CN212841619U - High-chlorine dangerous waste incineration disposal system - Google Patents
High-chlorine dangerous waste incineration disposal system Download PDFInfo
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- CN212841619U CN212841619U CN202021581076.5U CN202021581076U CN212841619U CN 212841619 U CN212841619 U CN 212841619U CN 202021581076 U CN202021581076 U CN 202021581076U CN 212841619 U CN212841619 U CN 212841619U
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- deacidification
- tower
- dry
- chlorine
- wet
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- 229910052801 chlorine Inorganic materials 0.000 title claims abstract description 36
- 239000000460 chlorine Substances 0.000 title claims abstract description 36
- 238000004056 waste incineration Methods 0.000 title description 5
- 238000001816 cooling Methods 0.000 claims abstract description 48
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000003546 flue gas Substances 0.000 claims abstract description 47
- ZAMOUSCENKQFHK-UHFFFAOYSA-N chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000007921 spray Substances 0.000 claims abstract description 15
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 13
- 238000000034 method Methods 0.000 claims abstract description 13
- 239000000779 smoke Substances 0.000 claims abstract description 13
- 238000005507 spraying Methods 0.000 claims abstract description 13
- 238000010791 quenching Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 7
- 238000010521 absorption reaction Methods 0.000 claims abstract description 5
- 238000001704 evaporation Methods 0.000 claims abstract description 5
- 239000000843 powder Substances 0.000 claims abstract description 5
- 239000000428 dust Substances 0.000 claims description 13
- 238000005406 washing Methods 0.000 claims description 13
- 238000002485 combustion reaction Methods 0.000 claims description 9
- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 8
- 239000002920 hazardous waste Substances 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 4
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 235000011194 food seasoning agent Nutrition 0.000 claims description 4
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 4
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 238000005260 corrosion Methods 0.000 description 10
- 239000002699 waste material Substances 0.000 description 7
- 239000002918 waste heat Substances 0.000 description 6
- 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 5
- 239000002253 acid Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 239000002893 slag Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000007769 metal material Substances 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000003009 desulfurizing Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 230000000171 quenching Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Abstract
The utility model provides a high chlorine danger is useless to burn processing system, it can stably handle the high chlorine danger that chlorine content > 5% useless, can discharge the flue gas that accords with the standard, and equipment operation is stable simultaneously, and the operation safety risk is little, and the cost is lower. It includes: the kiln that burns, its characterized in that, it still includes: a cooling tower, a quench tower, a dry deacidification device and a wet deacidification unit which are connected in sequence; the cooling tower is connected with a smoke exhaust port of the incineration kiln, a discharge port of the quench tower is connected with a dry deacidification device, smoke deacidified by the dry deacidification device enters a wet deacidification unit, and an exhaust port of the wet deacidification unit is connected with a chimney; the temperature of the tail gas flue gas at the outlet of the incineration kiln is reduced by the cooling tower through the processes of water spraying cooling and evaporation heat absorption cooling; the dry deacidification device adopts alkaline dry powder agent to carry out deacidification treatment on the smoke; a liquid spray head is arranged in the wet deacidification unit, and the flue gas is cooled and deacidified by adopting a mode of spraying deacidification liquid.
Description
Technical Field
The utility model relates to a solid useless incineration disposal technical field specifically is useless incineration disposal system that burns of high chlorine danger.
Background
High chlorine waste contains a large amount of chlorides, and high chlorine waste burns and deals with the in-process, and a large amount of chlorides have all brought very big corrosion threat to burning equipment such as waste heat recovery, flue gas deacidification, desulfurization, the dust removal in low reaches of burning furnace through burning in having got into the flue gas, and compare with ordinary danger useless burning system, high chlorine waste burns and deals with the system and mainly faces bigger challenge on the follow-up processing of burning the flue gas.
In the prior art, two processes are mainly adopted for cooling high-temperature incineration flue gas: waste heat boiler, heat exchanger (air cooling or water cooling). However, in the high-chlorine corrosion working condition, the risk that metal equipment is corroded by direct contact with high-chlorine flue gas is very high, and particularly, the safety risk caused by corrosion is greatly increased when the waste heat boiler is used as a pressure container, so that a hazardous waste incineration system with high fluorine content or more than 5% chlorine content is treated according to the requirements of HJ/T176-2005 hazardous waste centralized incineration disposal engineering construction technical specification, and the waste heat boiler cannot be used for cooling. And the heat exchanger is adopted, because a better heat exchange coefficient is obtained, the metal material is not selected, but in the high-chlorine corrosion flue gas, the metal material cannot ensure the use safety and the durability. Therefore, the two schemes can not cope with the temperature reduction of the high-chlorine flue gas, and if the high-chlorine flue gas is made of metal with good acid resistance, the cost of the system is too high.
Disclosure of Invention
In order to solve the system flue gas processing apparatus that burns among the prior art and all be not suitable for the useless problem of burning the flue gas cooling and handling of high chlorine danger, the utility model provides a high chlorine danger is useless to burn the processing system, and it can stably handle the high chlorine danger that chlorine content > 5% useless, can discharge the flue gas that accords with the standard, and equipment operation is stable simultaneously, and operation safety risk is little, and the cost is lower.
The technical scheme of the utility model is like this: high chlorine danger is useless to burn processing system, it includes: the kiln that burns, its characterized in that, it still includes: a cooling tower, a quench tower, a dry deacidification device and a wet deacidification unit which are connected in sequence;
the cooling tower is connected with the exhaust port of the incineration kiln, the discharge port of the quench tower is connected with the dry deacidification device, the flue gas deacidified by the dry deacidification device enters the wet deacidification unit, and the exhaust port of the wet deacidification unit is connected with a chimney;
the temperature of the tail gas flue gas at the outlet of the incineration kiln is reduced by the cooling tower through water spraying cooling and evaporation heat absorption cooling processes;
the dry deacidification device adopts alkaline dry powder agent to deacidify the smoke;
set up liquid shower nozzle in the wet process deacidification unit, adopt the mode that sprays deacidification liquid to cool down and deacidify the flue gas.
It is further characterized in that:
the dry deacidification device comprises two stages of dry deacidification units which are connected in sequence, and each stage of dry deacidification unit comprises a dry deacidification tower and a bag-type dust remover which are connected in sequence;
the first stage of the dry deacidification unit adopts slaked lime as a deacidification agent, and the second stage of the dry deacidification unit adopts baking soda as the deacidification agent;
the wet deacidification unit is used for deacidifying in a mode of spraying alkali liquor; the wet deacidification unit comprises a pre-cooling tower and a washing tower which are connected in sequence; a circulating spray structure is arranged in the pre-cooling tower, the washing tower is a seasoning type spray tower, and a packing layer, a demister and a circulating spray structure are arranged in the washing tower;
an activated carbon injection device is arranged in the first-stage dry deacidification unit;
arranging an SNCR denitration device in a flue at an inlet of the cooling tower;
the incineration kiln comprises a rotary kiln and a secondary combustion chamber which are connected in sequence.
The high-chlorine dangerous waste incineration disposal system provided by the utility model is provided with the cooling tower at the tail gas outlet of the incineration kiln, adopts the water spray cooling mode to replace the waste heat boiler and the heat exchanger in the prior art, avoids the problem that metal equipment is corroded quickly under the high-chlorine environment, and ensures that the equipment of the incineration disposal system can not generate safety accidents; the dry deacidification device is arranged in front of the wet deacidification unit, and the alkaline dry powder agent is used for performing two-stage dry deacidification on the flue gas, so that the risk of corrosion of subsequent equipment is reduced, the flue gas amount needing the wet deacidification unit for deacidification is reduced, the wastewater discharge of the wet deacidification unit is reduced, and the system cost is reduced; by arranging the two-stage dry deacidification unit, the flue gas is deacidified sequentially by the slaked lime and the baking soda, on the basis of ensuring that the system cost is low, the flue gas amount needing the wet deacidification unit to deacidify is further reduced, and the risk of corrosion of subsequent equipment is reduced; through the wet process deacidification unit who sets up the two-stage, the preliminary cooling of flue gas, preliminary deacidification are realized to first order wet process deacidification, and the degree of depth deacidification to the flue gas is realized to second level wet process deacidification, further reduction the risk that follow-up equipment is corroded.
Drawings
Fig. 1 is a schematic structural view of the waste incineration disposal system of the present invention.
Detailed Description
As shown in fig. 1, the utility model discloses high chlorine danger is useless to burn processing system, it includes: an incineration kiln consisting of a rotary kiln 2 and a secondary combustion chamber 3, and a cooling tower 7, a quench tower 9, a dry deacidification device and a wet deacidification unit which are connected in sequence.
The high-chlorine waste enters the rotary kiln 2 from the feeding hole 1, is subjected to high-temperature incineration treatment by a kiln system, inorganic parts such as ash, metal and the like are discharged from the slag outlet 5, organic matters are gasified in the rotary kiln 2 and continuously enter the secondary combustion chamber 3 to be subjected to pyrolysis under the aerobic condition, and the emergency smoke outlet 4 is arranged at the top of the secondary combustion chamber 3, so that the smoke discharge is ensured during emergency, and the use safety of equipment is improved; the incineration kiln adopts a two-stage combustion technology of a rotary kiln and a second combustion chamber, so that high-chlorine waste is decomposed more thoroughly, and the subsequent deacidification treatment can be more thorough.
The cooling tower 7 is connected with the smoke outlet of the secondary combustion chamber 3, an SNCR denitration device (not shown in the figure) is arranged in a flue at the inlet of the cooling tower 7 and used for carrying out denitration treatment on the smoke before deacidification, and the SNCR denitration device is used for ensuring that the cost of the whole system is lower; a discharge port 10 of a quenching tower 9 is connected with a first-stage dry deacidification unit 13 in a dry deacidification device, flue gas deacidified by the dry deacidification device enters a wet deacidification unit, and an exhaust port of the wet deacidification unit is connected with a chimney 30.
The flue gas after high-temperature decomposition in the secondary combustion chamber 3 enters a cooling tower 7; atomized water is sprayed into the cooling tower 7 through the spraying device 6, and the temperature of the flue gas is reduced in an evaporation and heat absorption mode; the temperature of the flue gas passing through the cooling tower 7 is reduced to 500-550 ℃ from more than 1100 ℃, the cooling tower is used as a flue gas temperature regulating section, and the temperature of the flue gas at the outlet of the incineration kiln is reduced by water spraying cooling and evaporation heat absorption cooling processes, so that a waste heat boiler commonly used in a common incineration process is replaced, and the problem of equipment corrosion under the condition of high chlorine is avoided; solid waste slag generated by the cooling tower 7 is discharged out of the tower body from a slag discharge port 8 of the cooling tower;
quench water is sprayed to the flue gas through a quench water spray head 31 in the quench tower 9, the temperature of the flue gas is reduced to 190-200 ℃ from 500-550 ℃, the cooling time of the flue gas in the quench tower 9 is less than 1 second, the regeneration of dioxin is reduced to the maximum extent (the temperature interval for the resynthesis of the dioxin is 250-450 ℃), the concentration of the dioxin in the flue gas is ensured to reach the standard, and the emission of the flue gas is ensured to accord with the national standard.
The dry deacidification device deacidifies the smoke through a dry powder deacidification agent; the dry deacidification device comprises two stages of dry deacidification units which are connected in sequence, and each dry deacidification unit comprises a dry deacidification tower and a bag-type dust remover which are connected in sequence; the first stage dry deacidification unit comprises: a first stage dry deacidification tower 13 and a first stage bag-type dust collector 15; the second-stage dry deacidification unit comprises a second-stage dry deacidification tower 18 and a second-stage bag-type dust collector 20; solid wastes generated by a first-stage dry-method deacidification tower 13, a first-stage bag-type dust remover 15, a second-stage dry-method deacidification tower 18 and a second-stage bag-type dust remover 20 are discharged out of the device from ash discharge openings 10, 14, 17 and 19 respectively;
the first-stage dry deacidification unit adopts slaked lime as a deacidification agent and enters a first-stage dry deacidification tower 13 from a first-stage deacidification agent inlet 11; the second-stage dry deacidification unit adopts baking soda as a deacidification agent and enters a second-stage dry deacidification tower 18 from a second-stage deacidification agent inlet 16; an active carbon injection device is arranged in the first-stage dry deacidification unit at the same time, active carbon enters the first-stage dry deacidification tower 13 from an active carbon inlet 12, the active carbon falls on the surface of a filter bag of the first-stage bag-type dust remover 15 after passing through the first-stage dry deacidification tower 13, heavy metals and dioxin in smoke entering the first-stage bag-type dust remover 15 are adsorbed, the content of the heavy metals and the dioxin in the smoke is reduced, and the smoke can be ensured to meet the national emission standard; the neutralization reaction of the dry deacidification mainly occurs in the dry deacidification towers 13 and 18 and the surfaces of filter bags of the bag-type dust collectors 15 and 20; through the treatment of the continuous two-stage dry deacidification unit, the dry deacidification efficiency and the dry deacidification share are greatly improved, the low chlorine content and the small corrosion effect of the flue gas reaching the downstream wet unit are ensured, the corrosion risk of downstream equipment is reduced, the wet deacidification share is reduced, the generation amount of wet waste water is reduced, and the improvement of the system operation economy is facilitated.
A liquid spray head is arranged in the wet deacidification unit, and the flue gas is cooled and deacidified by adopting a mode of spraying alkali liquor. The wet deacidification unit comprises a pre-cooling tower 21 and a washing tower 26 which are connected in sequence; a circulating spray structure 22 is arranged in the pre-cooling tower 21, and the alkali liquor is recycled in the pre-cooling tower 21 through a primary circulating pump 23; the washing tower 26 is a seasoning type spray tower, a packing layer 27, a demister 25 and a circulating spray structure 24 are arranged in the washing tower, and the alkali liquor is recycled in the precooling tower 21 through a secondary circulating pump 28; the exhaust of the scrubber 26 is connected to a stack 30 via an induced draft fan 29.
The flue gas after two-stage dry deacidification and cloth bag dust removal enters a wet deacidification unit, and the wet deacidification unit consists of a primary precooling tower and a secondary washing tower; the pre-cooling tower 21 has the process functions of 'primary cooling and primary deacidification of the flue gas', the flue gas is circularly sprayed with alkali liquor in the pre-cooling tower 21 through the circulating spraying structure 22 to realize temperature adjustment, the temperature of the flue gas is reduced from 160-180 ℃ to-70 ℃, and simultaneously, sodium hydroxide in the alkali liquor and acid gas are subjected to neutralization reaction to remove most of the acid gas; the flue gas treated by the pre-cooling tower 21 enters a washing tower 26 of a wet second stage, the washing tower 26 is a seasoning type spraying tower, a circulating spraying structure 24, a packing layer 27 and a demister 25 are arranged in the washing tower, acid gas in the flue gas is deeply removed by spraying a large amount of circulating alkali liquor, and meanwhile, the demister 25 separates fog drops carried by the flue gas, so that the probability of salt deposition, dust deposition, corrosion and other conditions of downstream equipment is reduced; finally, the purified flue gas is guided into a chimney 30 through a draught fan 28 and is discharged at high altitude after reaching the standard. Based on the utility model discloses technical scheme burns to the high chlorine waste material and deals with, directly handles the dangerous waste material that chlorine content can reach 5% ~20% through burning the mode, has promoted the useless technical response ability and the market competitiveness of handling the enterprise of danger.
Claims (7)
1. High chlorine danger is useless to burn processing system, it includes: the kiln that burns, its characterized in that, it still includes: a cooling tower, a quench tower, a dry deacidification device and a wet deacidification unit which are connected in sequence;
the cooling tower is connected with the exhaust port of the incineration kiln, the discharge port of the quench tower is connected with the dry deacidification device, the flue gas deacidified by the dry deacidification device enters the wet deacidification unit, and the exhaust port of the wet deacidification unit is connected with a chimney;
the temperature of the tail gas flue gas at the outlet of the incineration kiln is reduced by the cooling tower through water spraying cooling and evaporation heat absorption cooling processes;
the dry deacidification device adopts alkaline dry powder agent to deacidify the smoke;
set up liquid shower nozzle in the wet process deacidification unit, adopt the mode that sprays deacidification liquid to cool down and deacidify the flue gas.
2. The incineration disposal system for high-chlorine hazardous waste according to claim 1, characterized in that: the dry deacidification device comprises two stages of dry deacidification units which are connected in sequence, and each stage of dry deacidification unit comprises a dry deacidification tower and a bag-type dust remover which are connected in sequence.
3. The incineration disposal system for high-chlorine hazardous waste according to claim 2, characterized in that: the first-stage dry deacidification unit adopts slaked lime as a deacidification agent, and the second-stage dry deacidification unit adopts baking soda as the deacidification agent.
4. The incineration disposal system for high-chlorine hazardous waste according to claim 1, characterized in that: the wet deacidification unit is used for deacidifying in a mode of spraying alkali liquor; the wet deacidification unit comprises a pre-cooling tower and a washing tower which are connected in sequence; the pre-cooling tower is internally provided with a circulating spray structure, the washing tower is a seasoning type spray tower, and the inside of the washing tower is provided with a packing layer, a demister and a circulating spray structure.
5. The incineration disposal system for high-chlorine hazardous waste according to claim 2, characterized in that: an active carbon injection device is arranged in the first-stage dry deacidification unit.
6. The incineration disposal system for high-chlorine hazardous waste according to claim 1, characterized in that: and an SNCR denitration device is arranged in a flue at the inlet of the cooling tower.
7. The incineration disposal system for high-chlorine hazardous waste according to claim 1, characterized in that: the incineration kiln comprises a rotary kiln and a secondary combustion chamber which are connected in sequence.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021581076.5U CN212841619U (en) | 2020-08-03 | 2020-08-03 | High-chlorine dangerous waste incineration disposal system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021581076.5U CN212841619U (en) | 2020-08-03 | 2020-08-03 | High-chlorine dangerous waste incineration disposal system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212841619U true CN212841619U (en) | 2021-03-30 |
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ID=75128356
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021581076.5U Active CN212841619U (en) | 2020-08-03 | 2020-08-03 | High-chlorine dangerous waste incineration disposal system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212841619U (en) |
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2020
- 2020-08-03 CN CN202021581076.5U patent/CN212841619U/en active Active
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