CN102806006B - Flue gas desulfurization purifying system - Google Patents
Flue gas desulfurization purifying system Download PDFInfo
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- CN102806006B CN102806006B CN201210315849.9A CN201210315849A CN102806006B CN 102806006 B CN102806006 B CN 102806006B CN 201210315849 A CN201210315849 A CN 201210315849A CN 102806006 B CN102806006 B CN 102806006B
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- desulfurizing agent
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Abstract
The invention provides a flue gas desulfurization purifying system, which comprises a desulfurizer, a dust remover and a chimney communicated in sequence outside the smoke outlet of an industrial furnace through a pipeline, wherein a desulfurizing agent is used for reacting in the desulfurizer; flue gas exhausted out of the industrial furnace is subjected to desulfurizing and dust removing treatment by using the desulfurizer and the dust remover; the desulfurizing agent is conveyed to the desulfurizer through a conveying device; the conveying device is provided with a stock bin and a fluidizer positioned at the inner bottom of the stock bin; the center of the fluidizer is provided with a vertical Venturi conveyer; the sucking hole of the Venturi conveyer is positioned on the upper part of the fluidizer; the upper part of the Venturi conveyer is provided with a central pipe which is used for conveying upwards; and the lower end of the Venturi conveyer is communicated with a water vapor conveying pipeline. The conveying device in the flue gas desulfurization purifying system can be used for conveying quicklime serving as a desulfurizing agent, and the quicklime can be digested into lime hydrate by using water vapor during conveying, so that the digestibility of lime in an entire process can be increased greatly, and the desulfurization efficiency is increased greatly.
Description
Technical field
The present invention relates to gas cleaning, particularly simple the and flue gas desulfurization purification system that desulfuration efficiency is higher of a kind of structure.
Background technology
Figure 1 shows that a kind of semi-dry process flue gas desulphurization process for purifying of prior art flow process, it applies suspended absorb formula recirculating fluidized bed (GSA) technology, mainly comprises desulfurizing tower 102, deduster 103, middle ash silo 111, circulation ash bin 105, lime bank 109, lime service bin 108, pressurized gas system 110 and water system 112.Desulfurizing tower 102 is switched to the pipeline before chimney 101 by connecting flue 1131, there is in the middle part of the desulfurizing tower 102 of vertical installation desulfurizing agent entrance 1021 and circulating ash entrance 1022, middle part hypomere is venturi section 1023, and venturi section 1023 lower end is connected to flue 1131 by a control of dust bend pipe 1024.As shown in Figure 2, venturi section 1023 comprises: the flaring pipeline section 10233 being formed in the convergent pipeline section 10231 of control of dust bend pipe 1024 upper end, middle tubule section 10232 and top.Flue gas is accelerated by convergent pipeline section 10231, arrive expander section 10233 by tubule section 10232 again to discharge, gas-solid mixing district 10230 is defined in the position of the contiguous tubule section 10232 of expander section 10233, the material entered from desulfurizing agent entrance 1021 and circulating ash entrance 1022 and flue gas are in gas-solid mixing district 10230 acting in conjunction, produce fierce turbulence and mix, abundant contact, in the process risen, continuous formation floccule returns downwards, and floccule constantly disintegrates again by gas lift in fierce turbulence, form Inner eycle grain flow specific to similar cycle fluidized-bed combustion boiler.
Desulfurizing agent and circulating ash enter deduster 103 through rear pass 1132 with flue gas after gas-solid mixing district 10230 mixes, through the solid particle that deduster 103 traps, the middle ash silo 111 under deduster 103 is delivered to by conveying worm, flue gas clean after dedusting enters air-introduced machine 104 through smokejack 1133, then sends into chimney 101 and discharges.
Deliver to the solid particle of middle ash silo 111, major part delivers to circulation ash bin 105 as circulating ash, then send in desulfurizing tower 102 by rotatory feeder valve, auger conveyor through circulating ash entrance 1022, another part is transported to Desulphurization bank 106 through air-transport system, regularly sends outside.
Desulfurizing agent quick lime required for desulfurizing tower 102 is transported to lime service bin 108 by lime bank 109 through air-transport system, then is sent in desulfurizing tower 102 through desulfurizing agent entrance 1021 by conveying worm.
Be provided with water injector 1124 at the flaring pipeline section 10233 of venturi section 1023, the atomized water required for desulfurization sprays into desulfurizing tower by water injector 1124.The water system 112 of water injector 1124 comprises water pipe 1123, water pump 1121 and tank 1122.Pressurized gas system 110 energy provide the Compressed Gas needed for air-transport system to middle ash silo 111, circulation ash bin 105, lime bank 109 and lime service bin 108.
During the said equipment work, flue gas introduces desulfurizing tower 102 by flue 1131 before the chimney 101 of 1#, 2# sintering machine outlet 100, in desulfurizing tower 102, flue gas with add the quick lime of desulfurizing tower 102, water, circulating ash mix mutually, form violent turbulence state, the SO under these conditions in flue gas
2can react rapidly with quick lime and generate stable CaSO
42H
2o, the SO in flue gas
2be removed, the flue gas after desulfurization enters sack cleaner 103 and removes flue dust in flue gas, and flue gas clean after dedusting is sent into chimney 101 by air-introduced machine 104 and discharged.The mechanism of the flue gas humidification activation desulphurization reaction that desulfurizing tower 102 utilizes is mainly: form water membrane, desulfurizing agent and SO on sorbent particle surface
2gas dissolves all wherein, thus makes desulphurization reaction be changed into ionic reaction in moisture film by original gas-solid reaction, in flue gas major part not timely in burner hearth, participate in reacting CaO and flue gas in SO
2reaction generates CaSO
3and CaSO
4.According to the operation principle of recirculating fluidized bed, make desulfurizing agent iterative cycles in desulfurizing tower 102, and with the SO in flue gas
2abundant haptoreaction realizes desulfurization.
Current flue gas desulfurization purification system, this desulfurizing agent of quick lime will digested at desulfurizing tower be calcium hydroxide, make effective adsorption area of desulfurizing agent in reaction little, reactivity is lower, causes the operating efficiency of this smoke adsorption purification device process waste gas lower; And material uses venturi type or silo pump type conveying, complex structure, energy consumption are high, cause production cost to improve (comprising the operating cost of purchase cost and water, electricity etc.), take larger area, are unfavorable for installation and maintenance.
Summary of the invention
For solving the technical problem that prior art exists, object of the present invention is for providing that a kind of structure is simple, floor space is little, effective filtration area is large, operating efficiency is high and the flue gas desulfurization purification system that cost of manufacture is cheap.
For achieving the above object, technical scheme of the present invention is as follows:
A kind of flue gas desulfurization purification system, comprise the devulcanizer be communicated with successively outside industrial furnace outlet flue by pipeline, deduster and chimney, desulfurizing agent is delivered to described devulcanizer, described devulcanizer and deduster carry out desulfurization and dedusting process to industrial furnace flue gas out, wherein, described desulfurizing agent is delivered to described devulcanizer by conveying device, described conveying device has feed bin and is positioned at the fluidizer of feed bin inner bottom part, described feed bin top is provided with quick lime feeding mouth and circulating ash feeding mouth, and a vertical pneumatic conveyer is established at described fluidizer center, described pneumatic conveyer material sucking port is positioned at described fluidizer top, described pneumatic conveyer top is the central tube upwards carrying out carrying, described pneumatic conveyer lower end is communicated with moisture vapor transport pipeline, described pneumatic conveyer comprises: steam jet, reducing pipe, lower manifold and described central tube, described central tube lower end is connected with reducing pipe, there is spacing to form material sucking port between steam jet and reducing pipe, steam jet is communicated with described moisture vapor transport pipeline by lower manifold, and the center line of described pneumatic conveyer overlaps with the center line of described fluidizer, described conveying device is by desulfurizing agent described in moisture vapor transport, and described desulfurizing agent is quick lime, is digested for calcium hydroxide in described conveying device and described devulcanizer by steam.
The present invention is relative to the beneficial effect of prior art, flue gas desulfurization purification system of the present invention, have by feed bin, the conveying device that the fluidizer being positioned at described feed bin inner bottom part and the venturi conveyer arranged at described fluidizer center form, the activation of tool feed bin promotes conveying device, Geldart-D particle is carried out with venturi conveyer again after utilizing fluidizer to activate desulfurizing agent, conveying device is integrated with the feed bin of prior art, circulation feed bin, pay-off, the functions such as digester are in one, simplify the technique composition of desulphurization system, eliminate electric rotary dispenser conventional in conveying, decrease feed bin and simplify conveying equipment, and through the desulfurizing agent such as calcium oxide of overactivation, inner minute aperture increases, specific area increases, and the suction-operated that can improve other polluters, system desulfuration efficiency is improved.
Described venturi conveyer lower end is communicated with moisture vapor transport pipeline, like this, described fluidizer makes the desulfurizing agent fluidization entered in described feed bin, fluidised desulfurizing agent enters described venturi conveyer from the material sucking port of described venturi conveyer, upwards delivered into the central tube of described venturi conveyer by the steam of described venturi conveyer ejection, desulfurizing agent is by steam activation in this process.Desulfurizing agent after activation enters in the middle part of devulcanizer, immediately with the SO in the flue gas entered bottom described devulcanizer
2reaction, thus the sulphur in flue gas is removed.The flue gas desulfurization purification system of prior art, non-activated desulfurizing agent enters in the middle part of desulfurizing tower, flue gas enters in described desulfurizing tower bottom described desulfurizing tower, water sprays in described desulfurizing tower from the entrance in the middle part of described desulfurizing tower and between bottom, like this, desulfurizing agent by flue gas fluidization, and to be activated by water in described desulfurizing tower, and then with the SO in flue gas
2reaction, thus remove the sulphur in flue gas.Flue gas desulfurization purification system of the present invention is compared with the flue gas desulfurization purification system of prior art, because the fluidization of desulfurizing agent and activation carry out in the independent conveying device be made up of feed bin, the fluidizer being positioned at described feed bin inner bottom part and the venturi conveyer that arranges at described fluidizer center, the fluidising effect of desulfurizing agent is good, and activation rate is high; Owing to fully can contact with the fluidization desulfurizing agent of overactivity rate in flue gas desulfurization device, desulfurized effect improves greatly.
According to above-mentioned design, described industrial furnace outlet flue place is provided with and absorbs the air to water heat exchanger that heat produces steam, and described steam passes to described venturi conveyer lower end by described moisture vapor transport pipeline.Effectively utilize waste heat, reduce energy resource consumption.
According to above-mentioned design, described feed bin is round can shaped container, and top is provided with quick lime feeding mouth and circulating ash feeding mouth, and bottom has the tapered portion being convenient to blanking, and a circular bottom is closed in the bottom of described tapered portion removably.
According to above-mentioned design, described fluidizer comprises and is fixed at fluidisation air compartment inside described bottom and several fluidisation nozzles, described fluidisation nozzles is installed on described fluidisation air compartment top, these fluidisation nozzles are communicated with external fluidized air pipe line by described fluidisation air compartment, and the center line of described fluidizer overlaps with the center line of described feed bin.One is to prevent in feed bin inner bottom part buildup, and two is to make bulk materials be subject to sufficient impact, quick lime fully can be activated and be beneficial to follow-up digestion process.
According to above-mentioned design, described fluidisation nozzles is the shower nozzle that circumferential wall offers several fumarole.The air-flow all fluidisation nozzles being sprayed with this to formation level to crosscurrent, does not upwards blow material in feed bin inner bottom part level, can prevent from being directly blown in venturi conveyer by bulk materials and causing fault.
According to above-mentioned design, described central tube inwall has high-density polyethylene ene coatings or sintered ceramic material layer.Prevent calcium hydroxide and steam from luming on the tube wall of central tube with this, thus ensure the normal operation of course of conveying
According to above-mentioned design, described devulcanizer is fluidization desulfurizing tower, have the desulfurizing agent entrance be communicated with described central tube in the middle part of it, bottom has the smoke inlet be communicated with described industrial furnace outlet flue, and top has the outlet of the flue gas after desulfurization be communicated with the entrance of described deduster.
According to above-mentioned design, be provided with grey storage vault on the downside of described deduster bottom deslagging mouth, described grey storage vault is communicated to the circulating ash feeding mouth of described conveying device by return pipeline.Thus make its better and quick lime mixture slaking, acting in conjunction can be reached to improve the technique effect of bulk devulcanization efficiency.
Accompanying drawing explanation
Fig. 1 is prior art flue gas desulfurization process for purifying schematic flow sheet.
Fig. 2 is the schematic diagram of desulfurizing tower substructure in Fig. 1.
Fig. 3 is invention flue gas desulfurization purification system process flow diagram.
Fig. 4 is the structural representation of air to water heat exchanger in the present invention.
Fig. 5 is the structural representation of gas-liquid separator in the present invention.
Fig. 6 is the side-looking structural representation of conveying device in the present invention.
Fig. 7 be in the present invention conveying device look up structural representation.
Fig. 8 is the structural representation of fluidisation nozzles in the present invention.
Fig. 9 is the diffraction spectroscopy figure before steam activation of the present invention.
Figure 10 is the diffraction spectroscopy figure after steam activation of the present invention.
Wherein, description of reference numerals is as follows: 1 industrial furnace, 2 air to water heat exchangers, 21 heating sections, 22 heat pipes, 23 external connection pipes, 24 air outlet valves, 25 water receptacles, 26 water pipes, 27 outer water tube, 20 vapor lines, 3 conveying devices, 30 first smoke pipes, 31 feed bins, 311 shells, 312 tapered portion, 313 bottoms, 314 quick lime feeding mouths, 315 circulating ash feeding mouths, 32 fluidizers, 321 fluidisation nozzles, 3211 fumaroles, 322 fluidisation air compartments, 323 fluidized wind pipelines, 324 switch valves, 33 venturi conveyers, 331 steam jet, 332 material sucking ports, 333 reducing pipes, 334 lower manifold, 335 central tubes, 34 supports, 4 gas-liquid separators, 41 main bodys, 411 separation chambers, 412 locellus again, 413 air inlets, 42 riseies, 43 liquid-proof covers, 44 gaps, 45 blast pipes, 46 outer circulating tubes, 47 gas returning ports, 48 deflection plates, 40 desulfurizing agent pipes, 5 fluidized wind systems, 51 airducts, 52 fluidized air blowers, 50 return pipelines, 6 devulcanizers, 60 mixed pipe lines, 61 desulfurizing agent entrances, 62 smoke inlets, 7 dedusters, 70 smoke-exhaust pipelines, 8 grey storage vaults, 9 air-introduced machines, 10 chimneys, 100 sintering machine outlets, 101 chimneys, 102 desulfurizing towers, 1021 desulfurizing agent entrances, 1022 circulating ash entrances, 1023 venturi sections, 10231 draw sections, 10232 tubule sections, 10233 Zhejiang expander sections, 10230 gas-solid mixing districts, 1024 control of dust bend pipes, 103 dedusters, 104 air-introduced machines, 105 circulation ash bins, 106 Desulphurization banks, 108 lime service bins, 109 lime banks, 110 pressurized gas system, 111 middle ash silos, 112 water systems, 1121 water pumps, 1122 tanks, 1123 water pipes, 1124 water injectors, 1131 flues, 1132 rear pass, 1133 smokejacks.
Detailed description of the invention
The exemplary embodiments embodying feature & benefits of the present invention will describe in detail in the following description.Be understood that the present invention can have various changes in different embodiments, it neither departs from the scope of the present invention, and explanation wherein and to be shown in be use when explain in essence, and be not used to limit the present invention.
As shown in Figure 3, the invention provides a kind of flue gas desulfurization purification system, comprising: the activation of air to water heat exchanger 2, desulfurizing agent promotes the chimney 10 of conveying device 3, fluidized wind system 5, devulcanizer 6, deduster 7, grey storage vault 8 and least significant end.Industrial furnace 1 gas outlet is communicated with devulcanizer 6 by first smoke pipe 30, devulcanizer 6 is communicated with deduster 7 through mixed pipe line 60, the activation that grey storage vault 8 under deduster 7 ash hole is connected to desulfurizing agent through return pipeline 50 promotes conveying device 3, and deduster 7 gas outlet is communicated to chimney 10 through smoke-exhaust pipeline 70.Conveying device 3 carries devulcanizer 6 desulfurizer therefor through desulfurizing agent pipe 40, air to water heat exchanger 2 heat and produce steam in industrial furnace 1 outlet flue place Absorbable rod flue gas, here the steam produced can be delivered to the activation lifting conveying device 3 of desulfurizing agent again by vapor line 20, the activation of such desulfurizing agent promotes conveying device 3 and produced steam just can be utilized as the transmitting power of desulfurizing agent.
Air to water heat exchanger 2 of the present invention can select the existing various steam evaporator utilizing waste heat, as shown in Figure 4, the equipment such as in the present embodiment, air to water heat exchanger 2 is supplied water by outer water tube 27, inner heat pipe 22, external connection pipe 23, water pipe 26 and the heating section 21 overlapped by number form.Heat pipe about 22 two ends are respectively provided with upper header 222 and lower collecting box 221, and intermediate sleeve is in heating section 21, and upper header 222 is communicated to air outlet valve 24 by external connection pipe 23, and lower collecting box 221 is communicated to water receptacle 25 by water pipe 26.Its heating section 21 is placed in flue gas hot fluid air channel, heat smoke is horizontal plunders heating section 21, water in the middle part of heating heat pipe 22 and in lower collecting box 221, water becomes steam and enters upper header 222, enters the air inlet 413 of gas-liquid separator 4 eventually through external connection pipe 23 and air outlet valve 24.
As shown in Figure 5, in the present embodiment, the round can shaped main body 41 of gas-liquid separator 4 is divided into separation chamber 411 and locellus 412 again by dividing plate 49, separation chamber 411 top tangential direction is located at by air inlet 413, separation chamber 411 and locellus 412 is again communicated with by the riser 42 at middle part, the liquid-proof cover 43 that anti-liquid phase is wriggled is equipped with in surrounding bottom riser 42, locellus 412 top is provided with the smaller blast pipe of diameter 45 again, gap 44 is left between riser 42 and blast pipe 45, be communicated with one end of outer circulating tube 46 bottom locellus 412 again, the other end of outer circulating tube 46 extend into nearly bottom, separation chamber 411 and is communicated with the gas returning port 47 of a deflection plate 48.Deflection plate 48 center, round can shaped main body 41 axle center and riser 42 axle center and blast pipe 45 axle center are all located on the same line.In running, the steam that air to water heat exchanger 2 produces tangentially enters separation chamber 411 under pressure, liquid phase in steam is thrown toward round can shaped main body 41 inwall with drops under centrifugal action, the drop got rid of to inwall gets more and more, slowly accumulate liquid film, liquid film is more and more thicker, finally under gravity, liquid film flow to bottom round can shaped main body 41 along inwall, completes a gas-liquid separation.Lower rotational gas flow is still remaining Partial Liquid Phase, the stop of deflection plate 48 is run in backspin process, inward eddy is changed into by contour stealth, enter riser 42, in riser 42, the flow velocity of swirling eddy improves further, obvious to liquid phase separation effect wherein, continue upwards after separating liquid phase, a part enters locellus 412 by the gap 44 between riser 42 and blast pipe 45 again, then again enter separation chamber 411 by outer circulating tube 46 from gas returning port 47 and complete second time separation, a part, through blast pipe 45 drainage gas-liquid separator 4, enters vapor line 20.Flow to the water then recyclable recycling bottom round can shaped main body 41.Devulcanizer 6 can select the desulphurization reaction equipment such as existing flue gas reflux circulating fluidized bed (RCFB) or fluidization desulfurizing tower [belonging to suspended absorb formula recirculating fluidized bed (GSA)], as shown in Figure 3 (with reference to Fig. 2), in the specific embodiment of the invention, devulcanizer 6 is preferably the good fluidization desulfurizing tower of current effect, it is communicated with the desulfurizing agent entrance 61 of the activation lifting conveying device 3 of desulfurizing agent by desulfurizing agent pipe 40, for being communicated with the smoke inlet 62 of industrial furnace 1 outlet flue by first smoke pipe 30 bottom devulcanizer 6, devulcanizer 6 top is then the outlet 63 of flue gas after reacting with desulphurizer mixing, outlet 63 is communicated with mixed pipe line 60.Relative to the desulfurizing tower 102 in background technology, devulcanizer 6 difference of the present invention is, because the present invention utilizes moisture vapor transport meeting predigestion desulfurizing agent, in moisture vapor transport and predigestion, the moisture film on calcium hydroxide particle surface is formed tentatively, so devulcanizer 6 does not need digestion water can normally operate yet, certainly, in order to improve the digestibility of lime again, the discharge apparatus (no longer illustrating in figure) compensating atomized water in devulcanizer 6, also can be established.Inventive desulfurization device 6 charging place simultaneously need not establish spiral feeding structure to carry out charging again, promote conveying device 3 vapor flow by the activation controlling desulfurizing agent and can control desulfurizing agent input, and circulating ash charging aperture no longer established by inventive desulfurization device 6, circulating ash enters devulcanizer 6 again after activating digestion through the activation lifting conveying device 3 of desulfurizing agent.
Deduster 7 can be electrostatic precipitator or sack cleaner, be described with sack cleaner in the present embodiment, as shown in Figure 3, deduster 7 is provided with the outlet of flue gas after the import of mixed flue gas and dedusting, import is connected with devulcanizer 6 exhanst gas outlet 63 by mixed pipe line 60, and outlet is then communicated to chimney 10 by smoke-exhaust pipeline 70.Deduster 7 is separated dust from flue gas, is provided with grey storage vault 8 on the downside of deduster 7 bottom deslagging mouth, and the flying dust separated is delivered to the grey storage vault 8 under deduster 7 by conveying worm.Due to some available calcified material in flying dust, in order to improve the utilization rate of calcium, the flying dust that deduster 7 is collected can be returned recycling in a part of circulating ash to the activation lifting conveying device 3 of desulfurizing agent.The present invention's ash storage vault 8 has the return pipeline 50 that the activation being communicated to desulfurizing agent promotes conveying device 3, this point is different from prior art, circulating ash after desulphurization reaction can carry out once desulfurization operation through return pipeline 50 to the activation lifting conveying device 3 of desulfurizing agent again, can by circulating ash again through a moisture vapor transport, thus make its better and quick lime mixture slaking, acting in conjunction can be reached to improve the technique effect of bulk devulcanization efficiency.
Conveying device 3 of the present invention can adopt existing powdery material pneumatic conveying equipment, mainly using steam as transmitting power, such as can apply Chinese Patent Application No. 201020265959.5 and be called conveying equipment in " pressure-fired continuous pneumatic convey device ", namely, a quantitative discharging device is established at a lime bin bottom discharge mouth, be communicated with at a horizontal direction venturi conveyer under quantitative discharging device again, venturi conveyer is that power conveying desulfurizing agent is to devulcanizer 6 with high-pressure steam, steam and quick lime can carry out activating and digesting in conveying, to improve the efficiency of devulcanizer 6 desulphurization reaction.Shown in Fig. 9, Figure 10 is the diffraction spectroscopy that steam Transportation activates front and back respectively, and analysis result shows, Ca (OH) in desulfurizing agent before steam Transportation
2content be 9.1%, and Ca (OH) after activation
2content reach 16.9%. after steam activation, the Ca (OH) in desulfurizing agent
2add; Result shows simultaneously, and the CaO content after steam Transportation in mixed sweetening agent reduces 6.3%, illustrates that partial CaO wherein changes Ca (OH) into
2, the efficiency of desulphurization reaction just can be promoted with this.
Molal volume due to product becomes large, and reaction is exothermic reaction again, and the molal volume of the calcium hydroxide of generation is greater than the molal volume of calcium oxide, cause particle volume to expand, make breakage of particles, generate some less particles, grain diameter is reduced, and specific area increases.Above factor causes particle swelling fracture, and particle diameter diminishes.The product that particle diameter is little has larger specific area, is conducive to desulfurization.
In flue gas desulfurization course, under the effect of steam, have activated the activity of desulfurizing agent neutral and alkali material, improve the growing amount of Ca (OH) 2, make under identical Ca/S, improve reaction rate and the reactivity of sulfur dioxide and desulfurizing agent; Improve the specific area of desulfurizing agent simultaneously, thus improve desulfuration efficiency under identical Ca/S molar ratio.
Digestion powder activity is out high, and particle diameter is little, and quantity-produced efficiency is high.The product that particle diameter is little has larger specific area, and its reactivity is greater than the large product of particle diameter, is conducive to desulfurization.
As shown in Fig. 6 to 8, the present invention separately provides a kind of activation of desulfurizing agent to promote conveying device 3, its conveying effect is better, and the predigestion rate of this desulfurizing agent of lime is higher in conveying, the activation of desulfurizing agent promotes conveying device 3 to be had feed bin 31, is positioned at fluidizer 32 and the venturi conveyer 33 of feed bin 31 inner bottom part.As shown in Figure 6, Figure 7, the feed bin 31 of the activation lifting conveying device 3 of desulfurizing agent is preferably round can shaped container, top is provided with quick lime feeding mouth 314 and circulating ash feeding mouth 315, the bottom of the shell 311 of feed bin 31 is formed with the tapered portion 312 being convenient to blanking, and by several support 34, feed bin 31 is supported in ground, a removable bottom being closed in tapered portion 312 of circular bottom 313.Conveying device has by feed bin, the conveying device that the fluidizer being positioned at described feed bin inner bottom part and the venturi conveyer arranged at described fluidizer center form, the activation of tool feed bin promotes conveying device, Geldart-D particle is carried out with venturi conveyer again after utilizing fluidizer to activate desulfurizing agent, conveying device is integrated with the feed bin of prior art, circulation feed bin, pay-off, the functions such as digester are in one, simplify the technique composition of desulphurization system, eliminate electric rotary dispenser conventional in conveying, decrease feed bin and simplify conveying equipment, and through the desulfurizing agent such as calcium oxide of overactivation, inner minute aperture increases, specific area increases, and the suction-operated that can improve other polluters, system desulfuration efficiency is improved.
Fluidizer 32 can select the fluidizing equipments such as traditional fluid bed, as long as the desulfurizing agent powder bottom feed bin 31 can be realized fluidisation.As shown in Figure 6, Figure 7, fluidizer 32 is positioned at bottom feed bin 31, and the center line of fluidizer 32 overlaps with the center line of feed bin 31.Fluidizer 32 is made up of several fluidisation nozzles 321, fluidisation air compartment 322 and fluidized wind pipeline 323, fluidisation air compartment 322 is formed at inside bottom 313, fluidisation nozzles 321 is installed on this fluidisation air compartment 322 top, and these fluidisation nozzles 321 are communicated with external fluidized air pipe line 323 by fluidisation air compartment 322.As shown in Figure 8, fluidisation nozzles 321 is better is all the shower nozzle that circumferential wall offers several fumarole 3211, the air-flow all fluidisation nozzles 321 being sprayed with this in feed bin 31 inner bottom part level to formation level to crosscurrent, one is to prevent in feed bin 31 inner bottom part buildup, two is to make bulk materials be subject to sufficient impact, quick lime fully can be activated and be beneficial to follow-up digestion process, three is upwards do not blow material, can prevent from being directly blown into by bulk materials in venturi conveyer 33 and causing fault.
As shown in Figure 3, fluidized wind system 5 is the supply system of the fluidisation gases at high pressure of conveying device 3, and comprise tracheae 51 and fluidized air blower 52, tracheae 51 is communicated with fluidized wind pipeline 323.Fluidized air blower 52 can be the roots blower of high reliability, and suction supercharging air is fluidized wind by fluidized air blower 52, can certainly be fluidized wind by suction steam or other applying gas supercharging.
Venturi conveyer 33 can select traditional venturi structure for conveying, as long as the fluidized state desulfurizing agent powder bottom feed bin 31 outwards can be carried by upper pipeline.As shown in Figure 6, Figure 7, the center line of venturi conveyer 33 overlaps with the center line of fluidizer 32.Venturi conveyer 33 comprises: steam jet 331, reducing pipe 333, lower manifold 334 and central tube 335.Central tube 335 lower end is connected with reducing pipe 333, and have spacing between steam jet 331 and reducing pipe 333 to form material sucking port 332, steam jet 331 is communicated with vapor line 20 by lower manifold 334.Central tube 335 upper end is communicated to desulfurizing agent entrance 61 by vulcanizing agent pipe 40, to carry out the conveying of desulfurizing agent.Like this, steam jet 331 and reducing pipe 333 together constitute the venturi that the activation being positioned at desulfurizing agent promotes bottom conveying device 3 and spray structure for conveying, steam is from steam jet 331 ejection at a high speed, negative pressuren zone is formed, the quick lime after inlet flow gasifying device 32 activates at material sucking port 332 place of reducing pipe 333.
The operating process of the activation lifting conveying device 3 of inventive desulfurization agent is as follows: with reference to Fig. 6, first add lime and circulating ash from feed bin 31 top quick lime feeding mouth 314 and circulating ash feeding mouth 315, meanwhile, fluidized wind system 5 passes into hp fluid air by fluidized wind pipeline 323 to fluidisation air compartment 322 and fluidisation nozzles 321, and the quicklime particles activation bottom feed bin 31 blows afloat by the air-flow that fluidisation nozzles 321 sprays; Then, lower portion pipeline 334 passes into steam, steam jet 331 sprays high speed water steam in reducing pipe 333, negative pressuren zone is formed in reducing pipe 333 porch, quick lime after fluidizer 32 activates enters reducing pipe 333 entrance, mix with high speed water steam in reducing pipe 333, upwards carry through central tube 335.What apply here is Low pressure steam, and in central tube 335, temperature is generally at 85 ~ 95 degree, and these conditions all can accelerate the digestion rate of wherein quick lime, thus makes CaO in quick lime in central tube 335, be converted into Ca (OH)
2.Owing to digesting the Ca (OH) of generation in central tube 335
2relatively lighter, density is 0.55g/cm
3, and the density of CaO is 1g/cm
3, so CaO upward velocity is little, the vertical length of central tube 335 can extend the reaction time of CaO and steam, digests calcium hydroxide completely and arrives the top of central tube 335 and be transported to devulcanizer 6 by principle of overflow and use.
With reference to Fig. 3, during flue gas desulfurization purification system work of the present invention, sulfur-containing smoke gas introduces devulcanizer 6 from industrial furnace 1 gas outlet by first smoke pipe 30; Demineralized water produces steam after being delivered to by outer water tube 27 after pressurization and being subject to flue gas in air to water heat exchanger 2, after isolating water wherein by gas-liquid separator 4, enter the conveying source of the gas as venturi conveyer 33 bottom activation lifting conveying device 3 through vapor line 20; The quick lime adding the activation lifting conveying device 3 of desulfurizing agent is blown lower formation fluidization by the fluidized wind of the fluidizer 32 of bottom, under the delivering vapor air-flow of venturi conveyer 33 drives, deliver to devulcanizer 6; In devulcanizer 6, flue gas with add the lime of devulcanizer 6, water vapour, circulating ash mix mutually, forms violent turbulence state, the SO under these conditions in flue gas
2can react rapidly with lime and generate stable CaSO
42H
2o, the SO in flue gas
2be removed; Flue gas after desulfurization enters sack cleaner 7 and removes flue dust in flue gas; Flue gas clean after dedusting is sent into chimney 10 by air-introduced machine 9 and is discharged.Flue dust under sack cleaner 7 removes, a part turns back to activation lifting conveying device 3 and carries out digestion circulation again, and another part is put into grey storage vault 8, regularly sends outside.
In addition, central tube 335 inwall of the present invention is better has ultra high density polyethylene coating or sintered ceramic material wearing layer, make its inwall unusual light and can be high temperature resistant, prevent calcium hydroxide and steam from luming on the tube wall of central tube 335 with this, thus ensure the normal operation of course of conveying.In order to prevent sticky wall, blocking and moisture content from crossing high phenomenon, the ratio of lime and water (steam) controls between 0.8 ~ 2, digests all the other required water completely and sprays at fluid-bed sweetening tower bottom.
In addition, owing to all having material slag in lime, so, need regularly to empty feed bin 31 and open bottom 313 and carry out scarfing cinder, to enhance productivity.In the present embodiment, fluidisation air compartment 322, fluidisation nozzles 321, steam jet 331 and lower manifold 334 are all fixedly installed in bottom 313, and bottom 313 is connected with tapered portion 312 by removable connected modes such as Flange joint.When needs maintenance or deslagging, pull down bottom 313 from tapered portion 312.
Further, as shown in Figure 6, the fluidized wind pipeline 323 of the activation lifting conveying device 3 of desulfurizing agent also can be communicated with by a switch valve 324 with lower manifold 334, like this, whenever necessary, fluidized wind larger for pressure can be used for steam jet 331, clean the dredging of central tube 335 being carried out to tube wall is blocked up.Separately can certainly pass into HCS by vapor line 20 to fluidized wind pipeline 323, carry out fluidisation with HCS, to obtain better activation and digestion effect.
In operation, the conveying capacity of activation lifting conveying device 3 desulfurizing agent of inventive desulfurization agent controls by the emitted dose controlling steam jet 331, certainly, also needs fluidizer 32 to coordinate.In addition, quick lime required for desulphurization system also can be transported to a lime service bin by lime bank through induction system, quantitatively be transported in real time in conveying device 3 by conveying worm more afterwards and use, macroscopically better can control the consumption of this desulfurizing agent of lime like this.Find through test, the activation of this kind of desulfurizing agent promotes conveying device 3 and 40% to 60% of CaO total amount in lime can be digested in conveying, because various places lime quality is different, so digestibility has difference, in a word, greatly can promote the predigestion rate of quick lime, thus effectively improve the reaction efficiency of desulphurization system.
Although with reference to exemplary embodiment describing the present invention, should be appreciated that term used illustrates and exemplary and nonrestrictive term.Spirit or the essence of invention is not departed from because the present invention can specifically implement in a variety of forms, so be to be understood that, above-described embodiment is not limited to any aforesaid details, and explain widely in the spirit and scope that should limit in claim of enclosing, therefore fall into whole change in claim or its equivalent scope and remodeling and all should be claim of enclosing and contained.
Claims (8)
1. a flue gas desulfurization purification system, comprise the devulcanizer, deduster and the chimney that are communicated with successively outside industrial furnace outlet flue by pipeline, desulfurizing agent is delivered to described devulcanizer, and described devulcanizer and deduster carry out desulfurization and dedusting process to industrial furnace flue gas out, it is characterized in that
Described desulfurizing agent is delivered to described devulcanizer by conveying device, described conveying device has feed bin and is positioned at the fluidizer of feed bin inner bottom part, described feed bin top is provided with quick lime feeding mouth and circulating ash feeding mouth, and a vertical pneumatic conveyer is established at described fluidizer center, described pneumatic conveyer material sucking port is positioned at described fluidizer top, described pneumatic conveyer top is the central tube upwards carrying out carrying, and described pneumatic conveyer lower end is communicated with moisture vapor transport pipeline;
Described pneumatic conveyer comprises: steam jet, reducing pipe, lower manifold and described central tube; Described central tube lower end is connected with reducing pipe, there is spacing to form material sucking port between steam jet and reducing pipe, steam jet is communicated with described moisture vapor transport pipeline by lower manifold, and the center line of described pneumatic conveyer overlaps with the center line of described fluidizer;
Described conveying device is by desulfurizing agent described in moisture vapor transport, and described desulfurizing agent is quick lime, is digested for calcium hydroxide in described conveying device and described devulcanizer by steam.
2. flue gas desulfurization purification system as claimed in claim 1, is characterized in that, described industrial furnace outlet flue place is provided with and absorbs the air to water heat exchanger that heat produces steam, and described steam passes to described pneumatic conveyer lower end by described moisture vapor transport pipeline.
3. flue gas desulfurization purification system as claimed in claim 2, it is characterized in that, described feed bin is round can shaped container, and bottom has the tapered portion being convenient to blanking, and a circular bottom is closed in the bottom of described tapered portion removably.
4. flue gas desulfurization purification system as claimed in claim 3, it is characterized in that, described fluidizer comprises and is fixed at fluidisation air compartment inside described bottom and several fluidisation nozzles, described fluidisation nozzles is installed on described fluidisation air compartment top, these fluidisation nozzles are communicated with external fluidized air pipe line by described fluidisation air compartment, and the center line of described fluidizer overlaps with the center line of described feed bin.
5. flue gas desulfurization purification system as claimed in claim 4, it is characterized in that, described fluidisation nozzles is the shower nozzle that circumferential wall offers several fumarole.
6. the flue gas desulfurization purification system as described in any one of claim 1 to 5, is characterized in that, described central tube inwall has high-density polyethylene ene coatings or sintered ceramic material layer.
7. flue gas desulfurization purification system as claimed in claim 6, it is characterized in that, described devulcanizer is fluidization desulfurizing tower, there is in the middle part of it desulfurizing agent entrance be communicated with described central tube, bottom has the smoke inlet be communicated with described industrial furnace outlet flue, and top has the outlet of the flue gas after the desulfurization be communicated with the entrance of described deduster.
8. the flue gas desulfurization purification system as described in any one of claim 3 to 5, is characterized in that, be provided with grey storage vault on the downside of described deduster bottom deslagging mouth, described grey storage vault is communicated to the circulating ash feeding mouth of described conveying device by return pipeline.
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| CN201210315849.9A CN102806006B (en) | 2012-08-30 | 2012-08-30 | Flue gas desulfurization purifying system |
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| CN102806006B true CN102806006B (en) | 2015-06-24 |
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| CN105561753A (en) * | 2016-01-26 | 2016-05-11 | 南京圣火环境科技有限公司 | Novel dry process cement kiln flue gas online desulfurization device and technology |
| CN108671715A (en) * | 2018-05-11 | 2018-10-19 | 南京师范大学 | A kind of coal-fired flue-gas sulfur trioxide removing means and its application method and application |
| CN109045909A (en) * | 2018-08-31 | 2018-12-21 | 广州市环境保护工程设计院有限公司 | Environmentally friendly dust-arrest device for Furniture manufacturing workshop |
| CN112604611B (en) * | 2020-11-26 | 2022-03-29 | 清华大学 | Device and method for carrying out chemical energy storage/discharge by using carbide slag |
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| CN102114386B (en) * | 2009-12-30 | 2013-06-12 | 中国环境科学研究院 | Desulfurization and demercuration method for flue gas |
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| US5749684A (en) * | 1995-06-07 | 1998-05-12 | Fosfoquim S.A. | Particulate material feeding apparatus and process |
| CN1307926A (en) * | 2000-12-15 | 2001-08-15 | 清华大学 | Dry cyclic suspension bed fume desulfurizing process and system |
| CN2512998Y (en) * | 2001-12-04 | 2002-09-25 | 上海新星静电喷涂设备厂 | Coal firing boiler smoke desulfurizing agent Ca(OH)2 powder fluidizing bucket |
| CN2843598Y (en) * | 2005-11-04 | 2006-12-06 | 李仁刚 | Smoke circulating fluidized-bed desulfurizer |
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