CN1515349A - Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices - Google Patents
Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices Download PDFInfo
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- CN1515349A CN1515349A CNA031253237A CN03125323A CN1515349A CN 1515349 A CN1515349 A CN 1515349A CN A031253237 A CNA031253237 A CN A031253237A CN 03125323 A CN03125323 A CN 03125323A CN 1515349 A CN1515349 A CN 1515349A
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- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 82
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 239000003546 flue gas Substances 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title abstract description 12
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 67
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Abstract
The present invention provides a dry flue gas desulfurizing process with independent feeding, feeding back and water-spraying device. It includes desulfurizing agent preparation digestion system, desulfurizing reaction tower and desulfurizing reaction system and exterior desulfurizing granules separation and recirculating system. The water-spraying atomization device of desulfurizing reaction tower, desulfurizing agent feeding device and granules recirculating feed back device are independently placed, and the different heights of the desulfurizing reaction tower are equipped with respective nozzles, so that the structure can raise the utilization rate of the desulfurizing agent and can raise the desulfurizing effect.
Description
Technical field
The present invention relates to the dry flue gas desulphurization technology of a kind of independent feed back, feed and water spray, belong to the flue gas desulfurization technique field, dry method desulfuration system and technology in the particularly various combustion apparatus discharging flue gases.
Background technology
The improvement of sulfur dioxide gas body pollution is the emphasis of world's most countries environmental protection always, and its pollutant that produces causes the greatest contamination source of China's environmental destruction especially, has become the task of top priority of China's air pollution treatment at present.
Present improvement to sulfur dioxide, external general main employing wet type lime stone-gypsum method (W-FGD), adopt said method, though removal effect is better, investment is huge, water consumption is big but it exists, floor space is big, system complex, big, the complex structure of resistance, and need handle or the like a series of problems again to water.Therefore the high-efficiency flue gas desulfurization technology of dry type or half dry type becomes the emphasis of domestic and international research and development.
Desulfurization by dry method for the flue gas circulating fluidized bed method of present application, mostly desulfurizing agent (as calcium hydroxide etc.) and the isolated material of desulfurization reaction tower external discrete device are mixed earlier, together be injected in the desulfurization reaction tower then, this mode is because the influence of circulation feed back is difficult to guarantee that the desulfurizing agent fine particle can fully contact with particle water, sufficient surface devulcanization chemical reaction takes place, and the unreacted very difficult separated device of fine particle is completely separated, can enter atmosphere with flue gas, thereby reduced the desulfurizing agent utilization ratio, and be difficult to arrive the requirement of high desulfurization rate; Or earlier desulfurizing agent is made slurries.Spray into material that desulfurization reaction tower and external separator separate then as the circulation fluidized bed material, or earlier desulfurizing agent and feed back mixing and water adding are made slurries, spray into desulfurization reaction tower then, this dual mode not only water consumption is big, and very easily at desulfurization reaction tower internal face knot ash, expense height and desulfurized effect are poor.
At China's thermal power generation separate unit installed capacity is the flue gas desulfurization market demand of 600MW and the specific (special) requirements of power environment protection substantially, and country is to the reinforcement of water resource utilization protection.Simultaneously according to the objective law in flue gas desulfurization technique development and market in the world, advanced person's maximization (applicable to the above thermal power generation unit of 600MW) dry flue gas desulphurization technology will become the main force in domestic and international power environment protection technology and market.
But above-mentioned dry method (semidry method) desulfur technology, all do not have to consider after unit maximizes, because the increase of desulphurization reaction tower section and height will cause whole desulphurization reaction owing to the tissue failure in flue gas and particle flow field does not reach the desulfur technology requirement.
From above-mentioned introduction as seen, in the ciculation fluidized flue gas desulphurization system of dry method, the hybrid mode of feed, feed back and the feedwater of adopting mostly all is difficult to satisfy desulfuration efficiency higher under the low calcium-sulphur ratio at present, and system's operation water consumption is big, particularly when unit capacity increases, the more difficult requirement of satisfying low consumption, high desulfurization rate of this kind mode.
Summary of the invention
The problem that in engineering, exists at prior art and in the deficiency and the defective that exist aspect the maximization, the present invention proposes a kind of in the desulfurization reaction tower reaction zone, gas, solid, liquid three-phase mix fully, sorbent particle utilization rate height, the dry flue gas desulphurization technology of a kind of independent feed back, feed and water spray that desulphurization reaction speed is very fast, circulating resistance is lower.Adopt this kind technology, make it be issued to higher desulfuration efficiency (more than 90%～92%) in the situation that guarantees lower calcium sulfur ratio (Ca/S=1.1～1.3), reduce the water yield of carrying of water consumption and clean flue gas simultaneously, guarantee the sorbent particle higher surface activity, realized the wide regulating ratio characteristic of desulphurization system simultaneously, state in realization under the purpose prerequisite, and further simplify system, reduce equipment investment and operating cost, reduce flue gas resistance, thus the real purpose that realizes the dry flue gas desulphurization of efficient, wide regulating ratio, low cost, low water consumption.
The present invention is achieved by the following technical solutions:
The dry flue gas desulphurization technology of independent feed of the present invention, feed back and water spray comprises: desulfurizing agent prepares the separation and the recirculating system of digestive system, desulfurization reaction tower and desulphurization reaction system, outside sorbent particle.The present invention mainly carries out at desulfurization reaction tower and desulphurization reaction system, and the desulphurization reaction system comprises flue gas mixing-chamber, flue gas induction apparatus (Venturi nozzle, air-distribution device), desulfurization reaction tower, reaches various import and exports, separation (static, cloth bag, the inertia etc.) device of desulfurization reaction tower outside, desulfurizing tower flue gas recirculation device on the tower body.The present invention is independently being provided with to water atomization plant, desulfurizing agent charging gear and particle recirculation feeding back device desulfurization reaction tower, and at the differing heights setting nozzle separately of desulfurization reaction tower, thereby change the flow behavior in desulfurizing tower main reaction zone, strengthen turbulence intensity, reach abundant mixing and the velocity-slip of effectively organizing gas, solid, liquid three-phase in the desulfurization reaction tower, improve the utilization rate and the desulfurized effect of desulfurizing agent.
The dry flue gas desulphurization technology of described independent feed back, feed and water spray, its desulfurizing agent feed arrangement of nozzles exports the upwards position of 500～1500mm at distance desulfurizing tower flue gas induction apparatus; Particle recirculation feed back arrangement of nozzles is in the distance sulphur agent feed nozzle position of 500～3000mm upwards; Be arranged in apart from the particle recirculation feed back nozzle position of 800～3000mm upwards to water atomizing nozzle.
The dry flue gas desulphurization technology of described independent feed back, feed and water spray, wherein desulfurizing agent feed nozzle and particle recirculation feed back nozzle is arranged in the both sides of desulfurization reaction tower, be the front side that desulfurizing agent feed nozzle is positioned at desulfurizing tower, particle recirculation feed back arrangement of nozzles is at the desulfurizing tower rear side.
The dry flue gas desulphurization technology of described independent feed back, feed and water spray, particle recycle the feed back nozzle and arrange 1～2 layer to water atomizing nozzle, arrange one or more for every layer.
It gives water atomizing nozzle uniform on the horizontal cross-section of desulfurizing tower, or gives the desulfurizing tower front side wall of water atomizing nozzle on the horizontal cross-section of desulfurizing tower uniform.
The desulfurizing tower rear wall of its particle recirculation feed back nozzle on the horizontal cross-section of desulfurizing tower is uniform.
The dry flue gas desulphurization technology of described independent feed back, feed and water spray, its various nozzles are downward-sloping, and it is axial and horizontal direction is adjustable 5～60 ° of angular regions.
The dry flue gas desulphurization technology of described independent feed back, feed and water spray, it can also stretch in desulfurizing tower for water atomizing nozzle, and nozzle becomes seedpod of the lotus shape down.
All nozzles are axially scalable at it.
The dry flue gas desulphurization technology of described independent feed back, feed and water spray is characterized in that the tower body middle part at desulfurization reaction tower, arranges the flue gas jet nozzle, by the multiple jet flow of flue gas, forms the high intensity turbulent mixed zone at desulfurizing tower middle part.
Advantage of the present invention:
At first, the present invention adopts independently feed back, feed and water spray mode, considered that mainly the fresh sorbent particle that feed enters and the recirculation particle of feed back have the disparate surfaces chemical characteristic, and form the dynamic (dynamical) Different Effects of moisture film to desulfurization chemical reaction with the particle water effect, according to different particle characteristics, arrange the particle entry position targetedly, mainly improved the reaction efficiency of fresh sorbent particle, promptly improved desulphurization reaction efficient.
Secondly, under the prerequisite that guarantees identical desulfuration efficiency, adopt the present invention can reduce the capacity of returns of external recirculation particle, reduce the flow of flue gas resistance of desulfurizing tower and desulphurization reaction system, alleviated the particle separation burden of the erosion of wall and the outside dust arrester of desulfurizing tower, solved to a certain extent that maximization dry flue gas desulphurization equipment faced important technological problems.
The 3rd, the present invention will recycle the feed back inlet and be arranged in desulfurizing agent feed nozzle top, can be so that in fresh sorbent particle reaction to a certain degree, meet with the recirculation sorbent particle of a large amount of counter current directions, because the collision of particle, to break the surface reaction product of sorbent particle, improve the utilization rate and the reaction efficiency of desulfurizing agent.
The 4th; the present invention will recycle the feed back inlet and be arranged in desulfurizing agent feed nozzle top; because recirculation feed back major part is the bulky grain of complete reaction not; in the time of in feed back flow into desulfurization reaction tower; because the particle momentum very big (very big) that refluxes mainly due to backflow particle gross mass; sedimentation downwards earlier; mixed flow then again makes progress under the fluidisation wind action; and participation desulphurization reaction; if feedback outlet pastes the desulfurization reaction tower wall and arranges; then the feed back particle can be along under the desulfurization reaction tower internal face sticking wall flow; help washing away the desulfurizing tower internal face like this; prevent the sticking ash of internal face, simultaneously because gas-solid liquid phase turbulent flow and the mixing intensity in the tower strengthened in the sedimentation meeting of feed back.And the two all can increase the time of staying of feed back particle in desulfurization reaction tower, helps improving the utilization rate of desulfurizing agent.
The 5th, the present invention is easy to according to the structure of desulfurization reaction tower and shape, arranges that one or more layers gives water atomizing nozzle and circulation feed back inlet, organizes gas, solid, liquid three-phase flow field in the desulfurization reaction tower effectively, strengthens its strong mixing, reduces water loss.
The 6th, the present invention has strengthened the mixed intensity of gas-liquid solid phase in the tower owing to effectively organize the interior heterogeneous reaction pattern of desulfurization reaction tower, has strengthened tower inner transmission matter effect, has improved sorbent utilization, has effectively controlled the sticking ash of desulphurization reaction inner wall of tower; Desulphurization system is under the Ca/S=1.2 situation, and desulfuration efficiency reaches more than 90%, and the total circulating resistance of tower body is less than 1800Pa; Simultaneously, owing to can adopt flue gas recirculation and flue gas fluidic device, widened the load variations adaptive capacity of desulphurization system, can satisfy the high-efficiency desulfurization requirement of combustion apparatus (as boiler etc.) from the 20%-110% load variations.
Description of drawings
Fig. 1 is a system layout schematic diagram of the present invention.
Fig. 2, Fig. 3, Fig. 4 are the various layout schematic diagrames of each nozzle in the short transverse of tower.
Fig. 5 is an external recirculation particle feed back arrangement of nozzles schematic diagram.
Fig. 6, Fig. 7 are to the various layout schematic diagrames of water atomizing nozzle on the tower body horizontal cross-section.
Among the figure: the 2nd, flue gas induction apparatus (Rafael nozzle); the 3rd, desulfurization reaction tower; 3-1 is the bottom fluidisation area of desulfurization reaction tower; the 4th, flue gas mixing-chamber; the 5th, the exhanst gas outlet of desulfurization reaction tower; the 6th, flue gas pre-dedusting device (static; cloth bag; inertial dust separator etc.); the 7th, digestive system; the 8th, desulfurizing agent feed nozzle; the 9th, external recirculation particle feed back nozzle; the 10th, desulfurization is with giving water atomizing nozzle; the 11st, the particle sorting apparatus (static behind the desulfurizing tower; cloth bag; inertial dust separator etc.); the 12nd, main induced draft fan; the 13rd, chimney; the 14th, cinder tank; the 15th, jet flue gas nozzle; the 16th, clean flue gas recycled inlet tube; the 17th, the main flue gas inlet tube; the 18th, ash bucket.
The specific embodiment
Further introduce best embodiment of the present invention below in conjunction with accompanying drawing:
At first, the flue gas of discharging from combustion apparatus at first installs 6 through a pre-dedusting of flue gas (can be static, cloth bag, inertia or other kind deduster or a plurality of combinations), send into flue gas mixing-chamber 4 through the flue gas after the pre-dedusting through main flue gas inlet tube 17, and enter in the flue gas induction apparatus 2 of desulfurizing tower bottom, the muzzle velocity scope of keeping the flue gas jet is 20～55m/s, quickens to enter 3-1 district, desulfurizing tower bottom.
Simultaneously, desulfurizing agent raw material (as the CaO powder) being sent in the digestive system 7, generated highly active sorbent particle through digestion reaction, is that the desulfurizing agent of 1～8 μ m is (as Ca (OH) with digestion back particle size range
2) particle, be injected to desulfurization reaction tower bottom fluidisation area 3-1 by desulfurizing agent feed nozzle 8.
In the fluidisation area 3-1 of the bottom of desulfurization reaction tower 3, make progress about 500～1500mm highly in 2 outlets of distance flue gas induction apparatus, be fresh desulfurizing agent feed nozzle 8, it arranges that in the front side of desulfurizing tower this nozzle 8 can be fixed also scalable or adjust direction.
Follow the feed back nozzle 9 of bad particle again in 3～8 of the about 500～3000mm height placement that make progress apart from fresh desulfurizing agent feed nozzle 8, recirculation feed back nozzle is uniform on the horizontal cross-section of desulfurizing tower rear wall, sees Fig. 5.This feed back jet hole 9 can be fixing or scalable or adjust direction.
Be arranged in apart from particle for water atomizing nozzle 10 and recycle the upwards position of 800～3000mm of feed back nozzle.Injection flow rate is to form the required water yield for flue gas cool-down in the tower and sorbent particle moisture film; Give water atomizing nozzle uniform on the horizontal cross-section of desulfurizing tower, arrange 4～8 atomized water nozzles, as Fig. 7; Or give the desulfurizing tower front side wall of water atomizing nozzle on the horizontal cross-section of desulfurizing tower uniform, arrange that along the circumferential direction 1～3 is given water atomizing nozzle 10, as Fig. 6.Can fix for water atomizing nozzle, also telescopic or the adjustment direction; Can arrange one deck, also can arrange two-layer or two-layer more than, see Fig. 2, Fig. 4; Can also stretch in desulfurizing tower for water atomizing nozzle, nozzle down, as Fig. 3.
When giving water atomizing nozzle 10 two-layer layouts, lower floor adopts for water atomizing nozzle 10 and along the circumferential direction arranges 1～2 in the desulfurizing tower front side, and upper strata (second layer) is apart from the height of the 1500～3000mm of lower floor, and be uniform along 4～8 nozzles of tower body circumferencial direction.
Nozzle be with horizontal direction to 5～60 ° of angles of declivity, adjustable angle makes the atomizing cooling water spray in the tower under oblique from the desulfurization reaction tower internal face, as Fig. 2; Also can spray into downwards, as Fig. 3 from the desulfurization reaction tower central vertical.
Like this, the flue gas that enters desulfurization reaction tower 3 lower areas at first meets with the fresh sorbent particle that desulfurizing agent feed nozzle 8 enters, and the strong surface chemical reaction of generation under the influence of atomized water particle, flue gas mainly moves upward in the desulfurizing tower front side simultaneously, because the downward impact momentum of recirculation particle, with recirculation particle generation strong collision, with further raising particle utilization rate.Like this flue gas with from the highly active desulfurization agent particle of nozzle 8 spirts, by the 10 atomizing cooling waters that spray into, with mixing from the 9 recirculation sorbent particles that spray into of separating from deduster, strong three-phase turbulent heat transfer mass transfer takes place exchanges.Flue-gas temperature drops between 55～70 ℃ (be higher than in the tower flue gas dew point temperature 5～15 ℃ between) in the above-mentioned tower, also can be under some situation in about 80 ℃ operations of cigarette temperature, and most of sorbent particle particle diameter is between 1-5 μ m.Flue gas, particle water, sorbent particle and recirculation particle move upward under the drive of flue gas jet like this, are the fluidized suspension attitude in the whole desulfurizing tower.
Simultaneously since the recirculation particle from the desulfurization reaction tower internal face oblique down (with the angle of horizontal plane be 5～60 °) spray in the tower, impact downwards, make recirculation desulfurization particle flow back into the bottom of tower along the desulfurizing tower internal face, Zai Xunhuan sorbent particle can wash away internal face like this, reduces the dust stratification and the knot ash of internal face.
For large-scale desulfurization reaction tower, can be at the tower body middle part of desulfurization reaction tower 3, arrange flue gas jet nozzle 15, multiple jet flow by flue gas, form the high intensity turbulent mixed zone at desulfurizing tower middle part, and change the flow of flue gas form of tower body middle and upper part, strengthen the intensity of the desulphurization reaction of flue gas middle and upper part, and form the vortex of various forms, size, improve the interior cycle efficieny of particle.The jet flue gas can be drawn from any position of exhaust gases passes, also compressed air (humid air).
Again up; the tower endoparticle presents bigger falling trend substantially; most of particle moves downward along near the sidewall; and moved upward reciprocal by the flue gas drive again to the tower bottom; in tower, form high-intensity three-phase turbulent flow swap status, the complicated physical and chemical process of strong mixing, heat transfer, mass transfer and chemical reaction takes place.SO in tower in the flue gas
2With desulfurizing agent Ca (OH)
2Reaction generates calcium sulfite or calcium sulfate, and can deviate from a spot of SO in the flue gas simultaneously
3And pernicious gas compositions such as the HCl that may exist, HF, desulfuration efficiency can reach more than 90% at least.
Again; flue gas is drawn by the outlet conduit 5 at desulfurizing tower top; enter the separator 11 (static of desulfurization reaction tower outside; cloth bag or inertial separator; perhaps their combining form); the particle that carries in the flue gas is separated; wherein also contain some unreacted sorbent particle; in order to improve sorbent utilization; send back to them in the desulfurizing tower again by recirculation particle feed back nozzle 9; no longer participate in circulation and reacted most of granule (less than about 2 μ m) of finishing, promptly desulfuration byproduct and flying dust are then sent into cinder tank 14 storages; transhipment is walked.The clean flue gas up to standard that comes out from dust pelletizing system 11 is through main induced draft fan 12, and a part enters clean flue gas recirculation pipe 16, sends in the flue gas mixing-chamber 4, carries out flue gas recirculation, and all the other then send into chimney 13, enter atmosphere at last.
Claims (10)
1. independent feed, the dry flue gas desulphurization technology of feed back and water spray, comprise that desulfurizing agent prepares digestive system, the desulphurization reaction system, the separation and the recirculating system of outside sorbent particle, it is characterized in that the water atomization plant of giving with desulfurization reaction tower, desulfurizing agent charging gear and particle recirculation feeding back device independently are provided with, and the differing heights setting of desulfurization reaction tower separately feed nozzle, thereby change the flow behavior in desulfurizing tower main reaction zone, strengthen turbulence intensity, reach and effectively organize gas in the desulfurization reaction tower, Gu, the abundant mixing and the velocity-slip of liquid three-phase, the utilization rate and the desulfurized effect of raising desulfurizing agent.
2. the dry flue gas desulphurization technology of independent feed back according to claim 1, feed and water spray is characterized in that desulfurizing agent feed arrangement of nozzles exports the upwards position of 500～1500mm at distance desulfurizing tower flue gas induction apparatus; Particle recirculation feed back arrangement of nozzles is in the distance desulfurizing agent feed nozzle position of 500～3000mm upwards; Be arranged in apart from the particle recirculation feed back nozzle position of 800～3000mm upwards to water atomizing nozzle.
3, the dry flue gas desulphurization technology of independent feed back according to claim 1 and 2, feed and water spray, it is characterized in that desulfurizing agent feed nozzle and particle recirculation feed back nozzle is arranged in the both sides of desulfurization reaction tower, be the front side that desulfurizing agent feed nozzle is positioned at desulfurizing tower, particle recirculation feed back arrangement of nozzles is at the desulfurizing tower rear side.
4. the dry flue gas desulphurization technology of independent feed back according to claim 1 and 2, feed and water spray is characterized in that particle recirculation feed back nozzle and arranges 1～2 layer to water atomizing nozzle, arranges one or more for every layer.
5, the dry flue gas desulphurization technology of independent feed back according to claim 4, feed and water spray is characterized in that to water atomizing nozzle uniform on the horizontal cross-section of desulfurizing tower.
6, the dry flue gas desulphurization technology of independent feed back according to claim 4, feed and water spray is characterized in that to the desulfurizing tower front side wall of water atomizing nozzle on the horizontal cross-section of desulfurizing tower uniform.
7, the dry flue gas desulphurization technology of independent feed back according to claim 4, feed and water spray is characterized in that the desulfurizing tower rear wall of particle recirculation feed back nozzle on the horizontal cross-section of desulfurizing tower is uniform.
8, the dry flue gas desulphurization technology of independent feed back according to claim 2, feed and water spray is characterized in that nozzle is downward-sloping, and it is axial and horizontal direction is adjustable 5～60 ° of angular regions.
9, the dry flue gas desulphurization technology of independent feed back according to claim 1 and 2, feed and water spray is characterized in that stretching in desulfurizing tower to water atomizing nozzle, the particle water ejection that atomizes downwards.
10, the dry flue gas desulphurization technology of independent feed back according to claim 2, feed and water spray is characterized in that nozzle is axially scalable at it.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125323 CN1226073C (en) | 2003-08-25 | 2003-08-25 | Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03125323 CN1226073C (en) | 2003-08-25 | 2003-08-25 | Dry flue gas desulfurizing process with independent feeding, back-returning and water-spraying devices |
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| CN1515349A true CN1515349A (en) | 2004-07-28 |
| CN1226073C CN1226073C (en) | 2005-11-09 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100464825C (en) * | 2006-12-27 | 2009-03-04 | 吉林安洁环保有限公司 | Semi-dry desulfurizing process in double feedback circular fluidized bed |
| CN101116795B (en) * | 2006-08-03 | 2010-09-08 | 上海融新能源环境科技有限公司 | Graded water separation type circulating fluidized bed dry-type flue gas desulfurization technics and the special absorptive tower thereof |
| CN105107326A (en) * | 2015-09-14 | 2015-12-02 | 湖南省小尹无忌环境能源科技开发有限公司 | Membrane method dust collecting and desulfurizing device system for industrial smoke |
| CN107088359A (en) * | 2017-06-26 | 2017-08-25 | 深圳市友健科技有限公司 | A kind of biological purification plant for handling waste gas |
| CN109126412A (en) * | 2018-08-20 | 2019-01-04 | 中国华能集团清洁能源技术研究院有限公司 | Strengthen the method for solid waste mineralization of carbon dioxide using brine waste |
| CN110975584A (en) * | 2019-12-23 | 2020-04-10 | 陈军武 | Novel flue gas purification tower |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014110884A1 (en) * | 2013-01-18 | 2014-07-24 | 北京神雾环境能源科技集团股份有限公司 | Powdered solid fuel boiler and dry purification process system |
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2003
- 2003-08-25 CN CN 03125323 patent/CN1226073C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101116795B (en) * | 2006-08-03 | 2010-09-08 | 上海融新能源环境科技有限公司 | Graded water separation type circulating fluidized bed dry-type flue gas desulfurization technics and the special absorptive tower thereof |
| CN100464825C (en) * | 2006-12-27 | 2009-03-04 | 吉林安洁环保有限公司 | Semi-dry desulfurizing process in double feedback circular fluidized bed |
| CN105107326A (en) * | 2015-09-14 | 2015-12-02 | 湖南省小尹无忌环境能源科技开发有限公司 | Membrane method dust collecting and desulfurizing device system for industrial smoke |
| CN107088359A (en) * | 2017-06-26 | 2017-08-25 | 深圳市友健科技有限公司 | A kind of biological purification plant for handling waste gas |
| CN109126412A (en) * | 2018-08-20 | 2019-01-04 | 中国华能集团清洁能源技术研究院有限公司 | Strengthen the method for solid waste mineralization of carbon dioxide using brine waste |
| CN109126412B (en) * | 2018-08-20 | 2022-01-14 | 中国华能集团清洁能源技术研究院有限公司 | Method for intensifying mineralization of carbon dioxide by using salt-containing wastewater |
| CN110975584A (en) * | 2019-12-23 | 2020-04-10 | 陈军武 | Novel flue gas purification tower |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1226073C (en) | 2005-11-09 |
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