CN102068876A - Flue gas desulfurization process - Google Patents
Flue gas desulfurization process Download PDFInfo
- Publication number
- CN102068876A CN102068876A CN2009102378771A CN200910237877A CN102068876A CN 102068876 A CN102068876 A CN 102068876A CN 2009102378771 A CN2009102378771 A CN 2009102378771A CN 200910237877 A CN200910237877 A CN 200910237877A CN 102068876 A CN102068876 A CN 102068876A
- Authority
- CN
- China
- Prior art keywords
- ionic liquid
- flue gas
- process according
- liquid solution
- absorb
- 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
Abstract
The invention provides a flue gas desulfurization process employing an ionic liquid. In the process, the ionic liquid is used as an absorbent, different types of absorption towers are adopted to absorb SO2 in the flue gas at the temperature of 0-200 DEG C under the pressure of 0.09-5.0 MPa, wherein gas-liquid countercurrent contact is adopted, various types of towers are adopted to improve a mass transfer effect so as to realize the emission of flue gas reaching the standard. The ionic liquid after absorbing the SO2 is pumped into a desorber through a pump and is subjected to deabsorption by adopting a heating and/or decompressing method, and SO2 is recovered. The desorbed ionic liquid enters the absorption towers to be reused. The process provided by the invention can be used for effectively removing the SO2 in the flue gas and recovering the SO2.
Description
Technical field
The present invention relates to the process of flue gas desulfurization.Particularly, the present invention relates to the process that ionic liquid solution is used for flue gas desulfurization.
Background technology
As everyone knows, coal accounts for about 70% in China's primary energy consumption, and wherein the raw coal more than 80% adopts the directly mode of burning.The direct burning of a large amount of coals produces SO
2, NO
2, air pollutants such as NO, CO, cause China to become typical coal-smoke pollution country, seriously restricted the sustainable development of China's economy.
SO
2Being one of main composition of air pollutants, also is one of major pollutants in the coal combustion flue gas, and it can be detrimental to health, and can form acid rain, and agroecological environment and crop yield are produced serious influence.Therefore, SO
2Emission control be the primary study direction in using energy source and environmental protection field always.
Flue gas desulfurization is for reducing pollutant emission, and it is significant to improve the ecological environment.The technical method of flue gas desulfurization is of a great variety, and the flue gas desulfurization technique of commercial Application can be divided into wet desulphurization and dry method (containing semidry method) desulfurization.Wet desulphurization adopts liquid-absorbant washing flue gas to remove SO
2, at present, using maximum is calcium method desulfur technology, this desulfur technology is to adopt lime stone or lime as desulfurization absorbent, have the low advantage of cost, but the accessory substance that this kind method is produced is low-grade gypsum, reclaim and the value of utilization low.Dry desulfurization is to use solid absorbent, adsorbent or catalyst to remove SO in the flue gas
2, method commonly used has active carbon adsorption, molecular sieve adsorption, oxidizing process and metal oxide absorption process etc.Adopt solid absorbent (catalyst) to absorb and transform SO
2, for example use catalyst such as supporting cupric oxide on active carbon or the active carbon to absorb SO
2Desulfurized effect is good, but Preparation of catalysts is loaded down with trivial details, price is high, regeneration cost is also high.
In addition, the technology that adopts liquid phase method to carry out flue gas desulfurization is also arranged at present, this method good absorbing effect, but traditional liquid phase method absorbent is organic amine or its mixture, organic amine in use might volatilize, and causes the waste and the secondary pollution of solvent.
Ionic liquid is by organic cation and inorganic or organic anion is formed is the salts substances of liquid condition under room temperature to 100 ℃.It is developed by traditional high-temperature molten salt, but with respect to the conventional ion compound, and ionic liquid is in a liquid state in the very wide temperature range near room temperature.Ionic liquid has a lot of good character: the liquid temperature wide ranges, from being lower than or, having good heat endurance and chemical stability near more than the room temperature to 300 ℃; Almost there is not vapour pressure; Ion liquid structure is adjustable, and character is controlled; All show good dissolving ability to much organic with inorganic substances, can dissolve multiple gases, as CO
2, SO
2, ethene, ethane etc.Based on above characteristic, ionic liquid is considered to a kind of environmentally friendly solvent.Ion liquid many character makes it be used in many fields such as synthetic, separation, electrochemistry, and progressively becomes the focus that new industrial circle is paid close attention to.Along with development of technology, ionic liquid more and more is used for the separation of separation field, particularly gas.Since its good assimilation effect, and be easy to desorption and regeneration after absorbing, and therefore, ionic liquid has obtained paying close attention to widely in the application of desulfuration field.Yet because of ion liquid viscosity is big, mass transfer waits shortcoming slowly, mostly document is that the report ionic liquid is to SO at present
2Absorption characteristic, and remove SO for ionic liquid
2Technology do not appear in the newspapers.
Summary of the invention
Purpose of the present invention is exactly the problem that exists in the existing desulphurization technological process in order to solve, and from the angle of sustainable development, improves SO
2Assimilation effect and the reproducible utilization of absorbent, reduce environmental pollution.
The objective of the invention is to adopt following technical scheme to realize.
The invention provides a kind of process of flue gas desulfurization, this method comprises makes ionic liquid solution contact with flue gas, to absorb SO in the flue gas
2Step.
Preferably, flue gas desulfurization technique method of the present invention also comprises making and absorbs SO
2After the ionic liquid solution that do not reach capacity contact with flue gas again, to absorb SO in the flue gas again
2Step.
Preferably, flue gas desulfurization technique method of the present invention also comprises absorption SO
2After the ionic liquid solution desorb remove SO
2Afterwards, contact with flue gas again, to absorb SO in the flue gas again
2Step.
Preferably, flue gas desulfurization technique method of the present invention comprises the steps:
(1) ionic liquid solution is contacted in the absorption tower with flue gas, to absorb the SO in the flue gas
2
(2) SO will be absorbed in the step (1)
2Ionic liquid solution is afterwards sent in the desorber, removes wherein SO with desorb
2, obtain regeneration of ionic liquid;
(3) regeneration of ionic liquid that obtains in the step (2) is mixed with ionic liquid solution, it is contacted with flue gas again, to absorb the SO in the flue gas again
2
In the process of above flue gas desulfurization, absorb or absorb again SO in the flue gas
2Condition be preferably 0～200 ℃ of temperature, pressure 0.09～5.0MPa; More preferably temperature is 40～150 ℃, pressure 0.1～1.0MPa.
In the process of above flue gas desulfurization, SO is removed in desorb
2Condition be preferably 40～300 ℃ of temperature, pressure 0.00001～0.1MPa; More preferably temperature is 60～200 ℃, and pressure is 0.0001～0.02MPa.
In the process of above flue gas desulfurization, described absorption tower is spray column, packed tower, plate column or combined absorption tower.
In the process of above flue gas desulfurization, described ionic liquid comprises guanidinium ionic liquid, alcamines ionic liquid, glyoxaline ion liquid, ion liquid of quaternaries, season phosphonium salt class ionic liquid, pyridines ionic liquid, thiazoles ionic liquid, triazole ionic liquid, pyrrolin class ionic liquid, Thiazoling type ionic liquid and benzotriazole ionic liquid; Preferably, described ionic liquid is TMG lactate ions liquid, ionic liquid of ethanolamine lactate, 1-(1-aminopropyl)-3-methylimidazole hexafluorophosphate ionic liquid or triethyl group ammonia lactate ions liquid.
In the process of above flue gas desulfurization, the content range of described ionic liquid solution intermediate ion liquid is preferably 50wt.%～99wt.%, more preferably 70wt.%～95wt.%.Ionic liquid solution herein is meant the ionic liquid solution that regeneration of ionic liquid was mixed with after ionic liquid solution before the desorb and the desorb, wherein, the content of the ionic liquid solution intermediate ion liquid that regeneration of ionic liquid was mixed with after the desorb can be identical with the content of ionic liquid solution intermediate ion liquid before the desorb, also can be different.
In the process of above flue gas desulfurization, the solvent of described ionic liquid solution comprises water, ethanol, ethylene glycol, acetone and methyl alcohol; Described solvent is preferably water.
In the process of above flue gas desulfurization, described ionic liquid solution volume flow is preferably 1: 10 with the ratio of flue gas volume flow～and 1: 1000, more preferably 1: 50～1: 500.
The present invention compared with prior art has following beneficial effect at least:
The present invention adopts ionic liquid solution as absorbent, itself and traditional SO
2Absorbent is compared, and has following advantage at least: do not have vapour pressure, ionic liquid solution recycles and reuses easily; Utilize ion liquid adjustability of structure to design and have absorption SO
2The ionic liquid of ability; Absorbed SO
2Discharge easily, so not only do not produce secondary pollution, can also realize SO
2Resource.
In addition, ionic liquid absorbs SO
2After, the viscosity of ionic liquid solution rises greatly, influences ion liquid transportation and dispersion, and then influences ionic liquid to SO
2Assimilation effect.The present invention adds solvent in ionic liquid, greatly reduce ion liquid viscosity, thereby solves the problem of ion liquid transportation and dispersion.Solvent used in the present invention is preferably water, adopts water as solvent, low price, and can not produce secondary pollution.
Below will be for a more detailed description to desulphurization technological process of the present invention:
The principle of flue gas desulfurization technique method provided by the invention is: use the functionalized ion liquid solution contain a small amount of solvent as absorbent, under different conditions, absorb SO in the flue gas by various absorption towers
2, to reduce SO in the flue gas
2Concentration; Absorb SO
2After ionic liquid solution, the heating and/or the decompression situation under, make SO
2Desorption (or desorb) comes out, and reaches SO
2Enrichment and ion liquid regeneration.
Employed ionic liquid in the flue gas desulfurization technique method provided by the invention specifically comprises guanidinium ionic liquid, alcamines ionic liquid, glyoxaline ion liquid, ion liquid of quaternaries, season phosphonium salt class ionic liquid, pyridines ionic liquid, thiazoles ionic liquid, triazole ionic liquid, pyrrolin class ionic liquid, Thiazoling type ionic liquid and benzotriazole ionic liquid etc.; List 4 kinds of ion liquid application examples in the embodiments of the invention, 4 kinds of ion liquid application principles of other ionic liquids and this are identical; The content of employed ionic liquid solution intermediate ion liquid is 50wt.%～99wt.%; Acceptance condition is pressure 0.09～5.0MPa, 0～200 ℃ of temperature; The absorption tower type comprises packed tower, plate column and combined absorption tower; The temperature of desorption is 40～300 ℃, and vacuum is 0.00001～0.1MPa.
According to an embodiment of the invention, the technological process and the method for operating of desulfurization provided by the invention are as follows:
As shown in Figure 1, through the flue gas of pretreatment temperature between 0～200 ℃, the air inlet 5 of 1 below enters in the tower from the absorption tower, distribution device is arranged in the tower, pressure is 0.09-5.0 (absolute pressure) MPa, flue gas passes packing layer or column plate, and the flue gas after the desulfurization is discharged in the gas outlet 6 of 1 top from the absorption tower.Ionic liquid and solvent (for example water) are mixed with ionic liquid solution according to a certain percentage, be driven into the top on absorption tower 1 with pump, 1 top, absorption tower is furnished with spray equipment, ionic liquid solution (absorption liquid) is disperseed, and ionic liquid solution contacts the SO that absorbs wherein with flue gas by packing layer or column plate
2, ionic liquid solution arrives the bottom on absorption tower afterwards.Contain high concentration SO
2Ionic liquid solution be driven into pump and carry out desorb in the desorber 2.Wherein, desorber 2 can be packed tower or spray column.The condition of desorb can be 40～300 ℃ of temperature, and pressure limit is 0.00001～0.1MPa.Handle SO by desorb
2With the solvent of partial ion liquid solution, for example moisture is separated by desorb.Because SO
2At this solvent, for example solubility is little in the water, and the sulfurous acid instability of generation is easily decomposed, and therefore, the two can natural separation, collects SO
2Ionic liquid after the desorb enters in the ionic liquid storage tank 4, after the mensuration moisture, solvent is added ionic liquid storage tank 4 via colvent inlet 3, is mixed with the ionic liquid solution that needs ratio again, returns the SO that absorbs again in the absorption tower 1 in the flue gas
2, realize recycling.The solvent that desorbs can reclaim, and utilizes once more as the ion liquid solvent of preparation.
In above-mentioned sulfur removal technology, other compositions comprise the content of solids in the replacement cycle of ionic liquid solution and the flue gas, and the desorb situation of ionic liquid solution is relevant.
In above-mentioned sulfur removal technology, soak time depends on SO in the flue gas
2The ratio of the volume flow of concentration, ionic liquid kind and assimilation effect, flue gas and ionic liquid solution and the effect of filler.Desorption time and desorption mode, desorption temperature are relevant with desorption pressure.
Compare with traditional absorption process, process provided by the invention has the following advantages at least: can reduce the secondary pollution of sweetening process, this process neither produces solid waste, as low-grade calcium sulfate, can not cause again organic solvent volatilization and and then the atmosphere pollution that produces; The present invention uses ionic liquid solution, but not simple ionic liquid has overcome the big and absorption SO of ionic liquid own viscosity
2The unfavorable factor that back viscosity is bigger improves ion liquid transporting and dispersive property greatly, improves to absorb SO
2Effect; The desulfurization expense of this technology is cheaper than conventional method, and absorbent also can reuse; Process of the present invention is because ionic liquid optionally absorbs SO
2, therefore, when desorb, can isolate the higher SO of purity
2, can be used for other a lot of aspects (raw material that for example prepares sulfuric acid), realize SO
2Resource, meet the requirement of sustainable development; Isolated solvent, moisture for example, the solvent that can be used as ionic liquid solution joins in the ionic liquid storage tank again, realizes solvent, for example saving of water resource.
Description of drawings
Fig. 1 is the flue gas desulfurization technique flow chart according to an embodiment of the invention; Wherein, 1. absorption tower; 2. desorber; 3. colvent inlet; 4. ionic liquid storage tank; 5. air inlet; 6. gas outlet.
The specific embodiment
Below in conjunction with embodiment desulphurization technological process provided by the invention is described in further detail, but not thereby limiting the invention.
It is absorbent that TMG lactate ions liquid solution is adopted in the present embodiment explanation, and packed tower at 60 ℃, absorbs SO in the flue gas as the absorption tower under the condition of 0.1MPa
2Technology.
The TMG lactate is mixed with the aqueous solution of mass fraction 50%.From the flue gas that coal-burning boiler comes out, through after the dust removal process, flue-gas temperature is 150 ℃, SO
2Content is 2150mg/m
3, cool to 60 ℃, to send in the absorption tower, the absorption tower internal pressure is 0.1MPa.The ratio of ionic liquid solution consumption and flue gas flow is 1: 1000 (V/V), and the absorption tower is a packed tower, in Raschig ring is housed as filler.The top on absorption tower is feed tube, and liquid distributor is installed, and the bottom is an air inlet, and distribution device is arranged.Tail gas enters in the absorption tower from bottom air inlet and carries out contact mass transfer with ionic liquid solution at filling surface.Through mass transfer, the SO in the flue gas
2Absorbed by ionic liquid solution.Flue gas after being purified is discharged from the top, absorbs SO
2After ionic liquid solution (absorption liquid) flow at the bottom of the tower and discharge.Rich SO
2Ionic liquid solution emit from the bottom after, at 200 ℃, under the pressure of 0.1MPa, in the spray desorption that reduces pressure in the desorber, SO
2Come out SO in the ionic liquid solution behind the desorption by desorption with steam
2Content is 0.1%, and ionic liquid obtains regeneration.The aqueous solution (50wt.%) that ionic liquid after the regeneration is mixed with again certain content is reused.Desulfuration efficiency is 98.7%.
It is absorbent that ionic liquid of ethanolamine lactate solution is adopted in the present embodiment explanation, and conventional plate column at 60 ℃, absorbs SO in the flue gas as the absorption tower under the condition of 1.0MPa
2Technology.
Ethanolamine lactate is mixed with the aqueous solution of mass fraction 90%.From the boiler tail gas discharged, through after the dust removal process, SO
2Content is 2150mg/m
3, cool to 60 ℃.In order to improve assimilation effect, flue gas is boosted to 1.0MPa, to send in the absorption tower, the absorption tower internal pressure is 1.0MPa.The ratio of the volume of ionic liquid consumption and flue gas flow is 1: 60, and the absorption tower is a plate column.The top on absorption tower is feed tube, and liquid distributor is installed, and the bottom is an air inlet, and distribution device is arranged.Tail gas enters in the absorption tower from air inlet and carries out contact mass transfer with ionic liquid solution in tray surfaces.Through mass transfer, the SO in the flue gas
2Absorbed by ionic liquid solution.Flue gas after being purified is discharged from the top, absorbs SO
2After ionic liquid solution (absorption liquid) flow at the bottom of the tower and discharge.Rich SO
2Ionic liquid solution emit from the bottom after, at 60 ℃, under the pressure of 0.00001MPa, in the plate column desorption that reduces pressure, SO
2Come out SO in the ionic liquid solution behind the desorption by desorption with steam
2Content is 0.4%.Ionic liquid obtains regeneration.Ionic liquid after the regeneration is mixed with the solution (90wt.%) that contains certain water again to reuse.Desulfuration efficiency is up to 99.5%.
It is absorbent that 1-(1-aminopropyl)-3-methylimidazole hexafluorophosphate ionic liquid solution is adopted in the present embodiment explanation, and spray column at 70 ℃, absorbs SO in the flue gas as the absorption tower under the condition of 5.0MPa
2Technology.
1-(1-aminopropyl)-3-methylimidazole hexafluorophosphate is mixed with the aqueous solution of mass fraction 95%.From the boiler tail gas discharged, through after the dust removal process, flue-gas temperature is 150 ℃, SO
2Content is 2150mg/m
3, cooling to 70 ℃, supercharging is sent in the absorption tower, and the absorption tower internal pressure is 5.0MPa.The ratio of the volume of ionic liquid consumption and flue gas flow is 1: 10.The absorption tower is a spray column.The top on absorption tower is feed tube, and the bottom is an air inlet, and distribution device is arranged.Tail gas enters in the absorption tower and ionic liquid solution contact mass transfer in tower from air inlet.Through mass transfer, the SO in the flue gas
2Absorbed by ionic liquid solution.Flue gas after being purified is discharged from the top, absorbs SO
2After ionic liquid solution (absorption liquid) flow at the bottom of the tower and discharge.Rich SO
2Ionic liquid solution emit from the bottom after, at 100 ℃, under the pressure of 0.002MPa, at the plate column desorption that reduces pressure, SO
2Come out SO in the ionic liquid solution behind the desorption by desorption with steam
2Content is 0.5%.Ionic liquid recovers original character.Ionic liquid is mixed with the aqueous solution (95wt.%) again to reuse.Desulfuration efficiency reaches 99.9%.
It is absorbent that triethyl group ammonia lactate ions liquid solution is adopted in the present embodiment explanation, and packed column at 40 ℃, absorbs the SO in the flue gas as the absorption tower under the condition of 1.0MPa
2Technology.
Triethyl group ammonia lactate is mixed with the aqueous solution of mass fraction 95%, pours in the fluid reservoir on absorption tower.From the sinter fume of steel mill, through after the dust removal process, flue-gas temperature is 150 ℃, SO
2Content is 2550mg/m
3, cool to 40 ℃, to send in the absorption tower, the absorption tower internal pressure is 1.0MPa.The ratio of the volume of ionic liquid consumption and flue gas flow is 1: 100.The absorption tower is a packed column.The top on absorption tower is feed tube, and the bottom is an air inlet, and distribution device is arranged.Tail gas enters in the absorption tower and ionic liquid solution contact mass transfer in tower from air inlet.Through mass transfer, the SO in the flue gas
2Absorbed by ionic liquid solution.Flue gas after being purified is discharged from the top, absorbs SO
2After ionic liquid solution (absorption liquid) flow at the bottom of the tower and discharge.Rich SO
2Ionic liquid solution emit from the bottom after, at 90 ℃, under the pressure of 0.001MPa, the desorption that in plate column, reduces pressure, SO
2Come out SO in the ionic liquid solution behind the desorption by desorption with steam
2Content is 0.4%.Ionic liquid recovers original character.Ionic liquid is mixed with the aqueous solution (95wt.%) again to reuse.The desulfuration efficiency height is reached for 99.6%.
Embodiment 5
It is absorbent that the TMG lactate solution is adopted in the present embodiment explanation, and packed tower at 60 ℃, absorbs the SO in the flue gas as the absorption tower under the condition of 0.1MPa
2Technology.
The TMG lactate is mixed with the aqueous solution of mass fraction 99%, pours in the fluid reservoir on absorption tower.From the boiler tail gas discharged, through after the dust removal process, flue-gas temperature is 150 ℃, SO
2Content is 2150mg/m
3, cool to 60 ℃, to send in the absorption tower, the absorption tower internal pressure is 0.1MPa.The ratio of the volume of ionic liquid consumption and flue gas flow is 1: 500, and the absorption tower is a packed tower, in Raschig ring is housed as filler.The top on absorption tower is feed tube, and liquid distributor is installed, and the bottom is an air inlet, and distribution device is arranged.Tail gas enters in the absorption tower from bottom air inlet and carries out contact mass transfer with ionic liquid solution at filling surface.Through mass transfer, the SO in the flue gas
2Absorbed by ionic liquid solution.Flue gas after being purified is discharged from the top, absorbs SO
2After ionic liquid solution (absorption liquid) flow at the bottom of the tower and discharge.Rich SO
2Ionic liquid solution emit from the bottom after, at 120 ℃, under the pressure of 0.00001MPa, in the spray desorption that reduces pressure in the desorber, SO
2Come out SO in the ionic liquid solution behind the desorption by desorption with steam
2Content is 0.1%, and ionic liquid obtains regeneration.The aqueous solution (99wt.%) that ionic liquid after the regeneration is mixed with again certain content is reused.Owing to ion liquidly transport with dispersion effect badly, desulfuration efficiency is 72.7%.
Claims (10)
1. the process of a flue gas desulfurization, this method comprises makes ionic liquid solution contact with flue gas, to absorb SO in the flue gas
2Step.
2. process according to claim 1 is characterized in that, described method also comprises makes absorption SO
2After the ionic liquid solution that do not reach capacity contact with flue gas again, to absorb SO in the flue gas again
2Step.
3. process according to claim 1 is characterized in that described method also comprises absorption SO
2After the ionic liquid solution desorb remove SO
2Afterwards, contact with flue gas again, to absorb SO in the flue gas again
2Step.
4. process according to claim 1 is characterized in that described method comprises the steps:
(1) ionic liquid solution is contacted in the absorption tower with flue gas, to absorb the SO in the flue gas
2
(2) SO will be absorbed in the step (1)
2Ionic liquid solution is afterwards sent in the desorber, removes wherein SO with desorb
2, obtain regeneration of ionic liquid;
(3) regeneration of ionic liquid that obtains in the step (2) is mixed with ionic liquid solution, it is contacted with flue gas again, to absorb the SO in the flue gas again
2
5. process according to claim 4 is characterized in that, absorbs or absorb SO in the flue gas
2Condition be preferably 0～200 ℃ of temperature, pressure 0.09～5.0MPa; More preferably temperature is 40～150 ℃, pressure 0.1～1.0MPa.
6. process according to claim 4 is characterized in that SO is removed in desorb
2Condition be preferably 40～300 ℃ of temperature, pressure 0.00001～0.1MPa; More preferably temperature is 60～200 ℃, and pressure is 0.0001～0.02MPa.
7. process according to claim 4 is characterized in that, described absorption tower and desorber include spray column, packed tower, plate column or combined absorption tower.
8. process according to claim 4, it is characterized in that described ionic liquid comprises guanidinium ionic liquid, alcamines ionic liquid, glyoxaline ion liquid, ion liquid of quaternaries, season phosphonium salt class ionic liquid, pyridines ionic liquid, thiazoles ionic liquid, triazole ionic liquid, pyrrolin class ionic liquid, Thiazoling type ionic liquid and benzotriazole ionic liquid; Preferably, described ionic liquid is TMG lactate ions liquid, ionic liquid of ethanolamine lactate, 1-(1-aminopropyl)-3-methylimidazole hexafluorophosphate ionic liquid or triethyl group ammonia lactate ions liquid.
9. process according to claim 4 is characterized in that, the content range of described ionic liquid solution intermediate ion liquid is preferably 50wt.%～99wt.%, more preferably 70wt.%～95wt.%.Solvent for use comprises water, ethanol, ethylene glycol, acetone and methyl alcohol; Described solvent is preferably water.
10. process according to claim 4 is characterized in that, described ionic liquid solution volume flow is preferably 1: 10 with the ratio of flue gas volume flow～and 1: 1000, more preferably 1: 50～1: 500.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102378771A CN102068876A (en) | 2009-11-20 | 2009-11-20 | Flue gas desulfurization process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009102378771A CN102068876A (en) | 2009-11-20 | 2009-11-20 | Flue gas desulfurization process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102068876A true CN102068876A (en) | 2011-05-25 |
Family
ID=44027755
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009102378771A Pending CN102068876A (en) | 2009-11-20 | 2009-11-20 | Flue gas desulfurization process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102068876A (en) |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102274674A (en) * | 2011-06-20 | 2011-12-14 | 浙江大学 | Method for capturing carbon dioxide (CO2) by high-stability substituted phenol ionic liquid |
| CN102302894A (en) * | 2011-07-15 | 2012-01-04 | 攀钢集团攀枝花钢钒有限公司 | Renewable flue gas desulphurization process |
| CN102807221A (en) * | 2011-12-13 | 2012-12-05 | 南京信息工程大学 | Method for recovering byproduct silicon tetrachloride produced in process of producing polycrystalline silicon |
| CN102941008A (en) * | 2012-11-21 | 2013-02-27 | 北京化工大学 | Method for absorbing SO2 by soluble calcium saline solution and regenerating absorbent |
| CN103203171A (en) * | 2012-01-12 | 2013-07-17 | 北京化工大学 | Technology for removing SO2 in smoke through recovery method |
| CN103949147A (en) * | 2014-05-14 | 2014-07-30 | 北京国电龙源环保工程有限公司 | Desulfurization method for purifying flue gas |
| CN105194982A (en) * | 2015-10-14 | 2015-12-30 | 黄锐 | Ionic liquid capable of absorbing sulfur dioxide as well as preparation method and application of ionic liquid |
| CN105214450A (en) * | 2015-10-14 | 2016-01-06 | 黄锐 | A kind of selective absorbing SO 2absorbent and absorb SO 2process |
| CN105214458A (en) * | 2015-09-11 | 2016-01-06 | 河北科技大学 | Absorb SO 2composite absorber and using method |
| CN105498451A (en) * | 2015-11-25 | 2016-04-20 | 河北科技大学 | Ether-based bis-imidazole ionic liquid binary system used for absorbing SO2, and preparation method and application method thereof |
| CN105967968A (en) * | 2016-07-01 | 2016-09-28 | 北京神雾环境能源科技集团股份有限公司 | Acetylene purification system and method |
| CN106310943A (en) * | 2016-08-31 | 2017-01-11 | 上海交通大学 | Device for regenerating sodium sulfite desulphurization liquid and recycling sulfur dioxide with sodium sulfite desulphurization liquid and application of device |
| CN106422611A (en) * | 2016-08-09 | 2017-02-22 | 长安大学 | Sprinkling agent for reducing content of PM2.5 of haze producing matters in car exhaust gas |
| CN107349754A (en) * | 2017-08-28 | 2017-11-17 | 重庆千卡科技有限公司 | A kind of desulfurizing agent composition and sulfur method |
| CN107596866A (en) * | 2012-02-01 | 2018-01-19 | 耶路撒冷希伯来大学伊萨姆研究开发有限公司 | For the method for the emission for controlling flue gas |
| CN108993098A (en) * | 2018-08-13 | 2018-12-14 | 中国地质大学（北京） | A kind of efficiently trapping CO2Eutectic solvent system and the preparation method and application thereof |
| CN109439924A (en) * | 2018-12-05 | 2019-03-08 | 湖南锐异资环科技有限公司 | A kind of processing method of secondary lead-containing material |
| CN109517999A (en) * | 2018-12-05 | 2019-03-26 | 湖南锐异资环科技有限公司 | Side-blowing smelting method for secondary lead-containing material |
| CN109876601A (en) * | 2019-03-19 | 2019-06-14 | 北京化工大学 | A kind of functionalized ion liquid absorbing sulfur dioxide in flue and with the process of claus reaction low-temp recovery |
| CN111821813A (en) * | 2020-06-22 | 2020-10-27 | 江苏中江材料技术研究院有限公司 | Ternary eutectic solvent and method for adsorbing sulfur dioxide by using same |
| CN114367170A (en) * | 2021-12-13 | 2022-04-19 | 武钢资源集团有限公司 | Method for enriching sulfur dioxide in flue gas |
| CN115318080A (en) * | 2022-08-10 | 2022-11-11 | 浙江工业大学 | Liquid phase absorption purification method of industrial nitrogen oxide flue gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101063046A (en) * | 2007-06-07 | 2007-10-31 | 中国科学院过程工程研究所 | Oil sulfur removal method based on ion liquid |
| CN101264414A (en) * | 2008-04-23 | 2008-09-17 | 合肥工业大学 | Green high-efficiency recyclable SO2 gas absorbent and preparation thereof |
-
2009
- 2009-11-20 CN CN2009102378771A patent/CN102068876A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101063046A (en) * | 2007-06-07 | 2007-10-31 | 中国科学院过程工程研究所 | Oil sulfur removal method based on ion liquid |
| CN101264414A (en) * | 2008-04-23 | 2008-09-17 | 合肥工业大学 | Green high-efficiency recyclable SO2 gas absorbent and preparation thereof |
Non-Patent Citations (1)
| Title |
|---|
| 焦真等: "用于脱除酸性气体的离子液体型吸收剂研究进展", 《现代化工》 * |
Cited By (30)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102274674A (en) * | 2011-06-20 | 2011-12-14 | 浙江大学 | Method for capturing carbon dioxide (CO2) by high-stability substituted phenol ionic liquid |
| CN102274674B (en) * | 2011-06-20 | 2013-10-23 | 浙江大学 | Method for capturing carbon dioxide (CO2) by high-stability substituted phenol ionic liquid |
| CN102302894A (en) * | 2011-07-15 | 2012-01-04 | 攀钢集团攀枝花钢钒有限公司 | Renewable flue gas desulphurization process |
| CN102302894B (en) * | 2011-07-15 | 2013-06-19 | 攀钢集团攀枝花钢钒有限公司 | Renewable flue gas desulphurization process |
| CN102807221A (en) * | 2011-12-13 | 2012-12-05 | 南京信息工程大学 | Method for recovering byproduct silicon tetrachloride produced in process of producing polycrystalline silicon |
| CN103203171A (en) * | 2012-01-12 | 2013-07-17 | 北京化工大学 | Technology for removing SO2 in smoke through recovery method |
| CN107596866A (en) * | 2012-02-01 | 2018-01-19 | 耶路撒冷希伯来大学伊萨姆研究开发有限公司 | For the method for the emission for controlling flue gas |
| CN102941008A (en) * | 2012-11-21 | 2013-02-27 | 北京化工大学 | Method for absorbing SO2 by soluble calcium saline solution and regenerating absorbent |
| CN102941008B (en) * | 2012-11-21 | 2015-04-29 | 北京化工大学 | Method for absorbing SO2 by soluble calcium saline solution and regenerating absorbent |
| CN103949147B (en) * | 2014-05-14 | 2015-11-25 | 北京国电龙源环保工程有限公司 | A kind of sulfur method for gas cleaning |
| CN103949147A (en) * | 2014-05-14 | 2014-07-30 | 北京国电龙源环保工程有限公司 | Desulfurization method for purifying flue gas |
| CN105214458A (en) * | 2015-09-11 | 2016-01-06 | 河北科技大学 | Absorb SO 2composite absorber and using method |
| CN105194982A (en) * | 2015-10-14 | 2015-12-30 | 黄锐 | Ionic liquid capable of absorbing sulfur dioxide as well as preparation method and application of ionic liquid |
| CN105214450A (en) * | 2015-10-14 | 2016-01-06 | 黄锐 | A kind of selective absorbing SO 2absorbent and absorb SO 2process |
| CN105498451A (en) * | 2015-11-25 | 2016-04-20 | 河北科技大学 | Ether-based bis-imidazole ionic liquid binary system used for absorbing SO2, and preparation method and application method thereof |
| CN105967968A (en) * | 2016-07-01 | 2016-09-28 | 北京神雾环境能源科技集团股份有限公司 | Acetylene purification system and method |
| CN106422611A (en) * | 2016-08-09 | 2017-02-22 | 长安大学 | Sprinkling agent for reducing content of PM2.5 of haze producing matters in car exhaust gas |
| CN106422611B (en) * | 2016-08-09 | 2018-10-30 | 长安大学 | A kind of spray agent for reducing production haze object PM2.5 contents in vehicle exhaust |
| CN106310943B (en) * | 2016-08-31 | 2018-11-16 | 上海交通大学 | A kind of sodium sulfite desulfurization regeneration and recycling sulfur dioxide device and application |
| CN106310943A (en) * | 2016-08-31 | 2017-01-11 | 上海交通大学 | Device for regenerating sodium sulfite desulphurization liquid and recycling sulfur dioxide with sodium sulfite desulphurization liquid and application of device |
| CN107349754B (en) * | 2017-08-28 | 2020-08-28 | 重庆千卡科技有限公司 | Desulfurizing agent composition and desulfurizing method |
| CN107349754A (en) * | 2017-08-28 | 2017-11-17 | 重庆千卡科技有限公司 | A kind of desulfurizing agent composition and sulfur method |
| CN108993098A (en) * | 2018-08-13 | 2018-12-14 | 中国地质大学（北京） | A kind of efficiently trapping CO2Eutectic solvent system and the preparation method and application thereof |
| CN108993098B (en) * | 2018-08-13 | 2021-04-13 | 中国地质大学（北京） | Efficient CO capture2Eutectic solvent system and preparation method and application thereof |
| CN109439924A (en) * | 2018-12-05 | 2019-03-08 | 湖南锐异资环科技有限公司 | A kind of processing method of secondary lead-containing material |
| CN109517999A (en) * | 2018-12-05 | 2019-03-26 | 湖南锐异资环科技有限公司 | Side-blowing smelting method for secondary lead-containing material |
| CN109876601A (en) * | 2019-03-19 | 2019-06-14 | 北京化工大学 | A kind of functionalized ion liquid absorbing sulfur dioxide in flue and with the process of claus reaction low-temp recovery |
| CN111821813A (en) * | 2020-06-22 | 2020-10-27 | 江苏中江材料技术研究院有限公司 | Ternary eutectic solvent and method for adsorbing sulfur dioxide by using same |
| CN114367170A (en) * | 2021-12-13 | 2022-04-19 | 武钢资源集团有限公司 | Method for enriching sulfur dioxide in flue gas |
| CN115318080A (en) * | 2022-08-10 | 2022-11-11 | 浙江工业大学 | Liquid phase absorption purification method of industrial nitrogen oxide flue gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102068876A (en) | Flue gas desulfurization process | |
| Hanif et al. | Sulfur dioxide removal: An overview of regenerative flue gas desulfurization and factors affecting desulfurization capacity and sorbent regeneration | |
| CN101993378B (en) | Amido-containing ionic liquid used for absorbing acidic gases and preparation method and application thereof | |
| CN107715845B (en) | Flue gas desulfurization and denitrification adsorbent and preparation and use methods thereof | |
| CN201333374Y (en) | Device capable of collecting carbon dioxide contained in flue gases of power plant through ammonia by utilizing void tower | |
| CN105289209A (en) | Mixed organic solution for trapping CO2 and SO2 acid gas through phase transformation | |
| CN103877828B (en) | A kind of method of regeneration of absorption solution and special purpose device thereof | |
| JP2012530597A (en) | Removal of acid gas using absorbent containing stripping aid | |
| CN101036851A (en) | Method and apparatus for processing waste air including oxynitride | |
| KR101207532B1 (en) | Apparatus for performing drying and removing impurities process of bio-methane at high purity bio-methane purification system | |
| CN105214445A (en) | A kind of amine absorbent for removing sulfur dioxide in gaseous mixture | |
| CN102695553A (en) | Alcohol-based gas stripping process | |
| CN102580342A (en) | Process method for regenerating ionic liquid and separating and recovering absorbents | |
| CN103949147A (en) | Desulfurization method for purifying flue gas | |
| CN101537304B (en) | Cyclic amine sulfur dioxide gas absorbent and preparation method thereof | |
| CN103521035A (en) | High-efficiency desulfurizing combined solvent | |
| CN101537300B (en) | Recyclable sulfur dioxide gas absorbent and preparation method thereof | |
| CN103170216A (en) | Alcohol amine type ion liquor-containing compound absorbent capable of capturing carbon dioxide | |
| CN103752137B (en) | A kind of method containing ether pyridine ionic liquid trapping sour gas | |
| CN114832584A (en) | CO based on two-phase absorbent rich liquid concentrated phase desorption 2 Trapping system and method | |
| CN109529555B (en) | Eutectic solvent based on aprotic organic matter and method for efficiently absorbing sulfur dioxide by using eutectic solvent | |
| CN101890284A (en) | Method and device for obtaining CO2 from discharged gas fume | |
| CN109593583B (en) | Hydrogen sulfide removal system and desulfurization method | |
| CN105214450B (en) | A kind of selective absorbing SO2Absorbent and absorb SO2Process | |
| CN110801710B (en) | Gas trapping agent and preparation method and application thereof |
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: 20110525 |