CN211782802U - Energy-saving efficient synergistic treatment system for multiple pollutants in flue gas - Google Patents
Energy-saving efficient synergistic treatment system for multiple pollutants in flue gas Download PDFInfo
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- CN211782802U CN211782802U CN201921712244.7U CN201921712244U CN211782802U CN 211782802 U CN211782802 U CN 211782802U CN 201921712244 U CN201921712244 U CN 201921712244U CN 211782802 U CN211782802 U CN 211782802U
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 312
- 239000003546 flue gas Substances 0.000 title claims abstract description 241
- 239000003344 environmental pollutant Substances 0.000 title claims abstract description 33
- 231100000719 pollutant Toxicity 0.000 title claims description 22
- 230000002195 synergetic effect Effects 0.000 title claims description 14
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 79
- 239000007789 gas Substances 0.000 claims abstract description 69
- 238000001816 cooling Methods 0.000 claims abstract description 51
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 28
- 238000001514 detection method Methods 0.000 claims description 82
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 37
- 229910052760 oxygen Inorganic materials 0.000 claims description 37
- 239000001301 oxygen Substances 0.000 claims description 37
- 238000011084 recovery Methods 0.000 claims description 31
- 239000002918 waste heat Substances 0.000 claims description 31
- 239000000446 fuel Substances 0.000 claims description 30
- 238000011144 upstream manufacturing Methods 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 14
- 239000000779 smoke Substances 0.000 claims description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 7
- 238000010792 warming Methods 0.000 claims description 7
- 230000009467 reduction Effects 0.000 claims description 5
- 239000013589 supplement Substances 0.000 claims description 2
- 230000001502 supplementing effect Effects 0.000 claims description 2
- 238000006477 desulfuration reaction Methods 0.000 abstract description 37
- 230000023556 desulfurization Effects 0.000 abstract description 37
- 238000005245 sintering Methods 0.000 abstract description 30
- 238000000034 method Methods 0.000 abstract description 23
- 230000008569 process Effects 0.000 abstract description 20
- 230000003647 oxidation Effects 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract description 3
- 230000006872 improvement Effects 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 18
- 238000001179 sorption measurement Methods 0.000 description 15
- 229910052799 carbon Inorganic materials 0.000 description 10
- 238000010438 heat treatment Methods 0.000 description 10
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 9
- 239000000428 dust Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 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
- 238000004140 cleaning Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
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Abstract
An energy-saving flue gas multi-pollutant efficient cooperative treatment system comprises a desulfurization tower, a denitration tower, a flue gas cooling heat exchanger and a carbon monoxide treatment device; the original flue gas pipeline is communicated with the gas inlet of the desulfurizing tower; the gas outlet of the desulfurization tower is communicated with the gas inlet of the denitration tower through a first pipeline; the gas outlet of the denitration tower is communicated with the second pipeline; wherein, the flue gas cooling heat exchanger is arranged on the original flue gas pipeline; the carbon monoxide treatment device is arranged on the first pipeline. The technical scheme provided by the utility model, can effectively reduce the temperature that gets into the sintering flue gas of desulfurizing tower, improve desulfurization efficiency, can benefit to the chemical energy improvement of CO oxidation simultaneously and get into the temperature of the sintering flue gas of denitration tower. Thereby improving the efficiency of desulfurization and denitration of the whole system and increasing the process by-product value.
Description
Technical Field
The utility model relates to a many pollutants of flue gas treatment system, concretely relates to high-efficient treatment system in coordination of many pollutants of energy-saving flue gas belongs to sintering gas cleaning technical field.
Background
In the sintering process, the flue gas discharged by sintering is large in quantity, the pollutant components are complex, and SO is contained2、NOx、CO、CO2Dust, dioxin and other pollutants, the great fluctuation of the discharge temperature (110-2Dust, NOx, heavy metals and the like, and can realize by-product SO2The resource utilization is an advanced flue gas purification technology, and is widely popularized and applied in the sintering industry and the coking industry in recent years.
The active carbon adsorption is currently divided into two modes of single-stage adsorption and two-stage adsorption, wherein the single-stage adsorption is to simultaneously adsorb multiple pollutants in one adsorption tower, ammonia gas is added at the inlet of the adsorption tower, and the method can achieve SO2Efficiency of removal>98 percent, the denitration rate is about 50 percent, and the outlet concentration of the dust is less than 10mg/Nm 3. With the proposal of ultra-low emission standard, part of steel plants adopt two-stage adsorption, wherein, the first-stage tower carries out desulfurization, dust removal and the like, and the second-stage tower carries out denitration; or adopts a single-stage adsorption and SCR denitration process, fully utilizes the technical advantages of the active carbon process, realizes the advantage of resource utilization,the two process methods can realize the outlet SO2<35mg/Nm3，NOx<50mg/Nm3, dust<Target of 10mg/Nm3, also due to SO2The polarity is stronger, compared with NOx, the active carbon is easier to react with, therefore, in the active carbon double-stage adsorption process, the first stage mainly carries out desulfurization and the second stage mainly carries out denitration, but because the sintering flue gas components are greatly influenced by sintering ore, SO in the flue gas2Large fluctuation, high temperature, different humidity and uneven quality level of the activated carbon are not beneficial to the desulfurization of the activated carbon, SO that SO treated by the primary activated carbon process is very likely to appear on the engineering site2Under the condition of higher concentration, when the flue gas enters a secondary adsorption tower or an SCR denitration process, the denitration can be extremely adversely affected, for example, for the secondary adsorption tower, the using amount of ammonia can be increased, the system resistance can be improved, and the operation cost can be increased; for SCR denitration process, SO in flue gas2Sticky ammonium sulfate is produced on the catalyst to block the catalyst gap, resulting in catalyst deactivation. Aiming at the active carbon two-stage adsorption process and the active carbon + SCR combined desulfurization and denitrification process, the control of the desulfurization efficiency of the one-stage active carbon process plays an important role in the stable operation of the whole flue gas purification system.
Therefore, how to provide an energy-saving flue gas multi-pollutant efficient synergistic treatment system, the system can effectively reduce the temperature of the sintering flue gas entering the desulfurizing tower, improve the desulfurizing efficiency, and simultaneously can improve the temperature of the sintering flue gas entering the denitrifying tower by utilizing the chemical energy of CO oxidation. Therefore, the efficiency of desulfurization and denitrification of the whole system is improved, and the process by-product value is increased, which is a technical problem to be solved urgently by technical personnel in the field.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model aims to improve the desulfurization efficiency by reducing the temperature of the sintering flue gas entering the desulfurization tower; the temperature of the sintering flue gas entering the denitration tower is improved by the heat generated by CO oxidation. The utility model provides an energy-saving flue gas multi-pollutant high-efficiency cooperative treatment system, which comprises a desulfurizing tower, a denitrifying tower, a flue gas cooling heat exchanger and a carbon monoxide treatment device; the original flue gas pipeline is communicated with the gas inlet of the desulfurizing tower; the gas outlet of the desulfurization tower is communicated with the gas inlet of the denitration tower through a first pipeline; the gas outlet of the denitration tower is communicated with the second pipeline; wherein, the flue gas cooling heat exchanger is arranged on the original flue gas pipeline; the carbon monoxide treatment device is arranged on the first pipeline.
According to the utility model discloses an embodiment provides an energy-saving flue gas multiple pollutants high efficiency treatment system in coordination:
an energy-saving flue gas multi-pollutant efficient cooperative treatment system comprises a desulfurization tower, a denitration tower, a flue gas cooling heat exchanger and a carbon monoxide treatment device; the original flue gas pipeline is communicated with the gas inlet of the desulfurizing tower; the gas outlet of the desulfurization tower is communicated with the gas inlet of the denitration tower through a first pipeline; the gas outlet of the denitration tower is communicated with the second pipeline; the flue gas cooling is arranged on the original flue gas pipeline; the carbon monoxide treatment device is arranged on the first pipeline.
Preferably, the flue gas cooling heat exchanger comprises: a flue gas heat exchange area and a medium heat exchange area; the smoke heat exchange area and the medium heat exchange area are mutually attached; the original flue gas pipeline is communicated with the desulfurizing tower through a flue gas heat exchange area; a feed inlet of the medium heat exchange area is communicated with a low-temperature medium through a third pipeline; and a discharge hole of the medium heat exchange area is communicated with the fourth pipeline.
Preferably, the feed inlet of the medium heat exchange zone is communicated with the low-temperature medium through a third pipeline, and the system further comprises: a blower; an air outlet of the air blower is communicated with one end of the third pipeline, which is far away from the medium heat exchange area; and the air inlet of the blower is communicated with the atmosphere.
Preferably, the system further comprises: a water pump; a water outlet of the water pump is connected to a feed inlet of the medium heat exchange area through a third pipeline; the water inlet of the water pump is communicated with a low-temperature water source.
Preferably, the system further comprises a first flue gas temperature detection device, wherein the first flue gas temperature detection device is arranged on the original flue gas pipeline and is positioned at the downstream of the flue gas cooling heat exchanger.
Preferably, the system also comprises a flue gas flow detection device, a second flue gas temperature detection device, a medium flow detection device, a first medium temperature detection device and a second medium temperature detection device; the flue gas flow detection device and the second flue gas temperature detection device are arranged on the original flue gas pipeline, and the second flue gas temperature detection device is positioned at the upstream of the flue gas cooling heat exchanger; the smoke flow detection device is positioned at the upstream or the downstream of the smoke cooling heat exchanger; the medium flow detection device is arranged on the third pipeline or the fourth pipeline, the first medium temperature detection device is arranged on the third pipeline, and the second medium temperature detection device is arranged on the fourth pipeline.
Preferably, the flow rate of the raw flue gas measured by the flue gas flow rate detection device is qFlue gasThe temperature of the raw flue gas after heat exchange measured by the first flue gas temperature detection device is t1, the temperature of the raw flue gas before heat exchange measured by the second flue gas temperature detection device is t2, and the flow rate of the medium measured by the medium flow rate detection device is qMediumThe temperature of the medium before heat exchange measured by the first medium temperature detection device is t3, and the temperature of the medium after heat exchange measured by the second medium temperature detection device is t 4; the total heat exchange quantity of the flue gas cooling heat exchanger is QGeneral assemblySatisfying the following formula (1):
Qgeneral assembly＝qFlue gasρ1CCigarette with heating means(t2-t1)＝qMediumρ2CCold(t4-t3) (1)；
Obtaining formula (2) according to formula (1)
Where ρ is1Is the average density of the flue gas, p2Is the average density of the medium, CCigarette with heating meansIs the average specific heat capacity of the flue gas, CColdIs the average specific heat capacity of the medium.
Preferably, the carbon monoxide treatment device is a reaction device for converting carbon monoxide into carbon dioxide; preferably, the system further comprises an oxygen-containing gas delivery pipe connected to an oxygen-containing gas replenishment inlet of the carbon monoxide processing apparatus, the oxygen-containing gas delivery pipe replenishing the carbon monoxide processing apparatus with the oxygen-containing gas.
Preferably, the system further comprises a fuel delivery conduit connected to a fuel replenishment inlet of the carbon monoxide processing apparatus or to the first conduit upstream of the carbon monoxide processing apparatus, the fuel delivery conduit replenishing fuel to the carbon monoxide processing apparatus or to the first conduit upstream of the carbon monoxide processing apparatus.
Preferably, the oxygen-containing gas is used as a cooling medium, and the oxygen-containing gas is conveyed to a medium heat exchange area of the flue gas cooling heat exchanger through a third pipeline; then the carbon monoxide is conveyed to a carbon monoxide treatment device from a discharge hole of the medium heat exchange area through a fourth pipeline and an oxygen-containing gas conveying pipeline in sequence.
Preferably, the system further comprises: a temperature-rising heat exchanger; the temperature-raising heat exchanger is arranged on the first pipeline and is positioned at the upstream or the downstream of the carbon monoxide treatment device; the temperature-rising heat exchanger is used for adjusting the temperature of the flue gas upstream or downstream of the carbon monoxide treatment device.
Preferably, the system further comprises: a waste heat recovery heat exchanger; the waste heat recovery heat exchanger is arranged on the second pipeline; the heating heat exchanger and the waste heat recovery heat exchanger are respectively and independently indirect heat exchange devices, preferably shell-and-tube heat exchange devices, and more preferably DDH heat exchangers; preferably, the medium outlet of the warming heat exchanger is connected with the medium inlet of the waste heat recovery heat exchanger through a first medium conveying pipeline, and the medium outlet of the waste heat recovery heat exchanger is connected with the medium inlet of the warming heat exchanger through a second medium conveying pipeline.
Preferably, the desulfurization tower is a dry desulfurization system, a semi-dry desulfurization system or a wet desulfurization system.
Preferably, the denitration tower is an SCR denitration system or an SNCR denitration system.
In this application, the sintering flue gas is after the desulfurizing tower desulfurization, reentrants denitration tower carries out the denitration. The temperature that the active carbon technology got rid of the pollutant has following law after the experiment is verified repeatedly, and low temperature is favorable to desulfurization reaction promptly, and high temperature helps denitration reaction, and SCR denitration technology, high temperature helps the denitration. Therefore, in order to improve the removal efficiency of multiple pollutants and efficiently realize the ultra-low emission purification effect, the method canThe mode of respectively controlling the temperatures of a two-stage adsorption process and an active carbon and SCR combined process is realized, for example, in the two-stage active carbon flue gas purification process, the inlet flue gas temperatures of a desulfurizing tower and a denitration tower are respectively controlled, wherein the low-temperature control of the desulfurizing tower is met, and SO is treated under the condition of not adding ammonia2Realizing high-efficiency complete removal, controlling the high temperature of the denitration tower and avoiding SO2Or SO2Under the condition of extremely low content, the removal efficiency at higher temperature can be realized. In addition, because the fuel can be fully combusted in the sintering process and the fuel can not be fully combusted, the flue gas contains a certain amount of CO gas, the content is generally 4000-10000mg/Nm3, and the CO can be fully converted into CO2The heat, can improve denitration tower entry flue gas temperature, perhaps improve SCR entry flue gas temperature, reduce or even saved the process of heating up this flue gas through external fuel, the high-efficient many pollutions in the desorption flue gas in coordination. So, among the technical scheme that this application provided, lead to and be provided with flue gas cooling heat exchanger on the former flue gas pipeline of sintering flue gas, and be provided with carbon monoxide processing apparatus on the first pipeline between desulfurizing tower and denitration tower simultaneously. The flue gas cooling heat exchanger is used for reducing the temperature of sintering flue gas entering the desulfurizing tower; and the carbon monoxide treatment device is used for increasing the temperature of the sintering flue gas entering the denitration tower. The invention fully utilizes the excellent performances of high efficiency and large adsorption capacity of sulfur dioxide adsorption at low temperature and low denitration efficiency at low temperature but good denitration performance after heating to high temperature in the activated carbon technology, simultaneously utilizes a certain amount of carbon monoxide contained in the sintering flue gas, utilizes the heat emitted in the carbon monoxide conversion process to assist the heating of the flue gas for the purpose of denitration treatment when removing the carbon monoxide, can save the use of fuel, simultaneously treats the carbon monoxide in the flue gas and reduces the pollution of the flue gas to the environment.
In this application, one of flue gas cooling heat exchanger shell and tube type heat exchanger, GGH heat exchanger.
The flue gas cooling heat exchanger is a medium heat exchanger. Namely, the heat is transferred to other media through active indirect contact, and the heat is discharged through other media, so that the heat of the smoke in the original smoke pipeline is reduced. The medium in the flue gas cooling heat exchanger can be gas or liquid; the medium in the flue gas cooling heat exchanger is preferably air or water; the medium in the flue gas cooling heat exchanger is more preferably air. The air is used as a medium in the flue gas cooling heat exchanger, is preheated by the flue gas cooling heat exchanger and is conveyed to the carbon monoxide treatment device to be used as combustion-supporting gas. The temperature of flue gas preheats combustion-supporting gas before utilizing the desulfurization, make full use of heat resource, improve the desulfurization after, the temperature of flue gas before entering denitrification facility, and then guarantee denitration efficiency.
In this application, the medium that lets in medium heat transfer district among the flue gas cooling heat exchanger can be normal atmospheric temperature air or normal atmospheric temperature water. And normal temperature air or water flows into the medium heat exchange area under the action of the air blower or the water pump, so that the temperature of the original flue gas pipeline is taken away.
In this application, first flue gas temperature detection device sets up on former flue gas pipeline, and is located the low reaches of flue gas cooling heat exchanger, and first flue gas temperature detection device is on the former flue gas pipeline between flue gas cooling heat exchanger and desulfurizing tower promptly. The first flue gas temperature detection device can accurately measure the temperature of the original flue gas entering the desulfurizing tower. Can judge the cooling effect of flue gas cooling heat exchanger to former flue gas through the temperature value that measures, when the cooling temperature was not enough, the accessible cooperation was adjusted and is reduced the flow of former flue gas or is adjusted the flow that increases the medium of flue gas cooling heat exchanger, can be in order to improve the cooling effect of flue gas cooling heat exchanger to former flue gas.
In this application, through the cooperation of first flue gas temperature detection device, flue gas flow detection device, second flue gas temperature detection device, medium flow detection device, first medium temperature detection device and second medium temperature detection device jointly, can accurately measure the heat transfer volume Q that former flue gas pipeline needs in order to reach the cooling purposeGeneral assemblySo as to calculate the flow demand q of the mediumMediumFinally with reference to qMediumThe numerical value of the temperature-reducing gas flow rate is used for adjusting the flow rate of the medium of the flue gas temperature-reducing heat exchanger, so that the sintering flue gas is accurately cooled to the target temperature, and the optimal temperature requirement of the desulfurization process of the desulfurization tower is met.
In this application, the carbon monoxide treatment device is a reaction device for converting carbon monoxide into carbon dioxide, and heat is released in the process of oxidizing carbon monoxide into carbon dioxide.
In this application, an oxygen-containing gas delivery conduit passes an oxygen-containing gas from an oxygen-containing gas make-up inlet into a carbon monoxide processing apparatus to oxidize carbon monoxide to carbon dioxide.
In this application, fuel conveying pipe lets in fuel in first flue gas pipeline or carbon monoxide processing apparatus, utilizes the oxygen in the flue gas to heat the sintering flue gas through lighting the flue gas.
In this application, the flue gas still includes the waste heat recovery heat exchanger, and the waste heat recovery heat exchanger sets up on the second pipeline, sets up the low reaches at the denitration tower promptly. And after the flue gas is denitrated, the temperature of the sintering flue gas is high. And the waste heat recovery heat exchanger recovers and utilizes the energy of the denitrated sintering flue gas.
In this application, waste heat recovery heat exchanger can carry out the heat transfer with the intensification heat exchanger that sets up to be located carbon monoxide processing apparatus upper reaches and/or low reaches on first pipeline to in the sintering flue gas of first pipeline is got back to in the energy transfer of the flue gas after the denitration, thereby among the reduction carbon monoxide processing apparatus, in the energy that consumes for increasing the temperature.
In the present application, the desulfurization tower is one of a dry desulfurization system, a semi-dry desulfurization system, or a wet desulfurization system. The denitration tower is an SCR denitration system or an SNCR denitration system.
In the application, the medium heat exchanger, the warming heat exchanger and the waste heat recovery heat exchanger are all indirect heat exchange devices, preferably shell-and-tube heat exchange devices, and more preferably GGH heat exchangers.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the technical scheme provided by the application can reduce the temperature of the sintering flue gas entering the desulfurizing tower, thereby improving the desulfurizing efficiency and reducing the production cost;
2. the application provides a technical scheme can effectively improve the temperature of the sintering flue gas of denitration tower to improve the denitration efficiency of denitration tower.
3. The technical scheme provided by the application can effectively utilize the oxidation of CO in the sintering flue gas, and improve the temperature of the sintering flue gas.
4. The technical scheme that this application provided can utilize the energy of the sintering flue gas after the denitration to heat the sintering flue gas that gets into the denitration tower, reduces for the improvement get into denitration tower sintering flue gas temperature and the energy of extra consumption.
Drawings
FIG. 1 is a schematic view of the overall structure of the energy-saving efficient synergistic flue gas multi-pollutant treatment system of the present invention;
FIG. 2 is a schematic structural diagram of an embodiment of the present invention in which a temperature raising device is disposed downstream of a carbon monoxide treatment device;
FIG. 3 is a schematic structural view of an embodiment of the present invention in which a temperature raising device is disposed upstream of a carbon monoxide treatment device;
fig. 4 is the structure schematic diagram of the embodiment of preheating the oxygen-containing gas in the oxygen-containing gas conveying pipeline by the middle flue gas cooling heat exchanger.
Reference numerals:
1: a desulfurizing tower; 2: a denitration tower; 3: a flue gas cooling heat exchanger; 301: a flue gas heat exchange area; 302: a medium heat transfer zone; 4: a carbon monoxide treatment device; 5: a blower; 6: a water pump; 7: a temperature-rising heat exchanger; 8: a waste heat recovery heat exchanger; t1: a first flue gas temperature detection device; q1: a flue gas flow rate detection device; t2: a second flue gas temperature detection device; q2: a medium flow rate detection device; t3: a first medium temperature detection device; t4: a second medium temperature detection device;
l0: an original flue gas pipeline; l1: a first conduit; l2: a second conduit; l3: a third pipeline; l4: a fourth conduit; l5: an oxygen-containing gas delivery conduit; l6: a fuel delivery conduit; l7: a first medium delivery conduit; l8: a second media delivery conduit.
Detailed Description
According to the utility model discloses an embodiment provides an energy-saving flue gas multiple pollutants high efficiency treatment system in coordination:
an energy-saving flue gas multi-pollutant efficient cooperative treatment system comprises a desulfurization tower 1, a denitration tower 2, a flue gas cooling heat exchanger 3 and a carbon monoxide treatment device 4; the original flue gas pipeline L0 is communicated with the gas inlet of the desulfurizing tower 1; the gas outlet of the desulfurizing tower 1 is communicated with the gas inlet of the denitrifying tower 2 through a first pipeline L1; the gas outlet of the denitration tower 2 is communicated with a second pipeline L2; the flue gas cooling heat exchanger 3 is arranged on an original flue gas pipeline L0; the carbon monoxide treatment device 4 is provided on the first line L1.
Preferably, the flue gas cooling heat exchanger 3 comprises: a flue gas heat exchange area 301 and a medium heat exchange area 302; the flue gas heat exchange area 301 and the medium heat exchange area 302 are attached to each other; the original flue gas pipeline L0 is communicated with the desulfurizing tower 1 through a flue gas heat exchange area 301; the feed inlet of the medium heat exchange area 302 is communicated with the low-temperature medium through a third pipeline L3; the discharge port of the medium heat exchange area 302 is communicated with a fourth pipeline L4.
Preferably, the feed port of the medium heat exchange zone 302 is communicated with the low-temperature medium through a third pipeline L3, specifically, the system further comprises: a blower 5; an air outlet of the air blower 5 is communicated with one end of the third pipeline L3 far away from the medium heat exchange area 302; and an air inlet of the blower 5 is communicated with the atmosphere.
Preferably, the system further comprises: a water pump 6; the water outlet of the water pump 6 is connected to the inlet of the medium heat exchange area 302 through a third pipeline L3; the water inlet of the water pump 6 is communicated with a low-temperature water source.
Preferably, the system further comprises a first flue gas temperature detection device T1, and the first flue gas temperature detection device T1 is arranged on the original flue gas pipeline L0 and is located downstream of the flue gas temperature-reducing heat exchanger 3.
Preferably, the system further comprises a flue gas flow rate detection device Q1, a second flue gas temperature detection device T2, a medium flow rate detection device Q2, a first medium temperature detection device T3 and a second medium temperature detection device T4; the flue gas flow detection device Q1 and the second flue gas temperature detection device T2 are arranged on the original flue gas pipeline L0, and the second flue gas temperature detection device T2 is positioned at the upstream of the flue gas cooling heat exchanger 3; the smoke flow detection device Q1 is positioned at the upstream or downstream of the smoke cooling heat exchanger 3; the medium flow rate detecting device Q2 is provided on the third duct L3 or the fourth duct L4, the first medium temperature detecting device T3 is provided on the third duct L3, and the second medium temperature detecting device T4 is provided on the fourth duct L4.
Preferably, the flow rate of the raw flue gas measured by the flue gas flow rate detection device Q1 is QFlue gasThe temperature of the raw flue gas after heat exchange measured by the first flue gas temperature detection device T1 is T1, the temperature of the raw flue gas before heat exchange measured by the second flue gas temperature detection device T2 is T2, and the flow rate of the medium measured by the medium flow rate detection device Q2 is QMediumThe temperature of the medium before heat exchange measured by the first medium temperature detection device T3 is T3, and the temperature of the medium after heat exchange measured by the second medium temperature detection device T4 is T4; the total heat exchange quantity of the flue gas cooling heat exchanger 3 is QGeneral assemblySatisfying the following formula (1):
Qgeneral assembly＝qFlue gasρ1CCigarette with heating means(t2-t1)＝qMediumρ2CCold(t4-t3) (1)；
Obtaining formula (2) according to formula (1)
Where ρ is1Is the average density of the flue gas, p2Is the average density of the medium, CCigarette with heating meansIs the average specific heat capacity of the flue gas, CColdIs the average specific heat capacity of the medium.
Preferably, the carbon monoxide treatment apparatus 4 is a reaction apparatus for converting carbon monoxide into carbon dioxide; preferably, the system further includes an oxygen-containing gas delivery pipe L5, the oxygen-containing gas delivery pipe L5 being connected to an oxygen-containing gas supplement inlet of the carbon monoxide processing device 4, and the oxygen-containing gas delivery pipe L5 supplementing the oxygen-containing gas into the carbon monoxide processing device 4.
Preferably, the system further comprises a fuel delivery line L6, the fuel delivery line L6 being connected to a fuel make-up inlet of the carbon monoxide processing unit 4 or the first line L1 upstream of the carbon monoxide processing unit 4, the fuel delivery line L6 making up fuel into the carbon monoxide processing unit 4 or the first line L1 upstream of the carbon monoxide processing unit 4.
Preferably, oxygen-containing gas is used as the temperature reduction medium, and the oxygen-containing gas is conveyed to the medium heat exchange area 302 of the flue gas temperature reduction heat exchanger 3 through the third pipeline L3; then, the gas is sent from the outlet of the medium heat exchange zone 302 to the carbon monoxide treatment apparatus 4 through a fourth line L4 and an oxygen-containing gas line L5 in this order.
Preferably, the system further comprises: a temperature-rising heat exchanger 7; the temperature-raising heat exchanger 7 is disposed on the first pipeline L1, and the temperature-raising heat exchanger 7 is located upstream or downstream of the carbon monoxide processing apparatus 4; the temperature-raising heat exchanger 7 is used for adjusting the temperature of the flue gas upstream or downstream of the carbon monoxide treatment device 4.
Preferably, the system further comprises: a waste heat recovery heat exchanger 8; the waste heat recovery heat exchanger 8 is arranged on the second pipeline L2; the temperature rise heat exchanger 7 and the waste heat recovery heat exchanger 8 are respectively and independently indirect heat exchange devices, preferably shell-and-tube heat exchange devices, and more preferably DDH heat exchangers; preferably, the medium outlet of the warming heat exchanger 7 is connected to the medium inlet of the waste heat recovery heat exchanger 8 through a first medium conveyance line L7, and the medium outlet of the waste heat recovery heat exchanger 8 is connected to the medium inlet of the warming heat exchanger 7 through a second medium conveyance line L8.
Preferably, the desulfurization tower 1 is a dry desulfurization system, a semi-dry desulfurization system, or a wet desulfurization system.
Preferably, the denitration tower 2 is an SCR denitration system or an SNCR denitration system.
Example 1
An energy-saving flue gas multi-pollutant efficient cooperative treatment system comprises a desulfurization tower 1, a denitration tower 2, a flue gas cooling heat exchanger 3 and a carbon monoxide treatment device 4; the original flue gas pipeline L0 is communicated with the gas inlet of the desulfurizing tower 1; the gas outlet of the desulfurizing tower 1 is communicated with the gas inlet of the denitrifying tower 2 through a first pipeline L1; the gas outlet of the denitration tower 2 is communicated with a second pipeline L2;
wherein, the flue gas cooling heat exchanger 3 is arranged on the original flue gas pipeline L0; the carbon monoxide treatment device 4 is provided on the first line L1.
Example 2
Example 1 is repeated except that the flue gas cooling heat exchanger 3 comprises: a flue gas heat exchange area 301 and a medium heat exchange area 302; the flue gas heat exchange area 301 and the medium heat exchange area 302 are attached to each other; the original flue gas pipeline L0 is communicated with the desulfurizing tower 1 through a flue gas heat exchange area 301; the feed inlet of the medium heat exchange area 302 is communicated with the low-temperature medium through a third pipeline L3; the discharge port of the medium heat exchange area 302 is communicated with a fourth pipeline L4.
Example 3
Example 2 is repeated, except that the feed port of the medium heat exchange region 302 is communicated with the low-temperature medium through a third pipeline L3, specifically, the system further comprises: a blower 5; an air outlet of the air blower 5 is communicated with one end of the third pipeline L3 far away from the medium heat exchange area 302; and an air inlet of the blower 5 is communicated with the atmosphere.
Example 4
Example 3 is repeated, except that the feed port of the medium heat exchange region 302 is communicated with the low-temperature medium through a third pipeline L3, specifically, the system further comprises: a water pump 6; the water outlet of the water pump 6 is connected to the inlet of the medium heat exchange area 302 through a third pipeline L3; the water inlet of the water pump 6 is communicated with a low-temperature water source.
Example 5
Example 4 is repeated, except that the system further comprises a first flue gas temperature detection device T1, and the first flue gas temperature detection device T1 is arranged on the original flue gas pipeline L0 and is located downstream of the flue gas temperature-reducing heat exchanger 3.
Example 6
Example 5 is repeated except that the system further comprises a flue gas flow rate detection device Q1, a second flue gas temperature detection device T2, a medium flow rate detection device Q2, a first medium temperature detection device T3 and a second medium temperature detection device T4; the flue gas flow detection device Q1 and the second flue gas temperature detection device T2 are arranged on the original flue gas pipeline L0, and the second flue gas temperature detection device T2 is positioned at the upstream of the flue gas cooling heat exchanger 3; the smoke flow detection device Q1 is positioned at the upstream or downstream of the smoke cooling heat exchanger 3; the medium flow rate detecting device Q2 is provided on the third duct L3 or the fourth duct L4, the first medium temperature detecting device T3 is provided on the third duct L3, and the second medium temperature detecting device T4 is provided on the fourth duct L4.
Example 7
Example 6 was repeated except that the flow rate of the raw flue gas measured by the flue gas flow rate measuring device Q1 was QFlue gasThe temperature of the raw flue gas after heat exchange measured by the first flue gas temperature detection device T1 is T1, the temperature of the raw flue gas before heat exchange measured by the second flue gas temperature detection device T2 is T2, and the flow rate of the medium measured by the medium flow rate detection device Q2 is QMediumThe temperature of the medium before heat exchange measured by the first medium temperature detection device T3 is T3, and the temperature of the medium after heat exchange measured by the second medium temperature detection device T4 is T4; the total heat exchange quantity of the flue gas cooling heat exchanger 3 is QGeneral assemblySatisfying the following formula (1):
Qgeneral assembly＝qFlue gasρ1CCigarette with heating means(t2-t1)＝qMediumρ2CCold(t4-t3) (1)；
Obtaining formula (2) according to formula (1)
Where ρ is1Is the average density of the flue gas, p2Is the average density of the medium, CCigarette with heating meansIs the average specific heat capacity of the flue gas, CColdIs the average specific heat capacity of the medium.
Example 8
Example 7 was repeated except that the carbon monoxide treatment apparatus 4 was a reaction apparatus for converting carbon monoxide into carbon dioxide.
Example 9
Example 8 was repeated except that the system further included an oxygen-containing gas delivery pipe L5, an oxygen-containing gas delivery pipe L5 was connected to the oxygen-containing gas replenishment inlet of the carbon monoxide processing apparatus 4, and an oxygen-containing gas delivery pipe L5 was replenished with the oxygen-containing gas into the carbon monoxide processing apparatus 4.
Example 10
Example 9 is repeated except that the system further comprises a fuel supply line L6, the fuel supply line L6 being connected to a fuel replenishment inlet of the carbon monoxide processing apparatus 4, and the fuel supply line L6 replenishing the carbon monoxide processing apparatus 4 with fuel.
Example 11
Example 9 is repeated except that the system further comprises a fuel delivery line L6, the fuel delivery line L6 being connected to the first line L1 upstream of the carbon monoxide treatment unit 4, the fuel delivery line L6 replenishing the first line L1 upstream of the carbon monoxide treatment unit 4 with fuel.
Example 12
Example 11 was repeated except that the oxygen-containing gas was used as the temperature reducing medium and the oxygen-containing gas was delivered via a third conduit L3 to the medium heat transfer zone 302 of the flue gas temperature reducing heat exchanger 3; then, the gas is sent from the outlet of the medium heat exchange zone 302 to the carbon monoxide treatment apparatus 4 through a fourth line L4 and an oxygen-containing gas line L5 in this order.
Example 13
Example 12 is repeated except that the system further comprises: a temperature-rising heat exchanger 7; the temperature-raising heat exchanger 7 is disposed on the first pipeline L1, and the temperature-raising heat exchanger 7 is located upstream of the carbon monoxide treatment device 4; the temperature-raising heat exchanger 7 is used for adjusting the temperature of the flue gas upstream of the carbon monoxide treatment device 4.
Example 14
Example 12 is repeated except that the system further comprises: a temperature-rising heat exchanger 7; the temperature-raising heat exchanger 7 is disposed on the first pipeline L1, and the temperature-raising heat exchanger 7 is located upstream of the carbon monoxide treatment device 4; the temperature-raising heat exchanger 7 is used for adjusting the temperature of the flue gas upstream of the carbon monoxide treatment device 4.
Example 15
Example 14 is repeated except that the system further comprises: a waste heat recovery heat exchanger 8; the waste heat recovery heat exchanger 8 is arranged on the second pipeline L2; the temperature-rising heat exchanger 7 and the waste heat recovery heat exchanger 8 are respectively and independently indirect heat exchange devices, preferably shell-and-tube heat exchange devices, and more preferably DDH heat exchangers.
Example 16
Example 15 was repeated except that the medium outlet of the temperature-increasing heat exchanger 7 was connected to the medium inlet of the waste heat recovery heat exchanger 8 via the first medium conveyance conduit L7, and the medium outlet of the waste heat recovery heat exchanger 8 was connected to the medium inlet of the temperature-increasing heat exchanger 7 via the second medium conveyance conduit L8.
Example 17
Example 16 was repeated except that the desulfurization tower 1 was a dry desulfurization system. The denitration tower 2 is an SCR denitration system or an SNCR denitration system.
Claims (15)
1. The utility model provides an energy-saving flue gas high efficiency of multiple pollutants is administered system in coordination which characterized in that: the system comprises a desulfurizing tower (1), a denitration tower (2), a flue gas cooling heat exchanger (3) and a carbon monoxide treatment device (4); the original flue gas pipeline (L0) is communicated with the gas inlet of the desulfurizing tower (1); the gas outlet of the desulfurizing tower (1) is communicated with the gas inlet of the denitrifying tower (2) through a first pipeline (L1); the gas outlet of the denitration tower (2) is communicated with a second pipeline (L2); the flue gas cooling heat exchanger (3) is arranged on the original flue gas pipeline (L0); the carbon monoxide treatment device (4) is provided on the first line (L1).
2. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 1, wherein: the flue gas cooling heat exchanger (3) comprises: a flue gas heat exchange area (301) and a medium heat exchange area (302); the smoke heat exchange area (301) and the medium heat exchange area (302) are mutually attached; the original flue gas pipeline (L0) is communicated with the desulfurizing tower (1) after passing through the flue gas heat exchange area (301); the feed inlet of the medium heat exchange zone (302) is communicated with the low-temperature medium through a third pipeline (L3); the discharge hole of the medium heat exchange area (302) is communicated with a fourth pipeline (L4).
3. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 2, wherein: the feed inlet of the medium heat exchange zone (302) is communicated with the low-temperature medium through a third pipeline (L3). concretely, the system also comprises: a blower (5); an exhaust outlet and a third pipeline (L3) of the blower (5) are connected to a feed inlet of the medium heat exchange area (302); the air inlet of the blower (5) is communicated with the atmosphere; and/or
The system further comprises: a water pump (6); the water outlet of the water pump (6) is connected to the feed inlet of the medium heat exchange area (302) through a third pipeline (L3); the water inlet of the water pump (6) is communicated with a low-temperature water source.
4. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 3, wherein: the system also comprises a first flue gas temperature detection device (T1), wherein the first flue gas temperature detection device (T1) is arranged on the original flue gas pipeline (L0) and is positioned at the downstream of the flue gas cooling heat exchanger (3).
5. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 4, wherein: the system also comprises a smoke flow detection device (Q1), a second smoke temperature detection device (T2), a medium flow detection device (Q2), a first medium temperature detection device (T3) and a second medium temperature detection device (T4); the flue gas flow detection device (Q1) and the second flue gas temperature detection device (T2) are arranged on the original flue gas pipeline (L0), and the second flue gas temperature detection device (T2) is positioned at the upstream of the flue gas cooling heat exchanger (3); the smoke flow detection device (Q1) is positioned at the upstream or the downstream of the smoke cooling heat exchanger (3); the medium flow rate detection device (Q2) is arranged on the third pipeline (L3) or the fourth pipeline (L4), the first medium temperature detection device (T3) is arranged on the third pipeline (L3), and the second medium temperature detection device (T4) is arranged on the fourth pipeline (L4).
6. The energy-saving flue gas multi-pollutant high-efficiency cooperative treatment system according to any one of claims 1 to 5, characterized in that: the carbon monoxide treatment device (4) is a reaction device for converting carbon monoxide into carbon dioxide.
7. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 6, wherein: the system further includes an oxygen-containing gas delivery pipe (L5), the oxygen-containing gas delivery pipe (L5) being connected to an oxygen-containing gas supplement inlet of the carbon monoxide processing apparatus (4), the oxygen-containing gas delivery pipe (L5) supplementing the oxygen-containing gas into the carbon monoxide processing apparatus (4); and/or
The system further comprises a fuel transfer line (L6), the fuel transfer line (L6) being connected to a fuel replenishment inlet of the carbon monoxide processing unit (4) or to a first line (L1) upstream of the carbon monoxide processing unit (4), the fuel transfer line (L6) replenishing fuel into the carbon monoxide processing unit (4) or to the first line (L1) upstream of the carbon monoxide processing unit (4).
8. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 7, wherein: the oxygen-containing gas is used as a temperature reduction medium and is conveyed to a medium heat exchange area (302) of the flue gas temperature reduction heat exchanger (3) through a third pipeline (L3); then, the gas is conveyed from the outlet of the medium heat exchange zone (302) to the carbon monoxide treatment device (4) through a fourth pipeline (L4) and an oxygen-containing gas conveying pipeline (L5) in sequence.
9. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 6, wherein: the system further comprises: a temperature-raising heat exchanger (7); the temperature-raising heat exchanger (7) is arranged on the first pipeline (L1), and the temperature-raising heat exchanger (7) is positioned at the upstream or the downstream of the carbon monoxide treatment device (4); the temperature-rising heat exchanger (7) is used for adjusting the temperature of the flue gas at the upstream or the downstream of the carbon monoxide treatment device (4).
10. The energy-saving flue gas multi-pollutant high-efficiency cooperative treatment system according to claim 7 or 8, characterized in that: the system further comprises: a temperature-raising heat exchanger (7); the temperature-raising heat exchanger (7) is arranged on the first pipeline (L1), and the temperature-raising heat exchanger (7) is positioned at the upstream or the downstream of the carbon monoxide treatment device (4); the temperature-rising heat exchanger (7) is used for adjusting the temperature of the flue gas at the upstream or the downstream of the carbon monoxide treatment device (4).
11. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 9, wherein: the system further comprises: a waste heat recovery heat exchanger (8); the waste heat recovery heat exchanger (8) is arranged on the second pipeline (L2); the temperature-rising heat exchanger (7) and the waste heat recovery heat exchanger (8) are respectively independent indirect heat exchange devices.
12. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 10, wherein: the system further comprises: a waste heat recovery heat exchanger (8); the waste heat recovery heat exchanger (8) is arranged on the second pipeline (L2); the temperature-rising heat exchanger (7) and the waste heat recovery heat exchanger (8) are respectively independent indirect heat exchange devices.
13. The energy-saving flue gas multi-pollutant high-efficiency cooperative treatment system according to claim 11 or 12, characterized in that: the temperature-rising heat exchanger (7) and the waste heat recovery heat exchanger (8) are respectively and independently shell-and-tube heat exchange devices.
14. The energy-saving efficient synergistic treatment system for multiple pollutants in flue gas as claimed in claim 13, wherein: the temperature-rising heat exchanger (7) and the waste heat recovery heat exchanger (8) are respectively independent DDH heat exchangers.
15. The energy-saving flue gas multi-pollutant high-efficiency cooperative treatment system according to claim 11 or 12, characterized in that: the medium outlet of the warming heat exchanger (7) is connected with the medium inlet of the waste heat recovery heat exchanger (8) through a first medium conveying pipeline (L7), and the medium outlet of the waste heat recovery heat exchanger (8) is connected with the medium inlet of the warming heat exchanger (7) through a second medium conveying pipeline (L8).
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| CN112815730A (en) * | 2021-02-10 | 2021-05-18 | 秦皇岛新特科技有限公司 | Sintering flue gas treatment equipment |
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