CN213492812U - Flue gas treatment system - Google Patents
Flue gas treatment system Download PDFInfo
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- CN213492812U CN213492812U CN202022408316.8U CN202022408316U CN213492812U CN 213492812 U CN213492812 U CN 213492812U CN 202022408316 U CN202022408316 U CN 202022408316U CN 213492812 U CN213492812 U CN 213492812U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 198
- 239000003546 flue gas Substances 0.000 title claims abstract description 196
- 239000000428 dust Substances 0.000 claims abstract description 78
- 239000000779 smoke Substances 0.000 claims abstract description 47
- 239000012717 electrostatic precipitator Substances 0.000 claims abstract description 27
- 238000000034 method Methods 0.000 claims abstract description 12
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 40
- 238000010521 absorption reaction Methods 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 19
- 238000005406 washing Methods 0.000 claims description 16
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 14
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 14
- 239000004571 lime Substances 0.000 claims description 14
- 239000003344 environmental pollutant Substances 0.000 claims description 12
- 238000012856 packing Methods 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 12
- 231100000719 pollutant Toxicity 0.000 claims description 12
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 12
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 8
- 239000013618 particulate matter Substances 0.000 claims description 8
- 239000010802 sludge Substances 0.000 claims description 8
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 7
- 229910052753 mercury Inorganic materials 0.000 claims description 7
- 230000002378 acidificating effect Effects 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 150000002500 ions Chemical class 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 238000012546 transfer Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 230000000379 polymerizing effect Effects 0.000 claims description 2
- 238000010791 quenching Methods 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims 1
- 238000005200 wet scrubbing Methods 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 6
- 239000002253 acid Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 239000000443 aerosol Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000012716 precipitator Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000008570 general process Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Treating Waste Gases (AREA)
Abstract
A flue gas treatment system comprises an electrostatic dust collector, a flue gas heat exchanger, a quencher, a wet scrubbing tower and a bag type dust collector; the electrostatic precipitator is disposed upstream of the flue gas heat exchanger, the quencher, and the wet scrubber; the method is characterized in that the flue gas treated by the electrostatic dust collector is input into the flue gas heat exchanger; the baghouse is disposed downstream of the smoke heat exchanger, the quencher, and the wet scrubber so that the smoke processed through the smoke heat exchanger, the quencher, and the wet scrubber is input to the baghouse.
Description
Technical Field
The present disclosure relates to a flue gas treatment system, and more particularly, to a flue gas treatment system for sludge incineration.
Background
Fig. 1 shows a prior art flue gas treatment system for sludge incineration, where the flue gas temperature of the waste heat recovery system from the outlet of the sludge fluidized bed is about 200 ℃; the temperature of the flue gas after electrostatic dust collection is about 190 ℃; the temperature of the flue gas at the outlet of the bag type dust collector is about 180 ℃; the temperature of the smoke at the outlet of the high-temperature side of the smoke heat exchanger is about 140 ℃; the temperature of the flue gas at the outlet of the quencher is about 80 ℃; the temperature of the smoke at the low-temperature side inlet of the smoke heat exchanger is about 50 ℃; the smoke temperature at the low-temperature side outlet of the smoke heat exchanger is about 120 ℃; the temperature of the flue gas at the outlet of the ID fan is about 130 ℃.
The following problems exist in the prior art:
1) in order to ensure that the temperature of the flue gas entering the bag type dust collector is suitable for the activated carbon to adsorb gaseous pollutants, the conventional treatment process needs to reduce the temperature of the flue gas to a proper range by increasing the heat exchange area of a waste heat recovery system;
2) the temperature condition of the flue gas entering the bag type dust collector is not particularly suitable for the activated carbon to adsorb gaseous pollutants, and the adsorption capacity of the activated carbon is poor;
3) the bag filter is arranged at the upstream of the wet washing tower, and the filtering area of the bag filter is large;
4) aerosols formed by wet scrubbers are difficult to remove.
SUMMERY OF THE UTILITY MODEL
In order to address one or more of the deficiencies in the prior art, according to one aspect of the present disclosure, a flue gas treatment system is provided, which includes an electrostatic precipitator, a flue gas heat exchanger, a quencher, a wet scrubber and a bag house, wherein the electrostatic precipitator is configured to remove particulate matter and solid phase heavy metals; the smoke heat exchanger prevents white smoke from being generated in smoke emission; removing acid gas by a wet scrubber; the bag house scrubber combines activated carbon and lime injection to remove mercury and other gaseous pollutants.
The electrostatic precipitator is disposed upstream of the flue gas heat exchanger, the quencher, and the wet scrubber.
The flue gas treated by the electrostatic precipitator is input into the flue gas heat exchanger.
The baghouse is disposed downstream of the smoke heat exchanger, the quencher, and the wet scrubber so that the smoke processed through the smoke heat exchanger, the quencher, and the wet scrubber is input to the baghouse.
According to the above aspect of the present disclosure, powdered activated carbon for adsorbing gaseous pollutants remaining in flue gas is provided in the flue of the baghouse.
According to the above aspects of the present disclosure, mercury and other gaseous pollutants remaining in flue gas are adsorbed in a flue of the baghouse by spraying the activated carbon.
According to the above aspects of the present disclosure, powdered lime is further provided in the flue of the bag house.
According to the above aspects of the present disclosure, the flue gas from the low temperature side outlet of the flue gas heat exchanger is delivered to the baghouse inlet of the baghouse.
The temperature of the flue gas entering the inlet of the bag type dust collector is 125-145 ℃. When the temperature of the flue gas is not higher than 150 ℃, the mercury is effectively adsorbed by spraying activated carbon, and the effects of enhanced adsorption and advanced treatment (deacidification) can also be achieved by synchronously adding a certain amount of lime.
And the flue gas treated by the bag type dust collector is conveyed to a chimney through an ID fan through an outlet of the bag type dust collector.
The temperature of the flue gas passing through the outlet of the bag type dust collector is 120-140 ℃.
The bag type dust collector intercepts active carbon, lime and residual extremely small amount of particles in the flue gas, thereby realizing the purpose of thoroughly purifying the flue gas. The dust removal efficiency of the bag type dust collector can reach more than 99.9 percent, and submicron particles can be removed.
According to the above aspects of the present disclosure, the bag house is further provided with an auger.
The screw conveyor is arranged to discharge the activated carbon, the lime and the remaining particulate matter in the flue gas that are trapped by the bag house.
According to the above aspects of the present disclosure, the electrostatic precipitator is provided with an electrostatic precipitator inlet and an electrostatic precipitator outlet.
And the flue gas from the outlet of the sludge fluidized bed enters the electrostatic dust collector through the inlet of the electrostatic dust collector.
The temperature of the flue gas entering the inlet of the electrostatic dust collector is 220-240 ℃.
And the flue gas treated by the electrostatic dust collector is discharged through an outlet of the electrostatic dust collector.
The temperature of the hot flue gas discharged through the outlet of the electrostatic precipitator is 210-230 ℃.
According to the above aspects of the present disclosure, the electrostatic precipitator is further provided with a high-voltage discharge electrode, a dust collecting electrode plate, and a vibrator.
After particulate matters in the flue gas enter the electrostatic dust collector, the particulate matters pass through an ionization region around the high-voltage discharge electrode, and the high-voltage discharge electrode releases negatively charged ions to the flue gas by means of corona effect, so that the particulate matters are charged.
The charged particles migrate towards the surface of the grounded dust collecting plate and are accumulated on the surface of the dust collecting plate, and the charged particles release charges.
The vibrator vibrates the dust collecting polar plate, so that the collected particles are separated from the dust collecting polar plate and then fall into an ash hopper arranged below the electrostatic dust collector.
According to the above aspects of the present disclosure, the smoke heat exchanger is designed as a shell-and-tube structure.
And a PTFE heat exchange tube is arranged in the smoke heat exchanger.
According to the above aspects of the present disclosure, the smoke heat exchanger is provided with a heat exchanger inlet, a low temperature side inlet, a high temperature side outlet and a low temperature side outlet.
Through the heat exchanger inlet, the smoke heat exchanger receives hot smoke subjected to electrostatic dust removal by the electrostatic dust remover.
The flue gas heat exchanger receives the cold flue gas washed by the wet scrubber tower through the low temperature side inlet.
The hot flue gas gets into the PTFE heat exchange tube, cold flue gas is in the outside of PTFE heat exchange tube flows, the heat of hot flue gas passes through the PTFE heat exchange tube with cold flue gas carries out the heat exchange, after the cooling hot flue gas passes through high temperature side export gets into wet scrubber, after heaing up the cold flue gas passes through low temperature side export gets into bag collector.
The temperature of the hot flue gas discharged through the high-temperature side outlet is 150-170 ℃.
According to the above aspects of the present disclosure, the quench cooler comprises a venturi scrubber.
The flue gas from the high temperature side outlet increases in velocity from top to bottom as it passes through the converging section of the venturi scrubber, thereby creating a choking effect that converts the water injected therein into atomized droplets that saturate the flue gas, which then decrease in velocity as the flue gas passes through the diverging section of the venturi scrubber, the droplets colliding with and polymerizing with the particulate matter in the flue gas and separating from the gas phase, the saturated flue gas entering the interior of the wet scrubber from the bottom of the wet scrubber.
According to the above aspects of the present disclosure, two stages of packing contact reactors made of stainless steel are provided inside the wet scrubber tower, and the surfaces of the packing contact reactors provide mass transfer contact surfaces for flue gas and absorption liquid.
The absorption liquid is evenly distributed over and wets the packing in the packing contact reactor through the distribution pipe of the wet scrubber tower.
The absorption liquid is contacted with the flue gas moving from bottom to top of the wet scrubber tower, and acidic components in the flue gas are firstly dissolved in the absorption liquid and then react with alkaline components in the absorption liquid.
After the contact reaction with the filler, removing acidic components in the smoke.
According to the above aspects of the present disclosure, a flap-type demister is provided at the top of the wet scrubber tower.
When the flue gas reaches the top of the wet-type washing tower, atomized liquid drops generated in the absorption process are separated from the flue gas through the folded plate type demister, then cold flue gas is discharged from the top of the wet-type washing tower, and the cold flue gas enters the flue gas heat exchanger through a low-temperature side inlet of the flue gas heat exchanger.
According to the above aspects of the present disclosure, the flue gas treatment system further comprises an ID fan.
And the flue gas output through the bag type dust collector outlet is conveyed to the ID fan.
The temperature of the flue gas passing through the fan outlet of the ID fan is 120-140 ℃.
According to the above aspects of the present disclosure, the flue gas output through the fan outlet of the ID fan is delivered to a chimney.
The chimney is provided with a smoke emission monitoring system.
The process route according to the present disclosure enables the following technical advantages:
(1) this allows for higher flue gas temperatures (e.g., 240 ℃) entering the electrostatic precipitator, which reduces the heat exchange area of the heat recovery system and saves costs (in order to ensure that the flue gas temperature entering the bag precipitator is suitable for the activated carbon to adsorb gaseous pollutants, the conventional treatment process needs to increase the heat exchange area of the heat recovery system to reduce the temperature thereof to a suitable range).
(2) The temperature of the cold smoke can be raised to about 130 ℃, and the generation of white smoke during emission can be effectively prevented.
(3) The temperature of the hot flue gas is reduced to below about 170 ℃, so that the cooling water consumption of wet washing can be saved.
(4) The heat required by the temperature rise of the cold flue gas comes from the flue gas, so that the primary energy consumption can be saved.
(5) After the temperature is raised, the temperature condition (such as 135 ℃) of the flue gas is suitable for the activated carbon to adsorb gaseous pollutants, and meanwhile, the adsorption and deacidification effects can be enhanced by adding a certain amount of lime.
(6) By reducing the volumetric flow of flue gas through the baghouse in this manner, the filter area of the baghouse may be reduced, saving equipment costs (about 25% reduction in volumetric flow of flue gas due to the baghouse being downstream of the wet scrubber as compared to conventional treatment processes).
(7) The bag type dust collector is arranged at the downstream of the wet type washing tower, and can further remove aerosol formed by the wet type washing tower, so that the dust content of the discharged flue gas is ensured.
(8) The bag filter is arranged at the downstream of the wet washing tower and plays a role in further deacidification under the action of lime.
So that the manner in which the disclosure is made in detail herein can be better understood, and in which the contributions to the art may be better appreciated, the disclosure has been summarized rather broadly. There are, of course, embodiments of the disclosure that will be described below and which will form the subject matter of the claims appended hereto.
As such, those skilled in the art will appreciate that the conception upon which this disclosure is based may readily be utilized as a basis for the designing of other structures, methods and systems for carrying out the several purposes of the present disclosure. It is important, therefore, that the appended claims be regarded as including such equivalent constructions insofar as they do not depart from the spirit and scope of the present disclosure.
Drawings
The present disclosure will be better understood and its advantages will become more apparent to those skilled in the art from the following drawings. The drawings described herein are for illustrative purposes only of selected embodiments and not all possible implementations and are not intended to limit the scope of the present disclosure.
FIG. 1 shows a prior art flue gas treatment system for sludge incineration;
figure 2 illustrates a flue gas treatment system for sludge incineration according to the present disclosure.
Detailed Description
An embodiment according to the present disclosure is specifically described below with reference to fig. 2.
The general process route for flue gas treatment as shown in fig. 2 is: electrostatic precipitator → smoke heat exchanger → quencher and wet scrubber → baghouse → ID fan.
According to one embodiment of the present disclosure, as shown in fig. 2, a flue gas treatment system is proposed, which comprises an electrostatic precipitator 1, a flue gas heat exchanger 2, a quencher 3, a wet scrubber 4 and a bag house 5, wherein the electrostatic precipitator 1 is used for removing particulate matter and solid phase heavy metals; the smoke heat exchanger 2 prevents white smoke from being generated in smoke emission; the quencher 3 is used for generating saturated flue gas; the wet scrubber tower 4 removes acid gases; the bag house 5 combines activated carbon and lime injection to remove mercury and other gaseous pollutants.
The electrostatic precipitator 1 is arranged upstream of the flue gas heat exchanger 2, the quencher 3 and the wet scrubber 4.
The flue gas treated by the electrostatic precipitator 1 is fed to the flue gas heat exchanger 2.
The baghouse 5 is disposed downstream of the smoke heat exchanger 2, the quencher 3, and the wet scrubber 4, so that the flue gas treated by the smoke heat exchanger 2, the quencher 3, and the wet scrubber 4 is input to the baghouse 5.
According to the above various embodiments of the present disclosure, the electrostatic precipitator 1 is provided with an electrostatic precipitator inlet 1-1 and an electrostatic precipitator outlet 1-2.
Flue gas from the outlet of the sludge fluidized bed enters the electrostatic precipitator 1 through the inlet 1-1 of the electrostatic precipitator.
The temperature of the flue gas entering the inlet 1-1 of the electrostatic precipitator is about 220-240 ℃.
And the flue gas treated by the electrostatic dust collector 1 is discharged through an outlet 1-2 of the electrostatic dust collector.
The temperature of the hot flue gases exiting through the electrostatic precipitator outlet 1-2 is approximately 210-230 ℃.
This allows for higher flue gas temperatures (e.g., 240 ℃) entering the electrostatic precipitator, which reduces the heat exchange area of the heat recovery system and saves cost (in order to ensure that the flue gas temperature entering the bag precipitator is suitable for the activated carbon to adsorb gaseous pollutants, the conventional treatment process needs to reduce the temperature of the flue gas to a suitable range by increasing the heat exchange area of the heat recovery system).
According to the above-mentioned various embodiments of the present disclosure, the electrostatic precipitator 1 is further provided with high-voltage discharge electrodes 1-3, dust collecting electrode plates 1-4, and rappers 1-5.
After particulate matters in the flue gas enter the electrostatic dust collector 1, the particulate matters pass through an ionization region around the high-voltage discharge electrodes 1-3, and the high-voltage discharge electrodes release ions with negative charges to the flue gas by means of corona effect, so that the particulate matters are charged.
The charged particles migrate towards the surface of the grounded dust collecting plate 1-4 and are accumulated on the surface of the dust collecting plate 1-4, and the charged particles discharge electric charges.
The vibrator 1-5 vibrates the dust collecting polar plate 1-4, so that the collected particles are separated from the dust collecting polar plate 1-4 and then fall into an ash bucket 1-6 arranged below the electrostatic dust collector 1.
According to the above-described various embodiments of the present disclosure, the smoke heat exchanger 2 is designed as a shell-and-tube structure.
A PTFE heat exchange tube 2-1 is arranged in the smoke heat exchanger 2.
According to the various embodiments of the present disclosure described above, the smoke heat exchanger 2 is provided with a heat exchanger inlet 2-2, a low temperature side inlet 2-3, a high temperature side outlet 2-4 and a low temperature side outlet 2-5.
Through the heat exchanger inlet 2-2, the smoke heat exchanger 2 receives hot smoke subjected to electrostatic dust removal by the electrostatic dust collector 1.
Through the low temperature side inlet 2-3, the flue gas heat exchanger 2 receives the cold flue gas after being scrubbed by the wet scrubber tower 4.
The hot flue gas enters the PTFE heat exchange tube 2-1, the cold flue gas flows outside the PTFE heat exchange tube 2-1, the heat of the hot flue gas is subjected to heat exchange with the cold flue gas through the PTFE heat exchange tube, the hot flue gas after being cooled enters the wet type washing tower 4 through the high-temperature side outlet 2-4, and the cold flue gas after being heated enters the bag type dust collector 5 through the low-temperature side outlet 2-5.
The temperature of the hot flue gases exiting through the high temperature side outlets 2-4 is approximately 150-170 ℃. The temperature of the hot flue gas is about 150-170 ℃, and the cooling water consumption of wet washing can be saved.
According to the various embodiments of the present disclosure described above, the chiller 3 comprises a venturi scrubber 3-1.
The flue gas from the high temperature side outlet 2-4 increases in velocity from top to bottom as it passes through the converging section 3-1-1 of the venturi scrubber 3-1, thereby creating a choking effect that converts the water injected therein into atomized droplets that saturate the flue gas, and then the atomized droplets collide with and polymerize with the particulate matter in the flue gas and separate from the gas phase as the velocity of the flue gas decreases as it passes through the diverging section 3-1-2 of the venturi scrubber 3-1, and the saturated flue gas enters the interior of the wet scrubber tower 4 from the bottom of the wet scrubber tower 4.
According to the above embodiments of the present disclosure, two stages of packing contact reactors 4-1 made of stainless steel are disposed inside the wet scrubber tower 4, and the surfaces of the packing contact reactors 4-1 provide mass transfer contact surfaces for flue gas and absorption liquid (not shown). In order to achieve the purpose of efficiently removing acid gas (the removal efficiency is 99%), a wet scrubber which circularly sprays absorption liquid is adopted to absorb acid components such as SOx, HCl and the like in flue gas.
The absorption liquid is evenly distributed over and wets the packing (not shown) in the packing contact reactor 4-1 through the distribution pipe (not shown) of the wet scrubber tower 4.
The absorption liquid is contacted with the flue gas moving from bottom to top from the bottom of the wet scrubber tower 4, and acidic components in the flue gas are firstly dissolved in the absorption liquid and then react with alkaline components in the absorption liquid.
After the contact reaction with the filler, removing acidic components in the smoke.
According to the above embodiments of the present disclosure, a flap-type demister 4-2 is provided at the top of the wet scrubber tower 4.
When the flue gas reaches the top of the wet-type washing tower 4, atomized liquid drops generated in the absorption process are separated from the flue gas through the folded plate type demister 4-2, and then cold flue gas is discharged from the top of the wet-type washing tower 4 and enters the flue gas heat exchanger 2 through a low-temperature side inlet 2-3 of the flue gas heat exchanger 2.
According to the above-described embodiment of the present disclosure, powdered activated carbon (not shown) for adsorbing gaseous pollutants remaining in the flue gas is provided in the flue 5-1 of the baghouse 5.
According to the above-described respective embodiments of the present disclosure, mercury remaining in flue gas is adsorbed by spraying the activated carbon in the flue 5-1 of the baghouse 5.
According to the above-mentioned embodiments of the present disclosure, powdered lime (not shown) is also provided in the flue 5-1 of the bag house 5.
According to the above-described various embodiments of the present disclosure, the flue gas from the low temperature side outlet 2-4 of the flue gas heat exchanger 2 is delivered to the baghouse inlet 5-2 of the baghouse 5.
The temperature of the flue gas entering the inlet 5-2 of the bag type dust collector is 125-145 ℃. When the temperature of the flue gas is not higher than 150 ℃, the activated carbon is sprayed to effectively adsorb mercury and other gaseous pollutants, and the synchronous addition of a certain amount of lime can also play roles in strengthening adsorption and deep treatment (deacidification).
The flue gas treated by the baghouse 5 is transported through a baghouse outlet 5-3 to a stack 7 by an ID fan 6.
The temperature of the flue gas passing through the bag house outlet 5-3 is about 120-140 ℃. According to the process route of the disclosure, the temperature of the cold flue gas can be increased to about 130 ℃, and the generation of white smoke during emission can be effectively prevented. The heat required by the temperature rise of the cold flue gas comes from the flue gas, so that the primary energy consumption can be saved.
The bag type dust collector 5 intercepts active carbon, lime and residual extremely small amount of particulate matters in the flue gas, thereby realizing the purpose of thoroughly purifying the flue gas. The dust removal efficiency of the bag type dust collector can reach more than 99.9 percent, and submicron particles can be removed.
According to the above-described respective embodiments of the present disclosure, the bag house is further provided with an auger 5-4.
The screw conveyor 5-4 is arranged for discharging the activated carbon, the lime and the remaining particulate matter in the flue gas that are trapped by the bag house 5.
By reducing the volumetric flow of flue gas through the baghouse in this manner, the filter area of the baghouse may be reduced, saving equipment costs (about 25% reduction in volumetric flow of flue gas due to the baghouse being downstream of the wet scrubber as compared to conventional treatment processes).
According to the above various embodiments of the present disclosure, the flue gas treatment system further comprises an ID fan 6.
The flue gas output through the baghouse outlet 5-3 is delivered to the ID fan 6.
The temperature of the flue gas passing through the fan outlet of the ID fan 6 is about 130 ℃.
According to the above various embodiments of the present disclosure, the flue gas output through the fan outlet of the ID fan 6 is delivered to the chimney 7.
The chimney 7 is provided with a flue gas emission monitoring system 7-1.
While the disclosure has been described in the specification and drawings with reference to specific embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the disclosure as defined in the claims. Moreover, the combination and arrangement of features, elements and/or functions between specific embodiments herein is clearly apparent and thus, in light of this disclosure, one skilled in the art will appreciate that features, elements and/or functions of an embodiment may be incorporated into another specific embodiment as appropriate, unless described otherwise, above. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the disclosure without departing from the essential scope thereof. Therefore, it is intended that the disclosure not be limited to the particular embodiment illustrated by the drawings and described in the specification as the best mode presently contemplated for carrying out this disclosure, but that the disclosure will include all embodiments falling within the scope of the foregoing description and the appended claims.
Claims (15)
1. A flue gas treatment system comprises an electrostatic dust collector, a flue gas heat exchanger, a quencher, a wet scrubber and a bag type dust collector;
the electrostatic precipitator is disposed upstream of the flue gas heat exchanger, the quencher, and the wet scrubber;
it is characterized in that the preparation method is characterized in that,
the flue gas treated by the electrostatic dust collector is input into the flue gas heat exchanger;
the baghouse is disposed downstream of the smoke heat exchanger, the quencher, and the wet scrubber so that the smoke processed through the smoke heat exchanger, the quencher, and the wet scrubber is input to the baghouse.
2. The flue gas treatment system of claim 1,
powdered activated carbon is arranged in a flue of the bag type dust collector and is used for adsorbing residual gaseous pollutants in flue gas.
3. The flue gas treatment system of claim 2,
and adsorbing residual mercury in the flue gas by spraying the activated carbon in a flue of the bag type dust collector.
4. The flue gas treatment system of claim 3,
powdery lime is also arranged in the flue of the bag type dust collector.
5. The flue gas treatment system of claim 4,
the flue gas from the low temperature side outlet of the flue gas heat exchanger is conveyed to the baghouse inlet of the baghouse;
the temperature of the flue gas entering the inlet of the bag type dust collector is 130-150 ℃;
the flue gas treated by the bag type dust collector is conveyed to a chimney through an ID fan through an outlet of the bag type dust collector;
the temperature of the flue gas passing through the outlet of the bag type dust collector is 125-145 ℃.
6. The flue gas treatment system of claim 5,
the bag type dust collector is also provided with a spiral conveyor;
the screw conveyor is arranged to discharge the activated carbon, the lime and the remaining particulate matter in the flue gas that are trapped by the bag house.
7. The flue gas treatment system of claim 1,
the electrostatic dust collector is provided with an electrostatic dust collector inlet and an electrostatic dust collector outlet;
flue gas from the outlet of the sludge fluidized bed enters the electrostatic dust collector through the inlet of the electrostatic dust collector;
the temperature of the flue gas entering the inlet of the electrostatic dust collector is 220-240 ℃;
the flue gas treated by the electrostatic dust collector is discharged through an outlet of the electrostatic dust collector;
the temperature of the hot flue gas discharged through the outlet of the electrostatic precipitator is 210-230 ℃.
8. The flue gas treatment system of claim 7,
the electrostatic dust collector is also provided with a high-voltage discharge electrode, a dust collecting polar plate and a vibrator;
after the particulate matters in the flue gas enter the electrostatic dust collector, the particulate matters pass through an ionization region around the high-voltage discharge electrode, and the high-voltage discharge electrode releases negatively charged ions to the flue gas by means of a corona effect, so that the particulate matters are charged;
the charged particles migrate towards the surface of the grounded dust collecting polar plate so as to be accumulated on the surface of the dust collecting polar plate, and the charged particles release charges;
the vibrator vibrates the dust collecting polar plate, so that the collected particles are separated from the dust collecting polar plate and then fall into an ash hopper arranged below the electrostatic dust collector.
9. The flue gas treatment system of claim 8,
the smoke heat exchanger is designed into a shell-and-tube structure;
and a PTFE heat exchange tube is arranged in the smoke heat exchanger.
10. The flue gas treatment system of claim 9,
the smoke heat exchanger is provided with a heat exchanger inlet, a low-temperature side inlet, a high-temperature side outlet and a low-temperature side outlet;
the smoke heat exchanger receives hot smoke subjected to electrostatic dust removal by the electrostatic dust remover through the heat exchanger inlet;
the flue gas heat exchanger receives the cold flue gas washed by the wet scrubber tower through the low temperature side inlet;
the hot flue gas enters the PTFE heat exchange tube, the cold flue gas flows outside the PTFE heat exchange tube, heat of the hot flue gas exchanges heat with the cold flue gas through the PTFE heat exchange tube, the cooled hot flue gas enters the wet type washing tower through the high-temperature side outlet, and the heated cold flue gas enters the bag type dust collector through the low-temperature side outlet;
the temperature of the hot flue gas discharged through the high-temperature side outlet is 150-170 ℃.
11. The flue gas treatment system of claim 10,
the quench cooler comprises a venturi scrubber;
the flue gas from the high temperature side outlet increases in velocity from top to bottom as it passes through the converging section of the venturi scrubber, thereby creating a choking effect that converts the water injected therein into atomized droplets that saturate the flue gas, which then decrease in velocity as the flue gas passes through the diverging section of the venturi scrubber, the droplets colliding with and polymerizing with the particulate matter in the flue gas and separating from the gas phase, the saturated flue gas entering the interior of the wet scrubber from the bottom of the wet scrubber.
12. The flue gas treatment system of claim 11,
two stages of packing contact reactors made of stainless steel are arranged in the wet type washing tower, and the surfaces of the packing contact reactors provide mass transfer contact surfaces for flue gas and absorption liquid;
the absorption liquid is uniformly distributed over and wets the packing in the packing contact reactor through the distribution pipe of the wet scrubber tower;
the absorption liquid is contacted with the flue gas moving from bottom to top from the bottom of the wet scrubber tower, and acidic components in the flue gas are dissolved in the absorption liquid and then react with alkaline components in the absorption liquid;
after the contact reaction with the filler, removing acidic components in the smoke.
13. The flue gas treatment system of claim 12,
a folded plate type demister is arranged at the top of the wet washing tower;
when the flue gas reaches the top of the wet-type washing tower, atomized liquid drops generated in the absorption process are separated from the flue gas through the folded plate type demister, then cold flue gas is discharged from the top of the wet-type washing tower, and the cold flue gas enters the flue gas heat exchanger through a low-temperature side inlet of the flue gas heat exchanger.
14. The flue gas treatment system of claim 13,
the flue gas treatment system also comprises an ID fan;
the flue gas output through the bag type dust collector outlet is conveyed to the ID fan;
the temperature of the flue gas passing through the fan outlet of the ID fan is 120-140 ℃.
15. The flue gas treatment system of claim 14,
the flue gas output by the fan outlet of the ID fan is conveyed to a chimney;
the chimney is provided with a smoke emission monitoring system.
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| CN202022408316.8U CN213492812U (en) | 2020-10-26 | 2020-10-26 | Flue gas treatment system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114151817A (en) * | 2021-12-17 | 2022-03-08 | 四川九洲环保科技有限责任公司 | Flue gas treatment system and treatment method |
| CN114235645A (en) * | 2022-02-28 | 2022-03-25 | 南通市新叶能源科技有限公司 | Smoke emission monitoring device with self-cleaning function |
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2020
- 2020-10-26 CN CN202022408316.8U patent/CN213492812U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114151817A (en) * | 2021-12-17 | 2022-03-08 | 四川九洲环保科技有限责任公司 | Flue gas treatment system and treatment method |
| CN114235645A (en) * | 2022-02-28 | 2022-03-25 | 南通市新叶能源科技有限公司 | Smoke emission monitoring device with self-cleaning function |
| CN114235645B (en) * | 2022-02-28 | 2022-05-20 | 南通市新叶能源科技有限公司 | Smoke emission monitoring device with self-cleaning function |
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Address after: 3101, 27th Floor, Building 1, Yard 38, East 3rd Ring North Road, Chaoyang District, Beijing, 100026 Patentee after: Suez Environmental Technology (Beijing) Co.,Ltd. Address before: 100026 31 / F, Taikang financial building, building 1, courtyard 38, East Third Ring Road North, Chaoyang District, Beijing Patentee before: Suez Water Treatment Co,.Ltd. |