CN102350208B - Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof - Google Patents
Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof Download PDFInfo
- Publication number
- CN102350208B CN102350208B CN 201110180187 CN201110180187A CN102350208B CN 102350208 B CN102350208 B CN 102350208B CN 201110180187 CN201110180187 CN 201110180187 CN 201110180187 A CN201110180187 A CN 201110180187A CN 102350208 B CN102350208 B CN 102350208B
- Authority
- CN
- China
- Prior art keywords
- flue gas
- deionized water
- absorbent
- sodium
- potassium
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a flue gas absorbent which simultaneously has functions of desulphurization and denitration and a preparation method and an application thereof. Calculated according to 1L of deionized water, the flue gas absorbent provided by the invention is composed of 1.66-594g of an oxidizing agent, 3.8-1144g of a buffering agent, 2.7-222g of a stabilizing agent and 1L of deionized water. The preparation method provided by the invention comprises the following steps of: adding the buffering agent into 1L of deionized water, dissolving and uniformly mixing, adding the stabilizing agent, dissolving and uniformly mixing, adding the oxidizing agent, fully dissolving and uniformly mixing to obtain the absorbent. The absorbent provided by the invention and a calcium-based absorbent are simultaneously used so as to realize desulphurization and denitration in a same device, have high removal efficiency, and have less corrosion to the device with no discharge of desulphurization wastewater. In addition, desulphurization byproducts are dry, which is in favor of comprehensive utilization, disposal and stacking.
Description
Technical field
The invention belongs to the gas cleaning process field, relate to a kind of gas cleaning and handle absorbent and application thereof, relate in particular to a kind of flue gas and desulfurizing and denitrifying absorbent and its preparation method and application.
Background technology
At present, fossil fuel such as coal, oil, natural gas etc. are still human main energy sources.As everyone knows, the SO of its combustion process discharging
2And NO
xCan form acid rain and other secondary pollution, badly influence Human's production and life, and caused enormous economic loss, relevant data to show, the annual economic loss that causes because of acid rain of China is about 1,100 hundred million yuans.Therefore, the control that pernicious gases such as sulfur dioxide, nitrogen oxide are polluted and purify most importantly is related to development and national economy, especially sustainable development.
For sulfur dioxide and discharged nitrous oxides control, the means that flue gas desulfurization, equipment for denitrifying flue gas are set respectively in the tail flue gas section of boiler have almost all been adopted at present both at home and abroad.Problems such as this flue gas classification administration way ubiquity floor space is big, equipment investment and operating cost and energy consumption height, flue gas system poor stability have restricted the effective control of coal-fired flue-gas multi-pollutant under low fee condition.Therefore, exploitation has the flue gas and desulfurizing and denitrifying new technology that equipment investment is few, operating cost is low becomes the great demand that domestic and international coal-fired flue-gas pollutant is controlled.
The dry process that with flue gas circulating fluidized bed is representative has small investment, and advantages such as operating cost is low, equipment is simple, water saving come into one's own day by day.The subject matter of the current existence of dry technique be that removal efficiency is relatively low, the absorbent preparation process is loaded down with trivial details and utilization rate low etc.A kind of flue gas desulfuration and denitrification purification method and device are disclosed in the Chinese patent 200310103954.7, it is that spraying into a kind of in circulating fluid bed reactor is the solid highly active absorbent of basic substance with flyash, lime, additive, absorbs sulfur in smoke SO
2With nitrogen oxide NO
xUtilize feed back leg on the dust arrester will be not the highly active absorbent of complete reaction send back to and recycle in the charge pipe, but the preparation process of the highly active absorbent of the method is loaded down with trivial details.Disclose the integrated twin-stage fountain of a kind of flue gas and desulfurizing and denitrifying absorption reactor thermally in the Chinese patent 200720036607.0, comprised cylindrical shell, the one-level absorption reactor thermally, the secondary absorption reactor thermally, one-level absorption reactor thermally smoke inlet, one-level gas distributor, the one-level collecting tank, the one-level demister, one-level spray thrower, secondary absorption reactor thermally exhanst gas outlet, the secondary collecting tank, the secondary gas distributor, the secondary spray thrower, one-level demister and secondary gas distributor are by channel connection.And the flow of flue gas mode upwards become earlier upwards by single, the downward type of flow in back reduced the spatial altitude of flue gas purifying equipment, but the method equipment is loaded down with trivial details, floor space is big, can expect that this method is invested when practical engineering application and operating cost will be very huge.
In addition, desulphurization denitration when realizing under the low expense, the preparation of some desulfurization denitrification agents in the past adopts chloric strong oxidant to make additive more, as Chinese patent 200610051721.0 and Chinese patent 200610012525.2, though removal efficiency is higher, but easily produce equipment corrosion, and bring secondary pollution problems.
Summary of the invention
Purpose of the present invention solves the above-mentioned problems in the prior art exactly, a kind of flue gas and desulfurizing and denitrifying absorbent and its preparation method and application is provided, this absorbent and calcium-base absorbing agent use simultaneously that both can be implemented in the same equipment can desulfurization, purpose that again can denitration, and the removal efficiency height, less to equipment corrosion, no desulphurization denitration discharge of wastewater, and the desulphurization denitration byproduct is dry state, stacks favourable to comprehensive utilization and disposal.
For achieving the above object, technical solution of the present invention is: a kind of flue gas and desulfurizing and denitrifying absorbent, calculate according to the consumption that uses the 1L deionized water, the deionized water of the buffer of its oxidant by 1.66～594g, 3.8～1144g, the stabilizing agent of 2.7～222g and 1L is formed; Described oxidant is purity greater than 98% potassium ferrate K
2FeO
4Perhaps purity is greater than 98% Na2Fe04 Na
2FeO
4Described buffer is borax Na
2B
4O
710H
2O and potassium dihydrogen phosphate KH
2PO
4In at least a; Described stabilizing agent is sodium sulfite Na
2SO
3, sodium metasilicate Na
2SiO
3, sodium peroxydisulfate Na
2S
2O
8, SODIUM PERCARBONATE 2Na
2CO
33H
2O
2, clorox NaClO, sodium chlorite NaClO
2, sodium phosphate Na
3PO
4, potassium chlorate KClO
3, potash K
2CO
3, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2At least a among the O.
The preparation method of flue gas and desulfurizing and denitrifying absorbent described above: it may further comprise the steps:
(1) buffer of the described amount of adding in the deionized water of 1L obtains cushioning liquid behind the dissolving mixing;
(2) add the stabilizing agent of described amount in the above-mentioned cushioning liquid, behind the dissolving mixing, add the oxidant of described amount again, fully dissolve mixing and namely get absorbent.
Flue gas and desulfurizing and denitrifying absorbent described above is containing SO
2And NO
xApplication in the flue gas, it uses in semi-dry flue gas desulfurization device, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2Determine with the concentration of NOx.
The present invention is 7～11 humidification water or directly described flue gas and desulfurizing and denitrifying absorbent is sneaked in the solid phase calcium-base absorbing agent that uses in the semi-dry flue gas desulfurization device by the semidry method humidification process pH value that the described flue gas and desulfurizing and denitrifying absorbent of input is made in the semi-dry flue gas desulfurization device, spray into the pH value again and be 7～11 humidification water, making the interior ambient humidity of desulfurizer is 3～10%, the pH value is 7～11, calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N), when the input flue-gas temperature is 100～150 ℃, in semi-dry flue gas desulfurization device, realize gas, liquid, originally three alternate collisional activations, collisional activation process do not possess solid phase calcium-base absorbing agent and the quick oxidation of absorbent of the present invention of denitration function and absorb SO in the flue gas Gu can make
2And NO
x, it is oxidized to SO
4 2-, NO
3 -And NO
2 -Thereby, remove SO in the flue gas
2And NO
x, realize sulphur, the integrated purpose that removes of nitrogen oxide while in the flue gas.Its main chemical reactions is as follows:
SO
2+H
2O→H
2SO
3 (1)
Ca(OH)
2+H
2SO
3→CaSO
3+2H
2O (2)
CaSO
3+ Fe (VI) (oxidant)+NO → CaSO
4+ Fe (III) (reduzate)+NO
2(3)
NO+Fe (VI) (oxidant) → NO
2+ Fe (III) (reduzate) (4)
3NO
2+H
2O→2HNO
3+NO (5)
NO
2+NO+H
2O→2HNO
2 (6)
Ca(OH)
2+2HNO
3→Ca(NO
3)
2+2H
2O (7)
Ca(OH)
2+2HNO
2→Ca(NO
2)
2+2H
2O (8)
Flue gas and desulfurizing and denitrifying absorbent of the present invention can be under the prerequisite of not setting up new commercial plant, when using simultaneously with common calcium-base absorbing agent, it not only self has good denitration function, and when strengthening common calcium-base absorbing agent desulfuration efficiency, also make it have the denitration function, realized the modification of common calcium-base absorbing agent, made it have oxidation susceptibility.The present invention has the removal efficiency height, and preparation temperature is low, and it is easy, easy to use to prepare, the utilization rate height, floor space is little, and expense is low, be beneficial to old power plant and transform, can not produce secondary pollution and other side effect, desulfurization ash in the flue gas processing procedure and be dry state, stack favourable to comprehensive utilization and disposal.Simultaneously heavy metals such as Hg, As are also had higher removal efficiency, its investment and operating cost are low, stable, easy to utilize.Test shows, the present invention be used in flue gas circulating fluidized bed in, be 15～300m at flue gas flow
3/ h, the particle circulating ratio is 0.31kg/m
2S, gas residence time is 1.4～4.8 seconds, humidity is 3～10%, the pH value is 7～11, entrance flue gas temperature is that 100～150 ℃, calcium sulphur nitrogen are under 0.6～1.8 the condition than Ca/ (S+N), the removal efficiency of sulfur dioxide is more than 98%, removal of nitrogen oxide efficient is more than 72%, the absorbent utilization rate reaches more than 96%, its removal efficiency height.In addition, the present invention is less to the corrosivity of equipment such as the flue in desulfurizer and downstream thereof, chimney, can not adopt smoke re-heater, can not carry out preservative treatment to existing chimney; No desulfurization wastewater discharging.The present invention can carry out flue gas desulfurization and denitrification at same set of equipment, overcome that existing flue gas desulfurization and denitrification adopts the equipment investment and the operating cost height that install desulfurizer and denitrification apparatus respectively additional and exist, occupation of land face is big and shortcoming such as flue gas system complexity, also solved the problem that the desulfurization ash that produces in the prior art is difficult to utilize.
The specific embodiment
Be further described this law is bright below in conjunction with specific embodiment.
Embodiment 1: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% Na2Fe04 Na by the purity of 1.66g
2FeO
4, 300g borax Na
2B
4O
710H
2The sodium sulfite Na of O, 2.7g
2SO
3Form with the deionized water of 1L.The borax Na that in the deionized water of 1L, adds described amount
2B
4O
710H
2O obtains cushioning liquid behind the dissolving mixing; The sodium sulfite Na that in cushioning liquid, adds described amount
2SO
3, behind the dissolving mixing, the purity that adds described amount again is greater than 98% Na2Fe04 Na
2FeO
4, fully dissolve mixing and namely get absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 150m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 72%.
Embodiment 2: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% potassium ferrate K by the purity of 594g
2FeO
4, 3.8g potassium dihydrogen phosphate KH
2PO
4, 2.7g sodium metasilicate Na
2SiO
3Form with the deionized water of 1L.The potassium dihydrogen phosphate KH that in the deionized water of 1L, adds described amount
2PO
4, obtain cushioning liquid behind the dissolving mixing; The sodium metasilicate Na that in cushioning liquid, adds described amount
2SiO
3Behind the dissolving mixing, the purity that adds described amount again is greater than 98% potassium ferrate K
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 220m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 73%.
Embodiment 3: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% Na2Fe04 Na by the purity of 332g
2FeO
4, 1144g potassium dihydrogen phosphate KH
2PO
4, 222g sodium peroxydisulfate Na
2S
2O
8Form with the deionized water of 1L.The potassium dihydrogen phosphate KH that in the deionized water of 1L, adds described amount
2PO
4, obtain cushioning liquid behind the dissolving mixing; The sodium peroxydisulfate Na that in cushioning liquid, adds described amount
2S
2O
8Behind the dissolving mixing, the purity that adds described amount again is greater than 98% Na2Fe04 Na
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.When SO2 concentration at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 200m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 75%.
Embodiment 4: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% potassium ferrate K by the purity of 198g
2FeO
4, 500g borax Na
2B
4O
710H
2The SODIUM PERCARBONATE 2Na of O, 50g
2CO
33H
2O
2Form with the deionized water of 1L.The borax Na that in the deionized water of 1L, adds described amount
2B
4O
710H
2O obtains cushioning liquid behind the dissolving mixing; The SODIUM PERCARBONATE 2Na that in cushioning liquid, adds described amount
2CO
33H
2O
2Behind the dissolving mixing, the purity that adds described amount again is greater than 98% potassium ferrate K
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 150m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 75%.
Embodiment 5: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% potassium ferrate K by the purity of 5.94g
2FeO
4, 3.80g borax Na
2B
4O
710H
2The clorox NaClO of O, 7.44g and the deionized water of 1L are formed.The borax Na that in the deionized water of 1L, adds described amount
2B
4O
710H
2O obtains cushioning liquid behind the dissolving mixing; Add the clorox NaClO dissolving mixing of described amount in cushioning liquid after, the purity that adds described amount again is greater than 98% potassium ferrate K
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 39.24m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach more than 72%.
Embodiment 6: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% Na2Fe04 Na by the purity of 33.2g
2FeO
4, 3.8g potassium dihydrogen phosphate KH
2PO
4, 13.75g borax Na
2B
4O
710H
2The sodium chlorite NaClO of O, 18.1g
2Form with the deionized water of 1L.The potassium dihydrogen phosphate KH that in the deionized water of 1L, adds described amount
2PO
4Borax Na with described amount
2B
4O
710H
2The mixture of O obtains cushioning liquid behind the dissolving mixing; The sodium chlorite NaClO that in cushioning liquid, adds described amount
2Behind the dissolving mixing, the purity that adds described amount again is greater than 98% Na2Fe04 Na
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 20m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach more than 75%.
Embodiment 7: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% Na2Fe04 Na by the purity of 500g
2FeO
4, 100g potassium dihydrogen phosphate KH
2PO
4, 30g sodium phosphate Na
3PO
4Form with the deionized water of 1L.The potassium dihydrogen phosphate KH that in the deionized water of 1L, adds described amount
2PO
4, obtain cushioning liquid behind the dissolving mixing; The sodium phosphate Na that in cushioning liquid, adds described amount
3PO
4Behind the dissolving mixing, the purity that adds described amount again is greater than 98% Na2Fe04 Na
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 200m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 75%.
Embodiment 8: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% potassium ferrate K by the purity of 99g
2FeO
4, 38g borax Na
2B
4O
710H
2The potassium chlorate KClO of O, 23g
3, potash K
2CO
3, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2The deionized water of a kind of and 1L among the O is formed.The borax Na that in the deionized water of 1L, adds described amount
2B
4O
710H
2O obtains cushioning liquid behind the dissolving mixing; The potassium chlorate KClO that in cushioning liquid, adds described amount
3, potash K
2CO
3,, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2Behind a kind of dissolving mixing among the O, the purity that adds described amount again is greater than 98% potassium ferrate K
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 39.24m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach more than 72%.
Embodiment 9: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% Na2Fe04 Na by the purity of 50g
2FeO
4, 200g potassium dihydrogen phosphate KH
2PO
4, 80g sodium sulfite Na
2SO
3, sodium metasilicate Na
2SiO
3, sodium peroxydisulfate Na
2S
2O
8, SODIUM PERCARBONATE 2Na
2CO
33H
2O
2, clorox NaClO, sodium chlorite NaClO
2, sodium phosphate Na
3PO
4, potassium chlorate KClO
3, potash K
2CO
3,, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2Any two combination among the O and the deionized water of 1L are formed.The potassium dihydrogen phosphate KH that in the deionized water of 1L, adds described amount
2PO
4, obtain cushioning liquid behind the dissolving mixing; The sodium sulfite Na that in cushioning liquid, adds described amount
2SO
3, sodium metasilicate Na
2SiO
3, sodium peroxydisulfate Na
2S
2O
8, SODIUM PERCARBONATE 2Na
2CO
33H
2O
2, clorox NaClO, sodium chlorite NaClO
2, sodium phosphate Na
3PO
4, potassium chlorate KClO
3, potash K
2CO
3,, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2Behind any two combination dissolving mixing among the O, the purity that adds described amount again is greater than 98% Na2Fe04 Na
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 300m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 80%.
Embodiment 10: the desulphurization denitration absorbent of present embodiment, calculate according to the consumption that uses the 1L deionized water, and it is greater than 98% potassium ferrate K by the purity of 150g
2FeO
4, 400g borax Na
2B
4O
710H
2The sodium sulfite Na of O, 200g
2SO
3, sodium metasilicate Na
2SiO
3, sodium peroxydisulfate Na
2S
2O
8, SODIUM PERCARBONATE 2Na
2CO
33H
2O
2, clorox NaClO, sodium chlorite NaClO
2, sodium phosphate Na
3PO
4, potassium chlorate KClO
3, potash K
2CO
3, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H5Na
3O
72H
2Any three or any four or any five or any six or any seven or any eight or any nine or any ten among the O or any 11 or any 12 or any 13 or any 14 or 15 s' combination and the deionized water of 1L are formed.The borax Na that in the deionized water of 1L, adds described amount
2B
4O
710H
2O obtains cushioning liquid behind the dissolving mixing; The sodium sulfite Na that in cushioning liquid, adds described amount
2SO
3, sodium metasilicate Na
2SiO
3, sodium peroxydisulfate Na
2S
2O
8, SODIUM PERCARBONATE 2Na
2CO
33H
2O
2, clorox NaClO, sodium chlorite NaClO
2, sodium phosphate Na
3PO
4, potassium chlorate KClO
3, potash K
2CO
3, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2Behind any three or any four or any five or any six or any seven or any eight or any nine or any ten among the O or any 11 or any 12 or any 13 or any 14 or 15 s' the combination dissolving mixing, the purity that adds described amount again is greater than 98% potassium ferrate K
2FeO
4Fully the dissolving mixing namely gets absorbent.The desulphurization denitration absorbent uses in semi-dry flue gas desulfurization device the time described above, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).The consumption of described absorbent is by SO in exhaust gas volumn and the flue gas
2And NO
xConcentration determine.Work as SO
2Concentration is at 1500～2000mg/m
3, NO concentration is at 500～1000mg/m
3, flue gas flow is 225m
3During/h, its desulfuration efficiency can reach 98%, and denitration efficiency can reach 75%.
Claims (8)
1. flue gas and desulfurizing and denitrifying absorbent is characterized in that: calculate according to the consumption that uses the 1L deionized water, the deionized water of the buffer of its oxidant by 1.66～594g, 3.8～1144g, the stabilizing agent of 2.7～222g and 1L is formed; Described oxidant is purity greater than 98% potassium ferrate K
2FeO
4Perhaps purity is greater than 98% Na2Fe04 Na
2FeO
4Described buffer is borax Na
2B
4O
710H
2O and potassium dihydrogen phosphate KH
2PO
4In at least a; Described stabilizing agent is sodium sulfite Na
2SO
3, sodium metasilicate Na
2SiO
3, sodium peroxydisulfate Na
2S
2O
8, SODIUM PERCARBONATE 2Na
2CO
33H
2O
2, clorox NaClO, sodium chlorite NaClO
2, sodium phosphate Na
3PO
4, potassium chlorate KClO
3, potash K
2CO
3, potassium metaperiodate KIO
4, potassium peroxydisulfate K
2S
2O
8, ammonium persulfate (NH
4)
2S
2O
8, calcium hypochlorite Ca (ClO)
2, sodium acetate CH
3COONa and trisodium citrate C
6H
5Na
3O
72H
2At least a among the O.
2. flue gas and desulfurizing and denitrifying absorbent according to claim 1 is characterized in that: calculate according to the consumption that uses the 1L deionized water, it is greater than 98% Na2Fe04 Na by the purity of 332g
2FeO
4, 1144g potassium dihydrogen phosphate KH
2PO
4, 222g sodium peroxydisulfate Na
2S
2O
8Form with the deionized water of 1L.
3. flue gas and desulfurizing and denitrifying absorbent according to claim 1 is characterized in that: calculate according to the consumption that uses the 1L deionized water, it is greater than 98% potassium ferrate K by the purity of 198g
2FeO
4, 500g borax Na
2B
4O
710H
2The SODIUM PERCARBONATE 2Na of O, 50g
2CO
33H
2O
2Form with the deionized water of 1L.
4. flue gas and desulfurizing and denitrifying absorbent according to claim 1 is characterized in that: calculate according to the consumption that uses the 1L deionized water, it is greater than 98% potassium ferrate K by the purity of 5.94g
2FeO
4, 3.80g borax Na
2B
4O
710H
2The clorox NaClO of O, 7.44g and the deionized water of 1L are formed.
5. flue gas and desulfurizing and denitrifying absorbent according to claim 1 is characterized in that: calculate according to the consumption that uses the 1L deionized water, it is greater than 98% Na2Fe04 Na by the purity of 33.2g
2FeO
4, 3.8g potassium dihydrogen phosphate KH
2PO
4, 13.75g borax Na
2B
4O
710H
2The sodium chlorite NaClO of O, 18.1g
2Form with the deionized water of 1L.
6. flue gas and desulfurizing and denitrifying absorbent according to claim 1 is characterized in that: calculate according to the consumption that uses the 1L deionized water, it is greater than 98% Na2Fe04 Na by the purity of 500g
2FeO
4, 100g potassium dihydrogen phosphate KH
2PO
4, 30g sodium phosphate Na
3PO
4Form with the deionized water of 1L.
7. the preparation method of each described flue gas and desulfurizing and denitrifying absorbent of claim 1-6 is characterized in that it may further comprise the steps:
(1) buffer of the described amount of adding in the deionized water of 1L obtains cushioning liquid behind the dissolving mixing;
(2) add the stabilizing agent of described amount in the above-mentioned cushioning liquid, behind the dissolving mixing, add the oxidant of described amount again, fully dissolve mixing and namely get absorbent.
8. each described flue gas and desulfurizing and denitrifying absorbent of claim 1-6 is containing SO
2And NO
xApplication in the flue gas is characterized in that, it uses in semi-dry flue gas desulfurization device, and it requires in the desulfurizer, and ambient humidity is 3～10%, the pH value is 7～11, and entrance flue gas temperature is 100～150 ℃, and calcium sulphur nitrogen is 0.6～2.8 than Ca/ (S+N).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110180187 CN102350208B (en) | 2011-06-30 | 2011-06-30 | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110180187 CN102350208B (en) | 2011-06-30 | 2011-06-30 | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102350208A CN102350208A (en) | 2012-02-15 |
| CN102350208B true CN102350208B (en) | 2013-09-04 |
Family
ID=45573916
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110180187 Expired - Fee Related CN102350208B (en) | 2011-06-30 | 2011-06-30 | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102350208B (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103386250A (en) * | 2013-07-30 | 2013-11-13 | 福建龙净脱硫脱硝工程有限公司 | Dry desulphurization method |
| CN103752161B (en) * | 2013-12-20 | 2016-02-03 | 华北电力大学（保定） | There is wet method compound additive and the application process thereof of desulfuration demercuration effect simultaneously |
| CN106268293A (en) * | 2015-05-14 | 2017-01-04 | 王立群 | A kind of wet desulphurization denitration synergist for coal-burning boiler |
| CN106178862A (en) * | 2016-07-25 | 2016-12-07 | 合肥天翔环境工程有限公司 | Sintering smoke denitrifier and preparation method thereof |
| CN106178865B (en) * | 2016-09-14 | 2019-02-01 | 湖南省小尹无忌环境能源科技开发有限公司 | Industrial furnace smoke heavy metal and the purification of fluorine chlorine sulphur nitre and resource utilization method |
| CN106823747A (en) * | 2017-03-08 | 2017-06-13 | 湖南云平环保科技有限公司 | Calcium and magnesium base desulphurization denitration absorbent |
| CN107297144B (en) * | 2017-08-17 | 2020-06-12 | 山东大明消毒科技有限公司 | Desulfurization and denitrification agent and preparation method and application thereof |
| CN108211754A (en) * | 2018-02-02 | 2018-06-29 | 环境保护部华南环境科学研究所 | A kind of flue gas pollutant absorbent and its application |
| CN108654311A (en) * | 2018-04-26 | 2018-10-16 | 德施普科技发展温州有限公司 | A kind of high-efficiency desulfurization denitration absorbent and preparation method thereof |
| CN113731167B (en) * | 2021-09-02 | 2023-03-21 | 昆明理工大学 | Preparation method of modified carbide slag, product and application thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1539546A (en) * | 2003-11-02 | 2004-10-27 | 华北电力大学 | Method and equipment of desulfurization and denitrogenation for purifying flue gas |
| US20100139345A1 (en) * | 2005-09-15 | 2010-06-10 | Burnham Jeffrey C | Organic fertilizer made by alkaline conversion process |
| CN102068895A (en) * | 2010-12-15 | 2011-05-25 | 中山大学 | Method for treating odorous gas by utilizing solution of hexavalent ferric salt |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2977759B2 (en) * | 1996-03-01 | 1999-11-15 | 川崎重工業株式会社 | Exhaust gas dry treatment method and apparatus |
-
2011
- 2011-06-30 CN CN 201110180187 patent/CN102350208B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1539546A (en) * | 2003-11-02 | 2004-10-27 | 华北电力大学 | Method and equipment of desulfurization and denitrogenation for purifying flue gas |
| US20100139345A1 (en) * | 2005-09-15 | 2010-06-10 | Burnham Jeffrey C | Organic fertilizer made by alkaline conversion process |
| CN102068895A (en) * | 2010-12-15 | 2011-05-25 | 中山大学 | Method for treating odorous gas by utilizing solution of hexavalent ferric salt |
Non-Patent Citations (2)
| Title |
|---|
| JP特开平9-234333 1997.09.09 |
| 庄玉贵，颜文强，许冬梅等.高铁酸盐稳定剂的筛选.《福建师范大学福清分校学报》.2006,(第73期),第40～43页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102350208A (en) | 2012-02-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102350208B (en) | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof | |
| CN103480251B (en) | System and method for performing desulfurization, denitration and demercuration to flue gas simultaneously | |
| CN101745305A (en) | Method for removing various gaseous pollutants from smoke gas | |
| CN102091517A (en) | Integrated absorption solution for simultaneous desulfuration, denitration and mercury removal and preparation method and application thereof | |
| CN110787606B (en) | Denitration and demercuration integrated device and method for sintering flue gas circulating fluidized bed desulfurization | |
| CN103170228B (en) | A kind of denitrating flue gas mixed solution and application process thereof | |
| CN102989282A (en) | Method and device for collaborative removal of mercury in flue gas | |
| CN104906937A (en) | Flue gas desulfurization and denitrification device and method of coal fired boiler | |
| CN101632897B (en) | Method for simultaneously removing sulfur oxides and nitric oxides in flue gas | |
| CN203591690U (en) | System for removing sulfur, nitrate and mercury in flue gas at same time | |
| CN102068888A (en) | Method for simultaneously desulfurizing and denitrating flue gas by wet method | |
| CN101590369B (en) | Mercury removal process based on lime-gypsum method desulphurization system and mercury removal absorption liquid | |
| CN102658021A (en) | Advanced technology and device for integrating oxidation catalysis, desulfurization and denitrification | |
| CN105107373B (en) | Composite desulfurizer for oxidizing elemental mercury and removing HCl and preparation method thereof | |
| CN104941410A (en) | Flue gas desulfurization and denitrification integrated method and device based on two-step oxidation process of active molecules O3 at low temperature | |
| CN104524935A (en) | Single-tower type double-circulation sprinkling composite absorption device and method | |
| CN103801177B (en) | A kind of flue gas processing method of calcium magnesium processes simultaneous SO_2 and NO removal demercuration | |
| CN108043210A (en) | A kind of desulfurization of coke oven flue gas and dedusting denitrification integral system | |
| CN104801160A (en) | Method for reducing nitrogen oxides in flue gas of medium and small sized industrial coal burning boiler through combination with wet-method sulfur removing technology | |
| CN110064293B (en) | Method for desulfurization, denitrification and demercuration of flue gas | |
| CN102188889B (en) | Device and method for combined removal of sulphur dioxide (SO2), nitrogen oxide (NOX) and mercury from fume | |
| CN102847430B (en) | System and technology for cleaning flue gas | |
| CN204247052U (en) | Single tower type double-cycle spray composite absorption device | |
| CN202683045U (en) | High-level oxidizing, catalyzing, desulfurizing and denitrating integral device | |
| CN102728215B (en) | Composition and method for removing nitrogen oxides in desulfurizing tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130904 Termination date: 20160630 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |