CN210186679U - Dangerous waste disposal system adopting plasma gasification and melting - Google Patents
Dangerous waste disposal system adopting plasma gasification and melting Download PDFInfo
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- CN210186679U CN210186679U CN201920729983.0U CN201920729983U CN210186679U CN 210186679 U CN210186679 U CN 210186679U CN 201920729983 U CN201920729983 U CN 201920729983U CN 210186679 U CN210186679 U CN 210186679U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
Providing a plasma gasification melting hazardous waste disposal system, wherein the system comprises a plasma gasification melting furnace, a waste heat boiler, a washing tower, a dust removal device and an exhaust device, the plasma gasification melting furnace carries out melting treatment on the broken hazardous waste, and the waste heat boiler recovers sensible heat of synthesis gas discharged by the plasma gasification melting furnace; the washing tower is used for cooling, deacidifying and dedusting the synthetic gas passing through the waste heat boiler, and the dedusting device is used for further dedusting the synthetic gas discharged by the washing tower; the exhaust device comprises a torch or a gas boiler, the torch is used for carrying out combustion treatment on the synthetic gas passing through the dust removal device, and the gas boiler is used for carrying out chemical energy recovery on the gas passing through the dust removal device.
Description
Technical Field
The utility model relates to a dangerous waste disposal system and technology of plasma gasification melting.
Background
A plasma gasification melting system for centralized treatment of solid wastes comprises a plasma gasification melting furnace, wherein a synthesis gas outlet of the plasma gasification melting furnace is connected with a secondary combustion chamber, and a high-temperature flue gas outlet of the secondary combustion chamber is sequentially connected with a waste heat recovery system and a flue gas purification system.
In such systems, the molten hazardous waste is gasified using plasma, and the syngas at the outlet of the plasma gasifier is burned out directly in the secondary combustion chamber. The flue gas enters a quenching and semi-drying deacidification tower after the temperature of the flue gas is reduced to about 500 ℃ after heat exchange of a waste heat boiler, the flue gas is quenched (the temperature of the flue gas is reduced from 500 ℃ to 200 ℃) and deacidified in the process, then the flue gas respectively enters a dry-type deacidification tower and a bag-type dust collector with an active carbon injection device to complete deacidification, dust removal and adsorption (heavy metal and dioxin) in the process, and finally the flue gas enters a wet-type washing tower to be further deacidified and then is discharged from a chimney through a complex flue gas heating device (white smoke elimination).
The utility model discloses the people finds it to have following problem through carrying out the analysis to this system after.
The synthesis gas at the outlet of the plasma furnace is directly burnt out in the secondary combustion chamber, which has some problems. First, the use of air during the burn-out process inevitably results in the formation of thermodynamic NOx during the process, increasing the burden of subsequent denitration. Secondly, the incineration scheme is that the sensible heat of the flue gas in the range of 1100-plus-500 ℃ is collected by the waste heat boiler, and the energy recovery rate of the flue gas is low.
In the subsequent flue gas purification process, as the flue gas is cooled by using alkali liquor in the quenching and semi-drying process within 1s, the temperature of the flue gas is reduced from 500 ℃ to below 200 ℃, the process has extremely high control requirements, the temperature of the flue gas is reduced at an extremely high speed, the tower body corrosion caused by 'wall wetting' due to excessive water injection cannot be caused, small-particle atomized alkali liquor used in the quenching process is generated by a high-quality atomizing nozzle under high pressure, and the atomizing nozzle is inevitably blocked due to mechanical friction or scaling in the use process, so that frequent maintenance and replacement are required.
In addition, in the process route, alkali adopted by the quenching semi-dry method and the quenching dry method enters the bag-type dust remover in the form of particles, and activated carbon is required to be sprayed to adsorb heavy metals, so that the concentration of the particles in the flue gas is artificially increased, and the treatment load of the bag-type dust remover is increased. Most of the volatile heavy metals in the flue gas are still in the secondary fly ash discharged by the bag-type dust collector, and the fly ash needs to be further treated. And because most of the cloth bags at the present stage contain PTFE materials, the cloth bags also need to be incinerated for disposal after being used for 2-3 years, and F (fluorine) element is released in the disposal process, so the difficulty of flue gas purification and the corrosion prevention requirement of the system are increased.
SUMMERY OF THE UTILITY MODEL
It is an object of the present invention to provide a plasma gasification melting hazardous waste disposal system that can solve at least one of the aforementioned problems, such as improving energy recovery or avoiding too heavy a denitration burden.
The utility model discloses another purpose provides a dangerous waste disposal technology of plasma gasification melting.
The scheme 1 is that a plasma gasification melting hazardous waste disposal system is provided, which comprises a plasma gasification melting furnace, a waste heat boiler, a washing tower, a dust removal device and an exhaust device, wherein the plasma gasification melting furnace is used for melting the broken hazardous waste, and the waste heat boiler is used for recovering sensible heat of synthesis gas exhausted by the plasma gasification melting furnace; the washing tower is used for cooling, deacidifying and dedusting the synthetic gas passing through the waste heat boiler, and the dedusting device is used for further dedusting the synthetic gas discharged by the washing tower; the exhaust device comprises a torch or a gas boiler, the torch is used for carrying out combustion treatment on the synthetic gas passing through the dust removal device, and the gas boiler is used for carrying out chemical energy recovery on the gas passing through the dust removal device.
In one embodiment of the system, the scrubber tower comprises a venturi wet quench deacidification tower.
In one embodiment of the system, the scrubber tower comprises two stages of water scrubber towers, wherein the first stage of water scrubber tower is a venturi wet quenching deacidification tower, and the second stage of water scrubber tower carries out secondary water washing on the synthesis gas discharged from the first stage of water scrubber tower.
In one embodiment of the system, the system further comprises a filter press for filter pressing the bottoms solution of the scrubber to recover solids.
In one embodiment of the system, the dust removal device is a wet dust remover.
In one embodiment of the system, the exhaust device further includes a drying tower for drying the synthesis gas, a booster for boosting the synthesis gas dried by the drying tower, and a gas storage tank for storing the boosted synthesis gas, and the gas storage tank supplies the gas to the gas boiler.
The 2 nd mode provides a dangerous waste disposal process of plasma gasification melting, use the melting furnace of plasma gasification to carry on the melting treatment to the dangerous waste after breaking, the temperature range in the melting furnace of said plasma gasification is controlled between 1200 and 1600 ℃, control the oxygen content in the furnace to be lower than 1%, make the synthetic gas produced in the furnace stay in the furnace for time more than 3 s; guiding the synthesis gas discharged by the plasma gasification melting furnace to a waste heat boiler, and recovering the sensible heat of the synthesis gas by using the waste heat boiler; cooling, deacidifying and dedusting the synthesis gas passing through the waste heat boiler by using a washing tower, and cooling the synthesis gas to be below 100 ℃; dedusting the synthesis gas passing through the washing tower by adopting a deduster; and (3) burning the synthesis gas subjected to dust removal through a torch or recovering chemical energy through a gas boiler.
In one embodiment of the process, the temperature reduction, deacidification and dust removal are carried out by using two-stage water washing tower, wherein the gas-liquid ratio of the first-stage water washing tower is 3-10L/m3Controlling the temperature of the discharged synthetic gas below 100 ℃, wherein the gas-liquid ratio of the second-stage water scrubber is 1.5-8L/m3And the pH value of the circulating liquid of the two-stage water washing tower is controlled to be 8-11.5.
In one embodiment of the process, the dust separator is a wet dust separator that removes at least fine particulate matter having a particle size of 0.5um from the synthesis gas.
In one embodiment of the process, the dedusted synthesis gas is dried, pressurized, stored and then delivered to a gas boiler for chemical energy recovery, and the exhaust temperature of the gas boiler is more than 150 ℃.
In the scheme, the secondary combustion chamber is not arranged, the sensible heat of the synthesis gas is directly recovered by the waste heat boiler, then the synthesis gas is cooled, deacidified and dedusted, and the chemical energy of clean gas is recovered by the gas boiler, so that the energy recovery can be realized to the maximum extent, the generation of dioxin and NOx in the plasma furnace is reduced to the maximum extent by the system, the regeneration of NOx is reduced in the gas boiler in the later period by adopting a low-nitrogen combustion mode, the NOx in the flue gas is lower than the emission concentration, the denitration link can be omitted, and the investment cost and the operation cost are saved.
Drawings
The above and other features, properties and advantages of the present invention will become more apparent from the following description of the embodiments with reference to the accompanying drawings, in which:
fig. 1 is a flow diagram of a mobile hazardous waste disposal process according to one or more embodiments.
FIG. 2 is a schematic diagram of the overall configuration of one or more embodiments of a venturi scrubber.
Fig. 3 is a schematic plan view of the flow guide structure in fig. 2.
Fig. 4 is a schematic view showing a state in which the diffuser pipe in fig. 3 forms a flow guide.
Detailed Description
The following discloses many different embodiments or examples for implementing the subject technology described. Specific examples of components and arrangements are described below to simplify the present disclosure, but these are merely examples and are not intended to limit the scope of the present invention. For example, if a first feature is formed over or on a second feature described later in the specification, this may include embodiments in which the first and second features are formed in direct contact, and may also include embodiments in which additional features are formed between the first and second features, such that the first and second features may not be in direct contact. Additionally, reference numerals and/or letters may be repeated among the various examples throughout this disclosure. This repetition is for the purpose of simplicity and clarity and does not in itself dictate a relationship between the various embodiments and/or configurations discussed. Further, when a first element is described as being coupled or coupled to a second element, the description includes embodiments in which the first and second elements are directly coupled or coupled to each other, as well as embodiments in which one or more additional intervening elements are added to indirectly couple or couple the first and second elements to each other.
As shown in FIG. 1, the plasma gasification melting hazardous waste disposal system optionally comprises a crusher 1 for crushing the hazardous waste to a certain size, such as 100 and 500mm, and an existing four-shaft crusher can be selected.
The system optionally further includes a feeder 2, the feeder 2 being adapted to convey the crushed hazardous waste to a plasma stripping and gasification furnace 3, the feeder being selected from an existing screw feeder or a hydraulic feeder.
In the case of the system described above,the plasma gasification melting furnace 3 is a core device, wherein the heat energy is generated by a plasma torch, and the medium gas of the plasma torch is air, nitrogen and H2The furnace atmosphere is anaerobic atmosphere, the oxygen content in the furnace is lower than 1%, the temperature in the furnace generated by the plasma moment can be controlled between 1200 ℃ and 1600 ℃, all dangerous wastes can be subjected to melting treatment, the dangerous wastes are thermally cracked without combustion, slag and synthetic gas are generated, the slag is vitreous substance and can serve as refractory material, cement raw material and the like, most of the synthetic gas is combustible gas such as hydrogen and the like, and the synthetic gas can be used as clean fuel.
A waste heat boiler 4 is provided downstream of the plasma gasification melting furnace 3, and the sensible heat in the synthesis gas is recovered by introducing the synthesis gas through the waste heat boiler 4, and usually the synthesis gas can be reduced from 1200 ℃ to 500 ℃.
The downstream side of the waste heat boiler 4 is provided with a washing tower which utilizes the contact between the synthesis gas and the dilute alkali liquor to transfer the pollutants in the synthesis gas into the liquid, and then separates the synthesis gas from the dilute alkali liquor to achieve the purpose of cleaning the synthesis gas. One preferred mode is a two-stage water wash column 5. The first stage of the two-stage water washing tower 5 is preferably a Venturi wet quenching deacidification tower or a water washing tower with other configurations, wherein the liquid-gas ratio is controlled to be 3-10L/m3The syngas temperature is reduced to below 100 ℃, for example from 500 ℃ to below 100 ℃. The first-stage water washing tower sprays a large amount of dilute alkali liquor into the introduced flue gas, so that the effects of deacidification and dust removal are achieved while the temperature is reduced. Acidic substances in the synthesis gas, e.g. HCl, H2S and dilute alkali liquor are subjected to chemical reaction to be removed, heavy metals which are easy to volatilize in the synthetic gas exist in a solution or solid state form in the tower bottom circulating liquid after being washed by a large amount of water, precipitates can be formed at the tower bottom by adjusting the pH value of the tower bottom circulating liquid 51 of the two-stage water washing tower to be 8-11.5, and the tower bottom circulating liquid can be subjected to filter pressing by a filter press 12 to recover solids. The second stage water scrubber can also adopt a Venturi wet quenching deacidification tower or other water scrubbers with other configurations to pass through the first stageThe synthesis gas in the water scrubber is washed for the second time, and is further cooled, deacidified and dedusted, wherein the liquid-gas ratio is controlled to be 1.5-8L/m3And the temperature of the synthesis gas is reduced to about 60 ℃. The first stage and the second stage water washing towers can share the circulating liquid at the bottom of the tower and share the supply source of the dilute alkali liquid 16.
Venturi wet type rapid cooling deacidification tower A schematic structure of a Venturi wet type rapid cooling deacidification tower is shown in figures 2 to 4 and comprises an inlet pipe 41, a contraction pipe 42, a throat pipe 48 and a diffusion pipe 43 which are sequentially communicated, a regulator penetrates through the inlet pipe 41 and can penetrate through the throat pipe 48 to spray water in a vertically adjustable mode, a flow guide structure 49 is arranged between the diffusion pipe 43 and the throat pipe 48, and the diffusion pipe 43 leads to a water filtering unit. Preferably, the shrink tube 42 is integrally connected to the throat 48. The regulator is used to spray water to the throat 48 and may be replaced by other water supply means.
Wherein, the water filter unit includes water tank 44, and the end of diffuser 43 leads to water tank 44, is equipped with exhaust outlet 410 on the water tank 44, and the end of diffuser 43 slightly immerses under the water tank 44 liquid level, makes waste gas pass through the secondary washing, and water tank 44 design has certain volume for provide buffer space and deposit, discharge the dust particle wherein for the circulating water.
Referring to fig. 2 and 3, the flow guiding structure 49 is fixedly installed in the beginning of the connection between the diffuser 43 and the throat 48, and the flow guiding structure 49 includes a plurality of spiral-rotating flow guiding vanes 490 or flow guiding plates.
Referring to fig. 2, the inlet pipe 1 is provided at a side portion thereof with an exhaust gas inlet 411, and at an upper portion thereof with a mounting seat 412, and the upper end of the regulator 45 is mounted to the mounting seat 412 such that the regulator 45 is rotatable and movable up and down. Alternatively, the upper end of the regulator 45 is shown fixedly mounted to the mounting block 412.
Further, an actuator 46 is provided on the mounting base 412, and the actuator 46 controls the regulator 5 to rotate and move up and down.
Meanwhile, the upper end of the regulator 45 is provided with a rotary joint 47, the rotary joint 47 is connected into an external liquid pipeline, and the external liquid pipeline can be kept from rotating when the regulator 45 rotates.
On the other hand, the lower end of the regulator 45 is provided with an injection port, which injects in the radial direction. More preferably, the regulator 45 has a streamlined shape.
In this way, the regulator 45 takes a streamlined shape to reduce the resistance. The rotational movement of actuator 45 enhances turbulence and mixing of the gas-liquid stream in throat 48; the up-and-down movement of the regulator 45 is regulated according to the change of the working condition to adjust the size and flow rate of the gap at the throat 48, thereby ensuring the dust removal efficiency. The regulator 45, which may be a water jet, employs a high velocity radial spray, the atomization of which is not produced by a high velocity gas stream, but rather by a liquid nozzle, the throat merely providing intimate contact between the gas and liquid.
Returning to fig. 1, a dust collector is provided on the downstream side of the scrubber 5, and a preferable mode of the dust collector is a wet dust collector 6, the wet dust collector 6 forms a water film by shower water 17, and uses a non-conductive non-metal material as a dust collecting electrode, or uses a corrosion resistant material as the dust collecting electrode directly, and the dust deposited on the electrode plate can be washed off by water, and the washed dust can be filter-pressed by a filter press 12, and then heavy metals 13 are recovered. After the heavy metals in the wastewater generated in the washing tower and the dust collector are recovered by the filter press 12, the wastewater 14 is disposed, and the wastewater 14 is disposed by discharging the wastewater to a sewage plant through a sewage pipeline.
An alternative embodiment is to provide an oxygen sensor in the exhaust duct of the precipitator to detect the oxygen concentration in the syngas.
The exhaust device is arranged at the downstream side of the dust remover, and the exhaust device has two setting modes, namely a torch 11 is arranged, the synthetic gas subjected to dust removal is combusted through the torch 11 and is generally analyzed according to the oxygen content of the synthetic gas, if the oxygen content is too high, the storage is not facilitated, and when the detonation risk exists, the torch 11 is adopted for combustion. The other method is to arrange a gas drying tower 7, a pressurized gas 8 and a synthetic gas storage tank 9, analyze the oxygen content of the synthetic gas after dust removal, dry the synthetic gas through the gas drying tower 7 if the oxygen content is low, pressurize the synthetic gas through the pressurized gas 8, and finally store the synthetic gas in the storage tank 9. The storage tank 9 supplies the synthesis gas to the gas boiler 10, the synthesis gas is combusted in the gas boiler 10, the capacity recovery is performed by using the chemical energy of the synthesis gas, the combusted synthesis gas is discharged through the chimney 101, the temperature of the exhaust gas discharged from the chimney 101 is usually more than 150 ℃, the combustion of the synthesis gas in the gas filter 10 is low-nitrogen combustion, and substances generated by the combustion are usually water or carbon dioxide, wherein the particulate matters or nitrogen oxides are extremely low, and the emission requirements specified by relevant standards can be met.
The working principle of the system shown in fig. 1 is:
after being mixed, the hazardous waste enters a crusher 1 to be crushed to the size of 100-500mm and then is conveyed to a plasma gasification melting furnace 3 by a feeder 2, the dangerous waste is gasified and melted in the plasma gasification melting furnace 3, the temperature range in the plasma gasification melting furnace is between 1200 ℃ and 1600 ℃, simultaneously controlling the oxygen content in the furnace to be lower than 1 percent, controlling the residence time of the synthetic gas generated in the furnace to exceed 3s, the sensible heat between 1200 ℃ and 500 ℃ of the synthesis gas at the outlet of the plasma gasification melting furnace 3 is recovered by a waste heat boiler 4, the synthesis gas enters a two-stage water scrubber 5, the first stage is a Venturi wet quenching deacidification tower, the synthesis gas is directly quenched and deacidified by dilute alkali liquor 16 in the Venturi wet quenching deacidification tower, the temperature of the synthesis gas is directly reduced from 500 ℃ to below 100 ℃, and the preferable liquid-gas ratio is 3-10L/m.3Simultaneously to the acid substances (HCl and H) in the synthesis gas2S) and particles are removed for the first time, a large amount of water of volatile heavy metals in the synthesis gas exists in a solution or solid state form in tower bottom liquid after being washed, precipitates are formed at the tower bottom by adjusting the pH value of the tower bottom liquid to be between 8 and 11.5, the solids can be further recovered after being subjected to pressure filtration by a pressure filter 12, then the synthesis gas enters a second-stage washing tower for secondary washing, and the tower of the second-stage washing tower is subjected to secondary washing by dilute alkali liquor, wherein the preferable liquid-gas ratio is 1.5 to 8L/m3Reducing the temperature of the synthesis gas to about 60 ℃, and further reducing the acid gas (H)2S, HCl) and particulate matter are removed, heavy metal compounds in the synthesis gas are further washed, the heavy metal compounds are enriched at the bottom of the secondary washing tower in a precipitation form by adjusting the pH value of the bottom liquid of the secondary washing tower to be between 8 and 11.5, and the solid can be further recovered after pressure filtration by a pressure filter 12. The synthesis gas after passing through the secondary scrubber enters a wet scrubber 6, fine particulate matters (water droplets, aerosol, etc.) as low as 0.5um in the synthesis gas are further removed, and the waste liquid generated in the wet scrubber 6 can be subjected to filter pressing by a filter press 12 and then recovered as solid or heavy metal 13. The waste liquid generated in the two-stage water scrubber and the wet dust collector is subjected to pressure filtration by the filter press 12, and then discharged to a sewage line for disposal by a sewage treatment plant. The synthesis gas is usually dehydrated in a gas drying tower 7 to improve the quality of the synthesis gas, and is pressurized to 10KPa by a booster air compressor 8 and then enters a synthesis gas storage tank 9. The synthetic gas enters a gas boiler 10 from a synthetic gas storage tank 9 for low-nitrogen combustion, the chemical energy of the synthetic gas is recovered, and the flue gas after combustion enters a chimney 101 and the exhaust temperature is higher than 150 ℃. If the oxygen content in the synthesis gas is too high, there is a risk of deflagration, the synthesis gas is directed to a flare 11 for combustion on the downstream side of the precipitator. The high oxygen content in the synthesis gas is usually air introduced upstream of the system due to sealing problems, and under the condition that the sealing performance reaches the standard, the oxygen content in the synthesis gas is not high, so that the hidden danger of detonation is avoided.
From the foregoing description, it can also be understood that a process for disposing hazardous waste by plasma gasification and melting is provided, which employs a plasma gasification and melting furnace 3 to melt and process the broken hazardous waste, the temperature range in the plasma gasification and melting furnace is controlled between 1200 ℃ and 1600 ℃, the oxygen content in the furnace is controlled to be lower than 1%, and the residence time of the synthesis gas generated in the furnace is more than 3 s;
then guiding the synthesis gas discharged by the plasma gasification melting furnace to a waste heat boiler 4, and recovering the sensible heat of the synthesis gas by using the waste heat boiler;
then, cooling, deacidifying and dedusting the synthesis gas passing through the waste heat boiler by adopting a washing tower 5, and cooling the synthesis gas to be below 100 ℃;
then, a dust remover 6 is adopted to remove dust from the synthesis gas passing through the washing tower;
and finally, burning the synthesis gas subjected to dust removal through a torch or recovering chemical energy through a gas boiler.
The beneficial effects of the foregoing embodiments are embodied in:
1. the energy recovery is maximized by adopting a waste heat boiler and a gas boiler, and compared with the mode of performing energy recovery after combustion in a secondary combustion chamber, the heat recovery is increased by 10-30%;
2. the generation of dioxin and NOx is reduced to the maximum extent in the plasma melting furnace, the regeneration of NOx is reduced in a later stage in a gas boiler by adopting a low-nitrogen combustion mode, the NOx in the flue gas is lower than the emission concentration, so that a denitration link can be omitted, and the investment cost and the operation cost are saved;
3. the use of frequent replacement of the multi-fluid atomizing nozzle is avoided by adopting a wet quenching mode, and the control, operation and maintenance costs of the system are greatly simplified;
4. heavy metals and particles in the synthesis gas are washed to the bottom of the tower in a large water washing mode, so that the heavy metals are recycled after being subjected to filter pressing;
5. active carbon is not needed to adsorb heavy metals, so that the operation cost is saved;
6. the wet dust collector is used for replacing a bag dust collector, so that secondary fly ash can be avoided, and replacement and disposal of a bag can also be avoided.
7. The tail end of the gas boiler is used for combusting the synthesis gas to recover chemical energy, the exhaust temperature of the combusted synthesis gas is higher than 150 ℃, energy consumption and equipment for reheating the same products due to smoke whitening are avoided, and investment cost and operation cost are saved.
Although the present invention has been described with reference to the preferred embodiments, it is not intended to limit the present invention, and those skilled in the art can make various changes and modifications without departing from the spirit and scope of the present invention. Therefore, any modification, equivalent changes and modifications made to the above embodiments according to the technical spirit of the present invention, all without departing from the content of the technical solution of the present invention, fall within the scope of protection defined by the claims of the present invention.
Claims (6)
1. A plasma gasification melting hazardous waste disposal system, comprising:
the plasma gasification melting furnace is used for melting the broken dangerous waste;
a waste heat boiler for recovering sensible heat of the synthesis gas discharged from the plasma gasification melting furnace;
characterized in that, the system also includes:
the washing tower is used for cooling, deacidifying and dedusting the synthetic gas passing through the waste heat boiler;
the dust removal device is used for further removing dust from the synthetic gas discharged from the washing tower; and
and the gas exhausting device comprises a torch or a gas boiler, the torch is used for burning the synthetic gas passing through the dust removal device, and the gas boiler is used for recovering chemical energy of the gas passing through the dust removal device.
2. The plasma gasification melting hazardous waste disposal system of claim 1, wherein the scrubber tower comprises a venturi wet quench deacidification tower.
3. The plasma gasification melting hazardous waste disposal system of claim 1, wherein the scrubber tower comprises a two-stage water scrubber tower, wherein the first stage water scrubber tower is a venturi wet quenching deacidification tower, and the second stage water scrubber tower performs a secondary water washing on the synthesis gas discharged from the first stage water scrubber tower.
4. The plasma gasification melting hazardous waste disposal system of claim 3, further comprising a filter press for filter pressing the bottom solution of the scrubber to recover solids.
5. The plasma gasification melting hazardous waste disposal system of claim 1, wherein the dust removal device is a wet dust collector.
6. The system according to claim 1, wherein the exhaust unit further includes a drying tower for drying the synthesis gas, a booster for boosting the synthesis gas dried by the drying tower, and a gas storage tank for storing the boosted synthesis gas, and the gas storage tank supplies a gas to the gas boiler.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110038371A (en) * | 2019-05-20 | 2019-07-23 | 上海羿诚环保科技有限公司 | Plasma gasification melts danger wastes disposal system and technique |
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| CN110038371A (en) * | 2019-05-20 | 2019-07-23 | 上海羿诚环保科技有限公司 | Plasma gasification melts danger wastes disposal system and technique |
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