CN108722162B - Deep-whitening ultralow-emission device and method for flue gas - Google Patents
Deep-whitening ultralow-emission device and method for flue gas Download PDFInfo
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- CN108722162B CN108722162B CN201810942555.6A CN201810942555A CN108722162B CN 108722162 B CN108722162 B CN 108722162B CN 201810942555 A CN201810942555 A CN 201810942555A CN 108722162 B CN108722162 B CN 108722162B
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- flue gas
- desulfurizing tower
- heat pipe
- heat exchanger
- diwen
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 124
- 239000003546 flue gas Substances 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 30
- 230000023556 desulfurization Effects 0.000 claims abstract description 30
- 239000000779 smoke Substances 0.000 claims abstract description 27
- 230000001105 regulatory effect Effects 0.000 claims abstract description 25
- 230000002087 whitening effect Effects 0.000 claims abstract description 20
- 239000007921 spray Substances 0.000 claims abstract description 14
- 238000005507 spraying Methods 0.000 claims abstract description 10
- 230000001737 promoting effect Effects 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 57
- 239000000428 dust Substances 0.000 claims description 22
- 238000009833 condensation Methods 0.000 claims description 9
- 230000005494 condensation Effects 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 239000013049 sediment Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- 230000001502 supplementing effect Effects 0.000 claims description 6
- 230000018044 dehydration Effects 0.000 claims description 5
- 238000006297 dehydration reaction Methods 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 5
- 239000010865 sewage Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 claims 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 8
- 239000002245 particle Substances 0.000 abstract description 6
- 239000003595 mist Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a deep-whitening ultra-low emission device and method for flue gas, and relates to the field of deep treatment of the flue gas after desulfurization, wherein the deep-whitening ultra-low emission device comprises a desulfurizing tower, a heat pipe exchanger A, an induced draft fan and a whitening device; the desulfurizing tower comprises a desulfurizing tower efficiency lifting tray, a desulfurizing tower spray layer, a tube bundle turbulent ball condensing device, a demisting device and a desulfurizing tower outlet; the heat pipe heat exchanger A is connected with the desulfurizing tower through the induced draft fan; the desulfurizing tower efficiency promoting tray, the desulfurizing tower spraying layer, the tube bundle turbulent ball condensing device and the demisting device are sequentially arranged in the desulfurizing tower from bottom to top; the desulfurizing tower is externally connected with the whitening device, and comprises a liquid drop separator, a heat pipe exchanger B, a Bai Diwen removing fan and a first electric regulating valve. The invention realizes that the particle size of the flue gas emission is not higher than 5mg/m 3 Sulfur dioxide not higher than 35mg/m 3 . Basically has no visible white smoke, and really meets the requirement of ultra-low emission.
Description
Technical Field
The invention relates to the field of deep treatment of desulfurized flue gas, in particular to a deep whitening and ultralow emission device and method for flue gas.
Background
The flue gas of the original boiler (kiln) is desulfurized by a wet method, and then the flue gas is provided with water, gypsum rain and sulfate, dust and more serious, and the tail of the flue gas reaches several kilometers, so that the atmospheric pollution is caused. Expert analysis shows that the substances are one of factors causing haze weather. Reducing the content of harmful substances in the flue gas becomes an important subject in the field of deep treatment of the flue gas after desulfurization.
Therefore, those skilled in the art are working to develop a flue gas treatment and emission device and method, which improves the deep dust removal effect in flue gas.
Disclosure of Invention
In view of the above-mentioned drawbacks of the prior art, the present invention aims to solve the technical problem of how to achieve the deep dust removal effect of whitening and dewatering.
In order to achieve the above purpose, the invention provides a deep-whitening ultralow-emission device for flue gas, which comprises a desulfurizing tower, a heat pipe exchanger A, an induced draft fan and a whitening device;
the desulfurizing tower comprises a desulfurizing tower efficiency lifting tray, a desulfurizing tower spray layer, a tube bundle turbulent ball condensing device, a demisting device and a desulfurizing tower outlet;
the heat pipe heat exchanger A is connected with the desulfurizing tower through the induced draft fan; the desulfurizing tower efficiency promoting tray, the desulfurizing tower spraying layer, the tube bundle turbulent ball condensing device and the demisting device are sequentially arranged in the desulfurizing tower from bottom to top; the demisting device is connected with the outlet of the desulfurizing tower in an external mode, and the desulfurizing tower is connected with the whitening device in an external mode and comprises a liquid drop separator, a heat pipe exchanger B, a Bai Diwen removing fan and a first electric regulating valve; the liquid drop separator is connected with one end of the heat pipe heat exchanger B, the other end of the heat pipe heat exchanger B is connected with the de-Bai Diwen fan, the de-Bai Diwen fan is connected with the first electric regulating valve, after the first electric regulating valve regulates the de-Bai Diwen flue gas, the de-Bai Diwen flue gas enters the outlet of the desulfurizing tower and is mixed with main flue gas and then discharged.
Further, the heat pipe heat exchanger A is close to the heat pipe heat exchanger B; the heat pipe heat exchanger A is a high-temperature heat pipe heat exchanger and is used for cooling the flue gas; the heat pipe heat exchanger B is a low-temperature heat pipe heat exchanger and is used for heating the flue gas.
Further, the flue gas flow rate of the heat pipe heat exchanger A is 37 ten thousand cubic meters per hour, and the flue gas flow rate of the heat pipe heat exchanger B is 12 ten thousand cubic meters per hour.
Further, a main desulfurization pump and a desulfurization liquid plate heat exchanger are externally connected to the desulfurization tower spray layer; after the desulfurization liquid at the outlet of the main desulfurization pump is cooled by the desulfurization liquid plate heat exchanger, the desulfurization liquid enters the spray layer of the desulfurization tower inside the desulfurization tower to contact and react with hot flue gas.
Further, the tube bundle turbulent ball condensing device is sequentially connected with a condensate circulating storage tank, a condensate pump and a condensate plate heat exchanger, which are connected through pipelines to form a set of circulating condensing device; and after the condensed water generated after the flue gas is condensed passes through a gas-rising water-receiving device in the desulfurizing tower, the flue gas condensed water flows to the condensed water circulating storage tank for storage through the pipeline, and the condensed water in the condensed water circulating storage tank is pressurized by the condensed liquid pump and cooled by the condensed liquid plate type heat exchanger, and then enters the tube bundle turbulent ball condensing device through the pipeline to continuously cool the flue gas.
Further, part of sediment is generated after the condensate circulating storage tank circulates for a long time, the condensate and the sediment in the condensate circulating storage tank are conveyed to a sediment separation system through pump pressurization, the redundant condensate is conveyed to sewage deep treatment through a pump, and the redundant condensate is recycled as system circulating water after being treated by a membrane separation system; the water in the condensed water circulation storage tank is supplemented by process water supplementing from a process water tank.
Further, the de-Bai Diwen fan pressurizes the flue gas, and the air quantity of the de-Bai Diwen fan is 12 ten thousand cubic meters per hour.
Further, the de-Bai Diwen fan is also connected with a second electric regulating valve, and the second electric regulating valve regulates the de-Bai Diwen flue gas and then enters the original kiln chimney for heat preparation; the smoke flow rate of the first electric regulating valve is 5-6 ten thousand cubic meters per hour, and the smoke flow rate of the second electric regulating valve is 6-7 ten thousand cubic meters per hour.
Further, the height of the desulfurizing tower is 70 meters.
The invention also provides a method for deeply whitening and ultra-low emission of the flue gas, which comprises the following steps:
step 1, main flue gas enters the heat pipe exchanger A for heat exchange and then enters the desulfurizing tower through the induced draft fan, the main flue gas is flue gas after dust removal of a boiler or a kiln, the temperature of the main flue gas entering the heat pipe exchanger A is 150-180 ℃, and the temperature of the main flue gas entering the desulfurizing tower after heat exchange is reduced to 100-140 ℃;
step 2, after entering the desulfurizing tower, the main flue gas sequentially passes through the desulfurizing tower lifting tray and the desulfurizing tower spraying layer from bottom to top, and the temperature of the main flue gas is reduced to 55-65 ℃ after passing through the desulfurizing tower spraying layer;
step 3, continuously passing the main flue gas through the tube bundle turbulent ball condensing device and the demisting device from bottom to top in sequence to perform condensation, desulfurization, dust removal, demisting and dehydration, wherein the temperature of the condensed discharged flue gas is less than or equal to 45-47 ℃, and the dust concentration is lower than or equal to<10mg/Nm 3 ；
Step 4, the discharged flue gas of which 25% to 35% passes through the whitening device in the step 3 is subjected to whitening treatment, firstly passes through the droplet separator and then enters the heat pipe exchanger B, the discharged flue gas is heated to 130 ℃ to 160 ℃, then is divided into two paths under the action of the de-Bai Diwen fan, one path is connected with the first electric regulating valve, after the first electric regulating valve regulates the de-Bai Diwen flue gas, the de-Bai Diwen flue gas enters the outlet of the desulfurizing tower, and is mixed with 65% to 75% of the discharged flue gas in the step 3 and then is discharged, wherein the temperature of the mixed flue gas is 68 ℃ to 75 ℃.
The device and the method for deeply whitening and ultra-low emission of the flue gas are applied to the field of deep treatment of the desulfurized flue gas, and the deep whitening and dehydration dust removal effect is obvious. Through the measures of heat exchange temperature control, reconstruction condensation in the desulfurizing tower, flue gas reheating after desulfurization and the like, the method realizes that the discharged particulate matters of the flue gas are not higher than 5mg/m 3 Sulfur dioxide not higher than 35mg/m 3 . The smoke temperature after condensation in summer (4-10 months) reaches below 47 ℃, and the moisture content of the smoke is reduced by below 10%; the smoke temperature after condensation in winter (11 months-3 months of the next year) reaches below 45 ℃, and the moisture content of the smoke is below 15%. The smoke emission temperature reaches a certain critical temperature, so that 'white smoke' is basically not visible, the ultra-low emission requirement is truly realized, the atmosphere pollution environment is greatly improved, and the blue water and blue sky environment is created.
The conception, specific structure, and technical effects of the present invention will be further described with reference to the accompanying drawings to fully understand the objects, features, and effects of the present invention.
Drawings
FIG. 1 is an overall schematic of a preferred embodiment of the present invention.
The device comprises a 1-desulfurizing tower, a 101-desulfurizing tower lifting tray, a 102-desulfurizing tower spray layer, a 103-tube bundle turbulent ball condensing device, a 104-demisting device, a 105-desulfurizing tower outlet, a 2-heat pipe heat exchanger A, a 3-induced draft fan, a 4-whitening device, a 401-droplet separator, a 402-heat pipe heat exchanger B, a 403-Bai Diwen fan, a 404-first electric regulating valve, a 5-second electric regulating valve, a 6-main desulfurizing pump, a 7-desulfurizing liquid plate heat exchanger, an 8-condensate water circulating storage tank, a 9-precipitate separating system, 10-sewage deep treatment, 11-process water supplementing, a 12-membrane separating system, a 13-condensate liquid pump and a 14-condensate liquid plate heat exchanger.
Detailed Description
The following description of the preferred embodiments of the present invention refers to the accompanying drawings, which make the technical contents thereof more clear and easy to understand. The present invention may be embodied in many different forms of embodiments and the scope of the present invention is not limited to only the embodiments described herein.
In the drawings, like structural elements are referred to by like reference numerals and components having similar structure or function are referred to by like reference numerals. The dimensions and thickness of each component shown in the drawings are arbitrarily shown, and the present invention is not limited to the dimensions and thickness of each component. The thickness of the components is exaggerated in some places in the drawings for clarity of illustration.
As shown in figure 1, the temperature of the main flue gas with higher temperature after dust removal by a boiler (kiln) is between 150 ℃ and 180 ℃, the main flue gas firstly enters a heat pipe exchanger A2 to exchange heat with part of the lower temperature flue gas after desulfurization, the temperature of the main flue gas is reduced by about 40 ℃ to 50 ℃, and the temperature of the main flue gas can be controlled to be about 130 ℃ to 140 ℃ and then enters a desulfurizing tower 1. The heat pipe heat exchanger A2 is connected with the desulfurizing tower 1 through a draught fan 3. In the desulfurizing tower 1, main flue gas enters a tube bundle turbulent ball condensing device 103 from bottom to top through a desulfurizing tower lifting tray 101 and a desulfurizing tower spraying layer 102 for cooling, and the cooled flue gas is defogged through a defogging device 104. As the temperature of the flue gas decreases, the volume of the flue gas also correspondingly decreases. After entering the desulfurizing tower 1, the average rising flow velocity of the flue gas is correspondingly reduced, and the height of the flue gas is unchanged in the desulfurizing sectionUnder the condition of adopting a new technology of an extraction tower tray, the liquid-gas ratio is greatly reduced, the vaporization amount of the smoke is reduced, and the generation of the water vapor concentration of the smoke is fundamentally reduced. The temperature of the flue gas is reduced to about 65 ℃ after the flue gas rises to the spray layer 102 of the desulfurizing tower in the desulfurizing tower 1. If the temperature of the flue gas entering the desulfurizing tower 1 is 140 ℃, the temperature of the flue gas is 55 ℃ after the flue gas rises to a spraying layer 102 of the desulfurizing tower in the desulfurizing tower 1, the main flue gas seriously carries water mist, then enters a tube bundle turbulent ball condensing device 103 and a demisting device 104 at the upper part for condensation, desulfurization, dust removal, demisting and dehydration, the temperature of the discharged flue gas after condensation is about 45 ℃, and the dust concentration is high<10mg/Nm 3 The dehydration and defogging reach the advanced level of industry. After the main flue gas is treated by the tube bundle turbulent ball condensing device 103 and the demisting device 104, the flue gas temperature after condensation in summer (4-10 months) reaches below 47 ℃, and the moisture content of the flue gas is reduced by below 10%; the smoke temperature reaches below 45 ℃ after condensation in winter (11 months-3 months of the next year), and the moisture content of the smoke is below 15%. In summer, the temperature is less than or equal to 45 ℃, but is also at the saturated humidity of 45 ℃. If directly discharged, white smoke can be also displayed when the air temperature is low.
About 30% of flue gas is discharged from a side pipeline of an outlet of the tower top, the flue gas is subjected to whitening through a whitening device 4, firstly, the flue gas passes through a droplet separator 401 and enters a heat pipe exchanger B402, and then the flue gas is heated to about 145 ℃ with the gas volume ratio of about 3:1. The heated flue gas is pressurized by a de-Bai Diwen fan 403 and then is divided into two paths, wherein one path is controlled and regulated by a first electric regulating valve 404, the flue gas passing through the de-Bai Diwen enters a desulfurizing tower outlet 105 to be mixed with about 75% of main flue gas and discharged, the temperature of the mixed flue gas is between 68 and 75 ℃, and the water vapor of the mixed flue gas is far away from a saturation point. The chimney emission in summer basically has no visible white smoke; at ambient temperatures below-10 ℃ only, the visible white smoke is very small. And the other is controlled and regulated by a first electric regulating valve 5, and the original flue is used for sending the heat standby to a concrete chimney, so that the direct air draft of the heat standby during kiln emergency is ensured, and the safe operation of the kiln is ensured.
The condensed water cooled by the mixed flue gas with higher water vapor in the spray layer 102 of the desulfurization tower in the tube bundle turbulent ball condensing device 103 passes through the gas-rising water-receiving device in the desulfurization tower 1, and the flue gas condensed water automatically flows into the condensed water circulating storage tank 8 for circulating cooling. Part of the sediment after long-time circulation is pumped to a sediment separation system 9, water in a condensed water circulation storage tank 8 is supplemented by process water supplementing 11, and the process water supplementing 11 is from a process water tank. The superfluous condensate is pumped to the sewage deep treatment 10 and then treated by the membrane separation system 12, and then the superfluous condensate is used as the system circulating water for supplementing water for recycling, and the condensate is discharged in a zero way, so that secondary pollution is avoided.
The condensate pump 13 pressurizes, the condensate circulating liquid cooled by the condensate plate heat exchanger 14 enters the tube bundle turbulent ball condensing device 103 in the desulfurizing tower 1 through a pipeline, and the mixed flue gas with higher water vapor at the outlet of the spraying layer 102 of the desulfurizing tower is continuously cooled in a circulating way, so that the flue gas is cooled.
The desulfurization liquid at the outlet of the main desulfurization pump 6 is cooled by the desulfurization liquid plate heat exchanger 7, and then enters the desulfurization tower spray layer 102 in the desulfurization tower 1 to contact and react with hot flue gas. As the temperature is reduced, the desulfurization efficiency is improved, the vaporization rate of the desulfurizing liquid is reduced, the concentration of water vapor in the desulfurizing tower is greatly reduced, and a precondition is provided for the flue gas whitening.
In the process that main flue gas flows through the tube bundle turbulent ball condensing device 103 and the demisting device 104, circulating condensate in the condensate circulating storage tank 8 is pressurized by the condensate pump 13 and cooled by the condensate plate heat exchanger 14, and then flows downwards from the bottom of the super tube bundle turbulent ball dedusting demister A to spray reversely with the flue gas flow direction, a small amount of water mist enters from the bottom of the super tube bundle turbulent ball dedusting demister A and the main flue gas together under the action of the rising flow speed of the main flue gas, and performs multistage speed change and direction change movement under the action of the bottom guide plate, so that liquid drops with different particle diameters in the flue gas are collided between fine dust and fine dust, the particle diameters are increased, the turbulent ball is enabled to 'revolve' in the tube bundle under the action of rotational flow force and upward supporting force of the flue gas, and all turbulent balls are enabled to 'rotate' under the action of revolution force and friction force of the lower ball of the turbulent ball.
When the smoke impacts the turbulence ball, water mist in the smoke is adsorbed on the turbulence ball, more small liquid drops are adsorbed on the turbulence ball, a water film is formed on the surface of the turbulence ball, more liquid drops are adsorbed on the turbulence ball, so that the water film on the turbulence ball is thickened to form water drops, and desorption and discharge are carried out; the dust particles are absorbed by the liquid film, large liquid drops are discharged along with the desorption of the liquid drops, the bottom of the super tube bundle turbulent ball dust and mist eliminator enters the super tube bundle turbulent ball dust and mist eliminator B at the lower part together with the spray liquid under the action of gravity, clean smoke is discharged from the super tube bundle turbulent ball dust and mist eliminator B at the upper part, most of low-temperature spray liquid and the liquid drops containing trace dust particles removed from the top are mixed with main smoke in a countercurrent way, SO that the heat in the smoke is absorbed, the smoke is cooled, and meanwhile, harmful substances such as SO3, SO2 and dust particles and the like dissolved in the smoke are absorbed and enter the super tube bundle turbulent ball dust and mist eliminator B at the lower layer under the action of gravity.
After condensate enters the super tube bundle turbulent ball dedusting demister B, on one hand, due to the continuous change of the airflow speed and the impact of countercurrent liquid, more small foam is generated by liquid drops, and the contact area between the liquid drops and main flue gas is increased; on the other hand, the surface area of the turbulator is large, and the surface area of the turbulator is large, so that the contact surface area of a liquid film and the flue gas is also large, the efficiency of the thermal dissolution absorption reaction is improved, the flue gas is fully cooled, harmful substances in the flue gas are fully taken away by the liquid, in the cooling process, the flue gas originally containing saturated steam is removed due to the fact that the liquid phase of the water vapor is changed into water by cooling, finally, the water enters the low-resistance water receiving device at the bottom under the action of gravity, flows into a pipeline from a ring groove of the low-resistance water receiving device, and is discharged into a condensing solution circulation tank for continuous circulation.
Since the flue gas cooling process is accompanied by absorption of sulfur dioxide by the solution, a small amount of ammonium sulfate precipitate will be present in the bottom of the condensate circulating reservoir 8 after gradual concentration, and a portion of the precipitate is sent to the membrane separation system 12 by a pump.
The foregoing describes in detail preferred embodiments of the present invention. It should be understood that numerous modifications and variations can be made in accordance with the concepts of the invention without requiring creative effort by one of ordinary skill in the art. Therefore, all technical solutions which can be obtained by logic analysis, reasoning or limited experiments based on the prior art by the person skilled in the art according to the inventive concept shall be within the scope of protection defined by the claims.
Claims (2)
1. The deep-whitening ultralow-emission device for the flue gas is characterized by comprising a desulfurizing tower, a heat pipe exchanger A, an induced draft fan and a whitening device;
the desulfurizing tower comprises a desulfurizing tower efficiency lifting tray, a desulfurizing tower spray layer, a tube bundle turbulent ball condensing device, a demisting device and a desulfurizing tower outlet;
the heat pipe heat exchanger A is connected with the desulfurizing tower through the induced draft fan; the desulfurizing tower efficiency promoting tray, the desulfurizing tower spraying layer, the tube bundle turbulent ball condensing device and the demisting device are sequentially arranged in the desulfurizing tower from bottom to top; the demisting device is connected with the outlet of the desulfurizing tower in an external mode, and the desulfurizing tower is connected with the whitening device in an external mode and comprises a liquid drop separator, a heat pipe exchanger B, a Bai Diwen removing fan and a first electric regulating valve; the liquid drop separator is connected with one end of the heat pipe heat exchanger B, the other end of the heat pipe heat exchanger B is connected with the de-Bai Diwen fan, the de-Bai Diwen fan is connected with the first electric regulating valve, and after the first electric regulating valve regulates the de-Bai Diwen flue gas, the de-Bai Diwen flue gas enters the outlet of the desulfurizing tower and is mixed with main flue gas and then discharged; the heat pipe heat exchanger A is close to the heat pipe heat exchanger B; the heat pipe heat exchanger A is a high-temperature heat pipe heat exchanger and is used for cooling the flue gas; the heat pipe heat exchanger B is a low-temperature heat pipe heat exchanger and is used for heating the flue gas; the smoke flow rate of the heat pipe heat exchanger A is 37 ten thousand cubic meters per hour, and the smoke flow rate of the heat pipe heat exchanger B is 12 ten thousand cubic meters per hour; the spray layer of the desulfurizing tower is externally connected with a main desulfurizing pump and a desulfurizing liquid plate heat exchanger; after the desulfurization liquid at the outlet of the main desulfurization pump is cooled by the desulfurization liquid plate heat exchanger, the desulfurization liquid enters the desulfurization tower spray layer in the desulfurization tower and is in contact reaction with hot flue gas; the tube bundle turbulent ball condensing device is sequentially connected with a condensate water circulating storage tank, a condensate pump and a condensate plate type heat exchanger, and the condensate water circulating storage tank, the condensate pump and the condensate plate type heat exchanger are connected through pipelines to form a set of circulating condensing device; the condensate water generated after the flue gas is condensed passes through a gas-rising water-receiving device in the desulfurizing tower, the flue gas condensate water flows to the condensate water circulating storage tank through the pipeline for storage, and the condensate water in the condensate water circulating storage tank is pressurized by the condensate liquid pump and cooled by the condensate liquid plate heat exchanger, and then enters the tube bundle turbulent ball condensing device from the pipeline for continuously cooling the flue gas; the condensate water circulating storage tank can generate partial sediment after long-time circulation, the condensate water and the sediment in the condensate water circulating storage tank are conveyed to the sediment separation system through pump pressurization, the redundant condensate water is conveyed to sewage deep treatment through a pump, and the redundant condensate water is recycled as system circulating water after being treated by the membrane separation system; the water in the condensed water circulating storage tank is supplemented by process water supplementing from a process water tank; the de-Bai Diwen fan pressurizes the flue gas, and the air quantity of the de-Bai Diwen fan is 12 ten thousand cubic meters per hour; the de-Bai Diwen fan is also connected with a second electric regulating valve, and the second electric regulating valve regulates the de-Bai Diwen flue gas and then enters the original kiln chimney for heat preparation; the smoke flow rate of the first electric regulating valve is 5-6 ten thousand cubic meters per hour, and the smoke flow rate of the second electric regulating valve is 6-7 ten thousand cubic meters per hour; the height of the desulfurizing tower is 70 meters.
2. A method of deep whitening ultra low emission of flue gas using the deep whitening ultra low emission device of claim 1, the method comprising the steps of:
step 1, main flue gas enters the heat pipe exchanger A for heat exchange and then enters the desulfurizing tower through the induced draft fan, the main flue gas is flue gas after dust removal of a boiler or a kiln, the temperature of the main flue gas entering the heat pipe exchanger A is 150-180 ℃, and the temperature of the main flue gas entering the desulfurizing tower after heat exchange is reduced to 100-140 ℃;
step 2, after entering the desulfurizing tower, the main flue gas sequentially passes through the desulfurizing tower lifting tray and the desulfurizing tower spraying layer from bottom to top, and the temperature of the main flue gas is reduced to 55-65 ℃ after passing through the desulfurizing tower spraying layer;
step 3, the main flue gas continuously passes through the tube bundle turbulent ball condensing device and the demisting device from bottom to top in sequence to perform condensation, desulfurization, dust removal, demisting and dehydration, wherein the temperature of the condensed discharged flue gas is less than or equal to 45-47 ℃, and the dust concentration is lower than or equal to 45 DEG C<10mg/Nm 3 ；
Step 4, the discharged flue gas of which 25% to 35% passes through the whitening device in the step 3 is subjected to whitening treatment, firstly passes through the droplet separator and then enters the heat pipe exchanger B, the discharged flue gas is heated to 130 ℃ to 160 ℃, then is divided into two paths under the action of the de-Bai Diwen fan, one path is connected with the first electric regulating valve, after the first electric regulating valve regulates the de-Bai Diwen flue gas, the de-Bai Diwen flue gas enters the outlet of the desulfurizing tower, and is mixed with 65% to 75% of the discharged flue gas in the step 3 and then is discharged, wherein the temperature of the mixed flue gas is 68 ℃ to 75 ℃.
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| CN109569172A (en) * | 2018-11-30 | 2019-04-05 | 佛山丰汇环保工程有限公司 | A kind of self-loopa flue gas takes off white device |
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| CN110935277A (en) * | 2019-12-25 | 2020-03-31 | 河南心连心化学工业集团股份有限公司 | Coal chemical industry solid waste drying tail gas treatment device and treatment method |
| CN114590861B (en) * | 2022-03-24 | 2023-08-11 | 万华化学集团股份有限公司 | Low-energy-consumption deoxidizing device and low-energy-consumption deoxidizing process |
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