CN120506662A - Method and system for purifying waste incineration flue gas - Google Patents
Method and system for purifying waste incineration flue gasInfo
- Publication number
- CN120506662A CN120506662A CN202510937561.2A CN202510937561A CN120506662A CN 120506662 A CN120506662 A CN 120506662A CN 202510937561 A CN202510937561 A CN 202510937561A CN 120506662 A CN120506662 A CN 120506662A
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- China
- Prior art keywords
- flue gas
- heat
- waste incineration
- outlet
- pipe
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
- F28D20/02—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using latent heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chimneys And Flues (AREA)
Abstract
本发明公开了一种垃圾焚烧烟气净化方法与系统，垃圾焚烧烟气净化方法在垃圾焚烧烟气的流动方向上依次喷入小苏打粉末、活性炭粉和氨气；如此使得垃圾焚烧烟气先与小苏打粉末接触，而小苏打粉末在垃圾焚烧烟气的高温作用下迅速分解为具有微小多孔且高反应活性的无水碳酸钠微粒(即小苏打粉末在高温环境下通过所谓“爆米花效应”，迅速分解为具有高反应活性、多孔无水碳酸钠颗粒)，并与垃圾焚烧烟气中的SO2、HC l及HF等酸性气体发生反应并去除；垃圾焚烧烟气中的多数低沸点重金属物质及二噁英等全部被活性炭吸附截留，而与垃圾焚烧烟气一同进入的氨气，在催化剂作用下与垃圾焚烧烟气中的NOx气体发生脱硝还原反应，实现烟气的脱硝净化。
The present invention discloses a waste incineration flue gas purification method and system. The waste incineration flue gas purification method sequentially sprays baking soda powder, activated carbon powder and ammonia in the flow direction of the waste incineration flue gas. In this way, the waste incineration flue gas first contacts the baking soda powder, and the baking soda powder is rapidly decomposed into tiny, porous and highly reactive anhydrous sodium carbonate particles under the high temperature of the waste incineration flue gas (i.e., the baking soda powder rapidly decomposes into highly reactive, porous anhydrous sodium carbonate particles under the so-called "popcorn effect" in a high temperature environment). The baking soda powder reacts with and removes acidic gases such as SO2 , HCl and HF in the waste incineration flue gas. Most low-boiling-point heavy metal substances and dioxins in the waste incineration flue gas are adsorbed and retained by the activated carbon, while the ammonia entering together with the waste incineration flue gas undergoes a denitrification reduction reaction with NOx gas in the waste incineration flue gas under the action of a catalyst, thereby achieving denitrification and purification of the flue gas.
Description
Technical Field
The invention belongs to the technical field of flue gas treatment, and particularly relates to a method and a system for purifying waste incineration flue gas.
Background
The waste incineration flue gas purification system is the most main pollutant control system of a waste incineration plant and is responsible for efficiently purifying and removing acid gases (NO x、SO2, HCl, HF and the like), dust, heavy metals, dioxin and other harmful secondary pollutants in flue gas generated after waste incineration.
At present, a flue gas purification system of a garbage incineration project generally adopts a combined purification process system of SNCR (urea) +semi-dry method [ Ca (OH) 2 slurry ] +dry method [ Ca (OH) 2 ] +activated carbon injection+cloth bag dust removal+SCR (urea)'. The method comprises the steps of removing NO x gas in smoke through SNCR and SCR, removing SO 2, HCl, HF and other acid gases in the smoke through a semi-dry deacidification system and removing heavy metals, dioxin and other pollutants in the smoke through active carbon, intercepting and removing the heavy metals, the dioxin and other pollutants on the surface of a cloth bag dust collector together with dust particles in the smoke, and discharging the smoke after qualified purification into the atmosphere through a chimney.
In the process system, the flue gas at the outlet of a coal economizer of a waste heat furnace is usually discharged at a temperature of about 200 ℃, when passing through a Ca (OH) 2 slurry semi-dry deacidification system, hot flue gas and slaked lime slurry are subjected to chemical reaction, SO that SO 2, HCl, HF and other acid gases in the flue gas are removed, evaporation and drying of slurry moisture are realized, the flue gas at the outlet of a semi-dry deacidification tower is cooled to a temperature of about 150 ℃, and the flue gas is dedusted by a bag-type dust remover, SO that dust particles, heavy metals, dioxins and flue gas deacidification reaction products in the flue gas are removed. And the flue gas after dust removal enters the SCR reactor through a connecting flue. Because the temperature of the flue gas entering the SCR denitration system is lower and the catalytic denitration reaction temperature of the flue gas cannot be reached, the flue gas needs to be heated by an SGH (SEAM GAS HEAT exchange) heat Exchanger, so that the temperature of the flue gas before entering the catalyst module is raised to 180-185 ℃ or 220-230 ℃ (medium-temperature catalyst), and the catalytic denitration reaction temperature of the flue gas can be reached, thereby realizing further catalytic denitration of the flue gas. The flue gas after SCR catalytic denitration is subjected to heat recovery by a GGH (GAS GAS HEAT Exchanger) heat Exchanger arranged under a catalyst module, and is usually finally discharged into the atmosphere at a flue gas temperature of 165 ℃ (low temperature catalyst)/180 ℃ (medium temperature catalyst).
In the current technology, the hot flue gas of the boiler discharged from the outlet of the boiler economizer is subjected to the flue gas deacidification reaction in the semi-dry deacidification tower, and simultaneously, the moisture in the slurry is required to be evaporated and dried, so that the temperature of the flue gas entering the deacidification tower is reduced from about 200 ℃ at the inlet to about 150 ℃ at the outlet when the flue gas passes through the semi-dry deacidification tower, and the flue gas entering the SCR denitration reaction tower is required to be heated to the working temperature of the SCR denitration catalyst through the SGH heat exchanger in the SCR denitration process section, so that the further denitration purification of the flue gas can be realized. In the current desulfurization and denitrification process flow, the method has the technical problems of high flue gas temperature drop and flue gas temperature rise links, high flue gas overall flow resistance, complex process system, high running power consumption, low heat utilization rate and the like. If the ultra-low emission limit is further realized on the basis of the current desulfurization and denitrification process flow, a wet scrubbing tower is additionally arranged, and alkali liquor is used for further deacidifying the discharged flue gas, so that the whole flue gas purification process system is too complex, the flue gas flow and flow resistance are increased, and the electricity consumption and the running material consumption are increased.
Disclosure of Invention
In order to solve the technical problems, one of the purposes of the invention is to provide a method for purifying the waste incineration flue gas, which can be used for efficiently purifying and removing harmful secondary pollutants in the waste incineration flue gas.
In order to achieve the aim, the technical scheme of the invention is that the method for purifying the waste incineration flue gas comprises the steps of sequentially spraying sodium bicarbonate powder, activated carbon powder and ammonia gas in the flowing direction of the waste incineration flue gas, wherein the ammonia gas is used for carrying out denitration reduction reaction with NO x gas in the waste incineration flue gas under the action of a catalyst.
The technical scheme has the advantages that the sodium bicarbonate powder is quickly decomposed into anhydrous sodium carbonate particles with tiny holes and high reactivity under the high temperature effect of the waste incineration flue gas (namely, the sodium bicarbonate powder is quickly decomposed into porous anhydrous sodium carbonate particles with high reactivity under the high temperature environment through the SO-called popcorn effect), and reacts with SO 2, HCl, HF and other acid gases in the waste incineration flue gas to generate reaction products of Na 2SO4, naCl, naF and the like, SO that SO 2, HCl, HF and other acid gases in the waste incineration flue gas are removed, most high-boiling heavy metal substances, dioxin and the like in the waste incineration flue gas are all absorbed and trapped by active carbon, ammonia gas entering together with the waste incineration flue gas is subjected to denitration and reduction reaction with NO x gas in the waste incineration flue gas under the action of a catalyst, and NO x pollutants in the flue gas are reduced into harmless nitrogen and water vapor, and denitration is realized.
The second aim of the invention is to provide a waste incineration flue gas purification system which has a simple structure and can be used for efficiently purifying and removing harmful secondary pollutants in waste incineration flue gas.
In order to achieve the aim, the technical scheme of the invention is that the waste incineration flue gas purification system is used for executing the waste incineration flue gas purification method, and comprises a waste heat furnace economizer, a baking soda dry deacidification tower and a denitration filter bag dust collector, wherein the waste heat furnace economizer is provided with a first flue gas outlet, the baking soda dry deacidification tower is provided with a second flue gas inlet and a second flue gas outlet, the denitration filter bag dust collector is provided with a third flue gas inlet and a third flue gas outlet, the first flue gas outlet is communicated with the second flue gas inlet, baking soda fine powder is sprayed at the communication position of the first flue gas outlet and the second flue gas inlet, the second flue gas outlet is communicated with the third flue gas inlet, and activated carbon powder and ammonia gas are sprayed at the communication position of the second flue gas outlet and the third flue gas inlet.
The technical scheme has the beneficial effects that the garbage incineration flue gas can be firstly mixed with the sodium bicarbonate powder, at the moment, the sodium bicarbonate powder is expanded to form a porous structure under the high temperature effect, SO that the sodium bicarbonate powder reacts with SO 2, HCl, HF and other acid gases in the garbage incineration flue gas to generate reaction products such as Na 2SO4, naCl, naF and the like, thereby removing SO 2, HCl, HF and other acid gases in the garbage incineration flue gas, then the newly generated Na 2SO4, naCl and NaF are blown to a denitration filter bag dust remover along with active carbon powder, a layer of dust filter cake is formed on the surface of the filter bag along with fly ash separated by the filter bag, most low-boiling heavy metal substances, dioxin and the like in the garbage incineration flue gas are all adsorbed and trapped by the active carbon, the dust particles in the garbage incineration flue gas are separated from the flue gas flow together, and enter ammonia gas of the catalytic denitration dust remover together with the garbage incineration flue gas, when the catalytic denitration filter bag is filled with the catalyst, the catalyst layer is subjected to NO x gas in the garbage incineration flue gas under the effect of the catalyst layer, and the denitration reaction of NO x in the garbage flue gas is carried out, SO that the harmless smoke is reduced to realize the reduction of the nitrogen gas and the harmless smoke.
The waste heat boiler economizer also comprises a coupled waste heat recovery device, wherein the coupled waste heat recovery device is provided with a fourth flue gas inlet, a fourth flue gas outlet, a second water inlet, a second water outlet, a heat transfer medium inlet and a heat transfer medium outlet, the waste heat boiler economizer is further provided with a first water inlet and a first water outlet, the third flue gas outlet is communicated with the fourth flue gas inlet, and the first water inlet is communicated with the second water outlet.
The technical scheme has the beneficial effects that after acid gas, dust, heavy metal, dioxin and other harmful secondary pollutants in the waste incineration flue gas are removed, the heat in the waste incineration flue gas can be recycled by the coupled waste heat recovery device, one part of the heat is used for preheating main water fed into a boiler, and the other part of the heat can be used as other heat.
In the above technical scheme, the coupling type waste heat recovery device comprises a flue pipe, a heat exchange shell and a phase change heat pipe, wherein one end of the flue pipe forms a fourth flue gas inlet, the other end of the flue pipe forms a fourth flue gas outlet, two ends of the heat exchange pipe respectively pass through the pipe wall of the flue pipe to penetrate out of the flue pipe, one end of the heat exchange pipe forms a second water inlet, the other end of the heat exchange pipe forms a second water outlet, the heat exchange shell is arranged outside the flue pipe, the phase change heat pipe is provided with a condensation section and an evaporation section, the phase change heat pipe penetrates through the pipe wall of the flue pipe, the condensation section of the phase change heat pipe is positioned in the heat exchange shell, the evaporation section of the phase change heat pipe is positioned in the flue pipe, and the heat transfer medium inlet and the heat transfer medium outlet are arranged on the heat exchange shell and are communicated with the inside of the heat exchange shell.
The technical scheme has the beneficial effects that the main water entering the boiler can be preheated by the heat exchange tube, and the heat exchange shell and the phase change heat tube are combined to recover the heat in the flue tube for other use.
In the above technical scheme, the heat exchange tube is disposed at one end of the flue tube near the fourth flue gas inlet, and the phase change heat tube is near the fourth flue gas outlet.
The technical scheme has the beneficial effects that the heat exchange tube can recycle the heat of the high-temperature end of the flue tube, and the phase change heat tube can recycle the heat of the low-temperature end in the flue tube.
In the above technical solution, a plurality of phase-change heat pipes are provided.
The technical scheme has the beneficial effects that the heat at the low temperature end of the flue pipe is fully recycled by combining the plurality of phase change heat pipes with the heat exchange shell.
According to the technical scheme, fins are uniformly distributed on the evaporation section of the phase-change heat pipe.
The technical scheme has the beneficial effects that the evaporation section of the phase change heat pipe has better heat exchange effect.
In the technical scheme, the heat exchange tube is a serpentine coil.
The technical scheme has the beneficial effects that the heat exchange pipe has larger heat exchange area and heat exchange stroke in the flue pipe, so that the heat exchange effect is better.
In the technical scheme, the heat exchange shell and the flue pipe are integrally formed.
The technical scheme has the beneficial effects that the whole coupling type waste heat recovery device is more compact in size.
The heat exchanger comprises a heat exchange shell, a heat transfer medium inlet, a heat transfer medium outlet and a heat transfer medium inlet, wherein the heat exchange shell is used for accommodating heat transfer medium, the heat transfer medium outlet is communicated with the heat transfer medium inlet through the heat transfer pump, the heat transfer medium outlet is communicated with the heat transfer medium inlet, or the heat transfer medium outlet is communicated with the heat transfer medium inlet, and the heat transfer medium outlet is communicated with the heat transfer medium inlet through the heat transfer pump.
The technical scheme has the beneficial effects that the heat absorbed by the heat transfer medium in the heat exchange shell can be supplied to the user side heat exchanger, so that the user side heat exchanger can fully utilize the heat.
Drawings
Fig. 1 is a schematic structural diagram of a waste incineration flue gas purification system according to an embodiment of the present invention;
Fig. 2 is another schematic structural diagram of a waste incineration flue gas purification system according to an embodiment of the present invention;
Fig. 3 is a schematic structural diagram of the coupled waste heat recovery device according to an embodiment of the present invention.
In the figure, 1, a waste heat furnace economizer, 11, a first flue gas outlet, 12, a first water inlet, 13, a first water outlet, 2, a baking soda dry deacidification tower, 21, a second flue gas inlet, 22, a second flue gas outlet, 3, a denitration filter bag dust collector, 31, a third flue gas inlet, 32, a third flue gas outlet, 4, a coupling type waste heat recovery device, 41, a flue pipe, 411, a fourth flue gas inlet, 412, a fourth flue gas outlet, 42, a heat exchange pipe, 421, a second water inlet, 422, a second water outlet, 43, a heat exchange shell, 431, a heat transfer medium inlet, 432, a heat transfer medium outlet, 44, a phase change heat pipe, 441, fins, 5, a user side heat exchanger, 51, a refrigerant inlet, 52, a refrigerant outlet, 53, a heat medium inlet, 54, a heat medium outlet, 6 and a conveying pump.
Detailed Description
The principles and features of the present invention are described below with reference to the drawings, the examples are illustrated for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention. The invention is more particularly described by way of example in the following paragraphs with reference to the drawings. Advantages and features of the invention will become more apparent from the following description and from the claims. It should be noted that the drawings are in a very simplified form and are all to a non-precise scale, merely for convenience and clarity in aiding in the description of embodiments of the invention.
Example 1
The embodiment provides a method for purifying waste incineration flue gas, which comprises the steps of sequentially spraying sodium bicarbonate powder, activated carbon powder and ammonia gas in the flowing direction of the waste incineration flue gas, wherein the ammonia gas is used for carrying out denitration reduction reaction with NO x gas in the waste incineration flue gas under the action of a catalyst, the sodium bicarbonate powder mainly absorbs acid gas in the waste incineration flue gas, and the activated carbon powder is used for absorbing most high-boiling-point heavy metal substances, dioxin and the like in the waste incineration flue gas. The sodium bicarbonate powder is quickly decomposed into anhydrous sodium carbonate particles with tiny holes and high reactivity under the high temperature of the waste incineration flue gas (namely, the sodium bicarbonate powder is quickly decomposed into anhydrous sodium carbonate particles with high reactivity and porous sodium carbonate particles under the high temperature environment through a SO-called 'popcorn effect'), and the anhydrous sodium carbonate particles react with SO 2, HCl, HF and other acid gases in the waste incineration flue gas to generate reaction products such as Na 2SO4, naCl, naF and the like, SO that the removal of SO 2, HCl, HF and other acid gases in the waste incineration flue gas is realized, most high-boiling heavy metal substances, dioxin and the like in the waste incineration flue gas are all adsorbed and trapped by active carbon, and ammonia gas entering with the waste incineration flue gas is subjected to denitration and reduction reaction with NO x gas in the flue gas under the action of a catalyst, SO that NO x pollutants in the flue gas are reduced into harmless nitrogen and water vapor, and the denitration and purification of the flue gas are realized.
In this embodiment, the temperature of the waste incineration flue gas is 200-210 ℃, and after the waste incineration flue gas is subjected to denitration reduction reaction of baking soda powder, activated carbon powder and ammonia, the temperature of the waste incineration flue gas does not obviously drop, and heat in the waste incineration flue gas can be recycled later.
Example 2
As shown in fig. 1, the present embodiment provides a waste incineration flue gas purification system for performing the waste incineration flue gas purification method according to embodiment 1, comprising a waste heat boiler economizer 1, a baking soda dry deacidification tower 2 and a denitration filter bag dust collector 3, wherein the waste heat boiler economizer 1 is provided with a first flue gas outlet 11, the baking soda dry deacidification tower 2 is provided with a second flue gas inlet 21 and a second flue gas outlet 22, the denitration filter bag dust collector 3 is provided with a third flue gas inlet 31 and a third flue gas outlet 32, the first flue gas outlet 11 is communicated with the second flue gas inlet 21, baking soda fine powder is sprayed at the communication position of the first flue gas outlet 11 and the second flue gas inlet 31, and activated carbon powder and ammonia gas are sprayed at the communication position of the second flue gas outlet 22 and the third flue gas inlet 31; SO that the waste incineration flue gas is firstly mixed with the baking soda powder, the baking soda powder expands under the high temperature to form a porous structure, SO as to react with SO 2, HCl, HF and other acid gases in the waste incineration flue gas to generate Na 2SO4, naCl, naF and other reaction products, thereby removing SO 2, HCl, HF and other acid gases in the waste incineration flue gas, then the Na 2SO4, naCl and NaF are blown to a denitration filter bag dust collector along with active carbon powder, a layer of dust filter cake is formed on the surface of the filter bag along with fly ash separated by the filter bag, most low-boiling heavy metal substances, dioxin and the like in the waste incineration flue gas are all adsorbed and trapped by the active carbon, and are separated from the flue gas flow along with fly ash particles in the waste incineration flue gas, and enter ammonia gas of a catalytic denitration filter bag dust collector along with the waste incineration flue gas, when the waste incineration flue gas passes through the catalytic denitration filter bag (the catalyst is filled in the filter bag base cloth layer), and the catalyst is subjected to denitration reduction reaction with NO x gas in the flue gas, so that NO x pollutants in the flue gas are reduced into harmless nitrogen and water vapor, and denitration purification of the flue gas is realized. The activated carbon powder in this embodiment may be sprayed by an activated carbon spraying device to mix with the waste incineration flue gas.
In this embodiment, the flue gas discharged from the first flue gas outlet contains acidic gases such as SO 2, HCl, HF, NOx, dust, heavy metals, dioxin, oxygen, nitrogen, carbon dioxide, and water.
The temperature of the waste incineration flue gas is 200-210 ℃, baking soda powder can be expanded into a porous structure (similar to the forming principle of popcorn) at the temperature, the waste incineration flue gas can be slowed down after entering a baking soda dry deacidification tower, at the moment, the waste incineration flue gas is fully contacted with the expanded baking soda powder in the baking soda dry deacidification tower to fully absorb acid gases in the waste incineration flue gas by the expanded baking soda powder so as to generate powders such as Na 2SO4, naCl, naF and the like, the powders continuously flow along with the waste incineration flue gas, and active carbon powder and ammonia gas are added in the process, wherein the denitration filter bag dust collector 3 captures the dust in the waste incineration flue gas to form a layer of dust filter cake, the layer of dust filter cake can improve the dust capturing effect of the denitration filter bag dust collector, and meanwhile, the ammonia gas is subjected to denitration reduction reaction with NO x gas in the flue gas under the action of a catalyst (the catalyst is filled in a filter bag base cloth layer), so that NO x pollutants in the flue gas are reduced into harmless nitrogen and water vapor, and denitration purification of the flue gas is realized.
The mechanism of the reaction of the garbage incineration flue gas and the baking soda powder is as follows:
2NaHCO3(s)-→Na2CO3(s)+H2O(g)+CO2(g);
Na2CO3(s)+SO2(g)+1/2O2(g)-→Na2SO4(s)+CO2(g);
Na2CO3(s)+2HCl(g)→2NaCl(s)+H2O(g)+CO2(g);
Na2CO3(s)+2HF(g)→2NaF(s)+H2O(g)+CO2(g);
Wherein(s) is solid and (g) is gaseous.
The mechanism of the reaction of the waste incineration flue gas and ammonia gas is as follows:
4NO+4NH3+O2→4N2+6H2O;
6NO2+8NH3→7N2+12H2O;
NO+NO2+2NH3→2N2+3H2O;
As shown in fig. 2 and 3, the above technical solution further includes a coupled waste heat recovery device 4, where the coupled waste heat recovery device 4 has a fourth flue gas inlet 411, a fourth flue gas outlet 412, a second water inlet 421, a second water outlet 422, a heat transfer medium inlet 431, and a heat transfer medium outlet 432, the waste heat boiler economizer 1 further has a first water inlet 12 and a first water outlet 13, the third flue gas outlet 32 is communicated with the fourth flue gas inlet 411, and the first water inlet 12 is communicated with the second water outlet 422, so that after harmful secondary pollutants such as acid gas, dust, heavy metal, dioxin and the like in the waste incineration flue gas are removed, the temperature of the treated waste incineration flue gas is not significantly reduced, and the waste incineration flue gas has more heat, and at this time, the heat in the waste incineration flue gas can be recycled by the coupled waste heat recovery device, a part of the heat is used to preheat the main feed water entering the boiler, and another part of the heat can be used as it.
In the embodiment, dust removal and denitration of the waste incineration flue gas are completed on the surface of a denitration filter bag dust collector, a traditional denitration process SCR denitration reaction tower is not needed, the whole flue gas flow resistance is small, the denitration process system is simple, and no operation maintenance amount is needed.
In this embodiment, the fourth flue gas outlet is connected to the chimney under the action of the induced draft fan.
As shown in fig. 3, the coupled waste heat recovery device 4 in the above technical solution includes a flue pipe 41, a heat exchange pipe 42, a heat exchange shell 43 and a phase conversion heat pipe 44, one end of the flue pipe 41 forms the fourth flue gas inlet 411, the other end of the flue pipe 41 forms the fourth flue gas outlet 412, two ends of the heat exchange pipe 42 respectively pass through the pipe wall of the flue pipe 41 to outside the flue pipe 41, one end of the heat exchange pipe 42 forms the second water inlet 421, the other end of the heat exchange pipe 42 forms the second water outlet 422, the heat exchange shell 43 is disposed outside the flue pipe 41, the phase conversion heat pipe 44 has a condensation section and an evaporation section, the phase conversion heat pipe 44 passes through the pipe wall of the flue pipe 41 and the shell wall of the heat exchange shell 43, the condensation section of the phase conversion heat pipe 44 is located in the heat exchange shell 43, the evaporation section of the phase conversion heat pipe 44 is located in the heat exchange shell 41, the heat transfer medium inlet 431 and the medium outlet 432 are disposed on the heat exchange shell 43 and are both in communication with the heat exchange shell 43, and the heat exchange shell can be recovered by the heat exchange pipe and the heat exchange shell.
In this embodiment, the two ends of the phase change heat pipe are sealed, and the interior is vacuumized and filled with an organic solution (such as paraffin, fatty acid or polyol, which belongs to the prior art and is not described herein).
As shown in fig. 3, in the above technical solution, the heat exchange tube 42 is disposed at one end of the flue tube 41 near the fourth flue gas inlet 411, and the phase change heat pipe 44 is disposed near the fourth flue gas outlet 412, so that the heat exchange tube can recycle heat at the high temperature end of the flue tube, and the phase change heat pipe can recycle heat at the low temperature end of the flue tube.
As shown in fig. 3, the plurality of phase-change heat pipes 44 are provided in the above technical solution, so that the heat at the low temperature end of the flue pipe is fully recycled by combining the plurality of phase-change heat pipes with the heat exchange shell, in this embodiment, the temperature of the flue gas at the low temperature end is about 210 ℃ and the temperature of the flue gas at the low temperature end is about 140 ℃ relative to the temperature at the high temperature end.
In this embodiment, the phase-change heat pipes 44 are all vertically arranged, and the lower ends of the phase-change heat pipes are evaporation sections, while the upper ends thereof are condensation sections.
As shown in fig. 3, in the above technical solution, fins 441 are uniformly distributed on the evaporation section of the phase-change heat pipe 44, so that the evaporation section of the phase-change heat pipe has a better heat exchange effect.
As shown in FIG. 3, the heat exchange tube 42 is a serpentine coil in the above technical scheme, so that the heat exchange tube has a larger heat exchange area and heat exchange stroke in the flue tube, and the heat exchange effect is better.
As shown in fig. 3, a plurality of heat exchange tubes may be provided in this embodiment, so that the heat recovery effect of the waste incineration flue gas may be increased.
In the above technical solution, the heat exchange shell 43 and the flue pipe 41 are integrally formed, so that the whole coupling type waste heat recovery device is more compact.
As shown in fig. 2, the above technical solution further includes a user side heat exchanger 5 and a transfer pump 6, where the user side heat exchanger 5 has a refrigerant inlet 51, a refrigerant outlet 52, a heat medium inlet 53 and a heat medium outlet 54 (the refrigerant inlet 51 communicates with the refrigerant outlet 52, and the heat medium inlet 53 communicates with the heat medium outlet 54), the heat exchange shell 43 is used to accommodate a heat medium, the heat medium outlet 432 communicates with the heat medium inlet 53 through the transfer pump 6, the heat medium outlet 54 communicates with the heat medium inlet 431, or the heat medium outlet 432 communicates with the heat medium inlet 53, and the heat medium outlet 54 communicates with the heat medium inlet 431 through the transfer pump 6, so that the heat absorbed by the heat medium in the heat exchange shell can be supplied to the user side heat exchanger, so that the user side heat exchanger can fully utilize the heat. The heat transfer medium in this embodiment may be desalinated water or heat transfer oil. In this embodiment, the phase-change heat pipe is used to transfer the heat in the flue pipe to the heat exchange shell to heat the heat exchange medium, and the heat exchange medium circulates between the heat exchange shell and the user side heat exchanger under the action of the transfer pump to transfer the heat from the heat exchange shell to the user side heat exchanger. Wherein, the refrigerant inlet and the refrigerant outlet are communicated to form a refrigerant channel, and water is used as a medium to be introduced into the refrigerant channel.
The foregoing description is only a preferred embodiment of the present invention, and is not intended to limit the invention in any way, and those skilled in the art may easily implement the present invention as shown in the drawings and described above, but many modifications, adaptations and variations of the present invention using the above disclosed technical matters will be equivalent to the embodiments of the present invention without departing from the scope of the present invention, and meanwhile, any equivalent changes, adaptations and variations of the above embodiments according to the essential technology of the present invention are all within the scope of the technical matters of the present invention.
Claims (10)
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| CN101576360A (en) * | 2009-06-01 | 2009-11-11 | 南京工业大学 | Low-level energy recycling efficient combined type heat exchange device based on heat pipes and finned tubes |
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| CN113262623A (en) * | 2021-05-19 | 2021-08-17 | 北京中科润宇环保科技股份有限公司 | Process method for cooperatively treating various pollutants in flue gas of waste incinerator |
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| CN101576360A (en) * | 2009-06-01 | 2009-11-11 | 南京工业大学 | Low-level energy recycling efficient combined type heat exchange device based on heat pipes and finned tubes |
| KR20150141331A (en) * | 2014-06-10 | 2015-12-18 | (주)대장성보일러 | a waste heat recovery facility of boiler exhaust fumes |
| CN110756033A (en) * | 2019-10-25 | 2020-02-07 | 山东电力工程咨询院有限公司 | Deep purification treatment system and process for waste incineration power station flue gas |
| CN213913094U (en) * | 2021-05-19 | 2021-08-10 | 北京中科润宇环保科技股份有限公司 | Garbage incinerator flue gas multiple pollutant coprocessing device |
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