WO2023284636A1 - 一种危废焚烧烟气净化系统及净化方法 - Google Patents
一种危废焚烧烟气净化系统及净化方法 Download PDFInfo
- Publication number
- WO2023284636A1 WO2023284636A1 PCT/CN2022/104526 CN2022104526W WO2023284636A1 WO 2023284636 A1 WO2023284636 A1 WO 2023284636A1 CN 2022104526 W CN2022104526 W CN 2022104526W WO 2023284636 A1 WO2023284636 A1 WO 2023284636A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- flue gas
- deacidification
- reaction tower
- hazardous waste
- inlet pipe
- Prior art date
Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 172
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 171
- 239000002920 hazardous waste Substances 0.000 title claims abstract description 61
- 238000000746 purification Methods 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 55
- 238000004056 waste incineration Methods 0.000 title claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 59
- 238000001816 cooling Methods 0.000 claims abstract description 49
- 239000000126 substance Substances 0.000 claims abstract description 47
- 239000007789 gas Substances 0.000 claims abstract description 45
- 230000008878 coupling Effects 0.000 claims abstract description 34
- 238000010168 coupling process Methods 0.000 claims abstract description 34
- 238000005859 coupling reaction Methods 0.000 claims abstract description 34
- 238000010791 quenching Methods 0.000 claims abstract description 28
- 230000000171 quenching effect Effects 0.000 claims abstract description 25
- 239000007788 liquid Substances 0.000 claims description 59
- 239000000428 dust Substances 0.000 claims description 46
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 36
- 239000007921 spray Substances 0.000 claims description 29
- 239000002918 waste heat Substances 0.000 claims description 20
- 238000001179 sorption measurement Methods 0.000 claims description 13
- 150000002013 dioxins Chemical class 0.000 claims description 9
- 239000013618 particulate matter Substances 0.000 claims description 7
- 229910001385 heavy metal Inorganic materials 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 5
- 230000002378 acidificating effect Effects 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 32
- 239000002351 wastewater Substances 0.000 abstract description 17
- 238000005507 spraying Methods 0.000 abstract description 13
- 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 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 58
- 235000011121 sodium hydroxide Nutrition 0.000 description 25
- 239000002253 acid Substances 0.000 description 23
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 239000000498 cooling water Substances 0.000 description 10
- 150000003839 salts Chemical class 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 239000003795 chemical substances by application Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- 239000002699 waste material Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 229940079593 drug Drugs 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000012806 monitoring device Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000009418 renovation Methods 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010835 comparative analysis Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007728 cost analysis Methods 0.000 description 1
- -1 etc. Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
Definitions
- the invention relates to the technical field of hazardous waste incineration flue gas purification, in particular to a hazardous waste incineration flue gas purification system and purification method.
- Hazardous waste refers to "waste with hazardous characteristics that is included in the national list of hazardous waste or identified in accordance with the national hazardous waste identification standards and identification methods.” Different hazardous wastes are disposed of in incineration, landfill, materialization, comprehensive utilization and other disposal methods according to their characteristics.
- Two-stage wet deacidification needs to use a large amount of deacidification agents such as slaked lime and liquid caustic soda, and the production cost is high;
- One of the objectives of the present invention is to provide a hazardous waste incineration flue gas purification system and purification method to solve the bottleneck problems of the existing hazardous waste disposal industry flue gas purification technology that has a cumbersome process and produces a large amount of difficult-to-treat high-salt wastewater , It can also solve the purification efficiency problem of the flue gas purification method in the existing hazardous waste treatment industry.
- a high-efficiency quenching and deacidification coupling equipment for hazardous waste incineration flue gas including a reaction tower;
- a spraying device is installed on the top of the reaction tower, and the inlet end of the spraying device is connected with a first liquid inlet pipe and a second liquid inlet pipe, which are respectively used to transport cooling substances and deacidifying substances;
- the reaction tower is also provided with an air inlet pipe and an air outlet pipe;
- the bottom end of the reaction tower is also provided with an output pipeline for outputting the substances generated in the reaction tower;
- the cooling substance and deacidification substance in the first liquid inlet pipe and the second liquid inlet pipe are mixed with the flue gas through the spray device, and the purpose of rapid cooling and deacidification is realized at the same time.
- the spray device is a rotary spray device.
- the present invention also provides a hazardous waste incineration flue gas purification system, including the hazardous waste incineration flue gas high-efficiency rapid cooling and deacidification coupling device described in the present invention.
- it also includes an incineration device and a waste heat boiler connected in sequence, and the gas outlet end of the waste heat boiler is connected with the air inlet end of the air inlet pipe of the reaction tower.
- the bag dust removal device also includes a bag dust removal device and a flue gas discharge device connected in sequence, the inlet end of the bag dust removal device is connected with the gas outlet end of the gas outlet pipe of the reaction tower.
- it also includes a lye preparation and storage device, the liquid outlet of which is connected to the liquid inlet of the second liquid inlet pipe;
- an activated carbon adsorption device is also provided between the outlet pipe of the reaction tower and the bag dust removal device;
- the air inlet end of the activated carbon adsorption device is connected with the air outlet end of the air outlet pipe, and the air outlet end is connected with the air inlet end of the bag dust removal device.
- the waste heat boiler is also equipped with an SNCR denitrification device.
- the feed port end is connected to the outlet end of the output pipe of the reaction tower
- the exhaust port is connected to the inlet end of the first liquid inlet pipe of the reaction tower
- the discharge port The end is connected to a collection device.
- the present invention also provides a purification method for the hazardous waste incineration flue gas purification system, comprising the following steps:
- the flue gas before being treated by the bag dust removal device also passes through an activated carbon adsorption device to remove dioxins and heavy metals in the flue gas, and the lye preparation and storage device is a high-efficiency rapid cooling and deacidification coupling equipment to transport lye;
- the high-efficiency quenching and deacidification coupling equipment is also connected with a dust collection device.
- the high-efficiency quenching and deacidification coupling equipment for hazardous waste incineration flue gas provided by the present invention, by setting the first liquid inlet pipe and the second liquid inlet pipe in the reaction tower, the first liquid inlet pipe is used to transport cooling substances, and the second liquid inlet pipe
- the pipe is used to transport the deacidification substances such as lye, and the cooling substance and the deacidification substance are fully mixed with the flue gas through the spray device, so as to realize the purpose of rapid cooling and deacidification of the flue gas at the same time, prevent the resynthesis of dioxin and simultaneously Realize the removal of acid gas, simplify the process flow of flue gas purification, and the solid salt generated is directly discharged through the output pipe at the bottom, thus avoiding the generation of a large amount of high-salt wastewater, and solving the cumbersome process of the existing flue gas purification technology , and the bottleneck problem of producing a large amount of difficult-to-treat high-salt wastewater;
- the hazardous waste incineration flue gas purification system realizes the heat recovery in the flue gas by connecting the waste heat boiler behind the incineration device, and the heat generated can be used by the production line and other users in the factory area, increasing the heat of the flue gas The utilization rate of flue gas is avoided, and the heat loss of flue gas is avoided;
- the method for purifying hazardous waste incineration flue gas uses high-efficiency rapid cooling and deacidification coupling equipment to efficiently remove acid gases in flue gas, and solves the problem of wet wastewater treatment, thus changing the existing wet treatment as the main body
- the treatment mode has the value of popularization and application in the field of hazardous waste flue gas purification technology.
- Fig. 1 is a structural schematic diagram of the high-efficiency quenching and deacidification coupling equipment for hazardous waste incineration flue gas of the present invention
- Fig. 2 is a schematic structural view of the hazardous waste incineration flue gas purification system of the present invention
- Fig. 3 is the process flow diagram of the hazardous waste incineration flue gas purification method of the present invention.
- Fig. 4 is an automatic control flow chart of the hazardous waste purification process of the present invention.
- 1-reaction tower 101-intake pipe, 102-outlet pipe, 103-output pipe; 2-spray device, 201-first liquid inlet pipe, 202-second liquid inlet pipe; 3-incineration device; 4- Waste heat boiler; 5-bag dust removal device; 6-flue gas discharge device; 7-lye preparation and storage device; 8-activated carbon adsorption device; 9-SNCR denitrification device; 10-dust collection device; 11-collection device; 12-tap water Tube.
- a spray device 2 is installed on the top of the reaction tower 1, and the inlet end of the spray device 2 is connected with a first liquid inlet pipe 201 and a second liquid inlet pipe 202, which are respectively used to transport cooling substances and deacidification substances;
- the reaction tower 1 is also provided with an inlet pipe 101 and an outlet pipe 102;
- the bottom end of the reaction tower 1 is also provided with an output pipeline 103 for exporting the substances generated in the reaction tower 1;
- the spray device 2 After the flue gas inlet pipe 101 enters the reaction tower 1, the spray device 2 fully mixes the cooling substance and the deacidification substance in the first liquid inlet pipe 201 and the second liquid inlet pipe 202 with the flue gas, so as to realize simultaneous rapid cooling and deacidification Purpose.
- the first liquid inlet pipe and the second liquid inlet pipe By setting the first liquid inlet pipe and the second liquid inlet pipe in the reaction tower, the first liquid inlet pipe is used to transport the cooling substance, the second liquid inlet pipe is used to convey the deacidification substances such as lye, and the cooling substance and the The deacidification substance is fully mixed with the flue gas, thereby achieving the purpose of simultaneously rapidly cooling the flue gas to inhibit the formation of dioxins and deacidification, preventing the resynthesis of dioxins and achieving effective removal of acid gases, simplifying the process of flue gas purification Process flow, the generated solid salt is directly discharged through the output pipe at the bottom, thereby avoiding the generation of a large amount of high-salt wastewater, and solving the cumbersome process of the existing flue gas purification technology in the hazardous waste disposal industry, as well as the generation of a large amount of high-salt waste that is difficult to handle. Bottleneck problem of saline wastewater.
- the cooling material can be cooling water, etc., and any material that can be used to reduce the temperature of the flue gas can be used.
- the spray device has a liquid outlet nozzle, that is, the cooling water and lye enter the spray device through different liquid inlet pipes, spray from the same liquid outlet, and then mix with the flue gas to achieve simultaneous cooling and deacidification.
- the spray device adopts two liquid outlets, that is, after the cooling water enters from the first liquid inlet pipe, it is sprayed out from one liquid outlet of the spray device to cool down the flue gas, and the lye is discharged from the first liquid outlet. After the second liquid inlet pipe enters, it is sprayed from another liquid outlet of the spray device to deacidify the flue gas.
- the spray device 101 is a rotary spray device.
- the rotary spraying device is a rotary spraying device, that is, a rotary spraying device used in the SDA desulfurization process in the low-temperature flue gas desulfurization process of a steel plant.
- the rotation speed of the rotary spray equipment is above 10000r/min, and the droplet diameter is less than or equal to 50 ⁇ m.
- the inner diameter of the rotary spray equipment can be adjusted according to the actual amount of flue gas to be treated.
- the concentration of SO in the outlet flue gas after being treated by the high-efficiency quenching deacidification coupling equipment for hazardous waste incineration flue gas in this embodiment can be Reduced to below 20mg/Nm 3 , the removal efficiency can reach over 99%.
- the liquid inlet of the first liquid inlet pipe is connected with the tap water pipe 12 .
- the spray device used can also treat difficult-to-treat wastewater such as leachate because of its high-efficiency rotating spray flux, large flux, and not easy to clog.
- this embodiment provides a hazardous waste incineration flue gas purification system, including the high-efficiency quenching and deacidification coupling equipment for hazardous waste incineration flue gas in Embodiment 1.
- It also includes an incineration device 3 and a waste heat boiler 4 connected in sequence, and the gas outlet end of the waste heat boiler 4 is connected with the air inlet end of the air inlet pipe 101 of the reaction tower 1 .
- the heat in the flue gas can be recovered, and the heat generated can be used by the production line and other users in the factory area, which improves the utilization rate of flue gas heat and avoids the loss of flue gas heat.
- It also includes a bag dust removal device 5 and a flue gas discharge device 6 connected in sequence, and the air inlet end of the bag dust removal device 5 is connected with the gas outlet end of the gas outlet pipe 102 of the reaction tower 1 .
- lye preparation storage device 7 its liquid outlet is connected with the liquid inlet of the second liquid inlet pipe 202;
- An activated carbon adsorption device 8 is also provided between the outlet pipe 102 of the reaction tower 1 and the bag dust removal device 5;
- the air inlet end of activated carbon adsorption device 8 links to each other with the air outlet end of air outlet pipe 102, and the air outlet end links to each other with the air inlet end of bag dust removal device 5.
- An activated carbon adsorption device is installed between the outlet pipe of the reaction tower and the bag dust removal device to remove dioxins, heavy metals and other substances that can be adsorbed by activated carbon in the flue gas.
- the waste heat boiler 4 is also equipped with an SNCR denitrification device 9;
- dedusting device 10 its feed port end links to each other with the outlet end of the output pipe 103 of reaction tower 1, the exhaust port end links to each other with the inlet end of the first liquid inlet pipe 201 of reaction tower 1, and the discharge port end is connected with Collection device 11.
- the purification method for treating the incineration flue gas of hazardous waste is mainly SO 2 , Its purification method comprises the following steps:
- a hazardous waste is incinerated in the incineration device to produce high-temperature flue gas.
- the concentration of acid gas in the high-temperature flue gas is measured by the monitoring device, and the temperature of the flue gas is between 1100°C and 1200°C.
- the acid gas mainly includes SO 2 , HCl, HF and other acid gases;
- the temperature of the flue gas is about 550°C after being cooled and denitrated by the waste heat boiler, and it is transported from the waste heat boiler to the intake pipe of the high-efficiency rapid cooling and deacidification coupling equipment, and the acidic substances in the flue gas are cooled and removed at the same time.
- the content of acid gas in high-temperature flue gas, in the high-efficiency quenching and deacidification coupling equipment, the rotation speed of the rotary spraying equipment is set to 10000r/min, the cooling water is connected to the first liquid inlet pipe, and the inlet flow rate of the cooling water is about 3.05t/ h, the sodium hydroxide solution is connected to the second liquid inlet pipe, the concentration of the sodium hydroxide solution is about 30%, the liquid inlet flow rate is about 2m 3 /h, after the high-temperature flue gas passes through the reaction tower for rapid cooling and cooling, within 2s from
- the detected acid gas concentration in the flue gas of the outlet pipe is below 20mg/Nm 3 , and the flue gas temperature is about 200°C.
- the acid gas and sodium hydroxide are efficiently contacted and reacted to form fixed salts.
- the solid salts precipitate and pass through the bottom of the The output pipe is discharged, the cooling water enters the reaction tower, and under the high-efficiency rotation of the rotary spray equipment, the flue gas is cooled extremely rapidly;
- the flue gas that has been cooled and deacidified by the high-efficiency rapid cooling and deacidification coupling equipment is transported to the activated carbon adsorption device to absorb dioxins and heavy metals in the flue gas, and then the flue gas is transported to the bag filter for dust removal in the bag
- the temperature of the flue gas is 185 ° C ⁇ 195 ° C, remove the dust and particulate matter in the flue gas, and then pass through the monitoring device again to determine that the acid gas content in the flue gas reaches the standard, and then discharge it from the flue gas discharge device;
- the rotary spraying equipment rotates at high speed to make the lye and cooling water form droplets with a diameter of ⁇ 50 ⁇ m, which can achieve high mass transfer when in contact with the flue gas, and the total evaporation area of the droplets is large , the evaporation time is short, and the transition from liquid phase to gas phase or solid phase is realized in the reaction tower, so as to achieve the purpose of not generating waste liquid, which not only fully meets the environmental protection requirements, but also avoids the generation of high-salt wastewater.
- the flue gas purification process in this embodiment the removal effect of SO can reach 99%, and the waste S content limit is 4%;
- the flue gas purification process in this example the hazardous waste industry has not yet adopted this method as the main treatment process, and it is an innovative process;
- the flue gas purification process in this example 1 Increase the removal effect of SNCR denitration enhancement on NOx compounds; 2 Increase the high-efficiency rapid cooling and deacidification coupling equipment with SDA as the main body (also with dry alkaline powder circulating fluidization system) , realized the rapid cooling function and deacidification function at the same time, and the deacidification efficiency reached more than 99%; 3 Increase the area of the bag filter to ensure the removal of particulate matter;
- two-stage wet tower is added to the back end of the bag filter.
- the waste water generated by the wet tower is difficult to treat, and the second is to spray back to the quench tower for evaporation treatment, and the quench tower is enlarged. the blocking frequency;
- the flue gas purification process in this embodiment the rotary spraying equipment in the high-efficiency quenching and deacidification coupling equipment, during the rotary spraying process, the contact area between the lye and the flue gas is large, the mass transfer rate is fast, and the purification effect is good;
- the flue gas purification process in this embodiment the initial SO2 concentration: 3361mg / m3 , the removal rate of the high - efficiency quenching deacidification coupling equipment is 99%, and the SO2 concentration at the inlet end of the flue gas discharge device is 20mg/ m3 ;
- the flue gas purification process in this embodiment use urea as the reducing agent, the dosage is 2kg/h, and the cost is about 72 yuan/d; use powdered activated carbon as the adsorbent, the dosage is 10kg/h, the cost is about 960 yuan/d; use NaOH is used as a deacidification agent, the dosage is 122kg/h, and the chemical cost is about 5856 yuan/d; the total cost of adding chemicals per ton of hazardous waste is: 137.67 yuan/ton;
- the flue gas purification process in this example the output of fly ash is 230.61kg/h (5.45t/d), calculated according to the landfill cost (about 4000 yuan/t) and divided into a single ton of hazardous waste: 436 yuan/ton ;
- the output of fly ash is 243.34kg/h (5.84t/d), and the cost of landfill (about 4,000 yuan/t) and equalized to a single ton of hazardous waste is calculated: 467.2 yuan/ton;
- the flue gas purification process in this embodiment the high-efficiency rapid cooling and deacidification coupling equipment can process 50t/d of leachate, saving 4,000 yuan/d;
- the flue gas purification process in this embodiment is about 13 million yuan, including: high-efficiency quenching deacidification coupling equipment (about 6 million yuan), bag filter system (about 2.4 million yuan), wet deacidification tower system ( About 1.5 million yuan), flue gas heater (about 320,000 yuan), induced draft fan (about 340,000 yuan), supporting renovation facilities (about 1.5 million yuan) and installation project (about 1 million yuan);
- the total investment is about 12 million yuan, including: quenching tower system (about 2 million yuan), bag filter system (about 2.4 million yuan), circulating fluidized bed system (about 2 million yuan), two-stage Wet deacidification tower system (about 2.4 million yuan), flue gas heater (about 320,000 yuan), induced draft fan (about 340,000 yuan), supporting renovation facilities (about 1.6 million yuan) and installation project (about 1 million yuan) .
- quenching tower system about 2 million yuan
- bag filter system about 2.4 million yuan
- circulating fluidized bed system about 2 million yuan
- two-stage Wet deacidification tower system about 2.4 million yuan
- flue gas heater about 320,000 yuan
- induced draft fan about 340,000 yuan
- supporting renovation facilities about 1.6 million yuan
- installation project about 1 million yuan
- an instrument 1 is installed at the inlet end of the flue gas discharge device, and the sulfur dioxide content in the flue gas is monitored and automatically controlled by the instrument 1.
- the flow chart of the automatic control As shown in Figure 4.
- the dosage of lye Q 2.93 tons/day, as a theoretical value, when the meter 1 monitors that the acid gas content is below 80mg/L (the national emission standard), the lye is automatically controlled The dosage of lye is maintained between 1 and 1.1 times of the theoretical dosage; when the meter 1 detects that the content of acid gas is greater than 80mg/L (the discharge standard stipulated by the state), the dosage of lye is automatically controlled to increase amount, so that the actual dosage is between Q and 2Q, until the acid gas content monitored in instrument 1 is less than 80mg/L, gradually reduce the dosage of lye in the high-efficiency quenching deacidification coupling equipment through automatic control .
- the high-efficiency quenching and deacidification coupling equipment for hazardous waste incineration flue gas provided by the present invention, firstly, by setting the first liquid inlet pipe and the second liquid inlet pipe in the reaction tower, the first liquid inlet pipe is used to transport cooling substances , the second liquid inlet pipe is used to transport lye and other deacidification substances, and the cooling substance and deacidification substances are fully mixed with the flue gas through the spray device, so as to realize the simultaneous rapid cooling and cooling of the flue gas to inhibit the generation of dioxin and deacidification
- the purpose is to prevent the resynthesis of dioxins and realize the effective removal of acid gases, simplify the process flow of the existing flue gas purification technology, and the solid salt generated is directly discharged through the output pipe at the bottom, thereby avoiding a large amount of high-salt wastewater. It solves the cumbersome process flow of the existing flue gas treatment system and the bottleneck problem of producing a large amount of difficult-to-treat high-salt wastewater;
- the rotary spraying equipment rotates at high speed to make the lye and cooling water form droplets with a diameter of ⁇ 50 ⁇ m, which can achieve high mass transfer when in contact with the flue gas, and the total evaporation of the droplets
- the area is large, the evaporation time is short, and the transformation from liquid phase to gas phase or solid phase is realized in the reaction tower, so as to achieve the purpose of not generating waste liquid, which not only fully meets the environmental protection requirements, but also avoids the generation of high-salt wastewater.
- the flue gas purification system for hazardous waste incineration provided by the present invention, firstly, recovers the heat in the flue gas by connecting the waste heat boiler behind the incineration device, and the heat generated can be used by the production line and other users in the factory area, improving the efficiency of the flue gas.
- the utilization rate of the gas heat avoids the heat loss of the flue gas; secondly, by setting the bag dust removal device at the outlet end of the gas outlet pipe of the reaction tower, the dust and particulate matter in the flue gas are further removed, and the dust in the flue gas is avoided.
- an activated carbon adsorption device is installed between the outlet pipe of the reaction tower and the bag dust removal device to remove dioxins, heavy metals and other substances that can be adsorbed by activated carbon in the flue gas; finally, through the installation of dust Collection device. After the dust generated in the reaction tower passes through the dust collection device, the precipitated material is directly collected by the collection device.
- the gas after dust removal contains part of the alkaline powder, which can be returned to the reaction tower for repeated recycling, realizing internal cycle.
- the method for purifying flue gas from hazardous waste incineration uses high-efficiency rapid cooling and deacidification coupling equipment to efficiently remove acid gas in flue gas, solves the problem of wet wastewater treatment, and thus changes the existing wet treatment as the main treatment
- the model has the value of popularization and application in the field of hazardous waste flue gas purification technology.
Abstract
本发明提供了一种危废焚烧烟气净化系统及净化方法，涉及危废焚烧烟气净化技术领域。危废焚烧烟气高效急冷脱酸耦合设备包括反应塔；反应塔顶端设有喷雾装置，喷雾装置进口端设有第一进液管和第二进液管，用于输送冷却物质和脱酸物质；反应塔上设有进气管和出气管；反应塔底端设有输出管道，用于输出反应塔内生成的物质；烟气通过进气管进入反应塔后，通过喷雾装置使第一进液管和第二进液管中的冷却物质和脱酸物质与烟气混合，实现同时急冷降温抑制二噁英生成和脱酸的目的。本发明的净化系统包括高效急冷脱酸耦合设备。本发明解决了现有危废处置行业烟气净化技术存在工艺流程繁琐，以及产生大量难以处理的高盐废水的瓶颈问题。
Description
本发明涉及危废焚烧烟气净化技术领域，具体涉及一种危废焚烧烟气净化系统及净化方法。
危险废物是指“列入国家危险废物名录或者根据国家规定的危险废物鉴别标准和鉴别方法认定的具有危险特性的废物”。不同的危险废物根据其特性相应采取焚烧、填埋、物化、综合利用等处置方式。
近几年，随着危险废物处理处置的力度加大，危险废物的焚烧量剧增，其烟气治理的关键在于去除烟气中的SO
2、HCl、HF等酸性气体，尤其是包含的SO
2。目前，以两级湿法脱酸为核心的烟气净化工艺，能够实现酸性气体的有效去除，达到达标排放的目的，但是两级湿法脱酸后产生大量高盐废水，且对设备造成腐蚀，其处理流程存在的缺点如下：
1)两级湿法脱酸需使用大量的消石灰、液碱等多种脱酸剂，生产成本高；
2)两级湿法脱酸会产生大量的高盐废水，目前对高盐废水还没有很好的处理方法，污水处理难度大，处置成本高；
3)工艺流程较长，增加烟气流动阻力，对于烟气排放指标的控制严重滞后。
因此亟需研发一种危险废物焚烧烟气净化系统，在简化现有传统烟气净化流程的同时，避免产生高盐废水，而形成二次污染，并降低对设备造成的腐蚀，降低危险废物的处置成本，同时能够实现脱酸剂的循环使用，达到节能环保的目的。
发明内容
本发明的目的之一在于提供一种危废焚烧烟气净化系统及净化方法，以解决现有危废处置行业烟气净化技术存在工艺流程繁琐，以及产生大量难以处理的高盐废水的瓶颈问题，还可以解决现有危废处理行业的烟气净化方法的净化效率问题。
为了实现上述目的，本发明采用的技术方案如下：
一种危废焚烧烟气高效急冷脱酸耦合设备，包括反应塔；
所述反应塔的顶端安装有喷雾装置，喷雾装置的进口端连接有第一进液管和第二进液管，分别用于输送冷却物质和脱酸物质；
所述反应塔上还设有进气管和出气管；
所述反应塔的底端还设有输出管道，用于输出反应塔内生成的物质；
烟气通过进气管进入反应塔后，通过喷雾装置使第一进液管和第二进液管中的冷却物质和脱酸物质与烟气混合，同时实现急冷降温和脱酸的目的。
优选的，喷雾装置为旋转喷雾装置。
本发明还提供了一种危废焚烧烟气净化系统，包括本发明所述的危废焚烧烟气高效急冷脱酸耦合设备。
优选的，还包括依次连接的焚烧装置和余热锅炉，余热锅炉的出气口端与所述反应塔的进气管的进气口端相连。
优选的，还包括依次连接的布袋除尘装置和烟气排放装置，所述布袋除尘装置的进气口端与所述反应塔的出气管的出气口端相连。
优选的，还包括碱液制备储存装置，其出液口与第二进液管的进液口相连；
优选的，所述反应塔的出气管与所述布袋除尘装置之间还设有活性炭吸附装置；
活性炭吸附装置的进气口端与出气管的出气口端相连，出气口端与布袋除尘装置的进气口端相连。
优选的，所述余热锅炉还内设有SNCR脱硝装置。
优选的，还包括粉尘收集装置，其进料口端与所述反应塔的输出管道的出口端相连、排气口端与所述反应塔的第一进液管的进口端相连、出料口端连接有收集装置。
本发明还提供了所述危废焚烧烟气净化系统的净化方法，包括以下步骤：
1)在焚烧装置中将危险废物进行焚烧处理后产生高温烟气；
2)将高温烟气输送至余热锅炉内，进行SNCR脱硝处理和热量回收；
3)将降温后的烟气从余热锅炉输送至高效急冷脱酸耦合设备的进气管中，同时进行极速降温和去除烟气中的酸性物质；
4)将经过高效急冷脱酸耦合设备处理后的烟气输送至布袋除尘装置中，去除烟气中的粉尘和颗粒物质，然后从烟气排放装置中排出。
优选的，经过布袋除尘装置处理前的烟气还经过活性炭吸附装置，去除烟气中的二噁英和重金属，碱液制备储存装置为高效急冷脱酸耦合设备输送碱液；
高效急冷脱酸耦合设备还连接有粉尘收集装置。
本发明的有益效果：
1)本发明提供的危废焚烧烟气高效急冷脱酸耦合设备，通过在反应塔内设置第一进液管和第二进液管，第一进液管用于输送冷却物质，第二进液管用于输送碱液等脱酸物质，并通过喷雾装置使冷却物质和脱酸物质与烟气充分混合，从而实现了对烟气同时急冷降温 和脱酸的目的，防止二噁英再合成且同时实现酸性气体的去除，简化了烟气净化的工艺流程，生成的固体盐，直接通过底端的输出管道排出，从而避免了大量高盐废水的产生，解决了现有烟气净化技术存在工艺流程繁琐，以及产生大量难以处理的高盐废水的瓶颈问题；
2)本发明提供的危废焚烧烟气净化系统，通过在焚烧装置后连接余热锅炉，实现了烟气中的热量回收，产生的热量可供生产线内部及厂区其他用户使用，提高了烟气热量的利用率，避免了烟气热量损失；
3)通过在反应塔的出气管的出气口端设置布袋除尘装置，进一步去除了烟气中的粉尘和颗粒物质，避免了烟气中的粉尘造成二次污染；
4)通过在反应塔的出气管与布袋除尘装置之间设置活性炭吸附装置，去除烟气中的二噁英、重金属等可被活性炭吸附的物质；
5)通过设置粉尘收集装置，在反应塔中生成的粉尘质经过粉尘收集装置后，沉淀下来的物质直接用收集装置收集，除尘后的气体中含有部分碱性粉末返回反应塔，实现重复循环利用；
6)本发明提供的危废焚烧烟气净化方法，以高效急冷脱酸耦合设备高效脱除烟气中的酸性气体，解决了湿法废水处理的问题，从而改变了现有湿法处理为主体的处理模式，在危废烟气净化技术领域，具有推广应用价值。
图1为本发明的危废焚烧烟气高效急冷脱酸耦合设备的结构示意图；
图2为本发明的危废焚烧烟气净化系统的结构示意图；
图3为本发明的危废焚烧烟气净化方法的工艺流程图；
图4为本发明的危废净化工艺的自动控制流程图。
其中，1-反应塔，101-进气管，102-出气管，103-输出管道；2-喷雾装置，201-第一进液管，202-第二进液管；3-焚烧装置；4-余热锅炉；5-布袋除尘装置；6-烟气排放装置；7-碱液制备储存装置；8-活性炭吸附装置；9-SNCR脱硝装置；10-粉尘收集装置；11-收集装置；12-自来水管。
以下将参照附图和优选实施例来说明本发明的实施方式，本领域技术人员可由本说明书中所揭露的内容轻易地了解本发明的其他优点与功效。本发明还可以通过另外不同的具 体实施方式加以实施或应用，本说明书中的各项细节也可以基于不同观点与应用，在没有背离本发明的精神下进行各种修饰或改变。应当理解，优选实施例仅为了说明本发明，而不是为了限制本发明的保护范围。
需要说明的是，以下实施例中所提供的图示仅以示意方式说明本发明的基本构想，遂图式中仅显示与本发明中有关的组件而非按照实际实施时的组件数目、形状及尺寸绘制，其实际实施时各组件的型态、数量及比例可为一种随意的改变，且其组件布局型态也可能更为复杂。
实施例1
如图1所示，为本实施例中的危废焚烧烟气高效急冷脱酸耦合设备，其包括反应塔1；
反应塔1的顶端安装有喷雾装置2，喷雾装置2的进口端连接有第一进液管201和第二进液管202，分别用于输送冷却物质和脱酸物质；
反应塔1上还设有进气管101和出气管102；
反应塔1的底端还设有输出管道103，用于输出反应塔1内生成的物质；
烟气进气管101进入反应塔1后，喷雾装置2使第一进液管201和第二进液管202中的冷却物质和脱酸物质与烟气充分混合，实现同时急冷降温和脱酸的目的。
通过在反应塔内设置第一进液管和第二进液管，第一进液管用于输送冷却物质，第二进液管用于输送碱液等脱酸物质，并通过喷雾装置使冷却物质和脱酸物质与烟气充分混合，从而实现了对烟气同时急冷降温抑制二噁英生成和脱酸的目的，防止二噁英再合成的同时实现酸性气体的有效去除，简化了烟气净化的工艺流程，生成的固体盐，直接通过底端的输出管道排出，从而避免了大量高盐废水的产生，解决了现有危废处置行业烟气净化技术存在工艺流程繁琐，以及产生大量难以处理的高盐废水的瓶颈问题。
本实施例中，通过喷雾装置将第一进液管中的冷却物质进行加速后，与烟气充分混合，可实现在1s钟内使烟气的温度从550℃降低至200℃以下，从而达到急速降温的目的，其中冷却物质可采用冷却水等，能用于降低烟气温度的物质均可。
其中，喷雾装置具有一个出液管口，即冷却水和碱液分别通过不同的进液管进入喷雾装置后，从同一个出液口喷雾，然后与烟气混合，实现同时降温和脱酸。在实际试验中发现，当喷雾装置采用两个出液口时，即冷却水从第一进液管进入后，从喷雾装置的一个出液口喷出实现对烟气的降温，碱液从第二进液管进入后，从喷雾装置的另一个出液口喷出实现对烟气的脱酸，如此，对烟气的冷却和脱酸之间会形成一个时间差，一部分烟气会先 与冷却水接触后再与碱液接触，另一部分烟气会先与碱液接触后再与冷却水接触，在高温条件下，当烟气先与冷却物质接触降温后，再与碱性溶液进行中和反应时，会使得生成的盐中含水量增加，从而不利于后续处理，而烟气中的酸性气体先与碱性溶液中和生成固体盐后，再与冷却水接触降温时，其接触面积明显减小，从而降低了降温的效率。
喷雾装置101为旋转喷雾装置。
本实施例中，旋转喷雾装置为旋转喷雾设备，即用于钢厂低温烟气脱硫中的SDA脱硫工艺中的旋转喷雾设备。旋转喷雾设备的旋转速度为10000r/min以上，雾滴直径≤50μm，旋转喷雾设备的内径可根据实际需要处理的烟气量进行调整。
本实施例中，烟气中SO
2的进气浓度为3361mg/Nm
3时，经过本实施例中的危废焚烧烟气高效急冷脱酸耦合设备处理后的出口烟气中SO
2的浓度可降低至20mg/Nm
3以下，去除效率可达99％以上。
本实施例中，第一进液管的进液口与自来水管12相连。
本实施例中提供的危废焚烧烟气高效急冷脱酸耦合设备中，采用的喷雾装置，因其具有高效旋转喷雾通量大、不易堵塞的特点，还可处理渗滤液等不易处理的废水。
实施例2
如图2所示，本实施例中提供了危废焚烧烟气净化系统，包括实施例1中的危废焚烧烟气高效急冷脱酸耦合设备。
还包括依次连接的焚烧装置3和余热锅炉4，余热锅炉4的出气口端与反应塔1的进气管101的进气口端相连。
通过在焚烧装置后连接余热锅炉，以实现对烟气中的热量进行回收，产生的热量可供生产线内部及厂区其他用户使用，提高了烟气热量的利用率，避免了烟气热量损失。
还包括依次连接的布袋除尘装置5和烟气排放装置6，布袋除尘装置5的进气口端与反应塔1的出气管102的出气口端相连。
通过在反应塔的出气管的出气口端设置布袋除尘装置，以进一步去除烟气中的粉尘和颗粒物质，避免了烟气中的粉尘造成二次污染。
还包括碱液制备储存装置7，其出液口与第二进液管202的进液口相连；
在现有实际工业烟气处理中发现，烟气的脱酸效率常可达到98％左右，无法实现脱酸效率达99％。
反应塔1的出气管102与布袋除尘装置5之间还设有活性炭吸附装置8；
活性炭吸附装置8的进气口端与出气管102的出气口端相连，出气口端与布袋除尘装 置5的进气口端相连。
通过在反应塔的出气管与布袋除尘装置之间设置活性炭吸附装置，以去除烟气中的二噁英、重金属等可被活性炭吸附的物质。
余热锅炉4还内设有SNCR脱硝装置9；
通过设置SNCR脱硝装置，既实现了去除氮氧化物的目的，又保证了烟气热量的充分回收。
还包括除尘装置10，其进料口端与反应塔1的输出管道103的出口端相连、排气口端与反应塔1的第一进液管201的进口端相连、出料口端连接有收集装置11。
通过设置粉尘收集装置，在反应塔中生成的粉尘质经过粉尘收集装置后，沉淀下来的物质直接用收集装置收集，除尘后的部分碱性粉末，以返回反应塔中进行重复循环利用，实现内循环。
实施例3
如图3所示，本实施例中，通过采用实施例2中的危废焚烧烟气净化系统，对危险废物的焚烧烟气进行处理的净化方法，该烟气中酸性气体主要为SO
2，其净化方法，包括以下步骤：
1)在焚烧装置中将某危险废物进行焚烧处理后产生高温烟气，通过监测装置测定，高温烟气中的酸性气体的浓度为3361mg/m
3，烟气的温度为1100℃～1200℃之间，其中，酸性气体主要包括SO
2、HCl、HF等酸性气体；
2)将高温烟气输送至余热锅炉内，进行SNCR脱硝处理和热量回收；
3)烟气经过余热锅炉降温脱硝后的温度在550℃左右，并从余热锅炉输送至高效急冷脱酸耦合设备的进气管中，同时进行极速降温和去除烟气中的酸性物质，其中，根据高温烟气中酸性气体的含量，高效急冷脱酸耦合设备中，旋转喷雾设备的旋转速度设为10000r/min，第一进液管中连接冷却水，冷却水的进水流量为约3.05t/h，第二进液管中连接氢氧化钠溶液，氢氧化钠溶液的浓度约为30％，进液流量约为2m
3/h，高温烟气经过反应塔进行急冷降温后，在2s内从出气管的烟气中的检测到的酸性气体浓度为20mg/Nm
3以下，烟气温度为200℃左右，酸性气体与氢氧化钠高效接触反应，生成固定盐，固体盐沉淀下来，通过底部的输出管道排出，冷却水进入反应塔内，在旋转喷雾设备的高效旋转下，对烟气进行极速降温；
4)将经过高效急冷脱酸耦合设备进行降温脱酸处理后的烟气输送至活性炭吸附装置中，吸附烟气中的二噁英和重金属，然后将烟气输送至布袋除尘器中，在布袋除尘器中，烟气温度为185℃～195℃，去除烟气中的粉尘和颗粒物质，然后再次经过监测装置测定烟气 中的酸性气体含量达标后，从烟气排放装置中排出；
在高效急冷脱酸耦合设备中，旋转喷雾设备在高速旋转下，使碱液和冷却水形成直径≤50μm的雾滴，与烟气接触能达到高传质的目的，且雾滴总蒸发面积大，蒸发时间短，在反应塔内实现了液相至气相或固相的转变，从而达到不产生废液的目的，既充分满足了环保要求，又避免了高盐废水的产生。
通过将本实施例中的危废焚烧烟气净化工艺与湿法为主体的组合工艺进行对比分析，结果如下：
1)对酸性气体的去除效果(以SO
2处理为例)
本实施例中的烟气净化工艺：对SO
2的去除效果可达99％，废物S含量限值为4％；
湿式为主体的组合工艺：对SO
2的去除效果可达99.42％以上，废物S含量限值为4％；
2)可用性分析
本实施例中的烟气净化工艺：危废行业暂未采用该法作为主体处理工艺，属于创新型工艺；
湿式为主体的组合工艺：现有危废行业主打工艺，通过控制能够稳定实现烟气达标，广泛适用于提标改造及新建项目，但产生大量难以处理的高盐废水，且蒸发系统存在频繁堵塞的问题；
3)工艺过程
本实施例中的烟气净化工艺：①增加了SNCR脱硝强化对NOx化物的去除效果；②增加了SDA为主体的高效急冷脱酸耦合设备(同时兼具干式碱性粉末循环流化系统)，同步实现了急冷功能及脱酸功能，脱酸效率达到99％以上；③增大布袋除尘器面积，保证对颗粒类物质的去除；
湿式为主体的组合工艺：布袋除尘器的后端增加了两级湿法塔，湿法塔产生的废水一是难以处理，二是回喷至急冷塔进行蒸发处理时，又增大了急冷塔的堵塞频率；
4)单位时间的脱酸效果
本实施例中的烟气净化工艺：高效急冷脱酸耦合设备中的旋转喷雾设备，在旋转喷雾过程中，碱液与烟气接触面积大，传质速率快，净化效果好；
湿式为主体的组合工艺：虽然净化效果好，对酸性气体的去除率高，但其产生的的废水处理难度大、费用高；
5)烟气中酸性气体含量相同时，去除率分析(S含量1％，以SO
2分析)
本实施例中的烟气净化工艺：初始SO
2浓度：3361mg/m
3，高效急冷脱酸耦合设备的去 除率为99％，烟气排放装置的进口端SO
2的浓度20mg/m
3；
湿式为主体的组合工艺：初始SO
2浓度：3361mg/m
3，干法去除率30％，两级湿法的去除率99％，烟气排放出口SO
2浓度23.5mg/m
3；
6)药剂投加量及费用分析
本实施例中的烟气净化工艺：使用尿素作为还原剂，用量为2kg/h，费用约72元/d；使用粉末活性炭作为吸附剂，用量为10kg/h，费用约960元/d；使用NaOH作为脱酸剂，用量为122kg/h，药剂费用约5856元/d；合计单吨危废加药费用为：137.67元/吨；
湿式为主体的组合工艺：使用尿素作为还原剂，用量为2kg/h，费用约72元/d；使用粉末活性炭作为吸附剂，用量为10kg/h，费用约960元/d；使用Ca(OH)
2作为干法脱酸剂，用量为61.48kg/h，药剂费用约738元/d；使用小苏打作为干法脱酸剂，用量102.35kg/h，药剂费用约3250元/d；使用NaOH作为湿法脱酸剂，用量为74kg/h，药剂费用约3552元/d；使用阻盐剂减少急冷塔堵塞，阻盐剂投加量为2.4kg/h，药剂费用约为4608元/d；合计单吨危废加药费用为：198.6元/吨(使用氢氧化钙脱酸)或248.84元/吨(使用小苏打脱酸)；
7)飞灰(含盐)产量及处置费用分析
本实施例中的烟气净化工艺：飞灰产量为230.61kg/h(5.45t/d)，按填埋费用(约4000元/t)并平摊至单吨危废计：436元/吨；
湿式为主体的组合工艺：飞灰产量为243.34kg/h(5.84t/d)，按填埋费用(约4000元/t)并平摊至单吨危废计：467.2元/吨；
8)是否可用于处理渗滤液
本实施例中的烟气净化工艺：高效急冷脱酸耦合设备可处理50t/d的渗滤液，节约费用4000元/d；
湿式为主体的组合工艺：渗滤液如果回喷用于急冷塔急冷降温，将会造成急冷塔堵塞频繁的现象，故无法用于处置渗滤液。
9)工程投资分析
本实施例中的烟气净化工艺：总投资约1300万元，包含：高效急冷脱酸耦合设备(约600万元)，布袋除尘器系统(约240万元)，湿法脱酸塔系统(约150万元)，烟气加热器(约32万元)，引风机(约34万元)，配套改造设施(约150万元)及安装工程(约100万元)；
湿式为主体的组合工艺：总投资约1200万元，包含：急冷塔系统(约200万元)，布袋除尘器系统(约240万元)，循环流化床系统(约200万)，两级湿法脱酸塔系统(约240万 元)，烟气加热器(约32万元)，引风机(约34万元)配套改造设施(约160万元)及安装工程(约100万元)。
由上述对比分析可知，本实施例中的烟气净化工艺在工艺过程、生产成本、等方面均比湿法更优。
在实际的危废焚烧烟气净化方法的工艺流程中，在烟气排放装置的进口端设有仪表1，通过仪表1对烟气中的二氧化硫含量进行实时监测和自动控制，自动控制的流程图如图4所示。
其中，以实施例3中烟气的酸性气体的浓度为3361mg/m
3时，降低至20mg/Nm
3以下作为理论基础，通过计算得到高效急冷脱酸耦合设备中所用的30％的碱液投加量为Q＝2.93吨/天。在实际处理过程中，以碱液投加量Q＝2.93吨/天，作为理论值，当仪表1中监测到酸性气体的含量为80mg/L(国家规定排放标准)以下时，则自动控制碱液的投加量维持在理论投加量的1～1.1倍之间；当仪表1中监测到酸性气体的含量大于80mg/L(国家规定排放标准)时，则自动控制增加碱液的投加量，使得实际投加量在Q～2Q之间，直至仪表1中监测到酸性气体的含量小于80mg/L以下时，在通过自动控制逐渐降低高效急冷脱酸耦合设备中的碱液投加量。
综上所述，本发明提供的危废焚烧烟气高效急冷脱酸耦合设备，首先，通过在反应塔内设置第一进液管和第二进液管，第一进液管用于输送冷却物质，第二进液管用于输送碱液等脱酸物质，并通过喷雾装置使冷却物质和脱酸物质与烟气充分混合，从而实现了对烟气同时急冷降温抑制二噁英生成和脱酸的目的，防止二噁英再合成的同时实现酸性气体的有效去除，简化了现有烟气净化技术的工艺流程，生成的固体盐，直接通过底端的输出管道排出，从而避免了大量高盐废水的产生，解决了现有烟气处理系统工艺流程繁琐，以及产生大量难以处理的高盐废水的瓶颈问题；
其次，在高效急冷脱酸耦合设备中，旋转喷雾设备在高速旋转下，使碱液和冷却水形成直径≤50μm的雾滴，与烟气接触能达到高传质的目的，且雾滴总蒸发面积大，蒸发时间短，在反应塔内实现了液相至气相或固相的转变，从而达到不产生废液的目的，既充分满足了环保要求，又避免了高盐废水的产生。
本发明提供的危废焚烧烟气净化系统，首先，通过在焚烧装置后连接余热锅炉，以实现对烟气中的热量进行回收，产生的热量可供生产线内部及厂区其他用户使用，提高了烟气热量的利用率，避免了烟气热量损失；其次，通过在反应塔的出气管的出气口端设置布袋除尘装置，以进一步去除烟气中的粉尘和颗粒物质，避免了烟气中的粉尘造成二次污染； 其三，通过在反应塔的出气管与布袋除尘装置之间设置活性炭吸附装置，以去除烟气中的二噁英、重金属等可被活性炭吸附的物质；最后，通过设置粉尘收集装置，在反应塔中生成的粉尘质经过粉尘收集装置后，沉淀下来的物质直接用收集装置收集，除尘后的气体中含有部分碱性粉末，以返回反应塔中进行重复循环利用，实现内循环。
本发明提供的危废焚烧烟气净化方法，以高效急冷脱酸耦合设备高效脱除烟气中的酸性气体，解决了湿法废水处理的问题，从而改变了现有湿法处理为主体的处理模式，在危废烟气净化技术领域，具有推广应用价值。
以上实施例仅是为充分说明本发明而所举的较佳的实施例，本发明的保护范围不限于此。本技术领域的技术人员在本发明基础上所作的等同替代或变换，均在本发明的保护范围之内。
Claims (7)
- 一种危废焚烧烟气净化系统，其特征在于，包括危废焚烧烟气高效急冷脱酸耦合设备，所述危废焚烧烟气高效急冷脱酸耦合设备包括反应塔(1)；所述反应塔(1)的顶端安装有喷雾装置(2)，喷雾装置(2)的进口端连接有第一进液管(201)和第二进液管(202)，分别用于输送冷却物质和脱酸物质，喷雾装置(2)具有一个出液管口，冷却物质和脱酸物质分别通过不同的进液管进入喷雾装置(2)后，从同一个出液口喷雾；所述反应塔(1)上还设有进气管(101)和出气管(102)；所述反应塔(1)的底端还设有输出管道(103)，用于输出反应塔(1)内生成的物质；还包括依次连接的焚烧装置(3)和余热锅炉(4)，余热锅炉(4)的出气口端与所述反应塔(1)的进气管(101)的进气口端相连；所述余热锅炉(4)内设有SNCR脱硝装置(9)；烟气通过进气管(101)进入反应塔(1)后，通过喷雾装置(2)使第一进液管(201)和第二进液管(202)中的冷却物质和脱酸物质与烟气混合，实现同时急冷降温和脱酸的目的。
- 根据权利要求1所述的危废焚烧烟气净化系统，其特征在于，还包括依次连接的布袋除尘装置(5)和烟气排放装置(6)，所述布袋除尘装置(5)的进气口端与所述反应塔(1)的出气管(102)的出气口端相连。
- 根据权利要求2所述的危废焚烧烟气净化系统，还包括碱液制备储存装置(7)，其出液口与第二进液管(202)的进液口相连。
- 根据权利要求2所述的危废焚烧烟气净化系统，其特征在于，所述反应塔(1)的出气管(102)与所述布袋除尘装置(5)之间还设有活性炭吸附装置(8)；活性炭吸附装置(8)的进气口端与出气管(102)的出气口端相连，出气口端与布袋除尘装置(5)的进气口端相连。
- 根据权利要求1所述的危废焚烧烟气净化系统，其特征在于，还包括粉尘收集装置(10)，其进料口端与所述反应塔(1)的输出管道(103)的出口端相连、排气口端与所述反应塔(1)的第一进液管(201)的进口端相连、出料口端连接有收集装置(11)。
- 如权利要求1至权利要求5任一所述的危废焚烧烟气净化系统的净化方法，其特征在于，包括以下步骤：1)在焚烧装置中将危险废物进行焚烧处理后产生高温烟气；2)将高温烟气输送至余热锅炉内，进行SNCR脱硝处理和热量回收；3)将降温后的烟气从余热锅炉输送至高效急冷脱酸耦合设备的进气管中，同时进行极速降 温和去除烟气中的酸性物质；4)将经过高效急冷脱酸耦合设备处理后的烟气输送至布袋除尘装置中，去除烟气中的粉尘和颗粒物质，然后从烟气排放装置中排出。
- 根据权利要求6所述的净化方法，其特征在于，经过布袋除尘装置处理前的烟气还经过活性炭吸附装置，去除烟气中的二噁英和重金属，高效急冷脱酸耦合设备还连接有粉尘收集装置。
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110805574.6A CN115608131A (zh) | 2021-07-16 | 2021-07-16 | 一种危废焚烧烟气高效急冷脱酸耦合设备、净化系统及净化方法 |
| CN202121620947.4U CN216149409U (zh) | 2021-07-16 | 2021-07-16 | 一种急冷脱酸一体化装置及危废焚烧烟气净化系统 |
| CN202121620947.4 | 2021-07-16 | ||
| CN202110805574.6 | 2021-07-16 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO2023284636A1 true WO2023284636A1 (zh) | 2023-01-19 |
Family
ID=84919039
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/CN2022/104526 WO2023284636A1 (zh) | 2021-07-16 | 2022-07-08 | 一种危废焚烧烟气净化系统及净化方法 |
Country Status (1)
| Country | Link |
|---|---|
| WO (1) | WO2023284636A1 (zh) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116351222A (zh) * | 2023-05-10 | 2023-06-30 | 北京中科润宇环保科技股份有限公司 | 一种干法烟气脱酸反应装置及工作方法 |
| CN117138559A (zh) * | 2023-09-14 | 2023-12-01 | 江西兴南环保科技有限公司 | 一种基于含铜危固废料处理的烟气资源化净化工艺 |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000262853A (ja) * | 1999-03-16 | 2000-09-26 | Nkk Corp | 排ガス処理方法および装置 |
| CN207486806U (zh) * | 2017-08-24 | 2018-06-12 | 上海奕茂环境科技有限公司 | 危险废物三段式焚烧及尾气处理系统 |
| CN108870405A (zh) * | 2017-05-08 | 2018-11-23 | 衡水精臻环保技术有限公司 | 一种危险废物收集处置工艺 |
| CN112456797A (zh) * | 2020-12-21 | 2021-03-09 | 重庆大学 | 玻璃体制备方法和垃圾焚烧飞灰与铝电解槽大修渣无害化处置方法 |
| CN112460604A (zh) * | 2020-11-26 | 2021-03-09 | 中广核工程有限公司 | 危险废物焚烧烟气处理系统及危险废物焚烧烟气处理方法 |
| CN216149409U (zh) * | 2021-07-16 | 2022-04-01 | 重庆创绿环境保护有限公司 | 一种急冷脱酸一体化装置及危废焚烧烟气净化系统 |
-
2022
- 2022-07-08 WO PCT/CN2022/104526 patent/WO2023284636A1/zh unknown
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000262853A (ja) * | 1999-03-16 | 2000-09-26 | Nkk Corp | 排ガス処理方法および装置 |
| CN108870405A (zh) * | 2017-05-08 | 2018-11-23 | 衡水精臻环保技术有限公司 | 一种危险废物收集处置工艺 |
| CN207486806U (zh) * | 2017-08-24 | 2018-06-12 | 上海奕茂环境科技有限公司 | 危险废物三段式焚烧及尾气处理系统 |
| CN112460604A (zh) * | 2020-11-26 | 2021-03-09 | 中广核工程有限公司 | 危险废物焚烧烟气处理系统及危险废物焚烧烟气处理方法 |
| CN112456797A (zh) * | 2020-12-21 | 2021-03-09 | 重庆大学 | 玻璃体制备方法和垃圾焚烧飞灰与铝电解槽大修渣无害化处置方法 |
| CN216149409U (zh) * | 2021-07-16 | 2022-04-01 | 重庆创绿环境保护有限公司 | 一种急冷脱酸一体化装置及危废焚烧烟气净化系统 |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116351222A (zh) * | 2023-05-10 | 2023-06-30 | 北京中科润宇环保科技股份有限公司 | 一种干法烟气脱酸反应装置及工作方法 |
| CN116351222B (zh) * | 2023-05-10 | 2023-10-17 | 北京中科润宇环保科技股份有限公司 | 一种干法烟气脱酸反应装置及工作方法 |
| CN117138559A (zh) * | 2023-09-14 | 2023-12-01 | 江西兴南环保科技有限公司 | 一种基于含铜危固废料处理的烟气资源化净化工艺 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2023284636A1 (zh) | 一种危废焚烧烟气净化系统及净化方法 | |
| CN108480360B (zh) | 回转窑熔融法飞灰全资源回收利用及尾气超净排放方法 | |
| CN109458623B (zh) | 一种高含盐高含氯有机废液焚烧环保节能排放系统 | |
| WO2021114084A1 (zh) | 一种垃圾焚烧节能烟气超低净化系统 | |
| CN105289248B (zh) | 一种生活垃圾焚烧发电厂烟气湿式净化处理方法及装置 | |
| CN106861415B (zh) | 烟气净化系统及方法 | |
| WO2018192564A1 (zh) | 一种生活垃圾热解焚烧装置烟气净化系统 | |
| CN110665352A (zh) | 一种水泥窑尾中低硫烟气干法脱硫脱硝除尘装置及方法 | |
| CN211358310U (zh) | 一种垃圾焚烧炉的废水零排放烟气超净处理系统 | |
| CN103994447A (zh) | 气固液一体化焚烧系统 | |
| WO2012089089A1 (zh) | 用双效反应器处理高温废物焚化炉产生的烟气的方法和系统 | |
| CN203625223U (zh) | 一种应用于瓶罐玻璃窑炉的烟气综合治理装置 | |
| CN216149409U (zh) | 一种急冷脱酸一体化装置及危废焚烧烟气净化系统 | |
| CN112973408B (zh) | 含铜废物资源化利用烟气净化的处理工艺 | |
| CN102564149A (zh) | 工业窑炉废气净化回收工艺及设备 | |
| CN113883543A (zh) | 一种高含氯危废焚烧烟气净化及盐酸回收利用系统及方法 | |
| CN212025143U (zh) | 含Cu工业污泥危废资源化处理系统 | |
| CN211358316U (zh) | 一种水泥窑尾中低硫烟气干法脱硫脱硝除尘装置 | |
| CN202700337U (zh) | 一种烧结烟气净化装置 | |
| CN205570080U (zh) | 一种焦炉烟气脱硫系统 | |
| CN110787620A (zh) | 一种玻璃熔窑烟气协同减排耦合余热发电系统 | |
| CN201764834U (zh) | 一种工业窑炉烟气利用与处理装置 | |
| CN116293721A (zh) | 一种贵金属焚烧及尾气净化工艺 | |
| CN212651583U (zh) | 一种双循环式活性炭分离解析的垃圾焚烧烟气处理系统 | |
| CN213077965U (zh) | 一种用于尾气处理系统的干式反应装置 |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 22841272 Country of ref document: EP Kind code of ref document: A1 |
|
| NENP | Non-entry into the national phase |
Ref country code: DE |