CN101342464A - Regeneration and recycle process for slurry with dual-alkali process flue gas desulfurization - Google Patents
Regeneration and recycle process for slurry with dual-alkali process flue gas desulfurization Download PDFInfo
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- CN101342464A CN101342464A CNA2008101204161A CN200810120416A CN101342464A CN 101342464 A CN101342464 A CN 101342464A CN A2008101204161 A CNA2008101204161 A CN A2008101204161A CN 200810120416 A CN200810120416 A CN 200810120416A CN 101342464 A CN101342464 A CN 101342464A
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- absorption liquid
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Abstract
The invention discloses a regeneration and recycling technology of smoke gas desulfurization seriflux in a double alkali method; chitosan is used as a heavy metal flocculant to control the regeneration of absorption liquid in a pH vale range of 6 to 10 after desulfuration; a suspended substance can be quickly separated by deposition; and a heavy metal ion concentration in the separated absorption liquid can be controlled in a certain level. The regeneration and recycling technology of the smoke gas desulfurization seriflux in the double alkali method has the advantages of simple technology and convenient operation and realizes simultaneously the separation of particulate matter and the control of the heavy metal ion concentration by the chitosan heavy metal flocculant, thereby achieving the purpose of the regeneration of the absorption liquid and the anti-oxidation of an absorbent and improving a water recycling ratio.
Description
Technical field
The invention belongs to the resource and environment technical field, especially relate to a kind of double alkali method desulfurizing slurries process for regenerating, recovering and reutilizing.
Background technology
The dual alkali scrubbing FGD process technology grows up in order to overcome problems such as fouling in the wet method limestone/lime-gypsum law technology, obstruction.The key of the effective operation of two alkaline process system is that absorbent regeneration separates the oxidation that obtains clear liquid and control absorbent, thus the possibility of fouling and the circulation of realization regeneration of absorption solution in the minimizing desulfurizer.In absorption liquid recycles, contain the fluorine ion and chlorion and the dust that from raw coal, bring on a small quantity in the coal-fired flue-gas, be absorbed liquid and wash, the heavy metal in the dust constantly is dissolved in the absorption liquid, makes heavy metal ion, chlorion, fluorinion concentration constantly increase.Wherein concentration of heavy metal ion increases, and makes absorbent main component (SO
3 2-) easily oxidized and lost efficacy.Thereby the dual alkali scrubbing FGD process system need solve the particle separation of regeneration rear slurry and the control of heavy metal concentration.But there are the following problems: (1) is because the particulate size that the absorbent regeneration reaction is generated is little, precipitate and separate is very difficult, at present used gravitational settling equipment occupation of land is very big, settling efficiency is low, enter in the absorption liquid of desulfurizer and contain a large amount of particles, deposition causes stopping up easily in equipment and pipeline; (2) because concentration of heavy metal ion increases SO
3 2-Be oxidized to SO
4 2-Possibility also increase, easily in equipment and pipeline with absorption liquid in Ca
2+The deposition that reacts and cause stopping up does not fundamentally solve structure.Problems such as obstruction, thus the sizable application of two alkali process in actual production hindered.
At present, at the problems referred to above, the measure of mainly taking is for increasing regeneration rear slurry sedimentation time and periodic replacement part circulation fluid, in the hope of reaching particle and concentration of heavy metal ion in the control absorption liquid.Though these measures can guarantee the normal operation of dual alkali scrubbing FGD process system, whole system is taken up an area of big, and the recycling rate of waterused of water resource is low, and the desulfurization wastewater that effluxes generation could discharge after also needing further to handle.
Summary of the invention
The present invention is directed to the defective of prior art, a kind of desulfurization slurry process for regenerating, recovering and reutilizing that is used for the dual alkali scrubbing FGD process system is provided, can fundamentally solve fouling, blocking problem, and improved water circulation recycling rate of waterused.
Technology is used in a kind of desulfurization slurry regeneration that is used for the dual alkali scrubbing FGD process system, by adding shitosan as the heavy metal flocculant, in the pH value is the scope of 6-10, can remove heavy metal ion wherein when making absorption liquid after the desulfurization obtain regenerating, suppress in the absorption liquid heavy metal ion accumulation and improve the regenerating particulate settling efficiency to reach.Comprise the steps:
(1) chitosan solution is joined in the absorption liquid after the desulfurization, dispersed with stirring is even, makes the abundant flocculation reaction of shitosan and heavy metal ion; Mass ratio is more than 0.01 between the deposit seed thing that the shitosan addition should be guaranteed to produce behind the regeneration of absorption solution after itself and the desulfurization in the absorption liquid, because the chelate that shitosan in the solution and heavy metal ion form is under the particle existence condition, can with its generation co-precipitation, but the shitosan in the solution has precedence over chelation to heavy metal ion to the flocculation of particle, therefore, have only after particle fully flocculates, the chelate that shitosan and heavy metal ion form could with particle floccule body generation co-precipitation, thereby from absorption liquid, remove heavy metal ion.
(2) with the absorption liquid processing of in the scope of pH value 6-10, regenerating after regenerative agent and the flocculation; Under this pH condition, the absorbent after the desulfurization in the absorption liquid is (mainly with HSO
3-be main) be regenerated as effective absorption composition (with SO
3 2-and OH-be main), simultaneously the part heavy metal is separated out with hydroxide form, can with and shitosan-heavy metal chelate form co-precipitation, improve the removal of heavy metal ion in the absorption liquid; Regenerative agent commonly used has lime, lime stone, calcium hydroxide, sodium carbonate, NaOH etc.;
(3) absorption liquid after the regeneration advances precipitation, and the mud that obtains after the precipitate and separate concentrates the back dehydration, and supernatant returns desulfurizer to be continued to use.
Supernatant after the precipitate and separate is sent desulfurizer back to, so circular flow, and chlorine ion concentration reaches about 10000mg/L in absorption liquid, and no longer suitable desulfurization is used, and concentration of heavy metal ion can be controlled in certain level.
The present invention utilizes soluble chitosan existing particle flocculation in solution that the characteristic of heavy metals trapping is arranged again, make that concentration of heavy metal ion is controlled at certain level in the absorption liquid, realize the control of particulate separation and concentration of heavy metal ion simultaneously, reach the purpose that regeneration of absorption solution and absorbent oxidation suppress.
Description of drawings
Fig. 1 is a process chart of the present invention.
The specific embodiment
Embodiment 1
The chitosan solution of preparation 5%, joining quantity of circulating water is 140m
3In the absorption liquid, flow is 1.4m after the desulfurization of/h
3/ h, reaction overflowed to the regenerative response pond after 30 minutes through the mechanical agitation blender.
Add milk of lime regeneration in the regenerated reactor and handle, the pH value is 7.5 in the pond.
After horizontal sedimentation tank clarification and mud were concentrated, the suspended substance removal rate reached 99% in the absorption liquid, and manganese ion concentration is 5.5-6.0mg/L;
Send the supernatant after the precipitate and separate back to desulfurizer, so circular flow, chlorine ion concentration reaches 10000mg/L in absorption liquid, and manganese ion concentration also can be controlled in below the 6.0mg/L.
Embodiment 2
The chitosan solution of preparation 10%, joining quantity of circulating water is 140m
3In the absorption liquid, flow is 0.5m after the desulfurization of/h
3/ h, reaction overflowed to the regenerative response pond after 30 minutes through the mechanical agitation blender.
Add NaOH regeneration in the regenerated reactor and handle, the pH value is 8.0 in the pond;
After horizontal sedimentation tank clarification and mud are concentrated, the suspended substance removal rate reaches 99% in the absorption liquid, and manganese ion concentration is 5.50-5.80mg/L, and zinc ion concentration is 1.80-2.50mg/L, concentration of cadmium ions is 0.80-1.50mg/L, and nickel ion concentration is 3.80-4.50mg/L;
Send the supernatant after the precipitate and separate back to desulfurizer, so circular flow, chlorine ion concentration reaches 10000mg/L in absorption liquid, and manganese, zinc, cadmium, nickel ion concentration also can be controlled at 5.80mg/L, 2.50mg/L, 1.50mg/L respectively, below the 4.50mg/L.
Embodiment 3
The chitosan solution of preparation 1%, joining quantity of circulating water is 140m
3In the absorption liquid, flow is 8.2m after the desulfurization of/h
3/ h, reaction overflowed to the regenerative response pond after 30 minutes through the mechanical agitation blender.
Add calcium hydroxide regeneration in the regenerated reactor and handle, the pH value is 6.5 in the pond;
After horizontal sedimentation tank clarification and mud were concentrated, the suspended substance removal rate reached 99% in the absorption liquid, and manganese ion concentration is 5.7-6.3mg/L, and zinc ion concentration is 2.30-2.90mg/L;
Send the supernatant after the precipitate and separate back to desulfurizer, so circular flow, chlorine ion concentration reaches 10000mg/L in absorption liquid, and manganese, zinc concentration also can be controlled at 6.30mg/L respectively, below the 2.90mg/L.
Claims (3)
1, a kind of desulfurization slurry process for regenerating, recovering and reutilizing that is used for the dual alkali scrubbing FGD process system may further comprise the steps:
(1) chitosan solution is joined in the absorption liquid after the desulfurization, dispersed with stirring is even, makes the abundant flocculation reaction of shitosan and heavy metal ion;
(2) absorption liquid after regenerative agent and the flocculation is carried out regenerative response in the scope of pH value 6-10;
(3) absorption liquid after the regeneration advances precipitation, and the mud that obtains after the precipitate and separate concentrates the back dehydration, and supernatant returns desulfurizer to be continued to use.
2, the desulfurization slurry process for regenerating, recovering and reutilizing that is used for the dual alkali scrubbing FGD process system as claimed in claim 1 is characterized in that: the mass ratio of the precipitation that produces in the absorption liquid after shitosan that adds in the absorption liquid after the desulfurization and the regeneration is greater than 0.01.
3, the desulfurization slurry process for regenerating, recovering and reutilizing that is used for the dual alkali scrubbing FGD process system as claimed in claim 1, it is characterized in that: described regenerative agent is lime, lime stone, calcium hydroxide, sodium carbonate or NaOH.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101204161A CN101342464A (en) | 2008-09-01 | 2008-09-01 | Regeneration and recycle process for slurry with dual-alkali process flue gas desulfurization |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008101204161A CN101342464A (en) | 2008-09-01 | 2008-09-01 | Regeneration and recycle process for slurry with dual-alkali process flue gas desulfurization |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102210966A (en) * | 2010-04-02 | 2011-10-12 | 航空工业矿石公司 | Method for purifying flue gas |
| CN102247742A (en) * | 2011-07-15 | 2011-11-23 | 攀钢集团攀枝花钢钒有限公司 | Purification process for sintering flue gas desulfurization solution |
| CN105623710A (en) * | 2016-04-06 | 2016-06-01 | 成都天丰清洁能源发展有限公司 | Method for desulfurizing gasoline product by using ionic liquid |
| CN111701436A (en) * | 2020-06-23 | 2020-09-25 | 湖北真诚纸业有限公司 | Novel dual-alkali desulfurization method |
| CN113117505A (en) * | 2019-12-31 | 2021-07-16 | 苏州安建环保科技有限公司 | Double-alkali flue gas desulfurization and dust removal system |
-
2008
- 2008-09-01 CN CNA2008101204161A patent/CN101342464A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102210966A (en) * | 2010-04-02 | 2011-10-12 | 航空工业矿石公司 | Method for purifying flue gas |
| CN105597504A (en) * | 2010-04-02 | 2016-05-25 | 爱邦中国有限责任公司 | Purifying method for flue gas |
| CN102247742A (en) * | 2011-07-15 | 2011-11-23 | 攀钢集团攀枝花钢钒有限公司 | Purification process for sintering flue gas desulfurization solution |
| CN105623710A (en) * | 2016-04-06 | 2016-06-01 | 成都天丰清洁能源发展有限公司 | Method for desulfurizing gasoline product by using ionic liquid |
| CN113117505A (en) * | 2019-12-31 | 2021-07-16 | 苏州安建环保科技有限公司 | Double-alkali flue gas desulfurization and dust removal system |
| CN111701436A (en) * | 2020-06-23 | 2020-09-25 | 湖北真诚纸业有限公司 | Novel dual-alkali desulfurization method |
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