquid-gas ratio 1～20L/Nm
3
6. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1 is characterized in that desulfurization-ferrous sulfate generates section and desulfurization-bodied ferric sulfate synthesis stage absorption tower type is a kind of of packed tower, spray column or sieve-plate tower.
7. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1, it is characterized in that desulfurization-ferrous sulfate generates the section correspondence and independently is equipped with iron filings in the iron filings reaction tank, the time of staying of desulfurization absorption liquid in the pond is 5～30min, the sulfurous acid that produces in this desulfurization is sulfuric acid by air oxidation, and sulfuric acid and iron filings reaction generate ferrous sulfate.
8. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1, it is characterized in that desulfurization-bodied ferric sulfate synthesis stage is provided with independently circular response pond, the time of staying of desulfurization absorption liquid in the pond is 5～20min, add oxidant at this, the oxidant that adds is one or more combinations of sodium chlorate, potassium chlorate, hydrogen peroxide, and the addition of oxidant need consider that this conversion zone removes SO in the flue gas
2Amount and the amount of the ferrous sulfate that adds of this conversion zone, when using sodium chlorate or potassium chlorate to make oxidant, oxidant and remove SO
2The mol ratio of amount is 1: 3, and the mol ratio of the ferrous sulfate amount that oxidant and this conversion zone add is 1: 6, when using hydrogen peroxide to make oxidant, and oxidant and remove SO
2The amount mol ratio be 1: 1, the mol ratio of the ferrous sulfate amount that oxidant and this conversion zone add is 1: 2.
9. a kind of resource iron recovery method flue gas desulfurization technics according to claim 1, it is characterized in that working as the flue gas initial temperature greater than 160 ℃, when utilizing flue gas drying liquid polymeric ferric sulfate product, drying nest independently is provided with or is integral structure with desulfurizer, enters sweetening process after dry back flue-gas temperature is reduced to 100～120 ℃.
10. a resource reclaims iron processes flue gas desulfurization integrated apparatus, it is characterized in that: when flue-gas temperature during less than 160 ℃, device is divided into two sections, first section is desulfurization-ferrous sulfate generation section, second section is desulfurization-bodied ferric sulfate synthesis stage, and both are connected as a single entity, and middle distribution grid by setting separates, two sections have separately independently reaction tank, and device is called the desulfurization synthetic tower; When flue-gas temperature during greater than 160 ℃, device is divided into three sections, and first section is the spray-drying section, second section is desulfurization-ferrous sulfate generation section, the 3rd section is desulfurization-bodied ferric sulfate synthesis stage, all separates by distribution grid between three sections, and device is called the synthetic drying tower of desulfurization.
11. a kind of resource according to claim 10 reclaims iron processes flue gas desulfurization integrated apparatus, distributing plate structure is characterised in that: cover tower diameter fully along tower diameter direction distribution grid, the distribution grid periphery is welded on Ta Bishang, evenly have a plurality of circular holes on the distribution grid as gas passage, each circular hole top is welded with the equal altitudes steel pipe identical with Circularhole diameter, the steel pipe height is by absorption liquid storage setting value decision on the distribution grid, and the liquid on the distribution grid is flowed out by the liquid outlet pipeline on the tower body of distribution grid top; Each steel pipe upper side all has the duct, be used for as the gas vent passage, the block that each steel pipe top respectively has a resistant material to make, and block prevents that with the perforate road coating of steel pipe upper side institute absorption liquid from entering steel duct and flowing into next conversion zone from the duct of being offered.
12. a kind of resource according to claim 10 reclaims iron processes flue gas desulfurization integrated apparatus, it is characterized in that when flue-gas temperature during greater than 160 ℃, the spray-drying section top of the synthetic drying tower of desulfurization is cylindrical structural, the bottom is a conical structure, flue gas enters from the cylindrical structural bottom, discharge from the distribution grid of cylinder-shaped top, be provided with discharge port, be used for dried solid by-product bodied ferric sulfate is discharged from system in the circular cone bottom.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102828192A (en) * | 2012-08-29 | 2012-12-19 | 南京化工职业技术学院 | Resourceful treatment method for pickling waste liquor in steel industry |
| CN102989303A (en) * | 2012-09-12 | 2013-03-27 | 河南绿典环保节能科技有限公司 | Smoke wet-type oxidation integral desulfuration denitration and energy using method |
| CN114053854A (en) * | 2021-11-12 | 2022-02-18 | 湖南立泰环境工程有限公司 | VOCs desulfurization and concentration regulation jar |
| CN114471117A (en) * | 2022-01-07 | 2022-05-13 | 浙江浩普环保工程有限公司 | Ammonia-free denitration and desulfurization cooperative system for low-temperature flue gas of kiln |
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2007
- 2007-09-13 CN CNB2007100128503A patent/CN100506352C/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102828192A (en) * | 2012-08-29 | 2012-12-19 | 南京化工职业技术学院 | Resourceful treatment method for pickling waste liquor in steel industry |
| CN102989303A (en) * | 2012-09-12 | 2013-03-27 | 河南绿典环保节能科技有限公司 | Smoke wet-type oxidation integral desulfuration denitration and energy using method |
| CN102989303B (en) * | 2012-09-12 | 2014-10-08 | 河南绿典环保节能科技有限公司 | Smoke wet-type oxidation integral desulfuration denitration and energy using method |
| CN114053854A (en) * | 2021-11-12 | 2022-02-18 | 湖南立泰环境工程有限公司 | VOCs desulfurization and concentration regulation jar |
| CN114471117A (en) * | 2022-01-07 | 2022-05-13 | 浙江浩普环保工程有限公司 | Ammonia-free denitration and desulfurization cooperative system for low-temperature flue gas of kiln |
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