CN102728206A - Device for flue gas desulfurization by sodium-calcium double alkali method - Google Patents
Device for flue gas desulfurization by sodium-calcium double alkali method Download PDFInfo
- Publication number
- CN102728206A CN102728206A CN2012102524214A CN201210252421A CN102728206A CN 102728206 A CN102728206 A CN 102728206A CN 2012102524214 A CN2012102524214 A CN 2012102524214A CN 201210252421 A CN201210252421 A CN 201210252421A CN 102728206 A CN102728206 A CN 102728206A
- Authority
- CN
- China
- Prior art keywords
- outlet
- links
- sodium
- oxidation
- solution
- 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.)
- Pending
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a device for flue gas desulfurization, in particular to a device for flue gas desulfurization by a sodium-calcium double alkali method. The invention provides a device for flue gas desulfurization by the sodium-calcium double alkali method, which can more thoroughly oxidize sulfite so as to obtain higher-quality gypsum. The device comprises a desulfurizing absorption tower, a replacement reactor and an oxidation tank, wherein the desulfurizing absorption tower is provided with a sulfur-containing flue gas inlet, a purified flue gas outlet, a desulfurized rich liquid outlet and a desulfurizing liquid inlet; the replacement reactor is provided with a liquid inlet, a reactant outlet and a lime water inlet; the oxidation tank is provided with a before-oxidation desulfurized rich liquid inlet, an after-oxidation desulfurized rich liquid outlet, an air inlet and an air outlet; the desulfurized rich liquid outlet of the desulfurizing absorption tower is connected with the before-oxidation desulfurized rich liquid inlet of the oxidation tank by a pipeline; and the after-oxidation desulfurized rich liquid outlet of the oxidation tank is connected with the liquid inlet of the replacement reactor by a pipeline.
Description
Technical field
The present invention relates to a kind of flue gas desulfur device, especially a kind of flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device.
Background technology
The basic process of existing soda dual alkali scrubbing FGD process is that sulfur-containing smoke gas is made desulfurization absorbent solution with NaOH or sodium carbonate; At first carry out desulfurization in desulfuration absorbing tower inside with reverse contact of flue gas, the liquid in desulfuration absorbing tower behind the absorption sulphur is called the desulfurization rich solution, and the desulfurization rich solution mainly contains sodium sulfite; Then all desulfurization rich solutions are reacted with limewash in metathesis reactor; Generation calcium sulfite deposition displaces NaOH simultaneously, and bubbling air becomes calcium sulfate with calcium sulfite oxidation again; Through after the Separation of Solid and Liquid, sodium hydroxide solution returns desulfuration absorbing tower and recycles.
The main deficiency that above-mentioned flue gas desulfurization by sodium-calcium dual-alkali scrubbing method process unit exists technically:
The one, flue gas directly directly cools off with doctor solution in desulfuration absorbing tower, and the waste heat in the flue gas can not get recycling, and causes energy waste, and desulfurizing tower flue band water is many in addition;
The 2nd, the institute of desulfuration absorbing tower is to have the desulfurization rich solution all can enter into metathesis reactor to react, and the amount of desulfurization rich solution is just bigger like this, and therefore corresponding regenerative system specification of equipment is just bigger, causes construction investment huge, and desulphurization cost is too high;
The 3rd, calcium ions height in the recycle hydrogen sodium hydroxide solution in the entering desulfuration absorbing tower generates calcium sulfite with the sulfur dioxide reaction in desulfuration absorbing tower, cause relevant device and pipeline seriously to stop up, and often shut-down (breakdown) mainteance influences the main device production in the upper reaches;
The 4th, absorb rich solution and limewash reaction back and generate the calcium sulfite solid sediment, gas-liquid is difficult to complete intact contact when the bubbling air oxidation, and oxidation is not thorough, and the gypsum of generation is unstable, does not have value.
Summary of the invention
It is more thorough that technical problem to be solved by this invention provides a kind of sulfite oxidation that makes, and obtains the flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device of the higher gypsum of quality.
The present invention solves the flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device that its technical problem adopts; Comprise desulfuration absorbing tower, metathesis reactor and oxidation tank; Said desulfuration absorbing tower is provided with sulfur-containing smoke gas import, flue outlet, the outlet of desulfurization rich solution and doctor solution import; Said metathesis reactor is provided with liquid-inlet, reactant outlet and limewash import; Said oxidation tank is provided with desulfuration solution outlet after desulfurization rich solution import before the oxidation, the oxidation, air intlet and air outlet slit; The import of desulfurization rich solution links to each other through pipeline before the oxidation of the outlet of the desulfurization rich solution of said desulfuration absorbing tower and said oxidation tank, and desulfuration solution exports and links to each other through pipeline with the liquid-inlet of said metathesis reactor after the oxidation of said oxidation tank.
Further be; Also comprise the heat recovery cooler; Said heat recovery cooler is provided with gas approach and exhanst gas outlet, and said gas approach links to each other with the sulfur-containing smoke gas pipeline, and said exhanst gas outlet links to each other through pipeline with the sulfur-containing smoke gas import of said desulfuration absorbing tower; The flow direction with sulfur-containing smoke gas is reference, and the heat recovery cooler is made up of the low-temperature zone after being arranged on preceding high temperature section and being arranged on.
Further be that said sulfur-containing smoke gas pipeline is provided with the emergent program control butterfly valve of contact and cuts off flashboard.
Further be that the desulfurization rich solution outlet of said desulfuration absorbing tower also links to each other with said doctor solution import through pipeline.
Further be; Also comprise the circulation solution filter press; On the flow direction of desulfurization rich solution; The outlet of the desulfurization rich solution of said desulfuration absorbing tower at first with said circulation solution filter press, and then link to each other respectively through desulfurization rich solution import before the oxidation of said circulation solution filter press and said doctor solution import, said oxidation tank.
Further be that said circulation solution filter press leads to and is connected with sodium carbonate liquor on the pipeline of said oxidation tank and adds pipeline.
Further be; Also comprise decalcification reactor and regeneration alkali lye storage tank; Said decalcification reactor links to each other with the outlet of said metathesis reactor; The alkali lye outlet of said decalcification reactor links to each other with the regeneration alkali lye import of said regeneration alkali lye storage tank, and the regeneration alkali lye outlet of said regeneration alkali lye storage tank links to each other with the doctor solution import of said desulfuration absorbing tower.
Further be; Also comprise regeneration alkali lye filter press; On the flow direction of regeneration alkali lye, the outlet of the alkali lye of said decalcification reactor at first links to each other with said regeneration alkali lye filter press, links to each other with the regeneration alkali lye import of said regeneration alkali lye storage tank through regeneration alkali lye filter press again.
Further be, also comprise the gypsum filter press, the outlet of said metathesis reactor at first links to each other with said gypsum filter press, and then links to each other with said decalcification reactor through the gypsum filter press.
Further be, also comprise chimney, said chimney links to each other with the flue outlet of said desulfuration absorbing tower.
The invention has the beneficial effects as follows: flowing on the direction; Oxidation tank is arranged on before the metathesis reactor, just at first sodium sulfite is oxidized to sodium sulphate, will generate NaOH and calcium sulfate with the sodium sulphate reaction through limewash again; Because sodium sulfite is water-soluble; Therefore just easier and air haptoreaction when oxidation has so not only improved efficient, and has been the more thorough of sulfite oxidation; The calcium sulfate purity that generates at last also is greatly improved, and such gypsum has also obtained the value on the industry.Before desulfuration absorbing tower, the heat recovery cooler can also be set, the heat recovery cooler can be divided into low-temperature zone and high temperature section, and the water of high temperature section heat absorption can be used for boiler and give hot water; The hot water that the low-temperature zone heat absorption produces can be used for circulating hot water and use; So just make that waste heat obtains utilizing, reduced carbon emission, reduced the temperature of sulfur-containing smoke gas simultaneously; Heating efficiency in desulfuration absorbing tower just reduces greatly, and the water amount in flue gas after being purified just reduces greatly like this.The outlet of the desulfurization rich solution of desulfuration absorbing tower also links to each other with said doctor solution import through pipeline, and the carrying out that the desulfurization absorption liquid can be repeatedly when the absorption sulfur-containing smoke gas improved the absorption efficiency of desulfurization absorption liquid.Decalcification reactor and regeneration alkali lye storage tank can also be set; At first react through the alkali lye that cements out like this through decalcification; Store again, be used for desulfuration absorbing tower at last, because the calcium ion in the alkali lye has obtained handling; In absorption process, just avoid the generation of calcium sulfite like this, prevented the obstruction of equipment.
Description of drawings
Fig. 1 is a sketch map of the present invention;
Parts, position and numbering among the figure: desulfuration absorbing tower 1, metathesis reactor 2, oxidation tank 3, heat recovery cooler 4, circulation solution filter press 5, decalcification reactor 6, regeneration alkali lye storage tank 7, gypsum filter press 8, limewash import 9, chimney 10, flue outlet 11, sulfur-containing smoke gas import 12, desulfurization rich solution outlet 13, doctor solution import 14, regeneration alkali lye filter press 20, liquid-inlet 21, reactant outlet 22, sodium carbonate liquor add pipeline 30.
The specific embodiment
Below in conjunction with accompanying drawing the present invention is described further.
As shown in Figure 1; The present invention includes desulfuration absorbing tower 1, metathesis reactor 2 and oxidation tank 3; Said desulfuration absorbing tower 1 is provided with sulfur-containing smoke gas import 12, flue outlet 11, the outlet 13 of desulfurization rich solution and doctor solution import 14; Said metathesis reactor 2 is provided with liquid-inlet 21, reactant outlet 22 and limewash import 9; Said oxidation tank 3 is provided with desulfuration solution outlet after desulfurization rich solution import before the oxidation, the oxidation, air intlet and air outlet slit; The import of desulfurization rich solution links to each other through pipeline before the oxidation of the outlet 13 of the desulfurization rich solution of said desulfuration absorbing tower 1 and said oxidation tank 3, and desulfuration solution exports with the liquid-inlet of said metathesis reactor 2 21 and links to each other through pipeline after the oxidation of said oxidation tank 3.In the desulfuration absorbing tower 1 main use sodium hydroxide solution with or sodium carbonate liquor carry out desulfurization, mainly contain sulfur dioxide in the sulfur-containing smoke gas, sulfur-containing smoke gas gets into from the bottom of desulfuration absorbing tower 1; Contact with the doctor solution that gets into from top, reaction generates water-soluble sodium sulfite solution, and the flue gas after the desulfurization is discharged from the top of desulfuration absorbing tower 1; Reacted solution is then discharged from the bottom of desulfuration absorbing tower 1; Reacted solution enters into oxidation tank 3 through piping, oxidation tank 3 can connect be provided with a plurality of, two among Fig. 1 for example; Continue in the oxidation tank 3 to inject air through air compressor; Sodium sulfite in the solution will be oxidized to sodium sulphate, and the solution of contains sodium sulfate flows in the metathesis reactor 2 through pipeline again, in contains sodium sulfate solution, adds limewash through limewash import 9; Reaction generates calcium sulfate and NaOH; Because calcium sulfate is to be slightly soluble in water, therefore promptly can be made into product through post precipitation uses gypsum, and remaining sodium hydroxide solution can enter into doctor solution import 14 once more and use as doctor solution.Through comparing and to know with existing method; Traditional structure at first is to carry out displacement reaction, and promptly the solution after the desulfurization at first gets in the displacement reaction device, generates the calcium sulfite and the NaOH that are slightly soluble in water; And then oxidation generates calcium sulfate in the displacement reaction device; Exist because calcium sulfite basically all is the form of solid, air is difficult to fully contact with calcium sulfite, so just causes the last calcium sulfate purity that generates lower.And the present invention utilizes oxidation tank 3 and metathesis reactor 2 to carry out oxidation reaction and displacement reaction respectively, and sodium sulfite is oxidation generation sodium sulphate in oxidation tank 3 at first, and this moment, sulphite was to be in dissolved state; High with the contact rate of air, efficiency is high, and is more thorough; The final sodium sulphate that generates; Sodium sulphate enters into metathesis reactor 2 reactions again and generates calcium sulfate, and the gypsum purity that generates like this is higher, satisfies the requirement of commercialization fully.
In order to recycle the heat in the sulfur-containing smoke gas; Reduce the water amount of flue gas, the present invention also comprises heat recovery cooler 4, and said heat recovery cooler 4 is provided with gas approach and exhanst gas outlet; Said gas approach links to each other with the sulfur-containing smoke gas pipeline; The sulfur-containing smoke gas import 12 of said exhanst gas outlet and said desulfuration absorbing tower 1 links to each other through pipeline, is reference with the flow direction of sulfur-containing smoke gas, heat recovery cooler 4 by the high temperature section before being arranged on be arranged on after low-temperature zone form.Heat recovery cooler 4 contains two sections endotherm sections; High temperature section is arranged on the gas approach near heat recovery cooler 4; Low-temperature zone is arranged on the exhanst gas outlet near heat recovery cooler 4, and the flue-gas temperature of high temperature section contact is higher, and its hot water that reclaims the heat generation can be used for boiler feedwater hot water; Thereby reduce the fuel consumption of boiler, reduce carbon emission.Flue-gas temperature through after the high temperature section absorption is reduced, and utilizes this moment low-temperature zone to continue recovery waste heat again, and the hot water of low-temperature zone absorption back generation can be used for circulating hot water and uses.Flue-gas temperature through heat recovery cooler 4 has obtained great reduction; Heating benefit to desulfuration solution after in desulfuration absorbing tower 1, reacting like this reduces greatly; When getting rid of flue gas, the water content in the flue gas reduces greatly, has so just reduced the influence to desulfuration solution concentration at last.
In order to prevent that the present invention from impacting upstream equipment, as shown in Figure 1, said sulfur-containing smoke gas pipeline is provided with the emergent program control butterfly valve of contact and cuts off flashboard.When this device something unexpected happened, can close the emergent program control butterfly valve of contact rapidly and cut off flashboard, thereby prevent that liquids and gases from impacting upstream equipment.
In the production of reality; Doctor solution once absorbs and can't full consumption finish at desulfuration absorbing tower 1; It is just intact with the sulfur dioxide reaction consumes to be that NaOH or sodium carbonate in the doctor solution can once not circulate, and the doctor solution that conventional method will only once circulate after just will absorbing enters into next equipment, and the amount of liquid of processing certainty is very big like this; Cause equipment huge, increased production cost.In order to form the continuous several times circulation, the desulfurization rich solution outlet 13 of desulfuration absorbing tower 1 according to the invention also links to each other with said doctor solution import 14 through pipeline.In the production of reality; Can be through the switching of each pipeline of valve control, doctor solution forms the desulfurization rich solution after absorption; Part desulfurization rich solution enters into oxidation tank 3 follow-up equipments such as grade and carries out subsequent reactions; Part desulfurization rich solution enters into desulfuration absorbing tower 1 again to be mixed once more with initiate NaOH or sodium carbonate and absorbs, and reality has formed continuous a plurality of circulation like this, and promptly doctor solution repeatedly absorbs and circulates and the desulfurization regeneration cycle of treatment; So both reduced the treating capacity of subsequent regeneration equipment in a large number; It is less that metathesis reactor 2 and oxidation tank 3 follow-up equipments such as grade just can be provided with, and practiced thrift fund cost thus, and circulation absorbs the utilization rate that can also improve doctor solution.
For impurity screening; As shown in Figure 1; Also comprise circulation solution filter press 5; On the flow direction of desulfurization rich solution, the desulfurization rich solution of said desulfuration absorbing tower 1 outlet 13 at first with said circulation solution filter press 5, and then link to each other respectively through desulfurization rich solution import before the oxidation of said circulation solution filter press 5 and said doctor solution import 14, said oxidation tank 3.The desulfurization rich solution at first passes through the filtration of circulation solution filter press 5, thereby reduces the impurity that it carries, and helps the work of follow-up equipment.
Said circulation solution filter press 5 leads to and is connected with sodium carbonate liquor on the pipeline of said oxidation tank 3 and adds pipeline 30.Additional sodium carbonate has two effects, one be can sodium carbonate and solution in calcium ion can react, generate the very little calcium carbonate of solubility, can remove during filtration, avoid getting into and bring calcium ion in the desulfuration absorbing tower in the circulation solution into.If get into circulating absorption solution calcium ions in the absorption tower, will react with sulfur dioxide, generate calcium sulfate precipitation, occluding device and pipeline.Second effect is the alkali lye that replenishment cycles desulphurization system solid is taken away; Sodium carbonate can absorb the sulfur dioxide that is dissolved in the rich solution; Thereby make to absorb more thoroughly, the corrosion that the sulfur dioxide of avoiding dissolving causes equipment and pipeline is with balance circulation fluid basicity.
Doctor solution after regeneration forms obstruction in desulfuration absorbing tower 1; As shown in Figure 1; Also comprise decalcification reactor 6 and regeneration alkali lye storage tank 7; Said decalcification reactor 6 links to each other with the outlet of said metathesis reactor 2, and the alkali lye outlet of said decalcification reactor 6 links to each other with the regeneration alkali lye import of said regeneration alkali lye storage tank 7, and the regeneration alkali lye outlet of said regeneration alkali lye storage tank 7 links to each other with the doctor solution import 14 of said desulfuration absorbing tower 1.Pass through in the regenerative sulfur binding liquid after metathesis reactor 2 is handled and still contain more calcium ion, if do not handle, then it understands the calcium sulfite that be slightly soluble in water with sulfur in smoke production after getting into desulfuration absorbing tower 1 again, causes the obstruction of pipeline.After regeneration finishes, extract reacting slurry out with the gyp mud pump, filter with plate and frame filter press; Filtrating is sent into decalcification reactor 6, with the NaOH that flushing with clean water solid, washing attach, washings deallocation system limewash; Solid is a gypsum, does merchandise sales after outward transport or further the processing.The present invention utilizes decalcification reactor 6 to remove most calcium ion, and deliming can adopt carbonate solution to handle, and the doctor solution of avoiding regenerating is in use produced calcium sulfite and resulted in blockage.Regeneration alkali lye storage tank 7 can store unnecessary doctor solution, in needs, uses, and each pipeline opens and closes and adopts valve control, and the mobile employing pump of liquid drives.In decalcification reactor 6; The solubility with temperature of calcium sulfate raises and reduces, and when solution temperature reached about 80-90 ℃, the solubility of calcium sulfate (gypsum) was very low; The calcium sulfate that dissolves in the solution this moment all becomes solid and precipitates, thereby has removed the calcium sulfate that is dissolved in the solution.
For the filter regeneration doctor solution; As shown in Figure 1; Also comprise regeneration alkali lye filter press 20; On the flow direction of regeneration alkali lye, the outlet of the alkali lye of said decalcification reactor 6 at first links to each other with said regeneration alkali lye filter press 20, links to each other with the regeneration alkali lye import of said regeneration alkali lye storage tank 7 through regeneration alkali lye filter press 20 again.Utilize regeneration alkali lye filter press 20 can filter out the impurity in the regenerative sulfur binding liquid after 6 processing of decalcification reactor.
In order to filter the regenerative sulfur binding liquid after metathesis reactor 2 is handled, as shown in Figure 1, also comprise gypsum filter press 8, the outlet of said metathesis reactor 2 at first links to each other with said gypsum filter press 8, and then links to each other with said decalcification reactor 6 through gypsum filter press 8.Utilize gypsum filter press 8 can isolate gypsum, thereby guarantee that the impurity content in the regenerative sulfur binding liquid is less.
For the unified flue gas of discharging, as shown in Figure 1, also comprise chimney 10, said chimney 10 links to each other with the flue outlet 11 of said desulfuration absorbing tower 1.Flue gas after desulfurization can be discharged through chimney 10, simultaneously, when device of the present invention is stopped using, can directly sulfur-containing smoke gas be discharged through chimney 10.
Claims (10)
1. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device; Comprise desulfuration absorbing tower (1), metathesis reactor (2) and oxidation tank (3); Said desulfuration absorbing tower (1) is provided with sulfur-containing smoke gas import (12), flue outlet (11), the outlet of desulfurization rich solution (13) and doctor solution import (14); Said metathesis reactor (2) is provided with liquid-inlet (21), reactant outlet (22) and limewash import (9); Said oxidation tank (3) is provided with desulfuration solution outlet after desulfurization rich solution import before the oxidation, the oxidation, air intlet and air outlet slit; It is characterized in that: the desulfurization rich solution outlet (13) of said desulfuration absorbing tower (1) links to each other through pipeline with the preceding desulfurization rich solution import of the oxidation of said oxidation tank (3), and the desulfuration solution outlet links to each other through pipeline with the liquid-inlet (21) of said metathesis reactor (2) after the oxidation of said oxidation tank (3).
2. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 1; It is characterized in that: also comprise heat recovery cooler (4); Said heat recovery cooler (4) is provided with gas approach and exhanst gas outlet; Said gas approach links to each other with the sulfur-containing smoke gas pipeline; Said exhanst gas outlet links to each other through pipeline with the sulfur-containing smoke gas import (12) of said desulfuration absorbing tower (1), is reference with the flow direction of sulfur-containing smoke gas, heat recovery cooler (4) by the high temperature section before being arranged on be arranged on after low-temperature zone form.
3. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 2 is characterized in that: said sulfur-containing smoke gas pipeline is provided with the emergent program control butterfly valve of contact and cuts off flashboard.
4. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 1 is characterized in that: the desulfurization rich solution outlet (13) of said desulfuration absorbing tower (1) also links to each other with said doctor solution import (14) through pipeline.
5. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 4; It is characterized in that: also comprise circulation solution filter press (5); On the flow direction of desulfurization rich solution; The desulfurization rich solution of said desulfuration absorbing tower (1) outlet (13) at first with said circulation solution filter press (5), and then link to each other respectively with the preceding desulfurization rich solution import of the oxidation of said doctor solution import (14), said oxidation tank (3) through said circulation solution filter press (5).
6. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 5 is characterized in that: said circulation solution filter press (5) leads to and is connected with sodium carbonate liquor on the pipeline of said oxidation tank (3) and adds pipeline (30).
7. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 1; It is characterized in that: also comprise decalcification reactor (6) and regeneration alkali lye storage tank (7); Said decalcification reactor (6) links to each other with the outlet of said metathesis reactor (2); The alkali lye outlet of said decalcification reactor (6) links to each other with the regeneration alkali lye import of said regeneration alkali lye storage tank (7), and the regeneration alkali lye outlet of said regeneration alkali lye storage tank (7) links to each other with the doctor solution import (14) of said desulfuration absorbing tower (1).
8. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 7; It is characterized in that: also comprise regeneration alkali lye filter press (20); On the flow direction of regeneration alkali lye; The alkali lye outlet of said decalcification reactor (6) at first links to each other with said regeneration alkali lye filter press (20), links to each other with the regeneration alkali lye import of said regeneration alkali lye storage tank (7) through regeneration alkali lye filter press (20) again.
9. flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device as claimed in claim 7; It is characterized in that: also comprise gypsum filter press (8); The outlet of said metathesis reactor (2) at first links to each other with said gypsum filter press (8), and then links to each other with said decalcification reactor (6) through gypsum filter press (8).
10. like the described flue gas desulfurization by sodium-calcium dual-alkali scrubbing method device of the arbitrary claim of claim 1 to 9, it is characterized in that: also comprise chimney (10), said chimney (10) links to each other with the flue outlet (11) of said desulfuration absorbing tower (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012102524214A CN102728206A (en) | 2012-07-20 | 2012-07-20 | Device for flue gas desulfurization by sodium-calcium double alkali method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012102524214A CN102728206A (en) | 2012-07-20 | 2012-07-20 | Device for flue gas desulfurization by sodium-calcium double alkali method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102728206A true CN102728206A (en) | 2012-10-17 |
Family
ID=46984928
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012102524214A Pending CN102728206A (en) | 2012-07-20 | 2012-07-20 | Device for flue gas desulfurization by sodium-calcium double alkali method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102728206A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111701436A (en) * | 2020-06-23 | 2020-09-25 | 湖北真诚纸业有限公司 | Novel dual-alkali desulfurization method |
| CN113058412A (en) * | 2021-03-25 | 2021-07-02 | 洛南环亚源铜业有限公司 | Waste gas treatment process and treatment device thereof |
| CN114011231A (en) * | 2021-11-30 | 2022-02-08 | 中冶南方都市环保工程技术股份有限公司 | System and method for desulfurizing blast furnace gas by using hot alkali liquor |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4388282A (en) * | 1981-12-22 | 1983-06-14 | Research-Cottrell, Inc. | Method for regeneration of sodium sulfite from spent flue gas desulfurization processes |
| CN101239275A (en) * | 2007-11-26 | 2008-08-13 | 山西晋丰环保工程有限公司 | Dual-alkali-gypsum method flue gas desulfurization technique |
| CN201578988U (en) * | 2009-11-20 | 2010-09-15 | 中电投远达环保工程有限公司 | Double circulation double alkali method flue gas desulfurization device |
| CN202700350U (en) * | 2012-07-20 | 2013-01-30 | 成都德美工程技术有限公司 | Device for desulfurizing flue gas by using sodium-calcium dual alkali method |
-
2012
- 2012-07-20 CN CN2012102524214A patent/CN102728206A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4388282A (en) * | 1981-12-22 | 1983-06-14 | Research-Cottrell, Inc. | Method for regeneration of sodium sulfite from spent flue gas desulfurization processes |
| CN101239275A (en) * | 2007-11-26 | 2008-08-13 | 山西晋丰环保工程有限公司 | Dual-alkali-gypsum method flue gas desulfurization technique |
| CN201578988U (en) * | 2009-11-20 | 2010-09-15 | 中电投远达环保工程有限公司 | Double circulation double alkali method flue gas desulfurization device |
| CN202700350U (en) * | 2012-07-20 | 2013-01-30 | 成都德美工程技术有限公司 | Device for desulfurizing flue gas by using sodium-calcium dual alkali method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111701436A (en) * | 2020-06-23 | 2020-09-25 | 湖北真诚纸业有限公司 | Novel dual-alkali desulfurization method |
| CN111701436B (en) * | 2020-06-23 | 2022-10-04 | 湖北真诚纸业有限公司 | Double-alkali desulfurization method |
| CN113058412A (en) * | 2021-03-25 | 2021-07-02 | 洛南环亚源铜业有限公司 | Waste gas treatment process and treatment device thereof |
| CN114011231A (en) * | 2021-11-30 | 2022-02-08 | 中冶南方都市环保工程技术股份有限公司 | System and method for desulfurizing blast furnace gas by using hot alkali liquor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108079762B (en) | Flue gas desulfurization system and method for flue gas desulfurization by using same | |
| CN101254392B (en) | Energy-saving type sodium sulphite circulation desulfurizing device and method | |
| CN103977664B (en) | A kind of method of flue gas desulfurization denitration dust-removing | |
| CN104826463B (en) | A kind of sour gas produces NaHS technique and device | |
| CN102357337A (en) | Desulphurization technology through sodium-calcium dual-alkali method | |
| CN103977689A (en) | Device and method for removing sulfur dioxide in smoke by two-step alkalifying reproducing and sodium sulfite method | |
| CN104226096B (en) | Multi-flow-path circulating desulfurization system and multi-flow-path circulating desulfurization method | |
| CN102728205A (en) | Method for flue gas desulfurization by sodium-calcium double alkali method | |
| CN102614768B (en) | Desulfurization reactor device | |
| CN202700350U (en) | Device for desulfurizing flue gas by using sodium-calcium dual alkali method | |
| CN102728206A (en) | Device for flue gas desulfurization by sodium-calcium double alkali method | |
| CN103638802A (en) | Device and method for processing acid gas of refinery plant | |
| TWI633923B (en) | Method and device for processing acid gas | |
| CN104971597A (en) | Technical method and device of producing sodium hydrosulfide from acid gas | |
| CN105727714B (en) | A kind of process and device for producing NaHS | |
| CN105642090B (en) | A kind of Acidic Gas Treating method and device | |
| CN201578988U (en) | Double circulation double alkali method flue gas desulfurization device | |
| CN104971601B (en) | Acid gas vertical reactor and processing method | |
| CN105498503B (en) | A kind of dual alkali scrubbing FGD process method and flue gas desulphurization system | |
| CN104016382A (en) | Method for producing sodium sulfite by desulfurizing flue gas by double-alkali process | |
| CN105731388B (en) | A kind of method and device for preparing NaHS | |
| CN211487169U (en) | Sodium-alkali method desulphurization device | |
| CN105727715B (en) | A kind of Acidic Gas Treating technique and system | |
| CN106345254A (en) | Method and device for treating hydrogen sulfide-containing gas | |
| CN203694899U (en) | Treatment device for acid gas of refinery plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20121017 |