CN101081351A - Process for disposing SOx in discharge gas - Google Patents
Process for disposing SOx in discharge gas Download PDFInfo
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- CN101081351A CN101081351A CN 200610083432 CN200610083432A CN101081351A CN 101081351 A CN101081351 A CN 101081351A CN 200610083432 CN200610083432 CN 200610083432 CN 200610083432 A CN200610083432 A CN 200610083432A CN 101081351 A CN101081351 A CN 101081351A
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Abstract
The method of eliminating SOx from waste gas is to make waste gas containing SOx contact to absorption liquid, which contains ammonium compound and/or ammonia, and aluminum containing compound and/or silicon containing compound in the amount of 0.5-150 g/L. The method of eliminating SOx from waste gas has lowered water evaporating amount, lowered water consumption and power consumption, and no production of solid waste.
Description
Technical field
The present invention relates to SO in a kind of processing waste gas
xMethod.
Background technology
SO in the waste gas
xBe the main matter that forms acid rain, each state has all formulated strict emission control standards and has limited its discharging, and GB16297-1996 stipulates SO in China's waste gas
2Maximal emission: existing pollution sources are 700mg/Nm
3, new pollution sources are 550mg/Nm
3Generations such as coal-burning boiler, thermal power plant and oil plant FCC regeneration are a large amount of contains SO
xWaste gas, different according to the source, its concentration can reach 1000～15000mg/Nm
3, be much higher than national standard.
Remove SO in the waste gas at present
xTechnology have multiplely, absorption process is wherein a kind of important technology, has obtained extensive use.
FI851623 discloses powder calcium hydroxide or the magnesium hydroxide of a kind of utilization after by water or steam activation and has absorbed SO
XMethod.NL851622 discloses under the condition that sprays into water or water vapour and has utilized carbonate to remove SO
XMethod.
US799052 has announced a kind of method with sulfur dioxide in thiosulfate and the polythionate aqueous buffer solution absorption waste gas, and the concentrated solution after the absorption forms sulphur with hydrogen sulfide regeneration.
CN85103518 discloses a kind of method that removes sulfur dioxide in flue gas, comprises with basic aluminium sulphate solution absorbing sulfur in smoke, and the solution after absorbing with Steam Heating is deviate from pure sulfur dioxide gas, and the solution after the desorb recycles.
DK5528/85, DK5487/86 have announced the method that absorbs sulfur dioxide in the waste gas with the fresh alkali lye of calcium, magnesium, basic metal oxide or hydroxide.
CN92111928 has proposed to add desulfurization new method and the device that water absorbs sulfur in smoke with waste iron filing, and this method needs to promote the catalyst of sulfur dioxide absorption.
CN97105110 has announced high efficiency flue gas desulfurization technology in, comprises desulfurization and desulfurizing agent regeneration two parts.This technology at first absorbs sulfur in smoke with NaOH and generates solution of sodium bisulfite, and then regenerates with calcium hydroxide.
CN96106432 has proposed a kind of fume desulphurization method, with the ferrous sulfate is absorbent, with hydrogen peroxide, chlorine dioxide or potassium chlorate (sodium) is oxidant, with iron or nitrogen oxide is catalyst, with NaOH is conditioning agent, generate bodied ferric sulfate with the reaction of flue gas sulphur oxide under certain condition.
CN94102903 discloses a kind of method that absorbs sulfur oxide and produce ammonium sulfate simultaneously, and this method comprises the SO that contains with heat
xWaste gas in prepurifier, contact with the saturated ammonium sulfate aqueous solution, the solution after the contact enters in the prepurifier storage tank, the waste gas after the preliminary clearning contacts with dilute ammonium sulfate solution in absorber, removes SO wherein
x, purifying qualified waste gas and discharge, the dilute sulfuric acid ammonia solution after the contact enters in the absorber storage tank.In the prepurifier storage tank saturated ammonium sulfate aqueous solution that contains the suspension ammonium sulfate crystallization, a part is as the contact liquid of prepurifier, a part obtains ammonium sulfate crystallization by clasfficiator, and the loss of solution is replenished by introducing dilute ammonium sulfate solution in the prepurifier storage tank.Dilute ammonium sulfate solution is stored in the absorber storage tank, and to bubbling air wherein, is ammonium sulfate with absorbing the sulfite oxidation that forms; A dilute ammonium sulfate solution part is used as the absorption liquid of absorber, and a part is as the additional liquid of prepurifier; The loss that interpolation supplementing water and ammonia replenish dilute ammonium sulfate solution in the absorber simultaneously.The solubility of product ammonium sulfate in water of this method is bigger, needs a large amount of moisture of evaporation can make the saturated generation ammonium sulfate crystallization of solution, and this makes water consumption and energy consumption big, and the volatilization and losing easily of the ammonia in the absorption liquid.
CN200510023222 discloses a kind of method and apparatus that sulfur in smoke is produced the sulphur ammonium that reclaims.It is 110～180 ℃ of boiler smokes with weight concentration is that rare sulphur aqueous ammonium of 3～30% contacts in desulfurizing tower that this method comprises temperature, temperature is reduced to 50～100 ℃, flue gas decreasing temperature and increasing humidity in desulfurizing tower contacts with the absorption liquid that contains rare sulphur ammonium and ammonia more subsequently, removes SO wherein
xThe absorption liquid that contains rare sulphur ammonium and ammonia sprays into from the top of desulfurizing tower, absorbs SO
xAfter, the air of going into the tower pucking contacts, and is ammonium sulfate with absorbing the sulfite oxidation that forms.Absorption liquid after the oxidation is partly refluxed to the absorption tower and concentrates to obtain the sulphur crystalline ammonium.This method also exists a large amount of moisture of needs evaporation to make the problem of the saturated generation ammonium sulfate crystallization of ammonium sulfate.
Summary of the invention
The technical problem to be solved in the present invention is to overcome the existing absorption liquid that contains ammonia nitrogen of using to handle SO in the waste gas
xThe water evaporation quantity that exists in the technology is big, water consumes and the high shortcoming of energy consumption, and the absorption liquid that provides a kind of new usefulness to contain ammonia nitrogen is handled SO in the waste gas
xMethod.
SO in the processing waste gas provided by the invention
xMethod, comprise and will contain SO
xWaste gas contact with the absorption liquid that contains ammonium-containing compound and/or ammonia, also contain aluminum contained compound and/or silicon-containing compound in the wherein said absorption liquid, in oxide, the content of aluminum contained compound and/or silicon-containing compound is 0.5g/L to 150g/L in the described absorption liquid.
Utilize method of the present invention, can reduce the water evaporation quantity that ammonium sulfate is separated out in the absorption liquid, thereby reduce water consumption and energy consumption, particularly when utilizing the synthetic nitrogen-containing wastewater that produces of molecular sieve as absorption liquid, can either using water wisely, can handle nitrogen-containing wastewater again.For example, be 90g/L with ammonium sulfate concentrations, with Al
2O
3Meter sodium metaaluminate concentration is 9g/L, and the pH value is 13 absorption liquid, is 300Nm at the volume ratio of gas and absorption liquid
3/ m
3, the gas superficial linear velocity in a column is 9000Nm
3/ (m
2H) treatment S O under the condition
xContent is 2158mg/Nm
3The FCC regenerated flue gas, there is precipitation to separate out when ammonium sulfate concentrations is 212g/L in the absorption liquid, ammonium sulfate content in the precipitation is 73.1%, and with sulfate of ammoniac solution as absorption liquid, there is ammonium sulfate to separate out when ammonium sulfate concentrations is for 574g/L in the absorption liquid, evaporation capacity of moisture content has reduced 30% like this, the also corresponding reduction of the consumption of water and energy consumption.
Description of drawings
Fig. 1 is the FB(flow block) of a kind of specific embodiment of the present invention.
Fig. 2 is the FB(flow block) of the another kind of specific embodiment of the present invention.
The specific embodiment
Can contain a kind of of aluminum contained compound or silicon-containing compound in the absorption liquid of the present invention.When containing aluminum contained compound, in aluminium oxide, the content of aluminum contained compound is 0.5g/L to 100g/L in the described absorption liquid, is preferably 0.5g/L to 10g/L.When containing silicon-containing compound, in silica, the content of silicon-containing compound is 0.5g/L to 120g/L in the described absorption liquid, is preferably 0.5g/L to 15g/L.
Also can contain aluminum contained compound and silicon-containing compound simultaneously in the absorption liquid of the present invention, in oxide, the content of silicon-containing compound is 0.1g/L to 100g/L in the described absorption liquid, is preferably 0.1g/L to 10g/L; The content of aluminum contained compound is 0.1g/L to 50g/L, is preferably 0.1g/L to 10g/L.
Absorption liquid of the present invention can be easily by existing method preparation, for example, when containing ammonium-containing compound, ammonia, aluminum contained compound, silicon-containing compound simultaneously in the absorption liquid, can take following method preparation: in water, add ammonium-containing compound, add silicon-containing compound then, add aluminum contained compound again, add ammonia at last; When not containing wherein any compound in the absorption liquid, save corresponding preparation process; Wherein the amount of each component should make that each constituent content satisfies requirement of the present invention in the absorption liquid that finally obtains.
Aluminum contained compound is selected from one or more in aluminium oxide, aluminium colloidal sol, hydrated alumina or the water-soluble aluminium salt in the absorption liquid of the present invention, described aluminum contained compound exists with the form of ionic condition, colloidal sol in absorption liquid, and preferred aluminum contained compound is one or more in sodium metaaluminate, aluminum sulfate, aluminum nitrate, the aluminium chloride.
Silicon-containing compound is selected from one or more in water-soluble silicate, silicon dioxide gel or other silicon oxide compound in the absorption liquid of the present invention, preferred sodium metasilicate, Ludox or the mixture of the two.
When the aluminum contained compound in the absorption liquid and/or silicon-containing compound when being acid, the pH value of preferred absorption liquid is 5～14, more preferably 8～13, can improve its pH value by method with the alkali compounds neutralization, described alkali compounds can be selected from ammonia, NaOH, potassium hydroxide or sodium carbonate.
Ammonium-containing compound in the absorption liquid of the present invention is selected from one or more in water-soluble ammonium salt, and for example one or more in ammonium sulfate, ammonium carbonate, carbonic hydroammonium, ammonium phosphate, ammonium chloride, the ammonium nitrate are preferably ammonium sulfate.Described ammonium salt can be commercially available, and also can obtain with the method for ammoniacal liquor and the reaction of its respective acids.The content of ammonium is with NH in the absorption liquid
4+Meter is preferably 0.2g/L to 60g/L.Ammonia can obtain by adding ammoniacal liquor or feed ammonia in absorption liquid, and the content increase of ammonia helps SO in the absorption liquid
xAbsorb, but also can increase the loss of ammonia, the content of ammonia is no more than 10g/L in the preferred absorption liquid, and the ammonia that adds to make the pH value of absorption liquid be 8 to 13.It is pointed out that when absorption liquid neutral and alkali compound concentrations is higher the pH value can surpass 13, this helps SO
xAbsorption, do not need in solution to add the measure that ammonia also needn't take to reduce the pH value of solution value this moment.
When only containing ammonia in the absorption liquid, the content of ammonia is no more than 10g/L in the absorption liquid, and the amount of ammonia to make the pH value of absorption liquid be 8 to 13.
An embodiment preferred, described absorption liquid are derived from the waste water that contains ammonia nitrogen, silicon, aluminium or its mixture that produces in the sieve synthesis procedure.Generally this waste water contains the ammonium sulfate of 4g/L to 23g/L, contains with Al
2O
3Meter content is the aluminum contained compound of 0.8g/L to 4.2g/L, with SiO
2Meter content is the silicon-containing compound of 2.0g/L to 9.0g/L, and the pH value is 8 to 11.
The synthetic waste water that produces of molecular sieve, when the content of aluminum contained compound and silicon-containing compound is lower than 0.5g/L in the oxide absorption liquid, make it to meet the requirements by the mode of mending aluminum contained compound and/or silicon-containing compound, the pH value of preferred absorption liquid is 8 to 13, regulates the pH of absorption liquid by the method that adds ammoniacal liquor, ammonia or alkali compounds such as NaOH, potassium hydroxide in absorption liquid.
Method of the present invention comprises that also oxidation makes inferior sulfate radical in the absorption liquid be converted into the step of sulfate radical, and described method for oxidation is a known method, for example, bubbling air oxidation in the absorption liquid after contact, in the absorption liquid cumulative volume, the feeding amount of air is 1Nm in the absorption liquid
3/ m
3To 100Nm
3/ m
3
Method of the present invention, contacting preceding temperature with waste gas for absorption liquid does not have specific (special) requirements, preferably contains SO
xThe temperature of waste gas before contacting with absorption liquid be 90～150 ℃, absorption liquid contacts preceding temperature with waste gas be 50～100 ℃.
One of the present invention comprises and will contain SO preferred embodiment as shown in Figure 1
xWaste gas be incorporated into the bottom on absorption tower 6 by pipeline 1, with from the cat head spray and under the absorption liquid counter current contacting, the SO in the waste gas
xBe absorbed by liquid absorption, waste gas is discharged by the pipeline 3 at 6 tops, absorption tower.6 top enters the absorption tower to fresh absorption liquid from the absorption tower by pipeline 4, absorbs the SO in the waste gas
xAfter, flow in the oxidization and sedimentation basin 7 by pipeline 11.Constantly blast air in the absorption liquid in oxidization and sedimentation basin 7 by pipeline 2, make the inferior sulfate radical in the absorption liquid be oxidized to sulfate radical, air is discharged by pipeline 9.By moisture in the heater 10 heating evaporation oxidization and sedimentation basins 7, absorption liquid is concentrated, in oxidization and sedimentation basin 7, form solid matter and separate out, be deposited in the bottom of oxidization and sedimentation basin 7.Formed precipitation slurry is drawn by pipeline 8, is transported to filter with slush pump and filters, and filtrate is returned oxidization and sedimentation basin 7 and further handled, and can be used as soil conditioner after the filter residue and drying.Guarantee that formed beds of precipitation height in the oxidization and sedimentation basin 7 is no more than the height of air-distribution pipe under the liquid level, guarantees that promptly the distributor pipe of gas only contacts with absorption liquid.The structure on absorption tower, the operating condition of absorption should guarantee that waste gas can be fully purified, and this is known by persons skilled in the art, and the operating condition of optimization of the present invention is 200 to 2000Nm for the absorption tower gas liquid ratio
3/ m
3, the gas superficial linear velocity in a column is 1000 to 160000Nm
3/ (m
2H).
Another embodiment of the invention as shown in Figure 2, this embodiment is compared with embodiment shown in Figure 1 has increased the absorption liquid circulatory system.In order to guarantee that the ammonia in the absorption liquid can make full use of and utilize the heat energy of waste gas that absorption liquid is concentrated, liquid to the absorption tower that partially absorbs with circulation fluid pipeline 5 cyclic oxidation sedimentation basins 7 contacts with waste gas, reflux ratio (the absorption liquid measure of circulation and the ratio of fresh absorption liquid measure in the absorption cell 7) is 0.1 to 100, and the sediment that guarantee the beds of precipitation is not recycled liquid pipeline 5 and is circulated to the absorption tower.
Other mode that can realize that absorption liquid contacts with waste gas also can be used for implementing the present invention, and one of ordinary skill in the art can be implemented according to method provided by the present invention at an easy rate.
Utilize method of the present invention, waste gas is contacted with absorption liquid purify.Purifying the waste gas of discharging the back can further purify to remove other impurity wherein.Resulting solids is that nitrogenous composition can be used as soil conditioner.
The inventive method is suitable for containing SO
xThe improvement of waste gas, described waste gas can be the waste gas that FCC regenerated flue gas, coal-burning boiler or steam power plant etc. use sulfurous fuels to produce.
It is pointed out that Al in the absorption liquid
2O
3And/or SiO
2Concentration also can be used to handle above 150g/L and contains SO
xWaste gas, but absorption liquid cost height.
SO in the following examples
2Concentration adopt the infra-red sepectrometry analysis; In the sediment analytical method of ammonium sulfate be earlier with resulting sediment in 180 ℃ of oven dry, and then according to the formaldehyde method analysis of GB 535-1995; Ammonium sulfate analytical method in the absorption liquid is the absorption liquid of measuring 10ml earlier, adds water 100ml dilution then, again according to the formaldehyde method analysis of GB 535-1995.
Example 1
The preparation ammonium sulfate concentrations is the solution of 90g/L, adds sodium metaaluminate, makes Al in the solution
2O
3Concentration be 9g/L, add ammoniacal liquor then and regulate the pH value, the pH value that makes solution is 13.
According to flow process shown in Figure 1, in the small-sized absorption plant in laboratory (the absorption tower ratio of height to diameter is 5: 1), feeding temperature from the bottom, absorption tower is 130 ℃, SO
x(SO wherein
2With SO
3Volume ratio be 9: 1) content is 2158mg/Nm
3FCC regenerated flue gas (taking from the Jinan Refinery catalytic cracking unit); The absorption liquid of above-mentioned preparation is heated to 60 ℃, from the top spray of absorption plant, contacts with the waste gas that rises from the bottom, absorption tower, the volume ratio of gas and absorption liquid is 300Nm
3/ m
3, the gas superficial linear velocity in a column is 9000Nm
3/ (m
2H); Absorption liquid after the contact is collected in the storage tank of absorption tower bottom, and in storage tank bubbling air, in the cumulative volume of absorption liquid, the feeding amount of air is 10Nm
3/ m
3, the waste gas after the contact is discharged the absorption tower.Heating evaporation falls part moisture makes absorption SO
xAfter absorption liquid saturated.Analyze the SO in the waste gas of discharging
xConcentration is 113mg/Nm
3After treating to have in the storage tank solids to separate out, being cooled to 60 ℃ of ammonium sulfate concentrations in the analytical solution is 212g/L, and the content of ammonium sulfate is 73.1 weight % in the solids.
Example 2
Absorption liquid uses the waste water that contains ammonia nitrogen and sial (from Qilu Petrochemical company catalyst plant molecular sieve device) that Catalyst Production molecular sieve exchange washing produces in this example, and wherein ammonium sulfate concentrations is 18.1g/L, Al
2O
3Concentration is 3.6g/L, SiO
2Concentration is 5.1g/L, and the pH value is 9.5.
According to flow process shown in Figure 2, in the small-sized absorption plant in laboratory, feeding temperature from bottom of device is 130 ℃, SO
xContent is 2158mg/Nm
3(SO wherein
2With SO
3Volume ratio be 9: 1) FCC regenerated flue gas (taking from the Jinan Refinery catalytic cracking unit); Above-mentioned absorption liquid is heated to 80 ℃, contacts with the waste gas that rises from the bottom, absorption tower from the top spray of absorption plant; Absorption liquid after the contact is collected in the storage tank of absorption tower bottom, and in storage tank bubbling air, the waste gas after the contact is discharged the absorption tower.Spray to top, absorption tower with pump cyclic part absorption liquid from storage tank, evaporate part moisture and make absorption liquid saturated, reflux ratio is 10, and other condition is with example 1.Analyze the SO in the waste gas of discharging
xConcentration is 206mg/Nm
3After having solids to separate out in storage tank, being cooled to 60 ℃ of ammonium sulfate concentrations in the analytical solution is 198g/L, and the content of ammonium sulfate is 51.9 weight % in the solids.
Example 3
The preparation ammonium sulfate concentrations is the solution of 150g/L, adds sodium metasilicate, makes SiO in the solution
2Concentration be 14g/L, add ammoniacal liquor then and regulate the pH value, the pH value that makes solution is 11.
According to flow process shown in Figure 1, in the small-sized absorption plant in laboratory (the absorption tower ratio of height to diameter is 5: 1), be 130 ℃, SO from absorption tower bottom feeding degree
x(SO wherein
2With 8O
3Volume ratio be 9: 1) content is 2158mg/Nm
3FCC regenerated flue gas (taking from the Jinan Refinery catalytic cracking unit); The absorption liquid of above-mentioned preparation is heated to 90 ℃, from the top spray of absorption plant, contacts with the waste gas that rises from the bottom, absorption tower, the volume ratio of gas and absorption liquid is 300Nm3/m
3, the gas superficial linear velocity in a column is 9000Nm
3/ (m
2H); Absorption liquid after the contact is collected in the storage tank of absorption tower bottom, and in storage tank bubbling air, in the cumulative volume of absorption liquid, the feeding amount of air is 10Nm
3/ m
3, the waste gas after the contact is discharged the absorption tower.Heating evaporation falls part moisture makes absorption SO
xAfter absorption liquid saturated.Analyze the SO in the waste gas of discharging
xConcentration is 179mg/Nm
3After having solids to separate out in storage tank, being cooled to 60 ℃ of ammonium sulfate concentrations in the analytical solution is 287g/L, and the content of ammonium sulfate is 62.8 weight % in the solids.
Comparative Examples 1
The preparation ammonium sulfate concentrations is the solution of 90g/L, adds ammoniacal liquor then and regulates the pH value, and the pH value that makes solution is 13.
According to flow process shown in Figure 1, in the small-sized absorption plant in laboratory (the absorption tower ratio of height to diameter is 5: 1), feeding temperature from the bottom, absorption tower is 130 ℃, SO
x(SO wherein
2With 8O
3Volume ratio be 9: 1) content is 2158mg/Nm
3FCC regenerated flue gas (taking from the Jinan Refinery catalytic cracking unit); The absorption liquid of above-mentioned preparation is heated to 90 ℃, from the top spray of absorption plant, contacts with the waste gas that rises from the bottom, absorption tower, the volume ratio of gas and absorption liquid is 300Nm
3/ m
3, the gas superficial linear velocity in a column is 9000Nm
3/ (m
2H); Absorption liquid after the contact is collected in the storage tank of absorption tower bottom, and in storage tank bubbling air, in the cumulative volume of absorption liquid, the feeding amount of air is 10Nm
3/ m
3, the waste gas after the contact is discharged the absorption tower.Heating evaporation falls part moisture makes absorption SO
xAfter absorption liquid saturated.Analyze the SO in the waste gas of discharging
xConcentration is 327mg/Nm
3After having solids to separate out in storage tank, being cooled to 60 ℃ of ammonium sulfate concentrations in the analytical solution is 574g/L.
Claims (16)
1, SO in a kind of processing waste gas
xMethod, comprise and will contain SO
xWaste gas contact with the absorption liquid that contains ammonium-containing compound and/or ammonia, also contain aluminum contained compound and/or silicon-containing compound in the wherein said absorption liquid, in oxide, the content of aluminum contained compound and/or silicon-containing compound is 0.5g/L to 150g/L in the described absorption liquid.
2, according to claim 1 described method, it is characterized in that, contain aluminum contained compound in the described absorption liquid, in aluminium oxide, the content of aluminum contained compound is 0.5g/L to 100g/L in the described absorption liquid.
3, according to claim 2 described methods, it is characterized in that, contain aluminum contained compound in the described absorption liquid, in aluminium oxide, the content of aluminum contained compound is 0.5g/L to 10g/L in the described absorption liquid.
4, according to claim 1 described method, it is characterized in that, contain silicon-containing compound in the described absorption liquid, in silica, the content of silicon-containing compound is 0.5g/L to 120g/L in the described absorption liquid.
5, according to claim 4 described methods, it is characterized in that, contain silicon-containing compound in the described absorption liquid, in silica, the content of silicon-containing compound is 0.5g/L to 15g/L in the described absorption liquid.
6, according to claim 1 described method, it is characterized in that, contain aluminum contained compound and silicon-containing compound in the described absorption liquid, in oxide, the content of silicon-containing compound is 0.1g/L to 100g/L in the described absorption liquid, and the content of aluminum contained compound is 0.1g/L to 50g/L.
7, according to claim 6 described methods, it is characterized in that, contain aluminum contained compound and silicon-containing compound in the described absorption liquid, in oxide, the content of silicon-containing compound is 0.1g/L to 10g/L in the described absorption liquid, and the content of aluminum contained compound is 0.1g/L to 10g/L.
8, according to claim 1,2,3,6,7 each described methods, it is characterized in that described aluminum contained compound is one or more in sodium metaaluminate, aluminum sulfate, aluminum nitrate, the aluminium chloride.
According to claim 1,4,5,6,7 each described methods, it is characterized in that 9, described silicon-containing compound is sodium metasilicate, Ludox or its mixture.
According to claim 1 described method, it is characterized in that 10, described ammonium-containing compound is one or more of water-soluble ammonium salt, the content of ammonium-containing compound is with NH in the described absorption liquid
4 +Count 0.2g/L to 60g/L.
According to claim 10 described methods, it is characterized in that 11, described ammonium-containing compound is one or more in ammonium sulfate, ammonium carbonate, carbonic hydroammonium, ammonium phosphate, ammonium chloride, the ammonium nitrate.
According to claim 11 described methods, it is characterized in that 12, described ammonium-containing compound is an ammonium sulfate.
13, according to claim 1 described method, it is characterized in that the content of ammonia is no more than 10g/L in the described absorption liquid, and the content of ammonia to make the pH value of absorption liquid be 8～13.
According to claim 1 described method, it is characterized in that 14, described absorption liquid comes from the synthetic waste water that contains ammonia nitrogen, silicon, aluminium or its mixture that produces of molecular sieve.
15, according to claim 1 described method, it is characterized in that described waste gas stems from the FCC regenerated flue gas.
According to claim 1 described method, it is characterized in that 16, described method also comprises the step with the absorption liquid oxidation after the contact.
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| CN1647849A (en) * | 2004-12-17 | 2005-08-03 | 王明祥 | Smoke desulfurizing method by amino-thiamine method |
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2006
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| CN101862584B (en) * | 2010-06-24 | 2012-08-22 | 四川泸天化股份有限公司 | Novel process for comprehensive treatment of ammonium nitrate wastewater and flue gas |
| CN103721553A (en) * | 2014-01-07 | 2014-04-16 | 江苏新世纪江南环保股份有限公司 | Method for efficiently removing acid gas sulfide by ammonia process desulfurization technique |
| CN104307339A (en) * | 2014-10-30 | 2015-01-28 | 神华集团有限责任公司 | Desulfurization tower |
| 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 |
| CN113856441A (en) * | 2021-10-25 | 2021-12-31 | 江苏新世纪江南环保股份有限公司 | Ammonia desulfurization method and ammonia desulfurization apparatus |
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