CN1583230A - Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method - Google Patents
Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method Download PDFInfo
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- CN1583230A CN1583230A CN 200410024719 CN200410024719A CN1583230A CN 1583230 A CN1583230 A CN 1583230A CN 200410024719 CN200410024719 CN 200410024719 CN 200410024719 A CN200410024719 A CN 200410024719A CN 1583230 A CN1583230 A CN 1583230A
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- 239000000428 dust Substances 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000002002 slurry Substances 0.000 title claims abstract description 27
- 239000003513 alkali Substances 0.000 title claims abstract description 24
- 238000002425 crystallisation Methods 0.000 title claims description 31
- 230000008025 crystallization Effects 0.000 title claims description 31
- 230000006698 induction Effects 0.000 title description 2
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 230000008929 regeneration Effects 0.000 claims abstract description 18
- 238000011069 regeneration method Methods 0.000 claims abstract description 18
- 239000011734 sodium Substances 0.000 claims abstract description 15
- 238000007599 discharging Methods 0.000 claims abstract description 10
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 6
- 235000019738 Limestone Nutrition 0.000 claims abstract description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 6
- 239000004571 lime Substances 0.000 claims abstract description 6
- 239000006028 limestone Substances 0.000 claims abstract description 6
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 claims description 67
- 230000023556 desulfurization Effects 0.000 claims description 67
- 239000003546 flue gas Substances 0.000 claims description 63
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 61
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 29
- 239000006096 absorbing agent Substances 0.000 claims description 18
- 239000013078 crystal Substances 0.000 claims description 18
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 229910052925 anhydrite Inorganic materials 0.000 claims description 12
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 9
- 229910052602 gypsum Inorganic materials 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 8
- 230000001939 inductive effect Effects 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 6
- 239000001110 calcium chloride Substances 0.000 claims description 6
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 6
- 229910052681 coesite Inorganic materials 0.000 claims description 6
- 229910052906 cristobalite Inorganic materials 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- 239000000377 silicon dioxide Substances 0.000 claims description 6
- 229910052682 stishovite Inorganic materials 0.000 claims description 6
- 229910052905 tridymite Inorganic materials 0.000 claims description 6
- 239000002244 precipitate Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Inorganic materials [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 239000000047 product Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 230000001502 supplementing effect Effects 0.000 claims description 2
- 230000009977 dual effect Effects 0.000 claims 1
- 230000003009 desulfurizing effect Effects 0.000 abstract description 10
- 239000002585 base Substances 0.000 abstract description 2
- 239000003517 fume Substances 0.000 abstract 3
- 230000008021 deposition Effects 0.000 abstract 2
- 238000010410 dusting Methods 0.000 abstract 1
- 238000005086 pumping Methods 0.000 abstract 1
- 239000006228 supernatant Substances 0.000 abstract 1
- 239000011575 calcium Substances 0.000 description 11
- 235000010269 sulphur dioxide Nutrition 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000010440 gypsum Substances 0.000 description 5
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000004480 active ingredient Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- HUAUNKAZQWMVFY-UHFFFAOYSA-M sodium;oxocalcium;hydroxide Chemical compound [OH-].[Na+].[Ca]=O HUAUNKAZQWMVFY-UHFFFAOYSA-M 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000004291 sulphur dioxide Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Abstract
A concentrated slurry and dual-alkali process for desulfurizing, dusting and reclaming fume includes such steps as removing SO2 and dust from fume by the desulfurizing liquid, exhausting clean fume, returning part of resultant liquid base to desulfurizing liquid, pumping its rest in crystallizer, crystallizing, flowing the most of slurry in regenerator while flowing the rest in deposition pool, taking the supernatant from deposition pool and delivering it to regenerator, discharging deposit, and adding lime/lime stone and sodium alkali to said slurry in regenerator for regeneration.
Description
Technical Field
The invention belongs to the technical field of environment, relates to a flue gas treatment process, and particularly relates to a dense slurry dual-alkali flue gas desulfurization, dedusting and induced crystallization recycling process which is particularly used for eliminating flue gas pollution generated by burning fossil fuel.
Background
With the increasing awareness of sulfur dioxide and dust pollution, strict emission standards are implemented in some places, and the original emission concentration of sulfur dioxide in flue gas is required to be lower than 650mg/Nm3And the sulfur dioxide content in the treated flue gas is required to be lower than 150mg/Nm3Dust must be less than 50mg/Nm3. In this case, dry desulfurization and dust removal devices are often impractical or impractical to operate and have extremely high capital costs.
At present, the double-alkali desulfurization process in the wet desulfurization and dust removal technology is usually adopted by small and medium-sized systems. The dual-alkali desulfurizing process includes absorbing SO in main tower with soluble alkaline clear liquid as absorbent2And then regenerating the absorption liquid by lime milk or lime outside the tower. However, under some working conditions (such as when low-sulfur coal is combusted), CaSO is very likely to occur in actual operation due to high oxygen content in flue gas, impurity dissolution in dust, sufficient gas-liquid contact and the like4The supersaturation of (2) may cause the crystal blockage of desulfurizer and pipeline or the large loss of sodium salt, and seriously affects the energy consumption of system and the period of stable and reliable operation.
Disclosure of Invention
The invention provides a dense slurry dual-alkali flue gas desulfurization and dedusting induced crystallization recycling process which is stable in operation, simple and convenient to operate, low in investment and low in operation cost.
The flue gas desulfurization, dust removal, induced crystallization and cyclic utilization process of the dense slurry double-alkali method comprises the following steps:
the desulfurization solution is input into a desulfurization absorber and a waiting placeManaging the flue gas to convectively absorb and adsorb sulfur dioxide and dust in the flue gas, discharging the flue gas after purification, reflowing a part of bottom discharge liquid into desulfurization liquid again, and sending the other part into a crystallizing tank; adding seed crystals in a crystallization tank under the condition of stirring for induced crystallization, transferring most of the slurry after induced crystallization into a regeneration tank, and transferring a small part of the slurry into a sedimentation tank; transferring the clear liquid after precipitation in the precipitation tank into a regeneration tank, and discharging the precipitate; adding into slurry in a regeneration tankAdding lime/limestone for regeneration, and supplementing sodium base as required to raise pH value of regenerated desulfurizing liquid to 5.0-13.0, Na+Concentration less than 1.0 mol/l, Ca+The concentration is less than 2000ppm, and the product is output to a desulfurization absorber through a circulating pump for recycling.
The bottom liquid discharged from the desulfurization absorber can be mostly refluxed, and the reflux ratio of the liquid refluxed to the desulfurization absorber accounts for more than or equal to 60 percent of the total discharged amount.
The seed crystal added into the crystallizing tank is as follows: one or more substances capable of inducing CaSO4Formation of CaSO4·2H2Oxides or salts of O crystals, e.g. selected from SiO2、CaCl2、CaSO3、CaSO4、BaSO4One or a mixture of several of them.
In the desulfurization absorber, the desulfurization solution is contacted with the flue gas to be treated and mixed, and then SO in the flue gas is obtained2And residual dust is absorbed or adsorbed by the desulfurizing liquid, and the active component Na in the desulfurizing liquid2SO3And CaSO3With SO in flue gas2Reaction partial or complete conversion to NaHSO3And Ca (HSO)3)2At the same time, the flue gas contains SO3And O2And oxidation reaction exists simultaneously in the desulfurization process, so that the desulfurization solution discharged from the tower contains partially supersaturated calcium sulfate (gypsum). The main chemical reaction formula isas follows:
one part of the discharged liquid from the desulfurization absorber enters a reflux, the other part enters a crystallizing tank, and the induced crystallization of gypsum is carried out under the stirring action at normal temperature, so that CaSO dissolved in the desulfurization liquid4With CaSO4·2H2And crystallizing in the form of O, feeding most of the crystal slurry into a regeneration tank, discharging a small part of the crystal slurry into a sedimentation tank, separating out precipitate, discharging slag, and returning clear liquid to a system for use.
When the crystal seeds are selected during the induced crystallization of gypsum, according to the conventional crystallization theory and the characteristics of the crystallization in the invention, generally speaking, the substances capable of inducing and accelerating the crystallization mainly comprise the following types: (1) with CaSO4·2H2O oxides or salts with similar crystal structures; (2) with CaSO4·2H2O oxides or salts with similar surface charge states; (3) with CaSO4·2H2O oxides or salts whose crystallization mechanism is similar. In the present invention, the oxide or salt according to the above 3 similar crystallization principles is SiO2、CaCl2、CaSO3、CaSO4、BaSO4Etc., particularly according to the content of sulfur dioxide in the flue gas to be treatedThe amount and other harmful gases are selected from one or more mixtures.
The slurry from the crystallizing tank and clear liquid returned from the settling tank are neutralized in the regenerating tank with the added soda lime/limestone while replenishing partial sodium alkali as required to raise pH value and restore high desulfurizing activity, and the sodium alkali and the clear liquid are absorbed in the desulfurizing apparatus. The main chemical reactions in the regeneration tank are:
2NaHSO3+Ca(OH)2←→Na2SO3+CaSO3+2H2O (9)
Ca(HSO3)2+Ca(OH)2←→2CaSO3+2H2O (10)
NaHSO3+NaOH←→Na2SO3+2H2O (11)
Ca(HSO3)2+2NaOH←→CaSO3+Na2SO3+2H2O (12)
CaO+H2O←→Ca(OH)2(13)
the flue gas desulfurization and dust removal induced crystallization recycling process of the dense slurry dual-alkali method inherits the advantages of the dual-alkali method, simultaneously avoids the interference of high oxidation rate to the dual-alkali method, does not block a pipeline and an absorber in the processes of desulfurization and dust removal as the last stage, has high utilization rate of sodium alkali, directly reflows most of discharged liquid, has large backflow amount, less water loss, small volume of a sedimentation tank, low operation cost of desulfurization and dust removal and good desulfurization and dust removal effects.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The process of the invention comprises a desulfurization dust removal part, an induced crystallization part and a pH recovery part, and specifically comprises the following steps:
1. desulfurizing and dedusting part
The flue gas after dry or wet dust removal is mixed with Na in a desulfurization absorber2SO3And CaSO3The mixed liquid of the active ingredients is fully contacted and mixed, so that sulfur dioxide and dust in the flue gas are absorbed or adsorbed by the desulfurization liquid, and the flue gas after desulfurization and dust removal is discharged after water vapor is removed by the demister. The liquid, which has absorbed and adsorbed sulphur dioxide and dust, is discharged from the bottom. Most of the discharged liquid flows back to the desulfurization absorber, and a small part of the discharged liquid is sent to the crystallization tank.
2. Crystalline fraction
And (3) sending part of the discharged liquid absorbing and adsorbing sulfur dioxide and dust into a crystallizing tank, adding seed crystalsunder stirring to induce crystallization, discharging a small part of high-concentration slurry after crystallization into a settling tank, transferring most of the slurry in the crystallizing tank and clear liquid in the settling tank into a regeneration tank, and periodically discharging slag from precipitates.
pH recovery moiety
The clear liquid transferred into the regeneration tank has lower pH value, lime/limestone is added for regeneration to raise the pH value and restore high desulfurization capacity, and the clear liquid is reused in the desulfurization absorber, the pH value of the desulfurization liquid entering the desulfurization absorber is controlled to be 5.0-13.0, and Na is added+Concentration less than 1.0 mol/l, Ca+The concentration is less than 2000 ppm.
The specific process is shown in figure 1, the dense slurry dual-alkali flue gas desulfurization induced crystallization recycling process consists of three parts, namely desulfurization and dust removal, induced crystallization and pH recovery; the desulfurization absorber 1 can adopt plate towers such as a cyclone plate tower, a sieve plate tower, a bubble cap tower and the like, a packing tower, a Venturi tower, a spray tower and the like, desulfurization, dust removal and demisting are carried out in the same tower, the desulfurization liquid is atomized by utilizing the kinetic energy of gas, the gas and the liquid are fully contacted and mixed, sulfur dioxide and residual dust in the flue gas are absorbed or adsorbed by the desulfurization liquid, and the active ingredient Na in the desulfurization liquid2SO3And CaSO3With SO in flue gas2Reaction partial or complete conversion to NaHSO3And Ca (HSO)3)2At the same time, the flue gas contains SO3And O2The oxidation reaction is simultaneously existed in the desulfurization process, so that the catalyst is taken out of the tower for removalThe sulfur solution contains partially supersaturated calcium sulfate (gypsum).
All the discharged liquid from the desulfurizer enters a crystallizing tank 2, and crystal seeds are added under the stirring action to perform induced crystallization of gypsum so as to ensure that CaSO dissolved in the desulfurization liquid4With CaSO4·2H2Crystallizing out the O form at normal temperature, wherein the pH value is 3.0-10, discharging a small part of the crystal into a sedimentation tank 3 after the crystallization is carried out for a certain time, separating out a precipitate, and feeding a large part of the slurry into a regeneration tank 4.
The slurry from the crystallizing tank 2 and the clear liquid returned from the sedimentation tank in the regeneration tank 4 are subjected to neutralization reaction with the added soda lime/limestone to increase the pH value, and the supplementary alkali is added, wherein the supplementary alkali is soda ash, caustic soda or waste alkali, SO that the desulfurization liquid recovers the high desulfurization activity, and the desulfurization liquid circularly enters the desulfurization absorber 1 through the circulating pump 5 to absorb and adsorb SO2And dust.
Example 1
The temperature of the flue gas is 150 ℃, and the inlet flue gas SO2The concentration is 2000mg/m3The pH value of the desulfurization solution (namely the regeneration tank) entering the desulfurizer is 9.0, and Na is+Concentration of 0.02 mol/l, Ca+The concentration is 20ppm, and the liquid-gas ratio L/G of the flue gas to the flue gas is 3.0L/m3。
The amount of the bottom effluent refluxed to the desulfurization absorber was 95% based on the total amount of the effluent, i.e., the reflux ratio.
The pH value in the crystallizing tank is controlled to be 8.0, and the inducing seed crystal is proper SiO2、CaSO3、CaSO4A mixture of (a).
After the whole system is operated, the flue gas desulfurization efficiency reaches 90 percent.
Example 2
The temperature of the flue gas is 150 ℃, and the inlet flue gas SO2The concentration is 2000mg/m3The pH value of the desulfurization solution (namely the regeneration tank) entering the desulfurizer is 8.0, and Na is+Concentration of 0.01 mol/l, Ca+The concentration is 20ppm, and the liquid-gas ratio L/G of the flue gas to the flue gas is 3.0L/m3The reflux ratio was 85%.
The pH value in the crystallizing tank is controlledPrepared at 7.0, the induction seed crystal is SiO with proper amount2。
After the whole system is operated, the flue gas desulfurization efficiency reaches 85 percent.
Example 3
The temperature of the flue gas is 150 ℃, and the inlet flue gas SO2The concentration is 500mg/m3At a flue gas temperature of 120 ℃, the inlet flue gas SO2The concentration is 500mg/m3The pH value of the desulfurization solution entering the desulfurizer is 12.0, and Na is+Concentration of 0.4 mol/l, Ca+The concentration is 1000ppm, and the liquid-gas ratio L/G of the flue gas to the flue gas is 15.0L/m3The reflux ratio was 90%.
The pH value in the crystallizing tank is controlled to be 10.0, and the inducing seed crystal is proper SiO2、CaCl2、CaSO3、CaSO4、BaSO4A mixture of (a).
After the whole system is operated, the flue gas desulfurization efficiency reaches 99 percent.
Example 4
The temperature of the flue gas is 150 ℃, and the inlet flue gas SO2The concentration is 500mg/m3At a flue gas temperature of 130 ℃, the inlet flue gas SO2The concentration is 500mg/m3The pH value of the desulfurization solution entering the desulfurizer is 9.0, and Na is+Concentration of 0.6 mol/l, Ca+The concentration is 100ppm, and the liquid-gas ratio L/G of the flue gas to the flue gas is 15.0L/m3The reflux ratio was 70%.
The pH value in the crystallizing tank is controlled to be 6.0, and the inducing seed crystal is proper amount of CaCl2、CaSO3、CaSO4A mixture of (a).
After the whole system is operated, the flue gas desulfurization efficiency reaches 80 percent.
Example 5
The temperature of the flue gas is 150 ℃, and the inlet flue gas SO2The concentration is 4000mg/m3At the flue gas temperature of 140 ℃, the inlet flue gas SO2The concentration is 500mg/m3The pH value of the desulfurization solution entering the desulfurizer is 7.0, and Na is+Concentration of 0.06 mol/l, Ca+The concentration is 400ppm, and the liquid-gas ratio L/G of the flue gas to the flue gas is 1.0L/m3Reflux ratio of 80％。
The pH value in the crystallizing tank is controlled to be 5.0, and the inducing seed crystal is proper SiO2、CaCl2、CaSO3、CaSO4A mixture of (a).
After the whole system is operated, the flue gas desulfurization efficiency reaches 70 percent.
Claims (4)
1. A dense slurry dual-alkali flue gas desulfurization, dedusting, induced crystallization and cyclic utilization process comprises the following steps:
inputting the desulfurization solution into a desulfurization absorber to absorb and adsorb sulfur dioxide and dust in the flue gas in a convection way with the flue gas to be treated, discharging the flue gas after purification, reflowing one part of bottom discharge liquid into the desulfurization solution again, and sending the other part of the bottom discharge liquid into a crystallizing tank; adding seed crystals in a crystallization tank under the condition of stirring for induced crystallization, transferring most of the slurry after induced crystallization into a regeneration tank, and transferring a small part of the slurry into a sedimentation tank; transferring the clear liquid after precipitation in the precipitation tank into a regeneration tank, and discharging the precipitate; adding lime/limestone into the slurry in the regeneration tank for regeneration, and supplementing sodium alkali according to the requirement to increase the pH value of the regenerated desulfurization solution to 5.0-13.0, Na+Concentration less than 1.0 mol/l, Ca+The concentration is less than 2000ppm, and the product is output to a desulfurization absorber through a circulating pump for recycling.
2. The dense slurry dual-alkali flue gas desulfurization and dust removal induced crystallization recycling process as claimed in claim 1, characterized in that: the reflux ratio of the bottom discharge liquid of the desulfurization absorber to the desulfurization absorber accounts for more than or equal to 60 percent of the total discharge amount.
3. The dense slurry dual-alkali flue gas desulfurization and dust removal induced crystallization recycling process as claimed in claim 1, characterized in that: the seed crystal added into the crystallizing tank is as follows: one or more substances capable of inducing CaSO4Formation of CaSO4·2H2O crystalline oxides or salts.
4. The dense slurry dual alkali flue gas desulfurization and removal method according to claim 3The dust-induced crystallization recycling process is characterized by comprising the following steps: the seed crystal added into the crystallizing tank is as follows: selected from SiO2、CaCl2、CaSO3、CaSO4、BaSO4One or a mixture of several of them.
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| CN 200410024719 CN1245245C (en) | 2004-05-25 | 2004-05-25 | Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method |
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| CN 200410024719 CN1245245C (en) | 2004-05-25 | 2004-05-25 | Flue desulfuriznig and dust collecting induction and crystallization process for reuse by concentrated slurry double alkali method |
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| CN1245245C CN1245245C (en) | 2006-03-15 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100435910C (en) * | 2006-04-10 | 2008-11-26 | 广州市天赐三和环保工程有限公司 | Fume desulfurizing process employing multiple circulation and stable double alkali method and apparatus |
| CN101816887A (en) * | 2010-05-07 | 2010-09-01 | 吉林安洁环保有限公司 | High-alkaline double-alkali simplified desulfuration control method by adding agent at front end of canal |
| CN102085450A (en) * | 2010-12-17 | 2011-06-08 | 秦皇岛双轮环保科技有限公司 | Integrated desulfuration and dust removal method for medium and small boiler flue gas |
| CN102166470A (en) * | 2011-03-09 | 2011-08-31 | 西安西矿环保科技有限公司 | Dual-alkali smoke desulfurization device and desulfurization method thereof |
| CN102485323A (en) * | 2011-04-15 | 2012-06-06 | 安徽理工大学 | Rapid calcium desulphurization method for flue gas |
| CN103920396A (en) * | 2014-03-31 | 2014-07-16 | 煤科集团杭州环保研究院有限公司 | Automatic open-type double-alkali-method desulphurized gypsum oxidation system and control method thereof |
| CN105585177A (en) * | 2016-02-05 | 2016-05-18 | 大唐环境产业集团股份有限公司 | Desulfurization wastewater softening device and method |
| CN106904711A (en) * | 2017-04-20 | 2017-06-30 | 盐城工学院 | A kind of calcium carbonate waste water circulation recovery system and calcium carbonate circulating purification system |
| CN110302641A (en) * | 2019-04-25 | 2019-10-08 | 太仓北新建材有限公司 | A kind of desulfurizer and sulfur removal technology of flue gas |
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| CN115159555B (en) * | 2022-08-01 | 2023-12-22 | 华中科技大学 | Method and system for treating solid waste incineration flue gas |
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