CN1331568C - Method and apparatus for desulfurization comprising incorporating NO and/or NO2 in gas to be treated, to recover SO2 as CaSO4 - Google Patents

Method and apparatus for desulfurization comprising incorporating NO and/or NO2 in gas to be treated, to recover SO2 as CaSO4 Download PDF

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CN1331568C
CN1331568C CNB038201127A CN03820112A CN1331568C CN 1331568 C CN1331568 C CN 1331568C CN B038201127 A CNB038201127 A CN B038201127A CN 03820112 A CN03820112 A CN 03820112A CN 1331568 C CN1331568 C CN 1331568C
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gas
mentioned
processed gas
caso
processed
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CN1678384A (en
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定方正毅
徐旭常
西冈将辉
松岛德彦
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Japan Science and Technology Agency
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81—Solid phase processes
    • B01D53/83—Solid phase processes with moving reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids

Abstract

A method for desulfurization, characterized in that it comprises incorporating 10 to 5000 ppm of NO and/or NO2 in a SO2-containing gas to be treated, contacting a SO2 desulfurizing agent comprising carrier particles having a large particle diameter and, coated thereon, finely particulate Ca(OH)2 with the resulting gas to be treated in the state of a fluidized layer in a reaction tower, elevating them while reacting, allowing them to flow to a first gas-solid separator via the top of the reaction tower, precipitating and separating said carrier particles from a gas containing CaSO4 having been formed by the reaction of Ca(OH)2 on the surface of the above carrier particles with SO2 and been exfoliated, while allowing said gas containing CaSO4 to flow to a second gas-solid separator from the top of the above first gas-solid separator, and separating and recovering the above CaSO4 from the gas to be treated in the second gas-solid separator.

Description

Make coexistence NO and/or NO in the processed gas 2And with CaSO 4Form reclaims SO 2Sulfur method and desulfurizer
Technical field
The present invention relates to improve with CaSO 4Form is separated the SO that reclaims in processed gas, for example exhaust 2Sulfur method and the CaSO in the desulfurizer 4The sulfur method and the desulfurizer of above-mentioned processed gas of the rate of recovery, particularly so that the 10ppm that coexists at least in the processed gas, the preferred NO of 100ppm at least 2For feature with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method and desulfurizer.
Background technology
SO 2Be the material that environment and people's health is had significant impact, from the SO of generations such as burning of coal process 2It is big social concern.For this reason, just study absorption from the past and removing SO 2System.One has the absorption removal method of using CaO.This uses CaO to absorb and removes SO 2Via SO 2Diffusion and form CaSO by solid reaction 4/ CaSO 3Process carry out.Therefore, the particle properties of CaO, be that surface area, aperture, pore volume etc. have big influence to above-mentioned absorption reaction.Commercially available CaO removes SO about absorbing 2The not talkative calcium utilization of characteristic good.
In addition, Sander etc. has reported SO when using the mixed serum of flying dust and calcium hydroxide 2Absorption remove characteristic be enhanced (Sanders et al.I nd.Eng.Chem.Res.1995,34 (4), 302-307).Explanation: SO among its report 2The absorption improvement of removing characteristic be the existence of the calcium silicate hydrate that the hydration reaction by calcium and aluminium hydrosilicate generates, reactive difference is the structure of calcium silicate hydrate.In addition, gama-alumina-CaO adsorbent (Svoboda etc.) has been proposed, behind the slurries of about 100 ℃ of slakings from CaO, calcium sulfate and flying dust, dry and adsorbent (Hiroaki etc.) that obtain (is thought and formed entringite.Special fair 3-59737 communique also discloses similar techniques.) etc., but weak point is: the amount ratio of those preparation of adsorbent method water is more, and is bad in the usability of the bad region of water conservancy, and removes the energy that water need be long-time and/or many, and at preparation SO 2Improve the problem that is formed with process management difficulty etc. of the component of characterization of adsorption during adsorbent, therefore exist to be difficult to design SO 2The manufacturing installation of adsorbent and desulfurizer directly link the device of such desulfurizer.
To this, people of the present invention prepare the mechanism of the hydrating process in the process of adsorbent by knowing mixed C aO and flying dust in the water, have diligently carried out can becoming more practical art manufacturing with the above-mentioned raw materials manufacturing and have shown active SO 2Research (the Energy﹠amp of the desulfurizing agent of characterization of adsorption; Fuels, Vol.13, No5,1015-1020,1999. document A)., at this, the water yield for preparing this desulfurizing agent use is many, H 2O/ (carrier particle+Ca (OH) 2) weight ratio be 1.5, under the service condition of such water, also need to improve as the sulfur method utilization in the few region of water resource.And at that time, in order to reduce discarded object as far as possible, it is important improving the usability of accessory substance and the utilization ratio of the desulfurizing agent that improvement is added.So people of the present invention further develop above-mentioned technology, research can be with the desulfurizing agent of the design of realistic scale roughly dry type desulfurizing technology, finish and delivered by use have bigger particle diameter, conduct absorption SO can be covered on the surface 2The Ca (OH) of sweetening component 2Carrier particle, improve as absorbing SO 2The Ca (OH) of sweetening component 2The Ca utilization rate, and can separate recycle the high CaSO of property with byproduct efficiently 4Sulfur method and desulfurizer invention (spy opens the 2002-113326 communique).In addition, the inventor has delivered the NO that exists in the gas of sweetening process in [Fuel, 78/9,1089-1095 (1999)] xThe effect that produces of chain reaction, but about use big particle diameter carrier particle surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent is with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method in, to CaSO 4The effect of the rate of recovery is not investigation fully.
The problem of the present application is, provide use big particle diameter carrier particle surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent can reclaim useful byproduct CaSO more expeditiously 4Sulfur method and desulfurizer.State in the use in the sulfur method and desulfurizer of desulfurizing agent, at the Ca that has been covered (OH) 2Big particle diameter carrier particle surface, from carrier surface peel off efficiently with processed SO 2The CaSO that reaction generates 4, to reclaiming CaSO more expeditiously 4Be important.
Do not know that what kind of factor is related with the above-mentioned charge stripping efficiency of raising, but in order to improve the sulfur method that uses above-mentioned desulfurizing agent, the NO during the desulfurization that the invention described above people are conceived to deliver is handled x(x is more than 1, below 2) coexistence effect makes NO at least 2Coexistence found that CaSO 4The recovery characteristic be enhanced, and can solve above-mentioned problem.
Summary of the invention
The 1st invention of the present invention is with CaSO 4Form is separated the SO that reclaims in the above-mentioned processed gas 2Sulfur method, it is characterized in that: make to contain SO 2Processed gas in the 10-480ppm NO that coexists at least 2, make the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent and the above-mentioned SO that contains 2Processed gas in reaction tower, contact forming under the state of fluosolids, Yi Bian make above-mentioned desulfurizing agent and SO 2Reaction Yi Bian make it to rise in above-mentioned reaction tower with above-mentioned processed gas, makes by above-mentioned SO from this reaction tower top 2Particulate Ca (OH) with the carrier particle surface 2Reaction and the CaSO that forms 4Flow in the 1st gas-solid separator with above-mentioned carrier particle and processed gas, in above-mentioned the 1st gas-solid separator from containing Ca (OH) by above-mentioned carrier particle surface 2With SO 2Reaction and the CaSO that forms and peel off 4Gas in make this carrier grain in sedimentation and separate, make this contain CaSO 4Gas flow to the 2nd gas-solid separator from above-mentioned the 1st gas-solid separator top, in the 2nd gas-solid separator, separate and reclaim above-mentioned CaSO from processed gas 4Preferably have following characteristics with CaSO 4Form is separated the SO that reclaims in above-mentioned each processed gas 2Sulfur method, be in processed gas, not contain NO 2But the NO of the 10-480ppm that coexists at least 2And with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, described feature is: when there is NO in this sulfur method in processed gas, convert NO to via at least a portion with the NO in the processed gas 2The processing means, perhaps do not have NO and NO 2The time, convert NO at least a portion with NO 2The processing means before supply with NO or to handling gas, supply with NO from the outside 2After, with processed gas supply to have the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2In the reaction tower of desulfurizing agent, be more preferably at least a portion and convert NO to via with the NO in the processed gas with following characteristics 2The processing means and with CaSO 4Form is separated the SO that reclaims in above-mentioned each processed gas 2Sulfur method, described feature is: convert at least a portion of NO to NO 2The processing means, be by be pressed into the processing means that methyl alcohol, tert-butyl peroxide come oxidation 300 ℃ of-400 ℃ of atomizings.
The 2nd invention of the present invention is with CaSO 4Form is separated the SO that reclaims in the processed gas 2Desulfurizer, it is characterized in that having: the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Thereby desulfurizing agent is by supplying with the reaction tower 1 that processed gas forms fluosolids; To above-mentioned reaction tower supply with the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2The desulfurizing agent feedway of desulfurizing agent; Make and contain SO 2Processed gas in the 10-480ppm NO that coexists at least 2Device; Be blown into the above-mentioned amount NO that coexisted 2Contain SO 2The processed device for blowing gas of processed gas; Make above-mentioned desulfurizing agent and contain SO 2Processed gas in reaction tower, contact forming under the state of fluosolids, Yi Bian make above-mentioned desulfurizing agent and SO 2Reaction, Yi Bian make it in above-mentioned reaction tower, to rise with above-mentioned processed gas, will be from this reaction tower top by above-mentioned SO 2Particulate Ca (OH) with the carrier particle surface 2Reaction and the CaSO that forms 4Be blown into above-mentioned carrier particle and processed gas, from containing the CaSO that forms and break away from above-mentioned carrier surface 4Processed gas make above-mentioned carrier particle sedimentation and separate the 1st gas-solid separator of this carrier particle; And, be blown into the above-mentioned CaSO of containing from above-mentioned the 1st gas-solid separator 4Processed gas, and separate this CaSO from the processed gas that is blown into 4The 2nd gas-solid separator.Preferably have following characteristics with CaSO 4Form is separated the SO that reclaims in the above-mentioned processed gas 2Desulfurizer, described feature is: make to contain SO 2Processed gas in the 10-480ppm NO that coexists at least 2Device, be configured in CaSO 4Form is separated recovery SO 2Processed gas before the reaction tower that forms fluosolids is supplied with, comprise and supply with NO from the outside 2So that the NO in the above-mentioned processed gas 2Be at least the device of 10-480ppm and/or convert NO to NO 2Converter; Be more preferably have following characteristics with CaSO 4Form is separated the SO that reclaims in the above-mentioned processed gas 2Desulfurizer, described feature is: adopt to form the reaction tower 1 of fluosolids and from containing CaSO 4Processed gas in the 1st gas-solid separator of making above-mentioned carrier particle sedimentation and separating, form the circular form fluosolids.
The simple declaration of accompanying drawing
Fig. 1 is the concept map of desulfurizer of the present invention.The main structure of this device is: fluosolids forms return duct 5 that reaction tower 1, the 1st gas-solid separator 2, the 2nd gas-solid separator 3, processed gas be blown into portion 4, carrier of separating particle, contains CaSO 4Gas carrier pipe 6, the processed gas of handling 7, contain and reclaim CaSO 4Solid reactant take out pipe arrangement 8, SO 2Desulfurizing agent supply unit (SO 2Desulfurizing agent is made feedway) 9, NO 2Converter CV, oxidant feedway OD, boiler (processed gas generation source) B.
Fig. 2 represents to make and contains SO 2Coexistence NO and NO in the processed gas 2The time with CaSO 4Form is separated recovery SO 2Characteristic and the time dependent dependency relation of particle spittle amount.
The specific embodiment
Be described in more detail the present invention below.
A. Fig. 1 is that of the present invention making contains SO 2Processed gas in coexistence 10-500ppm NO and/or NO 2, make the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent and the above-mentioned SO that contains 2Processed gas in reaction tower, contact forming under the state of fluosolids, with CaSO 4Form is separated the SO that reclaims in the processed gas 2The concept map of desulfurizer.The 1st, the fluosolids that possesses porous plate (PP) forms reaction tower.Below the above-mentioned porous plate PP of above-mentioned reaction tower 1, connecting and supplying with the NO that makes the 10-480ppm that coexists at least in the processed gas that for example makes from boiler B 2Device, for example blast pump of processed gas.In order to make coexist at least NO of 10-480ppm of processed gas 2, be provided with in the device front of supplying with above-mentioned processed gas and supply with NO at least 2Device and/or at least a portion of the NO that will in processed gas, coexist convert NO to 2Device CV and the OD that is blown into the oxidant that promotes above-mentioned conversion.
Above porous plate PP, be provided with SO 2Desulfurizing agent feedway 9, at this, the manufacturing installation of desulfurizing agent and reaction tower 1 directly link.The later device class write up of desulfurizing agent and reaction tower is opened in the 2002-113326 communique the above-mentioned spy that people of the present invention have proposed.The technical descriptioon that above-mentioned communique is put down in writing, make the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent with contain SO 2Processed gas in reaction tower, contact forming under the state of fluosolids, with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method and desulfurizer in, except " making the NO that coexists at least in the processed gas 2" beyond this technical characterictic of the present invention, with close association of the present invention, therefore should be appreciated that becomes a part that constitutes technical descriptioon of the present invention.
Embodiment
Specify the present invention by the following examples, explain but the present invention is not limited ground by this illustration.
Embodiment 1
As processed gas, with SO 2Content is 1500ppm, CO 2Content is 12%, O 2Content is that 8% gas is as sample.As desulfurizing agent, use the Ca (OH) that on carrier particle, has been covered 2And make it and (carrier particle+Ca (OH) 2) weight ratio reach 1.5 desulfurizing agent, use as carrier particle to have chemical composition, average grain diameter 137 μ m, the surface area 126m that following table 1 is put down in writing 2The flying dust of/g.Supply with desulfurizing agent and make the Ca/S ratio reach 1.7, regulation gas superficial linear velocity in a column 0.75m/s, reactor (the circular form fluosolids forms reaction tower) temperature is 350 ℃, and gas residence time is 1.5 seconds (s), and the pressure loss is 1kPa (being equivalent to the particle-filled rate of desulfurizing agent).
Table 1
SiO 2 Al 2O 3 TiO 2 Fe 2O 3 CaO
49.0 24.4 1.35 5.79 8.89
MgO Na 2O K 2O SO 3 C
2.36 1.32 0.98 0.54 0.9
Table 2 expression NO and/or the NO that coexistence (ppm) table 2 is put down in writing that send as an envoy to 2During desulfurization and these NO that do not coexist xThe time desulfurization characteristic (%).Compare NO and/or NO 2The coexistence effect, under identical coexistence amount, NO 2The coexistence effect bigger, this can understand from table 2.By this things to know: be provided with and convert NO to NO 2Converter CV with CaSO 4Form is separated recovery SO 2Doctor treatment in brought significant improvement.In addition, NO and/or NO 2The coexistence amount when 50ppm-300ppm is above, these the coexistence effects roughly saturated, the least concentration that should coexist in processed gas is 10ppm, but does not have the upper limit.
Table 2
NO ppm Take off SO x (％) NO 2 ppm Take off SO x(％)
0 48.2 0 48.2
11 67.4 8.5 70.8
19.5 67.7 29.6 72.5
29.6 68.1 29.6
52 68.8 52.3 73.9
181 67.3 242 73.5
321 71.4 480 74.1
485 73
Embodiment 2
Table 3 is expressed about NO, NO 2The coexistence amount effect of the desulfurization degree when 480ppm (Ca/S) result that experimentizes and obtain respectively.
When implementing above-mentioned experiment, use SO as processed gas 2Content is 1500ppm, CO 2Content is 12%, O 2Content is 8% gas sample, uses the Ca (OH) that has been covered as desulfurizing agent on flying dust 2And make it and (carrier particle+Ca (OH) 2) weight ratio reach 1.5 desulfurizing agent, use flying dust with chemical composition, average grain diameter and the surface area identical with the flying dust of use in embodiment 1 as flying dust.By the result of table 3 clear and definite NO and NO 2Coexistence to the effect of desulfurization degree, also known NO 2Coexistence coexists to improving the effect stability of desulfurization degree than NO to the effect that improves desulfurization degree.This situation understands NO 2Coexistence the stable reaction of desulphurization reaction is produced effect.
Table 3
NOx 0ppm NO 480ppm NO 2 480ppm
Ca/S Take off SOx% Ca/S Take off SOx% Ca/S Take off SOx%
1.34 42.9 1.41 65 1.77 74.1
1.77 50.2 1.52 67.9
2.28 57.6 1.57 64.8
1.72 66.7
1.77 72.7
2.21 83.5
Embodiment 3
At this, use the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2During desulfurizing agent, NO (480ppm) and NO 2(480ppm) for particulate Ca (OH) by the carrier particle surface 2With SO 2The CaSO that reacts and form 4The coexistence effect of the characteristic that breaks away from from carrier particle surface, with particle spittle amount in time the change list of process be shown among table 4 and Fig. 2.
Table 4
Elapsed time [branch] NO x な し NO 480ppm NO 2 480ppm
30 0.120 0.085 0.153
60 0.099 0.277 0.253
90 0.124 0.541 0.410
120 0.145 0.490 0.539
150 0.176 0.332 0.530
180 0.191 0.422 0.294
210 0.299 0.351 0.397
240 0.141 0.268 0.361
270 0.217 0.722 0.370
300 0.207 0.642 0.339
330 0.155 0.475 0.439
360 0.139 0.369 0.389
390 0.239 0.338 0.353
420 0.222 0.554 0.324
450 0.121 0.318
480 0.227 0.601 0.344
510 0.214
540 0.265
570 0.314
600 0.325
Particle spittle amount=(spittle particle in Ca amount g/ branch) ÷ (the Ca amount g/ branch of the desulfurizing agent of supply).By adding NO () and NO 2(▲) increases spittle particle [NO and NO 2Do not represent with (◆) when not coexisting].This situation means: by coexistence NO and NO 2, desulfurizing agent works effectively, obtains gypsum efficiently.During NO, see the The above results of the relation of expression effluxion and spittle amount, fluctuation is big, and in other words spittle amount instability, does not carry out stable reaction, and is controlled not so good.In contrast to this, at coexistence NO 2The time, spittle amount is highly stable.Situation understands thus, at NO 2Coexistence is down with CaSO 4Form is separated recovery and is contained SO 2Processed gas in SO 2Doctor treatment more produce effect.
Industrial applicibility
The present invention has established to make and has contained SO2At least 10-480ppm NO coexists in the processed gas2, and make it with the carrier particle of large particle diameter surface-coated particulate Ca (OH)2SO2The desulfurizing agent contact, thereby with CaSO4Form is separated recovery SO2Sulfur method, providing can be expeditiously with useful accessory substance CaSO4Form reclaims SO2, and the high enhancement of environment technology of industrial applicibility, huge to contribution to society accordingly.

Claims (8)

1. one kind with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, wherein, make to contain SO 2Processed gas in the 10-480ppm NO that coexists at least 2, make the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent and the above-mentioned SO that contains 2Processed gas in reaction tower, contact forming under the state of fluosolids, Yi Bian make above-mentioned desulfurizing agent and SO 2Reaction Yi Bian make it to rise in above-mentioned reaction tower with above-mentioned processed gas, makes by above-mentioned SO from this reaction tower top 2Particulate Ca (OH) with the carrier particle surface 2Reaction and the CaSO that forms 4Flow in the 1st gas-solid separator with above-mentioned carrier particle and processed gas, in above-mentioned the 1st gas-solid separator from containing Ca (OH) by above-mentioned carrier particle surface 2With SO 2Reaction and the CaSO that forms and peel off 4Gas make this carrier particle sedimentation and separate, make this contain CaSO 4Gas flow to the 2nd gas-solid separator from above-mentioned the 1st gas-solid separator top, in the 2nd gas-solid separator, separate and reclaim above-mentioned CaSO from processed gas 4
2. one kind with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, be to make the 10-480ppm NO that coexists at least in the processed gas 2And with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, this sulfur method is containing SO 2Processed gas in do not contain NO 2Even, or contain NO 2But when not enough, by supply with NO from the outside 2Make the 10-480ppm NO that coexists at least in the processed gas 2The pre-treatment of processed gas after, make the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Desulfurizing agent and the above-mentioned SO that contains 2Processed gas in reaction tower, contact forming under the state of fluosolids, Yi Bian make above-mentioned desulfurizing agent and SO 2Reaction Yi Bian make it to rise in above-mentioned reaction tower with above-mentioned processed gas, makes by above-mentioned SO from this reaction tower top 2Particulate Ca (OH) with the carrier particle surface 2Reaction and the CaSO that forms 4Flow in the 1st gas-solid separator with above-mentioned carrier particle and processed gas, in above-mentioned the 1st gas-solid separator from containing Ca (OH) by above-mentioned carrier particle surface 2With SO 2Reaction and the CaSO that forms and peel off 4This carrier particle of gas sedimentation and separate, make this contain CaSO 4Gas flow to the 2nd gas-solid separator from above-mentioned the 1st gas-solid separator top, in the 2nd gas-solid separator, separate and reclaim above-mentioned CaSO from processed gas 4
3. one kind with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, be in processed gas, not contain NO 2, and the 10-480ppmNO that coexists at least 2And with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, when there is NO in this sulfur method in processed gas, convert the NO of 10-480ppm to via at least a portion with the NO in the processed gas 2The processing means, perhaps do not have NO and NO 2The time, convert NO at least a portion with NO 2The processing means before, supply with supplying with 10-480ppmNO 2Behind required enough NO, with processed gas supply to have the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2In the reaction tower of desulfurizing agent.
4. according to claim 3 with CaSO 4Form is separated the SO that reclaims in the processed gas 2Sulfur method, wherein, convert at least a portion of NO to NO 2The processing means, be by be pressed into the processing means that methyl alcohol, tert-butyl peroxide come oxidation 300 ℃ of-400 ℃ of atomizings.
5. one kind with CaSO 4Form is separated the SO that reclaims in the processed gas 2Desulfurizer, it is characterized in that having: the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2Thereby desulfurizing agent is by supplying with the reaction tower 1 that processed gas forms fluosolids; To above-mentioned reaction tower supply with the carrier particle of big particle diameter surface-coated particulate Ca (OH) 2SO 2The desulfurizing agent feedway of desulfurizing agent; Make and contain SO 2Processed gas in the 10-480ppmNO that coexists at least 2Device; Be blown into the 10-480ppmNO that coexists at least 2Contain SO 2The processed device for blowing gas of processed gas; Make above-mentioned desulfurizing agent and contain SO 2Processed gas in reaction tower, contact forming under the state of fluosolids, Yi Bian make above-mentioned desulfurizing agent and SO 2Reaction, Yi Bian make it in above-mentioned reaction tower, to rise with above-mentioned processed gas, will be from this reaction tower top by above-mentioned SO 2Particulate Ca (OH) with the carrier particle surface 2Reaction and the CaSO that forms 4Be blown into above-mentioned carrier particle and processed gas, from containing the CaSO that forms and break away from above-mentioned carrier surface 4Processed gas make above-mentioned carrier particle sedimentation and separate the 1st gas-solid separator of above-mentioned carrier particle; And, be blown into the above-mentioned CaSO of containing from above-mentioned the 1st gas-solid separator 4Processed gas, and separate this CaSO from the processed gas that is blown into 4The 2nd gas-solid separator.
6. according to claim 5 with CaSO 4Form is separated the SO that reclaims in the processed gas 2Desulfurizer, it is characterized in that, make to contain SO 2Processed gas in the 10-480ppmNO that coexists at least 2Device, be configured in CaSO 4Form is separated recovery SO 2Processed gas before the reaction tower that forms fluosolids is supplied with, contain and supply with NO from the outside 2So that the NO in the above-mentioned processed gas 2Content is at least the device of 10-480ppm and/or converts NO to 10-480ppmNO at least 2Converter.
7. according to claim 5 with CaSO 4Form is separated the SO that reclaims in the processed gas 2Desulfurizer, it adopts the reaction tower 1 that forms fluosolids and from containing CaSO 4Processed gas the 1st gas-solid separator of making above-mentioned carrier particle sedimentation and separating, form the circular form fluosolids.
8. according to claim 6 with CaSO 4Form is separated the SO that reclaims in the processed gas 2Desulfurizer, it adopts the reaction tower 1 that forms fluosolids and from containing CaSO 4Processed gas the 1st gas-solid separator of making above-mentioned carrier particle sedimentation and separating, form the circular form fluosolids.
CNB038201127A 2002-08-27 2003-08-25 Method and apparatus for desulfurization comprising incorporating NO and/or NO2 in gas to be treated, to recover SO2 as CaSO4 Expired - Fee Related CN1331568C (en)

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JP246125/2002 2002-08-27
JP2002246125A JP4012011B2 (en) 2002-08-27 2002-08-27 Desulfurization method and desulfurization apparatus for recovering SO2 as CaSO4 by coexisting NO2 in a gas to be treated

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