CN109589777A - A kind of Multi-stage spiral circulating fluid bed desulfurization device and its sulfur method - Google Patents
A kind of Multi-stage spiral circulating fluid bed desulfurization device and its sulfur method Download PDFInfo
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- CN109589777A CN109589777A CN201811538794.1A CN201811538794A CN109589777A CN 109589777 A CN109589777 A CN 109589777A CN 201811538794 A CN201811538794 A CN 201811538794A CN 109589777 A CN109589777 A CN 109589777A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 69
- 230000023556 desulfurization Effects 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 45
- 239000012530 fluid Substances 0.000 title claims abstract description 31
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 11
- 239000011593 sulfur Substances 0.000 title abstract description 7
- 229910052717 sulfur Inorganic materials 0.000 title abstract description 7
- 239000003546 flue gas Substances 0.000 claims abstract description 202
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 188
- 238000010521 absorption reaction Methods 0.000 claims abstract description 78
- 239000002250 absorbent Substances 0.000 claims abstract description 35
- 230000002745 absorbent Effects 0.000 claims abstract description 35
- 239000007787 solid Substances 0.000 claims abstract description 31
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 9
- 239000006227 byproduct Substances 0.000 claims abstract description 7
- 230000009471 action Effects 0.000 claims abstract description 6
- 239000000779 smoke Substances 0.000 claims description 52
- 230000001105 regulatory effect Effects 0.000 claims description 18
- 239000007789 gas Substances 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 13
- 230000008569 process Effects 0.000 claims description 12
- 230000000149 penetrating effect Effects 0.000 claims description 10
- 239000007921 spray Substances 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 7
- 239000005864 Sulphur Substances 0.000 claims description 5
- 239000002956 ash Substances 0.000 claims description 5
- 235000019504 cigarettes Nutrition 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 239000000428 dust Substances 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 3
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 239000011575 calcium Substances 0.000 claims description 3
- 229910052791 calcium Inorganic materials 0.000 claims description 3
- 239000000470 constituent Substances 0.000 claims description 3
- 239000004571 lime Substances 0.000 claims description 3
- 229910000831 Steel Inorganic materials 0.000 claims description 2
- 239000010881 fly ash Substances 0.000 claims description 2
- 239000010959 steel Substances 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 239000011800 void material Substances 0.000 claims description 2
- 230000005484 gravity Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 6
- 235000012255 calcium oxide Nutrition 0.000 description 4
- 239000000292 calcium oxide Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000002708 enhancing effect Effects 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 1
- 238000004026 adhesive bonding Methods 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000009955 starching Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- 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
- B01D53/346—Controlling the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of Multi-stage spiral circulating fluid bed desulfurization device and its sulfur methods, belong to flue gases purification field.The device includes level-one eddy flow flue (1), second level eddy flow flue (2), three swirler flue (3), absorption tower (4), gas-solid separator (5), feed back case (6).Absorbent is sufficiently mixed under the action of Multi-stage spiral with flue gas, and is reacted under the action of water with the sulfur dioxide in flue gas, and the desulfurizing byproduct of generation is most of through gas-solid separator supplementary set and to be continued to participate in reaction by feed back case return absorption tower and set.Due to the intake method using Multi-stage spiral, make to form strong Three dimensional Turbulent flow field in absorption tower, Radial Flow intensity is enhanced, mixed effect in tower of flue gas and absorbent is improved and extends the residence time, further improves desulfuration efficiency and absorbent utilization rate.
Description
Technical field
The present invention relates to flue gases purification fields, in particular it relates to which a kind of Multi-stage spiral recirculating fluidized bed is de-
Sulphur device and its sulfur method.
Background technique
Currently, flue gas desulfurization technique can be divided into three classes substantially: wet process, dry method and semidry method.Wet desulfurizing process takes off
Sulphur agent uses slurry form, and desulfurizing byproduct water content is higher, can just obtain the lower by-product of water content after needing thickening
Object；Dry desulfurization uses dry state desulfurizing agent, and desulfurizing byproduct is also the solid of dry state；Semidry method between both wet process and dry method it
Between, desulfurizing agent is present in sweetening process with the small particles form for being atomized or humidifying, and by-product is the solid of dry state.Flue gas recirculation
Fluid-bed sweetening technique belongs to semi-dry desulphurization technology, compared with wet desulfurizing process, has investment, operating cost low, system
The features such as equipment is few, and occupied area is small, and no desulfurization wastewater discharges, has a good application prospect.
German Lurgi company develops Analyss of Desulphurization Technology of Flue Gas Recirculation Fluid-bad earliest, flue gas in absorption tower with humidification
Absorbent and circulating ash mixing, desulphurization reaction occurs under fluidising conditions, then carries out gas by pre-duster and deduster
Gu separation, most of solid particle returns to absorption tower and continues to participate in reaction, and total residence time is improved up to 30 min or more
Sorbent utilization.Further, since flue-gas temperature is consistently higher than about 20 DEG C of dew-point temperature or more, equipment is without carrying out at anti-corrosion
Flue gas is discharged without reheating in reason.
German Wulff company develops smoke backflow formula circulating fluidized bed desulfurization technique, mainly increases in absorption tower
Spoiler and tower top material reflux device, the interior circulation of the tower of reinforcing desulfuration agent, improve absorbent utilization rate and desulfuration efficiency.Separately
Outside, reflux is generated in absorption tower so that the dust content of exhaust gas stream reduces about 15 % of % ~ 30, external recirculation inventory is reduced
The % of 30 % ~ 50, alleviates the load of deduster, eliminates pre-duster, simplify process flow, makes investment and operating cost
It further decreases.
The gas suspension of F. L. Smidth company, Denmark exploitation absorbs flue gas desulfurization technique, then is by increasing external rotation
Wind separator and corresponding feed back structure increase Matter Transfer multiplying power and suspended concentration, since the suspended particulate in absorption tower is
Lime slurry and flue gas provide very big contact area, so that the sorbent utilization and desulfuration efficiency of the technique further mention
It is high.Further, since recycle stock returns to absorption tower by cyclone separator, the Dust Capacity into deduster is seldom, gas moisture condensation
A possibility that it is lower so that absorption tower can be run at lower temperatures, further increase desulfuration efficiency, but simultaneously to whirlwind point
There is strict demand from device and heat preservation, the heating etc. of returning reservoir equipment.
Patent of invention ZL 200610072800.X provides a kind of internal-external double circulation fluid-bed sweetening technique, uses simultaneously
Tower inner top spoiler and tower external cyclone cyclone separator arrangement, are further optimized air inlet, feeding structure, increase flue gas
With the residence time of the contact area and absorbent of absorbent in reactor, to further increase absorbent utilization rate.
Since gas, solid two-phase and the gas, liquid, solid Three-phase Flow in recirculating fluidized bed absorption tower have inherently non-homogeneous
Property, it is unfavorable for the raising of desulfuration efficiency and absorbent utilization rate.By the way that the inner members such as spoiler are arranged in tower, although can be
Increase the residence time of absorbent to a certain extent, but from the point of view of tissue flowing, the measure is mainly to flow field in tower
Axial distribution generation effect, influences very little to radial distribution, can further enhance the heterogeneity flowed in absorption tower instead, this
Can also flow resistance be made to increase outside, and there may be corresponding the problems such as gluing wall, abrasion.
Patent of invention ZL 200310114619.7 and patent of invention ZL 200610042312.4 provides various forms of
Absorption tower rotation/direct flow composite fluidizing device, patent of invention ZL 200910143297.6 and patent of invention ZL
201110020755.4 also provide the absorption tower structure of tangential admission, are stopped with improving in tower flow uniformity and increasing reactant
Stay the time.The mode for increasing tower inward eddy used by above-mentioned patent is conducive to the turbulence intensity that enhancing absorbs flow field in tower, changes
Mixed effect in tower of kind flue gas and absorbent simultaneously extends the residence time, but the flow field in absorption tower is still based on axial flow
It leads, Radial Flow is weaker, and in terms of improving desulfuration efficiency and absorbent utilization rate, there are still further improved spaces.
Summary of the invention
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device and its sulfur method, using Multi-stage spiral into
Gas mode makes to form strong Three dimensional Turbulent flow field in absorption tower, enhances Radial Flow intensity, improves flue gas and absorbent in tower
Interior mixed effect simultaneously extends the residence time, to further increase desulfuration efficiency and the absorption of Analyss of Desulphurization Technology of Flue Gas Recirculation Fluid-bad
Agent utilization rate.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that including level-one eddy flow flue
(1), second level eddy flow flue (2), three swirler flue (3), absorption tower (4), gas-solid separator (5), feed back case (6).
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that absorption tower (4) bottom is equipped with
Discharge gate (40) and level-one flue gas spout (41)；Middle part is equipped with secondary smoke spout (42) and three-level flue gas spout (43), two
It is additionally provided with powder spout (44) between grade flue gas spout (42) and three-level flue gas spout (43), liquid spout (45), feedback outlet
(46)；Top is equipped with exhanst gas outlet (47).
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that absorption tower (4) are without interior structure
The cylindrical type void tower of part；Bottom is the cone section of flaring, and the angle of inner wall and vertical direction is 20 ~ 45 °；Middle part is isometrical or tool
There is local reducing structure；Base diameterD bWith mid diameterD mRatio be 0.3 ~ 0.5.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that the level-one on absorption tower (4)
Flue gas spout (41) quantity is 4 ~ 8, and flue gas edge is cut to penetrating, corresponding level-one eddy flow circular diameterD 1With absorb the bottom of the tower diameterD bRatio be 0.2 ~ 0.6, the level-one flue gas flow of penetratingQ 1Account for flue gas total flowQ t30% ~ 50%, each level-one flue gas spout
Flow velocityv 1For 10 ~ 30 m/s.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that the second level on absorption tower (4)
Flue gas spout (42) quantity is 4 ~ 8, and flue gas edge is cut to penetrating, corresponding second level eddy flow circular diameterD 2With absorption tower mid diameterD mRatio be 0.4 ~ 0.8, the secondary smoke flow of penetratingQ 2Account for flue gas total flowQ t30% ~ 40%, each secondary smoke spout
Flow velocityv 2For 20 ~ 60 m/s.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that the three-level on absorption tower (4)
Flue gas spout (43) quantity is 4 ~ 8, and flue gas edge is cut to penetrating, corresponding three swirler circular diameterD 3With absorption tower mid diameterD mRatio be 0.4 ~ 0.8, the three-level flue gas flow of penetratingQ 3Account for flue gas total flowQ t20% ~ 30%, each three-level flue gas spout
Flow velocityv 3For 20 ~ 60 m/s.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that level-one eddy flow flue (1) by
Level-one flue gas supervisor and level-one flue gas branch pipe composition, level-one flue gas supervisor is equipped with level-one flue gas flow regulating valve (11), and leads to
Ring pipe is crossed to be connected with level-one flue gas branch pipe, the quantity of level-one flue gas branch pipe is 4 ~ 8, respectively with level-one flue gas spout (41) phase
Even.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that second level eddy flow flue (2) by
Secondary smoke supervisor and secondary smoke branch pipe composition, secondary smoke supervisor are equipped with secondary smoke flow control valve (21) and second level
Flue gas booster fan (22), and be connected by ring pipe with secondary smoke branch pipe, the quantity of secondary smoke branch pipe is 4 ~ 8, point
It is not connected with secondary smoke spout (42).
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that three swirler flue (3) by
Three-level flue gas supervisor and three-level flue gas branch pipe composition, three-level flue gas supervisor are equipped with three-level flue gas flow regulating valve (31) and three-level
Flue gas booster fan (32), and be connected by ring pipe with three-level flue gas branch pipe, the quantity of three-level flue gas branch pipe is 4 ~ 8, point
It is not connected with three-level flue gas spout (43).
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that gas-solid separator (5) is attached most importance to
Power formula deduster or centrifugal dust collector are connected with the exhanst gas outlet (47) of absorption tower (4) and feed back case (6).
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device, which is characterized in that feed back case (6) and gas-solid point
It is connected from device (5) and the feedback outlet (46) of absorption tower (4), and is equipped with ash discharging hole (60).
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
In the total flow containing sulfur dioxide isQ tFlue gas, by level-one flue gas flow regulating valve (11), secondary smoke flow control valve
(21), three-level flue gas flow regulating valve (31) controls, and in secondary smoke booster fan (22) and three-level flue gas booster fan
(32) under the action of, it is by flowQ 1Flue gas be sent into level-one eddy flow flue (1), flow isQ 2Flue gas be sent into second level eddy flow cigarette
Road (2), flow areQ 3Flue gas be sent into three swirler flue (3), and respectively by level-one flue gas spout (41), secondary smoke spray
Mouth (42) and three-level flue gas spout (43) enter absorption tower (4), and absorbent is by powder spout (44) or passes through after pretreatment
Liquid spout (45) enters absorption tower (4), while water is sprayed into absorption tower (4) by liquid spout (45), comes from feed back case (6)
Recycle stock by feedback outlet (46) enter absorption tower (4).
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
In absorbent and flue gas are sufficiently mixed in absorption tower (4), and are occurred instead with the sulfur dioxide in flue gas under the action of water
It answers, the desulfurizing byproduct of generation is in solid-state, and the flue gas for passing through absorption tower (4) together with flue gas and the complete absorbent of unreacted goes out
Mouth (47) enters gas-solid separator (5), and wherein the lesser solid particle of granularity leaves gas-solid separator (5) into downstream with flue gas
Cleaner, the biggish solid particle of granularity are entered feed back case (6) by supplementary set, most of to return to absorption tower by feedback outlet (46)
(4) reaction is continued to participate in, fraction passes through ash discharging hole (60) discharger of feed back case (6).
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
In the absorbent is the mixture of lime, flyash, carbide slag, steel slag or above-mentioned substance, and absorbent is existed with dry powder
Pass through powder spout (44) under the control of conveying fan into absorption tower (4) or preprocessed formation slurries, and in slurries pump
Control is lower to enter absorption tower (4) by liquid spout (45) together with water.
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
In the molar ratio of element sulphur contained in calcium constituent contained in the absorbent and flue gas is 1.2 ~ 2.0, the absorption
The running temperature of tower (4) is 70 ~ 140 DEG C, and apparent velocity of the flue gas in absorption tower (4) is 4 ~ 12 m/s, and the residence time is greater than
3 s。
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
In the equipment for controlling the solids circulation for returning to absorption tower (4) by feedback outlet (46) is feed valve or feed
Spiral.
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
According to flue gas total flowQ t, import content of sulfur dioxideC inAnd desired outlet content of sulfur dioxideC out, calculate first true
Determine flue gas flow allocation proportion and corresponding flue gas spout flow velocity, is calculated needed for determination in conjunction with the physicochemical properties of absorbent
Absorbent dosageG aAnd solids circulationG s, and calculated according to above-mentioned operating parameter and determine spray water flowG w。
The present invention provides a kind of method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, and feature exists
In the adjustment process of the flue gas flow allocation proportion and corresponding flue gas spout flow velocity is, first by adjusting level-one cigarette
Air-flow adjustable valve (11) realizes the level-one flue gas flow for the condition that meetsQ 1And level-one flue gas spout flow velocityv 1, then by adjusting two
Grade flue gas flow regulating valve (21) and secondary smoke booster fan (22) realize the secondary smoke flow for the condition that meetsQ 2And second level
Flue gas spout flow velocityv 2, realized finally by adjusting three-level flue gas flow regulating valve (31) and three-level flue gas booster fan (32) full
The three-level flue gas flow of sufficient conditionQ 3And three-level flue gas spout flow velocityv 3。
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device and its sulfur method, wherein the rotation of flue gas at different levels
Intensity of flow is respectively secondary smoke, three-level flue gas, level-one flue gas from high to low.Under this swirl strength distribution occasion, formation
Flow location form are as follows: the side wall region of absorption tower middle and lower part forms higher-pressure region, and central area forms low-pressure area, level-one flue gas and big portion
The secondary smoke divided enters central area, the secondary smoke edge of three-level flue gas and fraction by volume inspiration along the tapered helix risen
The tapered helix of decline enters central area by volume inspiration.It is drawn through in journey mutually intervolving, three strands of air-flows are in absorption tower middle and lower part shape
Gas-liquid-solid three phase flow is thoroughly mixed to form herein at strong Three dimensional Turbulent flow field, while with the absorbent of penetrating and water, and after
It is continuous to rise along multi-spiral line, pass through the upper zone on absorption tower.The three-dimensional being especially in the region of middle and lower part in absorption tower is strong
Strong turbulent flow can significantly strengthen the mass transport process of wherein gas-liquid two-phase, liquid-solid two-phase.Since sulfur dioxide removal process is by mass transfer
The chemical reaction of rate control, the enhancing of mass transport process are conducive to accelerate extent of reaction.
The present invention provides a kind of Multi-stage spiral circulating fluid bed desulfurization device and its sulfur method, is realizing in absorption tower
It, can basis by using corresponding flue gas flow regulating valve and flue gas booster fan on the basis of stating Multi-stage spiral flow location form
The service condition of different load, flow and swirl strength to flue gases at different levels carry out differential adjusting control.It is transporting at full capacity
It is more demanding to the desulfuration efficiency of device under the conditions of row, it needs flue gas booster fan to run with higher motor speed at this time, mentions
For higher pressure head to increase corresponding flue gas spout flow velocity, to enhance the turbulence intensity in absorption tower middle and lower part flow field, to accelerate
Extent of reaction, to improve desulfuration efficiency；Under the conditions of underrun, the requirement to device desulfuration efficiency decreases, this
When absorption tower middle and lower part flow field turbulence intensity and corresponding flue gas spout flow velocity can suitably reduce, i.e. flue gas booster fan can be with
Lower motor speed operation, to reduce the whole energy consumption of device.In addition, by by absorbent dosageG a, solid particle follows
Circular rectorG s, spray water flowG wConsideration is cooperateed with the adjusting in flow field control, desulfuration efficiency, plant energy consumption, supplies consumption amount can be obtained
Etc. operating parameters optimal combination, be conducive to the load adaptability of enhancement device, reduce operating cost.
Based on foregoing invention content, the device have the advantages that being:
1. since the Radial Flow in the region of absorption tower middle and lower part significantly increases, flow uniformity be improved significantly, make to absorb
Agent utilization rate is improved, to reduce absorbent usage amount.
2. extending flue gas in the stop in the region since the Radial Flow in the region of absorption tower middle and lower part significantly increases
Time, more sulfur dioxide are removed, and desulfuration efficiency is improved.
3. the consumption of shower water can accordingly subtract due to the desulphurization reaction degree of progress speed in the region of absorption tower middle and lower part
It is few, without additional setting Multi-layer sprinkling equipment.
4. due to the desulphurization reaction degree of progress speed in the region of absorption tower middle and lower part, and desulfuration efficiency is improved, therefore
The diameter and height on absorption tower can suitably reduce.
5. due to using Multi-stage spiral air intake structure, by reasonable distribution adjust flue gases at different levels flow and eddy flow it is strong
Degree, can significantly increase the load adaptability of device.Under the conditions of oepration at full load, the desulfuration efficiency of device can be improved；And low
Under load operating conditions, the whole energy consumption of device can be reduced.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram of Multi-stage spiral circulating fluid bed desulfurization device provided by the invention.
Fig. 2 is a kind of level-one eddy flow flue (1) that Multi-stage spiral circulating fluid bed desulfurization device is related to provided by the invention,
Second level eddy flow flue (2), the arrangement orientation schematic diagram of three swirler flue (3) and its corresponding flue gas spout.
Fig. 3 is a kind of inside of the absorption tower that Multi-stage spiral circulating fluid bed desulfurization device is related to (4) provided by the invention
Flow field schematic diagram.
Wherein, 1- level-one eddy flow flue, 11- level-one flue gas flow regulating valve, 2- second level eddy flow flue, 21- secondary smoke
Flow control valve, 22- secondary smoke booster fan, 3- three swirler flue, 31- three-level flue gas flow regulating valve, 32- three-level cigarette
Gas booster fan, the absorption tower 4-, 40- discharge gate, 41- level-one flue gas spout, 42- secondary smoke spout, the spray of 43- three-level flue gas
Mouthful, 44- powder spout, 45- liquid spout, 46- feedback outlet, 47- exhanst gas outlet, 5- gas-solid separator, 6- feed back case, 60- row
Grey mouth.
Specific embodiment
Below in conjunction with attached drawing, detailed description of the preferred embodiments.
Embodiment 1
Use Multi-stage spiral circulating fluidized bed device as depicted in figs. 1 and 2 to metered flow for 350000 Nm3The flue gas of/h
Carry out desulfurization process (120 DEG C of flue-gas temperature, moisture content is 10 %), import content of sulfur dioxideC inDesign value is 2000 mg/
Nm3(dry state), it is desirable that outlet content of sulfur dioxideC outFor 35 mg/Nm3(dry state).The basic structure of corresponding absorption tower (4)
Size is as follows: base diameterD bIt is set as 2.5 m, mid diameterD mIt is set as 5 m；Level-one flue gas spout (41) quantity is set as 4
A, flue gas edge is cut to penetrating, corresponding level-one eddy flow circular diameterD 1It is taken as 0.8 m；Secondary smoke spout (42) quantity is set as 4
A, flue gas edge is cut to penetrating, corresponding second level eddy flow circular diameterD 2It is taken as 3.5 m；Three-level flue gas spout (43) quantity is set as 4
A, flue gas edge is cut to penetrating, corresponding three swirler circular diameterD 3It is taken as 3.5 m.Secondary smoke booster fan (22) and three-level
Flue gas booster fan (32) is all made of frequency control, can flow and rotation according to the service condition of different load, to flue gases at different levels
Intensity of flow carries out differential adjusting control.
When device is when full-load conditions are run, i.e. flue gas total flowQ tFor 350000 Nm3/ h, import content of sulfur dioxideC inFor 2000 mg/Nm3(dry state), to meet emission request, desulfuration efficiency need to reach 98.25 %.First by adjusting level-one cigarette
Air-flow adjustable valve (11) is by level-one flue gas flowQ 1Control is in about 140000 Nm3/ h, corresponding each level-one flue gas spout
Flow velocityv 1About 15 m/s；Again by adjusting secondary smoke flow control valve (21) and secondary smoke booster fan (22) for two
Grade flue gas flowQ 2Control is in about 120000 Nm3/ h, the flow velocity of corresponding each secondary smoke spoutv 2About 45 m/s, this
When secondary smoke booster fan (22) provide pressure head be about 1000 Pa；Finally by adjusting three-level flue gas flow regulating valve
(31) and three-level flue gas booster fan (32) is by three-level flue gas flowQ 3Control is in about 90000 Nm3/ h, corresponding each three-level
The flow velocity of flue gas spoutv 3About 35 m/s, the pressure head that three-level flue gas booster fan (32) provides at this time is about 600 Pa.Using
The quick lime that calcium oxide content is 90 % is as absorbent, by element sulphur contained in calcium constituent contained in absorbent and flue gas
Molar ratio be taken as 1.3, then needed for quick lime dosageG aAbout 0.9 t/h, slurries are made by pretreatment in absorbent, and are starching
Pass through liquid spout (45) under the control of liquid pump and enters absorption tower (4) together with water.Pass through feedback outlet by pressure feeding spiral control
(46) solids circulation of absorption tower (4) is returnedG s, and by adjusting spray water flowG wGas-solid separator (5) are controlled to go out
The flue-gas temperature of mouth is not less than 70 DEG C.
When device is when low load condition is run, such as flue gas total flowQ tFor 250000 Nm3/ h, import sulfur dioxide contain
AmountC inFor 1000 mg/Nm3(dry state), to meet emission request, desulfuration efficiency need to reach 96.5 %.First by adjusting level-one
Flue gas flow regulating valve (11) is by level-one flue gas flowQ 1Control is in about 100000 Nm3/ h, corresponding each level-one flue gas spray
The flow velocity of mouthv 1About 11 m/s；It again will by adjusting secondary smoke flow control valve (21) and secondary smoke booster fan (22)
Secondary smoke flowQ 2Control is in about 85000 Nm3/ h, the flow velocity of corresponding each secondary smoke spoutv 2About 35 m/s,
The pressure head that secondary smoke booster fan (22) provides at this time is about 600 Pa；Finally by adjusting three-level flue gas flow regulating valve
(31) and three-level flue gas booster fan (32) is by three-level flue gas flowQ 3Control is in about 65000 Nm3/ h, corresponding each three-level
The flow velocity of flue gas spoutv 3About 25 m/s, the pressure head that three-level flue gas booster fan (32) provides at this time is about 300 Pa.It is required
Quick lime dosageG aIt is corresponding to reduce, about 0.3 t/h.
By the present embodiment it is found that adjusting flue gases at different levels by reasonable distribution due to the air intake structure using Multi-stage spiral
The desulfuration efficiency of device can be improved under the conditions of oepration at full load in flow and swirl strength, and under the conditions of underrun,
By using frequency control to flue gas booster fan, the whole energy consumption of device can be reduced, to significantly enhance the load of device
Adaptability.
Claims (18)
1. a kind of Multi-stage spiral circulating fluid bed desulfurization device, including level-one eddy flow flue (1), second level eddy flow flue (2), three-level
Eddy flow flue (3), absorption tower (4), gas-solid separator (5), feed back case (6).
2. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the absorption tower
(4) bottom is equipped with discharge gate (40) and level-one flue gas spout (41)；Middle part is equipped with secondary smoke spout (42) and three-level flue gas sprays
Mouth (43), is additionally provided with powder spout (44), liquid spout between secondary smoke spout (42) and three-level flue gas spout (43)
(45), feedback outlet (46)；Top is equipped with exhanst gas outlet (47).
3. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the absorption tower
It (4) is the cylindrical type void tower without inner member；Bottom is the cone section of flaring, and the angle of inner wall and vertical direction is 20 ~ 45 °；In
Portion is isometrical or with local reducing structure；Base diameterD bWith mid diameterD mRatio be 0.3 ~ 0.5.
4. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the absorption tower (4)
On level-one flue gas spout (41) quantity be 4 ~ 8, flue gas is along cutting to penetrating, corresponding level-one eddy flow circular diameterD 1With absorption tower
Base diameterD bRatio be 0.2 ~ 0.6, the level-one flue gas flow of penetratingQ 1Account for flue gas total flowQ t30% ~ 50%, each level-one
The flow velocity of flue gas spoutv 1For 10 ~ 30 m/s.
5. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the absorption tower (4)
On secondary smoke spout (42) quantity be 4 ~ 8, flue gas is along cutting to penetrating, corresponding second level eddy flow circular diameterD 2With absorption tower
Mid diameterD mRatio be 0.4 ~ 0.8, the secondary smoke flow of penetratingQ 2Account for flue gas total flowQ t30% ~ 40%, each second level
The flow velocity of flue gas spoutv 2For 20 ~ 60 m/s.
6. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the absorption tower (4)
On three-level flue gas spout (43) quantity be 4 ~ 8, flue gas is along cutting to penetrating, corresponding three swirler circular diameterD 3With absorption tower
Mid diameterD mRatio be 0.4 ~ 0.8, the three-level flue gas flow of penetratingQ 3Account for flue gas total flowQ t20% ~ 30%, each three-level
The flow velocity of flue gas spoutv 3For 20 ~ 60 m/s.
7. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the level-one eddy flow
Flue (1) is made of level-one flue gas supervisor and level-one flue gas branch pipe, and level-one flue gas supervisor is equipped with level-one flue gas flow regulating valve
(11), and by ring pipe be connected with level-one flue gas branch pipe, the quantity of level-one flue gas branch pipe is 4 ~ 8, respectively with level-one flue gas
Spout (41) is connected.
8. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the second level eddy flow
Flue (2) is made of secondary smoke supervisor and secondary smoke branch pipe, and secondary smoke supervisor is equipped with secondary smoke flow control valve
(21) and secondary smoke booster fan (22), and by ring pipe it is connected with secondary smoke branch pipe, the quantity of secondary smoke branch pipe
It is 4 ~ 8, is connected respectively with secondary smoke spout (42).
9. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the three swirler
Flue (3) is made of three-level flue gas supervisor and three-level flue gas branch pipe, and three-level flue gas supervisor is equipped with three-level flue gas flow regulating valve
(31) and three-level flue gas booster fan (32), and by ring pipe it is connected with three-level flue gas branch pipe, the quantity of three-level flue gas branch pipe
It is 4 ~ 8, is connected respectively with three-level flue gas spout (43).
10. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the gas-solid point
It is gravity type deduster or centrifugal dust collector from device (5), is connected with the exhanst gas outlet (47) of absorption tower (4) and feed back case (6).
11. Multi-stage spiral circulating fluid bed desulfurization device according to claim 1, which is characterized in that the feed back case
(6) it is connected with the feedback outlet (46) of gas-solid separator (5) and absorption tower (4), and is equipped with ash discharging hole (60).
12. the method for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device as described in claim 1, feature exist
In the total flow containing sulfur dioxide isQ tFlue gas, by level-one flue gas flow regulating valve (11), secondary smoke flow control valve
(21), three-level flue gas flow regulating valve (31) controls, and in secondary smoke booster fan (22) and three-level flue gas booster fan
(32) under the action of, it is by flowQ 1Flue gas be sent into level-one eddy flow flue (1), flow isQ 2Flue gas be sent into second level eddy flow cigarette
Road (2), flow areQ 3Flue gas be sent into three swirler flue (3), and respectively by level-one flue gas spout (41), secondary smoke spray
Mouth (42) and three-level flue gas spout (43) enter absorption tower (4), and absorbent is by powder spout (44) or passes through after pretreatment
Liquid spout (45) enters absorption tower (4), while water is sprayed into absorption tower (4) by liquid spout (45), comes from feed back case (6)
Recycle stock by feedback outlet (46) enter absorption tower (4).
13. the method according to claim 12 for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, special
Sign is that absorbent and flue gas are sufficiently mixed in absorption tower (4), and are occurred under the action of water with the sulfur dioxide in flue gas
The desulfurizing byproduct of reaction, generation is in solid-state, passes through the flue gas of absorption tower (4) together with flue gas and the complete absorbent of unreacted
It exports (47) and enters gas-solid separator (5), wherein the lesser solid particle of granularity leaves under gas-solid separator (5) entrance with flue gas
Cleaner is swum, the biggish solid particle of granularity is entered feed back case (6) by supplementary set, and most of return by feedback outlet (46) absorbs
Tower (4) continues to participate in reaction, and fraction passes through ash discharging hole (60) discharger of feed back case (6).
14. the method according to claim 12 for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, special
Sign is that the absorbent is the mixture of lime, flyash, carbide slag, steel slag or above-mentioned substance, and absorbent is with dry powder-shaped
State enters absorption tower (4) or preprocessed formation slurries by powder spout (44) under the control of conveying fan, and in slurries
Pass through liquid spout (45) under the control of pump and enters absorption tower (4) together with water.
15. the method according to claim 12 for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, special
Sign is that the molar ratio of element sulphur contained in calcium constituent contained in the absorbent and flue gas is 1.2 ~ 2.0, described
The running temperature on absorption tower (4) is 70 ~ 140 DEG C, and apparent velocity of the flue gas in absorption tower (4) is 4 ~ 12 m/s, residence time
Greater than 3 s.
16. the method according to claim 12 for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, special
Sign is, the equipment for control the solids circulation for returning to absorption tower (4) by feedback outlet (46) be fed valve or
Pressure feeding spiral.
17. the method according to claim 12 for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, special
Sign is, according to flue gas total flowQ t, import content of sulfur dioxideC inAnd desired outlet content of sulfur dioxideC out, count first
It calculates and determines flue gas flow allocation proportion and corresponding flue gas spout flow velocity, calculate determination in conjunction with the physicochemical properties of absorbent
Required absorbent dosageG aAnd solids circulationG s, and calculated according to above-mentioned operating parameter and determine spray water flowG w。
18. the method according to claim 12 for carrying out flue gas desulfurization using Multi-stage spiral circulating fluidized bed device, special
Sign is that the adjustment process of the flue gas flow allocation proportion and corresponding flue gas spout flow velocity is, first by adjusting one
Grade flue gas flow regulating valve (11) realizes the level-one flue gas flow for the condition that meetsQ 1And level-one flue gas spout flow velocityv 1, then pass through tune
Section secondary smoke flow control valve (21) and secondary smoke booster fan (22) realize the secondary smoke flow for the condition that meetsQ 2And
Secondary smoke spout flow velocityv 2, real finally by adjusting three-level flue gas flow regulating valve (31) and three-level flue gas booster fan (32)
Now meet the three-level flue gas flow of conditionQ 3And three-level flue gas spout flow velocityv 3。
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110339803A (en) * | 2019-08-13 | 2019-10-18 | 江苏和纯化学工业有限公司 | Sodium hypophosphite reaction kettle surge tank anti-blockage structure |
| CN110496518A (en) * | 2019-08-14 | 2019-11-26 | 厦门大学 | A flue gas purification device and method for step-by-step oxidation and multi-stage fluidization |
| CN112915727A (en) * | 2021-01-22 | 2021-06-08 | 四川利达华锐机械有限公司 | Hinder and spray environmental protection equipment soon with adjustable structure of power |
| CN113307352A (en) * | 2021-06-07 | 2021-08-27 | 华东理工大学 | Device and method for enhancing oxidation of sulfur-containing wastewater |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101690867A (en) * | 2009-05-25 | 2010-04-07 | 中国石油大学(北京) | Tangential-flow and direct-flow composite air intake desulfurizing tower of half dry type circulating fluidized bed (CFB) |
| US20140356264A1 (en) * | 2011-08-17 | 2014-12-04 | Lujiang Environment Technology Co., Ltd | Method and device for cleaning exhaust gases by way of fluidized bed reactors |
| CN104984646A (en) * | 2015-04-24 | 2015-10-21 | 武金玉 | Desulfurization tower flue gas nozzle and desulfurization apparatus |
| CN205308114U (en) * | 2015-12-03 | 2016-06-15 | 陕西森弗天然制品有限公司 | Exhaust gas of boiler desulfurization system |
-
2018
- 2018-12-17 CN CN201811538794.1A patent/CN109589777A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101690867A (en) * | 2009-05-25 | 2010-04-07 | 中国石油大学(北京) | Tangential-flow and direct-flow composite air intake desulfurizing tower of half dry type circulating fluidized bed (CFB) |
| US20140356264A1 (en) * | 2011-08-17 | 2014-12-04 | Lujiang Environment Technology Co., Ltd | Method and device for cleaning exhaust gases by way of fluidized bed reactors |
| CN104984646A (en) * | 2015-04-24 | 2015-10-21 | 武金玉 | Desulfurization tower flue gas nozzle and desulfurization apparatus |
| CN205308114U (en) * | 2015-12-03 | 2016-06-15 | 陕西森弗天然制品有限公司 | Exhaust gas of boiler desulfurization system |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110339803A (en) * | 2019-08-13 | 2019-10-18 | 江苏和纯化学工业有限公司 | Sodium hypophosphite reaction kettle surge tank anti-blockage structure |
| CN110496518A (en) * | 2019-08-14 | 2019-11-26 | 厦门大学 | A flue gas purification device and method for step-by-step oxidation and multi-stage fluidization |
| CN112915727A (en) * | 2021-01-22 | 2021-06-08 | 四川利达华锐机械有限公司 | Hinder and spray environmental protection equipment soon with adjustable structure of power |
| CN112915727B (en) * | 2021-01-22 | 2023-02-17 | 四川利达华锐机械有限公司 | Hinder and spray environmental protection equipment soon with adjustable structure of power |
| CN113307352A (en) * | 2021-06-07 | 2021-08-27 | 华东理工大学 | Device and method for enhancing oxidation of sulfur-containing wastewater |
| CN113307352B (en) * | 2021-06-07 | 2023-09-26 | 华东理工大学 | Device and method for strengthening oxidization of sulfur-containing wastewater |
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