CN107596885A - The method of dry flue gas desulphurization - Google Patents
The method of dry flue gas desulphurization Download PDFInfo
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- CN107596885A CN107596885A CN201710939522.1A CN201710939522A CN107596885A CN 107596885 A CN107596885 A CN 107596885A CN 201710939522 A CN201710939522 A CN 201710939522A CN 107596885 A CN107596885 A CN 107596885A
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Abstract
The invention discloses a kind of method of dry flue gas desulphurization, comprise the following steps：(1) pre- dust removal step：Former flue gas is subjected to pre- dedusting to remove most of dust granules, so as to form pre- dedusting flue gas；(2) desulfurization catalyst step：Use desulphurization catalyst by the oxidizing sulfur dioxide in pre- dedusting flue gas for sulfur trioxide, so as to form pretreated fumes；The desulphurization catalyst includes carrier and active component；The carrier is nanoscale amphoteric oxide, selected from TiO2、ZrO2Or HfO2In one or more；The active component includes nanosize metal oxide, and the nanosize metal oxide includes V2O5、CoO、Co2O3And MnO2；(3) desulfurization absorption step：The desulfurization absorbent using magnesia as main component is used to carry out dry desulfurization to pretreated fumes, so as to form flue gas after processing.The method desulfuration efficiency of the present invention is high, and technique is simple, and water consumption is less, and operating cost is relatively low.
Description
Technical field
The present invention relates to a kind of method of dry flue gas desulphurization.
Background technology
China is the country using coal as main energy sources, in primary energy production and consumption structure, coal proportion difference
Up to 75% and 68.9%.84% coal is utilized by combustion system.As consumption of coal constantly increases, caused by coal-fired
Atmosphere pollution (such as dust, SO2、NOxAnd CO2Deng) be continuously increased.SO caused by power plant soot2Control turns into China
One of main task of Air Pollution Control.
At present, the process that sulfur dioxide is separated from burner flue gas is roughly divided into wet desulphurization and dry method
Two big type of desulfurization.Wet desulphurization is to add water that desulfurization slurry is made desulfurizing agent, then passes through spray using this desulfurization slurry
Mode fully contacts with the flue gas in flue, and the sulfur dioxide in the desulfurizing agent and flue gas that allow in slurry reacts to obtain not
Stable sulphite, then sulphite is set to be converted into sulfate by aeration again.The shortcomings that this method, is desulfurization
Equipment is huge, and cost is high, and desulfurization slurry is typically all acid solution, and anti-corrosion cost is high, and operating cost is high.It is existing dry
Method desulfurization is together to add desulfurizing agent and fuel or other comburants in burner hearth, the desulfurizing agent during furnace charge burns
Reacted with the sulphur in fuel and become sulphidisation, a this sulfide part, which is mingled in clinker, discharges, and another part mixes
Discharged in flue dust, this sulfur method is easy to operate.
One key issue of dry flue gas desulphurization technology is selective sweetening agent.Existing frequently-used dry-desulphurizer is basic
It is based on activated carbon or activated coke.Activated carbon or the desulfurization temperature of activated coke are low, simple to operate, and caused sulfuric acid can be with
Recycled as byproduct, thus be very promising sulfur method.Application No. 99104245.X Chinese patent application
A kind of method that desulfurizing agent is prepared by the use of activated carbon or NACF as carrier loaded cupric oxide is disclosed, due to carbon materials
Expect that low intensity, abrasion are high, recycling number is few, and production cost is high.
The content of the invention
In order to overcome drawbacks described above, present inventor has made intensive studies.It is an object of the invention to provide one
The method of kind dry flue gas desulphurization, its desulfuration efficiency is high, and technique is simple, and water consumption is less, and investment and operating cost are relatively low.This
It is a further objective that providing a kind of method of dry flue gas desulphurization, the byproduct of reaction after gas cleaning can be direct for invention
Utilize, thus there is preferable economic benefit.The present invention, which adopts the following technical scheme that, realizes above-mentioned purpose.
The present invention provides a kind of method of dry flue gas desulphurization, comprises the following steps：
(1) pre- dust removal step：Former flue gas is subjected to pre- dedusting to remove most of dust granules, so as to form pre- dedusting
Flue gas；
(2) desulfurization catalyst step：In bed apparatus is catalyzed, using desulphurization catalyst by the titanium dioxide in pre- dedusting flue gas
Sulphur is oxidized to sulfur trioxide, so as to form pretreated fumes；The desulphurization catalyst includes carrier and active component；The load
Body is nanoscale amphoteric oxide, selected from TiO2、ZrO2Or HfO2In one or more；The active component includes nanoscale
Metal oxide, the nanosize metal oxide include V2O5、CoO、Co2O3And MnO2；With
(3) desulfurization absorption step：In desulfurizer, it is the desulfurization absorbent of main component to pre- to use using magnesia
Handle flue gas and carry out dry desulfurization, so as to form flue gas after processing.
Method in accordance with the invention it is preferred that in step (1), pre- efficiency of dust collection is more than 90%.
Method in accordance with the invention it is preferred that in step (1), the content of sulfur dioxide of the former flue gas for 1000~
3000mg/Nm3, flow velocity is 2~5m/s and temperature is 95~160 DEG C.
Method in accordance with the invention it is preferred that in step (2), the catalysis bed apparatus includes shell, the front portion of shell
Provided with gas outlet, the rear portion of shell is provided with air inlet, and the inside of shell is provided with least two Catalytic Layers being arranged above and below；It is described
Pre- dedusting flue gas enters the Catalytic Layer by the air inlet, and is discharged from the gas outlet.
Method in accordance with the invention it is preferred that in step (2), based on 100 parts by weight desulphurization catalysts, the desulfurization catalyst
Agent includes following components：
Method in accordance with the invention it is preferred that in step (3), the desulfurization absorbent also includes calcium oxide and titanium dioxide
Silicon；The magnesia includes 70~85wt% activated magnesia, and content of the nanoscale magnesium in the magnesia is
10~20wt%.
Method in accordance with the invention it is preferred that in step (3), the desulfurizer is recirculating fluidized bed absorption tower, institute
Desulfurization absorbent is stated with the time of contact of the pretreated fumes in more than 30min.
Method in accordance with the invention it is preferred that in step (2), based on 100 parts by weight desulphurization catalysts, the desulfurization catalyst
Agent includes following components：
Method in accordance with the invention it is preferred that it also comprises the following steps：
(4) dust removal step：Flue gas after the processing is separated in bag-type dust collector, so as to obtain smoke-purifying
Gas, the desulfurization absorbent not being fully utilized and main component are the powdered accessory substance of sulfate；With
(5) desulfurization absorbent circulation step：The desulfurization absorbent not being fully utilized is recycled to desulfurizer.
Method in accordance with the invention it is preferred that it also comprises the following steps：
(6) by-product utilized step：Raw material including the powdered accessory substance and industrial solid wastes is mixed, from
And form construction material.
The present invention carries out flue gas desulfurization using desulphurization catalyst and desulfurization absorbent substep, and its desulfuration efficiency is improved,
And technique is simple, water consumption is less, and investment and operating cost are relatively low.Compared with wet desulphurization, the present invention can also reduce work
Industry discharge of wastewater.The method of the present invention directly using obtaining construction material, thus has the byproduct of reaction after gas cleaning
Preferable economic benefit.
Embodiment
With reference to specific embodiment, the present invention is further illustrated, but protection scope of the present invention is not limited to
This.
The method that the method for dry flue gas desulphurization is referred to as flue gas dry desulfurizing, is represented without using slurries to flue gas
The method for carrying out desulfurization.The dry flue gas desulphurization of the present invention is different from wet process of FGD, and it need not use a large amount of slurries,
Thus it can avoid producing a large amount of industrial wastes.
The method of the dry flue gas desulphurization of the present invention includes (1) pre- dust removal step, (2) desulfurization catalyst step, (3) desulfurization
Absorption step；(4) dust removal step, (5) desulfurization absorbent circulation step, (6) by-product utilized step can also be included.Below
Describe in detail.
<Pre- dust removal step>
The pre- dust removal step of the present invention is that former flue gas is carried out into pre- dedusting to remove most of dust granules, so as to be formed
Pre- dedusting flue gas.Above-mentioned steps can be carried out in pre- cleaner, and the concrete structure of the pre- cleaner can use ability
Known to domain those, such as electrostatic precipitator.The pre- efficiency of dust collection of the present invention can be more than 90%, preferably more than 95%.
The load of process below can be so reduced, improves the operation stability of desulfurization.
In the present invention, the content of sulfur dioxide of former flue gas can be 1000~3000mg/Nm3, be preferably 1500~
2500mg/Nm3, more preferably 1600~2000mg/Nm3.Oxygen content can be 10~20vol%, be preferably 15~
18vol%.Temperature can be 95~160 DEG C；Preferably 120~135 DEG C.In addition, the flow velocity of flue gas can be 2~5m/s,
Preferably 2.5~3.5m/s.Above-mentioned Gas Parameters represent the parameter at smoke inlet；The parameter of smoke outlet is according to reality
Depending on border desulfurization situation.Using above-mentioned technological parameter, be advantageous to improve desulfuration efficiency.
<Desulfurization catalyst step>
The desulfurization catalyst step of the present invention is to use desulphurization catalyst by the oxidizing sulfur dioxide in pre- dedusting flue gas for three
Sulfur oxide, so as to form pretreated fumes.Above-mentioned steps are carried out in bed apparatus is catalyzed.Catalysis bed apparatus includes shell, shell
Front portion be provided with gas outlet, the rear portion of shell is provided with air inlet, and the inside of shell is provided with least two catalysis being arranged above and below
Layer.Pre- dedusting flue gas enters the Catalytic Layer by the air inlet, and is discharged from the gas outlet.It is provided with Catalytic Layer de-
Sulfur catalyst.The shape of desulphurization catalyst can be cylinder, spheroid or Raschig ring body；Preferably spheroid.So be advantageous to by
The Catalytic Layer of catalysis bed apparatus is filled up.
In the present invention, desulphurization catalyst includes carrier and active component, and active component is supported on carrier, for inciting somebody to action
Oxidizing sulfur dioxide in flue gas is sulfur trioxide.Carrier can be nanoscale amphoteric oxide.For example, carrier is selected from TiO2、
ZrO2Or HfO2In one or more；Preferably TiO2And ZrO2Combination.Active component includes nanosize metal oxide；
The nanosize metal oxide includes V2O5、CoO、Co2O3And MnO2.These active components coordinate SO2Catalysis oxidation is SO3。
Such combination can be sulfur trioxide fully by the oxidizing sulfur dioxide in flue gas.
According to an embodiment of the invention, based on 100 parts by weight desulphurization catalysts, the desulphurization catalyst includes 30
~60 parts by weight TiO2, 10~30 parts by weight ZrO2, 2~10 parts by weight V2O5, 2~10 parts by weight CoO, 1~5 parts by weight Co2O3
With 5~15 parts by weight MnO2.Preferably, the desulphurization catalyst includes 50~58 parts by weight TiO2, 15~25 parts by weight ZrO2, 4
~9 parts by weight V2O5, 5~9 parts by weight CoO, 3~5 parts by weight Co2O3With 6~10 parts by weight MnO2.It is highly preferred that the desulfurization is urged
Agent includes 51~52 parts by weight TiO2, 20~25 parts by weight ZrO2, 6~8 parts by weight V2O5, 6~7 parts by weight CoO, 3~5
Parts by weight Co2O3With 8~10 parts by weight MnO2.Above-mentioned active component is controlled in above range, it can be significantly improved to cigarette
The oxidation effectiveness of sulfur dioxide in gas, so as to improve desulfurized effect.According to an embodiment of the invention, the desulfurization
Catalyst is only made up of said components.
The desulphurization catalyst of the present invention can use conventional method to obtain, such as infusion process.Nanosize metal oxide can
With using the synthesis of the conventional methods such as sol-gel process, Hydrolyze method, hydrothermal synthesis method.Here repeat no more.Nano level metal oxygen
The particle diameter of compound can be 2~100nm, and specific surface area is 100~300m2/g.Potassium permanganate can impregnate in the form of a solution.
<Desulfurization absorption step>
The desulfurization absorption step of the present invention is that to use using magnesia be the desulfurization absorbent of main component to pretreated fumes
Dry desulfurization is carried out, so as to form flue gas after processing.Above-mentioned steps can be carried out in desulfurizer.Desulfurizer can be
Recirculating fluidized bed absorption tower, so desulfurization absorbent can fully be contacted with pretreated fumes, improve desulfurized effect.Desulfurization
The time of contact of absorbent and pretreated fumes can be in more than 30min, for example, 30~60min, preferably in 35~50min.
Desulfurized effect and fume treatment efficiency can so be taken into account.
In the present invention, desulfurization absorbent includes magnesia.Magnesia can include light calcined magnesia, micron order aoxidizes
Magnesium and/or nanoscale magnesium.According to an embodiment of the invention, the magnesia includes 70~85wt% activity
Magnesia, preferably 80~85% activated magnesia；And content of the nanoscale magnesium in the magnesia be 10~
20wt%, preferably 15~20wt%.By using the exclusive property of some nanoparticles of nanoscale magnesium, Ke Yiti
High desulfurization efficiency.The formation of magnesium sulfate is so more beneficial for, so as to improve flue gas desulfurization effect.In the present invention, the desulfurization
Absorbent can only include magnesia, can also comprise additionally in the modifying agent such as calcium oxide and silica.Modifying agent is micron
Level, nano level metal oxide.In order to improve removal efficiency, desulfurization absorbent of the invention is powdered.Its particle diameter can
Think 0.5~10 micron, preferably 1~5 micron.So directly desulfurization absorbent can be mixed with flue gas, and then to flue gas
The removing of sulfur dioxide is carried out, so as to complete the desulfurization of flue gas in the case where not needing a large amount of water, and does not produce a large amount of works
Industry waste liquid.For example, desulfurization absorbent dry powder is sufficiently mixed with flue gas in flue, desulfurization is carried out subsequently into absorption tower
Processing, the flue gas after desulfurization are discharged by chimney.
In the present invention, the bottom of desulfurizer can be provided with smoke inlet, for the pretreated fumes to be introduced
To the desulfurizer.The bottom of desulfurizer can be provided with nozzle, for supplying water to desulfurizer.In the work of water
Under, desulfurization absorbent is more fully contacted and reacted with flue gas, improves desulfurized effect.
<Other steps>
The dust removal step of the present invention is is separated flue gas after the processing in bag-type dust collector, so as to obtain
Purifying smoke and the powdered accessory substance that main component is sulfate.The desulfurization absorbent circulation step of the present invention is in cloth bag
The desulfurization absorbent that the bottom collection of dust arrester is not fully utilized, and the desulfurization absorbent not being fully utilized is circulated
To desulfurizer.
In the present invention, the bottom of bag-type dust collector can be provided with desulfurization absorbent collector and accessory substance is collected
Device.Desulfurization absorbent collector is connected by the smoke inlet of pipeline and desulfurizer, for the desulfurization not being fully utilized to be inhaled
Receive agent and be recycled to the desulfurizer.Desulfurization absorbent can be so reused, reduces operating cost.Accessory substance collector
It is connected by pipeline with by-product recovery equipment, for accessory substance to be delivered into the by-product recovery equipment.Desulfurization absorbs
Agent collector can be at least one, such as two or more.
The by-product utilized step of the present invention is to mix the raw material including the powdered accessory substance and industrial solid wastes
Close, so as to form construction material.Powdered accessory substance comes from by-product recovery equipment.For example, by accessory substance and magnesia, work
Industry solid waste and additive, which are well mixed, obtains binder materials., can be by accessory substance, magnesia, industrial solid in the present invention
Waste and additive are respectively ground to more than 200 mesh in advance, preferably more than 250 mesh, are then mixed；By by-product
Thing, magnesia, industrial solid wastes and additive are well mixed to obtain mixture, and gained mixture then is ground into 200 mesh
More than, preferably more than 250 mesh；Or mix the accessory substance after grinding, magnesia, industrial solid wastes and additive, so
Further grinding obtains binder materials afterwards.
In the present invention, the weight ratio of accessory substance and magnesia, industrial solid wastes and additive can be 50~100:
50~100:30~80:2~10.Preferably, their weight ratio is 60~80:60~80:50~60:5~10.So may be used
To fully ensure that the combination property of binder materials.
In the present invention, the industrial solid wastes can be selected from one kind in flyash, slag powders or building waste powder
It is or a variety of；Preferably flyash and/or slag powders.The example of the slag powders of the present invention includes but is not limited to the stove after ball milling
Slag, slag, slag or scum.Flyash is the fine ash that catching is got off from the flue gas after coal combustion, and flyash is coal-burning power plant
The primary solids waste of discharge.Slag is ironmaking, the slag charge of steel-making discharge.Building waste powder be using building waste as raw material,
Crush the industrial solid wastes formed.Using above-mentioned industrial solid wastes, be advantageous to obtain the binder materials of steady quality.Work
The granularity of industry solid waste is preferably more than 200 mesh, more preferably more than 250 mesh.According to an embodiment of the invention,
The industrial solid wastes are selected from slag powders and flyash of the granularity more than 200 mesh.
In the present invention, the additive is selected from dihydric phosphate, dibasic alkaliine, tartaric acid, tartrate or amino
One or more in trimethylene phosphonic；Preferably dihydric phosphate or dibasic alkaliine.Specific example includes but unlimited
In sodium dihydrogen phosphate or disodium-hydrogen.Using above-mentioned additive, the combination property of binder materials can be fully ensured that.
According to an embodiment of the invention, it is 10~35 that the industrial solid wastes, which can be selected from weight ratio,:30~
The composition of 50 slag powders and flyash composition；Preferably weight ratio is 20~25:30~35 slag powders and flyash group
Into composition.
" part " in following preparation example and embodiment represents parts by weight, unless specifically stated otherwise.
Embodiment 1
By V2O5、CoO、Co2O3、MnO2As active component, TiO2And ZrO2Desulfurization is obtained using infusion process as carrier
Catalyst C1.
Table 1, desulphurization catalyst C1 formulas
| TiO2 | 55.0 parts by weight |
| ZrO2 | 23.0 parts by weight |
| V2O5 | 4.0 parts by weight |
| CoO | 6.0 parts by weight |
| Co2O3 | 4.0 parts by weight |
| MnO2 | 8.0 parts by weight |
The flow velocity of former flue gas is 2.5m/s；The other specification of smoke inlet, the parameter of exhanst gas outlet are as shown in tables 2 and 3.
Table 2, smoke inlet parameter
| Sequence number | Parameter | Unit | Numerical value |
| 1 | Inlet flue gas amount (operating mode) | m3/h | 220000 |
| 2 | Inlet flue gas amount (mark condition) | Nm3/h | 166718 |
| 3 | Inlet flue gas temperature | ℃ | 120 |
| 4 | SO2Entrance concentration | mg/Nm3 | 1900 |
| 5 | Humidity of flue gas | % | 5.9 |
Table 3, exhanst gas outlet parameter
| Sequence number | Project | Quantity | Unit |
| 1 | Exiting flue gas amount (operating mode) | 153463 | m3/h |
| 2 | Exhaust gas temperature | 65 | ℃ |
| 3 | Sulfur dioxide emissioning concentration | 46 | mg/Nm3 |
| 4 | Desulfuration efficiency | 98.48 | % |
| 5 | The quantum of output of accessory substance | 38.24 | t/h |
Former flue gas removes most of dust granules in advance by pre-duster, obtains pre- dedusting flue gas, and pre- efficiency of dust collection exists
More than 90%.Pre- dedusting flue gas is by catalysis bed apparatus, and the equipment includes two Catalytic Layers being arranged above and below, wherein filling up de-
Sulfur catalyst C1, it is by SO2Catalysis oxidation is SO3, so as to form pretreated fumes.Using desulfurization absorbent (magnesium oxide powder,
It contains 80wt% activated magnesia, and nano oxidized content of magnesium is 15wt%) carry out dry desulfurization.Desulfurization absorbent dry powder
It is well mixed, and enters in recirculating fluidized bed absorption tower with pretreated fumes into flue, then the water sprayed into nozzle
It is sufficiently mixed, so as to complete flue gas desulfurization.Flue gas is separated into powdered accessory substance, not complete by bag-type dust collector after processing
The desulfurization absorbent and purifying smoke of complete utilization, purifying smoke are discharged by chimney, and accessory substance then enters accessory substance collector, not
The desulfurization absorbent of full utilization is recycled in absorption tower.The concentration of the sulfur dioxide of purifying smoke is 46mg/Nm3, desulfurization effect
Rate reaches 98.48%.
By industrial solid wastes (flyash, slag powders) more than accessory substances more than 200 mesh and magnesia, 200 mesh and
Additive (sodium dihydrogen phosphate) is well mixed to obtain the binder materials.Binder materials material proportion and the performance test results are such as
Table 4 and table 5.The performance of binder materials is measured using GB/T50448-2008.Wherein, density, water absorption rate are maintenance
28d test result.
The material proportion of table 4, binder materials
| Specification | Accessory substance | Magnesia | Slag | Flyash | Additive |
| g | 80 | 60 | 20 | 35 | 5 |
The testing result of table 5, binder materials
Embodiment 2
Desulphurization catalyst C2 is obtained using the formula of table 6, other conditions are same as Example 1.Exhanst gas outlet parameter referring to
Table 7.The concentration of the sulfur dioxide of purifying smoke is 38mg/Nm3, desulfuration efficiency reaches 98.48%.
Table 6, desulphurization catalyst C2 formulas
Table 7, exhanst gas outlet parameter
| Sequence number | Project | Quantity | Unit |
| 1 | Exiting flue gas amount (operating mode) | 143436 | m3/h |
| 2 | Exhaust gas temperature | 65 | ℃ |
| 3 | Sulfur dioxide emissioning concentration | 38 | mg/Nm3 |
| 4 | Desulfuration efficiency | 98.48 | % |
| 5 | The quantum of output of accessory substance | 39.57 | t/h |
Embodiment 3
Desulphurization catalyst C3 is obtained using the formula of table 8, other conditions are same as Example 1.Exhanst gas outlet parameter referring to
Table 9.Flue gas after purification, the concentration of sulfur dioxide is 27mg/Nm3, desulfuration efficiency reaches 98.99%.
Table 8, desulphurization catalyst C3 formulas
| TiO2 | 51.0 parts by weight |
| ZrO2 | 23.0 parts by weight |
| V2O5 | 8.0 parts by weight |
| CoO | 6.0 parts by weight |
| Co2O3 | 4.0 parts by weight |
| MnO2 | 8.0 parts by weight |
Table 9, exhanst gas outlet parameter
| Sequence number | Project | Quantity | Unit |
| 1 | Desulfurizing tower exiting flue gas amount (operating mode) | 134644 | m3/h |
| 2 | Exhaust gas temperature | 65 | ℃ |
| 3 | Sulfur dioxide emissioning concentration | 27 | mg/Nm3 |
| 4 | Desulfuration efficiency | 98.99 | % |
| 5 | The quantum of output of accessory substance | 40.29 | t/h |
The present invention is not limited to above-mentioned embodiment, in the case of without departing substantially from the substantive content of the present invention, this area skill
Any deformation, improvement, the replacement that art personnel are contemplated that each fall within the scope of the present invention.
Claims (10)
- A kind of 1. method of dry flue gas desulphurization, it is characterised in that comprise the following steps：(1) pre- dust removal step：Former flue gas is subjected to pre- dedusting to remove most of dust granules, so as to form pre- dedusting flue gas；(2) desulfurization catalyst step：In bed apparatus is catalyzed, using desulphurization catalyst by the oxidizing sulfur dioxide in pre- dedusting flue gas For sulfur trioxide, so as to form pretreated fumes；The desulphurization catalyst includes carrier and active component；The carrier is nanometer Level amphoteric oxide, selected from TiO2、ZrO2Or HfO2In one or more；The active component aoxidizes including nano level metal Thing, the nanosize metal oxide include V2O5、CoO、Co2O3And MnO2；With(3) desulfurization absorption step：In desulfurizer, use using the desulfurization absorbent that magnesia is main component to pretreatment cigarette Gas carries out dry desulfurization, so as to form flue gas after processing.
- 2. according to the method for claim 1, it is characterised in that in step (1), pre- efficiency of dust collection is more than 90%.
- 3. according to the method for claim 1, it is characterised in that in step (1), the content of sulfur dioxide of the former flue gas is 1000~3000mg/Nm3, flow velocity is 2~5m/s and temperature is 95~160 DEG C.
- 4. according to the method for claim 1, it is characterised in that in step (2), the catalysis bed apparatus includes shell, outside The front portion of shell is provided with gas outlet, and the rear portion of shell is provided with air inlet, and the inside of shell is provided with least two catalysis being arranged above and below Layer；The pre- dedusting flue gas enters the Catalytic Layer by the air inlet, and is discharged from the gas outlet.
- 5. according to the method for claim 1, it is characterised in that, should based on 100 parts by weight desulphurization catalysts in step (2) Desulphurization catalyst includes following components：
- 6. according to the method for claim 5, it is characterised in that in step (3), the desulfurization absorbent also includes calcium oxide And silica；The magnesia includes 70~85wt% activated magnesia, and nanoscale magnesium is in the magnesia Content be 10~20wt%.
- 7. according to the method for claim 5, it is characterised in that in step (3), the desulfurizer is inhaled for recirculating fluidized bed The time of contact of receipts tower, the desulfurization absorbent and the pretreated fumes is in more than 30min.
- 8. according to the method for claim 1, it is characterised in that, should based on 100 parts by weight desulphurization catalysts in step (2) Desulphurization catalyst includes following components：
- 9. according to the method described in any one of claim 1~8, it is characterised in that it also comprises the following steps：(4) dust removal step：Flue gas after the processing is separated in bag-type dust collector, so as to obtain purifying smoke, not The desulfurization absorbent and main component of full utilization are the powdered accessory substance of sulfate；With(5) desulfurization absorbent circulation step：The desulfurization absorbent not being fully utilized is recycled to desulfurizer.
- 10. according to the method for claim 9, it is characterised in that it also comprises the following steps：(6) by-product utilized step：Raw material including the powdered accessory substance and industrial solid wastes is mixed, so as to be formed Construction material.
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