CN210251828U - Energy-saving biomass boiler flue gas purification system - Google Patents
Energy-saving biomass boiler flue gas purification system Download PDFInfo
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- CN210251828U CN210251828U CN201921133652.7U CN201921133652U CN210251828U CN 210251828 U CN210251828 U CN 210251828U CN 201921133652 U CN201921133652 U CN 201921133652U CN 210251828 U CN210251828 U CN 210251828U
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Abstract
The utility model relates to an energy-saving biomass boiler flue gas purification system, which comprises a cyclone dust collector, a deacidification tower connected with an outlet pipeline of the cyclone dust collector, an SCR reactor connected with an outlet pipeline of the deacidification tower, and a chimney connected with an outlet pipeline of the SCR reactor; the top of the deacidification tower is connected with a baking soda powder bin through a pipeline; and a bag type dust collector is arranged between the deacidification tower and the SCR reactor. The utility model discloses set up cyclone and bag dust removal two-stage dust collector to set up the deacidification tower between two dust collector, set up the SCR reactor again after removing dust for the second time, can effectively ensure the high-efficient safe operation of stabilizing of clean system, set up the cigarette cooler before the chimney again, effectively promoted system heat utilization rate.
Description
Technical Field
The utility model belongs to the technical field of flue gas purification, specifically speaking relates to an energy-saving biomass boiler flue gas purification system.
Background
In recent years, with the improvement of the environmental protection attention of the nation, the emission standard of the boiler flue gas is continuously improved. If the biomass (straw) boiler flue gas is required to achieve an ultralow emission effect, no good flue gas purification process which can simultaneously meet the emission effect and is low in operation cost exists at present. At present, only a few theoretical researches exist, and the process is as follows:
the process of 'cyclone dust removal, bag dust removal, booster fan, wet desulphurization, condensing device, SGH heater, GGH heat exchanger, SCR reactor and booster fan' is very high in investment cost and operation energy consumption. In the prior art, because the booster fan, the condensing device, the SGH heater, the GGH heat exchanger and other equipment are arranged, not only is the system investment large, but also the SGH heater needs to consume steam to heat flue gas, and the system resistance of the condensing device and the GGH heat exchanger is very large, so that the system operation cost is high. Although the prior art can meet the requirement of ultra-low emission of flue gas, the operation cost is overhigh.
SUMMERY OF THE UTILITY MODEL
Aiming at various defects in the prior art, the utility model discloses people research and design an energy-saving biomass boiler flue gas purification system in long-term practice.
In order to achieve the above object, the utility model provides a following technical scheme:
an energy-saving biomass boiler flue gas purification system comprises a cyclone dust collector, a deacidification tower connected with an outlet pipeline of the cyclone dust collector, an SCR (selective catalytic reduction) reactor connected with an outlet pipeline of the deacidification tower, and a chimney connected with an outlet pipeline of the SCR reactor; the top of the deacidification tower is connected with a baking soda powder bin through a pipeline; and a bag type dust collector is arranged between the deacidification tower and the SCR reactor.
Furthermore, a first ash hopper is arranged at the bottom of the cyclone dust collector, and a first gate valve is arranged on an outlet pipeline of the first ash hopper.
Further, the bottom of the baking soda powder bin is connected with a metering and feeding screw machine, and baking soda powder is conveyed to the grading grinder through the metering and feeding screw machine.
Further, a second gate valve and a rotary discharge valve are sequentially arranged between the baking soda powder bin and the metering feeding screw machine from top to bottom; a centrifugal fan is arranged on an output pipeline of the grading grinder, and a first filter and a first silencer are arranged on an input pipeline of the grading grinder; and a first spray gun is arranged on the deacidification tower.
Further, the bottom of the deacidification tower is provided with a second ash hopper, and a third gate valve is further arranged on an output pipeline of the second ash hopper.
Furthermore, a third ash hopper is arranged at the bottom of the bag type dust collector, and a fourth gate valve is further arranged on an output pipeline of the third ash hopper.
Furthermore, an inlet pipeline of the SCR reactor is connected with a urea pyrolysis furnace, and a heater, a first fan, a second silencer and a second filter are sequentially arranged on the other side of the urea pyrolysis furnace; and an ammonia injection grid and a static mixer are also arranged on the inlet pipeline of the SCR reactor.
Furthermore, a flue gas bypass system is installed at the inlet and the outlet of the SCR reactor, and the flue gas bypass system comprises a first flue damper, a second flue damper and a third flue damper.
Further, still be equipped with the cigarette cold ware between SCR reactor and the chimney, third muffler and third filter are connected at cigarette cold ware (8) top, the second fan is connected to cigarette cold ware bottom, still be equipped with the draught fan between cigarette cold ware and the chimney.
The utility model has the advantages that:
set up cyclone and bag dust removal two-stage dust collector to set up the deacidification tower between two dust collector, set up the SCR reactor again after removing dust for the second time, can effectively ensure the high-efficient safe operation of stabilizing of clean system, set up the cigarette cooler before the chimney again, effectively promoted system heat utilization rate.
Drawings
Fig. 1 is a schematic structural diagram of the purification system of the present invention.
In the drawings: 1-cyclone dust collector, 11-first ash bucket, 12-first gate valve, 2-deacidification tower, 21-baking soda powder bin, 22-second gate valve, 23-rotary discharge valve, 24-metering feed screw machine, 25-first filter, 26-first silencer, 27-grading grinder, 28-centrifugal fan, 29-desulfurizer injection device, 210-second ash bucket, 211-third gate valve, 3-bag type dust collector, 31-third ash bucket, 32-fourth gate valve, 41-first flue damper door, 42-second flue damper door, 43-third flue damper door, 5-ammonia injection grid, 6-static mixer, 7-SCR reactor, 71-urea solution spray gun, 72-urea pyrolysis furnace, 73-a second filter, 74-a second silencer, 75-a first fan, 76-a heater, 77-an SCR catalyst, 8-a smoke cooler, 81-a third filter, 82-a third silencer, 83-a second fan, 9-an induced draft fan and 10-a chimney.
Detailed Description
In order to make the technical solution of the present invention better understood by those skilled in the art, the following description is given with reference to the accompanying drawings of the present invention for clear and complete description of the technical solution of the present invention. Based on the embodiments in the present application, other similar embodiments obtained by persons of ordinary skill in the art without any creative effort shall fall within the protection scope of the present application. In addition, directional terms such as "upper", "lower", "left", "right", etc. in the following embodiments are directions with reference to the drawings only, and thus, the directional terms are used for the purpose of illustrating the present invention and not for the purpose of limiting the same.
The present invention will be further described with reference to the accompanying drawings and preferred embodiments.
Referring to fig. 1, the utility model discloses an energy-saving biomass boiler flue gas purification system, including cyclone 1, deacidify tower 2 that links to each other with cyclone outlet pipe, the SCR reactor 7 that links to each other with 2 outlet pipe of deacidify tower (SCR means selective catalytic reduction flue gas denitration) and the chimney 10 that links to each other with 7 outlet pipe of SCR reactor.
Cyclone 1's inlet pipe way and burning furnace (not shown in the figure) intercommunication, the utility model discloses an burn burning furnace for conventional general burning furnace that burns, biomass boiler flue gas carries out the SNCR denitration in burning furnace, and the flue gas after the denitration gets into cyclone 1.
The bottom of the cyclone dust collector 1 is provided with a first ash bucket 11, and the lower part of the first ash bucket is communicated with a fly ash conveying system to convey fly ash out. The outlet pipeline of the first ash bucket 11 is provided with a first gate valve 12, the first gate valve 12 is closed at ordinary times, the first gate valve 12 is opened after a certain amount of fly ash is accumulated, and the fly ash falls into the fly ash conveying system.
The top of the deacidification tower 2 is connected with a baking soda powder bin 21 through a pipeline, the bottom of the baking soda powder bin 21 is connected with a metering and feeding screw machine 24, and baking soda powder is conveyed to a grading grinder 27 through the metering and feeding screw machine 24 and then conveyed to the deacidification tower 2. A second gate valve 22 and a rotary discharge valve 23 are sequentially arranged between the baking soda powder bin 21 and the metering feeding screw machine 24 from top to bottom and are used for controlling and conveying baking soda powder.
The output pipeline of the grading grinder 27 is provided with a centrifugal fan 28, the input pipeline of the grading grinder 27 is provided with a first filter 25 and a first silencer 26, and a proper amount of ambient air passes through the first filter 25, the first silencer 26 and the grading grinder 27 under the action of the centrifugal fan 28, and is sprayed into the deacidification tower 2 through a first spray gun 29.
The bottom of the deacidification tower 2 is provided with a second ash hopper 210, and the lower part of the second ash hopper is communicated with a fly ash conveying system to convey fly ash out. And a third gate valve 211 is arranged on an outlet pipeline of the second ash hopper 210, the third gate valve 211 is closed at ordinary times, the third gate valve 211 is opened after certain amount of fly ash is accumulated, and the fly ash falls into the fly ash conveying system.
A bag type dust collector 3 is also arranged between the deacidification tower 2 and the SCR reactor 7, a third ash bucket 31 is arranged at the bottom of the bag type dust collector 3, and an output pipeline of the third ash bucket 31 is connected with a fly ash conveying system. A fourth gate valve 32 is arranged on an output pipeline of the third ash hopper 31 and used for controlling the discharge of ash fly. The filter bag of the bag type dust collector 3 of the embodiment is made of glass fiber material and can resist the high temperature of 280 ℃ at most.
An SCR catalyst 77 is arranged in the SCR reactor 7, an inlet pipeline of the SCR reactor 7 is connected with the urea pyrolysis furnace 72, and urea solution is sprayed into the urea pyrolysis furnace 72 in a mist form through a second spray gun 71. And the ambient air is introduced into the heater 76 through the second filter 73, the second silencer 74 and the first fan 75, and enters the urea pyrolysis furnace 72 after being heated.
An output pipeline of the urea pyrolysis furnace 72 is communicated with an inlet pipeline of the SCR reactor, an ammonia injection grid 5 and a static mixer 6 are further arranged on the inlet pipeline of the SCR reactor, and mixed gas of ammonia gas and air generated after urea pyrolysis is injected into the inlet pipeline of the SCR reactor 7 through the ammonia injection grid 5 and enters the SCR reactor 7 after being uniformly mixed with flue gas through the static mixer 6.
In order to avoid the damage to the SCR catalyst 77 caused by the over-low temperature of the flue gas when the boiler is started and under abnormal working conditions, a flue gas bypass system is installed at the inlet and the outlet of the SCR reactor 7. The flue gas bypass system includes a flue gas duct and first, second and third flue damper doors 41, 42, 43. During normal operation, first flue damper door 41 and third flue damper door 43 are open, and second flue damper door 42 is closed; during abnormal operation, first flue damper door 41 and third flue damper door 43 are closed and second flue damper door 42 is opened. Therefore, the low-temperature flue gas can be effectively prevented from entering the SCR reactor to damage the catalyst.
A smoke cooler 8 is further arranged between the SCR reactor 7 and the chimney 10, the top of the smoke cooler 8 is connected with a third silencer 82 and a third filter 81, and ambient air enters the smoke cooler 8 through the third filter 81 and the third silencer 82. The bottom of the smoke cooler 8 is connected with a second fan 83, and air from the smoke cooler 83 is blown into the incinerator through the second fan 83 to support combustion. An induced draft fan 9 is arranged between the smoke cooler 8 and the chimney 10, and the smoke purified by the system is introduced into the chimney 10 through the induced draft fan 9 and is exhausted into the atmosphere.
When the biomass boiler flue gas needs to be purified, the system purification method of the utility model is used as follows:
firstly, inputting the smoke of the biomass boiler into an incinerator for SNCR (selective non-catalytic reduction) denitration, wherein the temperature in a hearth is 800-3The denitration efficiency of the SNCR is about 50 percent, namely the concentration of NOx is reduced to 175mg/Nm through the SNCR denitration3。
The high-temperature boiler flue gas after SNCR denitration passes through a front section waste heat recovery device to recover partial heat energy, the temperature of the flue gas is reduced to 140-280 ℃, then the flue gas enters a cyclone dust collector 1, large-particle smoke dust or unburned particles in the flue gas are collected by the cyclone dust collector 1 and fall into a first ash bucket 11, and then the flue gas enters a fly ash conveying system through a first gate valve 12.
The flue gas after dust removal enters a deacidification tower 2, a deacidification agent first spray gun 29 is arranged at the top of the deacidification tower 2, baking soda serving as a deacidification agent is stored in a baking soda powder bin in powder form or in granular form, the baking soda powder enters a metering feeding screw machine 24 with adjustable feeding amount through a second gate valve 22 and a rotary discharge valve 23, and the feeding amount of the baking soda is automatically adjusted through the metering feeding screw machine; the baking soda powder falls into the pipe between the first silencer 26 and the classifying grinder 27 and is ground by the classifying grinder 27 to a fineness of D90 < 20 μm (i.e., the particle size corresponding to 90% of the cumulative particle size distribution of a sample, which means that the particle size is smaller than 90% of the particles); at the same time, the ambient air passes through the first filter 25, the first silencer 26, the classifying mill under the action of the centrifugal fan 2827, is injected into the deacidification tower together with the soda powder through the first spray gun 29, the soda powder has extremely high desulfurization efficiency, is fully mixed with the flue gas in the deacidification tower, and the SO in the flue gas is removed2Deeply removing; meanwhile, because the flow velocity of the flue gas in the deacidification tower is low, part of fly ash falls into the second ash hopper 210 under the action of gravity and then falls into the fly ash conveying system through the third gate valve 211.
The deacidified flue gas enters a bag type dust collector 3, dust in the flue gas is deeply removed through the bag type dust collector, falls into a third ash hopper 31 and enters a fly ash conveying system through a fourth gate valve 32.
Then, the 40% urea solution is sprayed into the urea pyrolysis furnace 72 in the form of mist through the second spray gun 71, the ambient air enters the urea pyrolysis furnace 72 after being heated to 600 ℃ through the second filter 73, the second silencer 74, the first fan 75 and the heater 76, and the urea solution is decomposed into NH in the urea pyrolysis furnace3And H2O，NH3The mixed gas with air is sprayed into a pipeline in front of the SCR reactor 7 through the ammonia spraying grid 5, and is uniformly mixed with the flue gas through the static mixer 6 and then enters the SCR reactor 7; meanwhile, the dedusted flue gas enters an SCR reactor 7, and the flue gas and NH are reacted under the action of an SCR catalyst 77 in the SCR reactor3Mixing, and carrying out denitration reaction on the flue gas.
The flue gas pollutants denitrated by the SCR reactor 7 have extremely low concentration and enter a flue gas cooler 8, meanwhile, the ambient air enters the flue gas cooler through a third filter 81 and a third silencer 82, after the ambient air and the high-temperature flue gas fully exchange heat, the temperature of the flue gas is reduced to about 80 ℃ (the temperature is higher than the dew point temperature of the flue gas by more than 20 ℃), and then the flue gas is discharged into the atmosphere through an induced draft fan 9 and a chimney 10; in addition, the environmental air after recovering the waste heat is used as combustion air and blown into the incinerator for continuous use through the third fan 83.
The utility model discloses flue gas purification technology relates to the principle as follows:
1. the desulfurization principle is as follows:
the desulfurizing agent is generally sodium bicarbonate (sodium bicarbonate, NaHCO)3) Or slaked lime (Ca (OH)2) The acidic pollutant in the flue gas is removed by chemical adsorption, and some organic and inorganic trace substances can be removed by physical adsorption.
The desulfurization principle and process of the baking soda are as follows: NaHCO is added3Spraying the fine powder into flue gas at a temperature higher than 140 deg.C, and NaHCO at a temperature higher than 140 deg.C3Decomposition to Na2CO3、H2O and CO2The reaction equation is as follows:
2NaHCO3→Na2CO3+H2O+CO2
by formation of Na2CO3Larger grain boundaries/active regions are formed. Production of Na2CO3In the presence of Na, since no lattice exists2CO3Is very active when the flue gas temperature is higher than 140 ℃, Na2CO3Will react immediately with the acidic pollutants in the flue gas.
Due to newly generated Na2CO3Has high reaction activity at the moment of reaction, the temperature of the boiler flue gas is between 140 and 300 ℃, and the flue gas can spontaneously react with acidic pollutants in the flue gas to remove SO2The desulfurization efficiency can reach more than 95 percent:
SO2+Na2CO3→Na2SO3+CO2
SO3+Na2CO3→Na2SO4+CO2
2HF+Na2CO3→2NaF+CO2+H2O
2HCl+Na2CO3→2NaCl+CO2+H2O
small part of SO2The following reactions occur:
SO2+Na2CO3+0.5O2→Na2SO4+CO2
2. the denitration principle is as follows:
the process carries out denitration by adopting a SNCR + SCR combined denitration mode, and the SNCR principle is as follows:
spraying urea solution or ammonia water with 10 percent of reducing agent into a high-temperature (800-3And reducing NOx in the flue gas into N2And H2And O. Denitration efficiency is about 50%. The main reaction equation is as follows:
SCR denitration principle:
adding a reducing agent NH3Spraying the mixture into a flue, uniformly mixing the mixture with the flue gas, then entering an SCR reactor filled with a catalyst, and under the action of the catalyst and oxygen, reducing NOx in the flue gas into N selectively by using a reducing agent ammonia in a lower temperature range (140-2And H2And O. The denitration efficiency can reach more than 80%. The main reaction equation is as follows:
3. the dust removal principle is as follows:
the process adopts two-stage dust removal of pre-dust removal and a bag type dust remover, the pre-dust removal usually adopts a mechanical dust remover and comprises three categories of a settling chamber, an inertial dust remover and a cyclone dust remover, and the process adopts the cyclone dust remover with higher efficiency.
The cyclone dust collector utilizes centrifugal force. Centrifugal force is the centripetal separation force exerted on an object in circular motion. The separation process of a centrifugal separation heterogeneous system is generally called centrifugal separation according to the reaction force of a rotating body. It works on the principle that the mass is large during rotation, and the centrifugal force obtained by the material with high rotation speed is also large.
The filtration mechanism of a baghouse is a result of a combination of effects. Filtration mechanisms the various effects are gravity, sieving, inertial impaction, hooking effects and diffusion and electrostatic attraction. When the dusty air flow flows through the filter cloth, particles larger than the gap of the filter cloth are settled due to the action of gravity or blocked by fibers due to the action of inertia, particles smaller than the gap of the filter cloth are hooked on the surface of the filter bag by the fibers after colliding with the fibers of the filter cloth or passing through the filter cloth, smaller particles are remained on the surface and the gap of the filter cloth due to intermolecular Brownian motion, and the smallest particles may flow through the filter cloth along with the air flow and run off. The comprehensive efficiency of two-stage dust removal can reach more than 99.9%.
4. Description of the combined process:
the flue gas purification process comprises three components of desulfurization, dust removal and denitration, and strict collaborative design is required to meet the requirement that the three-section process can be safely, stably and efficiently operated.
Because the dust removal efficiency of the system needs to reach more than 99.9 percent, the bag type dust collector is the best choice, and because biomass flue gas contains unburned particles, the filter bag can be burnt through when the biomass flue gas directly enters the bag type dust collector. Therefore, a pre-dust remover is arranged in front of the dust remover to collect large particle dust in the flue gas, including dust with sparks.
Because the denitration efficiency of the system needs to reach more than 86 percent and the single SNCR efficiency is only about 50 percent, the SNCR + SCR combined denitration process needs to be adopted. And because the biomass fly ash contains a large amount of alkali metals, if the SCR reactor is arranged in a high-temperature high-dust section according to a conventional arrangement mode, the SCR catalyst can be rapidly failed.
Simultaneously, a small amount of SO exists in the flue gas3(Jordan SO)20.5% -5% of the total amount) of the denitration catalyst and NH3Reaction to produce ammonium bisulfate NH4HSO4And a large amount of ammonium bisulfate can adhere to the surface of the SCR catalyst at low temperature, so that the SCR catalyst fails, fly ash can be gathered in a flue, the flow area of the flue is reduced, and the risk of system operation is brought. Therefore, the SCR catalyst is arranged after deep desulfurization, dust removal.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the scope of the invention, i.e. the present invention is intended to cover all equivalent variations and modifications within the scope of the present invention.
Claims (9)
1. An energy-saving biomass boiler flue gas purification system is characterized by comprising a cyclone dust collector (1), a deacidification tower (2) connected with an outlet pipeline of the cyclone dust collector, an SCR reactor (7) connected with an outlet pipeline of the deacidification tower (2), and a chimney (10) connected with an outlet pipeline of the SCR reactor (7); the top of the deacidification tower (2) is connected with a baking soda powder bin (21) through a pipeline; a bag type dust collector (3) is arranged between the deacidification tower (2) and the SCR reactor (7); and a smoke cooler (8) and an induced draft fan (9) are also arranged between the SCR reactor (7) and the chimney (10).
2. The energy-saving biomass boiler flue gas purification system according to claim 1, wherein a first ash hopper (11) is arranged at the bottom of the cyclone dust collector (1), and a first gate valve (12) is arranged on an outlet pipeline of the first ash hopper (11).
3. An energy-saving biomass boiler flue gas purification system according to claim 1, characterized in that the baking soda ash bin (21) is connected with a metering and feeding screw machine (24) at the bottom, and baking soda ash is conveyed to the grading grinder (27) through the metering and feeding screw machine (24).
4. The energy-saving biomass boiler flue gas purification system according to claim 3, wherein a second gate valve (22) and a rotary discharge valve (23) are arranged between the baking soda powder bin (21) and the metering and feeding screw machine (24) from top to bottom in sequence; a centrifugal fan (28) is arranged on an output pipeline of the grading grinder (27), and a first filter (25) and a first silencer (26) are arranged on an input pipeline of the grading grinder (27); and a first spray gun (29) is arranged on the deacidification tower (2).
5. The energy-saving biomass boiler flue gas purification system according to claim 4, wherein a second ash hopper (210) is arranged at the bottom of the deacidification tower (2), and a third gate valve (211) is further arranged on an output pipeline of the second ash hopper (210).
6. The energy-saving biomass boiler flue gas purification system according to claim 1, wherein a third ash hopper (31) is arranged at the bottom of the bag-type dust collector (3), and a fourth gate valve (32) is further arranged on an output pipeline of the third ash hopper (31).
7. The energy-saving biomass boiler flue gas purification system according to claim 1, wherein an inlet pipeline of the SCR reactor (7) is connected with a urea pyrolysis furnace (72), and a heater (76), a first fan (75), a second silencer (74) and a second filter (73) are sequentially arranged on the other side of the urea pyrolysis furnace (72); and an ammonia injection grid (5) and a static mixer (6) are also arranged on the inlet pipeline of the SCR reactor.
8. The energy-saving biomass boiler flue gas purification system according to claim 7, wherein a flue gas bypass system is installed at the inlet and the outlet of the SCR reactor (7), and the flue gas bypass system comprises a first flue damper door (41), a second flue damper door (42) and a third flue damper door (43).
9. The energy-saving biomass boiler flue gas purification system according to claim 8, wherein a third silencer (82) and a third filter (81) are connected to the top of the flue gas cooler (8), and a second fan (83) is connected to the bottom of the flue gas cooler (8).
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| CN110270210A (en) * | 2019-07-18 | 2019-09-24 | 北京首创环境科技有限公司 | A kind of energy-saving biomass boiler flue gas purification system and method |
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