CN1087643C - Flue gas desulfurization process and device of dry desulfurizing agent bed material internal circutation - Google Patents
Flue gas desulfurization process and device of dry desulfurizing agent bed material internal circutation Download PDFInfo
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- CN1087643C CN1087643C CN97103839A CN97103839A CN1087643C CN 1087643 C CN1087643 C CN 1087643C CN 97103839 A CN97103839 A CN 97103839A CN 97103839 A CN97103839 A CN 97103839A CN 1087643 C CN1087643 C CN 1087643C
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Abstract
The present invention relates to a flue gas desulfurization method and device for the internal circulation of dry desulfurizing agent bed materials, particularly to a method and a device for eliminating sulfur oxide in flue gas discharged by combustion devices. Flue gas and most of solid bed materials are separated through a gas-solid separating device arranged in a fluidized bed reactor, the internal circulation of bed materials is formed, and flue gas discharged from the fluidized bed reactor carries away a small quantity of bed materials simply. The device has the advantages that the utilization rate of calcium-based desulfurizing agents and the desulfurization efficiency of flue gas can be effectively improved (the flue gas desulfurization rate can reach more than 0.85 when the calcium-sulfur ratio is 1.5), the total circulation resistance of flue gas is obviously reduced, and corrosion can be avoided. Thereby, investment expense of operation and devices is effectively reduced.
Description
The present invention relates to a kind of flue gas desulfurization technique, relate in particular to sulfur oxide removes in the flue gas that a kind of pulverized-coal fired boiler, grate firing boiler or other combustion apparatus discharge method and device.
The semidry method or the dry type flue gas desulfurizing technology of the calcium-based desulfurizing agent (lime stone, dolomite, lime, calcium hydroxide etc.) that present pulverized-coal fired boiler, grate firing boiler or other combustion apparatus are used mainly contains the spraying flue gas desulfurization method, in-furnace calcium spraying adds humidification activation method and tail flue gas dry-type circulating fluidized bed desulfurization method.Before the calcium-based desulfurizing agent utilization rate lower (being generally 0.3-0.4) of flue gas desulfurization technique of binomial technology, smoke desulfurization efficiency not high (calcium sulfur ratio be 2 o'clock reach 0.5-0.8); Perishable and knot black dirt on reactor or humidification activation device inwall influences continuous safe operation simultaneously.Germany metal Co., Ltd is at Chinese patents CN85105199A, i.e. the dry-type circulating fluidized bed separation of flow method of tail flue gas ", effectively overcome above-mentioned defective, its calcium-based desulfurizing agent utilization rate is higher, can reach 0.7; Smoke desulfurization efficiency also has clear improvement, and can only reach more than 0.8 in 1.5 o'clock at calcium sulfur ratio.This kind dry-type circulating fluidized bed desulfurization system mainly comprises circulating fluid bed reactor, separator and outer send-back system.Its technical process is a flue gas of discharging from boiler, kiln or other combustion apparatus, sends into circulating fluid bed reactor, and its bed material is calcium-based desulfurizing agent, or the mixture of flying dust in desulfurizing agent and the flue gas.Sulfur in smoke is just reacted with the bed material, forms the solid calcium sulfite and stays in the desulfurizing agent, quantitatively discharges desulphurization system then.Discharge unreacted that flue gas leaves sorbent particle suspension completely with recirculating fluidized bed, enter and be arranged on fluid bed and send out the particle separator of the routine of the different types of answering the device outside (for example cyclone separator, venetian blind type inertia separator, electrostatic precipitator, sack cleaner etc., this type of separator or employing separately, or series connection is used), and the unreacted that separator is separated completely desulfurizing agent bed material send fluid bed back to, make it at fluid bed be attached in the loop that outside separator forms and circulate.The furnace high-temperature that this kind desulfur technology is different from fluidized bed combustion takes off thin, but with the flue gas of discharging as fluidizing gas, this kind desulfur technology since only outer part from and the circulation, internal circulating load is big, equipment is required high, its flue gas circulating resistance is also bigger, and flue gas circulation drag overall can be greater than 1500Pa in the loop.This just causes the raising of operating cost and the heavy wear of equipment.
Above-mentioned in recent years technology has had new development again, list of references for example: H.Sauer et al, " Opert ing Experience with a Dry FGD Plant using a Circulating FluidBed (CFB) at the Brown-Coal-Fired Power Station in Borken; FederalRepublic of Germany ", VGB Kraftwerkstechnik, Vol.69, No.10, (1989), pp.887-892.Introduced the applicable cases of this technology on the station boiler of German burning brown coal in the literary composition, and pointed out to make 7 convergent flaring spouts (venturinozzles), to reduce the flow of flue gas resistance at the gas approach place of circulating fluid bed reactor.Go back lay special stress on simultaneously and in circulating fluidized bed desulfurization reactor, internals must not be set, to avoid etching problem.
At problems of the prior art, one of purpose of the present invention provides the method and apparatus of the flue gas desulfurization of circulation in a kind of dry desulfurizing agent bed material, make it can not only effectively improve the utilization rate and the smoke desulfurization efficiency of calcium-based desulfurizing agent, the burden of external separator is reduced relatively, and can obviously reduce total circulating resistance of flue gas, avoid corrosion, thereby reach the purpose of effective reduction operating cost.
The present invention is achieved by the following technical solutions: the method for its flue gas desulfurization is that the flue gas that combustion apparatus is discharged is sent into the calcium-based desulfurizing agent is the circulating fluid bed reactor of bed material, make sulfur in smoke and the reaction of bed material, forming the solid calcium sulfite stays in the desulfurizing agent, discharge desulphurization system then, discharge the not sorbent particle of complete reaction of part that flue gas leaves with recirculating fluidized bed; By sending fluid bed back to behind the separator that is attached to the fluid bed outside, it is circulated in the loop that the separator of fluid bed and outside is formed, it is characterized in that by being arranged on the gas-solid separating device on fluid-bed sweetening reactor top, flue gas is separated with most of Solid Bed material, the bed material that separates is returned emulsion zone again, make sulfur in smoke and bed expect fully to contact and react, thereby form the fume desulphurization method that circulates in the bed material.
The device of realizing above-mentioned sulfur method is achieved in that the flue gas desulfur device that circulates in a kind of dry desulfurizing agent bed material, mainly comprise with the calcium-based desulfurizing agent being circulating fluidized bed desulfurization reactor body and separator that is attached to this reactor outside and the outer send-back system that bed is expected, mainly be provided with smoke inlet at the fluid-bed sweetening reactor lower part, slag-drip opening, bellows and air-distribution device is characterized in that on the top of fluid-bed sweetening reactor gas-solid separating device being set.
Above-mentioned gas-solid separating device adopts a plurality of spinning disks to form, and this spinning disk and reactor wall seal with annular top cover, annular top cover is partly done funnel and is connected the feed back pipeline section, above-mentioned gas-solid separating device also can be taked following structure: it is to be extended upward by the fluidized-bed reactor wall, cross after the smoke evacuation exit and the termination hat cavity that forms, its top cover is a flat board level or that tilt.
Because adopt such scheme, promptly the Dual-Phrase Distribution of Gas olid structure of the inner separator uniqueness in the fluidized-bed reactor (below will describe in detail) makes flue gas separate with most of Solid Bed material, and the bed material is fallen after rise in a large number along the near wall region territory of reactor, form circulation in the bed material.The bed material falling amount in bed can reach 80% (being that the inner loop amount is more than 4 times of outside internal circulating load in the system) of up amount, make in the reactor the bed material as far as possible fully with flue gas in sulfur oxide react.The interior circulation of this bed material is different from stirring and moving of general fluid bed lower bed material, but makes the bed material fall back to the bottom from top, circulation and desulphurization reaction in doing in bed.
Accompanying drawing 1 is expressed the structural representation of the flue gas desulfur device that circulates in the fluid-bed sweetening inside reactor is provided with the desulfurizing agent bed material of gas-solid separating device, what its gas-solid separating device adopted is a plurality of spinning disks.
Accompanying drawing 2 is 1-1 cutaway views of accompanying drawing 1, expresses the annexation of concrete structure and this spinning disk and the reactor wall of a plurality of spinning disks.
Accompanying drawing 3 is the 11-11 cutaway view of accompanying drawing 1, expression be annular top cover partly do funnel and be connected the feed back pipeline section.
What accompanying drawing 4 was represented is the structural representation of another kind of embodiment of the present invention, its separator is to be extended upward by the fluidized-bed reactor wall, cross after the smoke evacuation exit and the termination hat cavity that forms, the top of this hat cavity is a flat board level or that tilt.
Describe technical process of the present invention in detail below in conjunction with accompanying drawing, concrete structure and preferred forms:
With accompanying drawing 1 is example, and the present invention is mainly by with the calcium-based desulfurizing agent being the fluid-bed sweetening reactor body 1 of bed material and separator 2 and the outer send-back system 4 that is attached to this reactor outside.On the top of fluidized-bed reactor 1 gas-solid separating device 3 is housed, this separator is made up of 6-24 spinning disk, and the elevation angle of its spinning disk 5 is generally 15 °-30 °, is generally 25 °.The flue gas circulating resistance of this gas-solid separating device is no more than 300Pa usually.During operation, the flue gas that contains sulfur dioxide of discharging from combustion apparatus enters the bellows 16 of desulfurization reactor 1 bottom from smoke inlet 19, behind air-distribution device 17, with suitable calcium sulfur ratio 1.2-2.0, is generally 1.5 in the bed material, sprays into calcium-based desulfurizing agent continuously.Calcium-based desulfurizing agent can make water slurry 12, is generally lime white; Or without water slurry, desulfurizing agent changed in burner hearth, spray into agstone, under furnace high-temperature, be sintered into calcium oxide powder and absorb sub-fraction sulfur dioxide, enter desulfurization reactor 1 with flue gas and coal dust flying dust then, also can in bed, spray water 13; Or in the bed material, spray into desulfurizing agent powder 12, and promptly in bed, spraying into suitable calcium sulfur ratio continuously, also spray water 13 simultaneously this moment in the bed material.Spray lime white or water spray make original flue gas from boiler or the discharge of other combustion apparatus, from the common temperature more than 120 ℃, reduce to 50-85 ℃ rapidly in recirculating fluidized bed, are generally 70 ℃ even bed temperature, than the high 5-35 of flue gas dew point ℃.Because it is very fast that lime white that sprays into or water evaporate in fluid bed, bed material circulation up and down is very fast, and bed material integral body remains dry state.Solid particle is in the gas-solid separating device 3 on reactor top, because inertia and bump spinning disk 5, major part is separated; This part bed material directly is transmitted back in the dense bed of fluid bed along the near wall region territory of reactor 1 or along ad hoc funnel and pipeline section (can be contained within the reactor 1, or outside), thereby forms the interior circulation of bed material in desulfurization reactor 1.The diameter of spinning disk 5 is the 0.7-0.9 of reactor 1 top equivalent inside diameter D, is generally 0.8 times.With annular top cover 23 sealings, make it to help the original denseer particle that rises in nearly wall place and transfer the whereabouts between the wall of spinning disk 5 and reactor 1.The annulus top cover can partly be done funnel 15, and connects feed back pipeline section 6.Also contain the unreacted flue gas of sorbent particle completely from what reactor 1 was discharged, through being attached to the separator 2 (or deduster) of outside routine, collected desulfurizing agent and fly ash mixture are sent into the emulsion zone of desulfurization reactor 1 by outside loop back device 4, form the outer circulation loop of a small amount of desulfurizing agent bed material.The flue gas that upwards flows from desulfurization reactor 1 bottom has contacted by inside and outside a large amount of unreacteds of sending here desulfurizing agent bed material completely that loops back, and sulfur dioxide is absorbed in a large number.Simultaneously, the bed material that contains calcium sulfite is quantitatively discharged from the slag-drip opening 21 of reactor.
Another kind of embodiment of the present invention is the structure that adopts as shown in Figure 4, and its gas-solid separating device 3 is formed termination hat cavitys 18. on the smoke evacuation exit 20 of desulfurization reactor 1.It is to be extended upward by the fluidized-bed reactor wall, crosses after the smoke evacuation exit 20 formedly, and top board 24 is a flat board level or that tilt.The height of cavity segment, the top edge of promptly crossing smoke evacuation exit 20 should be equal to or greater than 1/2 of cross section equivalent diameter D on the desulfurization reactor to the height of top board.Experiment shows, the very simple special construction of this likeness in form can make flue gas when turn discharging desulfurization reactor 1, bed material particle before cavity and in the cavity along the reactor axis upward speed decrescence.Thereby, in the Dual-Phrase Distribution of Gas olid structure that the cavity of this uniqueness forms, granule density is increased gradually and gathering into bulk along axis, cluster of grains is more at nearly wall place.This dough can descend and merge mutually under the gravity effect, grow up gradually as seed, impel in the reactor, the near wall region territory on top is gathered to become bigger cluster of grains and is moved downward, thereby increases a flue gas and an interior circulation that fully contacts and form the bed material of expecting.Therefore the termination hat cavity 18 on this desulfurization reactor top is a kind of gas-solid separating device equally, can facilitate a large amount of interior circulation of bed material.
The present invention compared with prior art, except do not resemble emphasize in the above-mentioned documents Arrange in the fluid bed outside the problem that internals cause corrosion, also have following characteristics and beneficial effect: because Adopted method and the device of circulation in the dry desulfurizing agent bed material, therefore most of bed material can be anti-in desulfurization Answer and carry out interior separation and circulation in the device; Make from the flue gas that reactor is discharged and only carry a small amount of material, this Sample just makes the burden of outer separator relatively reduce, and its flue gas circulation drag overall also obviously reduces. Send out for this The drag overall of whole flue gas desulphurization system can be less than 1500Pa in bright, in addition only for this reason 2/3 of value with Lower, thereby it is less to consume electric energy. Because the interior circulation of bed material, make the flue gas that contains sulfur dioxide instead Answer to have contacted the very high a large amount of not desulfurizing agent bed materials of complete reaction of granule density in the device, it is fully connect Touch and reaction, thereby effectively raise the utilization rate of calcium-based desulfurizing agent and the desulfuration efficiency of flue gas, Calcium sulfur ratio is that 1.5 o'clock flue gas desulphuization rates can reach more than 0.85. Reaching under the same flue gas desulphuization rate, The prior art that compares, can effectively save the power consumption that makes flue gas circulation and desulfurizing agent expend and The investment cost of flue gas desulfurization device. When reaching flue gas near wet desulphurization and take off the rate of dredging, its investment Expense only for wet desulphurization half or still less. Because bed material integral body remains dry state, desulfurization reactor Internals and relevant pipeline, can not resemble in wet method and semi-dry desulphurization system easy being corroded.
Claims (6)
1. the fume desulphurization method of circulation in the dry desulfurizing agent bed material, it is that the flue gas that combustion apparatus is discharged is sent into the calcium-based desulfurizing agent is the circulating fluid bed reactor of bed material, make sulfur in smoke and the reaction of bed material, forming the solid calcium sulfite stays in the desulfurizing agent, discharge desulphurization system then, discharge the not sorbent particle of complete reaction of part that flue gas leaves with recirculating fluidized bed, by sending fluid bed back to behind the separator that is attached to the fluid bed outside, it is circulated in the loop that the separator of fluid bed and outside is formed, it is characterized in that by being arranged on the gas-solid separating device of fluid-bed sweetening inside reactor floating zone, flue gas is separated with most of Solid Bed material, make the bed that separates expect backspace emulsion zone again, make sulfur in smoke and bed expect fully to contact and react, thereby form the fume desulphurization method that circulates in the bed material.
2, the flue gas desulfur device of circulation in a kind of dry desulfurizing agent bed material, it mainly comprises with the calcium-based desulfurizing agent being the recirculating fluidized bed separation of flow reactor body [1] of bed material, be attached to the separator [2] and the outer send-back system of this reactor outside, be provided with slag-drip opening [21], bellows [16] and air-distribution device [17] in the bottom of described fluid bed separation of flow reactor, side bottom at this reactor is provided with smoke inlet [19], this smoke inlet links to each other with wind feather cockscomb [16], it is characterized in that on the top of the fluid bed separation of flow reactor gas-solid separating device [3] being set.
3. the flue gas desulfur device of circulation in the dry desulfurizing agent bed material according to claim 2, its special sheet is that described interior separator adopts a plurality of spinning disks to form, and this spinning disk and fluidized-bed reactor [1] wall seals with annular top cover, and annular top cover part funnel also connects the feed back pipeline section.
4. according to the flue gas desulfur device that circulates in claim 2 or the 3 described dry desulfurizing agent bed materials, it is characterized in that above-mentioned spinning disk is made up of 6-24 spinning disk, the diameter of this spinning disk is 0.7-0.9 a times of separation of flow reactor top equivalent internal diameter, and its elevation angle is 15 °-30 °.
5. the flue gas desulfur device of circulation in the dry desulfurizing agent bed material according to claim 2, it is characterized in that described interior separator is towards last extension by the fluid-bed sweetening reactor wall, cross after the smoke evacuation exit and the termination hat cavity that forms, its top cover is a flat board level or that tilt.
6. the flue gas desulfur device of circulation in the dry desulfurizing agent bed material according to claim 5, the height that it is characterized in that described termination hat cavity are equal to or greater than 1/2 of cross section equivalent internal diameter on the fluidized-bed reactor.
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| Application Number | Priority Date | Filing Date | Title |
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| CN97103839A CN1087643C (en) | 1997-04-04 | 1997-04-04 | Flue gas desulfurization process and device of dry desulfurizing agent bed material internal circutation |
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| CN97103839A CN1087643C (en) | 1997-04-04 | 1997-04-04 | Flue gas desulfurization process and device of dry desulfurizing agent bed material internal circutation |
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| CN1087643C true CN1087643C (en) | 2002-07-17 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1089023C (en) * | 1998-10-16 | 2002-08-14 | 清华大学 | Middle temp. dry type circulating fluidized bed fume desulfurizing method and device |
| CN1114467C (en) * | 2000-12-15 | 2003-07-16 | 清华大学 | Dry cyclic suspension bed fume desulfurizing process and system |
| CN1224446C (en) * | 2003-08-15 | 2005-10-26 | 武汉凯迪电力股份有限公司 | large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization |
| US7641878B2 (en) * | 2006-02-21 | 2010-01-05 | Pmi Ash Technologies, Llc | Fly ash beneficiation systems with sulfur removal and methods thereof |
| CN109647148B (en) * | 2019-02-28 | 2021-11-12 | 兖矿集团有限公司 | Circulating fluidized bed boiler flue gas desulfurization system and treatment method thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5500195A (en) * | 1992-11-13 | 1996-03-19 | Foster Wheeler Energy Corporation | Method for reducing gaseous emission of halogen compounds in a fluidized bed reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5500195A (en) * | 1992-11-13 | 1996-03-19 | Foster Wheeler Energy Corporation | Method for reducing gaseous emission of halogen compounds in a fluidized bed reactor |
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